CN112703022A - Raw liquid processing apparatus, method for operating raw liquid processing apparatus, and method for cleaning instrument - Google Patents
Raw liquid processing apparatus, method for operating raw liquid processing apparatus, and method for cleaning instrument Download PDFInfo
- Publication number
- CN112703022A CN112703022A CN201980058425.9A CN201980058425A CN112703022A CN 112703022 A CN112703022 A CN 112703022A CN 201980058425 A CN201980058425 A CN 201980058425A CN 112703022 A CN112703022 A CN 112703022A
- Authority
- CN
- China
- Prior art keywords
- liquid
- concentrator
- filter
- hollow fiber
- flow path
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 2863
- 238000004140 cleaning Methods 0.000 title claims abstract description 870
- 238000000034 method Methods 0.000 title claims abstract description 217
- 239000012528 membrane Substances 0.000 claims abstract description 1077
- 239000012510 hollow fiber Substances 0.000 claims abstract description 442
- 239000011796 hollow space material Substances 0.000 claims abstract description 140
- 239000012466 permeate Substances 0.000 claims abstract description 55
- 239000000706 filtrate Substances 0.000 claims description 638
- 239000012141 concentrate Substances 0.000 claims description 410
- 239000002699 waste material Substances 0.000 claims description 396
- 239000000243 solution Substances 0.000 claims description 344
- 238000001914 filtration Methods 0.000 claims description 239
- 239000011550 stock solution Substances 0.000 claims description 87
- 230000007423 decrease Effects 0.000 claims description 71
- 230000008878 coupling Effects 0.000 claims description 40
- 238000010168 coupling process Methods 0.000 claims description 40
- 238000005859 coupling reaction Methods 0.000 claims description 40
- 239000012530 fluid Substances 0.000 claims description 33
- 230000003247 decreasing effect Effects 0.000 claims description 31
- 238000010129 solution processing Methods 0.000 claims description 29
- 238000007599 discharging Methods 0.000 claims description 25
- 230000005856 abnormality Effects 0.000 claims description 6
- 239000000126 substance Substances 0.000 abstract description 29
- 230000000694 effects Effects 0.000 abstract description 25
- 210000004379 membrane Anatomy 0.000 description 402
- 238000011084 recovery Methods 0.000 description 176
- 230000007246 mechanism Effects 0.000 description 104
- 239000007789 gas Substances 0.000 description 64
- 210000002381 plasma Anatomy 0.000 description 28
- 208000002151 Pleural effusion Diseases 0.000 description 22
- 238000002360 preparation method Methods 0.000 description 18
- 230000000630 rising effect Effects 0.000 description 17
- 238000010586 diagram Methods 0.000 description 16
- 238000010790 dilution Methods 0.000 description 16
- 239000012895 dilution Substances 0.000 description 16
- 230000008569 process Effects 0.000 description 12
- 239000007787 solid Substances 0.000 description 12
- 238000011144 upstream manufacturing Methods 0.000 description 12
- 210000003567 ascitic fluid Anatomy 0.000 description 10
- 230000001276 controlling effect Effects 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 206010003445 Ascites Diseases 0.000 description 8
- 210000004027 cell Anatomy 0.000 description 8
- 238000007865 diluting Methods 0.000 description 8
- 210000004369 blood Anatomy 0.000 description 7
- 239000008280 blood Substances 0.000 description 7
- 238000002835 absorbance Methods 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 230000005484 gravity Effects 0.000 description 6
- 238000004904 shortening Methods 0.000 description 6
- 239000000725 suspension Substances 0.000 description 6
- 230000003187 abdominal effect Effects 0.000 description 5
- 238000003825 pressing Methods 0.000 description 5
- 238000002560 therapeutic procedure Methods 0.000 description 5
- 102000009027 Albumins Human genes 0.000 description 4
- 108010088751 Albumins Proteins 0.000 description 4
- 239000004480 active ingredient Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 102000004169 proteins and genes Human genes 0.000 description 4
- 108090000623 proteins and genes Proteins 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000002562 thickening agent Substances 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- 102000006395 Globulins Human genes 0.000 description 3
- 108010044091 Globulins Proteins 0.000 description 3
- 206010019280 Heart failures Diseases 0.000 description 3
- 206010028980 Neoplasm Diseases 0.000 description 3
- 208000004756 Respiratory Insufficiency Diseases 0.000 description 3
- 210000001772 blood platelet Anatomy 0.000 description 3
- 230000036772 blood pressure Effects 0.000 description 3
- 201000011510 cancer Diseases 0.000 description 3
- 208000019425 cirrhosis of liver Diseases 0.000 description 3
- 210000003743 erythrocyte Anatomy 0.000 description 3
- 238000001802 infusion Methods 0.000 description 3
- 210000000265 leukocyte Anatomy 0.000 description 3
- 210000002540 macrophage Anatomy 0.000 description 3
- 230000000149 penetrating effect Effects 0.000 description 3
- 210000003200 peritoneal cavity Anatomy 0.000 description 3
- 201000004193 respiratory failure Diseases 0.000 description 3
- 238000001356 surgical procedure Methods 0.000 description 3
- 210000000115 thoracic cavity Anatomy 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- BPYKTIZUTYGOLE-IFADSCNNSA-N Bilirubin Chemical compound N1C(=O)C(C)=C(C=C)\C1=C\C1=C(C)C(CCC(O)=O)=C(CC2=C(C(C)=C(\C=C/3C(=C(C=C)C(=O)N\3)C)N2)CCC(O)=O)N1 BPYKTIZUTYGOLE-IFADSCNNSA-N 0.000 description 2
- 206010061218 Inflammation Diseases 0.000 description 2
- 210000001015 abdomen Anatomy 0.000 description 2
- 210000000683 abdominal cavity Anatomy 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 2
- 210000000038 chest Anatomy 0.000 description 2
- 210000003722 extracellular fluid Anatomy 0.000 description 2
- 230000004054 inflammatory process Effects 0.000 description 2
- 239000003978 infusion fluid Substances 0.000 description 2
- 238000001990 intravenous administration Methods 0.000 description 2
- 239000002504 physiological saline solution Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000004094 surface-active agent Substances 0.000 description 2
- 210000001519 tissue Anatomy 0.000 description 2
- 210000001835 viscera Anatomy 0.000 description 2
- 206010015719 Exsanguination Diseases 0.000 description 1
- 206010016654 Fibrosis Diseases 0.000 description 1
- 102000001554 Hemoglobins Human genes 0.000 description 1
- 108010054147 Hemoglobins Proteins 0.000 description 1
- 206010030113 Oedema Diseases 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 210000004204 blood vessel Anatomy 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 210000003850 cellular structure Anatomy 0.000 description 1
- 230000007882 cirrhosis Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000000502 dialysis Methods 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- -1 etc.) Proteins 0.000 description 1
- 210000003701 histiocyte Anatomy 0.000 description 1
- 239000005556 hormone Substances 0.000 description 1
- 229940088597 hormone Drugs 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 208000015181 infectious disease Diseases 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 235000001705 insufficient nutrition Nutrition 0.000 description 1
- 238000007912 intraperitoneal administration Methods 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 210000003281 pleural cavity Anatomy 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 235000000346 sugar Nutrition 0.000 description 1
- 150000008163 sugars Chemical class 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 208000024891 symptom Diseases 0.000 description 1
- 210000004888 thoracic abdominal cavity Anatomy 0.000 description 1
- 239000011782 vitamin Substances 0.000 description 1
- 229940088594 vitamin Drugs 0.000 description 1
- 229930003231 vitamin Natural products 0.000 description 1
- 235000013343 vitamin Nutrition 0.000 description 1
Images
Classifications
-
- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61M—DEVICES FOR INTRODUCING MEDIA INTO, OR ONTO, THE BODY; DEVICES FOR TRANSDUCING BODY MEDIA OR FOR TAKING MEDIA FROM THE BODY; DEVICES FOR PRODUCING OR ENDING SLEEP OR STUPOR
- A61M1/00—Suction or pumping devices for medical purposes; Devices for carrying-off, for treatment of, or for carrying-over, body-liquids; Drainage systems
Abstract
The invention provides a raw liquid treatment device, a method for operating the raw liquid treatment device, and a method for cleaning an instrument, which can shorten the treatment time of raw liquid extracted from the body of a patient and improve the operability of an operator. The appliance has: a main body part (11) having a hollow space therein and a hollow fiber membrane (16) provided in the hollow space of the main body part (11), wherein when the hollow fiber membrane (16) in the appliance is cleaned, a cleaning liquid is caused to flow as follows: the liquid is allowed to permeate the hollow fiber membranes (16) in a state where the hollow space (12h) of the main body (11) and/or the hollow fiber membranes (16) are filled with the liquid to fill the region to be cleaned in the hollow fiber membranes (16). The effects of eliminating clogging of the hollow fiber membranes (16) and removing substances accumulated in the hollow fiber membranes (16) or the main body (11) can be improved.
Description
Technical Field
The present invention relates to a raw liquid treatment apparatus, a method for operating the raw liquid treatment apparatus, and a method for cleaning an instrument. More specifically, the present invention relates to a raw liquid treatment apparatus for obtaining a treatment liquid for intravenous infusion by filtering or concentrating a raw liquid such as pleural and peritoneal effusion accumulated in the chest or abdomen due to cancerous pleuroperitoneal inflammation, liver cirrhosis, or the like, or waste plasma of plasma exchange therapy, a method for operating the raw liquid treatment apparatus, and a method for cleaning instruments used in the raw liquid treatment apparatus.
Background
In cancerous pleuroperitoneal inflammation, liver cirrhosis, or the like, pleural effusion or abdominal effusion may accumulate in the thoracic cavity or abdominal cavity, and in a state where such pleural effusion or abdominal effusion is accumulated, problems such as the pleural effusion and abdominal effusion pressing peripheral internal organs may occur. To solve such a problem, a treatment for extracting the pleural effusion and the peritoneal cavity may be performed by puncturing.
On the other hand, the pleural effusion contains a part or all of plasma components exuded from blood, and the plasma contains major proteins (e.g., albumin, globulin, and the like). Although the above symptoms can be improved by extracting the accumulated fluid from the pleural cavity, components useful for the human body such as protein are lost together with water. Therefore, it is necessary to administer an albumin preparation, a globulin preparation, or the like intravenously to replace the lost components.
However, although it is possible to supplement a specific ingredient by administering an albumin preparation, a globulin preparation, or the like intravenously, the preparation is expensive and the treatment cost is high.
In addition, since only a limited amount of a specific component among the lost components can be supplied, there is a possibility that problems such as insufficient nutrition and susceptibility to infection may occur.
Therefore, a method of intravenously administering a treatment solution obtained by treating a pleural effusion or an abdominal effusion (hereinafter, sometimes referred to as a stock solution) extracted from the thoracic cavity or the abdominal cavity, that is, a so-called "pleuroperitoneal effusion filtration and concentration infusion Therapy" (CART) has been developed. In such CART, since most of the active ingredients other than the cellular components contained in the pleural effusion and the peritoneal effusion can be returned to the body of the patient, the components lost from the blood can be effectively supplied to the patient without being limited to specific components. Further, even if the concentrated solution is administered, the preparation can be supplemented with a component insufficient in an amount corresponding to the shortage, and therefore the amount of albumin preparation or the like used can be reduced as much as possible, and the cost of treatment can be suppressed.
In CART, treatment fluid is generated by filtration and concentration of pleural or peritoneal effusion and returned to the patient. In a treatment apparatus for producing such a treatment liquid, a raw liquid such as pleural effusion or peritoneal effusion is supplied to a filter having a filter member such as a hollow fiber membrane or a plate-like permeable membrane, and a liquid component (hereinafter, sometimes referred to as a filtrate) is separated. When the separated filtrate is passed through a concentrator to remove water from the filtrate, a concentrated solution obtained by concentrating the filtrate, that is, the above-mentioned treated solution can be obtained (see patent documents 1 to 4).
Documents of the prior art
Patent document
Patent document 1: japanese patent No. 5062631
Patent document 2: japanese patent laid-open publication No. 2015-126763
Patent document 3: japanese patent laid-open publication No. 2019-13487
Patent document 4: japanese patent laid-open publication No. 2019-13488
Disclosure of Invention
Technical problem to be solved by the invention
As described above, in CART, a treatment liquid obtained by treating a raw liquid extracted from the body of a patient is returned to the body of the patient, but if a filter or a concentrator is clogged, the treatment of the raw liquid cannot be performed properly. Therefore, in order to eliminate clogging of the filter and the concentrator, it is required to appropriately clean the filter and the concentrator.
In view of the above circumstances, an object of the present invention is to provide a raw liquid treatment apparatus, a method of operating the raw liquid treatment apparatus, and a method of cleaning an instrument, which can shorten a treatment time of raw liquid extracted from a body of a patient and improve workability of an operator.
Solution for solving the above technical problem
< method for cleaning utensil >
The method for cleaning an appliance of claim 1 is an appliance having a main body portion having a hollow space therein and a hollow fiber membrane provided in the hollow space of the main body portion, and is characterized in that, when cleaning the hollow fiber membrane in the appliance, a liquid is caused to flow as follows: the hollow fiber membranes are permeated with a liquid in a state where the hollow space of the main body and/or the hollow fiber membranes are filled with the liquid to fill the region where the hollow fiber membranes are washed.
The method for cleaning a device according to claim 2 is characterized in that, in the invention 1, the liquid is caused to flow in the following manner when the hollow fiber membranes in the device are cleaned: after filling the hollow space of the main body and/or the hollow fiber membranes with a liquid to fill the region of the hollow fiber membranes to be cleaned, the liquid is allowed to permeate the hollow fiber membranes.
The method of cleaning a tool according to claim 3 is characterized in that, in the 1 st or 2 nd invention, the tool includes: a first liquid supply unit which communicates with the first end of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane; a second liquid supply portion that communicates with the second end portion of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane; a port through which a discharge fluid is supplied between the inside and the outside of the hollow space of the main body, and through which a liquid flows in a state in which the axial direction of the hollow fiber membranes is oriented in the vertical direction: the hollow space of the main body and/or the hollow fiber membranes are filled with a liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid is allowed to permeate the hollow fiber membranes in this state.
The method of cleaning a tool according to claim 4 is characterized in that, in the 1 st or 2 nd invention, the tool includes: a first liquid supply unit which communicates with the first end of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane; a second liquid supply portion that communicates with the second end portion of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane; a port through which a discharge fluid is supplied between the inside and the outside of the hollow space of the main body, and through which a liquid flows in a state in which the axial direction of the hollow fiber membranes is oriented in the horizontal direction: the hollow space of the main body and/or the hollow fiber membranes are filled with a liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid is allowed to permeate the hollow fiber membranes in this state.
The method for cleaning an instrument according to claim 5 is characterized in that, in the 1 st, 2 nd, 3 rd or 4 th aspect, the instrument includes: a first liquid supply unit which communicates with the first end of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane; a second liquid supply portion that communicates with the second end portion of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane; and a port through which a discharge fluid is supplied between the inside and the outside of the hollow space of the main body, and through which the liquid is discharged from the first liquid supply unit and/or the second liquid supply unit when the liquid is supplied from the port, or through which the liquid is discharged from the first liquid supply unit and/or the second liquid supply unit when the liquid is supplied from the port.
< method of operating stock solution treating apparatus (cleaning method) >
A method for operating a raw liquid processing apparatus according to claim 6 is a method for operating an apparatus for concentrating a raw liquid to form a concentrated liquid, the apparatus comprising: a filter having a filter member for filtering the stock solution; a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated solution; a raw liquid supply unit configured to supply the raw liquid to the filter; a liquid supply passage for communicating the raw liquid supply unit with the raw liquid supply port of the filter; a filtrate supply passage for connecting the filtrate discharge port of the filter to the filtrate supply port of the concentrator; a concentrate flow path connected to a concentrate discharge port of the concentrator; a waste liquid flow path connected to a waste liquid discharge port for discharging the waste liquid separated from the concentrated liquid in the concentrator; a liquid feeding unit for feeding liquid to each flow path; and a control unit that controls an operation of the liquid feeding unit, wherein the filter and/or the concentrator has a main body having a hollow space therein and a hollow fiber membrane provided in the hollow space of the main body, and the control unit controls the operation of the liquid feeding unit so that the hollow fiber membrane is permeated by a liquid in a state where the hollow space of the main body and/or the hollow fiber membrane is filled with the liquid to fill a region where the hollow fiber membrane is cleaned, when the hollow fiber membrane in the filter and/or the concentrator is cleaned.
In the method for operating the raw liquid treatment apparatus according to claim 7, in the 6 th aspect, when the hollow fiber membranes in the filter and/or the concentrator are cleaned, the controller controls the operation of the liquid feeder so that the liquid permeates the hollow fiber membranes after the hollow space of the main body and/or the hollow fiber membranes are filled with the liquid to a state in which the region of the hollow fiber membranes to be cleaned is filled with the liquid.
The method of operating a raw liquid treatment apparatus according to claim 8 is characterized in that, in the 6 th or 7 th invention, the filter is disposed in a state in which the axial direction of the hollow fiber membranes is directed in the vertical direction, and the filter is provided with a port which is disposed above the raw liquid supply port or the filtrate discharge port when the hollow fiber membranes in the filter are cleaned and which is capable of communicating the inside of the hollow space of the main body with the outside, and the control unit controls the operation of the liquid feed unit so that the inside of the hollow space of the main body and/or the inside of the hollow fiber membranes is filled with a liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid is caused to permeate through the hollow fiber membranes of the filter in this state.
The method of operating the raw liquid treatment apparatus according to claim 9 is characterized in that, in the 6 th, 7 th or 8 th aspect, the concentrator is disposed in a state in which the axial direction of the hollow fiber membranes is directed in the vertical direction, and includes a port which is disposed above the concentrate discharge port or the waste liquid discharge port when the hollow fiber membranes in the concentrator are cleaned, and which is capable of communicating the inside of the hollow space of the main body with the outside, and the controller controls the operation of the liquid feed unit so that the inside of the hollow space of the main body and/or the inside of the hollow fiber membranes is filled with a liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid is caused to permeate through the hollow fiber membranes of the concentrator in this state.
The method of operating the raw liquid treatment apparatus according to claim 10 is characterized in that, in the 6 th or 7 th invention, the controller controls the operation of the liquid feeder so that the hollow space of the main body is filled with the liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid passes through the hollow fiber membranes in this state, in a state where the filter and/or the concentrator are disposed so that the axial direction of the hollow fiber membranes is oriented in a horizontal direction.
The method of operating the raw liquid treatment apparatus according to claim 11 is characterized in that in the 6 th, 7 th, 8 th, 9 th or 10 th aspect, the liquid is supplied into the concentrator from the filtrate supply port or the concentrated liquid discharge port.
< method for operating raw liquid processing apparatus >
A method for operating a raw liquid processing apparatus according to claim 12 is a method for operating an apparatus for concentrating a raw liquid to form a concentrated liquid, the apparatus comprising: a filter having a filter member for filtering the stock solution; a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated solution; a raw liquid supply unit configured to supply the raw liquid to the filter; a liquid supply passage for communicating the raw liquid supply unit with the raw liquid supply port of the filter; a filtrate supply passage for connecting the filtrate discharge port of the filter to the filtrate supply port of the concentrator; a concentrate flow path connected to a concentrate discharge port of the concentrator; a waste liquid flow path connected to a waste liquid discharge port for discharging the waste liquid separated from the concentrated liquid in the concentrator; a liquid feeding unit for feeding liquid to each flow path; and a control unit that controls an operation of the liquid feeding unit, and adjusts a liquid feeding amount from the filter to the concentrator and/or a concentration ratio of the concentrated liquid based on a filter-to-membrane differential pressure of the filter and/or a concentrator-to-membrane differential pressure of the concentrator.
The method of operating the raw liquid processing apparatus according to claim 13 is characterized in that, in the 12 th aspect, the liquid feeding unit includes a liquid feeding unit provided in the liquid feeding passage and a liquid feeding unit provided in the concentrated liquid passage or a liquid feeding unit provided in the waste liquid passage, and the method includes increasing a liquid feeding amount of the raw liquid to the filter when the inter-filter-membrane differential pressure is smaller than the set differential pressure of the filter, maintaining the liquid feeding amount of the raw liquid to the filter when the inter-filter-membrane differential pressure is within the set differential pressure of the filter, and decreasing the liquid feeding amount of the raw liquid to the filter when the inter-filter-membrane differential pressure is larger than the set differential pressure of the filter.
The method of operating the raw liquid treatment apparatus according to claim 14 is characterized in that in the 12 th or 13 th invention, the liquid feeding unit includes a liquid feeding passage liquid feeding unit provided in the liquid feeding passage and a concentrate passage liquid feeding unit provided in the concentrate passage or a waste passage liquid feeding unit provided in the waste passage, and the liquid feeding unit increases the amount of liquid fed from the filter to the concentrator when the inter-concentrator-membrane differential pressure of the concentrator is smaller than a set differential pressure, maintains the amount of liquid fed from the filter to the concentrator when the inter-concentrator-membrane differential pressure of the concentrator is within a set differential pressure, and decreases the amount of liquid fed from the filter to the concentrator when the inter-concentrator-membrane differential pressure of the concentrator is larger than the set differential pressure.
The method of operating the raw liquid treatment apparatus according to claim 15 is characterized in that in the 12 th, 13 th or 14 th invention, the liquid feeding unit includes a liquid feeding passage liquid feeding unit provided in the liquid feeding passage, and a concentrate passage liquid feeding unit provided in the concentrate passage or a waste passage liquid feeding unit provided in the waste passage, and when the inter-concentrator-membrane differential pressure of the concentrator is smaller than a set differential pressure, the flow rate of the concentrate passage is decreased or the flow rate of the waste passage is increased, and when the inter-concentrator-membrane differential pressure of the concentrator is within a set differential pressure range, the flow rates of the concentrate passage and the waste passage are maintained, and when the inter-concentrator-membrane differential pressure of the concentrator is larger than the set differential pressure, the flow rate of the concentrate passage is increased or the flow rate of the waste passage is decreased.
The method of operating the raw liquid treatment apparatus according to claim 16 is characterized in that, in the 12 th aspect, the liquid feeding unit includes a filtrate supply flow path liquid feeding unit provided in the filtrate supply flow path and a concentrate flow path liquid feeding unit provided in the concentrate flow path or a waste flow path liquid feeding unit provided in the waste flow path, and increases a liquid feeding amount of the filtrate to the concentrator when the inter-membrane differential pressure of the filter is smaller than the set differential pressure of the filter, maintains the liquid feeding amount of the filtrate to the concentrator when the inter-membrane differential pressure of the filter is within the set differential pressure of the filter, and decreases the liquid feeding amount of the filtrate to the concentrator when the inter-membrane differential pressure of the filter is larger than the set differential pressure of the filter.
The method for operating the raw liquid treatment apparatus according to claim 17 is characterized in that, in the 12 th or 16 th aspect, the liquid feeding unit comprises a filtrate supply channel liquid feeding unit provided in the filtrate supply channel, and a concentrate channel liquid feeding unit provided in the concentrate channel or a waste liquid channel liquid feeding unit provided in the waste liquid channel, reducing the amount of the concentrated liquid fed to the concentrated liquid flow path or increasing the amount of the waste liquid fed to the waste liquid flow path when the inter-membrane differential pressure of the concentrator is smaller than the set differential pressure of the concentrator, maintaining the amount of the concentrated solution in the concentrated solution channel and the amount of the liquid fed to the waste solution channel when the pressure difference between membranes in the concentrator falls within a range of a set pressure difference in the concentrator, and a liquid-feeding amount of the concentrated liquid in the concentrated liquid flow path is increased or a liquid-feeding amount of the waste liquid in the waste liquid flow path is decreased when the inter-membrane differential pressure of the concentrator is larger than a set differential pressure of the concentrator.
The method of operating the raw liquid treatment apparatus according to claim 18 is characterized in that in the 12 th, 16 th or 17 th aspect, the liquid feeding unit includes a filtrate supply flow path liquid feeding unit provided in the filtrate supply flow path, and a concentrate flow path liquid feeding unit provided in the concentrate flow path or a waste liquid flow path liquid feeding unit provided in the waste liquid flow path, and when the inter-concentrator-membrane differential pressure is smaller than the set differential pressure of the concentrator, the liquid feeding amount of the filtrate to the concentrator is increased, and when the inter-concentrator-membrane differential pressure is within the range of the set differential pressure of the concentrator, the liquid feeding amount of the filtrate to the concentrator is maintained, and when the inter-concentrator-membrane differential pressure is larger than the set differential pressure of the concentrator, the liquid feeding amount of the filtrate to the concentrator is decreased.
The method for operating the raw liquid treatment apparatus according to claim 19 is characterized in that, in the 12 th aspect, the liquid feeding unit includes a concentrate flow path liquid feeding unit provided in the concentrate flow path and a waste liquid flow path liquid feeding unit provided in the waste liquid flow path, and increases the liquid feeding amount of the concentrate and/or the waste liquid when the inter-filter-membrane differential pressure is smaller than the set differential pressure of the filter, maintains the liquid feeding amount of the concentrate and/or the waste liquid when the inter-filter-membrane differential pressure is within the set differential pressure of the filter, and decreases the liquid feeding amount of the concentrate and/or the waste liquid when the inter-filter-membrane differential pressure is larger than the set differential pressure of the filter.
The method for operating the raw liquid treatment apparatus according to claim 20 is characterized in that, in the 12 th and 19 th inventions, the liquid feeding unit includes a concentrate flow path liquid feeding unit provided in the concentrate flow path and a waste liquid flow path liquid feeding unit provided in the waste liquid flow path, reducing the amount of the concentrated liquid fed to the concentrated liquid flow path and/or increasing the amount of the waste liquid fed to the waste liquid flow path when the inter-membrane differential pressure of the concentrator is smaller than the set differential pressure of the concentrator, maintaining the feed amount of the concentrated solution and/or the feed amount of the waste solution in the waste solution channel when the inter-membrane differential pressure of the concentrator falls within a range of a set differential pressure of the concentrator, and a control unit configured to increase a liquid feeding amount of the concentrated liquid in the concentrated liquid passage and/or decrease a liquid feeding amount of the waste liquid in the waste liquid passage when the inter-membrane differential pressure of the concentrator is greater than a set differential pressure of the concentrator.
The method of operating the raw liquid treatment apparatus according to claim 21 is characterized in that in any one of the 12 th to 20 th inventions, a concentrate container for containing a concentrate is connected to the concentrate flow path, a flow path for supplying the concentrate in the concentrate container from the concentrate container to the filtrate supply port of the concentrator is provided, and the concentrate is sent so as to flow from the concentrate container to the filtrate supply port of the concentrator.
The method of operating the raw liquid treatment apparatus according to claim 22 is characterized in that, in any one of the inventions 12 to 21, gas or liquid is supplied to the filter when filtrate and/or concentrated liquid in the apparatus is collected.
The method of operating the raw liquid treatment apparatus according to claim 23 is characterized in that, in the 22 nd aspect, when the operation of recovering the concentrated liquid in the concentrator after recovering the filtrate in the filter is performed, if a differential pressure between concentrator membranes in the concentrator is larger than a set differential pressure, the liquid feeding from the filter to the concentrator is stopped.
The method of operating the raw liquid treatment apparatus according to claim 24 is characterized in that, in claim 23, after stopping the liquid supply from the filter to the concentrator, gas is supplied to the filtrate supply passage.
A method for operating a raw liquid treatment apparatus according to claim 25 is characterized in that in any one of the inventions 12 to 24, the filter includes a main body portion having a hollow space therein and a hollow fiber membrane provided in the hollow space of the main body portion, the filter is disposed so that a raw liquid is supplied into the hollow fiber membrane or the hollow space of the main body portion, and when the hollow fiber membrane of the filter is cleaned, the liquid in the hollow space or the hollow fiber membrane is discharged in a state where air and/or a cleaning liquid is supplied into the hollow space of the main body portion of the filter or the hollow fiber membrane, or the liquid in the hollow space and the hollow fiber membrane is discharged in a state where air and/or a cleaning liquid is supplied into the hollow space of the main body portion of the filter and the hollow fiber membrane, then, a cleaning liquid is supplied into the hollow space of the main body portion and/or the hollow fiber membrane so as to permeate the hollow fiber membrane and the hollow fiber membrane, or the cleaning liquid is supplied into the hollow fiber membrane so as to permeate the hollow fiber membrane, or the cleaning liquid is supplied into the hollow space of the main body portion so as to permeate the hollow space of the main body portion.
The method of operating the raw liquid treatment apparatus according to claim 26 is characterized in that, in the 25 th aspect, when the filter discharges the liquid in the hollow space and/or the hollow fiber membranes, the filter pressurizes air and/or a cleaning liquid and supplies the pressurized air and/or the cleaning liquid to the hollow space and/or the hollow fiber membranes, and/or discharges the liquid in the hollow space and/or the hollow fiber membranes by negative pressure.
The method of operating the raw liquid treatment apparatus according to claim 27 is characterized in that, in the 25 th or 26 th aspect, when the filter supplies air and/or the cleaning liquid into the hollow space of the main body and/or the hollow fiber membrane, the filter pressurizes the air and/or the cleaning liquid and supplies the pressurized air and/or the cleaning liquid into the hollow space and/or the hollow fiber membrane, and/or sets the pressure in the hollow space and/or the hollow fiber membrane to a negative pressure.
< stock solution treating apparatus (Filter, concentrator cleaning) >
A raw liquid processing apparatus according to claim 28 is an apparatus for concentrating a raw liquid to form a concentrated liquid, comprising: a filter having a filter member for filtering the stock solution; a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated solution; a raw liquid supply unit configured to supply the raw liquid to the filter; a liquid supply passage for communicating the raw liquid supply unit with the raw liquid supply port of the filter; a filtrate supply passage for connecting the filtrate discharge port of the filter to the filtrate supply port of the concentrator; a concentrate flow path connected to a concentrate discharge port of the concentrator; a waste liquid flow path connected to a waste liquid discharge port for discharging the waste liquid separated from the concentrated liquid in the concentrator; a liquid feeding unit for feeding liquid to each flow path; and a control unit that controls an operation of the liquid feeding unit, wherein the filter and/or the concentrator has a main body having a hollow space therein and a hollow fiber membrane provided in the hollow space of the main body, and the control unit controls the operation of the liquid feeding unit so that the hollow fiber membrane is permeated by a liquid in a state where the hollow space of the main body and/or the hollow fiber membrane is filled with the liquid to a region where the hollow fiber membrane is washed.
The raw liquid treatment apparatus according to claim 29 is characterized in that, in the 28 th aspect, when cleaning the hollow fiber membranes in the filter and/or the concentrator, the controller controls the operation of the liquid feeder so that the liquid permeates the hollow fiber membranes after the hollow space of the main body and/or the hollow fiber membranes are filled with the liquid to a state in which the region to be cleaned in the hollow fiber membranes is filled with the liquid.
The raw liquid treatment apparatus according to claim 30 is the raw liquid treatment apparatus according to claim 28 or 29, wherein the filter is disposed such that an axial direction of the hollow fiber membranes is directed in a vertical direction, and includes a port which is disposed above the raw liquid supply port or the filtrate discharge port when cleaning the hollow fiber membranes in the filter and which is capable of communicating the inside of the hollow space of the main body with the outside, and the control unit controls the operation of the liquid feeding unit such that the hollow space of the main body and/or the inside of the hollow fiber membranes are filled with liquid and the liquid permeates the hollow fiber membranes in the filter.
The raw liquid treatment apparatus according to claim 31 is the raw liquid treatment apparatus according to claim 28, 29 or 30, wherein the concentrator is disposed such that an axial direction of the hollow fiber membranes is directed in a vertical direction, and includes a port which is disposed above the concentrate discharge port or the waste liquid discharge port when the hollow fiber membranes in the concentrator are cleaned, and which is capable of communicating the inside of the hollow space of the main body with the outside, and the controller controls the operation of the liquid feeder such that the inside of the hollow space of the main body and/or the inside of the hollow fiber membranes is filled with a liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and such that the liquid in this state permeates the hollow fiber membranes of the concentrator.
The raw liquid treatment apparatus according to claim 32 is characterized in that, in the 28 th or 29 th aspect, the control unit controls the operation of the liquid feeding unit so that the hollow space of the main body and/or the hollow fiber membranes are filled with a liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid permeates the hollow fiber membranes in a state where the filter and/or the concentrator are arranged so that the axial direction of the hollow fiber membranes is oriented in a horizontal direction.
< stock solution treating apparatus >
A raw liquid processing apparatus according to claim 33 is an apparatus for concentrating a raw liquid to form a concentrated liquid, comprising: a filter having a filter member for filtering the stock solution; a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated solution; a raw liquid supply unit configured to supply the raw liquid to the filter; a liquid supply passage for communicating the raw liquid supply unit with the raw liquid supply port of the filter; a filtrate supply passage for connecting the filtrate discharge port of the filter to the filtrate supply port of the concentrator; a concentrate flow path connected to a concentrate discharge port of the concentrator; a waste liquid flow path connected to a waste liquid discharge port for discharging the waste liquid separated from the concentrated liquid in the concentrator; a liquid feeding unit for feeding liquid to each flow path; and a control unit that controls an operation of the liquid feeding unit, wherein the control unit adjusts a liquid feeding amount from the filter to the concentrator and/or a concentration ratio of the concentrated liquid by controlling the operation of the liquid feeding unit based on a filter membrane-to-membrane differential pressure of the filter and/or a concentrator membrane-to-membrane differential pressure of the concentrator.
The raw liquid treatment apparatus according to claim 34 is the raw liquid treatment apparatus according to claim 33, wherein the liquid feed unit includes a liquid feed passage liquid feed unit provided in the liquid feed passage, and a concentrate passage liquid feed unit provided in the concentrate passage or a waste passage liquid feed unit provided in the waste passage, and the control unit controls the operation of the liquid feed unit as follows: the method includes increasing a liquid feeding amount of a raw liquid to the filter when the inter-membrane differential pressure of the filter is smaller than a set differential pressure of the filter, maintaining the liquid feeding amount of the raw liquid to the filter when the inter-membrane differential pressure of the filter is within a range of the set differential pressure of the filter, and decreasing the liquid feeding amount of the raw liquid to the filter when the inter-membrane differential pressure of the filter is larger than the set differential pressure of the filter.
A raw liquid treatment apparatus according to claim 35 is the raw liquid treatment apparatus according to claim 33 or 34, wherein the liquid feeding unit includes a liquid feeding passage provided in the liquid feeding passage, and a concentrate passage provided in the concentrate passage or a waste passage provided in the waste passage, and the control unit controls the operation of the liquid feeding unit as follows: the method includes increasing a liquid feed amount from the filter to the concentrator when an inter-concentrator-membrane differential pressure of the concentrator is smaller than a set differential pressure, maintaining the liquid feed amount from the filter to the concentrator when the inter-concentrator-membrane differential pressure of the concentrator is within a range of the set differential pressure, and decreasing the liquid feed amount from the filter to the concentrator when the inter-concentrator-membrane differential pressure of the concentrator is larger than the set differential pressure.
A stock solution processing apparatus according to claim 36 is the apparatus according to claim 33, 34 or 35, wherein the liquid feeding unit includes a liquid feeding passage provided in the liquid feeding passage, and a concentrate passage provided in the concentrate passage or a waste passage provided in the waste passage, and wherein the control unit controls the operation of the liquid feeding unit as follows: when the pressure difference between concentrator membranes of the concentrator is smaller than a set differential pressure, the flow rate of the concentrate flow path is decreased or the flow rate of the waste liquid flow path is increased, when the pressure difference between concentrator membranes of the concentrator is within a range of the set differential pressure, the flow rates of the concentrate flow path and the waste liquid flow path are maintained, and when the pressure difference between concentrator membranes of the concentrator is larger than the set differential pressure, the flow rate of the concentrate flow path is increased or the flow rate of the waste liquid flow path is decreased.
The raw liquid treatment apparatus according to claim 37 is the raw liquid treatment apparatus according to claim 33, wherein the liquid feed unit includes a filtrate supply channel liquid feed unit provided in the filtrate supply channel, and a concentrate channel liquid feed unit provided in the concentrate channel or a waste liquid channel liquid feed unit provided in the waste liquid channel, and the control unit controls the operation of the liquid feed unit as follows: when the inter-membrane pressure difference of the filter is smaller than the set differential pressure of the filter, the amount of the filtrate sent to the concentrator is increased, when the inter-membrane pressure difference of the filter is within the range of the set differential pressure of the filter, the amount of the filtrate sent to the concentrator is maintained, and when the inter-membrane pressure difference of the filter is larger than the set differential pressure of the filter, the amount of the filtrate sent to the concentrator is decreased.
A raw liquid treatment apparatus according to claim 38 is the raw liquid treatment apparatus according to claim 33 or 37, wherein the liquid feed unit includes a filtrate supply channel liquid feed unit provided in the filtrate supply channel, and a concentrate channel liquid feed unit provided in the concentrate channel or a waste liquid channel liquid feed unit provided in the waste liquid channel, and the control unit controls the operation of the liquid feed unit as follows: when the inter-concentrator-membrane differential pressure is smaller than the set differential pressure of the concentrator, the amount of the concentrated liquid fed to the concentrated liquid flow path or the amount of the waste liquid fed to the waste liquid flow path is decreased, and when the inter-concentrator-membrane differential pressure is within the range of the set differential pressure of the concentrator, the amount of the concentrated liquid fed to the concentrated liquid flow path or the amount of the waste liquid fed to the waste liquid flow path is maintained, and when the inter-concentrator-membrane differential pressure is larger than the set differential pressure of the concentrator, the amount of the concentrated liquid fed to the concentrated liquid flow path is increased or the amount of the waste liquid fed to the waste liquid flow path is decreased.
A raw liquid treatment apparatus according to claim 39 is the raw liquid treatment apparatus according to claim 33, 37 or 38, wherein the liquid feed unit includes a filtrate supply channel liquid feed unit provided in the filtrate supply channel, and a concentrate channel liquid feed unit provided in the concentrate channel or a waste liquid channel liquid feed unit provided in the waste liquid channel, and the control unit controls the operation of the liquid feed unit as follows: when the pressure difference between the concentrator membranes is smaller than the set pressure difference of the concentrator, the liquid feeding amount of the filtrate to the concentrator is increased, when the pressure difference between the concentrator membranes is within the range of the set pressure difference of the concentrator, the liquid feeding amount of the filtrate to the concentrator is maintained, and when the pressure difference between the concentrator membranes is larger than the set pressure difference of the concentrator, the liquid feeding amount of the filtrate to the concentrator is decreased.
The raw liquid treatment apparatus according to claim 40 is the apparatus according to claim 33, wherein the liquid feeding unit includes a concentrate channel liquid feeding unit provided in the concentrate channel and a waste liquid channel liquid feeding unit provided in the waste liquid channel, and the control unit controls the operation of the liquid feeding unit as follows: when the filter-membrane differential pressure is smaller than the set filter differential pressure, the amount of the concentrated liquid to be fed and/or the amount of the waste liquid to be fed is increased, when the filter-membrane differential pressure is within the range of the set filter differential pressure, the amount of the concentrated liquid to be fed and the amount of the waste liquid to be fed are maintained, and when the filter-membrane differential pressure is larger than the set filter differential pressure, the amount of the concentrated liquid to be fed and/or the amount of the waste liquid to be fed are decreased.
The raw liquid treatment apparatus according to claim 41 is the apparatus according to claim 33 or 40, wherein the liquid sending unit includes a concentrate channel liquid sending unit provided in the concentrate channel and a waste liquid channel liquid sending unit provided in the waste liquid channel, and the control unit controls the operation of the liquid sending unit as follows: when the inter-membrane pressure difference between the concentrators is smaller than the set pressure difference between the concentrators, the amount of the concentrated solution fed to the concentrated solution channel is decreased and/or the amount of the waste solution fed to the waste solution channel is increased, and when the inter-membrane pressure difference between the concentrators is within the range of the set pressure difference between the concentrators, the amount of the concentrated solution fed to the concentrated solution channel and/or the amount of the waste solution fed to the waste solution channel is maintained, and when the inter-membrane pressure difference between the concentrators is larger than the set pressure difference between the concentrators, the amount of the concentrated solution fed to the concentrated solution channel is increased and/or the amount of the waste solution fed to the waste solution channel is decreased.
The raw liquid treatment apparatus according to claim 42 is characterized in that, in any one of claims 33 to 41, a concentrate container for containing a concentrate is connected to the concentrate flow path, a flow path for supplying the concentrate in the concentrate container from the concentrate container to the filtrate supply port of the concentrator is provided, and the control unit controls the operation of the liquid feed unit so that the concentrate flows from the concentrate container to the filtrate supply port of the concentrator.
The raw liquid treatment apparatus according to claim 43 is characterized in that, in any one of claims 33 to 42, the control unit supplies gas or liquid to the filter during an operation of recovering the filtrate in the filter.
The raw liquid treatment apparatus according to claim 44 is characterized in that, in the 43 th aspect, the control unit controls the operation of the liquid feeding unit to stop the liquid feeding from the filter to the concentrator when a differential pressure between concentrator membranes of the concentrator is larger than a set differential pressure when an operation of recovering the concentrated liquid in the concentrator after recovering the filtrate in the filter is performed.
The raw liquid treatment apparatus according to claim 45 is characterized in that, in the 44 th aspect, the apparatus is provided with a gas supply unit for supplying gas to the filtrate supply channel, and the control unit controls the operation of the liquid feed unit to stop the liquid feed from the filter to the concentrator, and then controls the operation of the gas supply unit to supply gas to the filtrate supply channel.
The raw liquid processing apparatus according to the 46 th aspect of the invention is the raw liquid processing apparatus according to any one of the 28 th to 45 th aspects of the invention, wherein the liquid feeding unit is a roller pump apparatus including rollers with tubes arranged between the roller pump apparatus and a holder, and includes a tube positioning member for holding the tubes wound around the rollers of the roller pump apparatus, the tube positioning member includes a pair of holding members arranged at a distance from each other in an axial direction of the tubes, and a connecting member for maintaining the pair of holding members at a predetermined distance from each other in the axial direction of the tubes, and a plurality of tube holding units for holding a plurality of tubes are provided in a line in each of the holding members, and the plurality of tubes are arranged in parallel to each other when the same tube is held by the corresponding tube holding unit in the pair of holding members, and the connecting member is formed between the pair of holding members, the tube holding member is bendable in a direction intersecting with the direction in which the plurality of tube holding portions are arranged and the axial direction of the plurality of tubes held by the plurality of tube holding portions, and is arranged such that the axial direction of the plurality of tubes held by the plurality of tube holding portions is parallel to the longitudinal direction of the coupling member in a state in which the coupling member is extended.
The raw liquid processing apparatus according to the 47 th aspect of the invention is the raw liquid processing apparatus according to the 46 th aspect of the invention, wherein the coupling member is provided with: when viewed from a direction in which the plurality of tube holding portions are aligned and a direction intersecting an axial direction of the plurality of tubes held by the plurality of tube holding portions in a state in which the coupling member is extended, the coupling member is positioned between adjacent tubes held by the plurality of tube holding portions.
The raw liquid treatment apparatus according to claim 48 is characterized in that, in the 46 th or 47 th aspect, the coupling member is provided with: the plurality of tube holding portions are arranged in a direction intersecting with an axial direction of the plurality of tubes held by the plurality of tube holding portions, and are offset from a central axis of the plurality of tubes held by the plurality of tube holding portions.
The raw liquid treatment apparatus according to claim 49 is characterized in that, in the 46 th, 47 th or 48 th invention, the pair of holding members has an asymmetrical shape with respect to a line bisecting the holding members in the direction in which the plurality of tube holding portions are arranged.
The raw liquid processing apparatus according to claim 50 is characterized in that, in the 46 th, 47 th, 48 th or 49 th aspect, the control unit has a function of rotating the roller in the normal direction and the reverse direction when the pipe is disposed between the holder and the roller.
The raw liquid processing apparatus according to claim 51 is characterized in that, in the 50 th aspect, the control unit has a function of sending an abnormality alarm when the rotation resistance becomes equal to or greater than a predetermined value when the roller is rotated in the normal direction and the reverse direction.
The raw liquid treatment apparatus according to claim 52 is characterized in that, in the 50 th or 51 th aspect, the roller pump device includes a pair of housing portions provided at positions sandwiching a surface including the rotation shaft of the roller, and a pair of holding members on which the tube positioning member is disposed.
The liquid processing apparatus according to 53 th aspect of the invention is the liquid processing apparatus according to any one of the 28 th to 50 th aspects of the invention, wherein the liquid processing apparatus includes a tube holder for holding the tube, and further includes a main body, a plurality of holding portions provided on a first surface of the main body for detachably holding the plurality of tubes, and a coupling portion for coupling the main body to another instrument, wherein the plurality of holding portions are arranged such that when the plurality of tubes are held by the plurality of holding portions, axial directions of the plurality of tubes are parallel to each other and the plurality of tubes are arranged along a surface of the first surface of the main body.
The raw liquid processing apparatus according to claim 54 is characterized in that, in the 53 th aspect, the coupling portion includes an engaging member which protrudes toward the second surface side opposite to the first surface of the body portion or protrudes toward the first surface side, and the engaging member has an opening formed at one end and a gap continuous with the opening.
Effects of the invention
< method for cleaning utensil >
According to the invention 1 to the invention 5, the effects of removing clogging of the hollow fiber membranes and removing substances accumulated in the hollow fiber membranes or the main body can be improved.
< method of operating stock solution treating apparatus (cleaning method) >
According to the invention 6 to the invention 11, the effects of removing clogging of the hollow fiber membranes of the filter and the concentrator and removing substances accumulated in the hollow fiber membranes or the main body of the filter and the concentrator can be improved.
< method for operating raw liquid processing apparatus >
According to the 12 th aspect of the present invention, since the liquid feeding unit is controlled based on the inter-membrane differential pressure of the filter and the inter-membrane differential pressure of the concentrator, the capacities of the filter and the concentrator can be effectively utilized.
< Positive pressure/Positive pressure >
According to the 13 th aspect of the present invention, the time required to produce a concentrated solution from a raw solution can be shortened, and the concentration efficiency can be improved.
According to the 14 th aspect of the present invention, it is possible to prevent problems such as the pressure in the concentrator rising and becoming unable to perform work or the concentrated solution being collected in a state of a low concentration.
According to the 15 th aspect of the present invention, it is possible to prevent problems such as the pressure in the concentrator increasing and making the operation impossible or the generation of a concentrated solution with a low concentration.
< negative pressure/Positive pressure >
According to the 16 th aspect of the present invention, the time required to produce a concentrated solution from a raw solution can be shortened, and the concentration efficiency can be improved.
