CN117642193A - Stock solution treatment device, method for operating stock solution treatment device, and adjustment tool - Google Patents
Stock solution treatment device, method for operating stock solution treatment device, and adjustment tool Download PDFInfo
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- CN117642193A CN117642193A CN202280050017.0A CN202280050017A CN117642193A CN 117642193 A CN117642193 A CN 117642193A CN 202280050017 A CN202280050017 A CN 202280050017A CN 117642193 A CN117642193 A CN 117642193A
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- 239000000706 filtrate Substances 0.000 claims abstract description 441
- 239000012141 concentrate Substances 0.000 claims abstract description 275
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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
-
- 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
- A61M39/00—Tubes, tube connectors, tube couplings, valves, access sites or the like, specially adapted for medical use
- A61M39/22—Valves or arrangement of valves
- A61M39/28—Clamping means for squeezing flexible tubes, e.g. roller clamps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
- B01D65/06—Membrane cleaning or sterilisation ; Membrane regeneration with special washing compositions
Landscapes
- Health & Medical Sciences (AREA)
- Heart & Thoracic Surgery (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Chemical & Material Sciences (AREA)
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- Hematology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biomedical Technology (AREA)
- General Health & Medical Sciences (AREA)
- Public Health (AREA)
- Veterinary Medicine (AREA)
- Water Supply & Treatment (AREA)
- Anesthesiology (AREA)
- Pulmonology (AREA)
- Vascular Medicine (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A stock solution treatment apparatus capable of improving the treatment efficiency of a stock solution and facilitating the control of the apparatus, and an operation method thereof, wherein the apparatus comprises a filter (10), a concentrator (20), a stock solution supply Unit (UB), a feed liquid flow path (2), a filtrate supply flow path (3), a concentrate flow path (4), a waste liquid flow path (5), a recovery unit (CB) for recovering a concentrate connected to the concentrate flow path, a branch flow path (6) for connecting the recovery unit and the filtrate supply flow path, a liquid feed unit (3 p) provided between a connection portion between the filtrate supply flow path and the branch flow path and the concentrator, and a control unit (30) for controlling the operation of the liquid feed unit, and the liquid feed unit is operated as follows: starting gravity filtration of the stock solution supplied to the filter from a stock solution supply unit disposed above a stock solution supply port (11 a) of the filter by gravity, and if the filter is in a predetermined state, feeding the stock solution from the filter to the concentrator, or transporting the stock solution transfer unit as follows: the gravity filtration is started while liquid is fed from the filter to the concentrator.
Description
Technical Field
The present invention relates to a raw liquid treatment apparatus, an operation method of the raw liquid treatment apparatus, and an adjustment tool. More specifically, the present invention relates to a stock solution treatment apparatus for obtaining a treatment solution by filtering or concentrating a stock solution such as a pleural and abdominal effusion accumulated in the chest or abdomen, or a waste liquid and plasma in a plasma exchange therapy in cancerous thoracoperitoneal inflammation, liver cirrhosis, etc., and a method for operating the stock solution treatment apparatus, and an adjusting tool used for the stock solution treatment apparatus.
Background
In cancerous thoracoperitonitis, liver cirrhosis, and the like, there is a possibility that pleural effusion or peritoneal effusion is accumulated in the chest cavity or abdominal cavity, and in a state where such pleural effusion is accumulated, there is a problem that the thoracoabdominal cavity is forced to surrounding internal organs, and the like. In order to solve such a problem, the treatment of extracting the pleuroperitoneal cavity effusion may be performed by puncturing.
On the other hand, the pleuroperitoneal cavity effusion contains a part or all of the plasma component exuded from the blood, and the plasma contains a main protein (for example, albumin, globulin, etc.). Although the above symptoms can be improved by extracting the pleuroperitoneal cavity effusion, components useful for the human body such as proteins are lost together with water. Therefore, it is necessary to administer albumin preparations, globulin preparations, etc. intravenously and the like to replenish lost components.
However, although albumin preparations, globulin preparations, and the like can be administered intravenously to supplement specific components, the preparations are expensive and the treatment costs are high.
Further, since a limited amount of a specific component among the lost components can be supplied, there is a possibility that the nutrition may be insufficient and the infection may be easy.
Accordingly, a therapeutic method for intravenous administration of a treatment solution obtained by treating a pleural effusion or a peritoneal effusion (hereinafter, referred to as "stock solution") extracted from the thoracic cavity or the peritoneal cavity, i.e., a so-called pleuroperitoneal effusion filtration concentration and reinfusion method (Cell-free and Concentrated Ascites Reinfusion Therapy; CART) has been developed. In the case of CART, since most of the active ingredients other than the cellular ingredients contained in the pleural effusion and the peritoneal effusion can be returned to the body of the patient, the ingredients lost from the blood can be effectively supplied to the patient without being limited to the specific ingredients. Even if the concentrated solution is administered, the insufficient component is only required to be supplemented by the preparation so as to correspond to the insufficient amount, and therefore the amount of the albumin preparation or the like to be used can be reduced as much as possible, and the treatment cost can be suppressed.
In CART, the pleural effusion or peritoneal effusion is filtered and concentrated to produce a treatment fluid that is returned to the patient. In a treatment apparatus for generating such a treatment liquid, a stock solution 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 to separate a liquid component (hereinafter, sometimes referred to as filtrate). If 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 treatment solution can be obtained.
When a stock solution such as pleural effusion or peritoneal effusion is supplied to a filter, there are a method of supplying the stock solution to the filter by gravity and a method of supplying the stock solution to the filter by a pump or the like (see patent documents 1 to 6). When the stock solution is supplied to the filter by a pump or the like, the stock solution can be stably supplied to the filter even if the viscosity of the stock solution is high. In addition, since the flow of the stock solution in the circuit can be controlled freely to some extent by using a plurality of pumps, the filtration and concentration process of the stock solution can be controlled appropriately, and the cleaning operation of the circuit, the filter, and the like can be performed easily.
However, in the case of CART being used at the bedside, it is desirable that the apparatus is as small as possible, and if a plurality of pumps are provided, the apparatus is enlarged. Further, if the number of pumps is increased, the flow of the stock solution in the circuit can be controlled freely to some extent, but on the other hand, in order to achieve proper filtration and concentration, the operation of a plurality of pumps must be controlled, and the control of the apparatus becomes difficult.
Patent document 7 discloses a body fluid filtering and concentrating device in which a pump is provided between a filter and a concentrator, and a raw fluid can be caused to flow by the pump alone. The following is noted: in this body fluid filtration and concentration device, a throttle valve is provided in a passage between the concentrator and the concentrated body fluid collection container, and a pressure difference between hollow fiber membranes of the concentrator is added to the throttle valve, so that concentration in the concentrator is smoothly performed.
Prior art literature
Patent literature
Patent document 1: japanese patent No. 5062631
Patent document 2: japanese patent application laid-open No. 2015-126763
Patent document 3: japanese patent application laid-open No. 2019-13487
Patent document 4: japanese patent application laid-open No. 2019-13488
Patent document 5: japanese patent laid-open No. 2020-25825
Patent document 6: japanese patent laid-open No. 2020-25864
Patent document 7: japanese patent application laid-open No. 2543466
Disclosure of Invention
Technical problem to be solved by the utility model
However, in patent document 7, a method of supplying the stock solution to the filter by the driving force of the pump is adopted. Therefore, when the viscosity of the stock solution is low, the initial treatment becomes slower than when the stock solution is supplied to the filter by gravity, and thus the total treatment time may be longer.
In patent document 7, a throttle valve is provided in the passage between the concentrator and the concentrated body fluid collection container instead of a pump to adjust the pressure difference between the membranes of the concentrator. Therefore, when the flow rate of the filtrate supplied to the concentrator fluctuates, it is necessary to adjust the pressure difference between the membranes of the concentrator by a throttle valve. Thus, in order to achieve proper filtration and concentration by the body fluid filtration and concentration device of patent document 7, both the pump and the throttle valve must be controlled, as in the case of providing a plurality of pumps, although only one pump is used, the control of the device becomes difficult.
In view of such circumstances, an object of the present invention is to provide a raw liquid treatment apparatus and an operation method of the raw liquid treatment apparatus, which can improve the treatment efficiency of raw liquid and facilitate control of the apparatus.
Further, an object is to provide an adjusting tool that can be used in the above-described raw liquid treatment apparatus.
Solution to the above technical problems
< stock solution treatment device >
The stock solution treatment apparatus according to claim 1 is an apparatus for forming a concentrated solution by filtering and concentrating a stock solution, 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 liquid supply channel arranged above the raw liquid supply port of the filter and communicating a raw liquid supply unit for supplying the raw liquid to the filter with the raw liquid supply port of the filter; a filtrate supply channel that communicates a filtrate discharge port of the filter with a 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 waste liquid separated from the concentrated liquid in the concentrator; a recovery unit disposed below the filtrate outlet of the filter, connected to the concentrate flow path, and configured to recover concentrate; a branch flow path for communicating the recovery unit with the filtrate supply flow path; a liquid feed portion provided between the concentrator and a connection portion of the filtrate supply flow path connected to the branch flow path; and a control unit that controls operation of the liquid feeding unit, wherein the control unit controls operation of the liquid feeding unit in such a manner that the branch flow path is maintained so as to be in a state in which liquid flows bi-directionally between the filtrate supply flow path and the recovery unit, by: and starting gravity filtration for supplying the raw liquid to the filter from the raw liquid supply portion disposed above the raw liquid supply port of the filter by gravity, and when the raw liquid is in a predetermined state, supplying the liquid from the filter to the concentrator, or controlling the operation of the liquid supply portion by: and starting gravity filtration, wherein the gravity filtration is used for supplying the stock solution to the filter from the stock solution supply part arranged above the stock solution supply port of the filter by gravity and simultaneously sending the liquid from the filter to the concentrator.
In the stock solution treatment apparatus according to claim 2, in claim 1, the predetermined state is a state in which the amount of the filtrate supplied to the recovery unit from the start of gravity filtration exceeds the amount of the liquid that can be accommodated in the recovery unit.
In the stock solution treatment apparatus according to claim 3, in claim 1 or claim 2, an adjustment unit for adjusting the concentrate passage to a predetermined state is provided in the concentrate passage.
In the stock solution treatment apparatus according to claim 4, in claim 3, the control unit controls the operation of the liquid feeding unit to adjust the flow rate of the liquid supplied to the concentrator, and controls the differential pressure between the concentrator membranes of the concentrator.
In the stock solution treatment apparatus according to claim 5, in claim 3 or claim 4, the concentrated solution flow path is a tube having a deformable cross section, the adjustment portion is a member having a gap in which the tube is disposed, and the gap of the adjustment portion is formed to have the following length: when water is flowed at 50mL/min in the tube disposed in the gap, the average pressure of the water in the tube can be maintained at a length of 10mmHg to 100 mmHg.
In the stock solution treatment apparatus according to claim 6, in claim 3 or claim 4, the concentrated solution flow path is a tube having a deformable cross section, the adjustment portion is a member having a gap in which the tube is disposed, and the gap of the adjustment portion is adjusted so that the total wall thickness of the tube is 95% to 110% in a state in which the tube is disposed in the gap.
In the stock solution treatment apparatus according to claim 7, in the 3 rd or 4 th aspect, the concentrated solution flow path is a pipe having a circular cross section formed of polyvinyl chloride or silicone rubber, the adjustment portion is a member having a gap in which the pipe is disposed, the pipe has an outer diameter of 3.0 to 12.0mm, an inner diameter of 2.0 to 8.0mm, and a wall thickness of 0.5 to 2.0mm, and the gap of the adjustment portion has a width of 0.95 to 4.40mm.
< method of operating stock solution treatment device >
The method of operating a stock solution treatment apparatus according to claim 8 is a method of operating an apparatus for forming a concentrated solution by filtering and concentrating a stock solution, 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 stock solution supply unit configured to supply the stock solution to the filter; a liquid supply passage for communicating the liquid supply portion with a liquid supply port of the filter; a filtrate supply channel that communicates a filtrate discharge port of the filter with a 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 waste liquid separated from the concentrated liquid in the concentrator; a recovery unit connected to the concentrate flow path and disposed below the filtrate outlet of the filter, for recovering the concentrate; a branch flow path for communicating the recovery unit with the filtrate supply flow path; a liquid feed portion provided between the concentrator and a connection portion of the filtrate supply flow path connected to the branch flow path; a control unit that controls operation of the liquid feeding unit, and operates the liquid feeding unit in such a manner that the branching flow path is maintained so that liquid flows in both directions between the filtrate supply flow path and the recovery unit, by: and starting gravity filtration for supplying the raw liquid to the filter from the raw liquid supply portion disposed above the raw liquid supply port of the filter by gravity, and when the raw liquid is in a predetermined state, feeding the liquid from the filter to the concentrator, or operating the liquid feeding portion by: and starting gravity filtration, wherein the gravity filtration is used for supplying the stock solution to the filter from the stock solution supply part arranged above the stock solution supply port of the filter by gravity and simultaneously sending the liquid from the filter to the concentrator.
In the method of operating the stock solution treatment apparatus according to claim 9, in claim 8, the predetermined state is a state in which the amount of the filtrate supplied to the recovery unit from the start of gravity filtration exceeds the amount of the liquid that can be accommodated in the recovery unit.
The method of operating the stock solution treatment apparatus according to claim 10 is characterized in that, in claim 8 or 9, the concentrate flow path is adjusted to a predetermined state.
In the method of operating the stock solution treatment apparatus according to claim 11, in claim 10, the flow rate of the liquid supplied to the concentrator is adjusted, and the differential pressure between the concentrator membranes of the concentrator is controlled.
In the method of operating the stock solution treatment apparatus according to claim 12, in the 10 th or 11 th aspect, the concentrated solution flow path is a pipe having a deformable cross section, the adjustment portion is a member having a gap in which the pipe is disposed, and the gap of the adjustment portion is formed to have the following length: when water is flowed at 50mL/min in the tube disposed in the gap, the average pressure of the water in the tube can be maintained at a length of 10mmHg to 100 mmHg.
In the method of operating the stock solution treatment apparatus according to claim 13, in the 10 th or 11 th aspect, the concentrated solution flow path is a pipe having a deformable cross section, the adjustment portion is a member having a gap in which the pipe is disposed, and the gap of the adjustment portion is adjusted so that the total wall thickness of the pipe is 95% to 110% in a state in which the pipe is disposed in the gap.
In the method of operating the stock solution treatment apparatus according to claim 14, in the 10 th or 11 th aspect, the concentrated solution flow path is a pipe having a circular cross section formed of polyvinyl chloride or silicone rubber, the adjustment portion is a member having a gap in which the pipe is disposed, the pipe has an outer diameter of 3.0 to 12.0mm, an inner diameter of 2.0 to 8.0mm, and a wall thickness of 0.5 to 2.0mm, and the gap of the adjustment portion has a width of 0.95 to 4.40mm.
The method of operating a stock solution treatment apparatus according to claim 15 is characterized in that, in any one of inventions 8 to 14, the filter has 2 stock solution supply ports, the stock solution supply port located above in the filtering and concentrating operation among the 2 stock solution supply ports is connected to the liquid supply flow path, the cleaning liquid is supplied from the filtrate discharge port in the filter when the filter is cleaned, and the cleaning liquid is discharged from either the stock solution supply port located below in the filtering and concentrating operation among the 2 stock solution supply ports or both of the 2 stock solution supply ports.
In the method of operating the stock solution treatment apparatus according to claim 16, in claim 15, the cleaning solution is supplied from the waste liquid discharge port of the thickener, and the cleaning solution is discharged from the stock solution supply port or both of the 2 stock solution supply ports of the filter located below during the filtering and concentrating operation.
< adjusting tool >
The adjustment instrument according to claim 17 is characterized by comprising 2 tube holding members, wherein the 2 tube holding members form a gap in which a tube having a deformable cross section is disposed, and wherein the width of the gap formed between the 2 tube holding members is formed to have the following length: when water is flowed at 50mL/min in a tube disposed in a gap, the average pressure of water in the tube can be maintained at a length of 10mmHg to 100 mmHg.
In the adjustment tool according to the 18 th aspect of the invention, in the 17 th aspect of the invention, the tube disposed in the gap between the 2 tube holding members is a tube having a circular cross section formed of a deformable material, and the width of the gap formed between the 2 tube holding members is adjusted so that the length of the smallest portion of the inner diameter of the tube becomes 95% to 110% of the total wall thickness of the tube in a state where the tube is disposed in the gap.
In the adjustment instrument according to the 19 th aspect of the invention, in the 18 th aspect, the tube disposed in the gap between the 2 tube holding members is a tube having a circular cross section and made of polyvinyl chloride or silicone rubber, and has an outer diameter of 3.0 to 12.0mm, an inner diameter of 2.0 to 8.0mm, and a wall thickness of 0.5 to 2.0mm, and a width of the gap formed between the 2 tube holding members of 0.95 to 4.40mm.
In the adjustment instrument according to claim 20, in the 17 th, 18 th or 19 th invention, the 2 pipe holding members are formed so that the radius of curvature of the portion facing each other and contacting the pipe is 1 to 10mm.
In the adjustment instrument according to claim 21, in the 17 th, 18 th, 19 th, or 20 th invention, the tube holding members are provided with 3 or more gaps in which the tubes are disposed are formed between adjacent tube holding members, and the tube holding members are disposed so that the widths of the gaps are different from each other.
The adjustment instrument according to claim 22 is the instrument according to any one of claims 17 to 21, which is used as the adjustment unit of the stock solution treatment apparatus according to claim 3.
Effects of the invention
< stock solution treatment device >
According to the inventions 1 and 2, the stock solution can be efficiently supplied from the stock solution supply unit to the filter, and therefore the treatment efficiency of the stock solution can be improved.
