CN115253687A - Low-carbon high-efficiency short-flow full-ceramic membrane filtration water treatment method and device - Google Patents
Low-carbon high-efficiency short-flow full-ceramic membrane filtration water treatment method and device Download PDFInfo
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- CN115253687A CN115253687A CN202210922238.4A CN202210922238A CN115253687A CN 115253687 A CN115253687 A CN 115253687A CN 202210922238 A CN202210922238 A CN 202210922238A CN 115253687 A CN115253687 A CN 115253687A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 328
- 239000000919 ceramic Substances 0.000 title claims abstract description 174
- 238000000034 method Methods 0.000 title claims abstract description 40
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 21
- 238000005374 membrane filtration Methods 0.000 title claims description 19
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 158
- 239000012528 membrane Substances 0.000 claims abstract description 150
- 238000001728 nano-filtration Methods 0.000 claims abstract description 139
- 238000004140 cleaning Methods 0.000 claims abstract description 85
- 239000012459 cleaning agent Substances 0.000 claims abstract description 38
- 239000003814 drug Substances 0.000 claims abstract description 18
- 239000002455 scale inhibitor Substances 0.000 claims abstract description 16
- 230000000844 anti-bacterial effect Effects 0.000 claims abstract description 8
- 239000003899 bactericide agent Substances 0.000 claims abstract description 8
- 239000002270 dispersing agent Substances 0.000 claims abstract description 8
- 238000011001 backwashing Methods 0.000 claims description 54
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 47
- 239000000126 substance Substances 0.000 claims description 30
- 238000004519 manufacturing process Methods 0.000 claims description 20
- 238000009792 diffusion process Methods 0.000 claims description 15
- 238000011010 flushing procedure Methods 0.000 claims description 15
- 238000011144 upstream manufacturing Methods 0.000 claims description 12
- 229920003023 plastic Polymers 0.000 abstract description 4
- 239000004033 plastic Substances 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000012423 maintenance Methods 0.000 description 10
- 238000001914 filtration Methods 0.000 description 9
- 238000010992 reflux Methods 0.000 description 9
- 241000196324 Embryophyta Species 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 239000002351 wastewater Substances 0.000 description 8
- 239000005708 Sodium hypochlorite Substances 0.000 description 7
- 238000011084 recovery Methods 0.000 description 7
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 7
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 6
- 235000020188 drinking water Nutrition 0.000 description 6
- 239000003651 drinking water Substances 0.000 description 6
- 238000003860 storage Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000008399 tap water Substances 0.000 description 5
- 235000020679 tap water Nutrition 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- 229920000426 Microplastic Polymers 0.000 description 2
- 238000009295 crossflow filtration Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 241001391944 Commicarpus scandens Species 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000009457 shenkang Substances 0.000 description 1
- 239000001509 sodium citrate Substances 0.000 description 1
- NLJMYIDDQXHKNR-UHFFFAOYSA-K sodium citrate Chemical compound O.O.[Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O NLJMYIDDQXHKNR-UHFFFAOYSA-K 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Images
Classifications
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- 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
- B01D61/58—Multistep processes
-
- 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
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/08—Apparatus 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
- B01D61/18—Apparatus therefor
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/04—Backflushing
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/16—Use of chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
Abstract
The application discloses a low-carbon high-efficiency short-flow full-ceramic-membrane filtered water treatment device and a method, raw water enters a ceramic membrane micro-ultrafiltration device through a micro-ultrafiltration water inlet to be subjected to ceramic membrane micro-ultrafiltration; then, the water enters a ceramic membrane nanofiltration device from a nanofiltration water inlet to carry out ceramic membrane nanofiltration; the method comprises the following steps of cleaning a ceramic membrane micro-ultrafiltration device, and feeding a first cleaning agent into the ceramic membrane micro-ultrafiltration device from a micro-ultrafiltration water inlet by a first pump; the method comprises the steps of cleaning the ceramic membrane nanofiltration device, conveying a second cleaning agent from a nanofiltration water inlet to the ceramic membrane nanofiltration device by a second medicine feeding pump, and conveying one or more of a scale inhibitor, a bactericide and a biological dispersant from the nanofiltration water inlet to the ceramic membrane nanofiltration device by a third medicine feeding pump. The method has the functions of reducing system energy consumption, medicine consumption, investment/operation cost, no newly increased plastic risk of effluent quality and the like.