According to the 17 th aspect of the present invention, it is possible to prevent problems such as the pressure in the concentrator rising and becoming unable to perform work or the concentrated solution being collected in a state of a low concentration.
According to the 18 th aspect of the present invention, it is possible to prevent problems such as the pressure in the concentrator increasing and becoming unable to perform work or the generation of a concentrated solution having a low concentration.
< negative pressure/negative pressure >
According to the 19 th aspect of the present invention, the time required to produce a concentrated solution from a raw solution can be shortened, and the concentration efficiency can be improved.
According to the 20 th aspect of the present invention, it is possible to prevent problems such as the pressure in the concentrator rising and becoming unable to perform work or the concentrated solution being collected in a state of a low concentration.
According to the 21 st aspect of the present invention, the re-concentration of the concentrated solution can be efficiently performed.
According to the 22 nd aspect of the present invention, the filtrate in the filter and filtrate supply passage and the concentrate in the concentrator and concentrate passage can be efficiently recovered.
According to the invention 23, it is possible to prevent the problem that the pressure in the concentrator continues to rise when the concentrate in the concentrator and the concentrate passage is collected.
According to the 24 th aspect of the present invention, it is possible to prevent the omission of recovery of the concentrated liquid in the concentrator or the concentrated liquid channel.
< cleaning >
According to the 25 th to 27 th aspects of the present invention, the discharge of the filtrate present in the filter by cleaning at the time of cleaning the filter is suppressed, and the filtrate present in the filter can be recovered as a concentrated solution by conveying the filtrate to the filter and concentrating the filtrate. Therefore, the recovery amount of the effective component contained in the stock solution into the concentrated solution can be increased.
< stock solution treating apparatus (Filter, concentrator cleaning) >
According to the 29 th to 32 th aspects of the present invention, the effects of removing clogging of the hollow fiber membranes and removing substances accumulated in the hollow fiber membranes or the main body can be improved.
< stock solution treating apparatus >
According to the 33 rd invention, since the liquid feeding part is controlled based on the inter-membrane pressure difference between the filters and the inter-membrane pressure difference between the concentrators, the capabilities of the filters and the concentrators can be effectively utilized, and further, the time for producing the concentrated liquid from the raw liquid can be shortened, and the concentration efficiency can be improved.
< Positive pressure/Positive pressure >
According to the 34 th aspect of the present invention, the time required to produce a concentrated solution from a raw solution can be shortened, and the concentration efficiency can be improved.
According to the 35 th aspect of the present invention, problems such as the pressure in the concentrator increasing to make the operation impossible or the concentrated solution being collected in a state of a low concentration can be prevented.
According to the 36 th aspect of the present invention, it is possible to prevent problems such as the pressure in the concentrator rising to make the operation impossible or the generation of a concentrated solution with a low concentration.
< negative pressure/Positive pressure >
According to the 37 th aspect of the present invention, the time required to produce a concentrated solution from a raw solution can be shortened, and the concentration efficiency can be improved.
According to the 38 th aspect of the present invention, it is possible to prevent problems such as the pressure in the concentrator rising and becoming unable to perform work or the concentrated solution being collected in a state of a low concentration.
According to the 39 th aspect of the present invention, it is possible to prevent problems such as the pressure in the concentrator rising to make the operation impossible or the generation of a concentrated solution with a low concentration.
< negative pressure/negative pressure >
According to the 40 th aspect of the present invention, the time required to produce a concentrated solution from a raw solution can be shortened, and the concentration efficiency can be improved.
According to the 41 st aspect of the present invention, it is possible to prevent problems such as the pressure in the concentrator rising and becoming unable to perform work or the concentrated solution being collected in a state of a low concentration.
According to the 42 th aspect of the present invention, the re-concentration of the concentrated solution can be efficiently performed.
According to the 43 th aspect of the present invention, the filtrate in the filter and filtrate supply passage and the concentrated solution in the concentrator and concentrated solution passage can be efficiently recovered.
According to the invention 44, it is possible to prevent the problem that the pressure in the concentrator continues to rise when the concentrate in the concentrator and the concentrate passage is collected.
According to the 45 th aspect of the present invention, the omission of recovery of the concentrated liquid in the concentrator or the concentrated liquid passage can be prevented.
< pipe positioning Member >
According to the 46 th aspect of the present invention, the tube for the roller pump can be easily and reliably provided.
According to the 47 th and 48 th aspects of the present invention, even if a plurality of tubes are arranged in a vertically aligned manner, the upper tube can be prevented from contacting the lower tube.
According to the 49 th aspect of the present invention, it is possible to prevent an operational error when the pipe is installed in the roller pump.
< roller Pump >
According to the 50 th aspect of the present invention, even if the arrangement of the pipe is slightly deviated from the proper position, the pipe can be moved to the proper position. This makes it possible to shorten the working time because the tubes do not need to be newly arranged.
According to the 51 st aspect of the present invention, it is possible to prevent damage to the apparatus due to improper tube arrangement, and the operator can quickly notice an abnormality.
According to the 52 th aspect of the present invention, it is possible to prevent an operational error when the pipe is installed in the roller pump.
< tube holder >
According to the 53 th aspect of the present invention, when the plurality of tubes are installed in the apparatus, the work of the operator can be easily performed.
According to the 54 th aspect of the present invention, the waste liquid can be easily discharged from the plurality of tubes to the tub or the like.
Drawings
Fig. 1 is a circuit diagram of a raw liquid treatment apparatus 1 according to embodiment 1, and is a schematic explanatory diagram of a filtering and concentrating operation.
Fig. 2 is a circuit diagram of the raw liquid treatment apparatus 1 according to embodiment 1, and is a schematic explanatory diagram of preparation for a cleaning operation.
Fig. 3 is a circuit diagram of the raw liquid treatment apparatus 1 according to embodiment 1, and is a schematic explanatory view of the re-concentration operation.
Fig. 4 is a circuit diagram of the raw liquid treatment apparatus 1 according to embodiment 1, and shows an example in which a waste liquid pipe sending part 5p is provided in the waste liquid pipe 5.
Fig. 5 is a schematic explanatory view of the filter 10.
Fig. 6 is a circuit diagram of the raw liquid treatment apparatus 1B according to embodiment 2, and is a schematic explanatory view of preparation for a cleaning operation.
Fig. 7 is a circuit diagram of the raw liquid treatment apparatus 1B according to embodiment 2, and is a schematic explanatory view of the filtering and concentrating operation.
Fig. 8 is a circuit diagram of the raw liquid treatment apparatus 1B according to embodiment 2, and is a schematic explanatory view of the re-concentration operation.
Fig. 9 is a circuit diagram of the raw liquid treatment apparatus 1B according to embodiment 2, and shows an example in which a waste liquid pipe sending part 5p is provided in the waste liquid pipe 5.
Fig. 10 is a circuit diagram of the raw liquid treatment apparatus 1C according to embodiment 3, and is a schematic explanatory view of preparation for a cleaning operation.
Fig. 11 is a circuit diagram of the raw liquid treatment apparatus 1C according to embodiment 3, and is a schematic explanatory view of the filtering and concentrating operation.
Fig. 12 is a circuit diagram of the raw liquid treatment apparatus 1C according to embodiment 3, and is a schematic explanatory view of the re-concentration operation.
Fig. 13 is a schematic explanatory view of the raw liquid processing apparatus 1 according to embodiment 1, and is a schematic explanatory view of a state in which the lid 112 of the roller pumps 110 and 120 is closed.
Fig. 14 is a schematic explanatory view of the raw liquid processing apparatus 1 according to embodiment 1, and is a schematic explanatory view of a state in which the lid 112 of the roller pumps 110 and 120 is opened.
Fig. 15 is a schematic explanatory view of the roller pump 110, and fig. 15 (a) is a schematic perspective view of a state in which the lid 112 is opened, and (B) is a schematic side view of the state in which the lid 112 is opened.
Fig. 16 is a schematic explanatory view of the pipe positioning member 160 in a state where the pipe T is attached, and fig. 16 (a) is a schematic perspective view of a bent state, (B) is a schematic plan view of the bent state, and (C) is a schematic rear view of the bent state.
Fig. 17 (a) is a schematic explanatory view of the tube positioning member 160 in an exploded state, and (B) is a schematic explanatory view of the tube positioning member 160 in a state where the tube T is attached.
Fig. 18 (a) is a schematic perspective view of the tube holder 150, and (B) is a schematic explanatory view of a state in which the tube holder 150 is attached to the tub.
Fig. 19 is a schematic explanatory view of the raw liquid processing apparatus 1 according to embodiment 1.
Fig. 20 is a schematic explanatory view of the filter 10 during the cleaning operation.
Fig. 21 is a circuit diagram of the raw liquid treatment apparatus 1 according to embodiment 1, and is a schematic explanatory view of a cleaning operation.
Fig. 22 is a circuit diagram of the raw liquid treatment apparatus 1B according to embodiment 2, and is a schematic explanatory view of a cleaning operation.
Fig. 23 is a circuit diagram of the raw liquid treatment apparatus 1C according to embodiment 3, and is a schematic explanatory view of a cleaning operation.
Fig. 24 (a) is a graph showing the differential pressure between the filter membranes when the flow rate of the raw liquid supplied to the filter 10 is adjusted, and (B) is a graph showing the flow rate fluctuation in the liquid supply pipe 2 when the flow rate of the raw liquid supplied to the filter 10 is adjusted.
Detailed Description
The stock solution treatment apparatus of the present invention is an apparatus for obtaining a treatment solution that is obtained by filtering and concentrating a stock solution such as pleural effusion and the like and then can be administered to a patient by a method such as intravenous infusion or intraperitoneal administration.
The stock solution to be treated by the stock solution treatment apparatus of the present invention is not particularly limited, and examples thereof include pleural effusion, plasma, and blood. Pleural effusion refers to pleural or peritoneal effusion that accumulates in the thoracic or abdominal cavity due to cancerous pleuroperitonitis, cirrhosis, etc. The pleural effusion and peritoneal cavity contain plasma components (proteins, hormones, sugars, lipids, electrolytes, vitamins, bilirubin, amino acids, etc.), hemoglobin, cancer cells, macrophages, tissue cells, leukocytes, erythrocytes, platelets, bacteria, etc., which are exuded from blood vessels or internal organs. In the raw liquid treatment apparatus of the present invention, solid components such as cancer cells, macrophages, histiocytes, white blood cells, red blood cells, platelets, bacteria and the like can be removed from the pleural and peritoneal effusion, thereby producing a concentrated liquid containing water and useful components contained in the pleural and peritoneal effusion.
The plasma may be waste plasma of plasma exchange therapy, and the blood may be collected by surgery. That is, if waste plasma, blood collected during surgery, or the like is purified by the stock solution treatment apparatus of the present invention, reusable regenerated plasma can be produced. In the stock solution processing apparatus of the present invention, when waste plasma of the plasma exchange therapy is processed, the filter may be replaced with a plasma component separator, and when blood collected during the operation is processed, the filter may be replaced with a plasma separator.
The filter member of the filter used in the raw liquid treatment apparatus of the present invention is not particularly limited. In addition, the same filter member may be used for concentrating the filtrate in the concentrator. The filter member used for such filtration or concentration is not particularly limited in terms of material, size, and shape as long as it allows the plasma, water, and the above-mentioned useful components contained in the pleural effusion and peritoneal cavity to permeate therethrough, but does not allow cell components (i.e., solid components) such as cancer cells, macrophages, tissue cells, leukocytes, erythrocytes, platelets, and bacteria to permeate therethrough, and also does not allow gas to permeate therethrough. For example, the shape of the filter member may be a hollow fiber membrane, a flat membrane, a laminated membrane, or the like. Further, the filter member may be formed of a material that functions to block gas when wetted with a liquid. Of course, a member formed of a material that functions to block gas even in a state of not being wetted with a liquid may be used. In the present specification, the gas that does not permeate the filter member means an inert gas such as nitrogen, air, oxygen, or the like, and means a gas generally used for leak inspection or the like.
As an example, a hollow fiber membrane used in a seroperitoneum filter, a plasma separator for plasma exchange, a plasma component separator for plasma exchange, and the like of CART can be used in the filter and the concentrator of the stock solution treatment apparatus of the present invention.
< stock solution treatment apparatus 1 of embodiment 1>
The raw liquid processing apparatus 1 according to embodiment 1 will be described with reference to fig. 13 to 19.
It is to be understood that the appearance of the raw liquid treatment apparatus 1 according to embodiment 1, the arrangement, relative sizes, number, and the like of the respective devices and the like are not limited to those shown in fig. 13 to 19, and may be appropriately changed according to the environment, purpose, and the like in which the raw liquid treatment apparatus 1 according to embodiment 1 is used.
As shown in fig. 13, 14, and 19, the raw liquid processing apparatus 1 according to embodiment 1 includes: a main body 100, a pair of roller pumps 110 and 120 provided in the main body 100, a filter holder 101 for holding the filter 10, a concentrator holder 102 for holding the concentrator 20, and a pair of suspending portions 103 and 103 for suspending the tube holder 150 or the bags B.
In the raw liquid processing apparatus 1 according to embodiment 1, when processing a raw liquid, the bags B are hung by the pair of hanging portions 103 and 103, and the filter 10 and the concentrator 20 are held by the filter holding portion 101 and the concentrator holding portion 102. The bags B, the filter 10, and the concentrator 20 are appropriately connected by a plurality of pipes T, and the appropriate pipes T are provided to the pair of roller pumps 110 and 120. In this state, if the pair of roller pumps 110 and 120 are operated, the raw liquid in the raw liquid bag UB can be filtered and concentrated to obtain a concentrated liquid.
Further, if the operating state of the pair of roller pumps 110 and 120 is changed, the bags B connected to the tubes T are changed, the tubes T through which the liquid flows are changed, and the like, it is possible to obtain the concentrated liquid, and further, it is possible to perform reconcentration of the concentrated liquid, cleaning of the filter 10 and the concentrator 20, collection of the liquid existing in the filter 10, the concentrator 20, and the like.
< description of the respective configurations of the raw liquid treatment apparatus 1 according to embodiment 1 >
Hereinafter, each part of the raw liquid processing apparatus 1 according to embodiment 1 will be described.
< body section 100>
As shown in fig. 13, 14, and 19, the main body 100 includes a control unit 106 at a central portion thereof. The control unit 106 has a function of controlling the operation of the pair of roller pumps 110 and 120 and the entire apparatus. The control unit 106 is provided with an operation panel for operating the apparatus and a panel unit 106p for displaying a display panel having various displays. That is, the operator can instruct the processing to be performed in the raw liquid processing apparatus 1 according to embodiment 1 by giving an instruction to the control unit 106 from the panel unit 106 p. The operator can also grasp the state of the raw liquid processing apparatus 1 according to embodiment 1 by checking the numerical values, warnings, and the like displayed on the panel portion 106p in response to instructions from the control portion 106.
The control unit 106 may include buttons for performing various operations in addition to the panel unit 106 p.
< roller pumps 110, 120>
As shown in fig. 13, 14, and 19, a pair of roller pumps 110 and 120 are provided on both sides of the control unit 106 of the main body 100. Since the pair of roller pumps 110 and 120 have substantially the same configuration, the roller pump 110 will be described below.
In fig. 15, in order to facilitate understanding of the roller pump 110, a portion functioning as the roller pump 110 is taken out from the main body 100. The roller pump 110 will be described below with reference to fig. 15.
As shown in fig. 15, the roller pump 110 includes a frame 111 and a lid 112 openably and closably attached to the frame 111. Specifically, when the lid 112 is opened, a roller 115 described later is exposed, and when the lid 112 is closed, the lid 112 is provided so that the roller 115 can be covered by the lid 112. In a state where the cover 112 is closed, the cover 112 is provided so that a space for accommodating the roller 115 is formed between the inner surface of the cover 112 and the upper surface of the frame 111.
A roller portion 115 (see fig. 16) including two rollers 116 is provided on the upper surface of the frame 111. The roller portion 115 has two rollers 116 attached to one shaft 117, and the shaft 117 is rotated by a driving source 114 such as a motor. That is, when the shaft 117 is rotated by the drive source 114, the two rollers 116 are rotated. The number of rollers 116 provided in the roller portion 115 is not limited to 2, and may be 1, or 3 or more. As long as the number of rollers 116 suitable for processing the job is set.
Further, a bracket 113 is provided on the upper surface of the frame 111 at a position facing the roller portion 115. On a surface of the bracket 113 facing the two rollers 116 of the roller unit 115, a recessed surface 113a is provided to sandwich the tube T between the roller unit and the two rollers 116. The holder 113 can be moved closer to and away from the roller 115 by a slider mechanism or the like in conjunction with the opening and closing of the lid 112. Specifically, when the lid 112 is opened, the bracket 113 is moved away from the roller 115 so that the space between the recessed surface 113a of the bracket 113 and the two rollers 116 becomes wider than the diameter of the tube T. When the lid 112 is closed, the bracket 113 approaches the roller 115 and moves so that the gap between the concave surface 113a of the bracket 113 and the two rollers 116 becomes narrower than the diameter of the pipe T. That is, when the lid 112 is opened, the tube T can be placed or removed between the lid and the roller 115, and when the lid 112 is closed, the tube T can be sandwiched between the recessed surface 113a of the holder 113 and the two rollers 116.
Therefore, by opening the lid 112, disposing the tube T between the roller 115 and the recessed surface 113a of the bracket 113, and closing the lid 112, the tube T can be pinched by the roller 115 and the bracket 113. Further, the liquid in the tube T can be fed by operating the drive source 114 in a state where the tube T is pinched by the roller portion 115 and the holder 113.
The roller 116 may have the same structure as a roller used in a general roller pump. For example, as shown in fig. 16 (C), the roller 116 may be a roller in which a plurality of rollers 116b (for example, 3 rollers 116b) are provided between a pair of cover plates 116 a. In the case of using such rollers 116, the tube T can be sandwiched between the plurality of rollers 116b and the recessed surface 113a of the holder 113, and when the rollers 116 rotate, the rollers 116b move so as to manipulate the tube T, and the liquid in the tube T can be sent.
When the lid 112 is closed, the size of the gap formed between the recessed surface 113a of the holder 113 and the two rollers 116 may be adjusted to an appropriate gap with the tubes T disposed in the rollers 116. Suitable gaps are those which are: when the roller 116 is not rotated, the pinching can be performed in such a manner that the liquid does not flow in the tube T, and when the roller 116 is rotated, the rotational resistance of the roller 116 does not increase so much.
In the case where a plurality of tubes T are arranged on the rollers 116 and the diameters of the arranged tubes T are different, the gap may be different depending on the position where each tube T is arranged. For example, if a step is provided on the recessed surface 113a of the bracket 113 so that the distance from the recessed surface 113a of the bracket 113 to the roller 116 is different, the gap can be changed according to the position where each tube T is disposed (that is, the disposed roller 116). On the other hand, if a plurality of rollers 116 are provided and the diameters of the tubes T arranged in the rollers 116 are different, the gap matching the tubes T can be changed by changing the diameters of the rollers 116.
< control of roller Pump 110 >
Here, when the pipe T is disposed between the roller portion 115 and the recessed surface 113a of the bracket 113, the pipe T may not be disposed at an appropriate position. When the driving source 114 is operated in such a state, the pipe T may interfere with the rollers 116 except the roller portion 115. If the pipe T interferes with the roller 116 other than the roller part 115, the liquid may not be fed, or the pipe T or the roller 116 may be damaged.
Therefore, the control unit 106 may have a function of operating the drive source 114 to rotate the roller 116 forward and backward when the closing of the lid 112 is detected. If the roller 116 is rotated in the normal direction and the reverse direction (for example, about ± 180 to 360 degrees), the tube T can be moved to an appropriate position even if the arrangement of the tube T is slightly deviated from the appropriate position. This makes it possible to shorten the working time because the pipe T does not need to be newly arranged.
Further, even if the roller 116 is rotated in the normal direction and the reverse direction, the pipe T may not be arranged at an appropriate position. Therefore, the control unit 106 is desired to have a safety function of disabling the driving source 114 when it is detected that the pipe T cannot be placed at an appropriate position, and an alarm function of notifying the operator of the improper placement of the pipe T. This prevents damage to the apparatus due to improper placement of the tubes T, and allows the operator to quickly notice an abnormality in placement of the tubes T.
For example, the alarm function may include the following functions: when the control unit 106 detects that the tube T is not arranged at an appropriate position, the control unit 106 causes the panel unit 106p to display an abnormal alarm or to emit an abnormal alarm sound.
As a method of detecting that the tube T is not disposed at an appropriate position, for example, a method of detecting the driving force of the driving unit 114 can be employed. In this case, when the driving force of the driving unit 114 is equal to or more than a certain value, the control unit 106 may determine that an abnormality has occurred in the arrangement of the tubes T. If the driving unit 114 is a motor, the control unit 106 can determine that an abnormality has occurred in the arrangement of the tubes T when the rotational resistance applied to the spindle is equal to or greater than a predetermined value. The rotational resistance applied to the spindle can be determined by, for example, detecting the value of current supplied to the motor.
< pipe positioning Member 160>
As a method of arranging the tube T at an appropriate position, the following tube positioning member 160 can be used. If the tube positioning member 160 described below is used, the tube T and the rollers 116 can be easily brought into close contact when the tube T is wound around the rollers 116, and the two tubes T can be easily wound around the two rollers 116 appropriately.
The structure of the tube positioning member 160 will be described below.
As shown in fig. 16 and 17, the tube positioning member 160 includes a pair of holding members 161, 161 and a coupling member 165.
< A pair of holding members 161, 161>
As shown in fig. 16 and 17, the pair of holding members 161 and 161 are members for holding the two tubes T and are disposed at a distance from each other (separated by a distance) along the axial direction of the two tubes T. The pair of holding members 161 and 161 have the same configuration, and are formed by combining the base member 162 and the guide member 163.
The base member 162 includes a base portion 162b that is a strip-shaped plate-like member. The base member 162 has a structure for holding the tube T such that the longitudinal direction of the base portion 162b is orthogonal to the axial direction of the tube T. Specifically, a tube arrangement portion 162c extending from the base portion 162b is provided on a side of the base member 162 in the short axis direction. The tube arrangement portion 162c is provided with a pair of outer holding portions d, d standing from the surface of the tube arrangement portion 162c, and a pair of inner holding portions c, c located between the pair of outer holding portions d, d and the base portion 162 b. The pair of inner holding portions c, c are disposed further inward in the longitudinal direction of the base portion 162b than the pair of outer holding portions d, d. The pair of inner holding portions c, c includes an upright portion that is erected from the surface of the tube arrangement portion 162c, and a curved portion that is curved outward in the longitudinal direction of the base portion 162b with respect to the upright portion. The pair of inner holding portions c, c are formed such that the distance between the outer surface of the standing portion and the inner surfaces of the pair of outer holding portions d, d in the longitudinal direction of the base portion 162b is substantially the same as the diameter of the tube T. The pair of inner holding portions c, c are formed such that the distance between the lower surface of the curved portion and the surface of the base portion 162b is also substantially the same as the diameter of the tube T.
Thus, when the base portion 162b is viewed in the short-axis direction, two holes (hereinafter referred to as virtual holes) are formed by the inner surfaces of the pair of outer holding portions d, the outer surfaces of the standing portions of the pair of inner holding portions c, the lower surface of the bent portion, and the surface of the base portion 162 b.
On the other hand, the guide member 163 is a member disposed so as to overlap the surface of the base portion 162b of the base member 162. The guide member 163 is provided with a pair of grooves 163g, 163g for accommodating the tube T on the surface of the base portion 162b which is located on the front surface side of the base portion 162b when the guide member overlaps the surface of the base portion 162 b. The pair of grooves 163g, 163g are provided so that the axial directions thereof are parallel to each other. The pair of grooves 163g and 163g is formed such that, when the guide member 163 is superimposed on the surface of the base portion 162b, the pair of grooves 163g and 163g are superimposed on (preferably coincide with) the two virtual holes when viewed from the short axis direction of the base portion 162 b.
Therefore, if two tubes T are disposed in the two imaginary holes of the base member 162, the two tubes T can be disposed in the base member 162 so as to be parallel to each other. In this state, if the guide member 163 is overlapped on the surface of the base portion 162b, the two tubes T can be arranged in the pair of grooves 163g and 163g, and the two tubes T can be held by the holding member 161 so as not to be separated.
The pair of grooves 163g and 163g of the tube arrangement portion 162c of the base member 162 and the guide member 163 corresponds to "a plurality of tube holding portions" in the claims. The longitudinal direction of the base portion 162b corresponds to "the direction in which the plurality of tube holding portions are arranged" in the claims. The minor axis direction of the base portion 162b corresponds to "the axial direction of the plurality of tubes held by the plurality of tube holding portions" in the claims.
< connecting Member 165>
As shown in fig. 16 and 17, the coupling member 165 couples the pair of pipe holders 161, 161. More specifically, the coupling member 165 is provided between the pair of tube holding portions 161, 161 in order to maintain the pair of tube holding portions 161, 161 at a predetermined distance apart in the axial direction of the tube T.
The coupling member 165 has a coupling structure at both ends thereof to couple the pair of tube holding portions 161, and is detachably coupled to the guide member 163 of the tube holding portion 161. Specifically, the coupling member 165 is provided so that an end of the coupling member 165 is coupled to a portion between the pair of grooves 163g and 163g in the guide member 163. That is, in a state where the coupling member 165 is extended, the coupling member 165 is coupled to the guide member 163 so as to be positioned between the adjacent tubes T held in the tube holding portion 161 when viewed from a direction intersecting the major axis direction and the minor axis direction of the base portion 162 b.
In a state where the coupling member 165 is extended, the coupling member 165 is coupled to the guide member 163 so as to be positioned on the opposite side of the base portion 162b from the central axis of the tube T held by the tube holding portion 161.
The coupling member 165 has a structure that can be bent between the pair of tube holding portions 161, 161 in a state where both ends are coupled to the pair of tube holding portions 161, 161. More specifically, the coupling member 165 has the following structure: can be bent in a direction intersecting the major axis direction and the minor axis direction of the base portion 162b between the pair of tube holding portions 161, 161.
For example, the coupling member 165 is formed of a plate-like member made of plastic. Both ends of the coupling member 165 are coupled to the guide members 163 of the pair of tube holding portions 161, 161 so that the width direction of the coupling member 165 is parallel to the longitudinal direction of the base portion 162 b. Thus, the coupling member 165 can be bent in a direction intersecting the major axis direction and the minor axis direction of the base portion 162b between the pair of tube holding portions 161, 161 (fig. 16).
When the pipe positioning member 160 is attached to the two pipes T, the following advantages can be obtained when the two pipes T are disposed in the roller pump 110.
First, when the tube T is wound around the two rollers 116 and 116 of the roller unit 115 of the roller pump 110, the stopper members T1 and T2 are provided in advance so as to be disposed at positions separated by an appropriate length (see fig. 16 and 17B). On the other hand, the pair of pipe holding portions 161, 161 are disposed between the stopper members T1, T2 so that the outer surfaces of the pair of pipe holding portions 161, 161 are in contact with the stopper members T1, T2, respectively. In a state where the tube T is extended and the outer surfaces of the pair of tube holding portions 161, 161 are in contact with the stopper members T1, T2 (hereinafter referred to as an appropriate arrangement state), the coupling member 165 is arranged between the pair of tube holding portions 161, 161 so as to be extended (see fig. 17B).
On the other hand, the roller pump 110 is provided with a pair of accommodating portions for accommodating the pair of pipe holding portions 161, 161. Specifically, a pair of accommodating portions for accommodating the pair of tube holding portions 161, 161 is provided in advance at positions sandwiching the surface including the rotation shaft 117 of the roller portion 115. The pair of accommodating portions are provided such that, when the pair of tube holding portions 161, 161 are accommodated in the pair of accommodating portions, respectively, the tube T is wound around the two rollers 116, 116 of the roller portion 115 in an appropriate state.
Thus, by simply arranging the pair of tube holding portions 161, 161 in the pair of housing portions, the two tubes T can be appropriately wound around the two rollers 116, 116 of the roller portion 115 (see fig. 15).
The coupling member 165 is coupled to the guide member 163 such that the coupling member 165 is positioned on the opposite side of the center axis of the tube T held by the tube holding portion 161 from the base portion 162 b. Thus, if the pipe T is wound around the roller 116 of the roller part 115 such that the guide member 163 is positioned on the roller 116 side, the coupling member 165 is positioned between the two pipes T with its center portion between both ends slightly bent (see fig. 16 (a) and (B)). Thus, even if two tubes T are arranged in a vertically aligned manner, the upper tube T can be prevented from contacting the lower tube T by the connecting member 165.
The coupling member 165 does not necessarily have to be located on the opposite side of the center axis of the tube T from the base portion 162 b. However, if this structure is adopted, the above-described effects can be obtained.
The tube holding portion 161 may be asymmetrical with respect to the middle of the base portion 162b in the longitudinal direction. In other words, the tube holding portion 161 may be formed asymmetrically with respect to the middle of the two tubes T held by the tube holding portion 161 in the longitudinal direction of the base portion 162 b. For example, as shown in fig. 17, the guide member 163 may have portions located outside the pair of grooves 163g and 163g with different lengths. In this way, when the pair of tube holding portions 161, 161 are disposed in the pair of housing portions, it is possible to prevent an error in putting the pair of tube holding portions 161, 161 in. That is, even if the pair of tube holding portions 161, 161 are arranged in the pair of accommodating portions from the wrong direction, the pair of tube holding portions 161, 161 can be set in a state where they cannot be accommodated in the pair of accommodating portions. This can prevent an operational error when the tube T is set in the roller pump 110. For example, when the tube T is provided in the roller pump, the tube T can be prevented from twisting or two tubes can be provided in the opposite rollers 116.
In addition, when a plurality of roller pumps are provided, the pipe holding portion 161 may be changed in size or shape by the roller pumps provided. This prevents the roller pump from being provided with the tube in an erroneous manner.
Further, the following functions may be provided: in the case where the pipe holding portion 161 is not appropriately provided in the pair of housing portions, the roller pump device is rendered inoperable. In this case, even if the roller 116 is rotated by mistake in the case where the tube T is not appropriately set, the tube T and the roller 116 can be prevented from being damaged. For example, if a button-type sensor or the like that is pressed when the appropriate tube holding portion 161 is disposed is provided in the pair of housing portions, the above-described function can be exhibited.
In the above example, the case where the tube positioning member 160 holds two tubes T has been described. However, the number of tubes T held by the tube positioning member 160 may be 3 or more, and is not particularly limited. When the tube positioning member 160 holds three or more tubes T, it is desirable to provide the connecting members 165 between the adjacent tubes T.
Further, the structures of the holding member 161 and the plurality of tube holding portions are not limited to the above-described structures. The holding member 161 and the plurality of tube holding portions may be any member as long as the plurality of tubes are parallel to each other and can be held in a line. For example, the plate-like holding member may be formed with only through holes arranged in a line to form a plurality of tube holding portions. The term "a column" as used herein also includes the following cases: when a plurality of tubes are arranged in the plurality of tube holding portions, the central axes of the plurality of tubes are substantially aligned on the same plane; when the tube T held by the plurality of tube holding portions is viewed in the axial direction of the tube T, the position of the center axis of the tube T may be displaced in the normal direction of the surface of the base member 162. For example, when the tubes T held by the plurality of tube holding portions are viewed in the axial direction of the tubes T, the case where the positions of the central axes of the tubes T are arranged in a staggered arrangement is also included in the above-described state where the plurality of tubes are held in a row.
< Filter holder 101 and concentrator holder 102>
As shown in fig. 13, 14, and 19, a filter holder 101 and a concentrator holder 102 are provided outside the pair of roller pumps 110 and 120, respectively. As shown in fig. 13 and 14, the roller pump 110 provided on the left side of the control unit 106 includes a filter holding unit 101, and the roller pump 120 provided on the right side of the control unit 106 includes a concentrator holding unit 102.
The filter holding portion 101 and the concentrator holding portion 102 have clamping portions 101c and 102c on the surfaces thereof, and the filter 10 and the concentrator 20 can be detachably held by the clamping portions 101c and 102 c.
The proximal ends of the filter holder 101 and the concentrator holder 102 are swingably connected to the frames of the pair of roller pumps 110 and 120. Specifically, if the filter holder 101 and the concentrator holder 102 are swung outward, the filter holder 101 and the concentrator holder 102 are coupled to the frames of the pair of roller pumps 110 and 120 so that the clamps 101c and 102c are exposed. On the other hand, if the filter holding unit 101 and the concentrator holding unit 102 are swung inward, the filter holding unit 101 and the concentrator holding unit 102 are coupled to the frames of the pair of roller pumps 110 and 120 so that the clamps 101c and 102c face the pair of rollers 116 and 116 of the pair of roller pumps 110 and 120. That is, when the operation of treating the raw liquid is not performed, the filter holder 101 and the concentrator holder 102 can be accommodated in the roller pumps 110 and 120. The filter holder 101 and the concentrator holder 102 are not necessarily connected to the frames of the pair of roller pumps 110 and 120 so as to be swingable, but are always exposed to the outside of the roller pumps 110 and 120. However, if the above-described configuration is adopted, there is an advantage that the raw liquid treatment apparatus 1 according to embodiment 1 can be compactly housed without using the raw liquid treatment apparatus 1 according to embodiment 1.
Fig. 13, 14, and 19 show the following cases: the filter holder 101 and the concentrator holder 102 hold the filter 10 and the concentrator 20 in a state in which the axial directions of the filter 10 and the concentrator 20 (for example, the axial directions of the hollow fiber membranes 16 in the case where the hollow fiber membranes 16 are provided inside as shown in fig. 5) are directed in the vertical direction. However, the filter holder 101 and the concentrator holder 102 may hold the filter 10 and the concentrator 20 in a state where the axial directions of the filter 10 and the concentrator 20 are oriented in the horizontal direction. The state in which the axial directions of the filter 10 and the concentrator 20 are directed vertically herein is a concept including a case in which the axial directions of the filter 10 and the concentrator 20 are inclined by about 0 to 45 degrees with respect to the vertical direction. The state in which the axial directions of the filter 10 and the concentrator 20 are oriented in the horizontal direction as used herein is a concept including a case in which the axial directions of the filter 10 and the concentrator 20 are inclined by about 0 to 45 degrees with respect to the horizontal direction.
The raw liquid treatment apparatus 1 according to embodiment 1 does not necessarily have to include the filter holder 101 and the concentrator holder 102. However, if the main body 100 includes the filter holder 101 and the concentrator holder 102, there is an advantage that a separate holder for holding the filter 10 and the concentrator 20 may not be provided.
< A pair of suspension sections 103, 103>
As shown in fig. 13, 14 and 19, a pair of hanging portions 103, 103 are provided on the rear surface of the main body 100. The pair of suspension portions 103, 103 are formed of shaft-like members, and base ends of the shafts are detachably attached to a pair of attachment portions 100h, 100h provided on the back surface of the main body portion 100. More specifically, a pair of attachment portions 100h, 100h are provided so that the axial direction of the pair of hanging portions 103, 103 becomes substantially vertical when the base ends of the pair of hanging portions 103, 103 are attached to the pair of attachment portions 100h, 100 h.
The pair of hanging portions 103 and 103 are provided with a hook portion 103b in the same manner as a general drip stand. The pair of hanging portions 103, 103 can hang the respective bags B on the hooking portions 103B.
Further, a hook 103f is provided on the pair of hanging portions 103, and the tube holder 150 can be hung on the hook 103 f.
The pair of suspending portions 103, 103 do not necessarily have to be detachable from the main body 100. However, if the pair of suspension portions 103 and 103 is detachably attached, the following advantages can be obtained: by removing the pair of suspending portions 103 and 103 when the raw liquid processing apparatus 1 according to embodiment 1 is not used, the raw liquid processing apparatus 1 according to embodiment 1 can be compactly housed.
The number of the suspending portions 103 provided in the raw liquid processing apparatus 1 according to embodiment 1 is not limited to 2, and may be 1, or 3 or more. The number of hanging portions 103 may be set to an appropriate number according to the number of bags B, the number of tubes T, and the like used for the treatment performed by the raw liquid treatment apparatus 1 according to embodiment 1.
The raw liquid processing apparatus 1 according to embodiment 1 does not necessarily have to have a pair of suspending portions 103 and 103. In this case, a general drip stand for hanging a drip may be used. However, if the main body 100 has the pair of hanging portions 103 and 103, there is an advantage that a drip stand or the like does not have to be separately prepared.
< tube holder 150>
As shown in fig. 18, the tube holder 150 is a member for holding a plurality of tubes T. If the tube holder 150 holds a plurality of tubes T in advance, the plurality of tubes T can be suspended in advance from the pair of suspending portions 103, 103 as shown in fig. 18 (see fig. 19). Accordingly, when the plurality of tubes T are provided to the control unit 106, the filter 10, the concentrator 20, and the pair of roller pumps 110 and 120 of the main body 100, only the necessary tubes T can be removed from the tube holder 150 and the work can be performed. That is, when the plurality of tubes T are set in the apparatus, it is not necessary for the operator to hold the tubes T which are not immediately used in advance, and therefore, the operation of the operator becomes easy.
< body 151>
As shown in fig. 18, the tube holder 150 includes a plate-shaped main body 151. The body 151 has a coupling portion 152 at an upper end edge 151a thereof. The coupling portion 152 is formed with a through hole 152h penetrating inside and outside, and the pipe holder 150 can be suspended from the suspending portion 103 with its upper end edge 151a directed upward by passing the hook portion 103f of the pair of suspending portions 103, 103 through the through hole 152 h.
In order to stably hang the pipe holder 150 from the pair of hanging portions 103, 103 with the upper end edge 151a facing upward, the through hole 152h and the hook portion 103f of the pair of hanging portions 103, 103 are preferably laterally long. That is, the through hole 152h of the coupling portion 152 is desirably a horizontally long hole that is long in the direction along the upper end edge 151 a. Further, it is desirable that the hook portions 103f of the pair of suspension portions 103, 103 also have a laterally long shape which is long in a direction orthogonal to the axial direction of the pair of suspension portions 103, 103.
< holding part 155>
A plurality of holding portions 155 for detachably holding the tubes T are provided on the surface 151c (first surface) of the body 151. The holding portion 155 has a tubular structure having a slit-like opening 155s formed in a front surface thereof, and a through hole 155h penetrating in a vertical direction. The width of the opening 155s of the through hole 155h of the holding portion 155 is smaller than the diameter of the tube T. That is, the tube T can be placed in the through hole 155h of the holding portion 155 and held by pushing the tube T into the through hole 155h from the opening 155s, and the tube T can be detached from the holding portion 155 by pulling the tube T.
The plurality of holding portions 155 are arranged in a row along the upper end edge 151a of the body portion 151. The plurality of holding portions 155 are provided such that the center axes of the through holes 155h are parallel to each other. Therefore, when the plurality of tubes T are held by the plurality of holding portions 155, the plurality of tubes T can be arranged in parallel with each other in the axial direction and aligned in a line along the surface 151c of the body portion 155. Thus, if a plurality of tubes T are mounted in advance in the order determined by the plurality of holding portions 155, it is possible to prevent an operator from making mistakes such as missing a plurality of tubes T. For example, the plurality of tubes T are attached to the plurality of holding portions 155 in advance from the left side of the plurality of holding portions 155 to the right side of the plurality of holding portions 155 so that the plurality of tubes T are sequentially arranged in the order of connection to the apparatus. Accordingly, the operator can remove the tubes T in order from the left without mistake, and thus the operator can prevent a mistake and reduce the work load.
The phrase "the plurality of holding portions 155 are aligned in a line along the upper end edge 151a of the main body 151" also includes a case where the plurality of holding portions 155 are arranged in a staggered manner, and a case where the plurality of holding portions are slightly offset in a direction intersecting the upper end edge 151a of the main body 151.
< engaging means 153>
The coupling portion 152 includes an engaging member 153 on the rear surface 151d (i.e., on the second surface opposite to the front surface 151 c) side of the body 151. The engaging member 153 is provided so as to protrude toward the rear surface 151d of the body 151, has an opening 153s at one end (upper end), and has a gap 153h continuous with the opening 153 s.
If such an engaging member 153 is provided, the tubes T held by the plurality of holding portions 155 of the body 151 can be faced downward at one time or the tubes T can be held downward. For example, if the edge of the tub or the like is inserted into the gap 153h through the opening 153s, the pipe holder 150 can be attached to the tub or the like so that the upper end edge 115a of the main body 151 faces downward. Thus, if the plurality of tubes T are attached to the plurality of holding portions 155 in advance such that the distal ends thereof face the upper end edge 115a side of the body 151 (upward in a state where the body 151 is suspended by the suspending portion 103), the distal ends of the plurality of tubes T can be arranged downward at one time. That is, when discharging liquid from the plurality of tubes T into the tub or the like, the engaging member 153 can be easily attached to the edge of the tub or the like to be able to discharge liquid from the plurality of tubes T.
The shape and the like of the coupling portion 152 are not limited to the above-described shapes and the like. The shape may be any shape as long as the body 151 can be connected to the pair of suspending portions 103, and the like in advance.
The shape and the like of the engaging member 153 are not limited to those described above, and may be any shape having the above-described functions. Further, the engaging member 153 is not necessarily provided.
Further, in the above example, the case where the engaging member 153 is provided on the back surface 151d of the main body 151 has been described, but the engaging member 153 may be provided on the front surface 151c of the main body 151, or may be provided on both the front surface 151c and the back surface 151d of the main body 151.
< Filter 10 and concentrator 20>
Before describing the circuit of the raw liquid treatment apparatus 1 according to embodiment 1, an example of a filter and a concentrator used in the raw liquid treatment apparatus 1 according to embodiment 1 will be described. In addition, although the filter and the concentrator using the hollow fiber membrane as the filter member will be described below, the filter and the concentrator used in the raw liquid treatment apparatus 1 according to embodiment 1 are not limited to the filter and the concentrator using the hollow fiber membrane as the filter member, and a filter and a concentrator using a known filter member other than the hollow fiber membrane may be used.
< Filter 10>
The filter 10 is, for example, a peritoneal fluid filter used for CART, a plasma separator used for plasma exchange, a plasma component separator, or the like. The filter 10 contains a filter member therein, and can separate a raw liquid such as pleural effusion and peritoneal effusion into a filtrate and a separation liquid including cells and the like by filtering the raw liquid with the filter member.
As shown in fig. 5, the filter 10 includes a main body 11 and a hollow fiber membrane bundle 15 disposed in the main body 11.
< hollow fiber Membrane bundle 15>
As shown in fig. 5, the hollow fiber membrane bundle 15 is configured by bundling a plurality of hollow fiber membranes 16.
The hollow fiber membranes 16 are tubular members each having a wall 16w with an annular cross section, and a through flow passage 16h penetrating the hollow fiber membranes 16 in the axial direction is formed inside the wall 16 w. The wall 16w of the hollow fiber membrane 16 has a function of allowing liquid to permeate, but not solid components such as cells and gas.
The thickness of the wall 16w of the hollow fiber membrane 16 is about 45 to 275 μm, and the diameter of the through channel 16h is about 50 to 500 μm, but the thickness of the wall 16w of the hollow fiber membrane 16, the diameter of the through channel 16h, and the like are not particularly limited.
One end portions and the other end portions of the plurality of hollow fiber membranes 16 of the hollow fiber membrane bundle 15 are bundled. That is, the hollow fiber membrane bundle 15 is formed by bundling a plurality of hollow fiber membranes 16 so that the through flow path 16h of each hollow fiber membrane 16 penetrates between one end portion and the other end portion of the hollow fiber membrane bundle 15.
In addition, the two end portions of the plurality of hollow fiber membranes 16 do not necessarily have to be bundled together with each other. In this case, both ends of the through channels 16h of the plurality of hollow fiber membranes 16 are arranged to communicate with the pair of header portions 13 and 14 of the main body portion 11, respectively.
The number of hollow fiber membranes 16 constituting the hollow fiber membrane bundle 15 is not particularly limited. For example, about 1000 to 20000 hollow fiber membranes 16 may be bundled to form the hollow fiber membrane bundle 15. In addition, the hollow fiber membrane bundle 15 may be formed by bundling a plurality of hollow fiber membranes 16 so that the cross-sectional area of the hollow fiber membrane bundle 15 becomes a desired cross-sectional area without limiting the number of hollow fiber membranes. For example, if the cross section of the hollow fiber membrane bundle 15 is circular, a plurality of hollow fiber membranes 16 may be bundled so that the diameter thereof becomes about 20 to 75 mm.
< body section 11>
As shown in fig. 5, the body portion 11 includes a body portion 12, and the body portion 12 has an internal space 12h which is a space hermetically and liquid-tightly isolated from the outside. The internal space 12h of the body portion 12 is formed to communicate with the outside only through a port described later, and accommodates the hollow fiber membrane bundle 15 described above therein. In a state where the hollow fiber membrane bundle 15 is accommodated inside, the internal space 12h is separated from the through channels 16h of the plurality of hollow fiber membranes 16 in an airtight manner, but liquid can pass through the wall 16w therebetween. That is, the liquid in the internal space 12h can be supplied to the through-flow passage 16h, and the liquid in the through-flow passage 16h can be supplied to the internal space 12 h.
The size and shape of the internal space 12h are not particularly limited. In the state where the hollow fiber membrane bundle 15 is accommodated, the liquid flowing into the internal space 12h through the port may flow between the hollow fiber membrane bundle 15 and the inner surface of the body portion 12 (i.e., the inner surface of the internal space 12 h) and between the plurality of hollow fiber membranes 16, and may have a size that allows the liquid to flow into the through flow channel 16h through the wall 16w of the hollow fiber membranes 16. In addition, the liquid (filtrate) that has flowed out of the through-flow channel 16h to the internal space 12h through the wall 16w of the hollow fiber membranes 16 may flow between the plurality of hollow fiber membranes 16 and between the hollow fiber membrane bundle 15 and the inner surface of the internal space 12h, as long as it has a size that allows the liquid to flow out from the port.
As shown in fig. 5, the body portion 11 is provided with a pair of header portions 13 and 14 so as to sandwich the body portion 12, that is, so as to sandwich the internal space 12 h. The pair of header portions 13 and 14 are spaces that are air-tight and liquid-tight isolated from the internal space 12h of the body portion 12 and the outside, and are formed to have spaces that communicate with the outside only through ports described later. The respective ends of the hollow fiber membrane bundle 15 are connected to the pair of header pipes 13 and 14. Specifically, both ends of the hollow fiber membrane bundle 15 are connected to the pair of header sections 13 and 14, respectively, so that openings at both ends of the through channels 16h of the plurality of hollow fiber membranes 16 constituting the hollow fiber membrane bundle 15 communicate with the spaces inside the pair of header sections 13 and 14. Therefore, the spaces inside the pair of header sections 13 and 14 are in a state of being communicated with each other through the through channels 16h of the plurality of hollow fiber membranes 16 constituting the hollow fiber membrane bundle 15.