According to claim 3, when the concentrate flow path is adjusted to a predetermined state by the adjusting portion, adjustment of the concentrate state becomes easy.
According to the invention of claim 4, the differential pressure between the concentrator membranes of the concentrator can be adjusted to a predetermined pressure by controlling only the operation of the liquid feeding portion, and thus the control of the apparatus becomes easy.
According to the invention of the 5 th to 7 th, the structure of the adjustment section can be simplified, and therefore the structure of the device can be simplified.
< method of operating stock solution treatment device >
According to the inventions 8 and 9, the stock solution can be efficiently supplied from the stock solution supply unit to the filter, and therefore the treatment efficiency of the stock solution can be improved.
According to the 10 th aspect of the present invention, when the concentrate flow path is adjusted to a predetermined state by the adjusting section, adjustment of the concentrate state is facilitated.
According to the invention of claim 4, the differential pressure between the concentrator membranes of the concentrator can be adjusted to a predetermined pressure by controlling only the operation of the liquid feeding portion, and thus the control of the apparatus becomes easy.
According to inventions 12 to 14, the structure of the adjustment unit can be simplified, and therefore the structure of the device can be simplified.
According to the 15 th aspect, the filter can be efficiently cleaned.
According to the 16 th aspect, the cleaning of the entire apparatus can be efficiently performed.
< adjusting tool >
According to the 17 th to 20 th inventions, the pressure in the pipe on the upstream side of the gap can be maintained at an appropriate value by adjusting the flow rate supplied to the pipe.
According to the 21 st aspect, the pipe can be disposed in an appropriate gap.
According to the invention 22, the load on the concentrator in the stock solution treatment apparatus can be reduced, and the concentrated solution can be adjusted to a desired concentrated state.
Drawings
Fig. 1 is a circuit diagram of a stock solution treatment apparatus 1 according to the present embodiment and is a schematic explanatory diagram of a circuit diagram for performing a filtration and concentration operation.
Fig. 2 is a schematic explanatory view of a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, in order to perform a preparation cleaning operation.
Fig. 3 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment and is a schematic explanatory diagram of a circuit diagram for performing a filtering operation.
Fig. 4 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, and is a schematic explanatory diagram of another circuit diagram for performing the filtering and concentrating operation.
Fig. 5 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment and is a schematic explanatory diagram of a circuit diagram for performing a filter cleaning operation.
Fig. 6 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment and is a schematic explanatory diagram of a circuit diagram for performing a re-concentration operation.
Fig. 7 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, and is a schematic explanatory diagram of a circuit diagram for performing a work of recovering a liquid from the filter 10.
Fig. 8 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, and is a schematic explanatory diagram of a circuit diagram for performing a work of recovering a liquid from the thickener 20.
Fig. 9 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, and is a schematic explanatory diagram of another circuit diagram for performing the cleaning operation of the filter 10.
Fig. 10 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, and is a schematic explanatory diagram of another circuit diagram for performing the filter cleaning operation.
Fig. 11 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, and is a schematic explanatory diagram of another circuit diagram for performing a cleaning operation of the entire circuit.
Fig. 12 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, and is a schematic explanatory view of a circuit in which the adjustment device 50 is provided in the concentrate line 4.
Fig. 13 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, and is a schematic explanatory diagram of another circuit diagram for performing the filtering and concentrating operation.
Fig. 14 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment and is a schematic explanatory diagram of a circuit diagram for performing a leak inspection operation.
Fig. 15 is a schematic explanatory view of the adjusting tool 50, fig. 15 (a) is a sectional view taken along line A-A of fig. 15 (B), fig. 15 (B) is a view taken along line B of fig. 15 (a), and fig. 15 (C) is an example in which 4 tube holding members 52 are provided.
Fig. 16 is a schematic explanatory view of the filter 10.
Fig. 17 is a schematic explanatory view of the concentrator 20.
Fig. 18 (a) is a schematic explanatory diagram of an experimental circuit, fig. 18 (B) is a table of experimental results, and fig. 18 (C) is a graph of experimental results.
Fig. 19 is a circuit diagram of the stock solution treatment apparatus 1 according to another embodiment and is a schematic explanatory diagram of a circuit diagram for performing a filtration and concentration operation.
Fig. 20 is a circuit diagram of the stock solution treatment apparatus 1 according to another embodiment and is a schematic explanatory diagram of a circuit diagram for performing a filter cleaning operation.
Fig. 21 is a circuit diagram of the stock solution treatment apparatus 1 according to the present embodiment, and is a schematic explanatory diagram of another circuit diagram for performing the leak inspection operation.
Detailed Description
The stock solution treatment apparatus according to the present embodiment is an apparatus for obtaining a treatment solution which is administered to a patient by a method such as intravenous infusion or intraperitoneal administration after filtering and concentrating a stock solution such as a pleural and peritoneal effusion.
The stock solution to be treated by the stock solution treatment apparatus according to the present embodiment is not particularly limited, and examples thereof include pleural effusion, plasma, and blood. Pleural effusion refers to pleural or peritoneal effusions that accumulate in the chest or abdomen due to cancerous thoracoperitonitis, cirrhosis, etc. The pleuroperitoneal cavity effusion contains plasma components (proteins, hormones, sugar, lipids, electrolytes, vitamins, bilirubin, amino acids, etc.), hemoglobin, cancer cells, macrophages, histiocytes, leukocytes, erythrocytes, platelets, bacteria, etc. which ooze from blood vessels or internal organs. In the stock solution treatment apparatus of the present invention, solid components such as cancer cells, macrophages, histiocytes, leukocytes, erythrocytes, platelets, bacteria, and the like can be removed from the pleuroperitoneal cavity effusion, and a concentrated solution containing water and useful components contained in the pleuroperitoneal cavity effusion can be produced.
Examples of the plasma include waste plasma of a plasma exchange therapy, and examples of the blood include blood collected during an operation. That is, if the 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 liquid stock treatment apparatus of the present invention, the plasma component separator may be used as a filter in the case of treating waste plasma in the plasma exchange therapy, and the plasma separator may be used as a filter in the case of treating blood collected in the operation.
The filter member used in the filter of the stock solution treatment apparatus of the present invention is not particularly limited. The concentration means for concentrating the filtrate in the concentrator is not particularly limited. As the concentration member, a member equivalent to a filter member for a filter may be used as the concentration member. The filter member or the concentration member (hereinafter, sometimes referred to as a filter member or the like) used for such filtration or concentration is not particularly limited as long as it is a member that allows permeation of plasma, moisture, and the above-mentioned useful components contained in the pleuroperitoneal cavity effusion, but allows permeation of cellular components (i.e., solid components) such as cancer cells, macrophages, histiocytes, leukocytes, erythrocytes, platelets, bacteria, and the like, and also allows permeation of gas. For example, hollow fiber membranes, flat membranes, laminated membranes, and the like can be used as the shape of the filter member or the like. In addition, a member formed of a material that functions to prevent permeation of gas when wetted with a liquid can be used as the filter member or the like. Of course, a member formed of a material that functions to prevent permeation of gas even in a state of being not wetted with liquid may be used as the filter member or the like. In the present specification, the gas that does not permeate the filter member or the like means an inert gas such as nitrogen, air, oxygen or the like, and is generally used for leak inspection or the like.
Examples of the filter member include hollow fiber membranes used in CART, such as a peritoneal fluid filter, a plasma separator for plasma exchange, and a plasma component separator for plasma exchange. That is, hollow fiber membranes used in CART, a peritoneal fluid filter, a plasma separator for plasma exchange, a plasma component separator for plasma exchange, and the like can be used as a filter member of the filter and a concentrating member of the concentrator of the stock solution treatment apparatus of the present invention.
< stock solution treatment apparatus 1 according to the present embodiment >
A stock solution treatment apparatus 1 according to the present embodiment will be described with reference to fig. 1.
In the following, a case where the stock solution to be treated is a pleuroperitoneal cavity effusion will be described as a representative.
In the following description, a case where the filter member provided in the filter 10 is a hollow fiber membrane will be described as a representative. When the filter member is a hollow fiber membrane, either one of the case of allowing the raw liquid supplied to the outside of the hollow fiber membrane to permeate the wall of the hollow fiber membrane and flow into the hollow fiber membrane for filtration (i.e., the case of an external pressure filtration method) and the case of allowing the raw liquid supplied to the inside of the hollow fiber membrane to permeate the wall of the hollow fiber membrane and flow out of the hollow fiber membrane for filtration (i.e., the case of an internal pressure filtration method) can be used. In the following description, a case will be described in which an external pressure filtration method is used for filtration in the filter 10. In the following description, the upstream side of the hollow fiber membrane means the upstream side of the outer surface of the wall of the hollow fiber membrane, and the downstream side of the hollow fiber membrane means the downstream side of the inner surface of the wall of the hollow fiber membrane. The hollow fiber membrane includes a through passage on the downstream side of the inner surface of the wall of the hollow fiber membrane.
In the following description, the case where each of the channels (feed channel, filtrate supply channel, concentrate channel, waste channel, and branch channel) described in the claims is formed of a flexible or soft tube (feed tube 2, filtrate supply tube 3, concentrate tube 4, waste tube 5, and branch tube 6) will be described. However, each flow path may be formed of a tube (for example, a tube made of a hard plastic, a steel tube, or a vinyl chloride tube) having no flexibility or softness, or may be formed of an integrated circuit obtained by resin molding.
Further, in the following description, a case where each flow path is formed by a flexible or soft pipe will be described, and therefore, a description will be made on the premise that a roller pump is used in a liquid feeding portion provided in a filtrate supply flow path. However, the liquid feeding portion may be capable of feeding the liquid in the filtrate supply channel in both the forward and reverse directions, and may be appropriately selected according to the material of the tube constituting the filtrate supply channel and the liquid flowing in the filtrate supply channel. In addition to the roller pump, for example, an infusion pump, a diaphragm pump, or the like can be used as the liquid feeding portion.
< constitution of stock solution treatment apparatus 1 according to the present embodiment >
First, the configuration of the stock solution treatment apparatus 1 according to the present embodiment will be described.
In fig. 1, the reference numeral UB denotes a stock solution bag for containing stock solution, that is, pleuroperitoneal cavity effusion extracted from the chest or abdomen. Further, reference numeral CB denotes a concentrate bag for accommodating a concentrate obtained by filtering and concentrating a raw liquid. Further, reference numeral DB denotes a waste liquid bag for accommodating waste liquid (i.e., moisture) separated from the concentrated liquid. The stock solution bag UB corresponds to the stock solution supply unit described in the claims, and the concentrate bag CB corresponds to the recovery unit described in the claims.
As shown in fig. 1, in a raw liquid treatment apparatus 1 according to the present embodiment, a raw liquid bag UB is connected to a filter 10 via a liquid supply pipe 2. The liquid feed pipe 2 is a pipe for feeding the raw liquid in the raw liquid bag UB to the filter 10, and one end is connected to the raw liquid bag UB and the other end is connected to the raw liquid feed port 11a of the filter 10. As shown in fig. 1, the filter 10 has 2 stock solution supply ports 11a, and when no other tube is connected to the stock solution supply port 11a to which the liquid supply tube 2 is not connected, the stock solution supply port 11a to which no other tube is connected may be closed by a filter connector or the like.
The liquid supply pipe 2 is provided with a flow rate adjustment mechanism 2c such as a clamp or a clip for stopping or opening the flow of the liquid in the liquid supply pipe 2. The liquid supply pipe 2 is provided with a pressure measuring unit 2s for measuring the pressure in the liquid supply pipe 2. The pressure measuring unit 2s may be directly connected to the raw liquid supply port 11a of the filter 10 to which the liquid supply pipe 2 is connected.
The filter 10 filters the stock solution to produce a filtrate. Specifically, the filter 10 is configured to filter the raw liquid supplied from the raw liquid supply port 11a by a hollow fiber membrane as a filter member, and then to discharge the filtrate from the filtrate discharge port 11 c. Specifically, the filter 10 is configured such that the raw liquid supplied from the raw liquid supply port 11a into the filter 10 is filtered when flowing from the outside of the hollow fiber membranes in the filter 10 into the through passages of the hollow fiber membranes through the walls of the hollow fiber membranes. The filter 10 is configured such that the filtered filtrate is discharged to the outside (filtrate supply pipe 3) from the through-flow passage of the hollow fiber membrane through the filtrate discharge port 11 c. The filter 10 is provided with a pressure measuring unit 10s, and the pressure measuring unit 10s measures the pressure in a space (i.e., a through passage of the hollow fiber membrane) isolated from the raw liquid supply port 11a by the hollow fiber membrane in the filter 10. The pressure measuring portion 10s is connected to a port 11b, and the port 11b communicates with a space isolated from the raw liquid supply port 11 a. Therefore, by comparing the measured value of the pressure measuring section 2s with the measured value of the pressure measuring section 10s, the pressure difference between the front and rear of the filter member, that is, the pressure difference between the inside and outside of the hollow fiber membrane (hereinafter referred to as the differential pressure between the filter membranes) can be grasped.
The filter member of the filter 10 is not limited to the hollow fiber membrane described above. The filter member may be a member capable of filtering the raw liquid when passing through the filter member, and capable of hermetically separating a space in the filter 10 communicating with the raw liquid supply port 11a from a space communicating with the filtrate discharge port 11c and the filtrate discharge port 11 b.
The filter 10 is connected to the concentrator 20 via a filtrate supply pipe 3. The filtrate supply pipe 3 is a pipe for supplying the filtrate generated by the filter 10 to the concentrator 20, and has one end connected to the filtrate discharge port 11c and the other end connected to the filtrate supply port 20a of the concentrator 20.
The filtrate supply pipe 3 is provided with a filtrate supply pipe liquid feed portion 3p for feeding the liquid in the filtrate supply pipe 3. The filtrate feed pipe liquid feed portion 3p has a function of feeding the liquid in the filtrate feed pipe 3 in both the forward and reverse directions. Specifically, the filtrate feed pipe liquid feed section 3p has the following functions: by adjusting the operation, the liquid in the filtrate supply pipe 3 can be fed in the direction (forward direction) from the filter 10 toward the concentrator 20, or the liquid in the filtrate supply pipe 3 can be fed in the direction (reverse direction) from the concentrator 20 toward the filter 10.
The filtrate supply pipe 3 is provided with a pressure measuring section 3s for measuring the pressure in the filtrate supply pipe 3. Specifically, the pressure measuring section 3s is provided in the filtrate supply pipe 3 between the filtrate feed section 3p of the filtrate supply pipe and the filtrate feed port 20a of the concentrator 20.
Further, one end of a branch pipe 6 is connected to the filtrate supply pipe 3. Specifically, one end of the branch pipe 6 is connected to a portion between the filtrate discharge port 11c of the filter 10 in the filtrate supply pipe 3 and the filtrate supply pipe liquid feed portion 3p, and the other end is connected to the concentrate bag CB. That is, the liquid in the filtrate supply pipe 3 can be supplied to the concentrate bag CB through the branch pipe 6, or conversely, the liquid (for example, concentrate) in the concentrate bag CB can be supplied to the filtrate supply pipe 3. The branch pipe 6 is provided with a flow rate adjustment mechanism 6c such as a clamp or a clip for stopping or opening the flow of the liquid in the branch pipe 6.
As shown in fig. 1, the filtrate supply pipe 3 may be further provided with a flow rate adjustment mechanism 3c such as a clamp or a clip for stopping or opening the flow of the liquid in the filtrate supply pipe 3. When the operation of the filtrate feed pipe liquid feed portion 3p is stopped, the flow of the liquid in the filtrate feed pipe 3 can be stopped by the filtrate feed pipe liquid feed portion 3 p. However, if the flow rate adjustment mechanism 3c is provided in advance, the following advantages can be obtained: when the other end of the filtrate supply pipe 3 is connected to the filtrate supply port 20a of the concentrator 20, the leakage of the filler in the filter 10 can be prevented. In addition, the following advantages are obtained: when the filtrate supply pipe 3 is discarded after the completion of the operation, leakage of liquid such as filtrate remaining in the filtrate supply pipe 3 can be prevented.
In fig. 1, the flow rate adjustment mechanism 3c is provided in the filtrate supply pipe 3 on the upstream side (filter 10 side) of the connection portion between the filtrate supply pipe liquid feed portion 3p and the branch pipe 6, but the position where the flow rate adjustment mechanism 3c is provided is not particularly limited. The flow rate adjustment mechanism 3c may be provided on the downstream side (the concentrator 20 side) of the filtrate feed pipe liquid feed portion 3p in the filtrate feed pipe 3, or the flow rate adjustment mechanism 3c may be provided between the connection portion of the filtrate feed pipe liquid feed portion 3p and the branch pipe 6. Of course, the flow rate adjustment mechanism 3c may be provided at all or at a plurality of positions among the positions.
The concentrator 20 generates a concentrated solution obtained by concentrating the filtrate. Specifically, the concentrator 20 is configured such that a part of liquid such as moisture (separation liquid, waste liquid, hereinafter referred to as waste liquid) is separated from the filtrate supplied from the filtrate supply port 20a by a moisture separation member (concentration member), the concentrated liquid from which the liquid such as moisture is separated is discharged from the concentrated liquid discharge port 20b, and the waste liquid separated from the filtrate is discharged from the waste liquid discharge port 20 c.
A concentrate bag CB is connected to the concentrator 20 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, and has one end connected to the concentrate outlet 20b of the concentrator 20 and the other end connected to the concentrate bag CB. The concentrate line 4 is provided with a flow rate adjustment mechanism 4c such as a clamp or a clip for stopping or opening the flow of the liquid in the concentrate line 4.