Description
Technical Field
The invention relates to a water treatment method and a water treatment device, in particular to a method and a device which can meet the water production requirement of high-quality drinking water with low carbon and high efficiency.
Background
The membrane technology is applied to the fields of chemical industry, medicines, petrifaction and the like in 2000, is gradually applied to the field of municipal sewage treatment in 2010, and is gradually exploded only after 2015 when applied in scale in the field of municipal sewage.
The application of the membrane technology in municipal tap water is started at the latest, and the outbreak trend begins to be highlighted only in two or three years. Although the start is late, the amount of the treated water of the municipal tap water is large, and by the end of 2019, the accumulative project of the Chinese membrane drinking water plant reaches 126, and the accumulative scale reaches 772 million tons/day.
The drinking water deep treatment process commonly used at home and abroad is ultrafiltration and nanofiltration, most of which are organic membranes and are made of high molecular polymers. The organic film has the advantages of low price, easy installation, high packing density and the like, but the organic film has poor mechanical strength and chemical stability, is easy to break or damage, has short service life, and has the risk of micro-plastic dissolution after long-term use because medicaments such as sodium hypochlorite and the like in operation and chemical cleaning of the organic film can damage the organic film (such as accelerated aging and the like). Along with the improvement of living standard, the requirement of people on good life is higher, the requirement on the quality of municipal tap water is higher, and the traditional process cannot meet the requirement.
The ceramic membrane technology is one of inorganic membranes, and the ceramic membrane can meet the requirement due to the unique advantages of stable physical and chemical properties, large flux and the like. In recent years, more and more ceramic membrane water production waterworks are used, and the market prospect is wide. In Japan, ceramic membranes have been widely used for drinking water treatment, and Metawater (alumina tubular ceramic membrane) corporation has operated over 200 ceramic membrane water purification plants, wherein the daily water supply capacity of the water plant in Fujing is 51900m 3 D, the water supply scale of the quiet post water plant reaches 10000m 3 (d) the water supply capacity of a tap water plant newly built in Shen-Kang county reaches 17 ten thousand meters 3 And d. The earliest ceramic membrane water plants of this company had been in operation for nearly 20 years to date, and the ceramic membranes had not yet been replaced. In 2014, PWN Technologies of the Netherlands Water works built a water supply scale of 12 ten thousand meters 3 Andijk III drinking water works of/d. In 2019, the largest-scale ceramic membrane water plant in the world, namely the Singapore Choa Chu Kang water plant, is built and put into operation, the scale of water production is 181,800m 3 /d。
The existing ceramic membrane technology for treating tap water has complex filtering process and long flow, and needs to be explored and researched for realizing the water production requirement of high-quality drinking water with low carbon and high efficiency.
Disclosure of Invention
Compared with the conventional organic membrane treatment process, the low-carbon high-efficiency short-flow water treatment device and method have the following remarkable advantages: low carbon, full ceramic, ultra-short flow, high recovery rate (ceramic ultrafiltration recovery rate is more than 97%, and ceramic nanofiltration recovery rate is more than 90%).
The first aspect of the application provides a low-carbon high-efficiency short-flow all-ceramic-membrane filtered water treatment device which comprises a ceramic membrane micro-ultrafiltration device and a ceramic membrane nanofiltration device; the ceramic membrane micro-ultrafiltration device comprises a micro-ultrafiltration water inlet and a micro-ultrafiltration water outlet, and the ceramic membrane nano-filtration device comprises a nano-filtration water inlet and a nano-filtration water outlet;
wherein, the micro-ultrafiltration water outlet is communicated with the nanofiltration water inlet; the micro-ultrafiltration water inlet is communicated with a micro-ultrafiltration cleaning device which comprises a first cleaning agent dosing container and a first dosing pump, and the first dosing container is communicated with the micro-ultrafiltration water inlet through the first dosing pump; the nanofiltration water inlet is communicated with a nanofiltration cleaning device which comprises a second cleaning agent dosing container, a second dosing pump, a scale inhibitor dosing container and a third dosing pump, the second cleaning agent dosing container is communicated with the nanofiltration water inlet through the second dosing pump, and the scale inhibitor dosing container is communicated with the nanofiltration water inlet through the third dosing pump.
In a second aspect, the present invention provides a low-carbon, high-efficiency and short-flow all-ceramic membrane filtration water treatment method, preferably a water treatment method using the all-ceramic membrane filtration water treatment device of the first aspect of the present invention.