< ports 11a to 11c >
As described above, the body portion 11 is provided with the port 11c for communicating the internal space 12h formed in the body portion 12 of the body portion 11 with the outside. Further, the pair of header portions 13 and 14 are provided with ports 11a and 11b, respectively, which communicate the internal space with the outside.
As shown in fig. 5, the header portion 13 provided at one end of the body portion 11 is provided with a raw liquid supply port 11a for communicating the space inside the header portion 13 with the outside. The raw liquid supply port 11a is a port to which one end of a tube or the like is connected. For example, in fig. 1, one end of the liquid feed tube 2 is connected to the raw liquid supply port 11a, and the other end of the liquid feed tube 2 is connected to the liquid discharge port of the raw liquid bag UB.
In fig. 1, the cleaning liquid recovery bag FB is connected to the raw liquid supply port 11a through the liquid supply tube 2, or directly connected to the raw liquid supply port 11 a. Specifically, one end of the cleaning liquid recovery tube 7 is connected to the liquid supply tube 2 or the raw liquid supply port 11a, and the other end of the cleaning liquid recovery tube 7 is connected to the cleaning liquid recovery bag FB.
The body portion 12 of the body portion 11 has 2 ports 11c on its side surface for communicating the internal space 12h with the outside. The 2 ports 11c are ports to which one ends of pipes and the like are connected. For example, in fig. 1, one end of the filtrate supply pipe 3 is connected to the lower port 11c, and the other end of the filtrate supply pipe 3 is connected to the filtrate supply port 20a of the concentrator 20. That is, the lower port 11c functions as a filtrate discharge port 11c for discharging the filtrate to the outside. On the other hand, the upper port 11c may function as a filtrate discharge port 11c for discharging the filtrate to the outside, as in the lower port 11c, and may also function as a port for supplying a fluid such as a liquid (cleaning liquid or the like) and a gas (air or the like) from the outside to the trunk portion 12 of the main body portion 11, or for discharging a fluid such as a liquid (filtrate, cleaning liquid or the like) and a gas (air or the like) from the trunk portion 12 of the main body portion 11. In fig. 5, 2 ports 11c are provided, but 1 port 11c may be provided, and 3 or more ports 11c may be provided.
The header 14 provided at the other end of the main body 11 is provided with a cleaning liquid supply port 11b that communicates between the space inside the header 14 and the outside. The cleaning liquid supply port 11b is a port to which one end of a pipe or the like is connected. For example, as shown in fig. 1, one end of the cleaning liquid supply pipe 6 is connected to the cleaning liquid supply port 11b, and the other end of the cleaning liquid supply pipe 6 is connected to the cleaning liquid bag SB.
The pair of header units 13 and 14 correspond to a first liquid supply unit and a second liquid supply unit in the claims. The pair of header units 13 and 14 may be such that the header unit 13 is a first liquid supply unit and the header unit 14 is a second liquid supply unit, or the header unit 13 may be a second liquid supply unit and the header unit 14 may be a first liquid supply unit.
< function of Filter 10 >
The filter 10 has the above-described configuration, and therefore can supply and discharge a fluid such as a liquid or a gas to and from the ports 11a to 11c through a pipe or the like.
For example, as shown in fig. 1, if the raw liquid bag UB and the cleaning liquid bag SB are connected to the ports 11a to 11c via the respective tubes, a filtrate obtained by filtering the raw liquid can be obtained. That is, the feed pipe liquid feeding portion 2p can be operated to supply the raw liquid from the raw liquid bag UB to the header portion 13 of the main body portion 11 via the feed pipe 2 and the raw liquid supply port 11 a. Thus, the raw liquid is supplied to the through flow channel 16h of the hollow fiber membranes 16 of the hollow fiber membrane bundle 15, and therefore, the raw liquid can be filtered by the hollow fiber membranes 16. That is, since the solid component contained in the raw liquid cannot pass through the hollow fiber membranes 16, it remains in the through flow path 16h, and only the liquid component, that is, the filtrate passes through the walls 16w of the hollow fiber membranes 16, so that the filtrate after filtration of the raw liquid can be obtained.
Further, if the tubes are connected to the ports 11a to 11c of the filter 10 as shown in fig. 1, the filtrate is discharged from the hollow fiber membranes 16 into the internal space 12h of the body portion 12 of the body portion 11, and then is supplied from the internal space 12h to the concentrator 20 through the filtrate discharge port 11c, the filtrate supply tube 3, and the filtrate supply port 20a of the concentrator 20.
On the other hand, if a circuit as shown in fig. 1 is provided, the filter 10 can be cleaned if the cleaning liquid recovery pipe liquid feeding unit 7p (or the liquid feeding pipe liquid feeding unit 2p) is operated to suck the liquid out of the filter 10. That is, since the cleaning liquid can be supplied from the cleaning liquid bag SB to the header part 14 of the main body part 11 via the cleaning liquid supply tube 6 and the cleaning liquid supply port 11b, the cleaning liquid can be supplied from the header part 14 into the through flow path 16h of the hollow fiber membrane 16 (see fig. 5). Then, the cleaning liquid flows from the header part 14 toward the header part 13 by the force of the sucked fluid generated by the cleaning liquid recovery pipe liquid feeding part 7p, and therefore the inside of the through flow passage 16h of the hollow fiber membrane 16, particularly the inner surface of the through flow passage 16h (inner surface of the wall 16 w) can be cleaned by the cleaning liquid flowing along the inner surface of the through flow passage 16 h. This enables solid matter and the like adhering to the inner wall of the through channel 16h of the hollow fiber membrane 16 to be efficiently washed away.
< cleaning of Filter 10 >
In particular, if the operation is performed as described below, the cleaning of the hollow fiber membranes 16 can be effectively performed.
In the following cleaning operation, a case will be described in which the filtering operation is performed in a state in which the raw liquid supply port 11a is positioned above the cleaning liquid supply port 11b, and the cleaning operation is performed in the same state.
As shown in fig. 21, the filtrate supply pipe 3 and the connecting pipe 9 are closed by a flow rate adjusting mechanism 3c provided in the filtrate supply pipe 3 and a connecting pipe liquid feeding portion 9p provided in the connecting pipe 9. On the other hand, the cleaning liquid supply pipe 6 is opened by the flow rate adjusting mechanism 6 c. In this state, the cleaning liquid recovery pipe liquid feeding portion 7p of the cleaning liquid recovery pipe 7 is operated.
As a result, a negative pressure is generated in the cleaning liquid recovery pipe 7 on the upstream side of the cleaning liquid recovery pipe liquid feeding portion 7p, that is, on the filter 10 side. If such a negative pressure is generated, the cleaning liquid flows from the cleaning liquid bag SB connected to the cleaning liquid supply tube 6 into the cleaning liquid recovery tube 7 through the cleaning liquid supply tube 6, the cleaning liquid supply port 11b, the header portion 14, the through flow path 16h of the hollow fiber membrane 16, the header portion 13, and the raw liquid supply port 11a by the negative pressure.
At this time, since the filtrate supply tube 3 and the connection tube 9 are closed, the cleaning liquid flows only in the through flow channel 16h of the hollow fiber membranes 16 without flowing from the hollow fiber membranes 16 to the internal space 12 h. Thus, only the inside of the through flow path 16h between the pair of header parts 13 and 14 and the hollow fiber membrane 16 can be cleaned with the cleaning liquid, and therefore the cleaning liquid for cleaning the filter 10 can be reduced.
Further, since the internal space 12h is not cleaned, even when the filter 10 is cleaned after the filtration concentration is performed, the filtrate can be left in the internal space 12 h. This can prevent the filtrate in the internal space 12h from being discharged together with the cleaning liquid, and thus can prevent a decrease in the recovery rate of the filtrate.
In cleaning the filter 10, both the liquid supply pipe liquid feeding portion 2p of the liquid supply pipe 2 and the cleaning liquid recovery pipe liquid feeding portion 7p of the cleaning liquid recovery pipe 7 may be operated.
In addition, when cleaning the filter 10, the feed pipe liquid feeding unit 2p may be operated instead of the cleaning liquid recovery pipe liquid feeding unit 7 p. In this case, since the raw liquid in the through channel 16h of the hollow fiber membrane 16 can be recovered to the raw liquid bag UB together with the cleaning liquid, if the cleaning liquid including the recovered raw liquid is supplied again to the filter 10, the amount of the raw liquid used for filtration and concentration can be prevented from decreasing.
As described above, when one or both of the liquid feeding portion 2p and the cleaning liquid recovery tube liquid feeding portion 7p are operated, negative pressure is generated in the through flow path 16h of the hollow fiber membrane 16. Thereby, even if the solid content is clogged inside the wall 16w of the hollow fiber membrane 16, the solid content can be sucked out, and therefore, the clogging of the wall 16w of the hollow fiber membrane 16 can be eliminated.
In addition, when the main purpose is to also remove clogging of the wall 16w of the hollow fiber membrane 16, the cleaning liquid bag SB may be connected to the connecting pipe 9 (see fig. 21) in advance, and the connecting pipe liquid feeding unit 9p may be operated so that the cleaning liquid flows from the cleaning liquid bag SB toward the filter 10. In this case, since the internal space 12h is also substantially cleaned, the clogging of the wall 16w of the hollow fiber membrane 16 can be more easily eliminated although the amount of cleaning liquid used increases. That is, in addition to the suction effect by the negative pressure described above, the effect of pushing the cleaning liquid into the connecting pipe liquid feeding portion 9p is also produced, and therefore, clogging of the wall 16w of the hollow fiber membrane 16 can be more easily eliminated. In addition, when the suction effect of the liquid feeding pipe liquid feeding portion 2p and the cleaning liquid recovery pipe liquid feeding portion 7p is sufficiently large, only the connecting pipe 9 may be maintained so that the cleaning liquid supplied from the cleaning liquid bag SB flows inside the connecting pipe 9. For example, by providing a jig or the like in the connecting pipe 9 instead of the connecting pipe liquid feeding portion 9p, cleaning of the internal space 12h and removal of clogging of the wall 16w of the hollow fiber membrane 16 can be effectively performed even if the connecting pipe 9 is opened in advance.
Further, if the cleaning operation is performed as described above, it becomes easy to eliminate the clogging of the header part 13 to which the stock solution is supplied.
In the header part 13 to which the stock solution is supplied, the solid component contained in the stock solution is supplied as it is to the liquid supply tube 2, and therefore, when the solid component is large, the opening of the through channel 16h of the hollow fiber membrane 16 may be blocked by the solid component. However, as described above, if a negative pressure is generated in the cleaning liquid recovery pipe 7 on the side closer to the filter 10 than the cleaning liquid recovery pipe liquid feeding portion 7p, the solid component can be sucked out from the header portion 13 to the cleaning liquid recovery pipe 7 by the negative pressure, and therefore the clogging of the header portion 13 can be eliminated. In this case, the cleaning solution bag SB may be connected to the connecting pipe 9 in advance, and the connecting pipe liquid feeding portion 9p may be operated so that the cleaning solution flows from the cleaning solution bag SB toward the filter 10. This produces an effect of pushing the cleaning liquid into the connecting pipe liquid feeding portion 9p in addition to the suction effect by the negative pressure, and therefore, the clogging of the collecting pipe portion 13 can be more easily eliminated.
In the above example, the case where the cleaning liquid is made to flow in the direction opposite to the direction in which the raw liquid flows has been described, but the cleaning liquid may be made to flow in the same direction as the direction in which the raw liquid flows (i.e., the direction in which the raw liquid flows at the time of filtration and concentration). Even in this case, there is a possibility that clogging of the wall 16w of the hollow fiber membrane 16 can be eliminated. For example, in fig. 21, the cleaning solution recovery bag FB is connected to the connecting pipe 9 instead of the cleaning solution bag SB, and the connecting pipe liquid feeding portion 9p is operated so that the liquid flows from the filter 10 to the cleaning solution recovery bag FB. At this time, if the operation of the liquid feeding pipe section 2p and the cleaning liquid recovery pipe section 7p is stopped in advance, the cleaning liquid supplied from the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6 can be made to flow so as to permeate through the wall 16w of the hollow fiber membranes 16, and therefore the solid content clogged in the wall 16w of the hollow fiber membranes 16 may be pushed out. In this case, the liquid feeding pipe liquid feeding unit 2p or the cleaning liquid collecting pipe liquid feeding unit 7p may be operated. This makes it possible to simultaneously remove clogging of the wall 16w of the hollow fiber membrane 16 and clean the inside of the through channel 16h of the hollow fiber membrane 16.
In the case of the above method (in the case where the cleaning liquid is made to flow in the direction in which the raw liquid flows at the time of filtration and concentration), the cleaning liquid may be made to flow so as to permeate through the wall 16w of the hollow fiber membrane 16 after the cleaning in the through channel 16h of the hollow fiber membrane 16 is performed. That is, first, the liquid feeding pipe liquid feeding unit 2p or the cleaning liquid collecting pipe liquid feeding unit 7p is operated in a state where the operation of the connecting pipe liquid feeding unit 9p is stopped. Thus, since the cleaning liquid can be made to flow through the through channel 16h of the hollow fiber membrane 16, the through channel 16h can be cleaned, and the deposits in the through channel 16h can be removed. Then, the operation of the liquid feeding pipe section 2p and the cleaning liquid collecting pipe section 7p is stopped, and the connecting pipe section 9p is operated. Accordingly, since the cleaning liquid can be flowed so as to permeate through the wall 16w of the hollow fiber membrane 16, clogging of the wall 16w of the hollow fiber membrane 16 can be eliminated. In addition, in this method, since the deposits in the through-flow channel 16h of the hollow fiber membrane 16 can be removed at an early stage, the wall 16w of the hollow fiber membrane 16 can be prevented from being clogged with the deposits.
In addition, the above method can be similarly implemented even in the following cases: the dope is supplied into the hollow space 12h of the body 12, and is filtered by flowing the dope from the hollow space 12h of the body 12 into the through-flow passage 16h of the hollow fiber membrane 16. In this case, after the cleaning in the hollow space 12h of the body portion 12 is performed, the cleaning liquid may be flowed so as to permeate through the wall 16w of the hollow fiber membrane 16.
< Another example of cleaning the Filter 10 >
When the filtration and concentration operation is performed in the middle of the circuit shown in fig. 1, 7, and 11, or when the filter 10 is cleaned after the completion of the filtration and concentration operation, the through flow path 16h of the hollow fiber membrane 16 of the filter 10 or the space between the pair of header parts 13 and 14 is filled with the raw liquid, and the internal space 12h of the trunk part 12 is filled with the filtrate. In this state, if the cleaning liquid is supplied from the cleaning liquid supply port 11b or the filtrate discharge port 11c, clogging in a predetermined region of the hollow fiber membranes 16 can be removed. That is, the clogging of the hollow fiber membranes 16 can be removed up to the position where the internal space 12H of the body portion is filled with the filtrate (for example, the position of H1 in fig. 20).
However, when the filter 10 is cleaned during the filtering and concentrating operation, the filter 10 may be cleaned after performing either or both of the operation of discharging the raw liquid in the through flow path 16h of the hollow fiber membrane 16 and the spaces of the pair of header sections 13 and 14 and the operation of discharging the filtrate in the internal space 12h of the trunk section (recovery operation described later). That is, the raw liquid in the through flow path 16h of the hollow fiber membrane 16 and the space between the pair of header sections 13 and 14 may be left as it is, and the filtrate in the internal space 12h of the trunk section may be discharged and then the filter 10 may be cleaned. On the other hand, the filtrate in the internal space 12h of the body may be left as it is, and the raw liquid in the through flow path 16h of the hollow fiber membrane 16 and the space of the pair of header parts 13 and 14 may be discharged and then the filter 10 may be cleaned. In this case, even if a liquid (filling liquid) such as a cleaning liquid is supplied into the through channel 16h of the hollow fiber membranes 16 or the internal space 12h of the body portion 12, the clogging of the hollow fiber membranes 16 can be removed only in the region where the filling liquid is present in the internal space 12h of the body portion 12 or the through channel 16h of the hollow fiber membranes 16.
Therefore, when performing both or either of the operation of discharging the raw liquid in the through-flow channel 16h of the hollow fiber membrane 16 and the space between the pair of header sections 13 and 14 and the operation of discharging the filtrate in the internal space 12h of the trunk section (recovery operation described later), it is desirable to supply the cleaning liquid to the filter 10 so that the cleaning liquid permeates the hollow fiber membrane 16 while the hollow space 12h of the trunk section 12 and/or the through-flow channel 16h of the hollow fiber membrane 16 are filled with the filling liquid to fill the region to be cleaned in the hollow fiber membrane 16. That is, it is desirable to supply the cleaning liquid to the filter 10 so that the cleaning liquid permeates the hollow fiber membranes 16 in a state where the entire or a part of the hollow fiber membranes 16 is filled with the filling liquid.
When the cleaning liquid is caused to flow from the outside of the hollow fiber membranes 16, that is, from the inside of the internal space 12h of the trunk portion into the through channels 16h of the hollow fiber membranes 16, the region to be cleaned does not necessarily have to be filled with the filling liquid in the through channels 16h of the hollow fiber membranes 16. However, the region to be cleaned needs to be filled with the filling liquid in the internal space 12h of the body portion 12. In the case where the cleaning liquid is caused to flow from the inside of the hollow fiber membranes 16, that is, from the inside of the through channels 16h of the hollow fiber membranes 16 into the internal space 12h of the trunk portion to perform cleaning (in the case where the cleaning liquid is caused to flow in the direction in which the raw liquid flows at the time of the above-described filtration and concentration), it is necessary to fill the through channels 16h of the hollow fiber membranes 16 with the filling liquid in the region to be cleaned.
The filling liquid filling the hollow space 12h of the body 12 and/or the through channel 16h of the hollow fiber membrane 16 is not limited to a cleaning liquid (e.g., physiological saline, an infusion liquid (extracellular fluid), etc.) used for cleaning. For example, a liquid containing a waste liquid or a substance (e.g., a surfactant) that enhances the cleaning effect may be used as the filling liquid, or a raw liquid may be used.
The cleaning liquid used for cleaning is not particularly limited as long as it can be used for cleaning. For example, a liquid containing a waste liquid or a substance (e.g., a surfactant) that enhances the cleaning effect may be used as the cleaning liquid, or a raw liquid may be used.
In the following description, a case where a cleaning liquid generally used for cleaning is used as the filling liquid and the cleaning liquid will be described.
For example, in fig. 21, first, the filtrate supply pipe 3 is closed by the flow rate adjustment mechanism 3c, and the operations of both the liquid supply pipe liquid feeding unit 2p and the cleaning liquid recovery pipe liquid feeding unit 7p are stopped. The cleaning liquid supply pipe 6 is also closed by the flow rate adjustment mechanism 6 c. When the hollow space 12h of the body portion 12 is filled with the cleaning liquid, the upper port 11c is opened to the atmosphere. When the through-flow passage 16h of the hollow fiber membranes 16 is filled with the cleaning solution, a portion of the liquid supply pipe 2 and/or the cleaning solution recovery pipe 7 on the side of the through-flow passage 16h of the hollow fiber membranes 16 closer to the liquid supply pipe liquid feeding portion 2P and/or the cleaning solution recovery pipe liquid feeding portion 7P than to the through-flow passage 16h of the hollow fiber membranes 16 (for example, a position of a pressure gauge P2 in fig. 21) is opened to the atmosphere. In this state, the connecting tube liquid feeding portion 9p is operated to supply the cleaning liquid from the cleaning liquid bag SB into the hollow space 12h of the body portion 12. The hollow space 12H of the body 12 and/or the through flow path 16H of the hollow fiber membrane 16 are filled with the cleaning liquid up to the region where cleaning is performed, for example, the region where filtrate is present in the filtration concentration operation (for example, the height of H1 in fig. 20).
After the cleaning liquid is filled in the above-described region, the cleaning liquid supply pipe 6 is opened by the flow rate adjusting mechanism 6c and the cleaning liquid recovery pipe liquid feeding portion 7p is operated while the connecting pipe liquid feeding portion 9p is kept in operation. Thus, the hollow space 12h of the hollow fiber membranes 16 and the trunk portion 12 can be cleaned by the cleaning liquid supplied from the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6 and the connecting pipe 9, and clogging of the hollow fiber membranes 16 in the region to be cleaned can be eliminated.
During the cleaning, the control unit 106 controls the flow rate sucked by the cleaning liquid recovery pipe liquid feeding unit 7p to be slightly larger than the flow rate of the cleaning liquid supplied from the connecting pipe 9. That is, the cleaning can be performed as follows: the cleaning liquid supplied from the cleaning liquid supply pipe 6 is caused to flow through the through channel 16h of the hollow fiber membrane 16 while maintaining the state in which the cleaning liquid is present in the region where the filtrate is present during the filtration concentration operation.
Before the cleaning, the cleaning liquid may be supplied from the cleaning liquid bag SB into the hollow space 12h of the trunk portion 12 by operating the cleaning liquid recovery pipe liquid feeding portion 7p and the connecting pipe liquid feeding portion 9p in a state where the cleaning liquid supply pipe 6 is opened by the flow rate adjustment mechanism 6c without separately performing the operation of filling the cleaning liquid into the region to be cleaned. Even in this case, the control unit 106 can fill the cleaning liquid into the hollow space 12h of the body portion 12 to the cleaning region by controlling the operations of the connecting pipe liquid feeding unit 9p and the cleaning liquid collecting pipe liquid feeding unit 7 p.
For example, the cleaning liquid supply pipe 6 is closed in advance by the flow rate adjustment mechanism 6c, and the upper port 11c is opened to the atmosphere, so that the connecting pipe liquid feeding portion 9p and the cleaning liquid recovery pipe liquid feeding portion 7p are operated. At this time, the flow rate of the cleaning liquid supplied from the connection pipe 9 is set to be larger than the flow rate sucked out by the cleaning liquid recovery pipe liquid feeding part 7 p. With this, the cleaning liquid can be filled into the hollow space 12h of the body portion 12 to the region to be cleaned over time. Then, the cleaning liquid supply pipe 6 is opened by the flow rate adjustment mechanism 6c to close the upper port 11c, and the flow rate of the cleaning liquid supplied from the connection pipe 9 is made smaller than the flow rate sucked out by the cleaning liquid recovery pipe liquid feeding portion 7p, so that the cleaning can be performed in a stable state. That is, the hollow fiber membranes 16 can be cleaned while maintaining the state in which the cleaning liquid is filled into the hollow space 12h of the trunk unit 12 up to the region to be cleaned.
The cleaning liquid in the hollow space 12h of the body portion 12 may be sucked out by a pump provided in a pipe connected to the upper port 11c until the cleaning liquid is filled in the hollow space 12h of the body portion 12. In this case, the cleaning liquid supply pipe 6 may be opened by the flow rate adjustment mechanism 6c while the flow rate of the cleaning liquid supplied from the connection pipe 9 is made larger than the flow rate sucked out by the cleaning liquid recovery pipe liquid feeding portion 7 p. Even in this case, if the cleaning liquid is filled into the hollow space 12h of the body portion 12 up to the region where cleaning is to be performed, cleaning can be performed in a stable state by closing the upper port 11c and making the flow rate of the cleaning liquid supplied from the connecting pipe 9 smaller than the flow rate sucked out by the cleaning liquid recovery pipe liquid feeding portion 7 p. That is, the hollow fiber membranes 16 can be cleaned while maintaining the state in which the cleaning liquid is filled into the hollow space 12h of the trunk unit 12 up to the region to be cleaned.
Even when the flow rate of the cleaning liquid supplied from the connection pipe 9 and the flow rate sucked out by the cleaning liquid recovery pipe liquid feeding section 7p are set to be the same flow rate, the through channels 16h of the hollow fiber membranes 16 up to the region where cleaning is performed can be filled with the cleaning liquid, and the through channels 16h of the hollow fiber membranes 16 up to the region where cleaning is performed can be filled with the cleaning liquid.
Although the cleaning liquid is filled in the cleaning region, the cleaning region is not necessarily limited to the region where the filtrate is present in the filtering and concentrating operation, and may be a region smaller than this region (for example, up to the height H3 in fig. 20) or a region larger than this region (for example, up to the height H2 in fig. 20). The entire hollow space 12h of the body portion 12 may be filled with the cleaning liquid. Further, as shown in fig. 20, in the case where the filtrate supply pipe 3 is connected to only the lower port 11c (filtrate discharge port 11c) of the pair of ports 11c, the entire inside of the hollow space 12H may be filled with the cleaning liquid up to a position where the cleaning liquid does not leak from the upper port 11c (up to the height of H2 in fig. 20).
In the above example, the case where the axial direction of the hollow fiber membranes 16 of the filter 10 is directed in the vertical direction was described, but the filter 10 may be arranged in a state where the axial direction of the hollow fiber membranes 16 is directed in a substantially horizontal direction. In this case, it is desirable to perform the cleaning operation so as to maintain the state of the entire hollow fiber membranes 16 immersed in the cleaning liquid (or after the cleaning liquid is filled into the hollow space 12h of the trunk portion 12 so that the entire hollow fiber membranes 16 are immersed in the cleaning liquid). Of course, depending on the position of the port 11c, the cleaning operation may be performed so as to maintain the state in which only a part of the hollow fiber membranes 16 is immersed in the cleaning liquid (or after the cleaning liquid is filled into the hollow space 12h of the trunk portion 12 so that a part of the hollow fiber membranes 16 is immersed in the cleaning liquid). The state in which only a part of the hollow fiber membranes 16 is immersed in the cleaning liquid corresponds to, for example: although the entire hollow fiber membrane 16 is not immersed in the cleaning liquid, the cleaning liquid does not leak from the port 11c to which the filtrate supply pipe 3 is not connected.
In the above example, the cleaning liquid is supplied from the connection pipe 9 connected to the filtrate supply pipe 3 into the hollow space 12h of the body portion 12, but the cleaning liquid may not be supplied through the filtrate supply pipe 3. For example, as shown in fig. 20, in a case where the filtrate supply pipe 3 is connected to only the lower port 11c (filtrate discharge port 11c) of the pair of ports 11c, the cleaning liquid may be supplied only from the upper discharge port 11 c. When the cleaning liquid is supplied into the hollow space 12h of the trunk unit 12 through the filtrate supply pipe 3, the cleaning liquid may be supplied to the concentrator 20 communicating with the filtrate supply pipe 3, and the cleaning liquid passing through the concentrator 20 may be supplied into the hollow space 12h of the trunk unit 12. In this case, when the filter 10 is cleaned, the concentrator 20 can be cleaned (for example, cleaning of the hollow fiber membrane of the filter 20).
For example, as shown in fig. 22, the cleaning liquid is supplied from the cleaning liquid bag SB to the concentrate discharge port 20b of the concentrator 20 directly or to the concentrator 20 via the concentrate pipe 4 communicating with the concentrate discharge port 20 b. Thus, the supplied cleaning liquid flows into the filtrate supply pipe 3 from the filtrate supply port 20a after passing through the concentrator 20, and is supplied into the hollow space 12h of the body 12 of the filter 10 from the filtrate supply pipe 3 through the filtrate discharge port 11 c. That is, the cleaning liquid supplied to the concentrator 20 can be used not only to clean the concentrator 20 but also to clean the filter 10.
In this case, the substance in the concentrator 20 flows through the hollow space 12h of the body portion 12, but the substance is a filtrate discharged from the filter 10 or a substance contained in the filtrate, and does not cause any problem even if it flows into the hollow space 12h of the body portion 12, and the filtrate diluted with the cleaning solution may be concentrated again.
Further, in the concentrator 20, the cleaning liquid may be supplied to the concentrator 20 through the waste liquid discharge port 20c instead of the concentrated liquid discharge port 20 b. If the cleaning liquid is supplied from the waste liquid discharge port 20c to the concentrator 20, the cleaning liquid can be made to flow in a direction perpendicular to the wall 16w of the hollow fiber membrane 16. That is, since the cleaning liquid can be supplied in the direction in which the cleaning liquid permeates the wall 16w of the hollow fiber membrane 16, there is an advantage that the clogging components accumulated in the concentrator 20 can be efficiently pushed and flowed to be cleaned.
< detailed description of concentrator 20 >
In the raw liquid treatment apparatus 1 according to embodiment 1, it is desirable that the respective pipes are connected to the concentrator 20 as follows. The connection between the concentrator 20 and each pipe to the concentrator 20 will be described below.
The concentrator 20 is supplied with the filtrate from the filter 10 and concentrates the filtrate. The concentrator 20 has substantially the same structure as the filter 10, and has a function of separating water from the filtrate to obtain a concentrated solution. That is, the concentrator 20 has a structure in which a moisture separating member having a function of separating moisture from the filtrate is housed inside, instead of the separating member of the filter 10. For example, a peritoneal fluid concentrator for CART, a filter for dialysis, a membrane type plasma component fractionator for double filtration plasma exchange therapy, and the like are used for the concentrator 20.
Specifically describing the concentrator 20, the concentrator 20 includes a filtrate supply port 20a that communicates with the filtrate discharge port 11c of the filter 10 via the filtrate supply pipe 3. That is, the liquid to be concentrated, i.e., the filtrate, is supplied from the filtrate supply port 20a to the concentrator 20.
The concentrator 20 also includes a waste liquid discharge port 20c for discharging liquid (separated liquid, waste liquid) separated from the filtrate, that is, moisture and the like. The waste liquid discharge port 20c communicates with the waste liquid bag DB via the waste liquid pipe 5. The concentrator 20 also includes a concentrated liquid outlet 20b through which the concentrated liquid is discharged. The concentrate discharge port 20b communicates with the concentrate bag CB via the concentrate pipe 4.
The concentrator 20 includes a moisture separation member. The moisture separating member has a function of allowing moisture to pass therethrough but not allowing useful components such as useful proteins contained in blood plasma to pass therethrough. If the concentrator 20 has the structure shown in fig. 5, the hollow fiber membrane bundle 15 of fig. 5 becomes a moisture separating member.
Therefore, if the filtrate is supplied from the filtrate supply port 20a into the concentrator 20, moisture is separated from the filtrate by the moisture separating member, and the separated moisture is discharged from the waste liquid discharge port 20c and supplied to the waste liquid bag DB through the waste liquid pipe 5. On the other hand, the concentrated solution in which a part of the water is removed and concentrated is discharged from the concentrated solution discharge port 20b, and the discharged concentrated solution is supplied to the concentrated solution bag CB through the concentrated solution pipe 4 (see fig. 1).
When the concentrator 20 includes a hollow fiber membrane as a moisture separation member, it has substantially the same configuration as the filter 10 (see fig. 5). That is, the following structure is provided: the water separator has a body section having a hollow space for accommodating a plurality of hollow fiber membranes (or a bundle of hollow fiber membranes obtained by bundling a plurality of hollow fiber membranes) as a water separating member, and a pair of header sections communicating both ends of the plurality of hollow fiber membranes. The pair of header portions has a port serving as the filtrate supply port 20a or the concentrated solution discharge port 20b, and the body portion has a port serving as the waste liquid discharge port 20 c. For example, the port 11a provided in the header portion 13 of fig. 5 serves as a filtrate supply port 20a, and the port 11b provided in the header portion 14 of fig. 5 serves as a concentrate discharge port 20 b. The port 11c provided in the body 12 of fig. 5 serves as a waste liquid discharge port 20 c. (refer to fig. 5).
In the case of the concentrator 20 having such a configuration, the pair of header portions (the pair of header portions 13 and 14 in fig. 5) correspond to the first liquid supply portion and the second liquid supply portion in the claims.
In the case where the concentrator 20 has substantially the same configuration as the filter 10, the removal of the clogging of the hollow fiber membranes and the cleaning of the flow paths in the hollow fiber membranes can be effectively performed by cleaning the same as the filter 10.
For example, in fig. 21, first, the filtrate supply pipe 3 is closed by the flow rate adjustment mechanism 3 c. Further, the operation of the concentrate pipe liquid sending part 4p is stopped in advance to close the concentrate pipe 4. When the hollow space of the body portion of the concentrator 20 is filled with the cleaning liquid, the upper port 20c of the 2 ports 20c is opened to the atmosphere. When the through-flow channels of the hollow fiber membranes are filled with the cleaning liquid, the portion of the filtrate supply pipe 3 on the hollow space side of the body portion with respect to the flow rate adjustment mechanism 3c is opened to the atmosphere. In this state, a cleaning liquid bag SB is connected to the other end of the waste liquid pipe 5 connected to the port 20c located below, instead of the waste liquid bag DB, and the cleaning liquid is supplied from the cleaning liquid bag SB into the hollow space of the body of the concentrator 20. Then, the cleaning liquid is filled into the hollow space of the body portion to a region where cleaning is performed, for example, a region where waste liquid is present in the filtering concentration operation.
After the cleaning liquid is filled in the above-described region, the filtrate supply pipe 3 is opened by the flow rate adjustment mechanism 3c, the connecting pipe liquid feeding portion 9p is operated to supply the cleaning liquid from the cleaning liquid bag SB connected to the connecting pipe 9 to the concentrator, and the concentrate pipe liquid feeding portion 4p is also operated. This allows the hollow fiber membranes and the hollow space of the trunk to be cleaned in the concentrator 20, and eliminates clogging of the hollow fiber membranes 16 in the region to be cleaned.
During the cleaning, the control unit 106 controls the flow rate sucked by the concentrated liquid pipe feeding unit 4p to be slightly larger than the flow rate of the cleaning liquid supplied from the connecting pipe feeding unit 9 p. That is, the cleaning can be performed as follows: the cleaning liquid supplied from the waste liquid pipe 5 is allowed to permeate the hollow fiber membranes 16 while maintaining the state where the cleaning liquid is present in the region where the concentrated liquid is present during the filtering concentration operation.
In a state where the cleaning liquid is supplied from the port serving as the waste liquid discharge port 20c into the hollow space 12h of the body portion 12 of the concentrator 20, the cleaning liquid may be supplied from the cleaning liquid bag SB into the hollow space 12h of the body portion 12 by operating the concentrated-pipe liquid feeding portion 4p and the connecting-pipe liquid feeding portion 9 p. Even in this case, the cleaning liquid can be filled into the hollow space 12h of the body portion 12 up to the region to be cleaned by controlling the operations of the connecting pipe liquid feeding portion 9p and the concentrated liquid pipe liquid feeding portion 4p by the control portion 106. In this case, the flow rate of the cleaning liquid supplied from the connecting pipe liquid feeding portion 9p is made larger than the flow rate sucked out from the concentrated pipe liquid feeding portion 4p until the cleaning liquid is filled in the region where cleaning is performed. Further, as long as the cleaning liquid is filled in the region to be cleaned, the control unit 106 may control the flow rate sucked by the concentrated-pipe liquid feeding unit 4p to be slightly larger than the flow rate of the cleaning liquid supplied from the connecting-pipe liquid feeding unit 9 p.
Although the cleaning liquid is filled in the region where cleaning is performed, the region where cleaning is performed is not necessarily limited to the region where the concentrated liquid is present in the filtering and concentrating operation, and may be a region smaller than this region (for example, up to the height H3 in fig. 20) or may be a region larger than this region. The entire hollow space 12h of the trunk portion may be filled with the cleaning liquid. Further, only in the case where the waste liquid pipe 5 is connected to the lower port 20c of the pair of ports 20c, the entire hollow space may be filled with the cleaning liquid up to a position where the cleaning liquid does not leak from the upper port 20c (up to the height of H2 in fig. 20).
In the above example, the following case is explained: the axial direction of the hollow fiber membranes of the concentrator 20 is directed vertically, and the concentration operation is performed in a state where the filtrate supply port 20a is positioned above the concentrated solution discharge port 20b, and the cleaning operation is performed in the same state. The concentrator 20 may be disposed in a state in which the axial direction of the hollow fiber membranes is oriented in a substantially horizontal direction. In this case, it is desirable to perform the cleaning operation so as to maintain the entire hollow fiber membrane in a state of being immersed in the cleaning liquid (or after the cleaning liquid is filled into the hollow space of the trunk portion so that the entire hollow fiber membrane is immersed in the cleaning liquid). Of course, depending on the position of the port 20c, the cleaning operation may be performed so as to maintain the state in which only a part of the hollow fiber membranes is immersed in the cleaning liquid (or after the cleaning liquid is filled into the hollow space of the trunk so that a part of the hollow fiber membranes is immersed in the cleaning liquid). The state in which only a part of the hollow fiber membrane is immersed in the cleaning liquid corresponds to, for example, the following states: although the entire hollow fiber membrane is not immersed in the cleaning liquid, the cleaning liquid does not leak from the port 20c to which the waste liquid pipe 5 is not connected.
< Loop construction of the raw liquid processing apparatus 1 according to embodiment 1 >
Next, a circuit configuration of the raw liquid processing apparatus 1 according to embodiment 1 will be described with reference to fig. 1.
Hereinafter, a case where the stock solution to be treated is a pleural effusion will be described as a representative example.
In the following description, a case will be described where the flow paths (feed flow path, filtrate supply flow path, concentrated liquid flow path, waste liquid flow path, cleaning liquid supply flow path, cleaning liquid recovery flow path, and connection flow path) described in the claims are formed of flexible or flexible tubes (feed tube 2, filtrate supply tube 3, concentrated liquid tube 4, waste liquid tube 5, cleaning liquid supply tube 6, cleaning liquid recovery tube 7, and connection tube 9). However, each flow path may be formed of a tube having no flexibility or softness (for example, a rigid plastic tube, a steel tube, a vinyl chloride tube, or the like), or an integrated circuit in which all or a part of the flow paths are integrally formed by resin molding or the like.
Further, since the raw liquid treatment apparatus 1 according to embodiment 1 includes the pair of roller pumps 110 and 120, the following description will be made on the assumption that each flow path is formed of a flexible or flexible pipe and the roller pump is used as a liquid feeding portion of each flow path. However, in the raw liquid processing apparatus 1 according to embodiment 1, the liquid feeding unit is not limited to the roller pump, and various apparatuses capable of feeding the liquid in each flow path can be used. The liquid feeding portion may be appropriately selected depending on the material of the tube constituting each flow path and the liquid flowing through the flow path. For example, a liquid delivery pump, a diaphragm pump, or the like may be used as the liquid delivery unit. Further, since the roller pump performs a pinching function (a function of closing the flow path to prevent the liquid from flowing) when the operation is stopped, no tool having the pinching function is provided in the flow path provided with the liquid feeding portion in the following description. However, when a device that does not exhibit a clamping function even when the operation is stopped or a device that does not exhibit a clamping function is used as the liquid feeding unit, an instrument having a clamping function (for example, a clamp, a clip, an electromagnetic valve, or the like) may be separately provided in the flow path in which the liquid feeding unit is provided, and the instrument having a clamping function may be caused to exhibit a clamping function when the operation of the liquid feeding unit is stopped. When the solenoid valve is used, the operation of the liquid feeding unit can be stopped by the control unit 106 and the clamping function can be performed at the same time or at a desired timing.
Since the operation of each liquid feeding unit is controlled by the control unit 106, the following description will be made on the premise that each liquid feeding unit is controlled by the control unit 106.
< schematic configuration of the raw liquid treatment apparatus 1 according to embodiment 1 >
First, a schematic configuration of the raw liquid processing apparatus 1 according to embodiment 1 will be described.
In fig. 1, reference character UB denotes a raw liquid bag for containing raw liquid, that is, raw liquid such as pleural effusion and abdominal dropsy drawn from the chest or abdomen. Further, reference sign CB denotes a concentrate bag which accommodates a concentrate obtained by filtering and concentrating the stock solution. Further, reference numeral DB denotes a waste liquid bag that accommodates waste liquid (i.e., moisture) separated from the concentrated liquid. Further, reference numeral SB denotes a washing solution bag containing a washing solution such as physiological saline or an infusion solution (extracellular fluid), and reference numeral FB denotes a washing solution recovery bag for recovering the washing solution.
As shown in fig. 1, in a raw liquid processing apparatus 1 according to embodiment 1, a raw liquid bag UB is connected to a filter 10 via a liquid feed pipe 2. The feed pipe 2 is a pipe for supplying the raw liquid in the raw liquid bag UB to the filter 10. The liquid supply tube 2 is provided with a liquid supply tube liquid supply portion 2p for supplying liquid in the liquid supply tube 2.
The filter 10 filters the raw liquid to generate a filtrate. The filter 10 is connected to a concentrator 20 via a filtrate supply line 3. The filtrate supply line 3 is a line for supplying the filtrate generated by the filter 10 to the concentrator 20. The filtrate supply pipe 3 is provided with a flow rate adjusting mechanism 3c such as a clamp, a clip, or an electromagnetic valve for stopping or opening the flow of the liquid in the filtrate supply pipe 3.
One end of a connecting pipe 9 is connected to the filtrate supply pipe 3 at a portion between the filter 10 and the flow rate adjusting mechanism 3 c. The connecting pipe 9 is provided with a connecting pipe liquid feeding portion 9p for feeding the liquid in the connecting pipe 9.
A cleaning liquid bag SB is connected to the filter 10 via the cleaning liquid supply pipe 6. The cleaning liquid supply pipe 6 is a pipe for supplying the cleaning liquid from the cleaning liquid bag SB to the filter 10. The cleaning liquid supply pipe 6 is provided with a flow rate adjusting mechanism 6c such as a clamp, a clip, or an electromagnetic valve for stopping or opening the flow of the liquid in the cleaning liquid supply pipe 6.
Further, a cleaning liquid recovery bag FB for recovering the cleaning liquid that has cleaned the filter 10 is connected to the filter 10 via a cleaning liquid recovery pipe 7. The cleaning liquid recovery pipe 7 is provided with a cleaning liquid recovery pipe liquid feeding portion 7p for feeding the liquid in the cleaning liquid recovery pipe 7.
The cleaning liquid recovery pipe 7 may be connected to the filter 10 via the liquid supply pipe 2, or may be directly connected to the filter 10.
The concentrator 20 produces a concentrated solution in which the filtrate is concentrated. In the concentrator 20, a concentrate bag CB is connected via a concentrate pipe 4. The concentrate pipe 4 is a pipe for supplying the concentrate concentrated by the concentrator 20 to the concentrate bag CB. The concentrate pipe 4 is provided with a concentrate pipe liquid sending part 4p for sending the liquid in the concentrate pipe 4. Further, a waste liquid pipe 5 may be provided with a waste liquid pipe sending part 5p instead of the concentrate liquid pipe sending part 4p (see fig. 4). Even in this case, the same function as in the case where the concentrate-pipe liquid feeder 4p is provided in the concentrate pipe 4 can be achieved by reducing the liquid feeding amount of the waste liquid by the waste-pipe liquid feeder 5p under the condition that the liquid feeding amount of the concentrate is increased by the concentrate-pipe liquid feeder 4p, and increasing the liquid feeding amount of the waste liquid by the waste-pipe liquid feeder 5p under the condition that the liquid feeding amount of the concentrate is reduced by the concentrate-pipe liquid feeder 4 p. Hereinafter, a case where the concentrate pipe liquid sending part 4p is provided in the concentrate pipe 4 will be described.
Further, a waste liquid bag DB is connected to the concentrator 20 via a waste liquid pipe 5. The waste liquid pipe 5 is a pipe for supplying waste liquid (moisture) separated from the concentrated liquid by the concentrator 20 to the waste liquid bag DB.
With the above-described configuration, in the raw liquid treatment apparatus 1 according to embodiment 1, if the raw liquid is supplied from the raw liquid bag UB to the filter 10 through the liquid feed pipe 2, the raw liquid can be filtered by the filter 10 to generate a filtrate. Then, if the generated filtrate is supplied to the concentrator 20 through the filtrate supply pipe 3, a concentrated liquid can be generated by the concentrator 20, and the concentrated liquid can be recovered to the concentrated liquid bag CB through the concentrated liquid pipe 4.
On the other hand, if the cleaning liquid is supplied to the filter 10 from the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6, the filter 10 can be cleaned by the cleaning liquid. Further, if the cleaning solution bag SB is connected to the concentrate pipe 4 instead of the concentrate bag CB, the concentrator 20 can be cleaned by the cleaning solution (see fig. 2).
In addition, in the case where the cleaning solution bag SB is connected to the concentrate pipe 4 instead of the concentrate bag CB, the cleaning solution after cleaning the concentrator 20 can be supplied to the filter 10 through the filtrate supply pipe 3. That is, the concentrator 20 and the filter 10 may be cleaned at the same time.
The operation of the raw liquid treatment apparatus 1 according to embodiment 1 will be described below.
< preparation for cleaning operation >
As shown in fig. 2, in the preparatory cleaning operation of the raw liquid treatment apparatus 1 according to embodiment 1, a cleaning liquid bag SB is connected to the other end of the concentrate pipe 4 in place of the concentrate bag CB, and a cleaning liquid recovery bag FB is connected to the other end of the waste pipe 5 in place of the waste bag DB. The other end of the waste liquid pipe 5 may be connected to the waste liquid bag DB, or the other end of the waste liquid pipe 5 may be simply disposed in a bucket or the like.
Further, a cleaning liquid recovery bag FB is also connected to the other end of the liquid feed pipe 2 instead of the raw liquid bag UB. The other end of the liquid supply tube 2 may be connected to the waste liquid bag DB, or the other end of the liquid supply tube 2 may be simply disposed in a tub or the like.
The other end of the connection pipe 9 is also connected to the cleaning liquid recovery bag FB. The other end of the connecting pipe 9 may be connected to the waste liquid bag DB, or the other end of the connecting pipe 9 may be simply disposed in a tub or the like.
Next, the flow rate adjustment mechanism 3c and the flow rate adjustment mechanism 6c are opened to allow the cleaning liquid to flow through the filtrate supply pipe 3 and the cleaning liquid supply pipe 6.
In the above state, the concentrate pipe liquid feeding portion 4p is operated so that the cleaning liquid flows from the cleaning liquid bag SB connected to the concentrate pipe 4 to the concentrator 20, and the connecting pipe liquid feeding portion 9p is operated so that the cleaning liquid flows from the concentrator 20 (i.e., the filtrate supply pipe 3) to the cleaning liquid recovery bag FB connected to the connecting pipe 9. Thereby, the cleaning liquid is supplied from the cleaning liquid bag SB connected to the concentrate pipe 4 to the concentrator 20 through the concentrate pipe 4. The supplied cleaning liquid passes through the concentrator 20, and is then collected into the cleaning liquid collection bag FB connected to the connection pipe 9 through the filtrate supply pipe 3 and the connection pipe 9. In addition, a part of the cleaning liquid is recovered through the waste liquid pipe 5 to the cleaning liquid recovery bag FB connected to the other end of the waste liquid pipe 5.