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 the waste liquid separated from the concentrated liquid by the concentrator 20 to the waste liquid bag DB, and has one end connected to the waste liquid discharge port 20c of the concentrator 20 and the other end connected to the waste liquid bag DB. The waste liquid pipe 5 is provided with a flow rate adjusting mechanism 5c such as a clamp or a clip for stopping or opening the flow of the liquid in the waste liquid pipe 5.
In the above-described configuration, in the raw liquid treatment apparatus 1 according to the present embodiment, if the raw liquid is supplied from the raw liquid bag UB to the filter 10 through the liquid supply pipe 2, the raw liquid can be filtered by the filter 10 to generate a filtrate. Further, if the generated filtrate is supplied to the concentrator 20 via the filtrate supply pipe 3, a concentrated solution can be generated by the concentrator 20. The produced concentrated solution can be recovered to the concentrated solution bag CB via the concentrated solution pipe 4, and the waste solution separated from the concentrated solution can be recovered to the waste solution bag DB.
Next, the operation of the stock solution treatment apparatus 1 according to the present embodiment will be described.
< preparation for cleaning operation >
In the preliminary cleaning operation of the stock solution treatment apparatus 1 according to the present embodiment, first, the operation of the filtrate feed pipe liquid feed portion 3p is stopped, and all the pipes 2 to 6 are closed by all the flow rate adjustment mechanisms 2c to 6 c. The pressure measuring portion 10s is detached from the port 11b of the filter 10, and the port 11b of the filter 10 is closed by a filter connector or the like.
Next, the state of the filter 10 and the concentrator 20 is reversed from the state at the time of the filtering and concentrating operation. That is, the following states are set: a state in which the port 11b of the filter 10 is located below and the filtrate discharge port 11c is located above, and a state in which the filtrate supply port 20a of the concentrator 20 is located below and the concentrate discharge port 20b is located above (refer to fig. 2).
In addition, when preparing the cleaning operation, the filter 10 and the concentrator 20 do not need to be reversed from the state at the time of the filtering and concentrating operation.
The postures of the filter 10 and the concentrator 20 during the preparation cleaning operation may be any postures that enable the cleaning liquid to be used for cleaning the filter 10 and the concentrator 20 when the cleaning liquid is flowing. For example, the cleaning operation may be prepared in a state in which the raw liquid supply port 11a and the waste liquid discharge port 20c of the filter 10 and the thickener 20 are directed upward, that is, in a state in which the filter 10 and the thickener 20 are horizontal or inclined.
The cleaning liquid recovery bag FB is connected to the other end of the concentrated liquid pipe 4 instead of the concentrated liquid bag CB, and the cleaning liquid recovery bag FB is connected to the other end of the waste liquid pipe 5 instead of the waste liquid bag DB (see fig. 2). The other end of the concentrate pipe 4 may be disposed in a simple tub or the like. The other end of the waste liquid pipe 5 may be connected to the waste liquid bag DB, or may be disposed in a simple tub or the like.
A cleaning liquid bag SB is connected to the other end of the liquid supply pipe 2 in place of the stock solution bag UB.
Finally, the flow rate adjusting mechanisms 2c to 4c can flow the liquid in the tubes 2 to 4. The flow rate adjustment mechanism 5c maintains the flow rate so that the liquid cannot flow through the waste liquid tube 5.
In the above state, the filtrate feed pipe liquid feed portion 3p is operated so that the liquid flows in the forward direction (see fig. 2). Thus, the cleaning liquid flows through the feed pipe 2, the filter 10, the filtrate supply pipe 3, the concentrator 20, and the concentrate pipe 4 in this order from the cleaning liquid bag SB connected to the feed pipe 2, and the cleaning liquid is recovered to the cleaning liquid recovery bag FB connected to the concentrate pipe 4.
This allows the cleaning liquid to flow through the passages and pipes 2 to 4 through which the concentrated liquid flows in the filter 10 and the concentrator 20, and therefore the passages and pipes 2 to 4 through which the concentrated liquid flows in the filter 10 and the concentrator 20 can be cleaned.
Next, after the concentrate line 4 is closed by the flow rate adjustment mechanism 4c so that the liquid does not flow through the concentrate line 4, the waste line 5 is opened by the flow rate adjustment mechanism 5c so that the liquid flows through the waste line 5. This allows the cleaning liquid to flow through the flow path through which the waste liquid flows in the concentrator 20, and therefore the flow path through which the waste liquid flows in the filter 10 and the concentrator 20, and the pipes 2, 3, and 5 can be cleaned.
As long as the above-described operation is performed, the whole of the stock solution treatment apparatus 1 of the present embodiment (except for the branch pipe 6) can be prepared for cleaning.
In addition, when preparing the cleaning operation, the branch pipe 6 may be detached from the filtrate supply pipe 3 (see fig. 2), or the cleaning operation may be performed while the branch pipe 6 remains connected. Accordingly, if the flow rate adjusting mechanism 6c can be used to flow the liquid into the branch pipe 6 during the preparation of the cleaning operation, the branch pipe 6 can be cleaned by the cleaning liquid. In this case, the cleaning liquid collection bag FB may be connected to the other end of the branch pipe 6 in advance instead of the concentrate bag CB or may be simply disposed in a tub or the like. Even when the branch pipe 6 is detached from the filtrate supply pipe 3 at the time of preparation for the cleaning operation, if the branch pipe 6 is connected to the filtrate supply pipe 3 during the preparation for the cleaning operation, the liquid can flow through the branch pipe 6 by the flow rate adjusting mechanism 6c, and the branch pipe 6 can be cleaned by the cleaning liquid.
As described above, the cleaning liquid may be made to flow only in either the concentrate line 4 or the waste liquid line 5 to perform the preparatory cleaning, but the cleaning liquid may be made to flow in both the concentrate line 4 and the waste liquid line 5 at the same time to perform the preparatory cleaning. In this case, the preparatory cleaning is performed in a state where both the flow rate adjustment mechanism 4c and the flow rate adjustment mechanism 5c are opened (see fig. 2).
In the above example, the explanation was given of the case where the cleaning liquid is made to flow from the filter 10 toward the concentrator 20 to perform the preparation cleaning, but the cleaning liquid may be made to flow from the concentrator 20 toward the filter 10 to perform the preparation cleaning. In this case, a cleaning liquid recovery bag FB (or a simple tub or the like) is connected to the other end of the liquid supply pipe 2 instead of the stock solution bag UB, a cleaning liquid bag SB is connected to the other end of the concentrated liquid pipe 4 instead of the concentrated liquid bag CB, and a cleaning liquid bag SB is connected to the other end of the waste liquid pipe 5 instead of the waste liquid bag DB. In this state, when the filtrate feed pipe liquid feed portion 3p is operated to flow the liquid in the reverse direction, the cleaning liquid can be made to flow from the concentrator 20 toward the filter 10, and the cleaning can be prepared. In the case of performing the preparation cleaning by this method, the cleaning liquid bag SB to which the cleaning liquid is supplied may be set to be the cleaning liquid bag SB to which only the other end of the concentrated liquid pipe 4 is connected or the cleaning liquid bag SB to which only the other end of the waste liquid pipe 5 is connected in the middle of the preparation cleaning operation. Further, the cleaning liquid may be supplied from the cleaning liquid bag SB connected to only the other end of the concentrate pipe 4 and the cleaning liquid bag SB connected to only the other end of the waste liquid pipe 5. The other end of the concentrate tube 4 may be connected to one of the other ends of the waste liquid tube 5, and the other end of the other tube may be connected to the cleaning liquid collection bag FB (or a simple tub or the like).
The postures of the filter 10 and the concentrator 20 may be kept constant during the preparation of the cleaning operation, but the filter 10 and the concentrator 20 may be reversed during the preparation of the cleaning operation. For example, at the start of the preparation cleaning operation, the filter 10 and the concentrator 20 may be held in the same posture as the state in which the filtration concentration operation is performed, and at the middle of the preparation cleaning operation, both or either of the filter 10 and the concentrator 20 may be reversed from the posture at the start of the preparation cleaning operation. In addition, at the start of the preparation cleaning operation, the filter 10 and the concentrator 20 may be held in a posture reversed from the state in which the filtration and concentration operation is performed, and at the middle of the preparation cleaning operation, both or either of the filter 10 and the concentrator 20 may be reversed from the posture at the start of the preparation cleaning operation. Further, at the start of the preparation cleaning operation, either one of the filter 10 and the concentrator 20 may be held in the same posture as the state in which the filtration and concentration operation is performed, and the other may be held in the posture reversed from the state in which the filtration and concentration operation is performed, and at the middle of the preparation cleaning operation, either one or both of the filter 10 and the concentrator 20 may be reversed from the posture at the start of the preparation cleaning operation. Of course, the filter 10 and the concentrator 20 may be reversed as many times as necessary during the preparation of the cleaning operation.
In the case where the filter 10 has 2 stock solution supply ports 11a, the surface of the filter member of the filter 10 (the outer surface of the hollow fiber membrane in the external pressure filtration method), that is, the surface on the side to which the stock solution is supplied and the space on the side to which the stock solution is supplied in the filter 10 may be prepared for cleaning. In this case, a cleaning liquid bag SB is connected to the other end of the liquid supply pipe 2 instead of the stock solution bag UB, one end of the cleaning liquid recovery pipe 7 is connected to the stock solution supply port 11a to which the liquid supply pipe 2 is not connected, and the other end of the cleaning liquid recovery pipe 7 is connected to the cleaning liquid recovery bag FB (or a simple tub or the like). Thus, when the cleaning liquid is supplied from the cleaning liquid bag SB, the cleaning liquid can flow along the surface of the filter member on the side to which the raw liquid is supplied (the outer surface of the hollow fiber membrane in the external pressure filtration method) in the space on the side to which the raw liquid is supplied in the filter 10. Therefore, the surface of the filter member of the filter 10 on the side to which the stock solution is supplied (the outer surface of the hollow fiber membrane in the external pressure filtration method) and the space of the filter 10 on the side to which the stock solution is supplied can be prepared for cleaning. In the cleaning preparation operation, that is, in the case of performing the cleaning preparation on the surface of the filter member of the filter 10, if the cleaning liquid bag SB is disposed at a position higher than the cleaning liquid recovery bag FB (or the simple tub or the like), the cleaning liquid can flow by gravity (fall). However, the method of flowing the cleaning liquid is not limited to the method using gravity, and the cleaning liquid may be flowed by a pump or the like. For example, a pump may be disposed in the liquid supply pipe 2 or the cleaning liquid collection pipe 7 to supply the liquid, or an aspirator may be disposed at the other end of the cleaning liquid collection pipe 7 to aspirate the liquid, so that the surface of the filter member on the side to which the raw liquid is supplied (the outer surface of the hollow fiber membrane in the external pressure filtration method) in the space on the side to which the raw liquid is supplied in the filter 10 may be cleaned.
< filtration operation >
When the preparation cleaning operation is finished, a filtering operation is performed.
When the preparation cleaning operation is completed, the circuit (circuit shown in fig. 3) having the configuration shown in fig. 1 is adjusted.
First, all the tubes 2 to 6 are temporarily closed by all the flow rate adjustment mechanisms 2c to 6c, and the liquid is not allowed to flow through all the tubes 2 to 6.
Next, the filter 10 and the concentrator 20 are reversed from the state of being ready for cleaning, and the filter concentration operation is returned to the state of being performed (the original state is maintained when the filter 10 and the concentrator 20 are not reversed during the ready for cleaning). The pressure measuring portion 10s is connected to the port 11b of the filter 10.
Further, from the state of preparing the cleaning work, a concentrated solution bag CB is connected to the other end of the concentrated solution tube 4 instead of the cleaning solution recovery bag FB, and a waste solution bag DB is connected to the other end of the waste solution tube 5 instead of the cleaning solution recovery bag FB. In addition, the other end of the waste liquid pipe 5 may be disposed in a tub or the like instead of the waste liquid bag DB.
In addition, in order to supply the concentrate discharged from the concentrate discharge port 20b of the concentrator 20 to the concentrate bag CB by gravity alone, it is desirable that the concentrate bag CB is disposed below the concentrate discharge port 20b of the concentrator 20. However, if the concentrate can be supplied to the concentrate bag CB by the liquid feed force of the filtrate feed pipe liquid feed portion 3p or the like, the height of the concentrate bag CB may be set to be the same as the height of the concentrate discharge port 20b of the concentrator 20 or may be set to be higher than the position of the concentrate discharge port 20b of the concentrator 20.
In order to supply the waste liquid discharged from the waste liquid discharge port 20c of the concentrator 20 to the waste liquid bag DB by gravity alone, it is desirable that the waste liquid bag DB is also disposed below the waste liquid discharge port 20c of the concentrator 20. However, if the waste liquid can be supplied to the waste liquid bag DB by the liquid feed force of the filtrate feed pipe liquid feed portion 3p or the like, the height of the waste liquid bag DB may be set to be the same as the height of the waste liquid discharge port 20c of the thickener 20 or may be set to be higher than the position of the waste liquid discharge port 20c of the thickener 20.
The liquid supply pipe 2 is connected to a stock solution bag UB instead of the cleaning solution bag SB, and the other end of the branch pipe 6 is connected to a concentrate bag CB to which the other end of the concentrate pipe 4 is connected. The raw liquid bag UB connected to the liquid supply pipe 2 is provided at a position higher than the raw liquid supply port 11a of the filter 10. That is, the stock solution bag UB is disposed so that the stock solution in the stock solution bag UB is supplied to the stock solution supply port 11a of the filter 10 by only gravity. In order to supply the filtrate supplied from the filtrate supply pipe 3 to the concentrate bag CB through the branch pipe 6 by gravity alone, it is desirable that the concentrate bag CB is disposed below the connection position between the filtrate supply pipe 3 and the branch pipe 6.
The flow rate adjusting mechanisms 3c to 6c are configured to allow the liquid to flow through the tubes 3 to 6. Further, since the filtrate supply pipe liquid feed portion 3p provided in the filtrate supply pipe 3 is maintained in a stopped state, the liquid is maintained in a state in which the liquid does not flow downstream of the connection position of the branch pipe 6 in the filtrate supply pipe 3.
When the state is set as described above, the flow rate adjustment mechanism 2c is opened, and the stock solution is supplied from the stock solution bag UB to the filter 10 through the liquid supply pipe 2, and the supplied stock solution is filtered in the filter 10 to generate a filtrate. The filtrate generated by the filter 10 is supplied to the concentrate bag CB through the filtrate supply pipe 3 and the branch pipe 6. That is, the raw liquid flows through the liquid feed pipe 2, the filter 10, the filtrate feed pipe 3, and the branch pipe 6 in this order by gravity alone, so that a filtrate obtained by filtering the raw liquid is produced, and the filtrate is recovered to the concentrate bag CB.
In a state in which the raw liquid is flowed by gravity and filtered (hereinafter, sometimes referred to as gravity filtration) as described above, when the raw liquid having a low viscosity is filtered, the filtration process of the raw liquid can be accelerated. That is, the flow rate of the raw liquid through each pipe and the filter 10 can be increased (i.e., the flow rate can be increased) compared with the case where the raw liquid is fed to the filter 10 through the filtrate feed pipe feeding portion 3p, and therefore the filtering process of the raw liquid in the filter 10 can be accelerated.
< filtration concentration operation >
In general, the volume of the stock solution bag UB, in other words, the amount of stock solution contained in the stock solution bag UB is larger than the volume of the concentrate bag CB. For example, in the case of a general pleuroperitoneal cavity fluid caused by cancer or liver cirrhosis, the stock solution bag UB contains about 3L, but the volume of the concentrate bag CB is generally about 1L. Therefore, when the above-described filtration operation is performed, the total amount of the filtrate supplied from the filter 10 to the concentrate bag CB through the branch pipe 6 exceeds the capacity of the concentrate bag CB during the operation. This makes it impossible to supply filtrate to the concentrate bag CB, and the filtration operation is stopped.
In the raw liquid treatment apparatus 1 of the present embodiment, when a predetermined time has elapsed since the start of the filtration operation, the control unit 30 operates the filtrate supply pipe liquid feed portion 3p so that the liquid flows in the positive direction in the filtrate supply pipe 3. Thus, a part (or the whole) of the filtrate is supplied to the concentrator 20 through the filtrate supply pipe 3, and the filtrate is concentrated in the concentrator 20. That is, the concentration operation of the filtrate in the concentrator 20 can be performed simultaneously with the filtration operation of the filter 10 (see fig. 4). The timing to start the operation of the filtrate feed tube liquid feed portion 3p may be instructed by an operator. For example, an operation instruction of the filtrate supply pipe liquid feeding portion 3p may be input by an operator, and the filtrate supply pipe liquid feeding portion 3p may be operated so that the liquid flows in the positive direction in the filtrate supply pipe 3.
< case where the filtrate supply tube liquid feed section 3p is operated before exceeding the capacity of the concentrate bag CB >
Here, when the control unit 30 (or an operator) operates the filtrate feed pipe liquid feed unit 3p at a timing before the total amount of filtrate fed from the filter 10 to the concentrate bag CB via the branch pipe 6 exceeds the capacity of the concentrate bag CB, the filtrate feed is performed in accordance with the operation state of the filtrate feed pipe liquid feed unit 3p, that is, the liquid feed amount of the filtrate feed pipe liquid feed unit 3p, as follows.