The full ceramic membrane filtering water treatment method comprises the following steps:
raw water enters a ceramic membrane micro-ultrafiltration device through a micro-ultrafiltration water inlet to carry out ceramic membrane micro-ultrafiltration;
then, the nano-filtration water enters a ceramic membrane nano-filtration device from a nano-filtration water inlet to carry out ceramic membrane nano-filtration;
the method comprises the following steps of cleaning a ceramic membrane micro-ultrafiltration device, and feeding a first cleaning agent into the ceramic membrane micro-ultrafiltration device from a micro-ultrafiltration water inlet by a first pump;
the method comprises the steps of cleaning the ceramic membrane nanofiltration device, conveying a second cleaning agent from a nanofiltration water inlet to the ceramic membrane nanofiltration device by a second medicine feeding pump, and conveying one or more of a scale inhibitor, a bactericide and a biological dispersant from the nanofiltration water inlet to the ceramic membrane nanofiltration device by a third medicine feeding pump.
In a preferred embodiment, the all-ceramic membrane filtration water treatment device comprises a water inlet pipe which is communicated with the micro-ultrafiltration water inlet. More preferably, the first dosing container is connected to the inlet tube by a first dosing pump.
In a more preferred embodiment, the all-ceramic membrane filtration water treatment device further comprises a ozone water producing device, such as a generator or an ozone pretreatment device, for performing ozone treatment on the inlet water. More preferably, the ozone water producing apparatus performs ozone pretreatment of the inlet water at or upstream of the micro-ultrafiltration water inlet.
In a more preferred embodiment, the ozone water producing apparatus is located upstream of the connection point of the first dosing pump and the water inlet pipe.
In a more preferred embodiment, the ozone pretreatment is carried out before the raw water enters the ceramic membrane micro-ultrafiltration device through the micro-ultrafiltration water inlet, wherein, more preferably, the ozone water production device has the ozone dosage of 2.5-5.5mg/L and ensures that the ozone content in the outlet water entering the ozone water production device is more than or equal to 0.5mg/L.
In a preferred embodiment, the ceramic membrane micro-ultrafiltration device comprises a micro-ultrafiltration return port, the ceramic membrane nano-filtration device comprises a nano-filtration return port, and the nano-filtration return port and the micro-ultrafiltration return port are respectively independent or return to the micro-ultrafiltration water inlet together, preferably return to the upstream of the connection point of the first dosing pump and the water inlet pipe, and more preferably return to the upstream of the ozone generator or the ozone pretreatment device.
More preferably, the return water of the nanofiltration water return port and the micro-ultrafiltration water return port at least partially flows back to the micro-ultrafiltration water inlet, for example, the return water of the nanofiltration water return port and the micro-ultrafiltration water return port has a volume ratio of 0.1-1.5% in the water entering the micro-ultrafiltration water inlet.
More preferably, the return water of the micro-ultrafiltration return port comprises the cleaning water and/or concentrated water (wastewater generated by filtering) of the ceramic membrane micro-ultrafiltration device.
More preferably, the return water of the nanofiltration water return port comprises cleaning water and/or concentrated water of the ceramic membrane nanofiltration device.
In a preferred embodiment, the water inlet pressure of the ceramic membrane micro-ultrafiltration device is 0.01-0.35MPa.
In a preferred embodiment, the discharge pressure of the return port of the ceramic membrane micro-ultrafiltration device is 0.1-0.45MPa, such as the discharge pressure of concentrated water.
In a preferred embodiment, the water inlet pressure of the cleaning water of the ceramic membrane micro-ultrafiltration device is 0.1-0.45MPa.
In a preferred embodiment, the water inlet pressure of the water inlet of the ceramic membrane nanofiltration device is 0.18-0.85MPa.
In a preferred embodiment, the discharge pressure of the reflux port of the ceramic membrane nanofiltration device is 0.25-1.0MPa, such as the discharge pressure of concentrated water.
In a preferred embodiment, the washing water inlet pressure of the ceramic membrane nanofiltration device is 0.25-1.0MPa.
In a preferred embodiment, before water enters the ceramic membrane nanofiltration device, a third dosing pump doses one or more of a scale inhibitor, a bactericide and a biological dispersant into the water, for example, the scale inhibitor, the bactericide and the biological dispersant. In a preferred embodiment, the amount is from 0.10 to 0.38ppm.