The connection pipe liquid feeding unit 9p is operated so that the cleaning liquid flows from the concentrator 20 to the cleaning liquid recovery bag FB connected to the connection pipe 9, and the liquid feeding pipe liquid feeding unit 2p is operated so that the cleaning liquid flows from the filter 10 to the cleaning liquid recovery bag FB connected to the liquid feeding pipe 2. Thereby, the cleaning liquid is supplied from the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6 to the filter 10 through the cleaning liquid supply pipe 6. After the supplied cleaning liquid passes through the filter 10, a part of the cleaning liquid is collected into the cleaning liquid collecting bag FB connected to the connecting pipe 9 through the filtrate supply pipe 3 and the connecting pipe 9, and a part of the cleaning liquid is collected into the cleaning liquid collecting bag FB connected to the liquid supply pipe 2 through the liquid supply pipe 2. Further, by operating the cleaning liquid recovery pipe liquid feeding portion 7p, a part of the cleaning liquid supplied to the filter 10 can be also made to flow to the cleaning liquid recovery pipe 7.
This enables the cleaning liquid to flow through the filter 10, the concentrator 20, and all the pipes, and thus the entire raw liquid treatment apparatus 1 according to embodiment 1 can be cleaned.
In fig. 2, the cleaning liquid is sucked out of the filter 10 by operating the liquid supply pipe liquid feeding unit 2p and the cleaning liquid recovery pipe liquid feeding unit 7p, and the flow of the cleaning liquid is generated in the filter 10, thereby cleaning the inside of the filter 10. However, the cleaning liquid may be pushed into the filter 10 to generate a flow of the cleaning liquid in the filter 10, thereby cleaning the inside of the filter 10.
For example, in fig. 2, a cleaning liquid supply pipe liquid feeding portion 6p is provided in the cleaning liquid supply pipe 6 instead of the flow rate adjusting mechanism 6c, and a cleaning liquid recovery pipe 7 is provided with a flow rate adjusting mechanism 7c instead of the cleaning liquid recovery pipe liquid feeding portion 7 p. Then, the cleaning liquid recovery pipe 7 is opened by the flow rate adjustment mechanism 7c, and the cleaning liquid supply pipe liquid feeding portion 6p is operated so that the cleaning liquid flows from the cleaning liquid bag SB toward the filter 10 in the cleaning liquid supply pipe 6. This can push the cleaning liquid into the filter 10, and the flow of the cleaning liquid is generated in the filter 10, so that the inside of the filter 10 can be cleaned with the cleaning liquid. In this case, the liquid feed pipe liquid feed portion 2p of the liquid feed pipe 2 may be operated to suck the cleaning liquid from the filter 10 so that the cleaning liquid flows through the liquid feed pipe 2. Further, only the cleaning liquid may be allowed to flow through the cleaning liquid recovery pipe 7 without operating the liquid supply pipe liquid feeding portion 2 p.
< filtration and concentration operation >
When the preparation cleaning operation is finished, the filtration and concentration operation is performed.
As shown in fig. 1, in the filtering and concentrating operation of the raw liquid processing apparatus 1 according to embodiment 1, from a state in which the cleaning operation is prepared (see fig. 2), the concentrate bag CB is connected to the concentrate pipe 4 instead of the cleaning liquid bag SB, and the waste liquid bag DB is connected to the waste pipe 5 instead of the cleaning liquid recovery bag FB.
On the other hand, a raw liquid bag UB is connected to the liquid supply pipe 2 instead of the cleaning liquid recovery bag FB.
The flow rate adjusting mechanism 3c maintains a state in which the liquid can flow in the filtrate supply pipe 3, while the flow rate adjusting mechanism 6c closes the flow rate adjusting mechanism so that the liquid cannot flow in the cleaning liquid supply pipe 6. In addition, the cleaning liquid recovery pipe liquid feeding portion 7p and the connecting pipe liquid feeding portion 9p are not operated and function as a jig.
In the above state, the feed pipe liquid sending part 2p is operated so that the raw liquid flows from the raw liquid bag UB connected to the feed pipe 2 to the filter 10, and the concentrate pipe liquid sending part 4p is operated so that the concentrate flows from the concentrator 20 to the concentrate bag CB connected to the concentrate pipe 4.
Thereby, the raw liquid is supplied from the raw liquid bag UB to the filter 10 through the liquid feed pipe 2. The supplied raw liquid is filtered by the filter 10, and the generated filtrate is supplied to the concentrator 20 through the filtrate supply pipe 3. Then, the filtrate supplied to the concentrator 20 is concentrated by the concentrator 20, and the resulting concentrated solution is collected into the concentrated solution bag CB through the concentrated solution pipe 4. On the other hand, the moisture separated from the concentrated solution is recovered to the waste liquid bag DB through the waste liquid pipe 5.
< operation of filtration and concentration >
Here, in the filtering and concentrating operation, the operation of the feed pipe liquid feeding part 2p and the concentrate pipe liquid feeding part 4p is controlled so that the concentration ratio falls within a predetermined range. However, the operation of the feed pipe liquid feeder 2p and the concentrate pipe liquid feeder 4p, that is, the flow rates of the liquid flowing through the feed pipe liquid feeder 2p and the concentrate pipe liquid feeder 4p may be controlled by the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure, as described below. This enables filtration and concentration to be performed by effectively utilizing the capabilities of the filter 10 and the concentrator 20, and therefore, the time required for producing a concentrated solution can be shortened, and the efficiency of the concentration operation can be improved.
Hereinafter, the operation of filtering and concentrating by controlling the operations of the feed pipe liquid feeding part 2p and the concentrate pipe liquid feeding part 4p by the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure will be described.
The inter-filter-membrane differential pressure is a differential pressure between the liquid supply side and the liquid discharge side of the filter member (hollow fiber membrane, etc.) of the filter 10. For example, if the filter member of the filter 10 is the hollow fiber membrane 16, the difference between the pressure in the through channel 16h of the hollow fiber membrane 16 and the pressure in the hollow space 12h of the body 12 corresponds to the inter-filter-membrane differential pressure.
The inter-membrane pressure difference between the concentrators means a pressure difference between the liquid supply side and the liquid discharge side of a moisture separation member (hollow fiber membrane or the like) of the concentrator 20. For example, if the filter member of the concentrator 20 is a hollow fiber membrane, the difference between the pressure in the through channel of the hollow fiber membrane and the pressure in the hollow space of the body corresponds to the inter-concentrator-membrane differential pressure.
In addition, the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure can be calculated by measuring the tube internal pressure connected to the filter 10 and the concentrator 20. For example, if pressure gauges are provided in the feed pipe 2 and the filtrate supply pipe 3 in advance and the signals are supplied to the control unit 106, the control unit 106 can calculate the differential pressure between the filter membranes. As shown in fig. 1, the control unit 106 can calculate the differential pressure between the filter membranes even when a pressure gauge is provided in the port 11c to which the filtrate supply pipe 3 is not connected (or a pipe connected to the port 11 c). Further, if pressure gauges are provided in the filtrate supply pipe 3 and the waste liquid pipe 5 in advance and the signals are supplied to the control unit 106, the control unit 106 can calculate the inter-membrane pressure difference of the concentrator. In addition, in the case where there is a port 20c to which the waste liquid pipe 5 is not connected, the control unit 106 can calculate the inter-membrane pressure difference of the concentrator even if a pressure gauge is provided in the port 20c (or a pipe connected to the port 20 c).
In the filter 10 and the concentrator 20, if either the liquid feed side or the liquid discharge side is in a state of being opened to the atmosphere, the control unit 106 can calculate the filter-membrane differential pressure and the concentrator-membrane differential pressure even if only the internal pressures of the tubes communicating with the side not opened to the atmosphere, out of the liquid feed side and the liquid discharge side, are measured. In other words, the control unit 106 can control the operation of the liquid feeding unit by using only the tube internal pressure communicated with the side not opened to the atmosphere instead of the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure. For example, if a tube connected to the filter 10 and the concentrator 20 is connected to a bag and the tube is not closed by the liquid feeding unit or the flow rate adjustment mechanism, the tube can be considered to be in a state of being nearly open to the atmosphere. In the state of fig. 1, the liquid supply tube 2 connected to the raw liquid bag UB of the tubes 2 and 3 connected to the filter 10 can be regarded as being open to the atmosphere. Further, the waste liquid pipe 5 connected to the waste liquid bag DB among the pipes 3 and 5 connected to the concentrator 20 can be regarded as being open to the atmosphere. Thus, if the state is shown in fig. 1, the controller 106 can control the operation of the liquid feeder by using only the tube internal pressure of the filter supply tube 3.
The flow rate of the liquid flowing through the liquid feed pipe 2 or the filtrate supply pipe 3 may be estimated from the operation of the liquid feed pipe liquid feed portion 2p and the concentrate pipe liquid feed portion 4p, or the flow rate may be directly measured by providing a flow meter in the liquid feed pipe 2 or the liquid feed pipe liquid feed portion 2p, and the concentrate pipe 4 or the concentrate pipe liquid feed portion 4 p.
< description of operation of filtration and concentration Using differential pressure between membranes of Filter and differential pressure between membranes of concentrator >
When filtration and concentration operations are performed using the pressure difference between the membranes of the filter and the pressure difference between the membranes of the concentrator, an allowable pressure difference is set in advance. That is, the differential pressures (allowable differential pressures) that can be allowed for the filter 10 and the concentrator 20 are set in accordance with the filter 10 and the concentrator 20, respectively. The allowable differential pressure may have a predetermined magnitude or may be set to a specific value. In the following description, the allowable differential pressure is typically a case having a predetermined width.
In addition, when performing filtration and concentration operations using the pressure difference between the filter membranes and the pressure difference between the concentrator membranes, it is desirable to set the allowable flow rate in advance. That is, it is desirable to set the flow rate (allowable flow rate) that can be allowed for the raw liquid in the feed pipe 2. The allowable flow rate may have a predetermined magnitude or may be set to a specific value. The allowable flow rate does not necessarily have to be set. However, if the flow rate of the raw liquid in the feed pipe 2 is too small, the time taken for the filtration and concentration becomes too long. Therefore, it is desirable to set the allowable flow rate in advance in order to prevent the treatment time of the raw liquid from increasing.
Further, when performing filtration and concentration operations using the pressure difference between the filter membranes and the pressure difference between the concentrator membranes, it is desirable to set the allowable concentration ratio in advance. That is, it is desirable to set the ratio of the flow rate of the raw liquid in the feed pipe 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4 (allowable concentration ratio). The allowable concentration ratio may have a predetermined width or may be set to a specific value. The allowable concentration ratio is not necessarily set. However, if the concentration ratio, which is the ratio of the flow rate of the raw liquid in the feed pipe 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4, is too low (i.e., the flow rate of the concentrated liquid becomes too large), the concentration efficiency deteriorates. Further, the amount of the concentrated solution increases, and a large amount of the filtered concentrated solution is re-intravenously fed, which may cause an increase in blood pressure, an increase in heart failure, and an increase in respiratory failure. Therefore, when the amount of the concentrate becomes excessive, it is necessary to add a re-concentration process, and the re-concentration process takes time. In the case of re-concentrating the concentrated solution, since the re-concentration process takes time, the total time for processing the raw solution becomes long. Therefore, in order to prevent the concentration ratio from being excessively decreased, it is desirable to set an allowable concentration ratio in advance.
At the start of filtration and concentration, the feed pipe liquid feed unit 2p is operated to increase the amount of the raw liquid fed to the filter 10. At this time, the concentrate pipe liquid feeding portion 4p is operated so that the concentrate has a predetermined concentration ratio in accordance with the flow rate of the raw liquid in the liquid feeding pipe 2. For example, when a concentrated solution having a concentration ratio of 10 times is to be produced, the operation of the concentrated solution pipe feed portion 4p may be adjusted so that the flow rate of the concentrated solution flowing through the concentrated solution pipe 4 becomes 1/10 of the flow rate of the raw solution flowing through the liquid feed pipe 2. In addition, instead of the concentration ratio of the concentrated liquid, the operation of the concentrated liquid pipe feed portion 4p may be adjusted so that the inter-membrane differential pressure of the concentrator becomes a set value within the allowable differential pressure (or maintained within the allowable differential pressure), or the inter-membrane differential pressure of the concentrator may become a set value within the allowable differential pressure (or maintained within the allowable differential pressure) while the concentrated liquid is maintained at a predetermined concentration ratio. While the amount of the stock solution sent to the filter 10 is increased, the operation of the concentrate pipe liquid sending part 4p is controlled so as to be in any of the above-described states.
When the filtration concentration advances, clogging of the filter 10 and the concentrator 20 gradually occurs. Thereby, the inter-membrane differential pressure of the filter and the inter-membrane differential pressure of the concentrator increase. However, the feed pipe liquid feeding portion 2p is operated to increase the amount of the raw liquid fed to the filter 10 until the inter-membrane differential pressure between the filter and the concentrator is within the allowable differential pressure.
< first method >
The amount of the feed liquid of the raw liquid to the filter 10 is increased until the differential pressure between the filter membranes is within the allowable differential pressure of the filter 10. When the filter membrane-to-membrane differential pressure falls within the allowable differential pressure of the filter 10, the feed pipe liquid feed unit 2p is controlled so as to maintain the flow rate of the raw liquid in the feed pipe 2 at a flow rate at which the filter membrane-to-membrane differential pressure falls within the allowable differential pressure of the filter 10. On the other hand, the concentrate pipe liquid feeding portion 4p is operated to adjust the flow rate of the concentrate flowing through the concentrate pipe 4.
Here, when the filter membrane-to-membrane differential pressure is within the allowable differential pressure of the filter 10, the operation of the feed pipe feed unit 2p is controlled so as to maintain the feed amount of the filtrate to the concentrator 20, in other words, the feed amount of the raw liquid to the filter 10. This enables the filtration by the filter 10 and the concentration by the concentrator 20 to be maintained in a predetermined state. Further, if the amount of liquid to be fed to the filter 10 is increased or decreased based on the value of the inter-membrane differential pressure between the filters, the amount of liquid to be fed to the filter 10 can be increased while maintaining the inter-membrane differential pressure between the filters within the allowable differential pressure of the filter 10. That is, there is a possibility that the efficiency of the filtration and concentration operation can be improved. In particular, if the inter-membrane differential pressure of the filter is maintained at the maximum allowable differential pressure PM of the filter 10, the amount of the stock solution sent to the filter 10 can be maximized, and therefore the effect of shortening the time for the filtration operation can be further improved.
On the other hand, when the filter inter-membrane differential pressure becomes larger than the allowable differential pressure (maximum allowable differential pressure PM) of the filter 10, the operation of the liquid feeding pipe liquid feeding section 2p is controlled so that the amount of the raw liquid fed to the filter 10 decreases. If the hollow fiber membranes 16 and the like are clogged even if the amount of the raw liquid fed to the filter 10 is constant, the pressure difference between the filter membranes may increase and the filtration may not be continued. However, if the amount of the raw liquid fed to the filter 10 is reduced, the pressure difference between the filter membranes can be reduced, and therefore the filtering operation can be continued even if the filter 10 is clogged. Further, since the amount of the raw liquid fed to the filter 10 is reduced, clogging of the hollow fiber membranes 16 and the like may be slightly reduced, and therefore, there is a possibility that the filtering operation can be continued easily and the time for the filtering operation can be shortened. In particular, when the filter-membrane differential pressure becomes greater than the maximum allowable differential pressure PM of the filter 10, the effect of reducing clogging of the hollow fiber membranes and the like can be enhanced by stopping the supply of the raw liquid to the filter 10 once and restarting the supply after a certain period of time.
When the inter-membrane differential pressure of the filter becomes smaller than the minimum allowable differential pressure PL of the filter 10 by, for example, reducing the amount of the raw liquid fed to the filter 10, the operation of the liquid feed pipe liquid feed unit 2p is controlled so that the amount of the raw liquid fed to the filter 10 increases. This can increase the filtration amount of the filter 10, and therefore, the time required for the filtration operation can be shortened. Further, if the amount of the feed liquid of the raw liquid to the filter 10 is increased until the inter-filter-membrane differential pressure falls within the allowable differential pressure of the filter 10, particularly the maximum allowable differential pressure PM, the filtering capacity of the filter 10 can be effectively used, and therefore the effect of shortening the time for the filtering operation can be further improved.
When the amount of the raw liquid supplied to the filter 10 is reduced when the filter membrane-to-membrane differential pressure becomes larger than the maximum allowable differential pressure PM of the filter 10, the amount of the raw liquid supplied may be gradually reduced or may be reduced in a stepwise manner. When the filter-membrane differential pressure becomes greater than the maximum allowable differential pressure PM (PM in fig. 24) of the filter 10, the flow of the raw liquid to the filter 10 may be stopped for a certain period of time and then the flow of the raw liquid to the filter 10 may be started (see fig. 24). In this case, the amount of the feed liquid of the raw liquid to the filter 10 may be adjusted while the pressure difference between the filter membranes is checked. For example, as shown in pattern 1 of fig. 24, when the liquid feeding of the raw liquid to the filter 10 is started after stopping the liquid feeding of the raw liquid to the filter 10 for a certain period of time, the liquid feeding is started at a flow rate of about 1/2 of the maximum allowable flow rate LM first, and the inter-filter-membrane differential pressure at that time is confirmed. If the inter-filter-membrane differential pressure is smaller than the minimum allowable differential pressure PL (PL in fig. 24) in this state, the flow rate around 1/2, which is the difference between the current flow rate and the maximum allowable flow rate LM, is increased and the inter-filter-membrane differential pressure at this time is confirmed. If the inter-filter-membrane differential pressure is still smaller than the minimum allowable differential pressure PL in this state, the flow rate around 1/2 of the difference between the current flow rate and the maximum allowable flow rate LM is further increased and the inter-filter-membrane differential pressure at this time is confirmed. This operation is repeated, and if the filter membrane-to-membrane differential pressure is equal to or higher than the minimum allowable differential pressure PL and equal to or lower than the maximum allowable differential pressure PM of the filter 10 (or if the maximum allowable differential pressure PM is reached), the increase in the flow rate is stopped. Even if the inter-filter-membrane differential pressure is within the allowable differential pressure of the filter 10, if the maximum allowable flow rate LM is not reached, the amount of the feed of the raw liquid to the filter 10 can be increased by the same method until the maximum allowable flow rate LM is reached while the inter-filter-membrane differential pressure is confirmed.
When the amount of the raw liquid supplied to the filter 10 is increased when the filter-membrane differential pressure becomes smaller than the minimum allowable differential pressure PL of the filter 10, the amount of the raw liquid supplied may be gradually increased. For example, the amount of the raw liquid to be fed to the filter 10 may be increased by the same method as the above-described method of increasing the flow rate, that is, the method of increasing the flow rate from the state where the feeding of the raw liquid to the filter 10 is stopped for a certain period of time.
In addition, while the amount of the raw liquid fed to the filter 10 is maintained in a state where the filter-membrane differential pressure is maintained within the allowable differential pressure of the filter 10, the amount of the raw liquid fed to the filter 10 may be increased until the maximum allowable flow rate LM is reached when the flow rate is smaller than the maximum allowable flow rate LM.
Even if the inter-membrane differential pressure of the filter becomes equal to or greater than the minimum allowable differential pressure PL of the filter 10, if the amount of the raw liquid fed to the filter 10 does not reach the minimum allowable flow rate LL (pattern 3 in fig. 24), it is determined that clogging of the hollow fiber membranes 16 or the like has occurred, and the filtration concentration operation is stopped and the operation is shifted to the cleaning operation.
Further, the concentrate pipe liquid feeding portion 4p can be controlled based on the inter-membrane differential pressure of the concentrator as follows, in a state where the inter-membrane differential pressure of the filter 10 is within the allowable differential pressure of the filter and the flow rate of the raw liquid in the liquid feeding pipe 2 is maintained at a flow rate in a state where the inter-membrane differential pressure of the filter reaches the allowable differential pressure of the filter 10.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the concentrate pipe liquid feeding unit 4p is operated so that the amount of the concentrated liquid fed to the concentrated liquid bag CB is reduced. That is, the operation of the concentrate-pipe liquid sending part 4p is controlled so that the concentration of the concentrate is increased.
< step 2>
Then, the amount of the concentrated solution sent to the concentrated solution bag CB is reduced until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. If the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20, the concentrate pipe liquid sending part 4p is controlled so that the flow rate of the concentrate in the concentrate pipe 4 is maintained at a flow rate at which the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20.
< step 3>
When the pressure difference between the concentrator membranes becomes larger than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the concentrate pipe liquid feeding part 4p is controlled so that the amount of the concentrated liquid fed to the concentrated liquid bag CB increases. Further, although the concentration ratio decreases as the amount of the concentrated liquid fed increases, the operation of the concentrated liquid pipe feeding portion 4p is controlled so that the concentration ratio decreases (the concentration of the concentrated liquid becomes low) while the allowable concentration ratio is satisfied.
When the liquid feed amount of the concentrated solution is increased to maintain the pressure difference between the membranes of the concentrator within the allowable pressure difference and the concentration ratio becomes smaller than the allowable concentration ratio, the following method (second method) can be used to cope with this.
When the amount of the concentrated liquid fed to the concentrated liquid bag CB increases, the inter-membrane differential pressure of the concentrator decreases, and therefore, when the inter-membrane differential pressure of the concentrator becomes lower than the minimum allowable differential pressure of the concentrator 20, the concentrated liquid pipe feeding portion 4p is operated again, so that the amount of the concentrated liquid fed to the concentrated liquid bag CB decreases.
That is, the above steps 1 to 3 are repeated while the inter-membrane differential pressure of the filter is within the allowable differential pressure of the filter 10. This method can ensure the maximum filtration flow rate (i.e., the maximum allowable flow rate LM) and the maximum concentration ratio, which are not possible to achieve when the amount of liquid fed to the filter 10 and the concentrate bag CB is constant, according to the membrane area and the clogging state of the filtration membranes of the filter 10 and the concentrator 20, or according to the state of the raw liquid (the concentration of a substance causing clogging of the filter and the concentrator, the concentration of a collected useful substance, the viscosity of the liquid, and the like). That is, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated solution from a raw solution can be shortened, and the re-concentration operation can be avoided or the time required for the re-concentration operation can be shortened.
Further, if the operation is performed as described above, at the start of the filtration concentration, the cleaning liquid filled in the filter 10, the concentrator 20, and the circuit, and the cleaning liquid in the filter 10 and the circuit immediately after the cleaning of the filter 10 can be removed as the waste liquid of the concentrator 20 in a short time. That is, dilution of the concentrated solution by the cleaning solution at the start and immediately after the cleaning of the filter as described above can be effectively prevented.
The above method (first method) is preferably employed when the maximum allowable differential pressure PM of the filter membrane-to-membrane differential pressure is larger than the maximum allowable differential pressure of the concentrator membrane-to-membrane differential pressure, but is not limited to this condition. The maximum allowable differential pressure PM of the filter membrane-to-membrane differential pressure can be used when it is smaller than the maximum allowable differential pressure of the concentrator membrane-to-membrane differential pressure.
In addition, when the filter membrane-to-membrane differential pressure is greater than the maximum allowable differential pressure PM, when the filter membrane-to-membrane differential pressure is less than the minimum allowable differential pressure PL, and when the feed rate of the raw liquid to the filter 10 is constant regardless of the filter membrane-to-membrane differential pressure, the above steps 1 to 3 may be repeated to adjust the feed rate of the concentrated liquid to the concentrator 20.
< second method >
In the first method, the flow rate of the concentrate in the concentrate pipe 4 can be adjusted based on the inter-concentrator-membrane differential pressure, and the flow rate of the raw liquid in the feed pipe 2 can be adjusted based on the inter-concentrator-membrane differential pressure as described below.
In addition, although the following description will be made of the case where the flow rate of the raw liquid in the feed pipe 2 is adjusted based on the pressure difference between the membranes of the concentrator, steps 1 to 3 of the first method may be performed together with the adjustment of the flow rate of the raw liquid in the feed pipe 2. That is, the flow rate of the raw liquid in the feed pipe 2 may be adjusted based on the pressure difference between the concentrator membranes, and the flow rate of the concentrated liquid in the concentrated liquid pipe, that is, the concentration ratio of the concentrated liquid may be adjusted.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the feed pipe liquid feed unit 2p is operated so that the amount of feed of the raw liquid to the filter 10 increases. That is, the operation of the feed pipe liquid feed portion 2p is controlled so as to increase the amount of filtrate to be fed to the concentrator 20. Further, the concentrate pipe liquid feeding portion 4p may be operated so that the amount of the raw liquid fed to the filter 10 is increased and the concentration of the concentrated liquid is increased.
< step 2>
Then, the amount of filtrate produced (in other words, the amount of feed liquid of the raw liquid to the filter 10) to be fed to the concentrator 20 is increased until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20 (i.e., the minimum allowable differential pressure is higher and the maximum allowable differential pressure is lower). Then, if the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20, the operation of the feed pipe liquid feeding portion 2p is controlled so that the flow rate of the raw liquid in the feed pipe 2 is maintained at a flow rate at which the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20. In this case, the flow rate of the raw liquid in the liquid supply pipe 2 is deviated from the flow rate in a state where the differential pressure between the filter membranes is within the allowable differential pressure of the filter 10, but it is desirable to maintain the flow rate of the raw liquid within a range of the allowable flow rate (not less than the minimum allowable flow rate and not more than the maximum allowable flow rate). The concentrate pipe liquid feeding unit 4p may be operated so that the flow rate of the concentrate in the concentrate pipe 4 is maintained at a flow rate in a state where the inter-membrane differential pressure of the concentrator is within the allowable differential pressure of the concentrator 20.
< step 3>
When the pressure difference between the concentrator membranes becomes larger than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like immediately after that, the operation of the feed pipe liquid feeding part 2p is controlled so that the flow rate of the raw liquid in the feed pipe 2 is reduced. That is, the operation of the feed pipe liquid feeding portion 2p is controlled so that the amount of generated filtrate fed to the concentrator 20 is reduced. In this case, the flow rate of the raw liquid in the feed pipe 2 is also deviated from the flow rate in a state where the differential pressure between the filter membranes is within the allowable differential pressure of the filter 10, but it is desirable to maintain the flow rate of the raw liquid within a range of the allowable flow rate. Further, the concentrate pipe liquid sending part 4p may be operated so that the concentration ratio is decreased (so that the concentration of the concentrate is decreased) while the allowable concentration ratio is satisfied.
Since the inter-membrane pressure difference between the concentrators is reduced when the flow rate of the raw liquid in the feed pipe 2 is reduced, when the inter-membrane pressure difference between the concentrators is lower than the minimum allowable differential pressure of the concentrator 20, the feed pipe liquid feed unit 2p is operated again to increase the flow rate of the raw liquid in the feed pipe 2.
That is, the above steps 1 to 3 are repeated while the inter-membrane differential pressure of the filter is within the allowable differential pressure of the filter 10. This method can ensure the maximum filtration flow rate (i.e., the maximum allowable flow rate LM) and the maximum concentration ratio, which are not possible to achieve when the amount of liquid fed to the filter 10 and the concentrate bag CB is constant, according to the membrane area and the clogging state of the filtration membranes of the filter 10 and the concentrator 20, or according to the state of the raw liquid (the concentration of a substance causing clogging of the filter and the concentrator, the concentration of a collected useful substance, the viscosity of the liquid, and the like). That is, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated solution from a raw solution can be shortened, and the re-concentration operation can be avoided or the time required for the re-concentration operation can be shortened.
Further, if the operation is performed as described above, at the start of the filtration concentration, the cleaning liquid filled in the filter 10, the concentrator 20, and the circuit, and the cleaning liquid in the filter 10 and the circuit immediately after the cleaning of the filter 10 can be removed as the waste liquid of the concentrator 20 in a short time. That is, dilution of the concentrated solution by the cleaning solution at the start and immediately after the cleaning of the filter as described above can be effectively prevented.
The above-described method (second method) is preferably employed when the maximum allowable differential pressure between the concentrator membranes is larger than the maximum allowable differential pressure PM between the filter membranes, but is not limited to this condition. The maximum allowable differential pressure between the concentrator membranes can be smaller than the maximum allowable differential pressure PM between the filter membranes.
In addition, when the filter membrane-to-membrane differential pressure is greater than the maximum allowable differential pressure PM, when the filter membrane-to-membrane differential pressure is less than the minimum allowable differential pressure PL, and when the feed rate of the raw liquid to the filter 10 is constant regardless of the filter membrane-to-membrane differential pressure, the above steps 1 to 3 may be repeated to adjust the feed rate of the concentrated liquid to the concentrator 20.
< cleaning of Filter >
When the filtration and concentration operation as described above is performed, the filter-membrane differential pressure becomes larger than the maximum allowable differential pressure PM of the filter 10 due to clogging of the filter 10 or the like. In this case, if the flow rate of the raw liquid in the feed pipe 2 is reduced by controlling the operation of the feed pipe liquid feeding unit 2p, the inter-filter-membrane differential pressure can be made smaller than the maximum allowable differential pressure PM of the filter 10, and the inter-filter-membrane differential pressure can be maintained within the allowable differential pressure (the range of the minimum allowable differential pressure PL or more and the maximum allowable differential pressure PM or less). However, if the clogging of the filter 10 or the like becomes serious, the flow rate of the raw liquid in the liquid supply pipe 2 may decrease to maintain the filter membrane-to-membrane differential pressure within the allowable differential pressure of the filter 10, and the flow rate of the raw liquid in the liquid supply pipe 2 may become smaller than the minimum allowable flow rate LL. When the above state is achieved, the operation of cleaning the filter 10 is performed in the middle of the filtering and concentrating operation of the raw liquid treatment apparatus 1 according to embodiment 1.
As shown in fig. 21, in the cleaning operation of the filter 10, the flow rate adjusting mechanism 3c closes the filter so that the liquid cannot flow through the filtrate supply pipe 3. In addition, the operation of the liquid feeding pipe liquid feeding portion 2p is stopped to function as a jig. On the other hand, the flow rate adjustment mechanism 6c can be opened to allow the liquid to flow through the cleaning liquid supply pipe 6.
In the above state, the cleaning liquid recovery pipe liquid feeding portion 7p is operated so that the liquid flows from the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6 to the cleaning liquid recovery bag FB connected to the cleaning liquid recovery pipe 7 through the filter 10. This allows the cleaning liquid to flow through the flow path of the filter 10 through which the raw liquid flows in the direction opposite to the direction in which the raw liquid flows during filtration and concentration, and thus allows the inside of the flow path of the filter 10 through which the raw liquid flows to be cleaned.
In addition to the above state, if the connecting pipe liquid feeding portion 9p is operated so that the cleaning liquid flows from the cleaning liquid bag SB connected to the connecting pipe 9 to the filter 10, the cleaning liquid is also supplied from the cleaning liquid bag SB connected to the connecting pipe 9 to the filter 10. This allows the cleaning liquid to permeate through the filter member in the direction opposite to the direction in which the filtrate permeates through the filter member, thereby eliminating clogging of the filter member. In this case, since the cleaning liquid is supplied to the filter 10 from both the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6 and the cleaning liquid bag SB connected to the connecting pipe 9, the operations of the cleaning liquid recovery pipe liquid feeding portion 7p and the connecting pipe liquid feeding portion 9p are adjusted so that the flow rate of the cleaning liquid flowing through the cleaning liquid recovery pipe 7 by the cleaning liquid recovery pipe liquid feeding portion 7p becomes larger than the flow rate of the cleaning liquid flowing through the connecting pipe 9 by the connecting pipe liquid feeding portion 9 p.
Further, the cleaning liquid recovery pipe liquid feeding portion 7p and the connecting pipe liquid feeding portion 9p may be operated in a state where the flow rate adjustment mechanism 6c is closed. In this case, the cleaning liquid is supplied to the filter 10 only from the cleaning liquid bag SB connected to the connecting pipe liquid feeding portion 9 p. In this case, the cleaning liquid also permeates through the filter member in the direction opposite to the direction in which the filtrate permeates through the filter member, so that clogging of the filter member can be eliminated.
In the case of using a filter having hollow fiber membranes 16 as the filter 10 as shown in fig. 5, it is desirable that the control unit 106 adjust the supply amount and supply timing of the cleaning liquid to the filter 10 so that the above-described cleaning of the filter 10 and the concentrator 20 can be appropriately performed. That is, it is desirable to adjust the supply amount and supply timing of the cleaning liquid to be supplied to the filter 10 so that the cleaning liquid permeates the hollow fiber membranes 16 in a state where the hollow space 12h of the trunk portion 12 is filled with the cleaning liquid to fill the region of the hollow fiber membranes 16 where cleaning is performed.
< recovery of filtrate >
On the other hand, when the filter cleaning is performed by the above-described method, the filtrate remaining in the internal space 12h of the main body 11 of the filter 10 is mixed with the cleaning liquid and discharged. This reduces the amount of the active ingredient recovered by concentration by filtration.
Here, when the filter cleaning is performed, it is desirable to feed the filtrate existing in the internal space 12h of the main body 11 of the filter 10 to the concentrator 20 in advance and then perform the filter cleaning.
< recovery (outside) by cleaning liquid >
As shown in fig. 1, the port 11c of the main body 11 of the filter 10 (the port 11c to which the filtrate supply tube 3 is not connected, hereinafter referred to as a cleaning port 11c) is connected to a cleaning solution bag SB via a tube. Then, the flow rate adjusting mechanism 3c keeps the liquid flowing in the filtrate supply pipe 3, and stops the operation of the liquid feeding pipe 2p while keeping the operation of the concentrated liquid pipe 4p continuing, thereby functioning as a jig. In this state, if the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10 by a pump provided in a pipe connected to the cleaning port 11c, the filtrate in the internal space 12h of the main body portion 11 of the filter 10 is supplied to the concentrator 20, and the cleaning liquid is relatively supplied from the cleaning liquid bag SB to the internal space 12 h. When all the filtrate in the internal space 12h is replaced with the cleaning liquid immediately after the start, the filtrate supply pipe 3 is closed by the flow rate adjusting mechanism 3c, and the operation of the concentrate pipe liquid feeding part 4p is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the operation of the feed pipe liquid feeding unit 2p is stopped and the recovery is performed, but the recovery may be performed while the operation of the feed pipe liquid feeding unit 2p is kept continued. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration. In this case, it is desirable to adjust the operation of the feed pipe liquid feeding portion 2p so as to reduce the amount of the raw liquid supplied to the filter 10.
It is sufficient to know whether or not all the filtrate in the internal space 12h has been replaced with the cleaning liquid by a method of measuring the amount of feed of a pump provided in a pipe connected to the cleaning port 11c and obtaining the amount theoretically or a method of measuring the concentration of the concentrated liquid. The concentration of the filtrate may be determined by observing the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a densitometer.
Further, a pump is not necessarily provided in the pipe connected to the cleaning port 11c of the main body 11 of the filter 10. In this case, if the concentrate-pipe liquid feeding unit 4p is operated, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be replaced with the cleaning liquid.
< recovery by gas such as air >
In the above description, the case where the cleaning solution bag SB is connected to the cleaning port 11c of the main body 11 of the filter 10 via a pipe has been described, but a gas such as air may be supplied to the cleaning port 11c of the main body 11 of the filter 10 via a pipe.
In this case, the flow rate adjusting mechanism 3c also maintains the state of flowing the liquid in the filtrate supply pipe 3, and stops the operation of the liquid feed pipe section 2p to function as a jig while keeping the operation of the concentrate pipe section 4p continued. In this state, if a gas such as air is supplied to the filter 10 from a pipe connected to the cleaning port 11c, the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20. When all the filtrate in the internal space 12h is discharged immediately after the start, the filtrate supply pipe 3 is closed by the flow rate adjusting mechanism 3c, and the operation of the concentrate pipe liquid feeding portion 4p is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the operation of the liquid feeding pipe liquid feeding unit 2p is stopped and the recovery is performed, but the recovery may be performed while the operation of the liquid feeding pipe liquid feeding unit 2p is kept continued. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration. In this case, it is desirable to adjust the operation of the feed pipe liquid feeding portion 2p so as to reduce the amount of the raw liquid supplied to the filter 10.
It is sufficient to know whether or not all the filtrate in the internal space 12 has been discharged by a method of providing a liquid detector or a bubble detector in the filtrate supply pipe 3, measuring the pressure in the filtrate supply pipe 3, or theoretically obtaining the amount of the filtrate fed by measuring the amount of the pump.
When the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the internal space 12h of the main body 11 of the filter 10 is filled with the gas such as air. Therefore, when the cleaning operation is performed after the recovery of the filtrate, it is desirable to perform the cleaning operation after the cleaning liquid fills the hollow space 12h of the body portion 12 and reaches the position of the region where the hollow fiber membranes 16 are cleaned (or the entire hollow space 12h of the body portion 12).
< recovery into bag >
In the above example, the filtrate is sent to the concentrator 20 and recovered in the state of the concentrated solution, but the filtrate may be recovered while remaining the filtrate. For example, a bag for recovering the filtrate is connected to the filtrate supply pipe 3 on the upstream side of the flow rate adjustment mechanism 3c (i.e., on the filter 10 side). In this state, if a gas such as a cleaning liquid or air is supplied to the filter 10 from the cleaning port 11c as described above in a state where the liquid cannot flow through the filtrate supply pipe 3 by the flow rate adjustment mechanism 3c, the filtrate in the internal space 12h of the main body portion 11 of the filter 10 can be collected into the bag. In this case, the filtrate can be recovered in a shorter time than in the case where the filtrate is sent to the concentrator 20 and recovered in a state of a concentrated solution, and therefore, the shift to the cleaning operation can be performed quickly.
< recovery by cleaning liquid (inside) >
In the above description, the following is explained: the raw liquid is supplied to the through channels 16h of the plurality of hollow fiber membranes 16 of the hollow fiber membrane bundle 15 of the filter 10, and the filtrate is discharged into the internal space 12h of the body portion 12 of the body portion 11 of the filter 10. However, the raw liquid may be supplied from the filtrate discharge port 11c into the internal space 12h of the body portion 12 of the body portion 11, and the filtrate obtained by filtration may be discharged into the through channels 16h of the plurality of hollow fiber membranes 16 of the hollow fiber membrane bundle 15 and discharged from the raw liquid supply port 11a to the outside.
In this case, the pipes and the like are connected as described below.
First, the filtrate supply pipe 3 is connected to the raw liquid supply port 11a, and the liquid supply pipe 2 is connected to the port 11c (i.e., the above-described cleaning port 11 c). The cleaning liquid supply pipe 6 is connected to a port 11c to which the liquid feed pipe 2 is not connected (i.e., the filtrate discharge port 11c), and a cleaning liquid bag SB connected to the cleaning port 11c is connected to the cleaning liquid supply port 11 b.
Then, the flow rate adjusting mechanism 3c keeps the liquid flowing in the filtrate supply pipe 3, and stops the operation of the liquid feeding pipe section 2p to function as a jig while keeping the operation of the concentrated liquid pipe section 4p continuing. In this state, if the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10 by a pump provided in a pipe connected to the cleaning liquid supply port 11b, the filtrate in the through flow path 16h of the hollow fiber membranes 16 of the filter 10 is supplied to the concentrator 20, and the cleaning liquid is relatively supplied from the cleaning liquid bag SB into the through flow path 16 h. When all the filtrate in the through-flow passage 16h is replaced with the cleaning liquid immediately after the start of the operation, the filtrate supply pipe 3 is closed by the flow rate adjusting mechanism 3c, and the operation of the concentrate pipe liquid feeding part 4p is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the operation of the liquid feeding pipe liquid feeding unit 2p is stopped and the recovery is performed, but the recovery may be performed while the operation of the liquid feeding pipe liquid feeding unit 2p is kept continued. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration. In this case, it is desirable to adjust the operation of the feed pipe liquid feeding portion 2p to reduce the amount of the raw liquid supplied to the filter 10.
It is sufficient to know whether or not all the filtrate in the internal space 12h has been replaced with the cleaning liquid by a method of measuring the amount of feed of a pump provided in a pipe connected to the cleaning port 11c and obtaining the amount theoretically or a method of measuring the concentration of the concentrated liquid. The concentration of the filtrate may be determined by observing the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a densitometer.
< recovery by gas such as air >
In the above description, the case where the cleaning liquid bag SB is connected to the cleaning liquid supply port 11b of the main body portion 11 of the filter 10 via a pipe has been described, but a gas such as air may be supplied to the cleaning supply port 11b of the main body portion 11 of the filter 10 via a pipe.
In this case, the flow rate adjusting mechanism 3c also maintains the state of flowing the liquid in the filtrate supply pipe 3, and stops the operation of the liquid feed pipe section 2p to function as a jig while keeping the operation of the concentrate pipe section 4p continuing. In this state, if a gas such as air is supplied from a pipe to the filter 10, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 can be supplied to the concentrator 20. When all the filtrate in the through flow channel 16h of the hollow fiber membrane 16 is discharged soon, the filtrate supply pipe 3 is closed by the flow rate adjusting mechanism 3c, and the operation of the concentrate pipe liquid feeding part 4p is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the recovery is performed by stopping the operation of the liquid feeding pipe liquid feeding unit 2p, but the recovery may be performed while the operation of the liquid feeding pipe liquid feeding unit 2p is kept continued. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration. In this case, it is desirable to adjust the operation of the feed pipe liquid feeding portion 2p so as to reduce the amount of the raw liquid supplied to the filter 10.
It is sufficient to know whether or not all the filtrate in the through flow channel 16h of the hollow fiber membrane 16 has been discharged by a method of providing a liquid detector or a bubble detector in the filtrate supply pipe 3, measuring the pressure in the filtrate supply pipe 3, or measuring the amount of feed of a pump to theoretically obtain the amount of feed.
When the filtrate in the through-flow channel 16h of the hollow fiber membrane 16 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the through-flow channel 16h of the hollow fiber membrane 16 of the filter 10 is filled with the gas such as air. Therefore, when the cleaning operation is performed after the filtrate is collected, it is desirable to perform the cleaning operation after the through-flow channel 16h is filled with the cleaning liquid in advance in a state where the region of the hollow fiber membranes 16 to be cleaned (or the entire hollow fiber membranes 16) is filled with the cleaning liquid.
< recovery into bag >
In the above example, the filtrate is sent to the concentrator 20 and recovered in the state of the concentrated solution, but the filtrate may be recovered while remaining the filtrate. For example, a bag for recovering the filtrate is connected to the filtrate supply pipe 3 at an upstream side (i.e., the filter 10 side) of the flow rate adjustment mechanism 3 c. In this state, if a gas such as a cleaning liquid or air is supplied to the filter 10 from the cleaning liquid supply port 16c as described above in a state where the liquid is not allowed to flow in the filtrate supply pipe 3 by the flow rate adjustment mechanism 3c, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 can be collected in the bag. In this case, the filtrate can be recovered in a shorter time than in the case where the filtrate is sent to the concentrator 20 and recovered in a state of a concentrated solution, and therefore, the shift to the cleaning operation can be performed quickly.
< other example of the method for collecting liquid in Filter 10 >
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and the filtrate is recovered as a concentrated solution, it is desirable to adjust the flow rate at the time of sending the filtrate to the concentrator 20 based on the inter-concentrator-membrane differential pressure of the concentrator 20. By adopting such a method, even if the concentrator 20 is clogged, the increase in the inter-membrane differential pressure of the concentrator can be suppressed, and the treatment can be prevented from being stopped, so that the filtrate in the filter 10 can be efficiently recovered.
For example, when the flow rate at the time of feeding the liquid to the concentrator 20 is adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rate can be adjusted as follows. First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the concentrate pipe liquid feeding portion 4p and the operation of the pump provided in the pipe connected to the cleaning port 11c are controlled to maintain the liquid feeding amount from the filter 10 to the concentrator 20. This prevents the occurrence of problems such as a large deviation of the pressure difference between membranes of the concentrator from the set pressure difference range.
On the other hand, when the pressure difference between the concentrator membranes of the concentrator 20 is larger than the maximum set pressure difference, the operation of the concentrate pipe liquid feeding portion 4p and the operation of the pump provided in the pipe connected to the cleaning port 11c are controlled so that the liquid feeding amount from the filter 10 to the concentrator 20 is reduced. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is smaller than the minimum set differential pressure, the operation of the concentrate-pipe liquid feeding portion 4p and the operation of the pump provided in the pipe connected to the cleaning port 11c are controlled so that the liquid feeding amount from the filter 10 to the concentrator 20 increases. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
< Another example of the method for recovering liquid in Filter 10 >
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and the filtrate is recovered as the concentrated solution, the flow rate from the concentrator 20 to the concentrate bag CB and/or the concentration ratio, which is the flow rate from the concentrator 20 to the waste bag DB, may be adjusted based on the inter-membrane pressure difference between the concentrators of the concentrator 20. In this method, while suppressing an increase in the inter-membrane differential pressure of the concentrator, the rate of recovering the concentrated solution can be kept constant without changing the flow rate of the solution sent from the filter 10 to the concentrator 20, and therefore the filtrate in the filter 10 can be recovered efficiently.
For example, when the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB are adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rates can be adjusted as follows.
First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the concentrate pipe liquid feeder 4p (the operation of the waste pipe liquid feeder 5p when the waste pipe liquid feeder 5p is provided) or the operation of the pump provided in the pipe connected to the cleaning port 11c is controlled so as to maintain the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB. This prevents the occurrence of problems such as a large deviation of the pressure difference between membranes of the concentrator from the set pressure difference range.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is greater than the maximum set differential pressure, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the pump provided in the pipe connected to the cleansing port 11c is controlled so that the flow rate from the concentrator 20 to the concentrate bag CB increases and/or the flow rate from the concentrator 20 to the waste bag DB decreases. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is smaller than the minimum set differential pressure, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the pump provided in the pipe connected to the cleaning port 11c is controlled so that the flow rate from the concentrator 20 to the concentrate bag CB decreases and/or the flow rate from the concentrator 20 to the waste bag DB increases. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
The set differential pressure of the pressure difference between the membranes of the concentrator when the filtrate in the filter 10 is recovered may be the same as the allowable differential pressure in the filtration and concentration operation, or may be a value (range) different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the range of the set differential pressure may be set to be larger than the range of the allowable differential pressure. In this case, it is desirable that the concentrated solution can be recovered to the end as much as possible even in a diluted state. In addition, when the range of the set differential pressure is set to be smaller than the range of the allowable differential pressure, it is desirable that the concentrated solution is recovered to the end as much as possible without diluting the concentrated solution even if it takes time. Further, the range of the allowable differential pressure and the range of the set differential pressure may be different from each other.
< reconcentration operation >
When the concentrated solution obtained by the filtering and concentrating operation is further concentrated, a re-concentrating operation is performed.