A) When the liquid feed amount of the filtrate feed section 3p is larger than the flow rate of the filtrate (see fig. 1)
First, when the liquid feed amount of the filtrate feed portion 3p of the filtrate feed pipe is larger than the flow rate of the filtrate fed from the filter 10 to the filtrate feed pipe 3, the filtrate in the concentrate bag CB is sucked out. That is, the filtrate sucked out from the concentrate bag CB is supplied to the concentrator 20 together with the filtrate supplied from the filter 10. Thus, the liquid (filtrate and concentrate) is stored in the concentrate bag CB in an amount of a difference between the filtrate sucked out from the concentrate bag CB and the concentrate supplied from the concentrator 20. As a result, both the filtrate and the concentrated solution are contained in the liquid sucked out from the concentrated solution bag CB, and the filtrate and the concentrated solution are supplied to the concentrator 20, so that the concentration of the filtrate and the re-concentration of the concentrated solution are simultaneously performed in the concentrator 20. That is, the filtrate can be concentrated and the concentrated solution can be re-concentrated while circulating the concentrated solution. Further, since the raw liquid can be filtered and concentrated while being supplied to the filter 10 by gravity, the speed of the filtering operation can be increased and the concentration of the filtrate (and the re-concentration of the concentrated liquid) can be performed. Therefore, the filtering and concentrating operation can be effectively performed.
The concentrate bag CB is filled in a short time, but when the concentrate bag CB is filled in, the resistance of supplying the liquid to the concentrator 20 increases. Thereby, the pressure in the filtrate supply pipe 3 (hereinafter referred to as the differential pressure between the concentrator membranes) detected by the pressure measuring section 3s increases. Since the inter-membrane differential pressure is transmitted to the control unit 30, if the inter-membrane differential pressure becomes a predetermined pressure, for example, the maximum inter-membrane differential pressure allowable by the concentrator 20 (hereinafter referred to as allowable inter-membrane differential pressure), the control unit 30 controls the operation of the filtrate supply pipe liquid feed unit 3p so that the liquid feed amount becomes a liquid feed amount that maintains the inter-membrane differential pressure equal to the allowable inter-membrane differential pressure or a pressure lower than the inter-membrane differential pressure of Xu Nongsu.
Even when the operation of the filtrate feed pipe feed section 3p is controlled so that the feed liquid amount becomes a feed liquid amount that maintains the pressure equivalent to the allowable inter-concentrator-membrane differential pressure or is lower than the allowable inter-membrane differential pressure of Xu Nongsu, the filtration concentration and the re-concentration can be performed simultaneously when the feed liquid amount of the filtrate feed pipe feed section 3p is larger than the flow rate of the filtrate fed from the filter 10.
B) When the liquid feed amount of the filtrate feed section 3p is smaller than the flow rate of the filtrate (see fig. 4)
On the other hand, when the liquid feed amount of the filtrate feed portion 3p of the filtrate feed pipe is smaller than the flow rate of the filtrate fed from the filter 10 to the filtrate feed pipe 3, a part of the filtrate fed from the filter 10 to the filtrate feed pipe 3 is fed to the filtrate feed portion 3p, and a part is fed to the concentrate bag CB through the branch pipe 6. That is, since the raw liquid can be filtered and concentrated while being supplied to the filter 10 by gravity, the speed of the filtering operation can be increased and the concentration operation of the filtrate can be performed in a state where the viscosity of the raw liquid is low. Therefore, the filtering and concentrating operation can be effectively performed. In this case, the liquid (filtrate and concentrate) is stored in the concentrate bag CB in an amount added to the amount of the filtrate supplied from the filter 10 through the branch pipe 6 and the amount of the concentrate supplied from the concentrator 20.
The concentrate bag CB is filled in a short time, but if the concentrate bag CB is filled in, the filtrate does not flow from the filter 10 to the concentrate bag CB. As a result, the filtrate in the amount of the liquid (water) discharged as the waste liquid in the concentrator 20 is supplied from the filter 10 to the filtrate supply pipe liquid feed portion 3 p. In this case, the filtration amount and the concentration amount are limited by the flow rate of the filtrate feed pipe liquid feed portion 3p, but the operation of the filtrate feed pipe liquid feed portion 3p is controlled by the control portion 30 so that the liquid feed amount becomes the maximum flow rate in the range in which the liquid feed amount can be achieved. That is, the operation of the filtrate feed pipe liquid feed section 3p is controlled by the control section 30 so that the liquid feed amount is set to a maximum flow rate at which the differential pressure between the concentrator membranes is maintained equal to the allowable differential pressure between the concentrator membranes or the differential pressure between the concentrator membranes is low and the total amount of the filtrate and the concentrate stored in the concentrate bag CB does not exceed the total amount of the concentrate bag CB.
In this state, the filtration operation of the stock solution and the concentration operation of the filtrate can be performed simultaneously, but the filtration concentration and the re-concentration of the concentrated solution cannot be performed simultaneously. In addition, the concentration of the filtrate in the concentrate bag CB cannot be performed. Therefore, in the case of performing concentration of the filtrate in the concentrate bag CB and re-concentration of the concentrate, the operation of the filtrate feed pipe feed section 3p may be switched so that the feed rate of the filtrate feed pipe feed section 3p is larger than the flow rate of the filtrate fed from the filter 10 to the filtrate feed pipe 3, or the re-concentration operation to be described later may be performed after the treatment of the stock solution in the stock solution bag UB is completed.
< case where the filtrate supply tube liquid feed portion 3p is operated after exceeding the capacity of the concentrate bag CB >
The total amount of filtrate supplied from the filter 10 to the concentrate bag CB through the branch pipe 6 exceeds the capacity of the concentrate bag CB at the timing when the filtrate supply pipe liquid feed section 3p is operated by the control section 30 (or an operator). In other words, when the control unit 30 (or the operator) operates the filtrate supply pipe liquid feeding portion 3p after exceeding the capacity of the concentrate bag CB, the control unit 30 (or the operator) controls the operation of the filtrate supply pipe liquid feeding portion 3p so as to achieve the following liquid feeding amount. That is, the operation of the filtrate feed pipe liquid feed section 3p is controlled by the control section 30 (or an operator) so that the liquid feed amount is a liquid feed amount which maintains the differential pressure between the concentrator membranes at a pressure equivalent to the allowable differential pressure between the concentrator membranes or a pressure lower than the differential pressure between the concentrator membranes of Xu Nongsu, and in which the total amount of the filtrate and the concentrate stored in the concentrate bag CB does not exceed the maximum flow amount of the total amount of the concentrate bag CB.
In this case, the filtration of the stock solution and the concentration of the filtrate can be performed simultaneously, but the concentration of the filtrate in the concentrate bag CB and the re-concentration of the concentrate cannot be performed simultaneously. Therefore, in the case of performing concentration of the filtrate in the concentrate bag CB and re-concentration of the concentrate, the operation of the filtrate feed pipe feed section 3p may be switched so that the feed rate of the filtrate feed pipe feed section 3p is larger than the flow rate of the filtrate fed from the filter 10 to the filtrate feed pipe 3, or the re-concentration operation to be described later may be performed after the treatment of the stock solution in the stock solution bag UB is completed.
The above-described state of "a certain time has elapsed since the start of the filtration operation" and the state of "exceeding the capacity of the concentrate bag CB" correspond to the "predetermined state" as defined in claim 1 and claim 8.
< end of filtration concentration operation >
When the filtration concentration is performed, the differential pressure between the filter membranes becomes equal to or less than a predetermined value, and the control unit 30 determines that the filtrate in the raw liquid bag UB is completely consumed, and stops the operation of the filtrate supply pipe liquid feed unit 3p, thereby ending the filtration concentration operation.
The filtering and concentrating operation may be automatically ended by the control unit 30, but the filtering and concentrating operation may be ended by an operator. In this case, it is desirable to set the following functions in advance at the apparatus: and a function (alarm function) for notifying the operator of the end of the operation when the differential pressure between the filter membranes is equal to or less than a predetermined value. For example, a function of notifying the operator of the end of the job by a buzzer or the like is set in advance. Thus, the operator who has grasped the completion of the operation by the buzzer or the like can stop the operation of the filtrate feed pipe liquid feed portion 3p, and complete the filtration and concentration operation.
The method by which the control unit 30 determines that the entire filtrate in the stock solution bag UB is consumed is not limited to the differential pressure between the filter membranes. For example, the weight of the stock solution bag UB may be measured in advance, and if the weight is equal to or less than a predetermined value, it may be determined that the stock solution in the stock solution bag UB is completely consumed. Further, a liquid-gas detection sensor for detecting the gas and liquid in the stock solution bag UB, a liquid level detection sensor for detecting the liquid level in the stock solution bag UB, or the like may be attached to the stock solution bag UB to determine that the stock solution in the stock solution bag UB is completely consumed. In the case where such a sensor is provided, if the alarm function of the apparatus is set to be operated in advance when the sensor or the like detects a predetermined state, the operator can end the filtering and concentrating operation.
< other examples of filtration concentration work >
In the above example, the case where the filtrate supply pipe liquid feed portion 3p is operated in the middle of the filtration operation has been described, but the filtrate supply pipe liquid feed portion 3p may be operated simultaneously with the start of the filtration operation (see fig. 1). That is, the filtrate supply pipe liquid feed portion 3p may be operated so that the liquid flows in the positive direction in the filtrate supply pipe 3 at the same time as the filtration operation is started.
A) When the liquid feed amount of the filtrate feed section 3p is larger than the flow rate of the filtrate
First, when the liquid feed amount of the filtrate feed portion 3p is larger than the flow rate of the filtrate fed from the filter 10, the whole filtrate fed from the filter 10 is fed to the concentrator 20. In this state, the filtrate is not stored in the concentrate bag CB, but the concentrate is stored in the concentrate bag CB. When the concentrate bag CB is filled, the resistance to supply of the liquid to the concentrator 20 increases, but when this state is established, the filtrate supply tube liquid feed portion 3p sucks the concentrate from the concentrate bag CB. That is, since both the filtrate and the concentrated solution supplied from the filter 10 to the filtrate supply pipe 3 are supplied to the concentrator 20, the concentration of the filtrate supplied from the filter 10 to the filtrate supply pipe 3 and the re-concentration of the concentrated solution are simultaneously performed in the concentrator 20 (see fig. 1). That is, the filtrate supplied from the filter 10 to the filtrate supply pipe 3 can be concentrated and the concentrated solution can be re-concentrated while circulating the concentrated solution. Further, since the raw liquid can be filtered and concentrated while being supplied to the filter 10 by gravity, the speed of the filtering operation can be increased and the filtering and concentration can be performed in a state where the viscosity of the raw liquid is low. Therefore, the filtering and concentrating operation can be effectively performed.
The inter-membrane differential pressure between the concentrators is increased in the near future, but since the inter-membrane differential pressure between the concentrators is sent to the control unit 30, the operation of the filtrate feed pipe liquid feed unit 3p is controlled so that the liquid feed amount becomes a liquid feed amount that maintains the inter-membrane differential pressure between the concentrators at a pressure equal to or lower than the allowable inter-membrane differential pressure between the concentrators by Xu Nongsu.
Even when the operation of the filtrate feed pipe feed section 3p is controlled so that the feed liquid amount becomes a feed liquid amount that maintains the pressure equivalent to the allowable inter-concentrator-membrane differential pressure or lower than the allowable inter-concentrator-membrane differential pressure Xu Nongsu, the filtration concentration and the re-concentration can be performed simultaneously when the feed liquid amount of the filtrate feed pipe feed section 3p is larger than the flow rate of the filtrate fed from the filter 10 to the filtrate feed pipe 3.
B) When the liquid feed amount of the filtrate feed section 3p is smaller than the flow rate of the filtrate (see fig. 4)
On the other hand, when the liquid feed amount of the filtrate feed pipe liquid feed portion 3p is smaller than the flow rate of the filtrate fed from the filter 10, a part of the filtrate fed from the filter 10 is fed to the filtrate feed pipe liquid feed portion 3p and a part is fed to the concentrate bag CB. In this case, since the raw liquid can be filtered and concentrated while being supplied to the filter 10 by gravity, the speed of the filtering operation can be increased and the filtering and concentration can be performed in a state where the viscosity of the raw liquid is low. Therefore, the filtering and concentrating operation can be effectively performed. In this case, the liquid (filtrate and concentrate) is stored in the concentrate bag CB in an amount added to the amount of the filtrate supplied from the filter 10 through the branch pipe 6 and the amount of the concentrate supplied from the concentrator 20.
The concentrate bag CB is filled in a short time, but if the concentrate bag CB is filled in, the filtrate does not flow from the filter 10 to the concentrate bag CB. Then, the filtrate in the amount of the liquid (water) discharged as the waste liquid in the concentrator 20 is supplied from the filter 10 to the filtrate supply pipe liquid feed portion 3 p. In this case, the filtration amount and the concentration amount are limited by the flow rate of the filtrate feed pipe liquid feed portion 3p, but the operation of the filtrate feed pipe liquid feed portion 3p is controlled by the control portion 30 so that the liquid feed amount becomes the maximum flow rate in the range in which the liquid feed amount can be achieved. That is, the operation of the filtrate feed pipe liquid feed section 3p is controlled by the control section 30 so that the liquid feed amount is set to a maximum flow rate at which the differential pressure between the concentrator membranes is maintained equal to the allowable differential pressure between the concentrator membranes or the differential pressure between the concentrator membranes is low and the total amount of the filtrate and the concentrate stored in the concentrate bag CB does not exceed the total amount of the concentrate bag CB.
In this state, the filtration operation of the stock solution and the concentration operation of the filtrate can be performed simultaneously, but the filtration concentration and the re-concentration of the concentrated solution cannot be performed simultaneously. In addition, the concentration of the filtrate in the concentrate bag CB cannot be performed. Therefore, in the case of performing concentration of the filtrate in the concentrate bag CB and re-concentration of the concentrate, the operation of the filtrate feed pipe feed section 3p may be switched so that the feed rate of the filtrate feed pipe feed section 3p is larger than the flow rate of the filtrate fed from the filter 10 to the filtrate feed pipe 3, or the re-concentration operation to be described later may be performed after the treatment of the stock solution in the stock solution bag UB is completed.
< still another example of filtration concentration work >
Of course, the filtering and concentrating may be performed while the flow rate adjusting mechanism 6c of the branch pipe 6 is closed (see fig. 13), and the filtering and concentrating may be performed while the flow rate adjusting mechanism 6c of the branch pipe 6 is opened from the middle (see fig. 1). That is, in the initial stage of the filtering and concentrating operation, the filtrate feed pipe liquid feed section 3p is operated to supply all the filtrate fed from the filter 10 to the filtrate feed pipe 3 to the concentrator 20. When the amount of the concentrated liquid in the concentrated liquid bag CB exceeds a predetermined amount, the flow rate adjusting mechanism 6c of the branch pipe 6 is opened, and the filtrate supply pipe liquid feeding portion 3p is operated to supply the whole of the filtrate supplied from the filter 10 to the filtrate supply pipe 3 and a part of the liquid in the concentrated liquid bag CB to the concentrator 20. Thus, the concentration operation can be continuously performed, and the concentrated solution in the concentrated solution bag CB can be re-concentrated by the concentrator 20. For example, when the viscosity of the raw liquid supplied from the raw liquid bag UB to the filter 10 is high or when the flow of the raw liquid supplied from the raw liquid bag UB to the filter 10 is not smooth as in the later stage of the filtration operation (the state in which the raw liquid in the raw liquid bag UB is reduced), the filtration concentration is performed simultaneously, and the filtration concentration and the re-concentration are performed simultaneously from the middle, whereby the treatment efficiency can be further improved.
< operating conditions concerning the filtrate feed section 3p of the filtrate feed tube >
In the filtration and concentration operation and the re-concentration operation, the condition of operating the filtrate feed tube liquid feed portion 3p, that is, the liquid feed amount in the filtrate feed tube 3 is obtained in advance by performing preliminary experiments, numerical simulations, and the like under various conditions (viscosity of the raw liquid, the amount of the raw liquid, the distance between the raw liquid bag UB and the raw liquid feed port 11a of the filter 10 in the height direction, and the like). That is, the amount of liquid feed in the filtrate feed pipe 3 in which the filtration and concentration operation and the re-concentration operation can be appropriately performed is obtained in advance by preliminary experiments, numerical simulations, or the like under various conditions. Further, if the state in which the filtrate supply pipe liquid feed portion 3p is operated is determined by the control portion 30 (or the operator) based on data of preliminary experiments, numerical simulations, or the like, even if various conditions change with the progress of the filtration and concentration operation and the re-concentration operation, the liquid feed of the filtrate supply pipe liquid feed portion 3p can be performed so that the filtration and concentration operation and the re-concentration operation can be appropriately performed.
< about Filter cleaning >
By performing filtration concentration, clogging of the hollow fiber membrane of the filter 10 is likely to occur. In order to eliminate such clogging or prevent clogging, the hollow fiber membrane of the filter 10 may be cleaned during the filtration and concentration operation and the re-concentration operation of the stock solution treatment apparatus 1 of the present embodiment. Specifically, filter cleaning was performed as follows.
First, the operation of the filtrate feed pipe liquid feed section 3p is stopped, and the flow of filtrate in the filtrate feed pipe 3 is stopped.
Next, as shown in fig. 5, a cleaning liquid bag SB is connected to the filtrate supply pipe 3 downstream of the filtrate supply pipe liquid feed portion 3p, that is, between the filtrate supply pipe liquid feed portion 3p and the concentrator 20. In this case, the method of connecting the cleaning solution bag SB to the filtrate supply pipe 3 is not particularly limited. For example, the pressure measuring portion 3s may be removed, the cleaning liquid bag SB may be connected to a portion (plug or the like) to which the pressure measuring portion 3s is connected, or a dedicated plug or the like to which the cleaning liquid bag SB is connected may be provided to the filtrate supply pipe 3.
Further, a cleaning liquid recovery bag FB is connected to one end of the liquid supply pipe 2 instead of the stock solution bag UB. The concentrated liquid pipe 4 and the waste liquid pipe 5 are closed by the flow rate adjusting means 4c and the flow rate adjusting means 5c so that the cleaning liquid does not flow from the filtrate supply pipe 3 to the concentrator 20. Further, a clip, a clamp, or the like may be provided on the downstream side (the concentrator 20 side) of the portion to which the cleaning liquid bag SB is connected, and the filtrate supply pipe 3 may be closed so that the cleaning liquid does not flow from the cleaning liquid bag SB to the concentrator 20.
After the above state is established, the filtrate feed pipe liquid feed section 3p is operated to flow the liquid in the reverse direction. This allows the cleaning liquid to flow in the flow path of the filter 10 through which the raw liquid flows in a direction opposite to the direction in which the raw liquid flows during the filtering and concentrating operation, and thus the inside of the flow path of the filter 10 through which the raw liquid flows can be cleaned (see fig. 5).
< case where the filter 10 has a plurality of stock solution supply ports 11a >
In the case where the filter 10 has a plurality of stock solution supply ports 11a, one of the stock solution supply ports 11a may be connected to the other end of the liquid supply pipe 2 as described above, and one end of the cleaning liquid recovery pipe 7 may be connected to the other stock solution supply port 11a (see fig. 9). In this case, a flow rate adjusting mechanism 7c such as a clamp or a clip for stopping or opening the flow of the liquid in the cleaning liquid recovery tube 7 is provided in advance in the cleaning liquid recovery tube 7. Accordingly, the cleaning liquid can be discharged from the filter 10 through the cleaning liquid recovery pipe 7 during the filter cleaning operation, and therefore, the cleaning liquid can be caused to flow in a direction opposite to the direction in which the stock solution flows during the filtering and concentrating operation, without switching the connection of the liquid supply pipe 2. That is, the liquid supply pipe 2 is closed by the flow rate adjusting mechanism 2c, and the other end of the cleaning liquid recovery pipe 7 is connected to the cleaning liquid recovery bag FB or disposed in a simple tub or the like. In this state, if the liquid can flow in the cleaning liquid recovery pipe 7 by the flow rate adjustment mechanism 7c, the cleaning liquid can flow in the direction opposite to the direction in which the raw liquid flows during the filtration and concentration operation without switching the connection of the liquid supply pipe 2. Of course, even when the cleaning liquid recovery tube 7 is provided, the other end of the liquid supply tube 2 may be connected to the cleaning liquid recovery bag FB or may be disposed in a simple tub or the like (see fig. 10). That is, both the other end of the liquid supply pipe 2 and the other end of the cleaning liquid recovery pipe 7 may be connected to the cleaning liquid recovery bag FB or may be disposed in a simple tub or the like.
As described above, in the case where the cleaning liquid recovery tube 7 is provided, the other end of the cleaning liquid recovery tube 7 may be always connected to the cleaning liquid recovery bag FB, or the other end may be connected to the stock solution bag UB in advance during the filtration and concentration operation, or the other end may be connected to the cleaning liquid recovery bag FB during the filter cleaning operation, or may be disposed in a simple barrel or the like. If the other end of the purge liquid recovery pipe 7 is connected to the stock solution bag UB during the filtration and concentration operation, there is an advantage that the protein remaining in the filter 10 can be recovered.
In addition, in the case of cleaning not only the filter 10 but also the concentrator 20, as shown in fig. 11, a cleaning liquid bag SB is connected to both the other end of the concentrate pipe 4 and the other end of the waste liquid pipe 5 (or only the other end of the waste liquid pipe 5) instead of the concentrate bag CB and the waste liquid bag DB. Both (or one of) the other end of the liquid supply pipe 2 and the other end of the cleaning liquid recovery pipe 7 are connected to the cleaning liquid recovery bag FB, or are disposed in a simple tub or the like. In this state, when the filtrate feed pipe liquid feed portion 3p is operated to flow the liquid in the reverse direction, not only the filter 10 but also the concentrator 20 can be cleaned.
< re-concentration operation >
In the case of further concentrating the concentrated solution obtained by the filtration and concentration operation, it is desirable to perform the re-concentration operation after the filtration and concentration operation is completed.
As shown in fig. 6, in the stock solution treatment apparatus 1 of the present embodiment, since the concentrate bag CB is connected to the other end of the branch pipe 6, if the filtrate supply pipe 3 is closed by the flow rate adjustment mechanism 3c (provided on the upstream side (filter 10 side) of the position where the branch pipe 6 and the filtrate supply pipe 3 are connected), and the liquid does not flow into the filtrate supply pipe 3 toward the filter 10, the re-concentration operation can be performed. That is, when the filtrate supply pipe liquid feed portion 3p is operated to flow the liquid in the positive direction in the above-described state, the concentrated liquid in the concentrated liquid bag CB can be circulated in the order of the branch pipe 6, the filtrate supply pipe 3, the concentrator 20, and the concentrated liquid pipe 4. Thus, the circulating concentrated solution is separated from the waste liquid in the concentrator 20, and thus a concentrated solution (re-concentrated solution) with an increased concentration ratio can be obtained.
In the above example, the case where the branch pipe 6 is always connected to the filtrate supply pipe 3 has been described, but the branch pipe 6 may be detachable from the filtrate supply pipe 3. In this case, the branch pipe 6 can be detached from the filtrate supply pipe 3 in advance without performing the re-concentration, and can be connected to the filtrate supply pipe 3 in the case of performing the re-concentration in the filtration concentration operation, in the case of performing the re-concentration operation, or the like. The method for attaching and detaching the branch pipe 6 to and from the filtrate supply pipe 3 is not particularly limited. For example, if a dedicated plug or the like for connecting the branch pipe 6 is provided in the filtrate supply pipe 3, the branch pipe 6 can be easily attached to or detached from the filtrate supply pipe 3.
Even when the branch pipe 6 is not provided, the concentration operation can be performed by simply removing one end of the filtrate supply pipe 3 from the filtrate discharge port 11c of the filter 10 and connecting it to the concentrate bag CB.
< transfer to Reconcentration operation >
In the case of continuously performing the re-concentration operation after the filtration and concentration, the operation of the filtrate feed pipe liquid feed portion 3p may be continued until the concentrated liquid in the concentrated liquid bag CB reaches a predetermined amount, that is, until the concentrated liquid in the concentrated liquid bag CB reaches a predetermined concentrated state. In this case, the method for determining that the concentrated solution in the concentrated solution bag CB has a predetermined concentrated state is not particularly limited. For example, if the concentration of the concentrated liquid in the concentrated liquid bag CB is advanced, the concentration of the concentrated liquid becomes concentrated (i.e., the water content becomes smaller), so that it is difficult to perform the concentration (in other words, the water removal) in the concentrator 20. Thus, even if the filtrate feed pipe liquid feed portion 3p is operated at the same flow rate, the resistance to feeding the concentrated liquid to the concentrator 20 increases, and the differential pressure between the concentrator membranes increases. When the amount of the concentrate in the concentrate bag CB is equal to or less than a predetermined amount, the differential pressure between the concentrator membranes becomes higher than a predetermined pressure even if the flow rate of the filtrate feed pipe liquid feed portion 3p is adjusted (that is, even if the flow rate is set to the minimum flow rate assumed in the re-concentration). That is, when the concentrated solution is in a predetermined concentrated state, the inter-membrane differential pressure between the concentrators becomes higher than the inter-membrane differential pressure of Xu Nongsu even if the flow rate of the filtrate feed pipe liquid feed portion 3p is adjusted. Therefore, when the pressure difference between the membranes of the flow rate concentrator is higher than the pressure difference between the membranes of Xu Nongsu even if the flow rate of the filtrate feed pipe liquid feed part 3p is adjusted, the control part 30 may determine that the concentrated liquid is in a predetermined concentrated state, and stop the operation of the filtrate feed pipe liquid feed part 3 p. In this case, when the inter-membrane differential pressure becomes equal to or greater than the allowable inter-membrane differential pressure, the function of notifying the operator of the completion of the operation by a buzzer or the like may be provided in advance, and the operator may stop the operation of the filtrate supply pipe liquid feed portion 3p to terminate the re-concentration operation.
In the case of continuously performing the re-concentration operation after the filtration concentration, it is also desirable to close in advance the gap between the stock solution bag UB and the filtrate supply pipe liquid feed portion 3 p. In this case, if an automatic valve is provided as the flow rate adjustment mechanism 3c in advance, the gap between the raw liquid bag UB and the filtrate feed pipe liquid feed portion 3p can be automatically closed by the flow rate adjustment mechanism 3c when the state is in a predetermined state. For example, when the filtrate in the stock solution bag UB is completely consumed and the operation is transferred to the re-concentration operation, the control unit 30 may operate the flow rate adjustment mechanism 3c, and the space between the stock solution bag UB and the filtrate supply pipe liquid feeding unit 3p may be closed by the flow rate adjustment mechanism 3 c. Of course, when the control unit 30 detects the transition to the re-concentration operation, a function of notifying the operator of the end of the operation by a buzzer or the like may be provided in advance, and the operator may operate the flow rate adjustment mechanism 3c to close the gap between the stock solution bag UB and the filtrate supply pipe liquid feeding portion 3 p.
The method of determining the timing of the transition to the re-concentration operation is not particularly limited. For example, the determination may be made based on whether or not the amount of the liquid in the concentrate bag CB exceeds a predetermined amount. Whether or not the amount of liquid in the concentrate bag CB exceeds a predetermined amount may be determined based on the weight of the concentrate bag CB, that is, the weight of the liquid stored in the concentrate bag CB. That is, the timing of switching from the filtration and concentration operation to the re-concentration operation may be determined based on the weight of the concentrate bag CB.
The method for determining whether or not the re-concentration operation is completed is not particularly limited. For example, the determination may be made based on the weight of the liquid stored in the concentrate bag CB. For example, the weight of the concentrate bag CB may be measured, and if the weight is smaller than a predetermined weight, it may be determined that the re-concentration operation is completed. Further, the amount of the concentrated liquid in the concentrated liquid bag CB may be measured by attaching a liquid-gas detection sensor for detecting the gas and the liquid in the concentrated liquid bag CB, a liquid level detection sensor for detecting the liquid level in the concentrated liquid bag CB, or the like to the concentrated liquid bag CB, and when the amount of the concentrated liquid becomes smaller than a predetermined amount, it may be determined that the re-concentration operation is completed.
< example of method for recovering liquid in Filter 10 >
Before the re-concentration operation described above is performed, the filtrate in the filter 10 is desirably sent to the concentrator 20 to be recovered as a concentrated solution.
In this case, as shown in fig. 7, the liquid feed pipe 2 is closed by the flow rate adjusting mechanism 2c of the liquid feed pipe 2, and in this state, the pressure measuring section 2s is removed from the liquid feed pipe 2 (or the raw liquid supply port 11 a), the liquid feed pipe 2 is connected to the outside, and the filtrate feed pipe liquid feeding section 3p is operated to flow the liquid in the forward direction. This allows the stock solution on the upstream side of the hollow fiber membrane to be filtered by the hollow fiber membrane and to flow to the downstream side of the hollow fiber membrane.
When the stock solution is exhausted on the upstream side of the hollow fiber membrane, the operation of the filtrate feed pipe liquid feed section 3p is stopped (or the filtrate feed pipe liquid feed section 3p is kept in operation), and the pressure measuring section 10s is removed from the port 11b of the filter 10. Thereby, the space on the downstream side of the hollow fiber membranes (i.e., the space communicating with the filtrate discharge port 11c, the through flow path of the hollow fiber membranes) communicates with the outside. In this state, when the filtrate feed pipe liquid feed portion 3p is operated to flow the liquid in the forward direction, the raw liquid existing downstream of the hollow fiber membranes in the filter 10 can be caused to flow to the filtrate feed pipe 3.
Further, it is possible to determine whether or not the stock solution is consumed on the upstream side of the hollow fiber membrane by checking the pressure of the pressure measuring section 10s. For example, when the stock solution exists on the upstream side of the hollow fiber membrane, the pressure of the pressure measuring unit 10s is maintained substantially constant, but when the stock solution on the upstream side of the hollow fiber membrane is exhausted, the pressure of the pressure measuring unit 10s is lowered. Therefore, when the pressure of the pressure measuring section 10s becomes equal to or lower than a predetermined value, it can be determined that the stock solution on the upstream side of the hollow fiber membrane is consumed.
As a method for determining whether or not the stock solution on the upstream side of the hollow fiber membrane of the filter 10 is consumed, the state in the filter 10 may be visually confirmed as long as the inside of the filter 10 can be visually confirmed. Further, a capacitance type sensor or the like may be attached to the filter 10 to detect the liquid level on the upstream side of the hollow fiber membrane of the filter 10.
Further, for example, it is also possible to determine whether or not the liquid on the downstream side of the hollow fiber membrane of the filter 10 is consumed by installing a liquid-gas detection sensor that detects the gas and the liquid in the filtrate supply pipe 3. In this case, if the liquid-gas detection sensor is mounted on the upstream side (filter 10 side) of the position where the branch pipe 6 is connected to the filtrate supply pipe 3 in advance, air can be prevented from being taken into the filtrate supply pipe 3 at the time of reconcentration.
After the pressure measuring section 2s and the pressure measuring section 10s are removed, the air filter may be attached to a portion where the pressure measuring section 2s and the pressure measuring section 10s are attached, instead of being directly opened to the atmosphere. This allows clean air to be taken into the liquid supply pipe 2.
Further, after the pressure measuring section 2s and the pressure measuring section 10s are removed, the external air may be sucked only by the operation of the filtrate supply pipe liquid feeding section 3p, but the cleaning liquid may be supplied to the liquid supply pipe 2 and the port 11 b.
In the case of recovering the liquid in the filter 10, as shown in fig. 7, when the waste liquid pipe 5 is closed by the flow rate adjusting means 5c of the waste liquid pipe 5, the filtrate recovered from the filter 10 is recovered to the concentrate bag CB without being concentrated. However, the liquid in the filter 10 may be collected in the concentrate bag CB while concentrating the filtrate. That is, when the liquid in the filter 10 is recovered, the liquid in the filter 10 can be recovered and the filtrate can be concentrated while the liquid can be flowed through the waste liquid pipe 5 by the flow rate adjusting mechanism 5 c.
In the above example, the case where the liquid in the filter 10 is recovered before the re-concentration operation is performed has been described, but the liquid in the filter 10 may be recovered after the re-concentration operation is completed. When the liquid in the filter 10 is recovered after the completion of the re-concentration operation, the liquid in the filter 10 can be recovered by the same method as described above.
< recovery operation of concentrator 20 >
When the concentrate in the concentrator 20 is recovered in the concentrate bag CB, the following method can be adopted.
< recovery of liquid feeding portion 3p by filtrate supply tube >
First, the above-described operation of recovering the liquid in the filter 10 is performed, and the raw liquid present on the downstream side of the hollow fiber membranes in the filter 10 is supplied to the filtrate supply pipe 3. The whole of the stock solution existing on the downstream side of the hollow fiber membranes is supplied to the filtrate supply pipe 3, but the operation of the filtrate supply pipe liquid feed section 3p is continued thereafter. As a result, air (or cleaning liquid) is sucked from the pressure measuring portion 10s, and therefore, the liquid (filtrate) in the filtrate supply pipe 3 is supplied to the concentrator 20, concentrated in the concentrator 20, and recovered to the concentrate bag CB through the concentrate pipe 4. If the operation of the filtrate feed pipe liquid feed section 3p is continued even if the liquid in the filtrate feed pipe 3 is exhausted, the concentrated liquid in the concentrator 20 is recovered to the concentrated liquid bag CB, and if the concentrated liquid in the concentrator 20 is exhausted, the operation of the filtrate feed pipe liquid feed section 3p is stopped. Thereby, the concentrated liquid in the concentrator 20 can be recovered.
Further, it is possible to determine whether or not the concentrate in the concentrator 20 is consumed by checking the concentrate pipe 4 and the concentrate bag CB. For example, when air is sucked from the pressure measuring portion 10s, if air bubbles flow in the concentrate pipe 4 or air bubbles occur in the concentrate bag CB, it can be determined that the concentrate in the concentrator 20 is exhausted.
In the case of collecting the concentrated liquid in the concentrator 20, the cleaning liquid may be supplied from the pressure measuring portion 10s or the like. In this case, by measuring the concentration, color, and specific gravity of the liquid in the concentrate bag CB, it can be confirmed whether the concentrate in the concentrator 20 is consumed. For example, when all of the concentrated liquid in the concentrator 20 is recovered, the cleaning liquid is recovered in the concentrated liquid bag CB. As a result, the color of the liquid in the concentrate bag CB becomes light, and it can be determined that the concentrate in the concentrator 20 is consumed. When the cleaning liquid is collected in the concentrate bag CB, the liquid in the concentrate bag CB is mixed with the cleaning liquid, and the concentration and specific gravity of the liquid change from those of the case of the concentrate alone. Therefore, it is possible to confirm that the concentrate in the concentrator 20 is consumed by collecting the liquid in the concentrate bag CB and measuring the concentration and specific gravity of the liquid by the densitometer. Further, in the case of using a pump using a motor capable of measuring the number of rotations (rotation angle) such as a stepping motor as the filtrate supply pipe liquid feeding portion 3p, the capacity of each pipe (filtrate supply pipe 3, concentrate pipe 4, etc.) and the capacity of the concentrator 20 are obtained by calculation or the like in advance, and the transport amount derived from the rotation speed of the pump is measured, whereby it is also possible to determine that the recovery of the concentrate in the concentrator 20 is completed.