As shown in fig. 3, in the reconcentration operation of the raw liquid treatment apparatus 1 according to embodiment 1, the other end of the connecting tube 9 is removed from the cleaning liquid bag SB, and the other end of the connecting tube 9 is connected to the concentrated liquid bag CB.
The flow rate adjusting mechanism 3c maintains a state in which liquid can flow in the filtrate supply pipe 3, and the liquid supply pipe liquid feeding portion 2p and the cleaning liquid recovery pipe liquid feeding portion 7p are not operated to function as a jig. In addition, the flow rate adjusting mechanism 6c closes the cleaning liquid supply pipe 6 so that the liquid cannot flow. This prevents the liquid from flowing through the filter 10.
In the above state, the connecting pipe liquid feeding portion 9p is operated so that the concentrated liquid flows from the concentrated liquid bag CB to the concentrator 20 through the connecting pipe 9, and the concentrated liquid pipe liquid feeding portion 4p is operated so that the concentrated liquid flows from the concentrator 20 to the concentrated liquid bag CB through the concentrated liquid pipe 4.
Thereby, the concentrated liquid is supplied from the concentrated liquid bag CB connected to the connection pipe 9 to the concentrator 20 through the connection pipe 9, and thus the re-concentrated liquid further concentrated by the concentrator 20 is recovered to the concentrated liquid bag CB through the concentrated liquid pipe 4. On the other hand, the moisture separated from the concentrated solution is recovered to the waste liquid bag DB through the waste liquid pipe 5. That is, a concentrated solution (reconcentrated solution) having an increased concentration ratio can be obtained.
< explanation of the operation of reconcentration using the pressure difference between membranes in the concentrator >
In the re-concentration operation, the flow rate from the concentrator 20 to the concentrate bag CB and/or the re-concentration ratio, which is the flow rate from the concentrator 20 to the waste liquid bag DB, may be adjusted based on the inter-concentrator-membrane differential pressure of the concentrator 20. In this method, an effect is obtained that the time for producing a concentrated solution having a high concentration can be shortened while suppressing an increase in the pressure difference between membranes of the concentrator.
In this case, when the re-concentration operation using the pressure difference between the membranes of the concentrator is performed in advance, it is desirable to set the allowable pressure difference. That is, the differential pressure that can be allowed by the concentrator 20 (allowable differential pressure) is set in accordance with the concentrator 20. The allowable differential pressure may have a predetermined magnitude or may be set to a specific value. In the following description, the allowable differential pressure is typically a case having a predetermined width.
In addition, when the re-concentration operation using the filter membrane is performed, it is desirable to set the allowable flow rate in advance. That is, it is desirable to set a flow rate (allowable flow rate) that can be allowed for the stock solution in the connecting pipe 9. The allowable flow rate may have a predetermined magnitude or may be set to a specific value. The allowable flow rate does not necessarily have to be set. However, if the flow rate of the raw liquid in the connecting pipe 9 is too small, the time taken for reconcentration becomes too long. Therefore, in view of the invention for preventing the treatment time of the concentrated solution from becoming long, it is desirable to set the allowable flow rate in advance. The allowable flow rate in the re-concentration operation may be the same as the allowable flow rate in the filtering concentration or may be different from the allowable flow rate in the filtering concentration.
Further, when the re-concentration operation using the pressure difference between the membranes of the concentrator is performed, it is desirable to set the allowable concentration ratio in advance. That is, it is desirable to set the ratio of the flow rate of the concentrated liquid flowing in the concentrated liquid pipe 4 to the flow rate of the concentrated liquid in the connecting pipe 9 (allowable concentration ratio). The allowable concentration ratio may have a predetermined width or may be set to a specific value. The allowable concentration ratio is not necessarily set. However, if the concentration ratio, which is the ratio of the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4 to the flow rate of the concentrated liquid through the connecting pipe 9, is too low (i.e., the flow rate of the concentrated liquid becomes too high), the concentration of the concentrated liquid becomes thin (the water content in the concentrated liquid becomes large), and therefore, it takes time for the re-concentration process. Therefore, in order to prevent the concentration ratio from being excessively decreased, it is desirable to set an allowable concentration ratio in advance. The allowable concentration ratio in the re-concentration operation may be the same as or different from the allowable concentration ratio in the filtration concentration.
At the start of re-concentration, the connecting pipe liquid feeding part 9p is operated to increase the amount of the concentrated liquid fed to the concentrator 20. At this time, the concentrate pipe liquid feeding portion 4p is operated so that the concentrate reaches a predetermined concentration ratio in accordance with the flow rate of the concentrate in the connecting pipe 9. For example, when a concentrated solution having a concentration ratio of 10 times is to be produced, the operation of the concentrated solution pipe feed portion 4p may be adjusted so that the flow rate of the concentrated solution flowing through the concentrated solution pipe 4 becomes 1/10 of the flow rate of the concentrated solution flowing through the connecting pipe 9. In addition, instead of the concentration ratio of the concentrated liquid, the operation of the concentrated liquid pipe feed portion 4p may be adjusted so that the inter-membrane differential pressure of the concentrator becomes a set value within the allowable differential pressure (or maintained within the allowable differential pressure), or the inter-membrane differential pressure of the concentrator may become a set value within the allowable differential pressure (or maintained within the allowable differential pressure) while the concentrated liquid is maintained at a predetermined concentration ratio. While the amount of the concentrated liquid to be fed to the concentrator 20 is increased, the operation of the concentrated liquid pipe feeding portion 4p is controlled to be in any of the above states.
When the re-concentration progresses, clogging of the concentrator 20 gradually occurs. This increases the inter-membrane differential pressure of the concentrator. However, the connecting pipe liquid feeding unit 9p is operated to increase the amount of the concentrated liquid fed to the concentrator 20 until the inter-membrane differential pressure of the concentrator reaches the allowable differential pressure.
< first method >
The amount of the concentrated liquid to be sent to the concentrator 20 is continuously increased until the pressure difference between the membranes of the concentrator falls within the allowable pressure difference of the concentrator 20. When the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20, the connecting pipe liquid feeding unit 9p is controlled so that the flow rate of the concentrated liquid in the connecting pipe 9 is maintained at a flow rate at which the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20. On the other hand, the concentrate pipe liquid feeding portion 4p is operated as follows based on the pressure difference between the membranes of the concentrator, and the flow rate of the concentrate flowing through the concentrate pipe 4 is adjusted.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the concentrate pipe liquid feeding unit 4p is operated so that the amount of the concentrated liquid fed to the concentrated liquid bag CB is reduced. That is, the operation of the concentrate-pipe liquid sending part 4p is controlled so that the concentration of the concentrate is increased.
< step 2>
Then, the amount of the concentrated solution sent to the concentrated solution bag CB is reduced until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. If the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20, the concentrate pipe liquid feeding part 4p is controlled so that the flow rate of the concentrate in the concentrate pipe 4 is maintained at a flow rate at which the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20.
< step 3>
When the pressure difference between the concentrator membranes becomes larger than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the concentrate pipe liquid feeding part 4p is controlled so that the amount of the concentrated liquid fed to the concentrated liquid bag CB increases. Further, although the concentration ratio decreases as the amount of the concentrated liquid fed increases, the operation of the concentrated liquid pipe feeding portion 4p is controlled so that the concentration ratio decreases (the concentration of the concentrated liquid becomes low) while the allowable concentration ratio is satisfied.
When the liquid feed amount of the concentrated solution is increased to maintain the pressure difference between the membranes of the concentrator within the allowable pressure difference and the concentration ratio becomes smaller than the allowable concentration ratio, the following method (second method) can be used to cope with this.
Since the inter-membrane differential pressure of the concentrator decreases as the amount of the concentrated liquid sent to the concentrated liquid bag CB increases, when the inter-membrane differential pressure of the concentrator becomes lower than the minimum allowable differential pressure of the concentrator 20, the concentrated liquid pipe sending part 4p is operated again to decrease the amount of the concentrated liquid sent to the concentrated liquid bag CB.
That is, the above steps 1 to 3 are repeated while the pressure difference between the concentrator membranes is within the allowable pressure difference of the concentrator 20. This method makes it possible to secure the maximum concentration ratio corresponding to the membrane area and the clogging state of the filtration membrane of the concentrator 20, which cannot be achieved when the amount of liquid to be fed to the concentrate bag CB is constant, or the state of the concentrate (the concentration of the substance causing clogging of the concentrator, the concentration of the collected useful substance, the viscosity of the liquid, etc.). That is, by increasing the concentration efficiency, the time required to produce a concentrated solution having a high concentration can be shortened, and the time required for the re-concentration operation can be shortened.
< second method >
In the first method, the flow rate of the concentrated liquid in the concentrated liquid pipe 4 can be adjusted based on the inter-membrane pressure difference between the concentrators, and the flow rate of the concentrated liquid in the connecting pipe 9 can be adjusted based on the inter-membrane pressure difference between the concentrators as described below.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the connecting pipe liquid feeding unit 9p is operated so that the amount of the concentrated liquid fed to the concentrator 20 is increased.
< step 2>
Then, the amount of the concentrated solution to be sent to the concentrator 20 is increased until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. Then, if the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20, the operation of the connecting pipe liquid feeding unit 9p is controlled so that the flow rate of the concentrated liquid in the connecting pipe 9 is maintained at a flow rate at which the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. In this case, it is desirable to maintain the flow rate of the concentrated liquid in the connecting pipe 9 within a range of an allowable flow rate (not less than the minimum allowable flow rate and not more than the maximum allowable flow rate).
< step 3>
When the inter-membrane differential pressure of the concentrator becomes larger than the maximum allowable differential pressure of the concentrator 20 due to clogging of the concentrator 20 or the like immediately after that, the operation of the connecting pipe liquid feeding portion 9p is controlled so that the flow rate of the concentrated liquid in the connecting pipe 9 is reduced. That is, the operation of the connecting pipe liquid feeding portion 9p is controlled so that the flow rate of the liquid fed to the concentrator 20 is reduced. In this case, it is also desirable to maintain the flow rate of the concentrated liquid in the connecting pipe 9 within the allowable flow rate.
Since the inter-membrane pressure difference between the concentrators is reduced when the flow rate of the concentrated liquid in the connecting pipe 9 is reduced, when the inter-membrane pressure difference between the concentrators is lower than the minimum allowable differential pressure of the concentrator 20, the connecting pipe liquid feeding unit 9p is operated again to increase the flow rate of the concentrated liquid in the connecting pipe 9.
That is, the above steps 1 to 3 are repeated while the pressure difference between the concentrator membranes is within the allowable pressure difference of the concentrator 20. This method makes it possible to secure a maximum recirculation flow rate and a maximum concentration ratio corresponding to the membrane area and the clogged state of the filtration membranes of the filter 10 and the concentrator 20 or the state of the raw liquid (the concentration of the substance causing clogging of the filter and the concentrator, the concentration of the collected useful substance, the viscosity of the liquid, etc.) which cannot be achieved when the amount of liquid fed to the concentrator 20 is constant. That is, by improving the recycling efficiency and the concentration efficiency, the time for generating a concentrated solution having a high concentration can be shortened, and the time taken for the re-concentration operation can be shortened.
The allowable differential pressure of the pressure difference between the membranes of the thickener at the time of re-concentration may be the same as the allowable differential pressure in the filtration and concentration operation, or may be a value (range) different from the allowable differential pressure in the filtration and concentration operation. For example, when the allowable differential pressure in the filtering concentration operation has a certain range, the allowable differential pressure in the re-concentration operation may be set to a range wider than this range. In this case, when the raw liquid having a property that the filter 10 is easily clogged is treated, the treatment is slowly performed without applying pressure to the filter 10 during the filtering operation, but it is desirable to be able to generate a concentrated liquid having a high concentration and to shorten the re-concentration time. In addition, when the range of the allowable differential pressure during the re-concentration is made narrower than the range of the allowable differential pressure during the filtering and concentrating operation, when the raw liquid having a property that the concentrator 20 is easily clogged is treated, the raw liquid is treated in a short time without applying pressure to the concentrator 20 during the filtering and concentrating operation, and it is desirable that a concentrated liquid having a high concentration can be produced through the re-concentration operation. Further, the range of the allowable differential pressure in the filtering concentration operation may be different from the range of the allowable differential pressure in the re-concentration operation.
The allowable concentration ratio at the time of performing the re-concentration may be the same as the allowable concentration ratio in the filtering and concentrating operation, or may be a value (range) different from the allowable concentration ratio in the filtering and concentrating operation. For example, when the allowable concentration ratio in the filtering concentration operation is within a certain range, the range of the allowable concentration ratio in the re-concentration operation may be set to be larger than this range. In this case, it takes time to perform concentration in the filtration concentration operation, and it is desired to shorten the time for the re-concentration operation. In addition, when the range of the allowable concentration ratio in the re-concentration is set to be narrower than the range of the allowable concentration ratio in the filtering and concentrating operation, it takes time to perform the concentration in the re-concentration operation, and it is desirable to be able to quickly end the filtering and concentrating operation. Further, the range of the allowable concentration ratio in the filtering concentration operation and the range of the allowable concentration ratio in the re-concentration operation may be different from each other.
< example of method for recovering liquid in Filter 10 >
Before the above-described re-concentration operation is performed, the filtrate in the filter 10 is sent to the concentrator 20, and the filtrate is recovered as a concentrated solution. In this case, it is desirable to adjust the flow rate when the liquid is sent to the concentrator 20 based on the pressure difference between the concentrator membranes of the concentrator 20. By adopting such a method, even if the concentrator 20 is clogged, the increase in the inter-membrane differential pressure of the concentrator can be suppressed, and the treatment can be prevented from being stopped, so that the filtrate in the filter 10 can be efficiently recovered.
For example, when the flow rate at the time of feeding the liquid to the concentrator 20 is adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rate can be adjusted as follows. First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the concentrate pipe liquid feeding portion 4p and the operation of the pump provided in the pipe connected to the cleaning port 11c are controlled to maintain the liquid feeding amount from the filter 10 to the concentrator 20. This prevents the occurrence of problems such as a large deviation of the pressure difference between membranes of the concentrator from the set pressure difference range.
On the other hand, when the pressure difference between the concentrator membranes of the concentrator 20 is larger than the maximum set pressure difference, the operation of the concentrate pipe liquid feeding portion 4p and the operation of the pump provided in the pipe connected to the cleaning port 11c are controlled so that the liquid feeding amount from the filter 10 to the concentrator 20 is reduced. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment. On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is smaller than the minimum set differential pressure, the operation of the concentrate-pipe liquid feeding portion 4p and the operation of the pump provided in the pipe connected to the cleaning port 11c are controlled so that the liquid feeding amount from the filter 10 to the concentrator 20 increases. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
< Another example of the method for recovering liquid in Filter 10 >
When the filtrate in the filter 10 is sent to the concentrator 20 and recovered as a concentrated solution, the flow rate from the concentrator 20 to the concentrated solution bag CB and/or the flow rate from the concentrator 20 to the waste solution bag DB, that is, the concentration ratio may be adjusted based on the inter-membrane pressure difference between the concentrators of the concentrator 20. In this method, while suppressing an increase in the inter-membrane differential pressure of the concentrator, the recovery rate can be kept constant without changing the flow rate of the liquid sent from the filter 10 to the concentrator 20, and therefore the filtrate in the filter 10 can be recovered efficiently.
For example, when the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB are adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rates can be adjusted as follows.
First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the concentrate pipe liquid feeder 4p (the operation of the waste pipe liquid feeder 5p when the waste pipe liquid feeder 5p is provided) or the operation of the pump provided in the pipe connected to the cleaning port 11c is controlled so as to maintain the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB. This prevents the occurrence of problems such as a large deviation of the pressure difference between membranes of the concentrator from the set pressure difference range.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is greater than the maximum set differential pressure, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the pump provided in the pipe connected to the cleansing port 11c is controlled so that the flow rate from the concentrator 20 to the concentrate bag CB increases and/or the flow rate from the concentrator 20 to the waste bag DB decreases. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is smaller than the minimum set differential pressure, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the pump provided in the pipe connected to the cleaning port 11c is controlled so that the flow rate from the concentrator 20 to the concentrate bag CB decreases and/or the flow rate from the concentrator 20 to the waste bag DB increases. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
The set differential pressure of the pressure difference between the membranes of the concentrator when the filtrate in the filter 10 is recovered may be the same as the allowable differential pressure in the filtration and concentration operation, or may be a value (range) different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the range of the set differential pressure may be set to be larger than the range of the allowable differential pressure. In this case, it is desirable that the concentrated solution can be recovered to the end as much as possible even in a diluted state. In addition, when the range of the set differential pressure is set to be smaller than the range of the allowable differential pressure, it is desirable that the concentrated solution is recovered to the end as much as possible without diluting the concentrated solution even if it takes time. Further, the range of the allowable differential pressure may deviate from the range of the set differential pressure.
< operation for collecting concentrator 20 >
When the concentrate in the concentrator 20 is also recovered after the raw liquid and the filtrate in the filter 10 are recovered, only a cleaning liquid or a fluid called a gas (hereinafter, simply referred to as a fluid) may be made to flow in the concentrator 20, and the concentrate or the like may be further recovered. However, as in the above case, the flow rate of the fluid supplied to the concentrated solution 20 may be adjusted while measuring the inter-membrane differential pressure of the concentrator. This prevents problems such as an increase in the pressure difference between the membranes of the concentrator and the inability to continue the treatment. If the inter-concentrator-membrane differential pressure of the concentrator 20 is greater than the maximum set differential pressure, the problem of the inter-concentrator-membrane differential pressure continuing to rise can be prevented by stopping the liquid feed (including the gas flow) from the filter 10 to the concentrator 20.
The set differential pressure (second set differential pressure) between the concentrator membranes when the concentrated solution in the concentrator 20 is recovered may be the same as the allowable differential pressure during the filtration and concentration operation or the set differential pressure (first set differential pressure) when the filtrate in the filter 10 is recovered, or may be a value (range) different from these. For example, when the allowable differential pressure and the first set differential pressure have a certain range, the range of the second set differential pressure may be set to be larger than the range of the allowable differential pressure and the first set differential pressure. In this case, it is desirable that the concentrated solution can be recovered to the end as much as possible even in a diluted state. In addition, when the range of the set differential pressure is set to be smaller than the range of the allowable differential pressure, it is desirable that the concentrated solution is recovered to the end as much as possible without diluting the concentrated solution even if it takes time. Further, the range of the second set differential pressure may be different from the range of the allowable differential pressure and the range of the first set differential pressure.
< operation for collecting liquid in filtrate supply pipe 3 >
After the recovery of the concentrated liquid in the concentrator 20, if the pressure difference between the concentrator membranes reaches a set pressure difference or a predetermined liquid amount is recovered, the liquid feed (including the gas flow) from the filter 10 to the concentrator 20 may be stopped, and then a gas such as air may be supplied to the filtrate supply pipe 3. This prevents the concentrated liquid in the concentrator 20 or the concentrated liquid passage 4 and the liquid in the passage on the downstream side of the filtrate supply pipe 3 from being recovered and left over. If the inter-membrane differential pressure of the concentrator does not reach the set differential pressure, the liquid feed from the filter 10 to the concentrator 20 may not necessarily be stopped.
< stock solution treatment apparatus 1B of embodiment 2 >
In the raw liquid treatment apparatus 1 according to embodiment 1 described above, the raw liquid is supplied to the filter 10 by being pressed in during filtration and concentration, but the raw liquid may be supplied to the filter 10 by being sucked out from the filter 10.
That is, as shown in fig. 7, the raw liquid treatment apparatus 1B according to embodiment 2 is configured to supply the raw liquid to the filter 10 so as to suck the raw liquid from the filter 10. That is, the raw liquid processing apparatus 1B according to embodiment 2 is the raw liquid processing apparatus 1 according to embodiment 1, in which the filtrate supply pipe 3 is provided with the filtrate supply pipe liquid feeding portion 3p instead of the flow rate adjusting mechanism 3c, and the liquid supply pipe 2 is provided with the flow rate adjusting mechanism 2c instead of the liquid supply pipe liquid feeding portion 2 p.
In the raw liquid treatment apparatus 1B, the filtrate supply pipe liquid feeding unit 3p is operated to flow the liquid (filtrate) from the filter 10 to the concentrator 20 at the time of filtration and concentration. When the filtrate supply pipe liquid feeding portion 3p is operated, a negative pressure is generated in the filtrate supply pipe 3 upstream of the filtrate supply pipe liquid feeding portion 3p, that is, in the filter 10 side, and the inside of the filter 10 (for example, the internal space 12h of the body portion 12 of the body portion 11) is also generated. Thus, if the liquid feed pipe 2 is brought into a state in which liquid can be fed by the flow rate adjustment mechanism 2c, the raw liquid in the raw liquid bag UB can be sucked into the filter 10 through the liquid feed pipe 2, and the sucked raw liquid can be sucked into the filtrate supply pipe 3.
In the raw liquid processing apparatus 1B, if the operation of the flow rate adjusting mechanism and the liquid sending unit provided in each pipe is adjusted by appropriately changing the bag connected to each pipe, the preparatory cleaning operation, the filtering concentration operation, and the re-concentration operation can be performed. In the raw liquid processing apparatus 1B, a waste liquid pipe 5 may be provided with a waste liquid pipe sending part 5p instead of the concentrated liquid pipe sending part 4p (see fig. 9). Even in this case, the same function as in the case where the concentrate-pipe liquid feeder 4p is provided in the concentrate pipe can be achieved by reducing the liquid feeding amount of the waste liquid by the waste-pipe liquid feeder 5p under the condition that the liquid feeding amount of the concentrate is increased by the concentrate-pipe liquid feeder 4p, and increasing the liquid feeding amount of the waste liquid by the waste-pipe liquid feeder 5p under the condition that the liquid feeding amount of the concentrate is reduced by the concentrate-pipe liquid feeder 4 p. Hereinafter, a case where the concentrate pipe liquid sending part 4p is provided in the concentrate pipe 4 will be described.
< preparation for cleaning operation >
As shown in fig. 6, a cleaning solution bag SB is connected to the other end of the concentrate pipe 4 in place of the concentrate bag CB, and a cleaning solution recovery bag FB is connected to the other end of the waste pipe 5 in place of the waste bag DB. The other end of the waste liquid pipe 5 may be connected to the waste liquid bag DB, or may be simply disposed in a bucket or the like.
Further, a cleaning liquid recovery bag FB is also connected to the other end of the liquid feed pipe 2 instead of the raw liquid bag UB. The other end of the liquid supply tube 2 may be connected to the waste liquid bag DB, or the other end of the liquid supply tube 2 may be simply disposed in a tub or the like.
The other end of the connection pipe 9 is also connected to a cleaning liquid recovery bag FB. The other end of the connecting pipe 9 may be connected to the waste liquid bag DB, or the other end of the connecting pipe 9 may be simply disposed in a tub or the like.
Further, the cleaning liquid recovery bag FB is connected to the other end of the cleaning liquid supply tube 6 in place of the cleaning liquid bag SB, and the cleaning liquid bag SB is connected to the other end of the cleaning liquid recovery tube 7 in place of the cleaning liquid recovery bag FB. The waste liquid bag DB may be connected to the other end of the cleaning liquid supply pipe 6 and the other end of the cleaning liquid recovery pipe 7, or the other end of the cleaning liquid supply pipe 6 and the other end of the cleaning liquid recovery pipe 7 may be simply disposed in a tub or the like.
Next, the flow rate adjustment mechanism 2c and the flow rate adjustment mechanism 2c are opened to flow the cleaning liquid through the liquid supply pipe 2 and the connection pipe 9.
In this state, the concentrate pipe liquid sending part 4p is operated so that the cleaning liquid flows from the cleaning liquid bag SB connected to the concentrate pipe 4 to the concentrator 20, and the filtrate supply pipe liquid sending part 3p is operated so that the cleaning liquid flows from the concentrator 20 (i.e., the filtrate supply pipe 3) to the cleaning liquid recovery bag FB connected to the connection pipe 9. Thereby, the cleaning liquid is supplied from the cleaning liquid bag SB connected to the concentrate pipe 4 to the concentrator 20 through the concentrate pipe 4. The supplied cleaning liquid passes through the concentrator 20, and is then collected into the cleaning liquid collection bag FB connected to the connection pipe 9 through the filtrate supply pipe 3 and the connection pipe 9. In addition, a part of the cleaning liquid is recovered through the waste liquid pipe 5 to the cleaning liquid recovery bag FB connected to the other end of the waste liquid pipe 5.
Further, the cleaning solution recovery pipe liquid feeding portion 7p is operated so that the cleaning solution flows from the cleaning solution bag SB connected to the cleaning solution recovery pipe 7 to the filter 10. Thereby, a part of the cleaning liquid is supplied from the cleaning liquid bag SB connected to the cleaning liquid recovery pipe 7 to the filter 10 through the cleaning liquid recovery pipe 7. The cleaning liquid supplied to the filter 10 passes through the filter 10, and then is collected into the cleaning liquid collection bag FB connected to the connection pipe 9 through the filtrate supply pipe 3 and the connection pipe 9. Further, by operating the cleaning liquid supply pipe liquid feeding portion 6p, a part of the cleaning liquid supplied to the filter 10 can be also made to flow into the cleaning liquid supply pipe 6. Further, a part of the cleaning liquid is collected from the cleaning liquid collection tube 7 to the cleaning liquid collection bag FB connected to the liquid supply tube 2 through the liquid supply tube 2.
This enables the cleaning liquid to flow through the filter 10, the concentrator 20, and all the pipes, and thus the entire raw liquid treatment apparatus 1B according to embodiment 2 can be cleaned.
< filtration and concentration operation >
When the preparation cleaning operation is finished, the filtration and concentration operation is performed.
As shown in fig. 7, in the filtration and concentration operation of the raw liquid treatment apparatus 1B according to embodiment 2, from the state in which the cleaning operation is prepared (see fig. 6), the concentrate bag CB is connected to the other end of the concentrate pipe 4 instead of the cleaning liquid bag SB, and the waste liquid bag DB is connected to the other end of the waste pipe 5 instead of the cleaning liquid recovery bag FB.
On the other hand, the stock solution bag UB is connected to the other end of the liquid feed pipe 2 in place of the cleaning solution recovery bag FB.
The flow rate adjusting mechanism 2c is opened to maintain a state in which the liquid can flow in the liquid supply pipe 2, while the flow rate adjusting mechanism 9c is closed to prevent the liquid from flowing in the connecting pipe 9. In addition, the cleaning liquid recovery pipe liquid feeding portion 7p and the cleaning liquid supply pipe liquid feeding portion 6p are not operated and function as jigs.
In the above state, the filtrate supply pipe liquid feeding part 3p is operated so that the filtrate flows from the filter 10 to the concentrator 20, and the concentrate pipe liquid feeding part 4p is operated so that the concentrate flows from the concentrator 20 to the concentrate bag CB.
Thereby, the raw liquid is supplied from the raw liquid bag UB to the filter 10 through the liquid feed pipe 2. The supplied raw liquid is filtered by the filter 10, and the generated filtrate is supplied to the concentrator 20 through the filtrate supply pipe 3. Then, the filtrate supplied to the concentrator 20 is concentrated by the concentrator 20, and the resulting concentrated solution is collected into the concentrated solution bag CB through the concentrated solution pipe 4. On the other hand, the moisture separated from the concentrated solution is recovered to the waste liquid bag DB through the waste liquid pipe 5.
< operation of filtration and concentration >
In the filtration and concentration operation, the operation of the filtrate supply pipe liquid sending part 3p and the concentrate pipe liquid sending part 4p is controlled so that the concentration ratio falls within a predetermined range. However, the operation of the filtrate supply pipe liquid feeding part 3p and the concentrate pipe liquid feeding part 4p, that is, the flow rate of the liquid flowing through the filtrate supply pipe 3 and the concentrate pipe 4 may be controlled by the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure as described below. This enables filtration and concentration to be performed by effectively utilizing the capabilities of the filter 10 and the concentrator 20, and therefore, the time required for producing a concentrated solution can be shortened, and the efficiency of the concentration operation can be improved.
Hereinafter, the operation of filtration and concentration by controlling the operation of the filtrate supply pipe liquid feeding part 3p and the concentrate pipe liquid feeding part 4p by the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure will be described.
In addition, the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure can be calculated by measuring the tube internal pressure connected to the filter 10 and the concentrator 20. For example, if pressure gauges are provided in the feed pipe 2 and the filtrate supply pipe 3 in advance and the signals are supplied to the control unit 106, the control unit 106 can calculate the differential pressure between the filter membranes. Further, the control unit 106 can calculate the filter membrane-to-membrane differential pressure even if a pressure gauge is provided at the port 11c to which the filtrate supply pipe 3 is not connected (or a pipe connected to the port 11 c). Further, if pressure gauges are provided in the filtrate supply pipe 3 and the waste liquid pipe 5 in advance and the signals are supplied to the control unit 106, the control unit 106 can calculate the inter-membrane pressure difference of the concentrator. In addition, in the case where there is a port 20c to which the waste liquid pipe 5 is not connected, the control unit 106 can calculate the inter-membrane pressure difference of the concentrator even if a pressure gauge is provided in the port 20c (or a pipe connected to the port 20 c).
In the filter 10 and the concentrator 20, if either the liquid feed side or the liquid discharge side is in a state of being opened to the atmosphere, the control unit 106 can calculate the filter-membrane differential pressure and the concentrator-membrane differential pressure even if only the internal pressures of the tubes communicating with the side not opened to the atmosphere, out of the liquid feed side and the liquid discharge side, are measured. In other words, the control unit 106 can control the operation of the liquid feeding unit by using only the tube internal pressure communicated with the side not opened to the atmosphere instead of the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure. For example, if a tube connected to the filter 10 and the concentrator 20 is connected to a bag and the tube is not closed by the liquid feeding unit or the flow rate adjustment mechanism, the tube can be considered to be in a state of being nearly open to the atmosphere. In the state of fig. 7, the liquid supply tube 2 connected to the raw liquid bag UB of the tubes 2 and 3 connected to the filter 10 can be regarded as being open to the atmosphere. Further, the waste liquid pipe 5 connected to the waste liquid bag DB among the pipes 3 and 5 connected to the concentrator 20 can be regarded as being open to the atmosphere. Thus, if the state is shown in fig. 7, the controller 106 can control the operation of the liquid feeder by using only the tube internal pressure of the filter supply tube 3.
The flow rates of the liquids flowing through the filtrate supply pipe 3 and the concentrate pipe 4 may be estimated from the operations of the filtrate supply pipe liquid sending part 3p and the concentrate pipe liquid sending part 4p, or flow meters may be provided in the filtrate supply pipe 3 or the filtrate supply pipe liquid sending part 3p, and the concentrate pipe 4 or the concentrate pipe liquid sending part 4p to directly measure the flow rates.
< description of operation of filtration and concentration Using differential pressure between membranes of Filter and differential pressure between membranes of concentrator >
When filtration and concentration operations are performed using the pressure difference between the membranes of the filter and the pressure difference between the membranes of the concentrator, an allowable pressure difference is set in advance. That is, the differential pressures (allowable differential pressures) that can be allowed for the filter 10 and the concentrator 20 are set in accordance with the filter 10 and the concentrator 20, respectively. The allowable differential pressure may have a predetermined magnitude or may be set to a specific value. In the following description, the allowable differential pressure is typically a case having a predetermined width.
In addition, when performing filtration and concentration operations using the pressure difference between the filter membranes and the pressure difference between the concentrator membranes, it is desirable to set the allowable flow rate in advance. That is, it is desirable to set the flow rate (allowable flow rate) that can be allowed for the raw liquid in the feed pipe 2. The allowable flow rate may have a predetermined magnitude or may be set to a specific value. The allowable flow rate does not necessarily have to be set. However, if the flow rate of the raw liquid in the feed pipe 2 is too small, the time taken for the filtration and concentration becomes too long. Therefore, it is desirable to set the allowable flow rate in advance in order to prevent the treatment time of the raw liquid from increasing.
Further, when performing filtration and concentration operations using the pressure difference between the filter membranes and the pressure difference between the concentrator membranes, it is desirable to set the allowable concentration ratio in advance. That is, it is desirable to set the ratio of the flow rate of the raw liquid in the feed pipe 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4 (allowable concentration ratio). The allowable concentration ratio may have a predetermined width or may be set to a specific value. The allowable concentration ratio is not necessarily set. However, if the concentration ratio, which is the ratio of the flow rate of the raw liquid in the feed pipe 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4, is too low (i.e., the flow rate of the concentrated liquid becomes too large), the concentration efficiency deteriorates. Further, the amount of the concentrated solution increases, and a large amount of the filtered concentrated solution is re-intravenously fed, which may cause an increase in blood pressure, an increase in heart failure, and an increase in respiratory failure. Therefore, when the amount of the concentrate becomes excessive, it is necessary to add a re-concentration process, and the re-concentration process takes time. In the case of re-concentrating the concentrated solution, since the re-concentration process takes time, the total time for processing the raw solution becomes long. Therefore, in order to prevent the concentration ratio from being excessively decreased, it is desirable to set an allowable concentration ratio in advance.
At the start of filtration and concentration, the filtrate supply pipe liquid feeding unit 3p is operated to increase the amount of the raw liquid fed to the filter 10. At this time, the concentrate-pipe liquid feeding unit 4p is operated so that the concentration ratio of the concentrate becomes a predetermined concentration ratio in accordance with the flow rate of the filtrate in the filtrate supply pipe 3. For example, when a concentrated solution having a concentration ratio of 10 times is to be produced, the operation of the concentrated solution pipe feed portion 4p may be adjusted so that the flow rate of the concentrated solution flowing through the concentrated solution pipe 4 becomes 1/10 of the flow rate of the filtrate flowing through the filtrate supply pipe 3. In addition, instead of the concentration ratio of the concentrated liquid, the operation of the concentrated liquid pipe feed portion 4p may be adjusted so that the inter-membrane differential pressure of the concentrator becomes a set value within the allowable differential pressure (or maintained within the allowable differential pressure), or the inter-membrane differential pressure of the concentrator may become a set value within the allowable differential pressure (or maintained within the allowable differential pressure) while the concentrated liquid is maintained at a predetermined concentration ratio. While the amount of the filtrate fed to the concentrator 20 is increased, the operation of the concentrate-pipe liquid feeding unit 4p is controlled so as to be in any of the above-described states.
When the filtration concentration advances, clogging of the filter 10 and the concentrator 20 gradually occurs. Thereby, the inter-membrane differential pressure of the filter and the inter-membrane differential pressure of the concentrator increase. However, the filtrate feed pipe liquid feeding unit 3p is operated to increase the amount of feed of the filtrate to the concentrator 20 (in other words, the amount of feed of the raw liquid to the filter 10) until the inter-membrane differential pressure between the filter membranes and the inter-membrane differential pressure between the concentrator membranes are within the allowable differential pressure.
< first method >
The increase in the amount of the filtrate fed to the concentrator 20 is continued until the inter-membrane differential pressure of the filter reaches the allowable differential pressure of the filter 10. When the inter-membrane pressure difference of the filter is within the allowable differential pressure of the filter 10, the filtrate supply pipe liquid feeding unit 3p is controlled so that the liquid feeding amount of the filtrate to the concentrator 20 is maintained at a flow rate at which the inter-membrane pressure difference of the filter is within the allowable differential pressure of the filter 10. On the other hand, the concentrate pipe liquid feeding portion 4p is operated to adjust the flow rate of the concentrate flowing through the concentrate pipe 4.
Here, when the inter-membrane differential pressure of the filter is within the allowable differential pressure of the filter 10, the operation of the filtrate feeding pipe 3p is controlled so as to maintain the amount of the filtrate fed to the concentrator 20, in other words, the amount of the stock solution fed to the filter 10. This enables the filtration by the filter 10 and the concentration by the concentrator 20 to be maintained in a predetermined state. Further, if the amount of liquid to be fed to the filter 10 of the raw liquid is increased or decreased based on the value of the inter-membrane differential pressure between the filters, the amount of liquid to be fed to the filter 10 of the raw liquid can be increased while maintaining the inter-membrane differential pressure between the filters 10 within the allowable differential pressure of the filter 10. That is, there is a possibility that the efficiency of the filtration and concentration operation is improved. In particular, if the inter-membrane differential pressure of the filter is maintained at the maximum allowable differential pressure PM of the filter 10, the amount of the stock solution sent to the filter 10 can be increased to the maximum, and therefore the effect of shortening the time for the filtration operation can be further enhanced.
On the other hand, when the inter-membrane differential pressure becomes greater than the maximum allowable differential pressure PM of the filter 10, the operation of the filtrate supply pipe liquid feeding portion 3p is controlled so that the amount of liquid to be fed to the filter 10 from the raw liquid is reduced. When the hollow fiber membranes or the like are clogged even if the amount of the raw liquid fed to the filter 10 is constant, there is a possibility that the pressure difference between the filter membranes increases and the filtration cannot be continued. However, if the amount of the raw liquid fed to the filter 10 is reduced, the pressure difference between the filter membranes can be reduced, and therefore the filtering operation can be continued even if the filter 10 is clogged. Further, since the amount of the raw liquid fed to the filter 10 is reduced, clogging of the hollow fiber membranes 16 and the like may be slightly reduced, and therefore, the filtering operation may be easily continued, and the time for the filtering operation may be shortened. In particular, when the inter-membrane differential pressure of the filter becomes larger than the maximum allowable differential pressure PM of the filter 10, if the supply of the raw liquid to the filter 10 is temporarily stopped and the supply is restarted after a certain period of time, there is a possibility that the effect of reducing clogging of the hollow fiber membranes and the like can be improved.
When the inter-membrane differential pressure of the filter becomes smaller than the minimum allowable differential pressure PL of the filter 10, for example, by reducing the amount of the raw liquid sent to the filter 10, the operation of the filtrate supply pipe liquid sending unit 3p is controlled so that the amount of the raw liquid sent to the filter 10 increases. This can increase the filtration amount of the filter 10, and therefore, the time for the filtration operation may be shortened. Further, if the amount of the raw liquid fed to the filter 10 is increased to the extent that the inter-membrane differential pressure of the filter 10 is within the allowable differential pressure of the filter 10, the filtering capacity of the filter 10 can be effectively used, and therefore the effect of shortening the time for the filtering operation can be further enhanced.
When the amount of the raw liquid to be fed to the filter 10 is reduced when the filter membrane-to-membrane differential pressure becomes larger than the maximum allowable differential pressure PM of the filter 10, the amount of the raw liquid to be fed may be gradually reduced, or the amount of the raw liquid to be fed may be reduced stepwise. When the filter-membrane differential pressure becomes greater than the maximum allowable differential pressure PM (PM in fig. 24) of the filter 10, the flow of the raw liquid to the filter 10 may be stopped for a certain period of time and then the flow of the raw liquid to the filter 10 may be started (see fig. 24). In this case, the amount of the feed liquid of the raw liquid to the filter 10 may be adjusted while the pressure difference between the filter membranes is checked. For example, as shown in pattern 1 of fig. 24, when the liquid feeding of the raw liquid to the filter 10 is started after stopping the liquid feeding of the raw liquid to the filter 10 for a certain period of time, the liquid feeding is started at a flow rate of about 1/2 of the maximum allowable flow rate LM first, and the inter-filter-membrane differential pressure at that time is confirmed. If the inter-filter-membrane differential pressure is smaller than the minimum allowable differential pressure PL (PL in fig. 24) in this state, the flow rate around 1/2, which is the difference between the current flow rate and the maximum allowable flow rate LM, is increased and the inter-filter-membrane differential pressure at this time is confirmed. If the inter-filter-membrane differential pressure is still smaller than the minimum allowable differential pressure PL in this state, the flow rate around 1/2 of the difference between the current flow rate and the maximum allowable flow rate LM is further increased and the inter-filter-membrane differential pressure at this time is confirmed. This operation is repeated, and if the filter membrane-to-membrane differential pressure is equal to or higher than the minimum allowable differential pressure PL and equal to or lower than the maximum allowable differential pressure PM of the filter 10 (or if the maximum allowable differential pressure PM is reached), the increase in the flow rate is stopped. Even if the inter-membrane differential pressure of the filter is not less than the minimum allowable differential pressure PL and not more than the maximum allowable differential pressure PM of the filter 10, the amount of the feed liquid of the raw liquid to the filter 10 can be increased to the maximum allowable flow rate LM in the same manner while confirming the inter-membrane differential pressure of the filter.
When the amount of the raw liquid supplied to the filter 10 is increased when the filter-membrane differential pressure becomes smaller than the minimum allowable differential pressure PL of the filter 10, the amount of the raw liquid supplied may be gradually increased. For example, the amount of the raw liquid to be fed to the filter 10 may be increased by the same method as the above-described method of increasing the flow rate, that is, the method of increasing the flow rate from the state where the feeding of the raw liquid to the filter 10 is stopped for a certain period of time.
In addition, while the amount of the raw liquid fed to the filter 10 is maintained in a state where the filter-membrane differential pressure is maintained within the allowable differential pressure of the filter 10, the amount of the raw liquid fed to the filter 10 may be increased until the maximum allowable flow rate LM is reached when the flow rate is smaller than the maximum allowable flow rate LM.
Even if the inter-membrane differential pressure of the filter becomes equal to or greater than the minimum allowable differential pressure PL of the filter 10, if the amount of the raw liquid fed to the filter 10 does not reach the minimum allowable flow rate LL (pattern 3 in fig. 24), it is determined that clogging of the hollow fiber membranes 16 or the like has occurred, and the filtration concentration operation is stopped and the operation is shifted to the cleaning operation.
Next, the concentrate pipe liquid feeding portion 4p can be controlled based on the inter-membrane pressure difference between the concentrators as follows, in a state where the inter-membrane pressure difference between the filters 10 is within the allowable pressure difference of the filters 10 and the flow rate of the raw liquid in the liquid feeding pipe 2 is maintained at a flow rate in a state where the inter-membrane pressure difference between the filters 10 is within the allowable pressure difference of the filters 10.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the concentrate pipe liquid feeding unit 4p is operated so that the amount of the concentrated liquid fed to the concentrated liquid bag CB is reduced. That is, the operation of the concentrate-pipe liquid sending part 4p is controlled so that the concentration of the concentrate is increased.
< step 2>
Then, the amount of the concentrated solution sent to the concentrated solution bag CB is reduced until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. If the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20, the concentrate pipe liquid feeding part 4p is controlled so that the flow rate of the concentrate in the concentrate pipe 4 is maintained at a flow rate at which the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20.
< step 3>
When the pressure difference between the concentrator membranes becomes larger than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the concentrate pipe liquid feeding part 4p is controlled so that the amount of the concentrated liquid fed to the concentrated liquid bag CB increases. Further, although the concentration ratio decreases as the amount of the concentrated liquid fed increases, the operation of the concentrated liquid pipe feeding portion 4p is controlled so that the concentration ratio decreases (the concentration of the concentrated liquid becomes low) while the allowable concentration ratio is satisfied. When the liquid feed amount of the concentrated solution is increased to maintain the pressure difference between the membranes of the concentrator within the allowable pressure difference and the concentration ratio becomes smaller than the allowable concentration ratio, the following method (second method) can be used to cope with this.
When the amount of the concentrated liquid fed to the concentrated liquid bag CB increases, the inter-membrane differential pressure of the concentrator decreases, and therefore, when the inter-membrane differential pressure of the concentrator becomes lower than the minimum allowable differential pressure of the concentrator 20, the concentrated liquid pipe feeding portion 4p is operated again, so that the amount of the concentrated liquid fed to the concentrated liquid bag CB decreases.
That is, the above steps 1 to 3 are repeated until the inter-membrane differential pressure of the filter reaches the allowable differential pressure of the filter 10. This method can ensure the maximum filtration flow rate (i.e., the maximum allowable flow rate LM) and the maximum concentration ratio, which are not possible to achieve when the amount of liquid fed to the filter 10 and the concentrate bag CB is constant, according to the membrane area and the clogging state of the filtration membranes of the filter 10 and the concentrator 20, or according to the state of the raw liquid (the concentration of a substance causing clogging of the filter and the concentrator, the concentration of a collected useful substance, the viscosity of the liquid, and the like). That is, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated solution from a raw solution can be shortened, and the re-concentration operation can be avoided or the time required for the re-concentration operation can be shortened.
Further, if the operation is performed as described above, at the start of the filtration concentration, the cleaning liquid filled in the filter 10, the concentrator 20, and the circuit, and the cleaning liquid in the filter 10 and the circuit immediately after the cleaning of the filter 10 can be removed as the waste liquid of the concentrator 20 in a short time. That is, dilution of the concentrated solution by the cleaning solution at the start and immediately after the cleaning of the filter as described above can be effectively prevented.
The above method (first method) is preferably employed when the maximum allowable differential pressure PM of the filter membrane-to-membrane differential pressure is larger than the maximum allowable differential pressure of the concentrator membrane-to-membrane differential pressure, but is not limited to this condition. The maximum allowable differential pressure PM of the filter membrane-to-membrane differential pressure can be used when it is smaller than the maximum allowable differential pressure of the concentrator membrane-to-membrane differential pressure. In addition, when the filter membrane-to-membrane differential pressure is greater than the maximum allowable differential pressure PM, when the filter membrane-to-membrane differential pressure is less than the minimum allowable differential pressure PL, and when the feed rate of the raw liquid to the filter 10 is constant regardless of the filter membrane-to-membrane differential pressure, the above steps 1 to 3 may be repeated to adjust the feed rate of the concentrated liquid to the concentrator 20.
< second method >
In the first method, the flow rate of the concentrate in the concentrate pipe 4 is adjusted based on the inter-membrane pressure difference between the concentrators, and the amount of the filtrate sent to the concentrator 20 can be adjusted based on the inter-membrane pressure difference between the concentrators as described below.
In addition, although the following description will be given of the case where the amount of the filtrate to be fed to the concentrator 20 is adjusted based on the inter-membrane differential pressure of the concentrator, steps 1 to 3 of the first method may be performed together with the adjustment of the amount of the filtrate to be fed to the concentrator 20. That is, the amount of the filtrate sent to the concentrator 20 may be adjusted based on the pressure difference between the membranes of the concentrator, and the flow rate of the concentrated solution in the concentrated solution pipe, that is, the concentration ratio of the concentrated solution may be adjusted.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the filtrate supply pipe liquid feeding unit 3p is operated so that the amount of liquid fed from the filtrate to the concentrator 20 (in other words, the amount of liquid fed from the raw liquid to the filter 10) increases. That is, the operation of the filtrate feed portion 3p of the filtrate feed pipe is controlled so as to increase the amount of the filtrate to be fed to the concentrator 20. The concentrate pipe liquid feeding portion 4p may be operated so that the amount of the filtrate fed to the concentrator 20 is increased and the concentration of the concentrate is increased.