In the case where the water separation member of the concentrator 20 is a hollow fiber membrane, if the hollow fiber membrane has a property of not allowing air to pass through, the exhaustion of the concentrated solution in the concentrator 20 can be detected by the following method. First, when the water separation member of the concentrator 20 is a hollow fiber membrane, the filtrate supply pipe 3, the concentrate pipe 4, and the waste liquid pipe 5 are connected so that the concentrated liquid passes through the hollow fiber membrane. In this thickener 20, the flow rate of the concentrated liquid pipe 4 is made smaller than the flow rate of the waste liquid pipe 5 when the concentrated liquid in the thickener 20 is recovered. That is, in a state where the liquid is caused to flow from the waste liquid pipe 5 to the waste liquid bag DB side by the flow rate adjusting mechanism 5c, the flow rate of the liquid flowing from the concentrate pipe 4 to the concentrate bag CB is made smaller than the flow rate of the liquid flowing from the waste liquid pipe 5 to the waste liquid bag DB by the flow rate adjusting mechanism 4 c. Thus, while the air is fed into the hollow fiber membranes of the concentrator 20 as the recovery of the concentrated liquid in the concentrator 20 advances, the air cannot pass through the hollow fiber membranes, that is, the air does not leak into the waste liquid bag DB, and thus the air is filled into the hollow fiber membranes of the concentrator 20. As a result, the differential pressure between the concentrator membranes increases, and therefore, when the differential pressure between the concentrator membranes exceeds a certain differential pressure, it can be determined that the concentrated solution in the concentrator 20 is replaced with air, that is, that the concentrated solution in the concentrator 20 is recovered in its entirety.
< recovery by gravity >
The concentrate in the concentrator 20 may be recovered to the concentrate bag CB by gravity. In this case, if it is determined that the stock solution on the upstream side of the hollow fiber membrane is exhausted, the operation of the filtrate supply pipe liquid feeding portion 3p is stopped, and the pressure measuring portion 3s is removed from the filtrate supply pipe 3 (see fig. 8). In this state, when the concentrate bag CB is disposed below the concentrate outlet 20b of the concentrator 20, the concentrate can be recovered to the concentrate bag CB by flowing the liquid in the flow path through which the concentrate flows in the concentrator 20 toward the concentrate bag CB by gravity.
In the case of recovering by gravity, after the pressure measuring portion 3s is removed, the cleaning liquid may be supplied from a portion to which the pressure measuring portion 3s is connected to the filtrate supply pipe 3.
In addition, in the case of recovering by gravity, it is possible to determine whether or not the concentrate in the concentrator 20 is consumed by checking the concentrate pipe 4 and the concentrate bag CB. For example, when air is sucked from the pressure measuring portion 3s, if air bubbles flow in the concentrate pipe 4 or air bubbles occur in the concentrate bag CB, it can be determined that the concentrate in the concentrator 20 is exhausted. Further, the speed at which the liquid flows by gravity in the filtrate supply pipe 3, the thickener 20, the concentrate pipe 4, and the like may be obtained in advance by calculation and experiment, and the assumed recovery time may be calculated from the speed, and if the assumed recovery time has elapsed, it may be determined that recovery of the concentrate in the thickener 20 is completed.
In the case of recovering the concentrated liquid in the concentrator 20 by gravity using the above-described method, since the filtrate on the upstream side of the pressure measuring section 3s cannot be recovered, the operation of the filtrate supply pipe liquid feeding section 3p may be stopped after the filtrate is not present on the upstream side of the pressure measuring section 3 s. It is possible to grasp that the filtrate is not present on the upstream side of the pressure measuring portion 3s by confirming the filtrate supply pipe 3.
The filtrate on the upstream side of the pressure measuring section 3s may be recovered in the filtrate state by the branch pipe 6 to the concentrate bag CB.
In the case where the filtrate on the upstream side of the pressure measuring section 3s is collected together with the concentrated solution in the concentrator 20, the following method may be employed. First, the filtrate feed pipe liquid feed portion 3p is removed from the filtrate feed pipe 3, and the liquid is allowed to freely flow in the filtrate feed pipe 3. Next, the pressure measuring section 2s and the pressure measuring section 10s, which are connected to the flow path isolated from the filtrate supply pipe liquid feeding section 3p by the hollow fiber membrane of the filter 10, that is, the flow path communicating with the filtrate supply pipe liquid feeding section 3p, are removed. Thus, as in the case of removing the pressure measuring portion 3s from the filtrate supply pipe 3, air can be introduced from the portion from which the pressure measuring portion 2s or the pressure measuring portion 10s is removed. This allows the filtrate present on the downstream side of the portion from which the pressure measuring portion 2s or the pressure measuring portion 10s is removed to be recovered together with the concentrate in the concentrator 20.
< leak check >
When the filter member of the filter 10 is damaged, the raw liquid may pass through the filter member without being filtered when the raw liquid is supplied to the filter 10. Thus, the stock solution cannot be properly filtered. Therefore, in the stock solution treatment apparatus 1 of the present embodiment, it is desirable to confirm the leakage (leak check) of the filter 10 before performing the preparation for cleaning (see fig. 14).
An example of performing the leak test will be described below. In the following description, the case where the filter 10 has two stock solution supply ports 11a and 11a will be described.
When the leak test is performed, the operation of the filtrate feed pipe liquid feed portion 3p is stopped, and all the pipes 2 to 6 are closed by all the flow rate adjustment mechanisms 2c to 6 c. Then, one end of the filtrate supply pipe 3 is connected to the stock solution supply port 11a of the filter 10 (the stock solution supply port 11a to which the stock solution bag UB is not connected). In addition, one end of the cleaning liquid recovery tube 7 is connected to the filtrate discharge port 11c of the filter 10 in a state where the flow rate adjustment mechanism 7c is closed.
Next, the pressure measuring unit 3s is removed from the filtrate supply pipe 3, and the flow rate adjusting mechanisms 3c and 7c are opened, so that the filtrate supply pipe liquid feeding unit 3p is operated to flow the fluid in the opposite direction. Thereby, the air sucked from the pressure measuring section 3s is pushed into the filter 10 from the stock solution supply port 11a, and the liquid existing on the upstream side of the hollow fiber membranes of the filter 10 passes through the hollow fiber membranes and is discharged from the filtrate discharge port 11c of the filter 10. Then, when all the liquid on the upstream side of the hollow fiber membranes is discharged, the pressure in the space isolated from the filtrate discharge port 11c by the hollow fiber membranes increases. Then, the filtrate supply pipe liquid feed portion 3p is operated until the differential pressure between the pressures measured by the pressure measuring portion 2s and the pressure measuring portion 10s becomes a predetermined pressure (for example, 100mmHg or more and less than 500 mmHg), and if the differential pressure becomes the predetermined pressure, the operation of the filtrate supply pipe liquid feed portion 3p is stopped.
It is desirable that the predetermined pressure is equal to or higher than the differential pressure between the filter membranes in the filtration and concentration operation. For example, if the differential pressure between the filter membranes during the filtration and concentration operation is 200mmHg to 300mmHg, the leak test may be performed at about 400 mmHg.
When there is a damage to the filter member of the filter 10, since the flow rate adjustment mechanism 7c of the cleaning liquid recovery pipe 7 connected to the filtrate discharge port 11c of the filter 10 is opened, air leaks from the space on the upstream side of the hollow fiber membrane into the space connected to the filtrate discharge port 11c (i.e., into the hollow fiber membrane) through the damage. Thus, the differential pressure between the pressures measured by the pressure measuring unit 2s and the pressure measuring unit 10s becomes smaller than the predetermined pressure.
Therefore, if the operation of the filtrate feed pipe liquid feed portion 3p is stopped for a predetermined time (for example, about 2 minutes) and the differential pressure of the pressure measured by the pressure measuring portion 2s and the pressure measuring portion 10s is maintained for a predetermined time, it can be determined that the filter member of the filter 10 is not damaged, and thus the leak inspection is terminated.
In the case where the leak test is performed by pressing air into the filter 10 as described above, the space on the upstream side of the hollow fiber membranes of the filter 10 is pressurized. Therefore, in the case where other operations such as preparation cleaning are continuously performed after the leak inspection, it is desirable to reduce the pressure in the space on the upstream side of the hollow fiber membranes of the filter 10. In order to reduce the pressure in the space upstream of the hollow fiber membranes of the filter 10, the space upstream of the hollow fiber membranes of the filter 10 may be connected to the outside. For example, when the flow rate adjusting mechanism 6c of the branch pipe 6 is opened, the air in the space upstream of the hollow fiber membrane of the filter 10 can be discharged to the outside, and the pressure in the space upstream of the hollow fiber membrane of the filter 10 can be reduced. When the pressure in the space upstream of the hollow fiber membrane of the filter 10 is reduced, the cleaning liquid recovery tube 7 is removed from the filtrate discharge port 11c, the filtrate supply tube 3 is removed from the stock solution supply port 11a and connected to the filtrate discharge port 11c, and then the flow rate adjustment mechanism 2c of the feed tube 2 is opened and the filtrate supply tube liquid feed portion 3p is operated so that the liquid flows in the forward direction in the filtrate supply tube 3, that is, the cleaning liquid is supplied from the cleaning liquid bag SB, so that the preparation cleaning can be directly performed (see fig. 2). The raw liquid supply port 11a connected to the filtrate supply pipe 3 may be closed by a filter connector or the like, but if the cleaning liquid recovery pipe 7 is connected to the raw liquid supply port 11a, the space on the upstream side of the hollow fiber membranes in the filter 10 and the outer surfaces of the hollow fiber membranes can be prepared for cleaning.
Further, by performing the preparatory cleaning operation while maintaining the pipe connection state at the time of performing the leak inspection, the pressure in the space on the upstream side of the hollow fiber membranes of the filter 10 can be reduced. For example, from the state of leak inspection (state of fig. 14), the flow rate adjustment mechanism 7c of the cleaning liquid recovery tube 7 is closed, the pressure measurement unit 3s is attached, the flow rate adjustment mechanism 4c of the concentrate tube 4 and the flow rate adjustment mechanism 5c of the waste liquid tube 5 are opened, and the filtrate supply tube liquid feed unit 3p is operated to suck the air in the space upstream of the hollow fiber membranes of the filter 10. Then, if the pressure of the pressure measuring unit 2s or the differential pressure between the filter membranes is checked to determine that the pressure has dropped, the cleaning liquid is supplied from the cleaning liquid bag SB by opening the flow rate adjusting mechanism 2c of the liquid supply pipe 2, so that the preparation cleaning can be performed directly.
In this method, since air enters the concentrator 20, if the air in the concentrator 20 is difficult to empty, the concentrator 20 may be removed from the filtrate supply pipe 3 in advance at the time of leak inspection, and the air in the filter 10 may be empty, and then the concentrator 20 may be connected to the filtrate supply pipe 3. Further, in order to efficiently fill the space on the upstream side of the hollow fiber membrane of the filter 10 with the cleaning liquid, the filter 10 may be reversed in advance before the flow rate adjusting mechanism 2c of the liquid supply pipe 2 is opened, and the cleaning liquid may be flowed from the lower side to the upper side.
In the method of performing the preparatory cleaning operation while maintaining the pipe connection state at the time of performing the leak inspection, the preparatory cleaning of the space on the upstream side of the hollow fiber membranes and the outer surfaces of the hollow fiber membranes in the filter 10 can be performed, but the preparatory cleaning of the space on the downstream side of the hollow fiber membranes in the filter 10 cannot be performed because the cleaning liquid is not supplied to the space on the downstream side of the hollow fiber membranes in the filter 10. In this case, if the connection between the cleaning liquid recovery pipe 7 and the filtrate supply pipe 3 is changed after the pressure in the space upstream of the hollow fiber membranes in the filter 10 is reduced or after the space upstream of the hollow fiber membranes in the filter 10 and the preparation cleaning of the outer surfaces of the hollow fiber membranes are performed to some extent, the preparation cleaning of the space downstream of the hollow fiber membranes in the filter 10 can also be performed. That is, the flow rate adjusting mechanism 2c of the liquid feed pipe 2 is temporarily closed, and the operation of the filtrate feed pipe 3 is also temporarily stopped, and the cleaning liquid recovery pipe 7 is detached from the filtrate discharge port 11c, and the filtrate feed pipe 3 is detached from the stock solution feed port 11a and connected to the filtrate discharge port 11 c. After that, by opening the flow rate adjustment mechanism 2c of the liquid feed pipe 2 and operating the filtrate feed pipe liquid feed portion 3p so that the liquid flows in the positive direction in the filtrate feed pipe 3, the cleaning liquid supplied from the cleaning liquid bag SB is made to pass through the hollow fiber membranes, so that the space on the downstream side of the hollow fiber membranes in the filter 10 can be prepared for cleaning.
In the above example, the case where the air is pushed into the filter 10 to perform the leak check was described, but as shown in fig. 21, the air may be sucked out from the filter 10 to perform the leak check. In this case, too, the operation of the filtrate feed pipe liquid feed section 3p is stopped first, and all the pipes 2 to 6 are closed by all the flow rate adjustment mechanisms 2c to 6 c. Then, one end of the filtrate supply pipe 3 is connected to the stock solution supply port 11a of the filter 10 (the stock solution supply port 11a to which the stock solution bag UB is not connected). In addition, one end of the cleaning liquid recovery tube 7 is connected to the filtrate discharge port 11c of the filter 10 in a state where the flow rate adjustment mechanism 7c is closed.
Next, the pressure measuring unit 3s is removed from the filtrate supply pipe 3, and the flow rate adjusting mechanisms 3c and 7c are opened, so that the filtrate supply pipe liquid feeding unit 3p is operated to flow the fluid in the forward direction. Thereby, the liquid and gas existing in the space on the upstream side of the hollow fiber membrane are sucked out, and the pressure in the space on the upstream side of the hollow fiber membrane, that is, the space isolated from the filtrate discharge port 11c by the hollow fiber membrane is reduced. Then, the filtrate supply pipe liquid feed portion 3p is operated until the differential pressure between the pressures measured by the pressure measuring portion 2s and the pressure measuring portion 10s becomes a predetermined pressure (for example, 100mmHg or more and less than 500 mmHg), and if the differential pressure becomes the predetermined pressure, the operation of the filtrate supply pipe liquid feed portion 3p is stopped.
It is desirable that the predetermined pressure is equal to or higher than the differential pressure between the filter membranes in the filtration and concentration operation. For example, if the differential pressure between the filter membranes during the filtration and concentration operation is 200mmHg to 300mmHg, the leak test may be performed at about 400 mmHg.
If there is damage to the filter member of the filter 10, in this case, since the flow rate adjustment mechanism 7c of the cleaning liquid recovery pipe 7 connected to the filtrate discharge port 11c of the filter 10 is opened, air leaks to the space on the upstream side of the hollow fiber membrane through the filtrate discharge port 11c via the damage. Thus, the differential pressure between the pressures measured by the pressure measuring unit 2s and the pressure measuring unit 10s becomes smaller than the predetermined pressure.
Therefore, if the operation of the filtrate feed pipe liquid feed portion 3p is stopped for a predetermined time (for example, about 2 minutes) and the differential pressure of the pressure measured by the pressure measuring portion 2s and the pressure measuring portion 10s is maintained for a predetermined time, it can be determined that the filter member of the filter 10 is not damaged, and thus the leak inspection is terminated.
When air is sucked out from the filter 10 and leak inspection is performed, the space on the upstream side of the hollow fiber membranes of the filter 10 is set to a low pressure. Therefore, the preparatory cleaning operation can be performed from the leak inspection as long as the operation is performed as follows. First, from the leak inspection state (the state of fig. 21), the flow rate adjustment mechanism 7c of the cleaning liquid collection tube 7 is closed, and the flow rate adjustment mechanism 2c of the liquid supply tube 2 is opened. Thereby, the cleaning liquid is supplied from the cleaning liquid bag SB to the filter 10, and the cleaning liquid is filled into the space on the upstream side of the hollow fiber membranes of the filter 10 and the hollow fiber membranes. After that, by installing the pressure measuring section 3s, the flow rate adjusting mechanism 4c of the concentrate pipe 4 and the flow rate adjusting mechanism 5c of the waste liquid pipe 5 are opened, and the filtrate supplying pipe liquid feeding section 3p is operated to cause the liquid to flow in the forward direction in the filtrate supplying pipe 3, so that the preparation cleaning can be directly performed. In order to efficiently fill the space upstream of the hollow fiber membrane of the filter 10 with the cleaning liquid, the filter 10 may be reversed in advance before the flow rate adjustment mechanism 2c of the liquid supply pipe 2 is opened, and the cleaning liquid may be flowed from below to above.
In the method of performing the preparatory cleaning operation after the leak inspection by sucking out air from the filter 10, the preparatory cleaning of the space on the upstream side of the hollow fiber membranes and the outer surfaces of the hollow fiber membranes in the filter 10 can be performed, but the cleaning liquid is not supplied to the space on the downstream side of the hollow fiber membranes in the filter 10. In this case, if the connection between the cleaning liquid collection pipe 7 and the filtrate supply pipe 3 is changed after the space on the upstream side of the hollow fiber membrane in the filter 10 and the preparation cleaning of the outer surface of the hollow fiber membrane are performed to some extent, the preparation cleaning of the space on the downstream side of the hollow fiber membrane in the filter 10 can also be performed. That is, the flow rate adjusting mechanism 2c of the liquid feed pipe 2 is temporarily closed, and the operation of the filtrate feed pipe 3 is also temporarily stopped, and the cleaning liquid recovery pipe 7 is detached from the filtrate discharge port 11c, and the filtrate feed pipe 3 is detached from the stock solution feed port 11a and connected to the filtrate discharge port 11 c. Thereafter, the flow rate adjusting mechanism 2c of the liquid feed pipe 2 is opened, and the filtrate feed pipe liquid feed portion 3p is operated so that the liquid flows in the positive direction in the filtrate feed pipe 3. Accordingly, since the cleaning liquid supplied from the cleaning liquid bag SB passes through the hollow fiber membranes, the space on the downstream side of the hollow fiber membranes in the filter 10 can also be prepared for cleaning.
< adjusting tool 50>
In the above example, the case where the flow rate adjustment mechanism 4c such as a clamp or a clip is provided in the concentrate line 4 has been described. A general clamp or clip used as the flow rate adjustment mechanism 4c has a function of closing or opening the concentrate pipe 4, and if the clamp is used, the flow rate of the liquid flowing in the concentrate pipe 4 can be adjusted. For example, a clamp commonly used in a medical field can be opened and closed only, but the flow rate of the liquid can be adjusted as long as the clamp can not completely close the tube. That is, if the clamp is a clamp capable of holding the member (roller or the like) of the squeeze tube at a desired position (fixable), the flow rate of the liquid flowing in the concentrate tube 4 can be adjusted by adjusting the position at which the member of the squeeze tube is fixed.
The adjustment tool 50 corresponds to an adjustment unit described in the claims.
However, in the case of a general clamp or the like, even if the clamp has a function of adjusting the flow rate of the liquid, the flow rate of the concentrate flowing through the concentrate pipe 4 cannot be accurately adjusted.
Therefore, when the following adjusting tool 50 is used as the flow rate adjusting means 4c, the flow rate of the concentrate flowing through the concentrate pipe 4 can be accurately adjusted. Further, by adjusting the operation of the filtrate feed pipe liquid feed section 3p, that is, the flow rate of the liquid flowing in the filtrate feed pipe 3, the differential pressure between the concentrator membranes can be adjusted to an appropriate range.
The following configuration can be adopted as the adjustment tool 50.
In the case where the above-described adjusting device 50 is provided in the concentrate pipe 4, the concentrate pipe 4 having flexibility or softness is used as the concentrate pipe 4. Examples of the tube include a tube made of polyvinyl chloride or silicone rubber.
As shown in fig. 15, the adjuster 50 includes a base member 51, 2 pipe holding members 52 provided to the base member 51, and a cover member 53.
The base member 51 is a plate-like member, and 2 columnar tube holding members 52 are provided on the surface thereof so as to be spaced apart from the gap 52 s. The lid member 53 is used to block the opening of the front end (upper end in fig. 15 (B) and 15 (C)) of the 2 tube holding members 52. That is, as will be described later, when the concentrate pipe 4 is disposed in the gap 52s of the 2 cylindrical pipe holding members 52, the lid member 53 is provided so that the concentrate pipe 4 does not come out of the gap 52 s.
The 2 pipe holding members 52 are formed such that the gap 52s formed therebetween satisfies the following condition. That is, by forming the gap 52s to have the width 52w, when water is caused to flow at 50mL/min in the concentrate pipe 4 placed in the gap 52s so as not to exert gravity on the water flowing direction, the average pressure of the water in the concentrate pipe 4 can be maintained at 10mmHg or more and 100mmHg or less.
According to this configuration, when the flow rate of the concentrate flowing through the concentrate line 4 is set to 200mL/min, the differential pressure between the concentrator membranes (that is, the pressure of the pressure measuring section 3 s) can be increased to about 400 mmHg. Thus, when the flow rate of the filtrate feed pipe liquid feed portion 3p is increased to the maximum flow rate that can be supplied to the general concentrator 20, in other words, the flow rate at which the concentration operation can be performed safely in the concentrator 20, the differential pressure between the concentrator membranes can be increased to about 400mmHg, which is the maximum differential pressure between the concentrator membranes at which the concentration operation can be performed safely in the concentrator 20. That is, the concentration process can be performed under the condition that the differential pressure between the concentrator membranes is maximized and the concentration efficiency in the concentrator 20 is maximized (the flow rate at which the concentration operation can be safely performed in the concentrator 20), and therefore the filtration efficiency and the concentration efficiency can be improved.
If a pipe having a circular cross section formed of polyvinyl chloride or silicone rubber is used as the concentrate pipe 4, the concentration process can be performed under the above-described conditions if the width 52w of the gap 52s is adjusted to be 95% to 110% of the thickness t4 of the concentrate pipe 4 (i.e., the total of the thicknesses t4 in the diameter direction). That is, the concentration process can be performed under the condition that the differential pressure between the membranes of the concentrator is maximized and the concentration efficiency in the concentrator is maximized.
For example, the concentrate pipe 4 is formed of polyvinyl chloride or silicone rubber, and has a circular cross section, the outer diameter D of the concentrate pipe 4 is 3.0 to 12.0mm, the inner diameter Dt is 2.0 to 8.0mm, and the wall thickness t4 is 0.5 to 2.0mm. In this case, if the width 52w of the gap 52s is adjusted to 0.95 to 4.40mm, the concentration process can be performed under the above-described conditions.
In the case of adjusting the width 52w of the gap 52s as described above, there are cases where not only a space is formed to some extent in the concentrate pipe 4 at the position of the 2 pipe holding members 52 (that is, a space is formed between the inner surfaces of the concentrate pipes 4), but also the inner surfaces of the concentrate pipes 4 are in contact with each other at the position of the 2 pipe holding members 52. However, in the case of adjusting the width 52w of the gap 52s as described above, even if the inner surfaces of the concentrate pipes 4 are in contact with each other at the positions of the 2 pipe holding members 52, the concentrate can be recovered from the concentrator 20 to the concentrate bag CB through the concentrate pipe 4 as long as the concentrate can ooze (leak) from between the inner surfaces of the concentrate pipes 4. The state where a certain space is formed in the concentrate pipe 4 and the state where the inner surfaces of the concentrate pipes 4 are in contact with each other corresponds to "the concentrate flow path is adjusted to a predetermined state" described in the claims. In addition, even when a flexible or soft tube is not used as the concentrate flow path, the state in which a space for flowing the concentrate (a space having the same width as the case where the adjustment tool 50 is used as described above and the concentrate tube 4) is formed in the concentrate flow path, or the state in which there is no space for flowing the concentrate or only a small gap is present in the concentrate flow path and the concentrate can leak (leak) is also equivalent to the "state in which the concentrate flow path is adjusted to a predetermined state" described in the claims. For example, the concentration liquid flow path may be configured to be capable of changing the distance between the pair of side walls, and the 2 states may be set.
< other examples of the adjusting tool 50 >
The adjustment tool 50 may have 3 or more tube holding members 52. In the case where 3 or more tube holding members 52 are provided, it is desirable to provide each tube holding member 52 so that the width of the gap formed between adjacent tube holding members 52 is different. For example, as shown in fig. 15 (C), in the case where 4 pipe holding members 52 are provided, the 4 pipe holding members 52 are provided so that the widths 52W1 to W3 of the gaps 52s1 to s3 are different. Accordingly, by disposing the concentrate pipe 4 in a gap having an appropriate width according to the concentrate pipe 4, the flow rate of the concentrate flowing in the concentrate pipe 4 can be accurately adjusted. By adjusting the flow rate of the liquid flowing through the filtrate supply pipe 3, the differential pressure between the concentrator membranes of the concentrator 20 can be adjusted to an appropriate range.
< concerning the base member 51 and the tube holding member 52>
The base member 51 is not limited to a plate-like member, and may be formed in any shape. The base member 51 may have a strength capable of maintaining the width of the concentrate pipe 4 when it is inserted into the gap between the adjacent pipe holding members 52.
< about tube holding Member 52>
In the above example, the tube holding member 52 has been described as being cylindrical, but the tube holding member 52 may be curved at the portion contacting the concentrate tube 4 on the surface facing each other, and the tube holding member 52 may not necessarily have a circular cross section. More specifically, the intersection line between the axial plane including the concentrate tube 4 in the portion in contact with the tube holding member 52 and the surface in contact with the concentrate tube 4 in the tube holding member 52 may be circular arc. In this case, the curvature radius of the curved surface of the portion in contact with the concentrate pipe 4, in other words, the curvature radius R of the circular arc (see fig. 15 a. The radius corresponding to the pipe holding member 52 in fig. 15 a) is preferably 1 to 10mm, more preferably 3 to 7mm. In particular, when the radius of curvature R is larger than 7mm, the variation in the differential pressure between the concentrator membranes can be made gentle when the flow rate of the liquid flowing in the concentrate pipe 4 is changed. Thus, even if the flow rate of the liquid flowing through the concentrate pipe 4 changes, the differential pressure between the concentrator membranes is easily maintained in a stable state. On the other hand, when the radius of curvature R is smaller than 7mm, the differential pressure between the concentrator membranes abruptly changes when the flow rate of the liquid flowing in the concentrate pipe 4 is changed. This can quickly reflect a change in the flow rate of the liquid flowing through the concentrate pipe 4 in the differential pressure between the concentrator membranes. Therefore, when the plurality of tube holding members 52 are provided and the plurality of gaps are provided, if the tube holding members having the same width but different radii of curvature of the surfaces in contact with the concentrate tubes 4 are provided in advance, the variation in the differential pressure between the concentrator membranes can be adjusted even when the differential pressure between the concentrator membranes is adjusted to be the same.
In the tube holding member 52, the portion in contact with the concentrate tube 4 does not have to be curved. The portion in contact with the concentrate pipe 4 may be a flat surface or a polygonal shape or a wave shape composed of a plurality of flat surfaces, as long as the shape of the concentrate pipe 4 is not damaged when the concentrate pipe 4 is held.
< yet another example of the adjusting tool 50 >
In the above example, the case where the adjustment tool 50 has a structure in which the concentrate pipe 4 is sandwiched between the cylindrical pipe holding members 52 has been described, but the adjustment tool 50 may not have a structure in which the concentrate pipe 4 is deformed by the cylindrical pipe holding members. For example, in the above-described adjusting tool 50, the concentrated liquid tube 4 may be deformed by being sandwiched between the base member 51 and the cover member 53. In this case, the base member 51 and the cover member 53 are brought close to each other, and a constant gap therebetween can be maintained. When the gap between the both is appropriately adjusted, the function of accurately adjusting the flow rate of the concentrate flowing through the concentrate pipe 4 can be exhibited in the same manner as in the case where the concentrate pipe 4 is sandwiched between the pipe holding members 52 described above when the concentrate pipe 4 is sandwiched between the both. In this case, the base member 51 and the cover member 53 correspond to the tube holding member described in the claims.
< detailed description of Filter 10 >
The filter 10 used in the raw liquid treatment apparatus 1 of the present embodiment is, for example, a peritoneal fluid filter used in CART, a plasma separator used in plasma exchange, a plasma component separator, or the like. The filter 10 accommodates a filter member therein, and can separate a filtrate from a separated liquid containing cells or the like by filtering a pleuroperitoneal cavity effusion with the filter member.
The structure of the filter 10 in the case where the filter member is a hollow fiber membrane 16 will be described below with reference to fig. 16.
As shown in fig. 16, the filter 10 includes a main body 11 and a hollow fiber membrane bundle 15 disposed in the main body 11.
< hollow fiber Membrane Beam 15>
As shown in fig. 16, the hollow fiber membrane bundle 15 is formed by bundling a plurality of hollow fiber membranes 16.
The hollow fiber membrane 16 is a tubular member having a wall 16w with an annular cross section, and a through flow path 16h penetrating the hollow fiber membrane 16 in the axial direction is formed in the wall 16 w. The wall 16w of the hollow fiber membrane 16 has a function of being impermeable to solid components such as cells and gases but permeable to liquids. The wall 16w of the hollow fiber membrane 16 may also function to be permeable to gas in general, but when immersed in liquid, gas cannot permeate therethrough and liquid can permeate therethrough.
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 with each other. That is, the hollow fiber membrane bundles 15 are formed by bundling the plurality of hollow fiber membranes 16 such that the through flow channels 16h of the hollow fiber membranes 16 penetrate between one end and the other end of the hollow fiber membrane bundle 15.
In addition, the two end portions of the plurality of hollow fiber membranes 16 may not be bound to each other. In this case, both ends of the through channels 16h of the plurality of hollow fiber membranes 16 are arranged so as to communicate with the pair of header portions 13, 14 of the main body 11, respectively.
< body portion 11>
As shown in fig. 16, the body 11 includes a trunk 12, and the trunk 12 has an inner space 12h which is a space that is airtight and liquid-tight from the outside. The internal space 12 of the trunk portion 12 is formed so as to communicate with the outside only through the stock solution supply port 11a provided on the side surface of the trunk portion 12, and accommodates the hollow fiber membrane bundle 15 therein. In the state where the hollow fiber membrane bundles 15 are accommodated therein, the internal space 12 is hermetically isolated from the through passages 16h of the plurality of hollow fiber membranes 16, but the liquid can pass through the wall 16w therebetween. That is, the liquid in the internal space 12 can be supplied to the through flow path 16h, and the liquid in the through flow path 16h can be supplied to the internal space 12.
The size and shape of the internal space 12 are not particularly limited. As long as the size has the following extent: in a state where the hollow fiber membrane bundle 15 is accommodated, the liquid flowing into the internal space 12 through the stock solution supply port 11a can flow between the hollow fiber membrane bundle 15 and the inner surface of the trunk portion 12 (i.e., the inner surface of the internal space 12) and between the plurality of hollow fiber membranes 16, and the liquid can flow into the through flow path 16h through the wall 16w of the hollow fiber membranes 16. In addition, the following sizes are only required: the liquid flowing out from the through-flow channel 16h to the internal space 12 through the wall 16w of the hollow fiber membrane 16 can 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 12, and can flow out from the filtrate discharge port 11 c.
As shown in fig. 16, a pair of header portions 13, 14 are provided in the body portion 11 so as to sandwich the trunk portion 12, that is, so as to sandwich the internal space 12 h. The pair of header portions 13 and 14 are air-tight and liquid-tight isolated from the inner space 12h of the trunk portion 12 and the outside. Of the pair of header parts 13, 14, the header part 13 communicates with the outside only through the above-mentioned cleaning liquid supply port 11b, and the header part 14 communicates with the outside only through the above-mentioned filtrate discharge port 11 c. The ends of the hollow fiber membrane bundles 15 are connected to the pair of header portions 13 and 14, respectively. Specifically, both end portions of the hollow fiber membrane bundle 15 are connected to the pair of header portions 13 and 14, respectively, so that openings at both ends of the through flow paths 16h of the plurality of hollow fiber membranes 16 constituting the hollow fiber membrane bundle 15 communicate with the inside of the pair of header portions 13 and 14. Accordingly, the pair of header portions 13 and 14 are connected to each other through the through-flow passages 16h of the plurality of hollow fiber membranes 16 constituting the hollow fiber membrane bundle 15.
< function of Filter 10 >
Since the filter 10 has the above-described structure, the raw liquid can be supplied from the raw liquid bag UB to the inner space 12h of the trunk portion 12 of the main body portion 11 through the liquid supply pipe 2 and the raw liquid supply port 11 a. Accordingly, the internal space 12h of the trunk portion 12 of the main body portion 11 communicates with the outside only through the raw liquid supply port 11a, and therefore the raw liquid supplied to the internal space 12h flows into the through flow path 16h through the wall 16w of the hollow fiber membrane 16. As a result, the solid component contained in the raw liquid cannot pass through the wall 16w of the hollow fiber membrane 16 and remain in the internal space 12h, and a filtrate obtained by filtering the raw liquid, which is a liquid component passing through the wall 16w of the hollow fiber membrane 16, can be obtained. The filtrate obtained by filtration can be supplied to the outside through the filtrate discharge port 11 c.
On the other hand, if the cleaning liquid is supplied from the filtrate discharge port 11c as described above, the cleaning liquid flows from the through flow path 16h of the hollow fiber membrane 16 through the wall 16w into the inner space 12h of the trunk portion 12 of the main body portion 11, and therefore clogging of the wall 16w of the hollow fiber membrane 16 or the like can be eliminated.
< detailed description of concentrator 20 >
The thickener 20 used in the stock solution treatment apparatus 1 of the present embodiment 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 described above, and has a function of separating moisture from filtrate to prepare a concentrated solution. That is, the concentrator 20 has a structure in which a moisture separation member having a function of separating moisture from the filtrate is accommodated in place of the separation member of the filter 10. For example, a peritoneal fluid concentrator for CART, a dialysis filter for dialysis, a membrane-type plasma component fractionator for double filtration plasma exchange therapy, or the like can be used for the concentrator 20.
For example, if the moisture separator is a hollow fiber membrane, the concentrator 20 has a structure including a trunk portion 22 and a pair of header portions 23 and 24, the trunk portion 22 having an internal space 22h which is a space for accommodating a bundle 25 of hollow fiber membranes formed by bundling the hollow fiber membranes 16, and the pair of header portions 23 and 24 connecting both ends of the bundle 25 (see fig. 17). The waste liquid discharge port 20c connected to the waste liquid pipe 5 is provided on a side surface of the trunk portion 22, and the trunk portion 22 of the concentrator 20 is formed so as to communicate with the outside only through the waste liquid discharge port 20 c. The above-described filtrate supply port 20a is provided in the header portion 23 disposed above the pair of header portions 23, 24 during the filtration and concentration operation, and the header portion 23 is formed to communicate with the outside only through the filtrate supply port 20 a. On the other hand, the header 24 disposed below during the filtration and concentration operation is provided with a concentrate outlet 20b to which the concentrate pipe 4 is connected, and the header 24 is formed to communicate with the outside only through the concentrate outlet 20 b.
Therefore, if the filtrate is supplied from the filtrate supply port 20a into the concentrator 20, moisture is separated from the filtrate by the hollow fiber membrane 26 as a moisture separation 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 liquid from which the waste liquid is removed and concentrated is supplied to the concentrated liquid bag CB through the concentrated liquid outlet 20b and the concentrated liquid pipe 4.