< step 2>
Then, the amount of filtrate produced (in other words, the amount of feed liquid of the raw liquid to the filter 10) to be fed to the concentrator 20 is increased to a level at which the inter-membrane differential pressure of the concentrator is within the allowable differential pressure of the concentrator 20 (above the minimum allowable differential pressure and below the maximum allowable differential pressure). Then, if the inter-membrane differential pressure of the concentrator is within the allowable differential pressure of the concentrator 20, the operation of the filtrate supply pipe liquid feeding portion 3p is controlled so that the amount of the filtrate fed to the concentrator 20 is maintained at a flow rate at which the inter-membrane differential pressure of the concentrator is within the allowable differential pressure of the concentrator 20. In this case, the amount of the feed of the raw liquid to the filter 10 is deviated from the flow rate in a state where the differential pressure between the filter membranes is within the allowable differential pressure of the filter 10, but it is desirable to maintain the flow rate of the raw liquid within a range of the allowable flow rate (not less than the minimum allowable flow rate and not more than the maximum allowable flow rate). The concentrate pipe liquid feeding unit 4p may be operated so that the flow rate of the concentrate in the concentrate pipe 4 is maintained at a flow rate in a state where the inter-membrane differential pressure of the concentrator is within the allowable differential pressure of the concentrator 20.
< step 3>
If the inter-membrane differential pressure of the concentrator becomes greater than the maximum allowable differential pressure of the concentrator 20 due to clogging of the concentrator 20 or the like immediately after that, the operation of the filtrate feed pipe 3p is controlled so that the amount of filtrate fed to the concentrator 20 decreases. That is, the operation of the filtrate supply pipe liquid feeding portion 3p is controlled so that the amount of generated filtrate to be fed to the concentrator 20 is reduced. In this case, the amount of the feed liquid of the raw liquid to the filter 10 is also deviated from the flow rate at which the inter-membrane differential pressure of the filter is within the allowable differential pressure of the filter 10, but it is desirable to maintain the flow rate of the raw liquid within the allowable flow rate range. Further, the concentrate pipe liquid feeding portion 4p may be operated to decrease the concentration ratio (to decrease the concentration of the concentrate) while satisfying the allowable concentration ratio.
Since the inter-membrane pressure difference between the concentrators is reduced when the amount of feed of the filtrate to the concentrator 20 is reduced, when the inter-membrane pressure difference between the concentrators becomes smaller than the minimum allowable pressure difference of the concentrator 20, the filtrate feed pipe liquid feed portion 3p is operated again so that the flow rate of the raw liquid in the feed pipe 2 is increased.
That is, the above steps 1 to 3 are repeated until the inter-membrane differential pressure of the filter reaches the allowable differential pressure of the filter 10. This method can ensure the maximum filtration flow rate (i.e., the maximum allowable flow rate LM) and the maximum concentration ratio, which are not possible to achieve when the amount of liquid fed to the filter 10 and the concentrate bag CB is constant, according to the membrane area and the clogging state of the filtration membranes of the filter 10 and the concentrator 20, or according to the state of the raw liquid (the concentration of a substance causing clogging of the filter and the concentrator, the concentration of a collected useful substance, the viscosity of the liquid, and the like). That is, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated solution from a raw solution can be shortened, and the re-concentration operation can be avoided or the time required for the re-concentration operation can be shortened. Further, if the operation is performed as described above, at the start of the filtration concentration, the cleaning liquid filled in the filter 10, the concentrator 20, and the circuit, and the cleaning liquid in the filter 10 and the circuit immediately after the cleaning of the filter 10 can be removed as the waste liquid of the concentrator 20 in a short time. That is, dilution of the concentrated solution by the cleaning solution at the start and immediately after the cleaning of the filter as described above can be effectively prevented.
The above-described method (second method) is preferably employed when the maximum allowable differential pressure between the concentrator membranes is larger than the maximum allowable differential pressure between the filter membranes, but is not limited to this condition. The maximum allowable differential pressure between the concentrator membranes can be smaller than the maximum allowable differential pressure between the filter membranes. In addition, when the filter membrane-to-membrane differential pressure is greater than the maximum allowable differential pressure PM, when the filter membrane-to-membrane differential pressure is less than the minimum allowable differential pressure PL, and when the feed rate of the raw liquid to the filter 10 is kept constant regardless of the filter membrane-to-membrane differential pressure, the above steps 1 to 3 may be repeated to adjust the feed rate of the concentrated liquid to the concentrator 20.
< cleaning of Filter >
In the raw liquid treatment apparatus 1B according to embodiment 2, when the filtration and concentration operation is performed as described above, the filter-membrane differential pressure becomes larger than the maximum allowable differential pressure PM of the filter 10 due to clogging of the filter 10 or the like. In this case, if the flow rate of the raw liquid in the feed pipe 2 is reduced, the inter-filter-membrane differential pressure can be made smaller than the maximum allowable differential pressure PM of the filter 10, and the inter-filter-membrane differential pressure can be maintained within the allowable differential pressure (the range of the minimum allowable differential pressure PL to the maximum allowable differential pressure PM). However, if the clogging of the filter 10 or the like becomes serious, the flow rate of the raw liquid in the feed pipe 2 may be reduced to maintain the pressure difference between the filter membranes within the allowable pressure difference of the filter 10, and the flow rate of the raw liquid in the feed pipe 2 may become smaller than the minimum allowable flow rate LL. In this state, the operation of cleaning the filter 10 is performed in the middle of the filtering and concentrating operation of the raw liquid treatment apparatus 1 according to embodiment 2.
As shown in fig. 22, the flow rate adjusting mechanism 2c closes the liquid supply pipe 2 so that the liquid cannot flow. In addition, the operation of the filtrate supply pipe liquid feeding portion 3p and the concentrate pipe liquid feeding portion 4p is stopped to function as a jig. In the case where the filter cleaning is performed in the middle of the concentration and filtration operation, after the preparatory cleaning operation is completed, the cleaning liquid bag SB is connected to the other end of the cleaning liquid supply pipe 6 in place of the cleaning liquid recovery bag FB, and the cleaning liquid recovery bag FB is connected to the other end of the cleaning liquid recovery pipe 7 in place of the cleaning liquid bag SB.
In the above state, the cleaning liquid supply pipe liquid feeding portion 6p is operated so that the cleaning liquid flows from the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6 to the filter 10, and the cleaning liquid recovery pipe liquid feeding portion 7p is operated so that the cleaning liquid flows from the filter 10 to the cleaning liquid recovery bag FB connected to the cleaning liquid recovery pipe 7. This allows the cleaning liquid to flow through the hollow fiber membranes 16 in the direction opposite to the direction in which the raw liquid flows during filtration and concentration, and thus allows the cleaning liquid to clean the inside of the hollow fiber membranes 16.
After the preparation cleaning operation is completed, the cleaning liquid bag SB is connected to the other end of the connecting pipe 9 in place of the cleaning liquid recovery bag FB. Thus, if the liquid is caused to flow through the connecting pipe 9 by the flow rate adjusting mechanism 9c, the cleaning liquid can be supplied to the filter 10 from the cleaning liquid bag SB connected to the connecting pipe 9 in addition to the above state. Thus, the cleaning liquid supplied through the connection pipe 9 permeates the hollow fiber membranes 16 in the direction opposite to the direction in which the filtrate permeates the hollow fiber membranes 16, and therefore clogging of the hollow fiber membranes 16 can be eliminated. In this case, since the cleaning liquid is supplied to the filter 10 from both the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6 and the cleaning liquid bag SB connected to the connecting pipe 9, the flow rate of the cleaning liquid flowing through the cleaning liquid recovery pipe 7 through the cleaning liquid recovery pipe liquid feeding portion 7p is adjusted to be larger than the flow rate of the cleaning liquid flowing through the cleaning liquid supply pipe 6 through the cleaning liquid supply pipe liquid feeding portion 6 p.
In addition, when the liquid is caused to flow through the connecting pipe 9 by the flow rate adjusting mechanism 9c, the cleaning liquid recovery pipe liquid feeding portion 7p may be operated with the operation of the cleaning liquid supply pipe liquid feeding portion 6p stopped. In this case, the cleaning liquid is supplied to the filter 10 only from the cleaning liquid bag SB connected to the connecting pipe 9. In this case, the cleaning liquid also permeates the hollow fiber membranes 16 in the direction opposite to the direction in which the filtrate permeates the hollow fiber membranes 16, and therefore clogging of the hollow fiber membranes 16 can be eliminated.
In the case of using a filter having hollow fiber membranes 16 as the filter 10 as shown in fig. 5, it is desirable that the control unit 106 adjusts the supply amount and supply timing of the cleaning liquid to the filter 10 so that the above-described cleaning of the filter 10 and the concentrator 20 can be appropriately performed. That is, it is desirable to adjust the supply amount and supply timing of the cleaning liquid to be supplied to the filter 10 so that the cleaning liquid permeates the hollow fiber membranes 16 in a state where the hollow space 12h of the trunk portion 12 is filled with the cleaning liquid to fill the region of the hollow fiber membranes 16 where cleaning is performed.
< recovery of filtrate >
On the other hand, when the filter cleaning is performed in the above method, the filtrate remaining in the internal space 12h of the main body 11 of the filter 10 is mixed with the cleaning liquid and discharged. This reduces the amount of the active ingredient recovered by concentration by filtration.
Here, when the filter cleaning is performed, it is desirable to feed the filtrate existing in the internal space 12h of the main body 11 of the filter 10 to the concentrator 20 in advance and then perform the filter cleaning.
< recovery (outside) by cleaning liquid >
As shown in fig. 7, the port 11c of the body 11 of the filter 10 (the port 11c to which the filtrate supply tube 3 is not connected, hereinafter referred to as a cleaning port 11c) is connected to the cleaning solution bag SB via a tube. Next, the filtrate supply pipe liquid feeding unit 3p keeps the state where the liquid flows from the filter 10 to the concentrator 20, and the feed pipe 2 is closed by the flow rate adjusting mechanism 2c while the operation of the concentrate pipe liquid feeding unit 4p is kept continued. In this state, if the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10 by a pump provided in the pipe, the filtrate in the internal space 12h of the main body portion 11 of the filter 10 is supplied to the concentrator 20, and the cleaning liquid is relatively supplied from the cleaning bag SB to the internal space 12 h. When all the filtrate in the internal space 12h is replaced with the cleaning liquid immediately after the start, the operation of the filtrate supply pipe liquid feeding part 3p is stopped, the filtrate supply pipe 3 is closed, and the operation of the concentrate pipe liquid feeding part 4p is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the liquid feed pipe 2 is closed by the flow rate adjusting mechanism 2c to perform collection, but the liquid feed pipe 2 may be kept open to perform collection. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration.
It is sufficient to know whether or not all the filtrate in the internal space 12h has been replaced with the cleaning liquid by a method of measuring the amount of feed of a pump provided in a pipe connected to the cleaning port 11c and obtaining the amount theoretically or a method of measuring the concentration of the concentrated liquid. The concentration of the filtrate may be determined by observing the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a densitometer.
Further, a pump is not necessarily provided in the pipe connected to the cleaning port 11c of the main body 11 of the filter 10. Even in this case, by operating the filtrate supply pipe liquid feeding unit 3p, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be replaced with the cleaning liquid. When both the pump provided in the pipe connected to the cleaning port 11c and the filtrate supply pipe liquid feeding unit 3p are operated, both the pumps are operated so that the flow rates thereof become equal to each other.
< recovery by gas such as air >
In the above description, the case where the cleaning solution bag SB is connected to the cleaning port 11c of the main body portion 11 of the filter 10 via a pipe has been described, and a gas such as air may be supplied to the cleaning pipe 11c of the main body portion 11 of the filter 10 via a pipe.
In this case, the filtrate supply pipe liquid feeding unit 3p maintains the state where the liquid flows from the filter to the concentrator 20, and the feed pipe 2 is closed by the flow rate adjusting mechanism 2c while the operation of the concentrate pipe liquid feeding unit 4p is kept continued. In this state, if a gas such as air is supplied to the filter 10 from a pipe connected to the cleaning port 11c, the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20. When all the filtrate in the internal space 12h is discharged, the operation of the filtrate supply pipe liquid feeding part 3p is stopped to function as a jig, the filtrate supply pipe 3 is closed, and the operation of the concentrate pipe liquid feeding part 4p is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the liquid supply tube 2 is closed by the flow rate adjusting mechanism 2c to perform collection, and the liquid supply tube 2 may be kept open to perform collection. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration.
It is sufficient to know whether or not all the filtrate in the internal space 12 has been discharged by a method of providing a liquid detector or a bubble detector in the filtrate supply pipe 3, measuring the pressure in the filtrate supply pipe 3, or theoretically obtaining the amount of the filtrate fed by measuring the amount of the pump.
When the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the internal space 12h of the main body 11 of the filter 10 is filled with the gas such as air. Therefore, when the cleaning operation is performed after the recovery of the filtrate, it is desirable to perform the cleaning operation after the hollow space 12h of the body portion 12 is filled with the cleaning liquid to fill the region of the hollow fiber membranes 16 to be cleaned (or the entire hollow space 12h of the body portion 12).
< recovery into bag >
In the above example, the filtrate is sent to the concentrator 20 and recovered as a concentrated solution, but the filtrate may be recovered while remaining the filtrate. For example, a bag for recovering the filtrate is connected to the filtrate supply pipe 3 upstream of the filtrate supply unit 3p (i.e., on the filter 10 side). In this state, if a cleaning liquid, air, or other gas is supplied to the filter 10 from a pipe connected to the cleaning port 11c in a state in which the liquid is not allowed to flow through the filtrate supply pipe 3 by the filtrate supply pipe liquid feeding portion 3p, the filtrate in the internal space 12h of the main body portion 11 of the filter 10 can be recovered into the bag. In this case, the filtrate can be recovered in a shorter time than in the case where the filtrate is sent to the concentrator 20 and recovered in a state of a concentrated solution, and therefore, the shift to the cleaning operation can be performed quickly.
Further, the bag for recovering the filtrate is disposed on the upstream side of the filtrate supply pipe liquid feeding portion 3p, but may be disposed on the downstream side of the filtrate supply pipe liquid feeding portion 3p as long as it is on the front side of the concentrator 20. In this case, the filtrate can flow into the bag by operating the filtrate supply pipe liquid feeding portion 3p, and therefore, a pump may not be provided in the pipe connected to the cleaning port 11 c. On the other hand, it is necessary to provide a tool such as a clamp capable of closing and opening the tube on the upstream side of the bag and the tube connected to the cleaning port 11 c.
< recovery by cleaning liquid (inside) >
In the above description, the following is explained: the raw liquid is supplied to the through channels 16h of the plurality of hollow fiber membranes 16 of the hollow fiber membrane bundle 15 of the filter 10, and the filtrate is discharged into the internal space 12h of the body portion 12 of the body portion 11 of the filter 10. However, the raw liquid may be supplied from the filtrate discharge port 11c into the internal space 12h of the body portion 12 of the body portion 11, and the filtrate obtained by filtration may be discharged into the through channels 16h of the plurality of hollow fiber membranes 16 of the hollow fiber membrane bundle 15 and discharged from the raw liquid supply port 11a to the outside.
In this case, the pipes and the like are connected as described below.
First, the filtrate supply pipe 3 is connected to the raw liquid supply port 11a, and the liquid supply pipe 2 is connected to the port 11c (i.e., the above-described cleaning port 11 c). The cleaning liquid supply pipe 6 is connected to a port 11c to which the liquid feed pipe 2 is not connected (i.e., the filtrate discharge port 11c described above), and a cleaning liquid bag SB once connected to the cleaning port 11c is connected to the cleaning liquid supply port 11 b.
The filtrate supply pipe liquid feeding unit 3p maintains the state where the liquid flows from the filter 10 to the concentrator 20, and the feed pipe 2 is closed by the flow rate adjusting mechanism 2c while the operation of the concentrate pipe liquid feeding unit 4p is continued. In this state, when the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10 by a pump provided in a pipe connected to the cleaning liquid supply port 11b, the filtrate in the through flow path 16h of the hollow fiber membranes 16 of the filter 10 is supplied to the concentrator 20, and the cleaning liquid is relatively supplied from the cleaning liquid bag SB to the through flow path 16 h. When all the filtrate in the through-flow passage 16h is replaced with the cleaning liquid immediately after the start of the operation, the operation of the filtrate supply pipe feeding part 3p is stopped, the filtrate supply pipe 3 is closed, and the operation of the concentrate pipe feeding part 4p is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the liquid supply tube 2 is closed by the flow rate adjusting mechanism 2c to perform collection, and the liquid supply tube 2 may be kept open to perform collection. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration.
It is sufficient to know whether or not all the filtrate in the internal space 12h has been replaced with the cleaning liquid by a method of measuring the amount of feed of a pump provided in a pipe connected to the cleaning port 11c and obtaining the amount theoretically or a method of measuring the concentration of the concentrated liquid. The concentration of the filtrate may be determined by observing the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a densitometer.
< recovery by gas such as air >
In the above description, the case where the cleaning liquid bag SB is connected to the cleaning liquid supply port 11b of the main body portion 11 of the filter 10 via a pipe has been described, but a gas such as air may be supplied to the cleaning liquid supply port 11b of the main body portion 11 of the filter 10 via a pipe.
In this case, the feed pipe 2 is closed by the flow rate adjusting mechanism 2c while the liquid is maintained in a state of flowing from the filter 10 to the concentrator 20 by the filtrate supply pipe liquid feeding portion 3 p. In this state, if a gas such as air is supplied from a pipe to the filter 10, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 can be supplied to the concentrator 20. When all the filtrate in the through flow path 16h of the hollow fiber membrane 16 is discharged soon, the operation of the filtrate supply pipe liquid feeding part 3p is stopped to function as a jig, the filtrate supply pipe 3 is closed, and the operation of the concentrate pipe liquid feeding part 4p is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the liquid supply tube 2 is closed by the flow rate adjusting mechanism 2c to perform collection, and the liquid supply tube 2 may be kept open to perform collection. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration.
It is sufficient to know whether or not all the filtrate in the through flow channel 16h of the hollow fiber membrane 16 has been discharged by a method of providing a liquid detector or a bubble detector in the filtrate supply pipe 3, measuring the pressure in the filtrate supply pipe 3, or measuring the amount of feed of a pump to theoretically obtain the amount of feed.
When the filtrate in the through-flow channel 16h of the hollow fiber membrane 16 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the through-flow channel 16h of the hollow fiber membrane 16 of the filter 10 is filled with the gas such as air. Therefore, when the cleaning operation is performed after the filtrate is collected, it is desirable to perform the cleaning operation after the through-flow channel 16h is filled with the cleaning liquid in advance in a state where the region of the hollow fiber membranes 16 to be cleaned (or the entire hollow fiber membranes 16) is filled with the cleaning liquid.
< recovery into bag >
In the above example, the filtrate is sent to the concentrator 20 and recovered as a concentrated solution, but the filtrate may be recovered while remaining the filtrate. For example, a bag for recovering the filtrate is connected to the filtrate supply pipe 3 upstream of the filtrate supply unit 3p (i.e., on the filter 10 side). In this state, if the liquid is supplied to the filter 10 from the cleaning liquid supply port 11b in a state where the liquid is caused to flow through the filtrate supply pipe 3 by the filtrate supply pipe feeding portion 3p, and the cleaning liquid, air, or other gas is supplied to the filter 10 as described above, the filtrate in the through flow path 16h of the hollow fiber membranes 16 of the filter 10 can be recovered. In this case, the filtrate can be recovered in a shorter time than in the case where the filtrate is sent to the concentrator 20 and recovered in a state of a concentrated solution, and therefore, the shift to the cleaning operation can be performed quickly.
The bag for recovering the filtrate may be disposed upstream of the filtrate supply pipe liquid-feeding portion 3p, or may be disposed downstream of the filtrate supply pipe liquid-feeding portion 3p before the concentrator 20. In this case, the filtrate can flow into the bag by operating the filtrate supply pipe liquid feeding portion 3p, and therefore, a pump may not be provided in the pipe connected to the cleaning port 11 c. Instead, a tool such as a clamp that can close and open the tube needs to be provided on the upstream side of the bag and the tube connected to the cleaning port 11 c.
< Another example of the method for recovering liquid in Filter 10 >
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and the filtrate is recovered as a concentrated solution, it is desirable to adjust the flow rate at the time of sending the filtrate to the concentrator 20 based on the inter-membrane pressure difference between the concentrators of the concentrator 20. By adopting such a method, even if the concentrator 20 is clogged, the treatment for preventing the increase in the pressure difference between the membranes of the concentrator can be prevented from being stopped, and therefore the filtrate in the filter 10 can be efficiently recovered.
For example, when the flow rate at the time of feeding the liquid to the concentrator 20 is adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rate can be adjusted as follows. First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the filtrate supply pipe liquid feeding unit 3p and the operation of the concentrate pipe liquid feeding unit 4p are controlled to maintain the liquid feeding amount from the filter 10 to the concentrator 20. This prevents the occurrence of problems such as the pressure difference between membranes of the concentrator greatly falling within the range of the set pressure difference.
On the other hand, when the pressure difference between the concentrator membranes of the concentrator 20 is larger than the maximum set pressure difference, the operation of the filtrate supply pipe liquid feeding section 3p and the operation of the concentrate pipe liquid feeding section 4p are controlled so that the amount of liquid fed from the filter 10 to the concentrator 20 is reduced. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is smaller than the minimum set differential pressure, the operation of the filtrate supply pipe liquid feeding section 3p and the operation of the concentrate pipe liquid feeding section 4p are controlled so that the amount of liquid fed from the filter 10 to the concentrator 20 increases. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
< Another example of the method for recovering liquid in Filter 10 >
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and the filtrate is recovered as the concentrate, the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB, that is, the concentration ratio may be adjusted based on the inter-membrane pressure difference between the concentrators of the concentrator 20. In this method, while suppressing an increase in the inter-membrane differential pressure of the concentrator, the rate of feeding the concentrated solution from the filter 10 to the concentrator 20 can be kept constant without changing the flow rate, and therefore the filtrate in the filter 10 can be recovered efficiently.
For example, when the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB are adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rates can be adjusted as follows.
First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the filtrate supply pipe liquid sending part 3p is controlled so as to maintain the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB. This prevents the occurrence of problems such as the pressure difference between membranes of the concentrator greatly falling within the range of the set pressure difference.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is greater than the maximum set differential pressure, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the filtrate supply pipe liquid sending part 3p is controlled so that the flow rate from the concentrator 20 to the concentrate bag CB increases and/or the flow rate from the concentrator 20 to the waste bag DB decreases. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is smaller than the minimum set differential pressure, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the filtrate supply pipe liquid sending part 3p is controlled so that the flow rate from the concentrator 20 to the concentrate bag CB decreases and/or the flow rate from the concentrator 20 to the waste bag DB increases. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
The set differential pressure of the pressure difference between the membranes of the concentrator when the filtrate in the filter 10 is recovered may be the same as the allowable differential pressure in the filtration and concentration operation, or may be a value different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the range of the set differential pressure may be set to be larger than the range of the allowable differential pressure. In this case, it is desirable that the concentrated solution can be recovered to the end as much as possible even in a diluted state. Further, the range of the allowable differential pressure and the range of the set differential pressure may be different from each other.
< reconcentration operation >
When the concentrated solution obtained by the filtering and concentrating operation is further concentrated, a re-concentrating operation is performed.
As shown in fig. 8, in the reconcentration operation of the raw liquid treatment apparatus 1B according to embodiment 2, the other end of the connecting tube 9 is removed from the cleaning liquid bag SB, and the other end of the connecting tube 9 is connected to the concentrated liquid bag CB.
The flow rate adjusting mechanism 9c maintains a state in which the liquid can flow in the connecting pipe 9, and the cleaning liquid supply pipe liquid feeding portion 6p and the cleaning liquid recovery pipe liquid feeding portion 7p are not operated to function as a jig. In addition, the flow rate adjusting mechanism 2c closes the liquid supply pipe 2 so that the liquid cannot flow. This prevents the liquid from flowing through the filter 10.
In the above state, the filtrate supply pipe liquid feeding part 3p is operated so that the concentrated liquid flows from the concentrated liquid bag CB to the concentrator 20 through the connecting pipe 9, and the concentrated liquid pipe liquid feeding part 4p is operated so that the concentrated liquid flows from the concentrator 20 to the concentrated liquid bag CB through the concentrated liquid pipe 4.
Thereby, the concentrated liquid is supplied from the concentrated liquid bag CB connected to the connection pipe 9 to the concentrator 20 through the connection pipe 9, and thus the re-concentrated liquid further concentrated by the concentrator 20 is recovered to the concentrated liquid bag CB through the concentrated liquid pipe 4. On the other hand, the moisture separated from the concentrated solution is recovered to the waste liquid bag DB through the waste liquid pipe 5. That is, a concentrated solution (reconcentrated solution) having an increased concentration ratio can be obtained.
< Re-concentration operation Using differential pressure between membranes in concentrator >
In the re-concentration operation, the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB, that is, the re-concentration ratio can be adjusted based on the inter-concentrator-membrane differential pressure of the concentrator 20. In this method, the effect of reducing the time required to produce a concentrated solution having a high concentration can be obtained while suppressing the increase in the pressure difference between the membranes of the concentrator.
In this case, when the re-concentration operation using the pressure difference between the membranes of the concentrator is performed in advance, it is desirable to set the allowable pressure difference. That is, the differential pressure (allowable differential pressure) that can be allowed by the concentrator 20 is set in accordance with the concentrator 20. The allowable differential pressure may have a predetermined magnitude or may be set to a specific value. In the following description, the allowable differential pressure is typically a case having a predetermined width.
In addition, when the re-concentration operation is performed using the pressure difference between the filter membranes, it is desirable to set the allowable flow rate in advance. That is, it is desirable to set the allowable flow rate (allowable flow rate) of the concentrated solution in the filtrate supply pipe 3. The allowable flow rate may have a predetermined magnitude or may be set to a specific value. The allowable flow rate does not necessarily have to be set. However, if the flow rate of the concentrated liquid in the filtrate supply line 3 is too low, the time required for reconcentration becomes too long. Therefore, it is desirable to set the allowable flow rate in advance in order to prevent the treatment time of the concentrated solution from increasing.
Further, when the re-concentration operation using the pressure difference between the membranes of the concentrator is performed, it is desirable to set the allowable concentration ratio in advance. That is, it is desirable to set the ratio (allowable concentration ratio) of the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4 to the flow rate of the concentrated liquid in the filtrate supply pipe 3 (in other words, in the connecting pipe 9). The allowable concentration ratio may have a predetermined width or may be set to a specific value. The allowable concentration ratio is not necessarily set. However, if the concentration ratio, which is the ratio of the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4 to the flow rate of the concentrated liquid in the filtrate supply pipe 3, is too low (i.e., the flow rate of the concentrated liquid becomes too large), the concentration efficiency deteriorates, and therefore, a time for the re-concentration process is required. Thus, it is desirable to set the permissible concentration ratio in advance, while preventing an excessive decrease in the concentration ratio. The allowable concentration ratio in the re-concentration operation may be the same as the allowable concentration ratio in the filtration concentration or may be different from the allowable concentration ratio in the filtration concentration.
At the start of the re-concentration, the filtrate supply pipe feeding portion 3p is operated so as to increase the amount of the concentrated solution fed to the concentrator 20. At this time, the concentrate-pipe liquid feeding portion 4p is operated so that the concentrate has a predetermined concentration ratio in accordance with the flow rate of the filtrate in the filtrate supply pipe 3. For example, when a concentrated solution having a concentration ratio of 10 times is to be produced, the operation of the concentrated solution pipe feed portion 4p may be adjusted so that the flow rate of the concentrated solution flowing through the concentrated solution pipe 4 becomes 1/10 of the flow rate of the filtrate flowing through the filtrate supply pipe 3. In addition, instead of the concentration ratio of the concentrated liquid, the operation of the concentrated liquid pipe feed portion 4p may be adjusted so that the pressure difference between the concentrator membranes becomes a set value within the allowable differential pressure (or maintained within the allowable differential pressure), or so that the pressure difference between the concentrator membranes becomes a set value within the allowable differential pressure (or maintained within the allowable differential pressure) while the concentrated liquid is maintained at a predetermined concentration ratio. While the amount of the concentrated liquid sent to the concentrator 20 is increased, the operation of the concentrated liquid pipe sending part 4p is controlled so as to be in any of the above states.
When the re-concentration progresses, clogging of the concentrator 20 gradually occurs. This increases the inter-membrane differential pressure of the concentrator. However, the filtrate supply pipe liquid feeding portion 3p is operated so as to increase the amount of the concentrated liquid fed to the concentrator 20 until the inter-membrane differential pressure of the concentrator reaches the allowable differential pressure.
< first method >
The increase in the amount of the filtrate fed to the concentrator 20 is continued until the inter-membrane differential pressure of the concentrator reaches the allowable differential pressure of the concentrator 20. The filtrate feed portion 3p of the filtrate supply pipe is controlled so as to maintain the flow rate of the concentrated solution to the concentrator 20 in a state where the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. On the other hand, the concentrate pipe liquid feeding portion 4p is operated as follows based on the pressure difference between the membranes of the concentrator, and the flow rate of the concentrate flowing through the concentrate pipe 4 is adjusted.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the allowable differential pressure of the concentrator 20, the concentrate pipe liquid feeding unit 4p is operated to reduce the amount of the concentrated liquid fed to the concentrated liquid bag CB. That is, the operation of the concentrate-pipe liquid feeding portion 4p is controlled so as to increase the concentration of the concentrate.
< step 2>
Then, the amount of the concentrated solution sent to the concentrated solution bag CB is reduced until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. If the inter-membrane pressure difference of the concentrator is within the allowable pressure difference of the concentrator 20, the concentrate pipe liquid feeding part 4p is controlled so that the flow rate of the concentrate in the concentrate pipe 4 is maintained at a flow rate at which the inter-membrane pressure difference of the concentrator is within the allowable pressure difference of the concentrator 20.
< step 3>
When the pressure difference between the concentrator membranes becomes larger than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like immediately after that, the concentrate pipe feed portion 4p is controlled so that the feed amount of the concentrate to the concentrate bag CB is increased. Further, although the concentration ratio decreases as the amount of the concentrated solution fed increases, the operation of the concentrated solution pipe feed portion 4p is controlled so as to decrease the concentration ratio (so as to decrease the concentration of the concentrated solution) while satisfying the allowable concentration ratio.
When the liquid feed amount of the concentrated solution is increased to maintain the pressure difference between the membranes of the concentrator within the allowable pressure difference and the concentration ratio becomes smaller than the allowable concentration ratio, the following method (second method) can be used to cope with this.
When the amount of the concentrated liquid fed to the concentrated liquid bag CB increases, the inter-membrane differential pressure of the concentrator decreases, and therefore, when the inter-membrane differential pressure of the concentrator becomes smaller than the minimum allowable differential pressure of the concentrator 20, the concentrated liquid pipe feeding portion 4p is operated again to decrease the amount of the concentrated liquid fed to the concentrated liquid bag CB.
That is, the above steps 1 to 3 are repeated until the pressure difference between the membranes of the thickener falls within the allowable pressure difference of the thickener 20. This method makes it possible to secure the maximum concentration ratio corresponding to the membrane area and the clogging state of the filtration membrane of the concentrator 20 or the state of the raw liquid (the concentration of the substance causing clogging of the filter and the concentrator, the concentration of the collected useful substance, the viscosity of the liquid, etc.) which cannot be achieved when the amount of liquid fed to the concentrate bag CB is constant. That is, by increasing the concentration efficiency, the time required to produce a concentrated solution having a high concentration can be shortened, and the time required for the re-concentration operation can be shortened.
< second method >
In the first method, the flow rate of the concentrated liquid in the concentrated liquid pipe 4 is adjusted based on the inter-membrane pressure difference between the concentrators, and the liquid feed amount of the concentrated liquid in the connecting pipe 9 can be adjusted based on the inter-membrane pressure difference between the concentrators as described below.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the allowable differential pressure (minimum allowable differential pressure) of the concentrator 20, the filtrate supply pipe liquid feeding unit 3p is operated so as to increase the amount of the concentrated liquid fed to the concentrator 20.
< step 2>
Then, the amount of the concentrated solution to be sent to the concentrator 20 is increased until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. Then, if the inter-membrane differential pressure of the concentrator is within the allowable differential pressure of the concentrator 20, the operation of the filtrate supply pipe liquid feeding portion 3p is controlled so that the amount of the concentrated liquid fed to the concentrator 20 is maintained at a flow rate at which the inter-membrane differential pressure of the concentrator is within the allowable differential pressure of the concentrator 20. In this case, it is desirable to maintain the amount of the concentrated liquid fed to the concentrator 20 within a range of an allowable flow rate (not less than the minimum allowable flow rate and not more than the maximum allowable flow rate).
< step 3>
When the pressure difference between the concentrator membranes becomes larger than the allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like, the filtrate supply pipe feeding portion 3p is controlled so that the amount of the concentrated solution fed to the concentrator 20 is reduced. That is, the operation of the filtrate supply pipe liquid feeding portion 3p is controlled so that the flow rate of the filtrate supplied to the concentrator 20 is reduced. In this case, it is also desirable that the amount of the concentrated liquid to be sent to the concentrator 20 be maintained within the allowable capacity.
Since the inter-membrane differential pressure of the concentrator decreases as the amount of the concentrated liquid fed to the concentrator 20 decreases, when the inter-membrane differential pressure of the concentrator becomes smaller than the minimum allowable differential pressure of the concentrator 20, the filtrate feed pipe liquid feeding unit 3p is operated again to increase the flow rate of the concentrated liquid in the filtrate feed pipe 3.
That is, the above steps 1 to 3 are repeated while the pressure difference between the concentrator membranes is within the allowable pressure difference of the concentrator 20. This method makes it possible to secure the maximum recirculation flow rate and the maximum concentration ratio corresponding to the membrane area and the clogged state of the filtration membrane of the concentrator 20 or the state of the raw liquid (the concentration of the substance causing clogging of the filter and the concentrator, the concentration of the collected useful substance, the viscosity of the liquid, etc.) which cannot be achieved when the amount of liquid fed to the concentrator 20 is constant. That is, by improving the recycling efficiency and the concentration efficiency, the time for generating a concentrated solution having a high concentration can be shortened, and the time taken for the re-concentration operation can be shortened.
Further, if the operation is performed as described above, the concentrator 20 immediately after the filter 10 is cleaned and the cleaning liquid in the circuit can be removed as the waste liquid of the concentrator 20 in a short time. That is, dilution of the concentrated solution by the cleaning solution immediately after the cleaning of the filter as described above can be effectively prevented.
The allowable differential pressure of the pressure difference between the membranes of the thickener at the time of re-concentration may be the same as the allowable differential pressure in the filtration and concentration operation, or may be a value (range) different from the allowable differential pressure in the filtration and concentration operation. For example, when the allowable differential pressure in the filtering concentration operation has a certain range, the allowable differential pressure in the re-concentration operation may be set to a range wider than this range. In this case, when the filter 10 is used to treat a raw liquid having a property of being easily clogged, the filter 10 is slowly treated so as not to apply pressure to the filter 10 during the filtering operation, but it is desired to generate a concentrated liquid having a high concentration and shorten the re-concentration time. In addition, when the range of the allowable differential pressure during the re-concentration is made narrower than the range of the allowable differential pressure during the filtering and concentrating operation, when the concentrator 20 treats the raw liquid having a property of being easily clogged, the raw liquid is treated in a short time without applying pressure to the concentrator 20 during the filtering and concentrating operation, and it is desirable that a concentrated liquid having a high concentration can be produced by the re-concentration operation. Further, the range of the allowable differential pressure in the filtering concentration operation may be different from the range of the allowable differential pressure in the re-concentration operation.
The allowable concentration ratio at the time of re-concentration may be the same as the allowable concentration ratio in the filtering and concentrating operation, or may be a value (range) different from the allowable concentration ratio in the filtering and concentrating operation. For example, when the allowable concentration ratio in the filtering concentration operation is within a certain range, the range of the allowable concentration ratio in the re-concentration operation may be set to be larger than this range. In this case, it takes time to perform concentration in the filtration concentration operation, and it is desired to shorten the time for the re-concentration operation. In addition, when the range of the allowable concentration ratio in the re-concentration is set to be narrower than the range of the allowable concentration ratio in the filtering and concentrating operation, it takes time to perform the concentration in the re-concentration operation, and it is desirable to be able to quickly end the filtering and concentrating operation. Further, the range of the allowable concentration ratio in the filtering concentration operation and the range of the allowable concentration ratio in the re-concentration operation may be different from each other.
< example of method for recovering liquid in Filter 10 >
Before the above-described re-concentration operation is performed, the filtrate in the filter 10 is sent to the concentrator 20, and the filtrate is recovered as a concentrated solution. In this case, it is desirable to adjust the flow rate when the liquid is sent to the concentrator 20 based on the pressure difference between the concentrator membranes of the concentrator 20. By adopting such a method, even if the concentrator 20 is clogged, the increase of the pressure difference between the membranes of the concentrator can be suppressed, and the stop of the treatment can be prevented, so that the filtrate in the filter 10 can be efficiently recovered.
For example, when the flow rate at the time of feeding the liquid to the concentrator 20 is adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rate can be adjusted as follows. First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the filtrate supply pipe liquid feeding unit 3p and the operation of the concentrate pipe liquid feeding unit 4p are controlled to maintain the liquid feeding amount from the filter 10 to the concentrator 20. This prevents the occurrence of problems such as the pressure difference between membranes of the concentrator greatly falling within the range of the set pressure difference.
On the other hand, when the pressure difference between the concentrator membranes of the concentrator 20 is larger than the maximum set pressure difference, the operation of the filtrate supply pipe liquid feeding section 3p and the operation of the concentrate pipe liquid feeding section 4p are controlled so that the amount of liquid fed from the filter 10 to the concentrator 20 is reduced. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is smaller than the minimum set differential pressure, the operation of the filtrate supply pipe liquid feeding section 3p and the operation of the concentrate pipe liquid feeding section 4p are controlled so that the amount of liquid fed from the filter 10 to the concentrator 20 increases. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
< Another example of the method for recovering liquid in Filter 10 >
When the filtrate in the filter 10 is sent to the concentrator 20 and recovered as a concentrated solution, the flow rate from the concentrator 20 to the concentrated solution bag CB and/or the flow rate from the concentrator 20 to the waste solution bag DB, that is, the concentration ratio may be adjusted based on the inter-membrane pressure difference between the concentrators of the concentrator 20. In this method, the filtrate in the filter 10 can be efficiently recovered without changing the flow rate of the liquid sent from the filter 10 to the concentrator 20 and without increasing the pressure difference between the membranes of the concentrator.
For example, when the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB are adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rates can be adjusted as follows.
First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the filtrate supply pipe liquid sending part 3p is controlled so as to maintain the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste bag DB. This prevents the occurrence of problems such as the pressure difference between membranes of the concentrator greatly falling within the range of the set pressure difference.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is greater than the maximum set differential pressure, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the filtrate supply pipe liquid sending part 3p is controlled so that the flow rate from the concentrator 20 to the concentrate bag CB increases and/or the flow rate from the concentrator 20 to the waste bag DB decreases. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment.
On the other hand, when the inter-concentrator-membrane differential pressure of the concentrator 20 is smaller than the minimum set differential pressure, the operation of the concentrate pipe liquid sending part 4p (the operation of the waste pipe liquid sending part 5p in the case where the waste pipe liquid sending part 5p is provided) or the operation of the filtrate supply pipe liquid sending part 3p is controlled so that the flow rate from the concentrator 20 to the concentrate bag CB decreases and/or the flow rate from the concentrator 20 to the waste bag DB increases. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
The set differential pressure of the pressure difference between the membranes of the concentrator when the filtrate in the filter 10 is recovered may be the same as the allowable differential pressure in the filtration and concentration operation, or may be a value (range) different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the range of the set differential pressure may be set to be larger than the range of the allowable differential pressure. In this case, it is desirable that the concentrated solution can be recovered to the end as much as possible even in a diluted state. In addition, when the range of the set differential pressure is set to be smaller than the range of the allowable differential pressure, it is desirable that the concentrated solution is recovered to the end as much as possible without diluting the concentrated solution even if it takes time. Further, the range of the allowable differential pressure and the range of the set differential pressure may be different from each other.
< operation for collecting concentrator 20 >
When the concentrate in the concentrator 20 is also recovered after the raw liquid and the filtrate in the filter 10 are recovered, only a cleaning liquid or a fluid called a gas (hereinafter, simply referred to as a fluid) may be made to flow in the concentrator 20, and the concentrate or the like may be further recovered. However, as in the above case, the flow rate of the fluid supplied to the concentrated solution 20 may be adjusted while measuring the inter-membrane differential pressure of the concentrator. This prevents problems such as an increase in the pressure difference between the membranes of the concentrator and the inability to continue the treatment. If the inter-concentrator-membrane differential pressure of the concentrator 20 is greater than the set differential pressure, the problem of the inter-concentrator-membrane differential pressure continuing to rise can be prevented by stopping the liquid feed (including the gas flow) from the filter 10 to the concentrator 20.
The set differential pressure (second set differential pressure) between the concentrator membranes when the concentrated solution in the concentrator 20 is recovered may be the same as the allowable differential pressure during the filtration and concentration operation or the set differential pressure (first set differential pressure) when the filtrate in the filter 10 is recovered, or may be a value (range) different from these. For example, when the allowable differential pressure and the first set differential pressure have a certain range, the range of the second set differential pressure may be set to be larger than the range of the allowable differential pressure and the first set differential pressure. In this case, it is desirable that the concentrated solution can be recovered to the end as much as possible even in a diluted state. In addition, when the range of the second set differential pressure is set to be smaller than the range of the allowable differential pressure and the first set differential pressure, it is desirable that the concentrated solution is recovered to the end as much as possible without diluting the concentrated solution even if it takes time. Further, the range of the second set differential pressure may be different from the range of the allowable differential pressure and the range of the first set differential pressure.
< operation for collecting liquid in filtrate supply pipe 3 >
After the recovery of the concentrated liquid in the concentrator 20, when the pressure difference between the concentrator membranes reaches a set pressure difference or a predetermined liquid amount is recovered, the liquid feed (including the gas flow) from the filter 10 to the concentrator 20 may be stopped, and then a gas such as air may be supplied to the filtrate supply pipe 3. This prevents the concentrated solution in the concentrator 20 or the concentrated solution channel 4 and the liquid in the channel on the downstream side of the filtrate supply pipe 3 from being recovered and left over. If the inter-membrane differential pressure of the concentrator does not reach the set differential pressure, the liquid feed from the filter 10 to the concentrator 20 does not necessarily have to be stopped.
< stock solution treatment apparatus 1C of embodiment 3 >
In the raw liquid treatment apparatus 1B according to embodiment 2 described above, the filtrate supply pipe 3 is provided with a filtrate supply pipe liquid feeding unit 3p, and the raw liquid is sucked out from the filter 10 at the time of filtration and concentration. In the case of such a configuration, the waste-pipe liquid sending unit 5p may be provided in the waste pipe 5 instead of the filtrate-supply-pipe liquid sending unit 3p being provided in the filtrate supply pipe 3 (see fig. 10 to 12).
In the raw liquid treatment apparatus 1C, the concentrate-pipe liquid sending part 4p and the waste-pipe liquid sending part 5p are operated to flow the liquid (filtrate) from the filter 10 to the concentrator 20 at the time of filtration and concentration. When the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p are operated, the filtrate supply pipe 3 becomes a negative pressure, and the inside of the filter 10 (for example, the internal space 12h of the body 12 of the body 11) also becomes a negative pressure. Thus, if the liquid feed pipe 2 is set in a state capable of feeding liquid in advance by the flow rate adjustment mechanism 2c, the raw liquid in the raw liquid bag UB can be sucked into the filter 10 through the liquid feed pipe 2, and the sucked raw liquid can be sucked into the filtrate supply pipe 3.
In the raw liquid processing apparatus 1C, if the operation of the flow rate adjusting mechanism and the liquid sending unit provided in each pipe is adjusted by appropriately changing the bag connected to each pipe, the preparatory cleaning operation, the filtering concentration operation, and the re-concentration operation can be performed.
< preparation for cleaning operation >
As shown in fig. 10, in the preparatory cleaning operation of the raw liquid treatment apparatus 1C according to embodiment 3, a cleaning liquid bag SB is connected to the other end of the concentrate pipe 4 in place of the concentrate bag CB, and a cleaning liquid recovery bag FB is connected to the other end of the waste pipe 5 in place of the waste bag DB. The other end of the waste liquid pipe 5 may be connected to the waste liquid bag DB, or may be simply disposed in a bucket or the like.
Further, a cleaning liquid recovery bag FB is also connected to the other end of the liquid feed pipe 2 in place of the raw liquid bag UB. The other end of the liquid supply tube 2 may be connected to the waste liquid bag DB, or the other end of the liquid supply tube 2 may be simply disposed in a tub or the like.
The other end of the connection pipe 9 is also connected to a cleaning liquid recovery bag FB. The other end of the connecting pipe 9 may be connected to the waste liquid bag DB, or the other end of the connecting pipe 9 may be simply disposed in a tub or the like.
Further, the cleaning liquid recovery bag FB is connected to the other end of the cleaning liquid supply tube 6 in place of the cleaning liquid bag SB, and the cleaning liquid bag SB is connected to the other end of the cleaning liquid recovery tube 7 in place of the cleaning liquid recovery bag FB. The waste liquid bag DB may be connected to the other end of the cleaning liquid supply pipe 6, or the other end of the cleaning liquid supply pipe 6 may be simply disposed in a tub or the like.
Next, the cleaning liquid is made to flow through the liquid supply pipe 2 and the connecting pipe 9 by the flow rate adjusting mechanism 2c and the flow rate adjusting mechanism 9 c.
In this state, the concentrate pipe liquid sending part 4p is operated to flow the cleaning liquid from the cleaning liquid bag SB connected to the concentrate pipe 4 to the concentrate 20. Thereby, the cleaning liquid is supplied from the cleaning liquid bag SB connected to the concentrate pipe 4 to the concentrator 20 through the concentrate pipe 4. The supplied cleaning liquid passes through the concentrator 20, and is then collected into the cleaning liquid collection bag FB connected to the connection pipe 9 through the filtrate supply pipe 3 and the connection pipe 9. Further, if the waste-tube liquid sending part 5p is operated so that the liquid flows from the concentrator 20 to the cleaning-liquid recovery bag FB, a part of the cleaning liquid is recovered to the cleaning-liquid recovery bag FB connected to the other end of the waste tube 5 through the waste tube 5.
Further, the cleaning liquid recovery pipe liquid feeding portion 7p is operated to flow the cleaning liquid from the cleaning liquid bag SB connected to the cleaning liquid recovery pipe 7 to the filter 10. Thereby, a part of the cleaning liquid is supplied from the cleaning liquid bag SB connected to the cleaning liquid recovery pipe 7 to the filter 10 through the cleaning liquid recovery pipe 7. The cleaning liquid supplied to the filter 10 passes through the filter 10, and then is collected into the cleaning liquid collection bag FB connected to the connection pipe 9 through the filtrate supply pipe 3 and the connection pipe 9. Further, by operating the cleaning liquid supply pipe liquid feeding portion 6p, a part of the cleaning liquid supplied to the filter 10 can be also made to flow into the cleaning liquid supply pipe 6. Further, a part of the cleaning liquid is collected from the cleaning liquid collection tube 7 to the cleaning liquid collection bag FB connected to the liquid supply tube 2 through the liquid supply tube 2.
This enables the cleaning liquid to flow through the filter 10, the concentrator 20, and all the pipes, and thus the entire raw liquid treatment apparatus 1C according to embodiment 3 can be cleaned.
< filtration and concentration operation >
When the preparation cleaning operation is finished, the filtration and concentration operation is performed.
As shown in fig. 11, in the filtering concentration operation of the raw liquid treatment apparatus 1C according to embodiment 3, from the state in which the cleaning operation is prepared, the concentrate bag CB is connected to the other end of the concentrate pipe 4 instead of the cleaning liquid bag SB, and the waste liquid bag DB is connected to the other end of the waste pipe 5 instead of the cleaning liquid recovery bag FB.
On the other hand, the raw liquid bag UB is connected to the other end of the liquid feed pipe 2 in place of the cleaning liquid recovery bag FB.
The flow rate adjusting mechanism 2c is opened to maintain a state in which the liquid can flow in the liquid supply pipe 2, while the flow rate adjusting mechanism 9c is closed to prevent the liquid from flowing in the connecting pipe 9. In addition, the cleaning liquid recovery pipe liquid feeding portion 7p and the cleaning liquid supply pipe liquid feeding portion 6p are not operated and function as jigs.
In the above state, the concentrate-pipe liquid sending part 4p is operated so that the concentrate flows from the concentrator 20 to the concentrate bag CB, and the waste-pipe liquid sending part 5p is operated so that the waste liquid flows from the concentrator 20 to the waste-bag DB.
Thereby, the raw liquid is supplied from the raw liquid bag UB to the filter 10 through the liquid feed pipe 2. The supplied raw liquid is filtered by the filter 10, and the generated filtrate is supplied to the concentrator 20 through the filtrate supply pipe 3. Then, the filtrate supplied to the concentrator 20 is concentrated by the concentrator 20, and the resulting concentrated solution is collected into the concentrated solution bag CB through the concentrated solution pipe 4. On the other hand, the moisture separated from the concentrated solution is recovered to the waste liquid bag DB through the waste liquid pipe 5.
< operation of filtration and concentration >
Here, in the filtering and concentrating operation, the operation of the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p is controlled so that the concentration ratio falls within a predetermined range. However, as described below, the operation of the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p, that is, the flow rates of the liquids in the concentrate pipe 4 and the waste pipe 5 may be controlled by the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure. This enables filtration and concentration to be performed by effectively utilizing the capabilities of the filter 10 and the concentrator 20, and therefore, the time required for producing a concentrated solution can be shortened, and the efficiency of the concentration operation can be improved.
Hereinafter, the operation of filtering and concentrating by controlling the operation of the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p by the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure will be described.
In addition, the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure can be calculated by measuring the tube internal pressure connected to the filter 10 and the concentrator 20. For example, if pressure gauges are provided in the feed pipe 2 and the filtrate supply pipe 3 in advance and the signals are supplied to the control unit 106, the control unit 106 can calculate the differential pressure between the filter membranes. As shown in fig. 10, the control unit 106 can calculate the differential pressure between the filter membranes even when a pressure gauge is provided in the port 11c to which the filtrate supply pipe 3 is not connected (or a pipe connected to the port 11 c). Further, if pressure gauges are provided in the filtrate supply pipe 3 and the waste liquid pipe 5 in advance and the signals are supplied to the control unit 106, the control unit 106 can calculate the inter-membrane pressure difference of the concentrator. In addition, in the case where there is a port 20c to which the waste liquid pipe 5 is not connected, the control unit 106 can calculate the inter-membrane pressure difference of the concentrator even if a pressure gauge is provided in the port 20c (or a pipe connected to the port 20 c).
In the filter 10 and the concentrator 20, if either the liquid feed side or the liquid discharge side is in a state of being opened to the atmosphere, the control unit 106 can calculate the filter-membrane differential pressure and the concentrator-membrane differential pressure even if only the internal pressures of the tubes communicating with the side not opened to the atmosphere, out of the liquid feed side and the liquid discharge side, are measured. In other words, the control unit 106 can control the operation of the liquid feeding unit by using only the tube internal pressure communicated with the side not opened to the atmosphere instead of the filter membrane-to-membrane differential pressure and the concentrator membrane-to-membrane differential pressure. For example, if a tube connected to the filter 10 and the concentrator 20 is connected to a bag and the tube is not closed by the liquid feeding unit or the flow rate adjustment mechanism, the tube can be considered to be in a state of being nearly open to the atmosphere. In the state of fig. 12, the liquid supply tube 2 connected to the raw liquid bag UB of the tubes 2 and 3 connected to the filter 10 can be regarded as being open to the atmosphere. Further, the waste liquid pipe 5 connected to the waste liquid bag DB among the pipes 3 and 5 connected to the concentrator 20 can be regarded as being open to the atmosphere. Thus, if the state is shown in fig. 12, the controller 106 can control the operation of the liquid feeder by using only the tube internal pressure of the filter supply tube 3.
The flow rates of the liquids flowing through the concentrate pipe 4 and the waste pipe 5 may be estimated from the operations of the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p, or flow meters may be provided in the concentrate pipe 4 or the concentrate pipe liquid sending part 4p, and the waste pipe 5 or the waste pipe liquid sending part 5p to directly measure the flow rates.
< description of operation of filtration and concentration Using differential pressure between membranes of Filter and differential pressure between membranes of concentrator >
When filtration and concentration operations are performed using the pressure difference between the membranes of the filter and the pressure difference between the membranes of the concentrator, an allowable pressure difference is set in advance. That is, the differential pressures (allowable differential pressures) that can be allowed for the filter 10 and the concentrator 20 are set in accordance with the filter 10 and the concentrator 20, respectively. The allowable differential pressure may have a predetermined magnitude or may be set to a specific value. In the following description, the allowable differential pressure is typically a case having a predetermined width.
In addition, when performing filtration and concentration operations using the pressure difference between the filter membranes and the pressure difference between the concentrator membranes, it is desirable to set the allowable flow rate in advance. That is, it is desirable to set the flow rate (allowable flow rate) that can be allowed for the raw liquid in the feed pipe 2. The allowable flow rate may have a predetermined magnitude or may be set to a specific value. The allowable flow rate does not necessarily have to be set. However, if the flow rate of the raw liquid in the feed pipe 2 is too small, the time taken for the filtration and concentration becomes too long. Therefore, it is desirable to set the allowable flow rate in advance, while preventing the treatment time of the raw liquid from increasing.
Further, when performing filtration and concentration operations using the pressure difference between the filter membranes and the pressure difference between the concentrator membranes, it is desirable to set the allowable concentration ratio in advance. That is, it is desirable to set the ratio of the flow rate of the raw liquid in the feed pipe 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4 (allowable concentration ratio). The allowable concentration ratio may have a predetermined width or may be set to a specific value. The allowable concentration ratio is not necessarily set. However, if the concentration ratio, which is the ratio of the flow rate of the raw liquid in the feed pipe 2 to the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4, is too low (i.e., the flow rate of the concentrated liquid becomes too large), the concentration efficiency deteriorates. Further, the amount of the concentrated solution increases, and a large amount of the filtered concentrated solution is re-intravenously fed, which may cause an increase in blood pressure, an increase in heart failure, and an increase in respiratory failure. Therefore, when the amount of the concentrate becomes excessive, it is necessary to add a re-concentration process, and the re-concentration process takes time. In the case of re-concentrating the concentrated solution, since the re-concentration process takes time, the total time for processing the raw solution becomes long. Therefore, it is desirable to set the permissible concentration ratio in advance, on the premise of preventing the concentration ratio from decreasing excessively.
At the start of filtration concentration, the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p are operated so that the amount of the raw liquid sent to the filter 10 is increased. At this time, the concentrate-pipe liquid sending part 4p and the waste-pipe liquid sending part 5p are operated so that the concentrate has a predetermined concentration ratio. For example, when a concentrated solution having a concentration ratio of 10 times is to be produced, the flow rate of the concentrated solution flowing through the concentrated solution pipe 4 and the flow rate of the waste solution flowing through the waste solution pipe 5 are adjusted to be 1: 9. In addition, instead of the concentration ratio of the concentrated solution, the operation of the concentrated solution sending part 4p and the operation of the waste solution sending part 5p may be adjusted so that the pressure difference between the filter membranes and the pressure difference between the concentrator membranes are set to values within the allowable differential pressure (or maintained within the allowable differential pressure), or the pressure difference between the filter membranes and the pressure difference between the concentrator membranes are set to values within the allowable differential pressure (or maintained within the allowable differential pressure) while the concentrated solution is maintained at a predetermined concentration ratio. While the amount of the feed liquid of the raw liquid to the filter 10 is increased, the operation of the concentrate-pipe liquid feeding unit 4p and the waste-pipe liquid feeding unit 5p are controlled so as to be in any of the above-described states.
When the filtration concentration advances, clogging of the filter 10 and the concentrator 20 gradually occurs. Thereby, the inter-membrane differential pressure of the filter and the inter-membrane differential pressure of the concentrator increase. However, the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p are operated to increase the amount of the raw liquid sent to the filter 10 until the inter-membrane differential pressure between the filter membranes and the inter-membrane differential pressure between the concentrator membranes are within the allowable differential pressure.
< first method >
Here, the increase in the amount of the feed liquid of the raw liquid to the filter 10 is continued until the inter-filter-membrane differential pressure reaches the allowable differential pressure of the filter 10. When the filter membrane-to-membrane differential pressure falls within the allowable differential pressure of the filter 10, the operation of the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p is controlled so that the flow rate of the raw liquid in the feed pipe 2 is maintained at a flow rate at which the filter membrane-to-membrane differential pressure falls within the allowable differential pressure of the filter 10.
Here, when the filter membrane-to-membrane differential pressure is within the allowable differential pressure of the filter 10, the operation of the concentrate-pipe liquid feeding unit 4p and the waste-pipe liquid feeding unit 5p is controlled so as to maintain the liquid feeding amount of the filtrate to the concentrator 20, in other words, the liquid feeding amount of the raw liquid to the filter 10. This enables the filtration by the filter 10 and the concentration by the concentrator 20 to be maintained in a predetermined state. Further, if the amount of liquid to be fed to the filter 10 of the raw liquid is increased or decreased based on the value of the inter-membrane differential pressure between the filters, the amount of liquid to be fed to the filter 10 of the raw liquid can be increased while maintaining the inter-membrane differential pressure between the filters 10 within the allowable differential pressure of the filter 10. That is, there is a possibility that the efficiency of the filtration and concentration operation can be improved. In particular, if the inter-membrane differential pressure of the filter is maintained at the maximum allowable differential pressure PM of the filter 10, the amount of the stock solution sent to the filter 10 can be increased to the maximum, and therefore the effect of shortening the time for the filtration operation can be further enhanced.
On the other hand, when the filter membrane-to-membrane differential pressure becomes greater than the maximum allowable differential pressure PM of the filter 10, the operation of the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p is controlled so that the amount of the raw liquid sent to the filter 10 is reduced. When the hollow fiber membranes or the like are clogged even if the amount of the raw liquid fed to the filter 10 is constant, there is a possibility that the pressure difference between the filter membranes increases and the filtration cannot be continued. However, if the amount of the raw liquid fed to the filter 10 is reduced, the pressure difference between the filter membranes can be reduced, and therefore the filtering operation can be continued even if the filter 10 is clogged. Further, since the amount of the raw liquid fed to the filter 10 is reduced, clogging of the hollow fiber membrane or the like may be slightly reduced, and therefore, there is a possibility that the filtering operation can be continued easily and the time for the filtering operation can be shortened. In particular, when the filter-membrane differential pressure becomes greater than the maximum allowable differential pressure PM of the filter 10, the effect of reducing clogging of the hollow fiber membranes and the like can be enhanced by stopping the supply of the raw liquid to the filter 10 once and restarting the supply after a certain period of time.
When the inter-membrane differential pressure of the filter becomes smaller than the minimum allowable differential pressure PL of the filter 10, for example, by reducing the amount of the raw liquid sent to the filter 10, the operation of the concentrate pipe liquid sending unit 4p and the waste pipe liquid sending unit 5p is controlled so that the amount of the raw liquid sent to the filter 10 increases. This can increase the amount of filtration by the filter 10, and therefore, the time required for the filtration operation can be shortened. Further, if the amount of the feed liquid of the raw liquid to the filter 10 is increased until the inter-filter-membrane differential pressure falls within the allowable differential pressure of the filter 10, particularly the maximum allowable differential pressure PM, the filtering capacity of the filter 10 can be effectively used, and therefore the effect of shortening the time for the filtering operation can be further improved.
When the amount of the raw liquid to be fed to the filter 10 is reduced when the filter membrane-to-membrane differential pressure becomes larger than the maximum allowable differential pressure PM of the filter 10, the amount of the raw liquid to be fed may be gradually reduced, or the amount of the raw liquid to be fed may be reduced stepwise. When the filter-membrane differential pressure becomes greater than the maximum allowable differential pressure PM of the filter 10, the supply of the raw liquid to the filter 10 may be started after stopping the supply of the raw liquid to the filter 10 for a certain period of time (see fig. 24). In this case, the amount of the feed liquid of the raw liquid to the filter 10 may be adjusted while the pressure difference between the filter membranes is checked. For example, as shown in pattern 1 of fig. 24, when the liquid feeding of the raw liquid to the filter 10 is started after stopping the liquid feeding of the raw liquid to the filter 10 for a certain period of time, the liquid feeding is started at a flow rate of about 1/2 of the maximum allowable flow rate LM first, and the inter-filter-membrane differential pressure at that time is confirmed. If the inter-filter-membrane differential pressure becomes smaller than the minimum allowable differential pressure PL (PL in fig. 24) in this state, the flow rate around 1/2, which is the difference between the current flow rate and the maximum allowable flow rate LM, is increased and the inter-filter-membrane differential pressure at this time is confirmed. If the inter-filter-membrane differential pressure is still smaller than the minimum allowable differential pressure PL in this state, the flow rate around 1/2 of the difference between the current flow rate and the maximum allowable flow rate LM is further increased and the inter-filter-membrane differential pressure at this time is confirmed. This operation is repeated, and if the filter membrane-to-membrane differential pressure is equal to or higher than the minimum allowable differential pressure PL and equal to or lower than the maximum allowable differential pressure PM of the filter 10 (or if the maximum allowable differential pressure PM is reached), the increase in the flow rate is stopped. Even if the inter-filter-membrane differential pressure is within the allowable differential pressure of the filter 10, if the maximum allowable flow rate LM is not reached, the amount of the feed of the raw liquid to the filter 10 can be increased by the same method until the maximum allowable flow rate LM is reached while the inter-filter-membrane differential pressure is confirmed.
When the amount of the raw liquid supplied to the filter 10 is increased when the filter-membrane differential pressure becomes smaller than the minimum allowable differential pressure PL of the filter 10, the amount of the raw liquid supplied may be gradually increased. For example, the amount of the raw liquid to be fed to the filter 10 may be increased by the same method as the above-described method of increasing the flow rate, that is, the method of increasing the flow rate from the state where the feeding of the raw liquid to the filter 10 is stopped for a certain period of time.
In addition, while the amount of the raw liquid fed to the filter 10 is maintained in a state where the filter-membrane differential pressure is maintained within the allowable differential pressure of the filter 10, the amount of the raw liquid fed to the filter 10 may be increased until the maximum allowable flow rate LM is reached when the flow rate is smaller than the maximum allowable flow rate LM.
Even if the inter-membrane differential pressure of the filter becomes equal to or greater than the minimum allowable differential pressure PL of the filter 10, if the amount of the raw liquid fed to the filter 10 does not reach the minimum allowable flow rate LL (pattern 3 in fig. 24), it is determined that clogging of the hollow fiber membranes 16 or the like has occurred, and the filtration concentration operation is stopped and the operation is shifted to the cleaning operation.
Next, the concentrate pipe liquid feeding portion 4p can be controlled based on the inter-membrane differential pressure of the concentrator as follows, in a state where the inter-membrane differential pressure of the filter 10 is within the allowable differential pressure of the filter and the flow rate of the raw liquid in the liquid feeding pipe 2 is maintained at a flow rate in a state where the inter-membrane differential pressure of the filter is within the allowable differential pressure of the filter 10.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the concentrate pipe liquid feeding part 4p is operated so as to reduce the amount of the concentrated liquid fed to the concentrated liquid bag CB. That is, the operation of the concentrate-pipe liquid feeding portion 4p is controlled so as to increase the concentration of the concentrate. At this time, the waste liquid pipe feeding section 5p can maintain the operation state, and the feeding amount of the waste liquid flowing in the waste liquid pipe 5 can be maintained.
On the other hand, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the amount of the concentrated liquid fed to the concentrator 20 can be maintained while controlling the operation of the waste-liquid-tube liquid feeding unit 5p so that the amount of the waste liquid fed to the waste-liquid tube 5 can be increased.
< step 2>
Then, the amount of the concentrated solution sent to the concentrated solution bag CB is reduced until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. Then, when the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20, the concentrate pipe liquid feeding portion 4p is controlled so that the flow rate of the concentrate in the concentrate pipe 4 is maintained at a flow rate at which the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20. At this time, the waste liquid pipe feeding section 5p can be kept in operation, and the amount of waste liquid fed to the waste liquid pipe 5 can be maintained.
< step 3>
When the pressure difference between the concentrator membranes becomes larger than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like immediately after that, the concentrate pipe feed portion 4p is controlled so that the feed amount of the concentrate to the concentrate bag CB is increased. Further, although the concentration ratio decreases as the amount of the concentrated solution fed increases, the operation of the concentrated solution pipe feed portion 4p is controlled so as to decrease the concentration ratio (so as to decrease the concentration of the concentrated solution) while satisfying the allowable concentration ratio. At this time, the waste liquid pipe feeding section 5p can maintain the operation state, and the feeding amount of the waste liquid flowing in the waste liquid pipe 5 can be maintained.
On the other hand, when the inter-membrane differential pressure of the concentrator is greater than the maximum allowable differential pressure of the concentrator 20, the operation of the waste-liquid-pipe liquid-sending section 5p is controlled so that the liquid-sending amount of the waste liquid flowing in the waste liquid pipe 5 is reduced. Further, although the concentration ratio decreases as the amount of the waste liquid fed increases, the operation of the waste liquid pipe feeding portion 5p is controlled so as to decrease the concentration ratio (to decrease the concentration of the concentrated liquid) while satisfying the allowable concentration ratio.
When the amount of the concentrated solution fed to the concentrated solution bag CB increases (or when the amount of the waste solution fed to the waste solution pipe 5 decreases), the inter-membrane pressure difference between the concentrators decreases. When the inter-membrane differential pressure of the concentrator becomes smaller than the minimum allowable differential pressure of the concentrator 20, the concentrate pipe liquid feeding unit 4p is operated again to decrease the amount of the concentrated liquid fed to the concentrate bag CB (or the operation of the waste pipe liquid feeding unit 5p is controlled to increase the amount of the waste liquid fed to the waste pipe 5).
That is, the above steps 1 to 3 are repeated while the inter-membrane differential pressure of the filter is within the allowable differential pressure of the filter 10. This method can ensure the maximum filtration flow rate (i.e., the maximum allowable flow rate LM) and the maximum concentration ratio, which are not possible to achieve when the liquid feed amount to the filter 10 and the concentrate bag CB is constant, and which correspond to the membrane area and the clogging state of the filtration membranes of the filter 10 and the concentrator 20, or the state of the raw liquid (the concentration of the substance causing clogging of the filter and the concentrator, the concentration of the collected useful substance, the viscosity of the liquid, and the like). That is, by improving the filtration efficiency and the concentration efficiency, the time required to produce a concentrated solution from a raw solution can be shortened, and the re-concentration operation can be avoided or the time required for the re-concentration operation can be shortened. Further, if the operation is performed as described above, at the start of the filtration concentration, the cleaning liquid filled in the filter 10, the concentrator 20, and the circuit, and the cleaning liquid in the filter 10 and the circuit immediately after the cleaning of the filter 10 can be removed as the waste liquid of the concentrator 20 in a short time. That is, dilution of the concentrated solution by the cleaning solution at the start and immediately after the cleaning of the filter as described above can be effectively prevented.
In the above method (first method), the above steps 1 to 3 may be repeated to adjust the amount of the concentrated solution to be fed to the concentrator 20 when the inter-membrane differential pressure between the filter membranes is greater than the maximum allowable differential pressure PM, when the inter-membrane differential pressure between the filter membranes is smaller than the minimum allowable differential pressure PL, and when the amount of the stock solution to be fed to the filter 10 is constant regardless of the inter-membrane differential pressure between the filter membranes.
Further, the above-mentioned method (first method) may be employed for the entire period of the filtration concentration, or may be employed only for a certain period of time such as at the start of the filtration concentration or immediately after the filter is cleaned, and the concentration may be performed at a set concentration ratio for other periods of time.
< cleaning of Filter >
In the raw liquid treatment apparatus 1C according to embodiment 3, when the filtration and concentration operation is performed as described above, the filter-membrane differential pressure becomes larger than the maximum allowable differential pressure PM of the filter 10 due to clogging of the filter 10 or the like. In this case, if the flow rate of the raw liquid in the feed pipe 2 is reduced, the inter-filter-membrane differential pressure can be made smaller than the maximum allowable differential pressure PM of the filter 10, and the inter-filter-membrane differential pressure can be maintained within the allowable differential pressure (the range of the minimum allowable differential pressure PL to the maximum allowable differential pressure PM). However, if the clogging of the filter 10 or the like becomes serious, the flow rate of the raw liquid in the feed pipe 2 may be reduced to maintain the inter-membrane differential pressure of the filter 10 within the allowable differential pressure, and the flow rate of the raw liquid in the feed pipe 2 may become smaller than the minimum allowable flow rate LL. When the above state is attained, the operation of cleaning the filter 10 is performed in the middle of the filtering and concentrating operation of the raw liquid treatment apparatus 1C according to embodiment 3.
As shown in fig. 23, the flow rate adjusting mechanism 2c closes the liquid supply pipe 2 so that the liquid cannot flow. In addition, the operation of the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p is stopped to function as a jig. In the case where the filter cleaning is performed in the middle of the concentration and filtration operation, after the preparatory cleaning operation is completed, the cleaning liquid bag SB is connected to the other end of the cleaning liquid supply pipe 6 in place of the cleaning liquid recovery bag FB, and the cleaning liquid recovery bag FB is connected to the other end of the cleaning liquid recovery pipe 7 in place of the cleaning liquid bag SB.
In the above state, the cleaning liquid supply pipe liquid feeding portion 6p is operated so that the cleaning liquid flows from the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6 to the filter 10, and the cleaning liquid recovery pipe liquid feeding portion 7p is operated so that the cleaning liquid flows from the filter 10 to the cleaning liquid recovery bag FB connected to the cleaning liquid recovery pipe 7. This allows the cleaning liquid to flow through the hollow fiber membranes 16 in the direction opposite to the direction in which the raw liquid flows during filtration and concentration, and thus allows the cleaning liquid to clean the inside of the hollow fiber membranes 16.
After the preparation cleaning operation is finished, the cleaning liquid bag SB is connected to the other end of the connecting pipe 9 in place of the cleaning liquid recovery bag FB. Thus, if the flow rate adjustment mechanism 9c is opened to flow the liquid through the connecting pipe 9, the cleaning liquid can be supplied to the filter 10 from the cleaning liquid bag SB connected to the connecting pipe 9 in addition to the above state. Thus, the cleaning liquid supplied through the connection pipe 9 permeates the hollow fiber membranes 16 in the direction opposite to the direction in which the filtrate permeates the hollow fiber membranes 16, and therefore clogging of the hollow fiber membranes 16 can be eliminated. In this case, since the cleaning liquid is supplied to the filter 10 from both the cleaning liquid bag SB connected to the cleaning liquid supply pipe 6 and the cleaning liquid bag SB connected to the connecting pipe 9, the flow rate of the cleaning liquid flowing through the cleaning liquid recovery pipe 7 through the cleaning liquid recovery pipe liquid feeding portion 7p is adjusted to be larger than the flow rate of the cleaning liquid flowing through the cleaning liquid supply pipe 6 through the cleaning liquid supply pipe liquid feeding portion 6 p.
In addition, when the liquid is caused to flow through the connecting pipe 9 by the flow rate adjusting mechanism 9c, the cleaning liquid recovery pipe liquid feeding portion 7p may be operated with the operation of the cleaning liquid supply pipe liquid feeding portion 6p stopped. In this case, the cleaning liquid is supplied to the filter 10 only from the cleaning liquid bag SB connected to the connecting pipe 9. In this case, the cleaning liquid also permeates the hollow fiber membranes 16 in the direction opposite to the direction in which the filtrate permeates the hollow fiber membranes 16, and therefore clogging of the hollow fiber membranes 16 can be eliminated.
In addition, as shown in fig. 5, when a filter having hollow fiber membranes 16 is used as the filter 10, it is desirable to adjust the supply amount and supply timing of the cleaning liquid to the filter 10 by the control unit 106 so as to perform the cleaning of the filter 10 as described above. That is, it is desirable to adjust the supply amount and supply timing of the cleaning liquid to be supplied to the filter 10 so that the cleaning liquid permeates the hollow fiber membranes 16 in a state where the hollow space 12h of the trunk unit 12 is filled with the cleaning liquid in the hollow fiber membranes 16 and the region where cleaning is performed is filled.
< recovery of filtrate >
On the other hand, when the filter cleaning is performed in the above method, the filtrate remaining in the internal space 12h of the main body 11 of the filter 10 is mixed with the cleaning liquid and discharged. This reduces the amount of the active ingredient recovered by concentration by filtration.
Therefore, when the filter is cleaned, it is desirable to feed the filtrate in the internal space 12h of the main body 11 of the filter 10 to the concentrator 20 and then clean the filter.
< recovery (outer side) of cleaning liquid >
As shown in fig. 10, the port 11c of the body 11 of the filter 10 (the port 11c to which the filtrate supply tube 3 is not connected, hereinafter referred to as a cleaning port 11c) is connected to a cleaning solution bag SB via a tube. Then, the flow rate adjusting mechanism 3c maintains the state of flowing the liquid in the filtrate supply pipe 3, and the feed pipe 2 is closed by the flow rate adjusting mechanism 2c while the operation of the concentrate pipe liquid sending part 4p and/or the waste pipe liquid sending part 5 is continued. In this state, if the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10 by a pump provided in the pipe, the filtrate in the internal space 12h of the main body portion 11 of the filter 10 is supplied to the concentrator 20, and the cleaning liquid bag SB is relatively supplied from the cleaning bag SB to the internal space 12 h. When all the filtrate in the internal space 12h is replaced with the cleaning liquid immediately after the start, the filtrate supply pipe 3 is closed by the flow rate adjusting mechanism 3c, and the operation of the concentrate pipe liquid sending part 4p and/or the waste pipe liquid sending part 5 is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the feed pipe 2 is closed by the flow rate adjusting mechanism 2c and the recovery is performed, but the recovery may be performed while the feed pipe 2 is kept open. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration.
It is sufficient to know whether or not all the filtrate in the internal space 12h has been replaced with the cleaning liquid by a method of measuring the amount of feed of a pump provided in a pipe connected to the cleaning port 11c and obtaining the amount theoretically or a method of measuring the concentration of the concentrated liquid. The concentration of the filtrate may be determined by observing the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a densitometer.
Further, a pump is not necessarily provided in the pipe connected to the cleaning port 11c of the main body 11 of the filter 10. In this case, if the concentrate-pipe liquid feeder 4p or the waste-pipe liquid feeder 5p is operated, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be replaced with the cleaning liquid.
< recovery by gas such as air >
In the above description, the case where the cleaning solution bag SB is connected to the cleaning port 11c of the main body 11 of the filter 10 via a pipe has been described, but a gas such as air may be supplied to the cleaning port 11c of the main body 11 of the filter 10 via a pipe.
In this case, the flow rate adjusting mechanism 3c maintains the state in which the liquid flows in the filtrate supply pipe 3, and the feed pipe 2 is closed by the flow rate adjusting mechanism 2c while the operation of the concentrate pipe liquid sending part 4p and/or the waste pipe liquid sending part 5p is continued. In this state, if a gas such as air is supplied to the filter 10 from a pipe connected to the cleaning port 11c, the filtrate in the internal space 12h of the main body 11 of the filter 10 can be supplied to the concentrator 20. When all the filtrate in the internal space 12h is discharged, the filtrate supply pipe 3 is closed by the flow rate adjusting mechanism 3c, and the operation of the concentrate pipe liquid sending part 4p and/or the operation of the waste pipe liquid sending part 5p are stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the feed pipe 2 is closed by the flow rate adjusting mechanism 2c and the recovery is performed, but the recovery may be performed while the feed pipe 2 is kept open. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration.
It is sufficient to know whether or not all the filtrate in the internal space 12 has been discharged by a method of providing a liquid detector or a bubble detector in the filtrate supply pipe 3, measuring the pressure in the filtrate supply pipe 3, or theoretically obtaining the amount of the filtrate fed by measuring the amount of the pump.
When the filtrate in the internal space 12h of the main body 11 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the internal space 12h of the main body 11 of the filter 10 is filled with the gas such as air. Therefore, when the cleaning operation is performed after the recovery of the filtrate, it is desirable to perform the cleaning operation after the hollow space 12h of the body portion 12 is filled with the cleaning liquid in advance until the region of the hollow fiber membranes 16 to be cleaned is filled (or the entire hollow space 12h of the body portion 12).
< recovery into bag >
In the above example, the filtrate is sent to the concentrator 20 and recovered in the state of the concentrated solution, but the filtrate may be recovered while remaining the filtrate. For example, a bag for recovering the filtrate is connected to the filtrate supply pipe 3 at an upstream side (i.e., the filter 10 side) of the flow rate adjustment mechanism 3 c. In this state, if a gas such as a cleaning liquid or air is supplied to the filter 10 from the cleaning port 11c as described above in a state where the liquid cannot flow through the filtrate supply pipe 3 by the flow rate adjustment mechanism 3c, the filtrate in the internal space 12h of the main body portion 11 of the filter 10 can be collected into the bag. In this case, the filtrate can be recovered in a shorter time than in the case where the filtrate is sent to the concentrator 20 and recovered in a state of a concentrated solution, and therefore, the shift to the cleaning operation can be performed quickly.
< recovery by cleaning liquid (inside) >
In the above description, the following is explained: the raw liquid is supplied to the through channels 16h of the plurality of hollow fiber membranes 16 of the hollow fiber membrane bundle 15 of the filter 10, and the filtrate is discharged into the internal space 12h of the body portion 12 of the body portion 11 of the filter 10. However, the raw liquid may be supplied from the filtrate discharge port 11c into the internal space 12h of the body portion 12 of the body portion 11, and the filtrate obtained by filtration may be discharged into the through channels 16h of the plurality of hollow fiber membranes 16 of the hollow fiber membrane bundle 15 and discharged from the raw liquid supply port 11a to the outside.
In this case, the pipes and the like are connected as described below.
First, the filtrate supply pipe 3 is connected to the raw liquid supply port 11a, and the liquid supply pipe 2 is connected to the port 11c (i.e., the above-described cleaning port 11 c). The cleaning liquid supply pipe 6 is connected to a port 11c to which the liquid feed pipe 2 is not connected (i.e., the filtrate discharge port 11c), and a cleaning liquid bag SB connected to the cleaning port 11c is connected to the cleaning liquid supply port 11 b.
Then, the feed pipe 2 is closed by the flow rate adjusting mechanism 2c while the flow rate of the liquid in the filtrate supply pipe 3 is maintained by the flow rate adjusting mechanism 3c and the operation of the concentrate pipe liquid sending part 4p and/or the waste pipe liquid sending part 5p is continued. In this state, if the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10 by a pump provided in a pipe connected to the cleaning liquid supply port 11b, the filtrate in the through flow path 16h of the hollow fiber membranes 16 of the filter 10 is supplied to the concentrator 20, and the cleaning liquid is relatively supplied from the cleaning liquid bag SB into the through flow path 16 h. When all the filtrate in the through space 16h is replaced with the cleaning liquid immediately after the start, the filtrate supply pipe 3 is closed by the flow rate adjusting mechanism 3c, and the operation of the concentrate pipe liquid sending part 4p and/or the waste pipe liquid sending part 5p is stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the feed pipe 2 is closed by the flow rate adjusting mechanism 2c and the recovery is performed, but the recovery may be performed while the feed pipe 2 is kept open. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration.
It is sufficient to know whether or not all the filtrate in the internal space 12h has been replaced with the cleaning liquid by a method of measuring the amount of feed of a pump provided in a pipe connected to the cleaning port 11c and obtaining the amount theoretically or a method of measuring the concentration of the concentrated liquid. The concentration of the filtrate may be determined by observing the color of the filtrate, measuring the absorbance, or measuring the specific gravity of the filtrate using a densitometer.
< recovery by gas such as air >
In the above description, the case where the cleaning liquid bag SB is connected to the cleaning liquid supply port 11b of the main body portion 11 of the filter 10 via a pipe has been described, but a gas such as air may be supplied to the cleaning supply port 11b of the main body portion 11 of the filter 10 via a pipe.
In this case, the flow rate adjusting mechanism 3c maintains the state in which the liquid flows in the filtrate supply pipe 3, and the feed pipe 2 is closed by the flow rate adjusting mechanism 2c while the operation of the concentrate pipe liquid sending part 4p and/or the waste pipe liquid sending part 5p is continued. In this state, if a gas such as air is supplied from a pipe to the filter 10, the filtrate in the through flow path 16h of the hollow fiber membrane 16 of the filter 10 can be supplied to the concentrator 20. When all the filtrate in the through flow channel 16h of the hollow fiber membrane 16 is discharged soon, the filtrate supply pipe 3 is closed by the flow rate adjusting mechanism 3c, and the operation of the concentrate pipe liquid sending part 4p and/or the operation of the waste pipe liquid sending part 5p are stopped. After this state is reached, if the filter 10 is cleaned by the above-described method for cleaning the filter 10, re-concentration of the filtrate discharged together with the cleaning liquid can be suppressed.
In the above example, the feed pipe 2 is closed by the flow rate adjusting mechanism 2c and the recovery is performed, but the recovery may be performed while the feed pipe 2 is kept open. That is, the filtrate in the filter 10 may be recovered while continuing the filtration and concentration.
It is sufficient to know whether or not all the filtrate in the through flow channel 16h of the hollow fiber membrane 16 has been discharged by a method of providing a liquid detector or a bubble detector in the filtrate supply pipe 3, measuring the pressure in the filtrate supply pipe 3, or measuring the amount of feed of a pump to theoretically obtain the amount of feed.
When the filtrate in the through-flow channel 16h of the hollow fiber membrane 16 of the filter 10 is supplied to the concentrator 20 by a gas such as air, the through-flow channel 16h of the hollow fiber membrane 16 of the filter 10 is filled with the gas such as air. Therefore, when the cleaning operation is performed after the filtrate is collected, it is desirable to perform the cleaning operation after the through-flow passage 16h is filled with the cleaning liquid in advance until the region where the hollow fiber membranes 16 are cleaned (or the entire hollow fiber membranes 16) is filled with the cleaning liquid.
< recovery into bag >
In the above example, the filtrate is sent to the concentrator 20 and recovered in the state of the concentrated solution, but the filtrate may be recovered while remaining the filtrate. For example, a bag for recovering the filtrate is connected to the filtrate supply pipe 3 at an upstream side (i.e., the filter 10 side) of the flow rate adjustment mechanism 3 c. In this state, if a gas such as a cleaning liquid or air is supplied to the filter 10 from the cleaning liquid supply port 11b in such a manner that the liquid cannot flow through the filtrate supply pipe 3 by the flow rate adjustment mechanism 3c, the filtrate in the through flow path 16h of the hollow fiber membranes 16 of the filter 10 can be collected in the bag. In this case, the filtrate can be recovered in a shorter time than in the case where the filtrate is sent to the concentrator 20 and recovered in a state of a concentrated solution, and therefore, the shift to the cleaning operation can be performed quickly.
< example of method for recovering liquid in Filter 10 >
As described above, when the filtrate in the filter 10 is sent to the concentrator 20 and the filtrate is recovered as a concentrated solution, it is desirable to adjust the flow rate at the time of sending the filtrate to the concentrator 20 based on the inter-membrane pressure difference between the concentrators of the concentrator 20. If such a method is adopted, even if the concentrator 20 is clogged, the increase in the pressure difference between the membranes of the concentrator can be suppressed to prevent the stop of the treatment, and therefore the filtrate in the filter 10 can be recovered efficiently.
For example, when the flow rate at the time of feeding the liquid to the concentrator 20 is adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rate can be adjusted as follows. First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the concentrate-pipe liquid sending unit 4p and the operation of the waste-pipe liquid sending unit 5p are controlled to maintain the liquid sending amount from the filter 10 to the concentrator 20. This prevents the occurrence of problems such as the pressure difference between membranes of the concentrator greatly falling within the range of the set pressure difference.
On the other hand, when the pressure difference between the concentrator membranes of the concentrator 20 is larger than the maximum set pressure difference, the operation of the concentrate-pipe liquid-sending section 4p and/or the operation of the waste-pipe liquid-sending section 5p are controlled so that the amount of liquid sent from the filter 10 to the concentrator 20 is reduced. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment.
On the other hand, when the pressure difference between the concentrator membranes of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrate-pipe liquid-sending part 4p and/or the operation of the waste-pipe liquid-sending part 5p are controlled so that the amount of liquid sent from the filter 10 to the concentrator 20 increases. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
The set differential pressure of the pressure difference between the membranes of the concentrator when the filtrate in the filter 10 is recovered may be the same as the allowable differential pressure in the filtration and concentration operation, or may be a value (range) different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the range of the set differential pressure may be set to be larger than the range of the allowable differential pressure. In this case, it is desirable that the concentrated solution can be recovered to the end as much as possible even in a diluted state. In addition, when the range of the set differential pressure is set to be smaller than the range of the allowable differential pressure, it is desirable that the concentrated solution is recovered to the end as much as possible without diluting the concentrated solution even if it takes time. Further, the range of the allowable differential pressure and the range of the set differential pressure may be different from each other.
< reconcentration operation >
When the concentrated solution obtained by the filtering and concentrating operation is further concentrated, a re-concentrating operation is performed.
As shown in fig. 12, in the reconcentration operation of the undiluted liquid processing apparatus 1C according to embodiment 3, the other end of the connecting tube 9 is removed from the cleaning liquid bag SB, and the other end of the connecting tube 9 is connected to the concentrated liquid bag CB.
The flow rate adjusting mechanism 3c maintains a state in which liquid can flow through the filtrate supply pipe, and the flow rate adjusting mechanism 9c maintains a state in which liquid can flow through the connecting pipe 9, while the cleaning liquid pipe feeding portion 6p and the cleaning liquid recovery pipe feeding portion 7p are not operated and function as a jig. In addition, the flow rate adjusting mechanism 2c closes the liquid supply pipe 2 so that the liquid cannot flow. This prevents the liquid from flowing through the filter 10.
In this state, the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p are operated so that the concentrate flows from the concentrator 20 to the concentrate bag CB through the concentrate pipe 4.
Thereby, the concentrated liquid is supplied from the concentrated liquid bag CB connected to the connection pipe 9 to the concentrator 20 through the connection pipe 9, and thus the re-concentrated liquid further concentrated by the concentrator 20 is recovered to the concentrated liquid bag CB through the concentrated liquid pipe 4. On the other hand, the moisture separated from the concentrated solution is recovered to the waste liquid bag DB through the waste liquid pipe 5. That is, a concentrated solution (reconcentrated solution) having an increased concentration ratio can be obtained.
< explanation of the operation of reconcentration using the pressure difference between membranes in the concentrator >
In the re-concentration operation, the flow rate from the concentrator 20 to the concentrate bag CB and/or the flow rate from the concentrator 20 to the waste liquid bag DB, that is, the re-concentration ratio can be adjusted based on the inter-concentrator-membrane differential pressure of the concentrator 20. In this method, an effect is obtained that the time for producing a concentrated solution having a high concentration can be shortened while suppressing an increase in the pressure difference between membranes of the concentrator.
In this case, when the re-concentration operation using the pressure difference between the membranes of the concentrator is performed in advance, it is desirable to set the allowable pressure difference. That is, the differential pressure that can be allowed by the concentrator 20 (allowable differential pressure) is set in accordance with the concentrator 20. The allowable differential pressure may have a predetermined magnitude or may be set to a specific value. In the following description, the allowable differential pressure is typically a case having a predetermined width.
In addition, when the re-concentration operation using the pressure difference between the membranes of the concentrator is performed, it is desirable to set the allowable flow rate in advance. That is, it is desirable to set the flow rate (allowable flow rate) that can be allowed by the concentrated liquid in the connecting pipe 9. The allowable flow rate may have a predetermined magnitude or may be set to a specific value. The allowable flow rate does not necessarily have to be set. However, if the flow rate of the concentrated liquid in the connecting pipe 9 is too small, the time taken for re-concentration becomes too long. Therefore, when the processing time for preventing the re-concentration is long, it is desirable to set the allowable flow rate in advance. The allowable flow rate in the re-concentration operation may be the same as or different from the allowable flow rate in the filtering concentration.
Further, when the re-concentration operation using the pressure difference between the filter membranes is performed, it is desirable to set the allowable concentration ratio in advance. That is, it is desirable to set the ratio of the flow rate of the concentrated liquid flowing in the concentrated liquid pipe 4 to the flow rate of the concentrated liquid in the connecting pipe 9 (allowable concentration ratio). The allowable concentration ratio may have a predetermined width or may be set to a specific value. The allowable concentration ratio is not necessarily set. However, if the concentration ratio, which is the ratio of the flow rate of the concentrated liquid flowing through the concentrated liquid pipe 4 to the flow rate of the concentrated liquid through the connecting pipe 9, is too low (i.e., the flow rate of the concentrated liquid becomes too large), the concentration efficiency deteriorates and the re-concentration process takes time. Thus, in order to prevent the concentration ratio from being excessively decreased, it is desirable to set an allowable concentration ratio in advance. The allowable concentration ratio in the re-concentration operation may be the same as or different from the allowable concentration ratio in the filtration concentration.
At the start of re-concentration, the concentrate-pipe liquid feeding part 4p and the waste-pipe liquid feeding part 5p are operated so as to increase the amount of the concentrated liquid fed to the concentrator 20 (i.e., the flow rate of the concentrated liquid in the connecting pipe 9). At this time, the concentrate-pipe liquid sending part 4p and the waste-pipe liquid sending part 5p are operated so that the concentrate has a predetermined concentration ratio. For example, when a concentrated solution having a concentration ratio of 10 times is to be produced, the flow rate of the concentrated solution flowing through the concentrated solution pipe 4 and the flow rate of the waste solution flowing through the waste solution pipe 5 can be adjusted to be 1: 9. further, the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p may be also operated so as to adjust the pressure difference between the concentrator membranes to a set value. While the amount of the concentrated liquid to be fed to the concentrator 20 is increased, the operation of the concentrated liquid-feeding portion 4p and the waste liquid-feeding portion 5p are controlled so as to be in any of the above-described states.
When the re-concentration progresses, clogging of the concentrator 20 gradually occurs. This increases the inter-membrane differential pressure of the concentrator. However, the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p are operated to increase the amount of the concentrated liquid sent to the concentrator 20 until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure.
< first method >
Here, the increase in the amount of the concentrated liquid fed to the concentrator 20 is continued until the pressure difference between the concentrator membranes reaches the allowable pressure difference of the concentrator 20. Then, if the inter-membrane pressure difference between the concentrator membranes is within the allowable pressure difference of the concentrator 20, the operation of the concentrate pipe liquid sending part 4p and the waste pipe liquid sending part 5p is controlled based on the inter-membrane pressure difference between the concentrator membranes so that the flow rate of the concentrate in the connection pipe 9 is maintained at a flow rate in a state where the inter-membrane pressure difference between the concentrator membranes is within the allowable pressure difference of the concentrator 20.
< step 1>
First, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the concentrate pipe liquid feeding part 4p is operated so as to reduce the amount of the concentrated liquid fed to the concentrated liquid bag CB. That is, the operation of the concentrate-pipe liquid feeding portion 4p is controlled so as to increase the concentration of the concentrate. At this time, the waste liquid pipe feeding section 5p can maintain the operation state, and the feeding amount of the waste liquid flowing in the waste liquid pipe 5 can be maintained.
On the other hand, when the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the amount of the concentrated liquid fed to the concentrator 20 can be maintained while controlling the operation of the waste-liquid-tube liquid feeding unit 5p so that the amount of the waste liquid fed to the waste-liquid tube 5 can be increased.
< step 2>
Then, the amount of the concentrated solution sent to the concentrated solution bag CB is reduced until the inter-membrane differential pressure of the concentrator falls within the allowable differential pressure of the concentrator 20. Then, when the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20, the concentrate-pipe liquid feeding portion 4p is controlled so that the flow rate of the concentrate in the concentrate pipe 4 is maintained at a flow rate at which the inter-membrane pressure difference between the concentrators is within the allowable pressure difference of the concentrator 20. At this time, the operation of the waste liquid pipe feeding section 5p can be controlled to maintain the feeding amount of the waste liquid flowing in the waste liquid pipe 5.
< step 3>
When the pressure difference between the concentrator membranes becomes larger than the maximum allowable pressure difference of the concentrator 20 due to clogging of the concentrator 20 or the like immediately after that, the concentrate pipe feed portion 4p is controlled so that the feed amount of the concentrate to the concentrate bag CB is increased. Further, although the concentration ratio decreases as the amount of the concentrated solution fed increases, the operation of the concentrated solution pipe feed portion 4p is controlled so as to decrease the concentration ratio (so as to decrease the concentration of the concentrated solution) while satisfying the allowable concentration ratio. At this time, the waste liquid pipe feeding section 5p can maintain the operation state, and the feeding amount of the waste liquid flowing in the waste liquid pipe 5 can be maintained.