< function of concentrator 20 >
Since the concentrator 20 has the above-described structure, the filtrate can be supplied from the filtrate supply pipe 3 into the through-flow path 26h of the hollow fiber membrane 26 through the filtrate supply port 20 a. Thus, while the filtrate passes through the hollow fiber membranes 26, the waste liquid can be separated from the filtrate, and the separated waste liquid can be recovered to the waste liquid bag DB through the waste liquid discharge port 20c and the waste liquid pipe 5. On the other hand, the concentrated solution from which the waste liquid is separated and concentrated can be recovered to the concentrated solution bag CB through the concentrated solution outlet 20b and the concentrated solution pipe 4.
< other example of the stock solution treatment apparatus 1 of the present embodiment >
In the above description, the case where the so-called external pressure filtration method is adopted in the stock solution treatment apparatus 1 of the present embodiment, in which the stock solution is supplied from the outside of the hollow fiber membrane as the filter member of the filter 10 and the filtrate is discharged to the inside of the hollow fiber membrane, is described. However, a so-called internal pressure filtration method may be employed in which a stock solution is supplied to the inside of the hollow fiber membranes of the filter 10 and a filtrate is discharged to the outside of the hollow fiber membranes.
In the case of using the internal pressure filtration method in the raw liquid treatment apparatus 1 of the present embodiment, for example, the circuit is configured as shown in fig. 19 and 20 in the filtration concentration operation and the filter cleaning operation.
First, in the filtration and concentration operation, as shown in fig. 19, the raw liquid bag UB communicates with a port of the through flow path 16h communicating with the hollow fiber membrane 16 in the main body 11 of the filter 10 via the liquid feed pipe 2, and the concentrator 20 communicates with a port communicating with the internal space 12 of the trunk 12 in the main body 11 of the filter 10 via the filtrate feed pipe 3. That is, the stock solution bag UB communicates with the cleaning solution supply port 11b of the filter 10 in fig. 16, and the concentrator 20 communicates with the stock solution supply port 11a of the filter 10 in fig. 16. The other components are constituted as a circuit in the same manner as in the case of using the external pressure filtration method (see fig. 1), and the filtration and concentration operation is performed.
In addition, at the time of filter cleaning operation, as shown in fig. 20, a port to which the feed pipe 2 is not connected among ports of the main body 11 of the filter 10 that communicate with the through flow paths 16h of the hollow fiber membranes 16 communicates with the cleaning liquid recovery bag FB (or a tub or the like) via the cleaning liquid recovery pipe 7. That is, the stock solution bag UB communicates with the cleaning solution supply port 11b of the filter 10 in fig. 16, and the cleaning solution recovery bag FB communicates with the filtrate discharge port 11c of the filter 10 in fig. 16. The other components constitute a circuit in the same manner as in the case of using the external pressure filtration method (see fig. 5), and the filter cleaning operation is performed.
In other operations, if the pipes are connected as described above, even in the case where the stock solution processing apparatus 1 of the present embodiment adopts the internal pressure filtration method, the operations can be performed in the same manner as in the case where the external pressure filtration method is adopted. That is, when the feed pipe 2 and the cleaning liquid collection pipe 7 are connected to the port communicating with the through-flow passage 16h of the hollow fiber membrane 16 in the main body 11 of the filter 10, and the filtrate supply pipe 3 and the pressure measurement section 10s are connected to the port communicating with the internal space 12 of the trunk 12 in the main body 11 of the filter 10, each operation can be performed in the same manner as in the case of using the external pressure filtration method even when the internal pressure filtration method is employed in the raw liquid treatment apparatus 1 of the present embodiment.
Examples
In the case of using the regulator of the present invention, the relationship between the flow rate and the pressure in the tube was confirmed when the physiological saline was flowed through the tube.
In the experiment, the change in the pressure in the tube when the flow rate of the physiological saline flowing through the tube was changed was measured using the circuit shown in fig. 18 (a). In this circuit, the tube is disposed so that a space (about 1500 mm) between a pump for feeding the physiological saline and a portion sandwiched by a pair of tube holding members of the adjustment instrument is horizontal. This is to prevent the weight of the physiological saline between the pump for feeding the physiological saline and the portion sandwiched by the pair of tube holding members of the regulator from affecting the pressure measurement.
The tube used in the experiment was a tube (model: KMT-K007-5, manufactured by Chuancheng chemical Co., ltd.) having a circular cross-section and made of polyvinyl chloride, and had an outer diameter of 4.9mm, a wall thickness of 0.75mm and an inner diameter of 3.4mm.
The pair of tube holding members were circular in cross section (radius 7 mm), and the width of the gap between the pair of tube holding members was 1.55mm.
In addition, the pressure inside the tube is measured by a pressure sensor (SMC model: PSE 543A-M5) at the upstream side of a pair of tube holding members of the regulator.
The liquid feeding in the pipe is performed using a roller pump, and the flow rate in the pipe is measured by the rotation amount of the pump.
The results are shown in fig. 18 (B) and (C).
As shown in fig. 18 (B) and (C), it was confirmed that the pressure in the pipe can be changed by increasing the flow rate. Further, the relationship between the pressure in the tube and the flow rate was shown in the case where the upper limit value (1.48 mm) and the lower limit value (1.70 mm) of the gap were conceivable, and it was confirmed that the slope of the pressure rise with respect to the change in the flow rate could be adjusted by the width of the gap between the pair of tube holding members.
Industrial applicability
The stock solution treatment device of the present invention is suitable for use as a device for filtering and concentrating a pleuroperitoneal cavity effusion containing cells or the like, blood or the like during surgery or exsanguination to obtain a concentrated solution, and a device for purifying and reutilizing plasma such as waste liquid plasma of blood exchange.
Description of the reference numerals
1 stock solution treatment device
2 liquid feeding pipe
2s pressure measuring part
3 filtrate supply pipe
3c flow adjusting mechanism
3p filtrate supply pipe liquid feeding part
3s pressure measuring part
4 concentrated liquid pipe
4c flow regulating mechanism
5 waste liquid pipe
5c flow regulating mechanism
6 branch pipe
6c flow regulating mechanism
7 cleaning liquid recovery pipe
7c flow regulating mechanism
7p cleaning liquid recovery pipe liquid feeding part
9 connecting pipe
9c flow regulating mechanism
9f flow adjusting mechanism
9p connecting pipe liquid feeding part
10 filter
10s pressure measuring part
11. Main body part
11 a stock solution supply port
11 b cleaning liquid supply port
11 c filtrate discharge port
12 trunk parts
12h of interior space
15 hollow fiber membrane bundle
16 hollow fiber membrane
16h through flow path
16w hollow fiber membrane wall
20 concentrator
20a filtrate supply port
20b concentrate discharge outlet
20c waste liquid discharge outlet
30 control part
50 adjusting part
52 tube holding member
52s gap
Width of 52w
UB stock solution bag
CB concentrated solution bag
DB waste liquid bag
SB cleaning liquid bag
FB cleaning liquid recovery bag.
Claims (22)
1. A stock solution treatment device for filtering and concentrating a stock solution to form a concentrated solution, 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 liquid supply channel which is arranged above the raw liquid supply port of the filter and communicates a raw liquid supply unit for supplying the raw liquid to the filter with the raw liquid supply port of the filter;
a filtrate supply channel that communicates a filtrate discharge port of the filter with a 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 waste liquid separated from the concentrated liquid in the concentrator;
a recovery unit disposed below the filtrate outlet of the filter, connected to the concentrate flow path, and configured to recover concentrate;
a branch flow path for communicating the recovery unit with the filtrate supply flow path;
a liquid feed portion provided between the concentrator and a connection portion of the filtrate supply flow path connected to the branch flow path;
a control part for controlling the operation of the liquid feeding part,
in a state where the control unit maintains the branch flow path so as to be in a state where liquid flows bi-directionally between the filtrate supply flow path and the recovery unit,
the operation of the liquid feeding portion is controlled by: starting gravity filtration for supplying the raw liquid from the raw liquid supply unit to the filter by gravity and, when the raw liquid is in a predetermined state, sending the liquid from the filter to the concentrator,
Or controlling the operation of the liquid feeding part by the following method: and starting gravity filtration, wherein the gravity filtration is used for supplying the stock solution from the stock solution supply part to the filter and simultaneously sending the liquid from the filter to the concentrator.
2. The stock solution treatment apparatus according to claim 1, wherein the predetermined state is a state in which an amount of the filtrate supplied to the recovery unit exceeds an amount of the liquid that can be accommodated in the recovery unit.
3. The stock solution processing apparatus according to claim 1 or 2, wherein the concentrate passage is provided with an adjusting portion for adjusting the concentrate passage to a predetermined state.
4. The stock solution processing apparatus according to claim 3, wherein the control unit controls the operation of the liquid feeding unit to adjust the flow rate of the liquid supplied to the concentrator, and controls the differential pressure between the concentrator membranes of the concentrator.
5. A stock solution treatment apparatus according to claim 3 or 4, wherein,
the concentrate flow path is a tube with a deformable cross section,
the adjustment part is a member having a gap in which the tube is disposed,
the gap of the adjustment portion is formed to have the following length:
when water is flowed at 50mL/min in the tube disposed in the gap, the average pressure of the water in the tube can be maintained at a length of 10mmHg to 100 mmHg.
6. A stock solution treatment apparatus according to claim 3 or 4, wherein,
the concentrate flow path is a tube with a deformable cross section,
the adjustment part is a member having a gap in which the tube is disposed,
the gap of the adjustment portion is adjusted so that the total wall thickness of the tube is 95-110% in a state where the tube is disposed in the gap.
7. A stock solution treatment apparatus according to claim 3 or 4, wherein,
the concentrate flow path is a pipe with a circular cross section formed of polyvinyl chloride or silicone rubber,
the adjustment part is a member having a gap in which the tube is disposed,
the outer diameter of the tube is 3.0-12.0 mm, the inner diameter is 2.0-8.0 mm, the wall thickness is 0.5-2.0 mm,
the width of the gap of the adjusting part is 0.95-4.40 mm.
8. A method of operating a stock solution treatment apparatus for filtering and concentrating a stock solution to form a concentrated solution, 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 stock solution supply unit configured to supply the stock solution to the filter;
A liquid supply passage for communicating the liquid supply portion with a liquid supply port of the filter;
a filtrate supply channel that communicates a filtrate discharge port of the filter with a 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 waste liquid separated from the concentrated liquid in the concentrator;
a recovery unit connected to the concentrate flow path and disposed below the filtrate outlet of the filter, for recovering the concentrate;
a branch flow path for communicating the recovery unit with the filtrate supply flow path;
a liquid feed portion provided between the concentrator and a connection portion of the filtrate supply flow path connected to the branch flow path;
a control part for controlling the operation of the liquid feeding part,
in a state where the branch flow path is maintained so as to be in a state where liquid flows in both directions between the filtrate supply flow path and the recovery section,
the liquid feeding part is operated as follows: starting gravity filtration for supplying the raw liquid to the filter from the raw liquid supply portion disposed above the raw liquid supply port of the filter by gravity, and sending the liquid from the filter to the concentrator when the raw liquid is in a predetermined state,
Or the liquid feeding part is operated by the following modes: and starting gravity filtration, wherein the gravity filtration is used for supplying the stock solution to the filter from the stock solution supply part arranged above the stock solution supply port of the filter by gravity and simultaneously sending the liquid from the filter to the concentrator.
9. The method of operating a stock solution treatment apparatus according to claim 8, wherein the predetermined state is a state in which an amount of filtrate supplied to the recovery unit exceeds an amount of liquid that can be accommodated in the recovery unit.
10. The method of operating a stock solution treatment apparatus according to claim 8 or 9, wherein an adjusting portion for adjusting the concentrate flow path to a predetermined state is provided in the concentrate flow path.
11. The method of operating a liquid concentrate processing apparatus according to claim 10, wherein a flow rate of the liquid supplied to the concentrator is adjusted, and a differential pressure between concentrator membranes of the concentrator is controlled.
12. A method of operating a liquid-handling apparatus according to claim 10 or 11, characterized in that,
the concentrate flow path is a tube with a deformable cross section,
the adjustment part is a member having a gap in which the tube is disposed,
The gap of the adjustment portion is formed to have the following length:
when water is flowed at 50mL/min in the tube disposed in the gap, the average pressure of the water in the tube can be maintained at a length of 10mmHg to 100 mmHg.
13. A method of operating a liquid-handling apparatus according to claim 10 or 11, characterized in that,
the concentrate flow path is a tube with a deformable cross section,
the adjustment part is a member having a gap in which the tube is disposed,
the gap of the adjustment portion is adjusted such that, in a state in which the tube is disposed in the gap, the length of the smallest portion of the inner diameter of the tube is 95% to 110% of the total wall thickness of the tube.
14. A method of operating a liquid-handling apparatus according to claim 10 or 11, characterized in that,
the concentrate flow path is a pipe with a circular cross section formed of polyvinyl chloride or silicone rubber,
the adjustment part is a member having a gap in which the tube is disposed,
the outer diameter of the tube is 3.0-12.0 mm, the inner diameter is 2.0-8.0 mm, the wall thickness is 0.5-2.0 mm,
the width of the gap of the adjusting part is 0.95-4.40 mm.
15. A method of operating a liquid processing apparatus according to any one of claims 8 to 14, wherein,
The filter has 2 stock solution supply ports,
the feed liquid flow path is connected to a stock liquid supply port located above the 2 stock liquid supply ports during the filtering and concentrating operation,
when the filter is cleaned, cleaning liquid is supplied from a filtrate outlet in the filter, and the cleaning liquid is discharged from a stock solution supply port or both of the 2 stock solution supply ports which are positioned below during the filtering and concentrating operation.
16. The method of operating a liquid concentrate processing apparatus according to claim 15, wherein the cleaning liquid is supplied from a waste liquid discharge port of the thickener, and the cleaning liquid is discharged from a liquid concentrate supply port or both of the 2 liquid concentrate supply ports located below the filter during the filtering and concentrating operation.
17. An adjusting device is characterized in that,
there are provided 2 tube holding members which are provided with a plurality of tube holding members,
the 2 tube holding members form a gap for a tube arrangement with deformable cross-sections,
the width of the gap formed between the two of the 2 tube holding members is formed to be as follows:
when water is flowed at 50mL/min in a tube disposed in a gap, the average pressure of water in the tube can be maintained at a length of 10mmHg to 100 mmHg.
18. The adjustment instrument of claim 17, wherein,
the tube disposed in the gap between the 2 tube holding members is a tube having a circular cross section formed of a deformable material,
the width of the gap formed between both of the 2 tube holding members is adjusted to be,
the wall thickness of the tube is 95 to 110% of the total wall thickness of the tube when the tube is disposed in the gap.
19. The adjustment instrument of claim 18, wherein,
the tube disposed in the gap between the 2 tube holding members is a tube having a circular cross section and formed of polyvinyl chloride or silicone rubber, has an outer diameter of 3.0 to 12.0mm, an inner diameter of 2.0 to 8.0mm, and a wall thickness of 0.5 to 2.0mm,
the width of the gap formed between the two of the 2 tube holding members is 0.95 to 4.40mm.
20. An adjustment instrument according to claim 17, 18 or 19, characterized in that the radius of curvature of the portions of the 2 tube holding members which are opposed to each other and in contact with the tube is formed to be 1 to 10mm.
21. An adjustment device as claimed in claim 17, 18, 19 or 20, characterized in that,
the tube holding member is provided with 3 or more,
gaps for disposing the tubes are formed between the adjacent tube holding members,
The tube holding members are disposed so that the widths of the gaps are different.
22. The adjustment instrument according to any one of claims 17 to 21, which is used as the adjustment unit of the stock solution treatment apparatus according to claim 3.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2021-133949 | 2021-08-19 | ||
| JP2021133949 | 2021-08-19 | ||
| PCT/JP2022/029393 WO2023021967A1 (en) | 2021-08-19 | 2022-07-29 | Stock solution treatment apparatus, stock solution treatment apparatus operating method, and adjuster |
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| Publication Number | Publication Date |
|---|---|
| CN117642193A true CN117642193A (en) | 2024-03-01 |
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| CN202280050017.0A Pending CN117642193A (en) | 2021-08-19 | 2022-07-29 | Stock solution treatment device, method for operating stock solution treatment device, and adjustment tool |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JPWO2023021967A1 (en) |
| CN (1) | CN117642193A (en) |
| WO (1) | WO2023021967A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117839436A (en) * | 2024-03-06 | 2024-04-09 | 山西绿泉环保工程有限公司 | Reverse osmosis membrane online cleaning and desalination performance testing device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3847370A (en) * | 1972-02-16 | 1974-11-12 | Horizon Ind Ltd | Tube servicing device |
| US5318546A (en) * | 1992-08-28 | 1994-06-07 | Bierman Steven F | Method of catheter irrigation and aspiration |
| JP2012075520A (en) * | 2010-09-30 | 2012-04-19 | Nihon Covidien Kk | Tool for preventing incorrect operation of clamp |
| JP6527884B2 (en) * | 2014-12-26 | 2019-06-05 | 旭化成メディカル株式会社 | Body cavity fluid treatment system |
| JP6584221B2 (en) * | 2015-08-24 | 2019-10-02 | 旭化成メディカル株式会社 | Medical materials |
| 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 |
| JP6667852B2 (en) * | 2018-08-18 | 2020-03-18 | 国立大学法人徳島大学 | Stock solution processing device and method of operating stock solution processing device |
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2022
- 2022-07-29 CN CN202280050017.0A patent/CN117642193A/en active Pending
- 2022-07-29 WO PCT/JP2022/029393 patent/WO2023021967A1/en active Application Filing
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117839436A (en) * | 2024-03-06 | 2024-04-09 | 山西绿泉环保工程有限公司 | Reverse osmosis membrane online cleaning and desalination performance testing device |
| CN117839436B (en) * | 2024-03-06 | 2024-05-14 | 山西绿泉环保工程有限公司 | Reverse osmosis membrane online cleaning and desalination performance testing device |
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