On the other hand, when the inter-membrane differential pressure of the concentrator is greater than the maximum allowable differential pressure of the concentrator 20, the operation of the waste-liquid-pipe liquid-sending section 5p is controlled so that the liquid-sending amount of the waste liquid flowing in the waste liquid pipe 5 is reduced. Further, although the concentration ratio decreases as the amount of the waste liquid fed decreases, the operation of the waste liquid tube feeding portion 5p is controlled so as to decrease the concentration ratio (to decrease the concentration of the concentrated liquid) while satisfying the allowable concentration ratio.
Since the inter-membrane differential pressure of the concentrator decreases as the amount of the concentrated liquid sent to the concentrated liquid bag CB increases (or as the amount of the waste liquid sent to the waste liquid pipe 5 decreases), if the inter-membrane differential pressure of the concentrator is smaller than the minimum allowable differential pressure of the concentrator 20, the concentrated liquid pipe sending part 4p is operated again to decrease the amount of the concentrated liquid sent to the concentrated liquid bag CB (or the operation of the waste liquid pipe sending part 5p is controlled to increase the amount of the waste liquid sent to the waste liquid pipe 5).
That is, the above steps 1 to 3 are repeated while the pressure difference between the membranes of the concentrator is within the allowable pressure difference of the filter 20. This method makes it possible to ensure the maximum filtration flow rate and the maximum concentration ratio corresponding to the membrane area and the clogged state of the filtration membrane of the concentrator 20 or the state of the concentrated solution (the concentration of the substance causing clogging of the concentrator, the concentration of the collected useful substance, the viscosity of the solution, etc.) which cannot be achieved when the amount of liquid fed to the concentrated solution bag CB is constant. That is, by improving the circulation efficiency and the concentration efficiency, the time required for generating a concentrated solution having a high concentration can be shortened, and the time required for the re-concentration operation can be shortened.
The set differential pressure between the concentrator membranes at the time of re-concentration may be the same as the allowable differential pressure in the filtration and concentration operation, or may be a value (range) different from the allowable differential pressure in the filtration and concentration operation. For example, when the allowable differential pressure for the filtering concentration operation has a certain range, the range of the allowable differential pressure for reconcentration may be set to be larger than the range. In this case, when the filter 10 is used to treat a raw liquid having a property of being easily clogged, the treatment is performed slowly so as not to apply pressure to the filter 10 during the filtering operation, but it is desired to generate a concentrated liquid having a high concentration and shorten the re-concentration time. In addition, when the range of the allowable differential pressure for re-concentration is set to be smaller than the range of the allowable differential pressure for the filtering and concentrating operation, when the concentrator 20 treats a raw liquid having a property of being easily clogged, the concentrate 20 is treated in a short time without applying pressure to the filtering and concentrating operation, and it is desirable that a concentrated liquid with a high concentration can be generated in the re-concentration operation. Further, the range of the allowable differential pressure for the filtration and concentration operation may deviate from the range of the allowable differential pressure for the re-concentration operation.
The allowable concentration ratio at the time of re-concentration may be the same as the allowable concentration ratio in the filtering and concentrating operation, or may be a value (range) different from the allowable concentration ratio in the filtering and concentrating operation. For example, when the allowable concentration ratio for the concentration filtration work is within a certain range, the range of the allowable concentration ratio for reconcentration may be set to be larger than the range. In this case, instead of performing concentration with a long time in the filtering concentration operation, it is desirable to shorten the time for the re-concentration operation. In addition, when the range of the allowable concentration ratio for re-concentration is set to be smaller than the range of the allowable concentration ratio for the filtering and concentrating operation, it is desirable to be able to finish the filtering and concentrating operation as soon as possible, instead of performing concentration with time in the re-concentration operation. Further, the range of the allowable concentration ratio for the filtering concentration operation and the range of the allowable concentration ratio for the re-concentration operation may be varied.
< example of method for recovering liquid in Filter 10 >
Before the above-described re-concentration operation is performed, the filtrate in the filter 10 is sent to the concentrator 20, and the filtrate is recovered as a concentrated solution. In this case, it is desirable to adjust the flow rate when the liquid is sent to the concentrator 20 based on the pressure difference between the concentrator membranes of the concentrator 20. If such a method is adopted, even if the concentrator 20 is clogged, the increase of the pressure difference between the membranes of the concentrator can be suppressed to prevent the stop of the treatment, and therefore the filtrate in the filter 10 can be recovered efficiently.
For example, when the flow rate at the time of feeding the liquid to the concentrator 20 is adjusted based on the pressure difference between the concentrator membranes of the concentrator 20, the flow rate can be adjusted as follows. First, when the pressure difference between the concentrator membranes of the concentrator 20 is within the set pressure difference range, the operation of the concentrate pipe liquid sending unit 4p and/or the operation of the waste pipe liquid sending unit 5p are controlled to maintain the liquid sending amount from the filter 10 to the concentrator 20. This prevents the occurrence of problems such as the pressure difference between membranes of the concentrator greatly falling within the range of the set pressure difference.
On the other hand, when the pressure difference between the concentrator membranes of the concentrator 20 is larger than the maximum set pressure difference, the operation of the concentrate-pipe liquid-sending section 4p and/or the operation of the waste-pipe liquid-sending section 5p are controlled so that the amount of liquid sent from the filter 10 to the concentrator 20 is reduced. This prevents the inter-membrane differential pressure of the concentrator from rising to the maximum set differential pressure and continuing to rise, which makes it impossible to continue the treatment.
On the other hand, when the pressure difference between the concentrator membranes of the concentrator 20 is smaller than the minimum set pressure difference, the operation of the concentrate-pipe liquid-sending part 4p and/or the operation of the waste-pipe liquid-sending part 5p are controlled so that the liquid-sending amount from the filter 10 to the concentrator 20 is increased. This prevents problems such as dilution of the concentrated solution, which would occur if the pressure difference between the membranes of the concentrator were reduced to the minimum set pressure difference and continued to decrease.
The set differential pressure of the pressure difference between the membranes of the concentrator when the filtrate in the filter 10 is recovered may be the same as the allowable differential pressure in the filtration and concentration operation, or may be a value (range) different from the allowable differential pressure. For example, when the allowable differential pressure has a certain range, the range of the set differential pressure may be set to be larger than the range of the allowable differential pressure. In this case, it is desirable that the concentrated solution can be recovered to the end as much as possible even in a diluted state. In addition, when the range of the set differential pressure is smaller than the range of the allowable differential pressure, it is desirable that the concentrated solution is recovered to the end as much as possible without diluting the concentrated solution even if it takes time. Further, the range of the allowable differential pressure and the range of the set differential pressure may be different from each other.
< operation for collecting concentrator 20 >
When the raw liquid and the filtrate in the filter 10 are recovered and then the concentrated liquid in the concentrator 20 is recovered, only the cleaning liquid or the fluid called gas (hereinafter, simply referred to as fluid) may be made to flow through the concentrator 20, and the concentrated liquid or the like may be further recovered. However, as in the above case, the flow rate of the fluid supplied to the concentrated solution 20 may be adjusted while measuring the inter-membrane differential pressure of the concentrator. This prevents the occurrence of problems such as the inability to continue treatment due to an increase in the pressure difference between the membranes of the concentrator. When the inter-membrane pressure difference between the concentrators 20 becomes larger than the maximum set pressure difference, the problem of the inter-membrane pressure difference between the concentrators continuing to rise can be prevented by stopping the liquid supply (including the gas flow) from the filter 10 to the concentrator 20.
The set differential pressure (second set differential pressure) between the concentrator membranes when the concentrated solution in the concentrator 20 is recovered may be the same as the allowable differential pressure during the filtration and concentration operation or the set differential pressure (first set differential pressure) when the filtrate in the filter 10 is recovered, or may be a value (range) different from these. For example, when the allowable differential pressure and the first set differential pressure have a certain range, the range of the second set differential pressure may be set to be larger than the range of the allowable differential pressure and the first set differential pressure. In this case, it is desirable that the concentrated solution can be recovered to the end as much as possible even in a diluted state. When the range of the second set differential pressure is set to be smaller than the range of the allowable differential pressure and the first set differential pressure, it is desirable that the concentrated solution is recovered to the end as much as possible without diluting the concentrated solution even if it takes time. Further, the range of the second set differential pressure may be different from the range of the allowable differential pressure and the range of the first set differential pressure.
< operation for collecting liquid in filtrate supply pipe 3 >
After the recovery of the concentrated liquid in the concentrator 20, when the pressure difference between the concentrator membranes reaches a set pressure difference or a predetermined liquid amount is recovered, the liquid feed (including the gas flow) from the filter 10 to the concentrator 20 may be stopped, and then a gas such as air may be supplied to the filtrate supply pipe 3. This prevents the concentrated solution in the concentrator 20 or the concentrated solution channel 4 and the liquid in the channel on the downstream side of the filtrate supply pipe 3 from being recovered and left over. Further, if the inter-membrane differential pressure of the concentrator reaches the set differential pressure, the liquid feed from the filter 10 to the concentrator 20 does not necessarily have to be stopped.
Industrial applicability
The stock solution processing apparatus of the present invention is suitable for a method of obtaining a concentrated solution by filtering and concentrating a pleural effusion containing cells and the like, blood during surgery or during exsanguination, or cleaning a filter in an apparatus for purifying and reusing plasma such as waste blood plasma after blood exchange.
Description of the reference numerals
1 stock solution treating apparatus
2 liquid feeding pipe
2c flow adjusting mechanism
2p liquid feeding part of liquid feeding pipe
3 filtrate supply pipe
3c flow adjusting mechanism
3p filtrate supply pipe liquid feeding part
4 concentrated liquid pipe
4p concentrated liquid pipe liquid sending part
5 waste liquid pipe
5c flow adjusting mechanism
6 cleaning liquid supply pipe
6c flow adjustment mechanism
Liquid feeding part of 6p cleaning liquid supply pipe
7 cleaning liquid recovery pipe
7c flow adjusting mechanism
Liquid feeding part of 7p cleaning liquid recovery pipe
9 connecting pipe
9c flow regulating mechanism
9f flow adjusting mechanism
9p connecting pipe liquid feeding part
10 filter
11 body part
11a stock solution supply port
11b cleaning liquid supply port
11c filtrate discharge port
12 trunk part
12h inner space
15 hollow fiber membrane bundle
16 hollow fiber membrane
16h through flow path
Wall of 16w hollow fiber membrane
20 concentrator
20a filtrate supply port
20b filtrate outlet
20c waste liquid discharge port
100 main body part
103 suspension part
106 control part
110 roller pump
120 roller pump
150 pipe support
155 holding part
152 connecting part
153 engaging member
160 pipe locating component
161 holding member
165 connecting member
UB stock solution bag
CB concentrate bag
DB waste liquid bag
SB cleaning solution bag
FB cleaning solution recovery bag
GB concentrator cleaning solution recovery bag
P1 pressure gauge
P2 pressure gauge.
Claims (54)
1. A method of cleaning an appliance having hollow fiber membranes, the appliance having:
a main body having a hollow space therein; a hollow fiber membrane disposed in the hollow space of the main body,
the cleaning method is characterized in that the cleaning method comprises the following steps,
in cleaning the hollow fiber membranes in the appliance, the liquid is made to flow as follows: the hollow fiber membranes are permeated with a liquid in a state where the hollow space of the main body and/or the hollow fiber membranes are filled with the liquid to fill the region where the hollow fiber membranes are washed.
2. The method of cleaning an implement having a hollow fiber membrane according to claim 1,
in cleaning the hollow fiber membranes in the appliance, the liquid is caused to flow in the following manner: after filling the hollow space of the main body and/or the hollow fiber membranes with a liquid to fill the region of the hollow fiber membranes to be cleaned, the liquid is allowed to permeate the hollow fiber membranes.
3. The method of cleaning an implement having a hollow fiber membrane according to claim 1 or 2,
the instrument is provided with:
a first liquid supply unit which communicates with the first end of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane;
a second liquid supply portion that communicates with the second end portion of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane;
a port for supplying and discharging fluid between the inside and the outside of the hollow space of the main body,
in a state where the hollow fiber membranes are arranged so that the axial direction of the hollow fiber membranes is directed in the vertical direction,
the liquid is caused to flow as follows: the hollow space of the main body and/or the hollow fiber membranes are filled with a liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid is allowed to permeate the hollow fiber membranes in this state.
4. The method of cleaning an implement having a hollow fiber membrane according to claim 1 or 2,
the instrument is provided with:
a first liquid supply unit which communicates with the first end of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane;
A second liquid supply portion that communicates with the second end portion of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane;
a port for supplying and discharging fluid between the inside and the outside of the hollow space of the main body,
in a state where the hollow fiber membranes are arranged so that the axial direction of the hollow fiber membranes faces the horizontal direction, a liquid is caused to flow as follows: the hollow space of the main body and/or the hollow fiber membranes are filled with a liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid is allowed to permeate the hollow fiber membranes in this state.
5. The method of cleaning an implement having a hollow fiber membrane according to any one of claims 1, 2, 3 or 4,
the instrument is provided with:
a first liquid supply unit which communicates with the first end of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane;
a second liquid supply portion that communicates with the second end portion of the hollow fiber membrane and supplies a discharge fluid between the inside and the outside of the hollow fiber membrane;
a port for supplying and discharging fluid between the inside and the outside of the hollow space of the main body,
Discharging liquid from the first liquid supply part and/or the second liquid supply part when liquid is supplied from the port, or discharging liquid from the port when liquid is supplied from the first liquid supply part and/or the second liquid supply part.
6. A method for operating a raw liquid processing apparatus for concentrating a raw liquid to form a concentrated liquid,
the device is provided with:
a filter having a filter member for filtering the stock solution;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated solution;
a raw liquid supply unit configured to supply the raw liquid to the filter;
a liquid supply passage for communicating the raw liquid supply unit with the raw liquid supply port of the filter;
a filtrate supply passage for connecting the filtrate discharge port of the filter to the filtrate supply port of the concentrator;
a concentrate flow path connected to a concentrate discharge port of the concentrator;
a waste liquid flow path connected to a waste liquid discharge port for discharging the waste liquid separated from the concentrated liquid in the concentrator;
a liquid feeding unit for feeding liquid to each flow path;
A control part for controlling the operation of the liquid feeding part,
the filter and/or the concentrator have:
a main body having a hollow space therein;
a hollow fiber membrane disposed in the hollow space of the main body,
when cleaning the hollow fiber membranes in the filter and/or the concentrator, the control unit controls the operation of the liquid feed unit so that the liquid permeates the hollow fiber membranes in a state where the hollow space of the main body and/or the hollow fiber membranes are filled with the liquid to fill the region to be cleaned in the hollow fiber membranes.
7. The method of operating a stock solution processing apparatus according to claim 6,
when cleaning the hollow fiber membranes in the filter and/or the concentrator, the control unit controls the operation of the liquid feed unit so that the liquid permeates the hollow fiber membranes after the hollow space of the main body and/or the hollow fiber membranes are filled with the liquid to a state where the region to be cleaned in the hollow fiber membranes is filled with the liquid.
8. The method of operating a stock solution processing apparatus according to claim 6 or 7,
The filter is disposed in a state in which the axial direction of the hollow fiber membrane faces the vertical direction,
the filter includes a port which is disposed above the raw liquid supply port or the filtrate discharge port when the hollow fiber membrane in the filter is cleaned and which is capable of communicating the inside of the hollow space of the main body with the outside,
the controller controls the operation of the liquid feeder so that the hollow space of the main body and/or the hollow fiber membranes are filled with liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid passes through the hollow fiber membranes of the filter in this state.
9. The method of operating a stock solution processing apparatus according to any one of claims 6, 7 or 8,
the concentrator is disposed in a state in which the axial direction of the hollow fiber membranes is directed in the vertical direction,
the concentrator includes a port which is disposed above the concentrated solution discharge port or the waste solution discharge port when the hollow fiber membranes in the concentrator are cleaned, and which is capable of communicating the inside of the hollow space of the main body with the outside,
The control unit controls the operation of the liquid feeding unit so that the hollow space of the main body and/or the hollow fiber membranes are filled with liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid passes through the hollow fiber membranes of the concentrator in this state.
10. The method of operating a stock solution processing apparatus according to claim 6 or 7,
in a state where the filter and/or the concentrator are arranged so that the axial direction of the hollow fiber membranes is directed in the horizontal direction,
the controller controls the operation of the liquid feeder so that the hollow space of the main body and/or the hollow fiber membranes are filled with liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid is allowed to permeate the hollow fiber membranes in this state.
11. The method of operating a stock solution treatment apparatus as recited in any one of claims 6, 7, 8, 9 or 10,
and supplying a liquid into the concentrator from the filtrate supply port or the concentrated liquid discharge port.
12. A method for operating a raw liquid processing apparatus for concentrating a raw liquid to form a concentrated liquid,
The device is provided with:
a filter having a filter member for filtering the stock solution;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated solution;
a raw liquid supply unit configured to supply the raw liquid to the filter;
a liquid supply passage for communicating the raw liquid supply unit with the raw liquid supply port of the filter;
a filtrate supply passage for connecting the filtrate discharge port of the filter to the filtrate supply port of the concentrator;
a concentrate flow path connected to a concentrate discharge port of the concentrator;
a waste liquid flow path connected to a waste liquid discharge port for discharging the waste liquid separated from the concentrated liquid in the concentrator;
a liquid feeding unit for feeding liquid to each flow path;
a control part for controlling the operation of the liquid feeding part,
the amount of liquid fed from the filter to the concentrator and/or the concentration ratio of the concentrated liquid are adjusted based on the inter-filter-membrane differential pressure of the filter and/or the inter-concentrator-membrane differential pressure of the concentrator.
13. The method of operating a stock solution processing apparatus according to claim 12,
the liquid feeding unit includes:
a liquid feeding section provided in the liquid feeding passage;
A concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
increasing the amount of the raw liquid fed to the filter when the inter-membrane differential pressure of the filter is smaller than the set differential pressure of the filter,
maintaining the amount of the feed liquid of the raw liquid to the filter when the inter-membrane differential pressure of the filter is within the range of the set differential pressure of the filter,
and reducing the amount of the raw liquid sent to the filter when the filter-to-membrane differential pressure is greater than the set filter differential pressure.
14. The method for operating a stock solution processing apparatus according to claim 12 or 13,
the liquid feeding unit includes:
a liquid feeding section provided in the liquid feeding passage;
a concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
increasing the amount of liquid sent from the filter to the concentrator when the inter-concentrator-membrane differential pressure in the concentrator is smaller than a set differential pressure,
maintaining the amount of liquid fed from the filter to the concentrator when the inter-concentrator-membrane differential pressure of the concentrator falls within a predetermined differential pressure range,
And a step of reducing the amount of liquid sent from the filter to the concentrator when the pressure difference between concentrator membranes in the concentrator is greater than a set pressure difference.
15. The method of operating a stock solution treatment apparatus as set forth in any one of claims 12, 13 or 14,
the liquid feeding unit includes:
a liquid feeding section provided in the liquid feeding passage;
a concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
reducing the flow rate of the concentrated solution flow path or increasing the flow rate of the waste liquid flow path when the inter-concentrator-membrane differential pressure of the concentrator is smaller than a set differential pressure,
maintaining the flow rates of the concentrate flow path and the waste liquid flow path when the inter-concentrator-membrane differential pressure of the concentrator falls within a range of a set differential pressure,
and a flow rate control unit configured to increase a flow rate of the concentrated liquid flow path or decrease a flow rate of the waste liquid flow path when a pressure difference between concentrator membranes of the concentrator is greater than a set pressure difference.
16. The method of operating a stock solution processing apparatus according to claim 12,
the liquid feeding unit includes:
a filtrate supply flow path liquid feeding unit provided in the filtrate supply flow path;
A concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
increasing the amount of filtrate fed to the concentrator when the filter membrane differential pressure is smaller than the set filter differential pressure,
maintaining the amount of the filtrate fed to the concentrator when the inter-membrane differential pressure of the filter is within the range of the set differential pressure of the filter,
and reducing the amount of the filtrate fed to the concentrator when the pressure difference between the membranes of the filter is greater than the set pressure difference of the filter.
17. The method of operating a stock solution processing apparatus according to claim 12 or 16,
the liquid feeding unit includes:
a filtrate supply flow path liquid feeding unit provided in the filtrate supply flow path;
a concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
reducing the amount of the concentrated liquid fed to the concentrated liquid flow path or increasing the amount of the waste liquid fed to the waste liquid flow path when the inter-membrane differential pressure of the concentrator is smaller than the set differential pressure of the concentrator,
maintaining the amount of the concentrated solution in the concentrated solution channel and the amount of the liquid fed to the waste solution channel when the pressure difference between membranes in the concentrator falls within a range of a set pressure difference in the concentrator,
And a liquid-feeding amount of the concentrated liquid in the concentrated liquid flow path is increased or a liquid-feeding amount of the waste liquid in the waste liquid flow path is decreased when the inter-membrane differential pressure of the concentrator is larger than a set differential pressure of the concentrator.
18. The method of operating a stock solution treatment apparatus as set forth in any one of claims 12, 16 or 17,
the liquid feeding unit includes:
a filtrate supply flow path liquid feeding unit provided in the filtrate supply flow path;
a concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
increasing the amount of filtrate fed to the concentrator when the pressure difference between the membranes of the concentrator is smaller than the set pressure difference of the concentrator,
maintaining the amount of the filtrate fed to the concentrator when the inter-membrane differential pressure of the concentrator falls within the range of the set differential pressure of the concentrator,
and reducing the amount of the filtrate fed to the concentrator when the pressure difference between membranes of the concentrator is greater than a set pressure difference of the concentrator.
19. The method of operating a stock solution processing apparatus according to claim 12,
the liquid feeding unit includes:
a concentrate flow path liquid feeding unit provided in the concentrate flow path;
A waste liquid channel liquid-feeding section provided in the waste liquid channel,
increasing the amount of the concentrated liquid and/or the amount of the waste liquid to be fed when the pressure difference between the membranes of the filter is smaller than the set pressure difference of the filter,
maintaining the feed amount of the concentrated solution and/or the feed amount of the waste liquid when the filter-to-membrane differential pressure falls within a range of a set filter differential pressure,
and reducing the amount of the concentrated liquid and/or the amount of the waste liquid to be fed when the pressure difference between the membranes of the filter is larger than the set pressure difference of the filter.
20. The method of operating a stock solution processing apparatus according to claim 12 or 19,
the liquid feeding unit includes:
a concentrate flow path liquid feeding unit provided in the concentrate flow path;
a waste liquid channel liquid-feeding section provided in the waste liquid channel,
reducing the amount of the concentrated liquid fed to the concentrated liquid flow path and/or increasing the amount of the waste liquid fed to the waste liquid flow path when the inter-membrane differential pressure of the concentrator is smaller than the set differential pressure of the concentrator,
maintaining the feed amount of the concentrated solution and/or the feed amount of the waste solution in the waste solution channel when the inter-membrane differential pressure of the concentrator falls within a range of a set differential pressure of the concentrator,
And a control unit configured to increase a liquid feeding amount of the concentrated liquid in the concentrated liquid passage and/or decrease a liquid feeding amount of the waste liquid in the waste liquid passage when the inter-membrane differential pressure of the concentrator is greater than a set differential pressure of the concentrator.
21. The method according to any one of claims 12 to 20, wherein the operation of the raw liquid treatment apparatus,
a concentrate container for containing a concentrate is connected to the concentrate flow path, and a flow path for supplying the concentrate in the concentrate container from the concentrate container to the filtrate supply port of the concentrator is provided,
the liquid is sent so that the concentrated liquid flows from the concentrated liquid container to the filtrate supply port of the concentrator.
22. The method according to any one of claims 12 to 21, wherein the operation of the raw liquid treatment apparatus,
when recovering the filtrate and/or the concentrated solution in the apparatus, a gas or a liquid is supplied to the filter.
23. The method of operating a stock solution processing apparatus according to claim 22,
when the operation of recovering the concentrated liquid in the concentrator is performed after the filtrate in the filter is recovered,
and stopping the liquid feeding from the filter to the concentrator if the inter-concentrator-membrane differential pressure of the concentrator is greater than a set differential pressure.
24. The method of operating a stock solution processing apparatus according to claim 23,
after stopping the liquid feeding from the filter to the concentrator, gas is supplied to the filtrate supply channel.
25. The method according to any one of claims 12 to 24, wherein the operation of the stock solution treatment apparatus,
the filter is provided with:
a main body portion having a hollow space inside:
a hollow fiber membrane disposed in the hollow space of the main body,
the filter is disposed so as to supply a raw liquid into the hollow fiber membrane or into the hollow space of the main body,
when the hollow fiber membranes of the filter are cleaned,
discharging the liquid in the hollow space or the hollow fiber membrane in a state where air and/or a cleaning liquid is supplied to the hollow space or the hollow fiber membrane of the main body of the filter, or discharging the liquid in the hollow space and the hollow fiber membrane in a state where air and/or a cleaning liquid is supplied to the hollow space and the hollow fiber membrane of the main body of the filter,
then, a cleaning liquid is supplied into the hollow space of the main body and/or the hollow fiber membrane so as to permeate the hollow fiber membrane and the hollow fiber membrane, or the cleaning liquid is supplied into the hollow fiber membrane so as to permeate the hollow fiber membrane, or the cleaning liquid is supplied into the hollow space of the main body so as to permeate the hollow space of the main body.
26. The method of operating a stock solution processing apparatus according to claim 25,
when the filter discharges the liquid in the hollow space and/or the hollow fiber membranes,
the method includes pressurizing air and/or a cleaning liquid and supplying the pressurized air and/or cleaning liquid into the hollow space and/or the hollow fiber membrane, and/or discharging the liquid in the hollow space and/or the hollow fiber membrane by negative pressure.
27. The method of operating a stock solution treatment apparatus as set forth in claim 25 or 26,
when the filter supplies air and/or a cleaning liquid into the hollow space of the main body and/or the hollow fiber membranes,
the method includes pressurizing air and/or a cleaning liquid and supplying the pressurized air and/or cleaning liquid into the hollow space and/or the hollow fiber membrane, and/or setting the pressure in the hollow space and/or the hollow fiber membrane to a negative pressure.
28. A raw liquid processing apparatus for concentrating a raw liquid to form a concentrated liquid, comprising:
a filter having a filter member for filtering the stock solution;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated solution;
A raw liquid supply unit configured to supply the raw liquid to the filter;
a liquid supply passage for communicating the raw liquid supply unit with the raw liquid supply port of the filter;
a filtrate supply passage for connecting the filtrate discharge port of the filter to the filtrate supply port of the concentrator;
a concentrate flow path connected to a concentrate discharge port of the concentrator;
a waste liquid flow path connected to a waste liquid discharge port for discharging the waste liquid separated from the concentrated liquid in the concentrator;
a liquid feeding unit for feeding liquid to each flow path;
a control part for controlling the operation of the liquid feeding part,
the filter and/or the concentrator have:
a main body having a hollow space therein;
a hollow fiber membrane disposed in the hollow space of the main body,
when cleaning the hollow fiber membranes in the filter and/or the concentrator, the control unit controls the operation of the liquid feed unit so that the liquid permeates the hollow fiber membranes in a state where the hollow space of the main body and/or the hollow fiber membranes are filled with the liquid to fill the region to be cleaned in the hollow fiber membranes.
29. The stock solution processing apparatus as set forth in claim 28,
When cleaning the hollow fiber membranes in the filter and/or the concentrator, the control unit controls the operation of the liquid feed unit so that the liquid permeates the hollow fiber membranes after the hollow space of the main body and/or the hollow fiber membranes are filled with the liquid to a state where the region of the hollow fiber membranes to be cleaned is filled with the liquid.
30. The stock solution treatment apparatus as set forth in claim 28 or 29,
the filter is disposed in a state in which the axial direction of the hollow fiber membrane faces the vertical direction,
the filter includes a port which is disposed above the raw liquid supply port or the filtrate discharge port when the hollow fiber membrane in the filter is cleaned and which is capable of communicating the inside of the hollow space of the main body with the outside,
the control unit controls the operation of the liquid feeding unit so that the hollow space of the main body and/or the hollow fiber membranes are filled with liquid and the liquid permeates the hollow fiber membranes of the filter.
31. The stock solution treatment apparatus as claimed in any one of claims 28, 29 or 30,
The concentrator is disposed in a state in which the axial direction of the hollow fiber membranes is directed in the vertical direction,
the concentrator includes a port which is disposed above the concentrated solution discharge port or the waste solution discharge port when the hollow fiber membranes in the concentrator are cleaned, and which is capable of communicating the inside of the hollow space of the main body with the outside,
the control unit controls the operation of the liquid feeding unit so that the hollow space of the main body and/or the hollow fiber membranes are filled with liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid passes through the hollow fiber membranes of the concentrator in this state.
32. The stock solution treatment apparatus as set forth in claim 28 or 29,
in a state where the filter and/or the concentrator are arranged so that the axial direction of the hollow fiber membranes is directed in the horizontal direction,
the controller controls the operation of the liquid feeder so that the hollow space of the main body and/or the hollow fiber membranes are filled with liquid until the hollow fiber membranes are wholly or partially immersed in the liquid, and the liquid is allowed to permeate the hollow fiber membranes in this state.
33. A raw liquid processing apparatus for concentrating a raw liquid to form a concentrated liquid, comprising:
a filter having a filter member for filtering the stock solution;
a concentrator to which the filtrate filtered by the filter is supplied and which concentrates the filtrate to form the concentrated solution;
a raw liquid supply unit configured to supply the raw liquid to the filter;
a liquid supply passage for communicating the raw liquid supply unit with the raw liquid supply port of the filter;
a filtrate supply passage for connecting the filtrate discharge port of the filter to the filtrate supply port of the concentrator;
a concentrate flow path connected to a concentrate discharge port of the concentrator;
a waste liquid flow path connected to a waste liquid discharge port for discharging the waste liquid separated from the concentrated liquid in the concentrator;
a liquid feeding unit for feeding liquid to each flow path;
a control part for controlling the operation of the liquid feeding part,
the control unit controls the operation of the liquid feeding unit based on a filter membrane-to-membrane differential pressure of the filter and/or a concentrator membrane-to-membrane differential pressure of the concentrator, thereby adjusting the amount of liquid fed from the filter to the concentrator and/or the concentration ratio of the concentrated liquid.
34. The stock solution processing apparatus as set forth in claim 33,
the liquid feeding part comprises:
a liquid feeding section provided in the liquid feeding passage;
a concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
the control unit controls the operation of the liquid feeding unit as follows:
increasing the amount of the raw liquid fed to the filter when the inter-membrane differential pressure of the filter is smaller than the set differential pressure of the filter,
maintaining the amount of the feed liquid of the raw liquid to the filter when the inter-membrane differential pressure of the filter is within the range of the set differential pressure of the filter,
and reducing the amount of the raw liquid sent to the filter when the filter-to-membrane differential pressure is greater than the set filter differential pressure.
35. The stock solution treatment apparatus as set forth in claim 33 or 34,
the liquid feeding part comprises:
a liquid feeding section provided in the liquid feeding passage;
a concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
the control unit controls the operation of the liquid feeding unit as follows:
Increasing the amount of liquid sent from the filter to the concentrator when the inter-concentrator-membrane differential pressure in the concentrator is smaller than a set differential pressure,
maintaining the amount of liquid fed from the filter to the concentrator when the inter-concentrator-membrane differential pressure of the concentrator falls within a predetermined differential pressure range,
and a step of reducing the amount of liquid sent from the filter to the concentrator when the pressure difference between concentrator membranes in the concentrator is greater than a set pressure difference.
36. The stock solution treatment apparatus as claimed in any one of claims 33, 34 or 35,
the liquid feeding part comprises:
a liquid feeding section provided in the liquid feeding passage;
a concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
the control unit controls the operation of the liquid feeding unit as follows:
reducing the flow rate of the concentrated solution flow path or increasing the flow rate of the waste liquid flow path when the inter-concentrator-membrane differential pressure of the concentrator is smaller than a set differential pressure,
maintaining the flow rates of the concentrate flow path and the waste liquid flow path when the inter-concentrator-membrane differential pressure of the concentrator falls within a range of a set differential pressure,
And a flow rate control unit configured to increase a flow rate of the concentrated liquid flow path or decrease a flow rate of the waste liquid flow path when a pressure difference between concentrator membranes of the concentrator is greater than a set pressure difference.
37. The stock solution processing apparatus as set forth in claim 33,
the liquid feeding part comprises:
a filtrate supply flow path liquid feeding unit provided in the filtrate supply flow path;
a concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
the control unit controls the operation of the liquid feeding unit as follows:
increasing the amount of the filtrate fed to the concentrator when the pressure difference between the membranes of the filter is smaller than the set pressure difference of the filter,
maintaining the amount of the filtrate fed to the concentrator when the inter-membrane differential pressure of the filter is within the range of the set differential pressure of the filter,
and reducing the amount of the filtrate fed to the concentrator when the pressure difference between the membranes of the filter is greater than the set pressure difference of the filter.
38. The stock solution treatment apparatus as set forth in claim 33 or 37,
the liquid feeding part comprises:
a filtrate supply flow path liquid feeding unit provided in the filtrate supply flow path;
A concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
the control unit controls the operation of the liquid feeding unit as follows:
reducing the amount of the concentrated liquid fed to the concentrated liquid flow path or increasing the amount of the waste liquid fed to the waste liquid flow path when the inter-membrane differential pressure of the concentrator is smaller than the set differential pressure of the concentrator,
maintaining the feed amount of the concentrated solution in the concentrated solution channel and the feed amount of the waste solution in the waste solution channel when the inter-membrane differential pressure of the concentrator falls within a range of a set differential pressure of the concentrator,
and a liquid-feeding amount of the concentrated liquid in the concentrated liquid flow path is increased or a liquid-feeding amount of the waste liquid in the waste liquid flow path is decreased when the inter-membrane differential pressure of the concentrator is larger than a set differential pressure of the concentrator.
39. The stock solution treatment apparatus as claimed in any one of claims 33, 37 or 38,
the liquid feeding part comprises:
a filtrate supply flow path liquid feeding unit provided in the filtrate supply flow path;
a concentrate flow path liquid feeding section provided in the concentrate flow path or a waste liquid flow path liquid feeding section provided in the waste liquid flow path,
The control unit controls the operation of the liquid feeding unit as follows:
increasing the amount of filtrate fed to the concentrator when the pressure difference between the membranes of the concentrator is smaller than the set pressure difference of the concentrator,
maintaining the amount of the filtrate fed to the concentrator when the inter-membrane differential pressure of the concentrator falls within the range of the set differential pressure of the concentrator,
and reducing the amount of the filtrate fed to the concentrator when the pressure difference between membranes of the concentrator is greater than a set pressure difference of the concentrator.
40. The stock solution processing apparatus as set forth in claim 33,
the liquid feeding part comprises:
a concentrate flow path liquid feeding unit provided in the concentrate flow path;
a waste liquid channel liquid-feeding section provided in the waste liquid channel,
the control unit controls the operation of the liquid feeding unit as follows:
increasing the amount of the concentrated liquid to be fed and/or decreasing the amount of the waste liquid to be fed when the pressure difference between the membranes of the filter is smaller than the set pressure difference of the filter,
maintaining the feed amount of the concentrated liquid and the feed amount of the waste liquid when the filter-to-membrane differential pressure falls within a range of a set filter differential pressure,
And a step of decreasing the amount of the concentrated liquid to be fed and/or increasing the amount of the waste liquid to be fed when the pressure difference between the membranes of the filter is larger than the set pressure difference of the filter.
41. The stock solution processing apparatus as set forth in claim 33 or 40,
the liquid feeding part comprises:
a concentrate flow path liquid feeding unit provided in the concentrate flow path;
a waste liquid channel liquid-feeding section provided in the waste liquid channel,
the control unit controls the operation of the liquid feeding unit as follows:
reducing the amount of the concentrated liquid fed to the concentrated liquid flow path and/or increasing the amount of the waste liquid fed to the waste liquid flow path when the inter-membrane differential pressure of the concentrator is smaller than the set differential pressure of the concentrator,
maintaining the feed amount of the concentrated solution and/or the feed amount of the waste solution in the waste solution channel when the inter-membrane differential pressure of the concentrator falls within a range of a set differential pressure of the concentrator,
and a control unit configured to increase a liquid feeding amount of the concentrated liquid in the concentrated liquid passage and/or decrease a liquid feeding amount of the waste liquid in the waste liquid passage when the inter-membrane differential pressure of the concentrator is greater than a set differential pressure of the concentrator.
42. The stock solution treatment apparatus as claimed in any one of claims 33 to 41,
a concentrate container for containing a concentrate is connected to the concentrate flow path, and a flow path for supplying the concentrate in the concentrate container from the concentrate container to the filtrate supply port of the concentrator is provided,
the control unit controls the operation of the liquid feed unit so that the concentrated liquid flows from the concentrated liquid container to the filtrate supply port of the concentrator.
43. The stock solution treatment apparatus as claimed in any one of claims 33 to 42,
the control unit supplies gas or liquid to the filter when performing an operation of recovering the filtrate in the filter.
44. The stock solution processing apparatus as set forth in claim 43,
when the control unit performs an operation of recovering the concentrated solution in the concentrator after recovering the filtrate in the filter,
and a control unit that controls operation of the liquid feed unit to stop liquid feed from the filter to the concentrator when a pressure difference between concentrator membranes of the concentrator is greater than a set pressure difference.
45. The stock solution processing apparatus as set forth in claim 44,
a gas supply unit for supplying gas to the filtrate supply passage,
The control unit controls the operation of the liquid feeding unit to stop the liquid feeding from the filter to the concentrator, and then controls the operation of the gas supply unit to supply gas to the filtrate supply flow path.
46. The stock solution treatment apparatus as claimed in any one of claims 28 to 45,
the liquid feeding section is a roller pump device having a roller with a tube disposed between the roller and the holder,
the liquid feeding part is provided with a pipe positioning component for holding the pipe wound on the roller of the roller pump device,
the pipe positioning member includes: a pair of holding members arranged at intervals in the axial direction of the pipe;
a connecting member for maintaining the pair of holding members at a predetermined distance apart from each other in the axial direction of the pipe,
a plurality of tube holding portions for holding a plurality of tubes are provided in a row on each of the holding members,
the plurality of tube holding parts are arranged such that,
when the plurality of tubes are arranged so that the same tube is held by the corresponding tube holding portion of the pair of holding members, the plurality of tubes are parallel to each other,
the connecting member is formed in such a manner that,
between the pair of holding members, the plurality of tubes can be bent in a direction intersecting with the direction in which the plurality of tube holding portions are aligned and the axial direction of the plurality of tubes held by the plurality of tube holding portions,
The connecting member is disposed in a state in which the connecting member is extended such that the axial direction of the plurality of tubes held by the plurality of tube holding portions is parallel to the longitudinal direction of the connecting member.
47. The stock solution processing apparatus as set forth in claim 46,
the coupling member is provided in the following manner: when viewed from a direction in which the plurality of tube holding portions are aligned and a direction intersecting an axial direction of the plurality of tubes held by the plurality of tube holding portions in a state in which the coupling member is extended, the coupling member is positioned between adjacent tubes held by the plurality of tube holding portions.
48. The stock solution processing apparatus as set forth in claim 46 or 47,
the connecting member is disposed as follows:
the plurality of tube holding portions are arranged in a direction intersecting with an axial direction of the plurality of tubes held by the plurality of tube holding portions, and are offset from a central axis of the plurality of tubes held by the plurality of tube holding portions.
49. The stock solution processing apparatus as set forth in any one of claims 46, 47 or 48,
the pair of holding members are formed in an asymmetrical shape with respect to a line bisecting the holding members in a direction in which the plurality of tube holding portions are arranged.
50. The stock solution treatment apparatus as claimed in any one of claims 46, 47, 48 or 49,
the control unit has a function of rotating the roller in the normal direction and the reverse direction when the pipe is disposed between the bracket and the roller.
51. The stock solution processing apparatus as set forth in claim 50,
the control unit has a function of sending an abnormality alarm when the rotational resistance becomes equal to or greater than a predetermined value when the roller is rotated in the normal direction and the reverse direction.
52. The stock solution processing apparatus as set forth in claim 50 or 51,
the roller pump device comprises a pair of accommodating parts, a pair of holding members for arranging the pipe positioning member,
the pair of housing portions are provided at positions sandwiching a surface including the rotation shaft of the roller.
53. The stock solution treatment apparatus as set forth in any one of claims 28 to 53,
a tube holder for holding a tube is provided,
and is provided with:
a main body portion;
a plurality of holding portions provided on the first surface of the main body portion and detachably holding a plurality of tubes;
a connecting part for connecting the main body part to other appliances,
the plurality of holding portions are arranged such that, when the plurality of tubes are held by the plurality of holding portions, the plurality of tubes are parallel to each other in the axial direction and are aligned along the surface of the first surface of the main body portion.
54. The stock solution processing apparatus as set forth in claim 53,
the coupling portion includes an engaging member protruding toward a second surface side opposite to a first surface of the body portion or protruding toward the first surface side,
the engaging member has an opening formed at one end and a gap continuous with the opening.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2018153760A JP6667852B2 (en) | 2018-08-18 | 2018-08-18 | Stock solution processing device and method of operating stock solution processing device |
| JP2018-153760 | 2018-08-18 | ||
| JP2019-149495 | 2019-08-16 | ||
| JP2019149495A JP7411924B2 (en) | 2019-08-16 | 2019-08-16 | How to clean instruments, how to operate the stock solution processing equipment and the stock solution processing equipment |
| PCT/JP2019/032204 WO2020040069A1 (en) | 2018-08-18 | 2019-08-17 | Undiluted solution treatment device, method for operating undiluted solution treatment device, and method for cleaning instrument |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112703022A true CN112703022A (en) | 2021-04-23 |
Family
ID=69592926
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201980058425.9A Pending CN112703022A (en) | 2018-08-18 | 2019-08-17 | Raw liquid processing apparatus, method for operating raw liquid processing apparatus, and method for cleaning instrument |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN112703022A (en) |
| WO (1) | WO2020040069A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2022063108A (en) * | 2020-10-09 | 2022-04-21 | 旭化成メディカル株式会社 | Body cavity liquid treatment system |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101801507A (en) * | 2007-09-18 | 2010-08-11 | 旭化成化学株式会社 | Hollow yarn film filtering apparatus |
| JP2015157054A (en) * | 2014-02-25 | 2015-09-03 | 旭化成メディカル株式会社 | Method for concentrating abdominal dropsy or pleural effusion filtrate and system for concentrating the same |
| CN106794287A (en) * | 2014-10-16 | 2017-05-31 | 旭化成医疗株式会社 | The filter method of hollow fiber membrane-type body fluid filter and protein solution |
| CN106999855A (en) * | 2015-01-07 | 2017-08-01 | 旭化成医疗株式会社 | Filter, body cavity liquid treating system and body cavity liquid processing method |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6230907B2 (en) * | 2013-12-27 | 2017-11-15 | 旭化成メディカル株式会社 | Ascites filtration and concentration system, filter and concentrator washing method in ascites filtration and concentration system, and filtrate and concentrate recovery method during washing of filter and concentrator |
| WO2017170797A1 (en) * | 2016-03-29 | 2017-10-05 | 国立大学法人徳島大学 | Stock solution processing device, roller pump device, and bag arrangement method |
| JP6250847B1 (en) * | 2017-01-12 | 2017-12-20 | アトムメディカル株式会社 | Tube holder |
| JP6501421B2 (en) * | 2017-07-07 | 2019-04-17 | 旭化成メディカル株式会社 | Body cavity fluid treatment device |
| JP6532913B2 (en) * | 2017-07-07 | 2019-06-19 | 旭化成メディカル株式会社 | Body cavity fluid treatment device |
-
2019
- 2019-08-17 CN CN201980058425.9A patent/CN112703022A/en active Pending
- 2019-08-17 WO PCT/JP2019/032204 patent/WO2020040069A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101801507A (en) * | 2007-09-18 | 2010-08-11 | 旭化成化学株式会社 | Hollow yarn film filtering apparatus |
| JP2015157054A (en) * | 2014-02-25 | 2015-09-03 | 旭化成メディカル株式会社 | Method for concentrating abdominal dropsy or pleural effusion filtrate and system for concentrating the same |
| CN106794287A (en) * | 2014-10-16 | 2017-05-31 | 旭化成医疗株式会社 | The filter method of hollow fiber membrane-type body fluid filter and protein solution |
| CN106999855A (en) * | 2015-01-07 | 2017-08-01 | 旭化成医疗株式会社 | Filter, body cavity liquid treating system and body cavity liquid processing method |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2020040069A1 (en) | 2020-02-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP4091873B2 (en) | Dialysis machine | |
| JP5519427B2 (en) | Hemodialysis machine | |
| US11679190B2 (en) | Blood treatment device priming devices, methods, and systems | |
| US20160022895A1 (en) | Stock solution concentrating device, stock solution treatment device, and circulation-type treatment device | |
| EP2708249B1 (en) | Dialysis device | |
| JP5217355B2 (en) | Blood purification control device | |
| JP2004049494A (en) | Automatic blood return system | |
| JP6960906B2 (en) | How to arrange undiluted solution treatment equipment, roller pump equipment and bags | |
| CN112703022A (en) | Raw liquid processing apparatus, method for operating raw liquid processing apparatus, and method for cleaning instrument | |
| JP2023105264A (en) | Liquid concentrate processor, and operation method of liquid concentrate processor | |
| JP6667852B2 (en) | Stock solution processing device and method of operating stock solution processing device | |
| JP7422986B2 (en) | Undiluted solution processing equipment and how to operate the undiluted solution processing equipment | |
| JP7411924B2 (en) | How to clean instruments, how to operate the stock solution processing equipment and the stock solution processing equipment | |
| JP2009165500A (en) | Blood purifying device and priming method thereof | |
| JP6646733B2 (en) | Blood purification system and priming method thereof | |
| WO2023021967A1 (en) | Stock solution treatment apparatus, stock solution treatment apparatus operating method, and adjuster | |
| WO2020096016A1 (en) | Blood purification device | |
| JP6953162B2 (en) | Blood purifier | |
| JP6011701B2 (en) | Dialysis machine | |
| JP2022107559A (en) | Thoracicoabdominal fluid processing system and cleaning method therefor | |
| JP2004049496A (en) | Automatic blood return system | |
| JP5822152B2 (en) | Hemodialysis machine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20221018 Address after: Japan in Nara County Applicant after: Takatori Corp. Address before: Tokushima County, Japan Applicant before: THE University OF TOKUSHIMA Applicant before: Takatori Corp. |