In a preferred embodiment, the micro-ultrafiltration cleaning device and the nanofiltration cleaning device further respectively and independently comprise an air source, or the micro-ultrafiltration cleaning device and the nanofiltration cleaning device can share the same air source, so that backwash power is provided for the micro-ultrafiltration cleaning device and the nanofiltration cleaning device, and the micro-ultrafiltration cleaning device and the nanofiltration cleaning device form steam water washing together with backwash water. More preferably, the gas source may comprise a gas tank, a gas pump, a blower, etc.
In a preferred embodiment, the method further comprises the step of backwashing the ceramic membrane micro-ultrafiltration device, wherein backwashing power is provided by the gas source.
In a preferred embodiment, the method further comprises the step of backwashing the ceramic membrane nanofiltration device, and the backwashing power is provided by a gas source.
More preferably, the steam water flushing enters from the water outlet of the micro-ultrafiltration cleaning device and the nanofiltration cleaning device.
In a preferred embodiment, the cleaning of the ceramic membrane micro-ultrafiltration device further comprises: and (3) conveying the water generated by the ozone water generating device to the ceramic membrane micro-ultrafiltration device through a water inlet of the ceramic membrane micro-ultrafiltration device by a flushing pump, preferably conveying the water to the ceramic membrane micro-ultrafiltration device within 5-30 seconds at the water inlet flow rate of 1.5-4.5 times, and performing forward diffusion cleaning. More preferably, the positive diffusion cleaning interval is 2-168 hours.
The cleaning of the ceramic membrane micro-ultrafiltration device also comprises back washing, wherein the back washing is steam water washing, water used for the back washing is water filtered by the ceramic membrane nanofiltration device, and gas is from a gas source; the back washing pressure is 0.15-0.45MPa, the back washing water quantity is 5-20L, the back washing time is 0.5-5 seconds, and the back washing time interval is 0.5-10 hours; the back-washed steam water enters from the water inlet.
Preferably, the backwashed water of the ceramic membrane micro-ultrafiltration device enters the backwashed water through a backwashed port of the ceramic membrane micro-ultrafiltration device.
In a preferred embodiment, the first dosing container contains a chemical cleaning agent, such as sodium hypochlorite. More preferably, when the ceramic membrane micro-ultrafiltration device is cleaned, the concentration of the chemical cleaning agent fed into the water inlet of the ceramic membrane micro-ultrafiltration device by the first pump is 100-1000mg/L.
In a preferred embodiment, the cleaning of the ceramic membrane nanofiltration device further comprises: the water produced by the ceramic membrane nanofiltration device directly enters the ceramic membrane nanofiltration device within 2 to 15 seconds at the flow rate of 2.0 to 6.0 times of the water inlet flow rate, and is subjected to forward diffusion cleaning, wherein the forward diffusion cleaning interval time is 0.5 to 8 hours.
In a preferred embodiment, the method further comprises the step of backwashing the ceramic membrane nanofiltration device, wherein the backwashing is steam water flushing, water used for backwashing is water filtered by the ceramic membrane nanofiltration device, and the gas is from a gas source; the back washing pressure is 0.2-0.6MPa, the back washing water quantity is 2-30L, the back washing time is 0.2-3 seconds, and the back washing time interval is 0.5-8 hours.
Preferably, the backwashed water of the ceramic membrane nanofiltration device enters the backwashed water through a backwashed port of the ceramic membrane nanofiltration device.
In a preferred embodiment, a chemical cleaning agent, such as one or more of sodium hypochlorite and sodium citrate, is arranged in the second dosing container. More preferably, when the ceramic membrane micro-nanofiltration device is cleaned, the concentration of the chemical cleaning agent fed into the water inlet of the ceramic membrane nanofiltration device by the second pump is 100-1000mg/L.
Wherein, the chemical cleaning agent can be added at the same time of the positive diffusion cleaning.
In a preferred embodiment, all the pipelines and the like of the low-carbon high-efficiency short-flow-path all-ceramic membrane filtration water treatment device are made of food-grade stainless steel or food-grade glass materials.
Compared with the traditional organic ultrafiltration and organic nanofiltration systems, the low-carbon high-efficiency short-flow full-ceramic-membrane filtration water treatment device and method have the following remarkable advantages: the method has the advantages of low carbon, full ceramics, ultra-short flow, high recovery rate (the micro-ultrafiltration recovery rate is more than 97 percent, and the nanofiltration recovery rate is more than 90 percent), wherein the ceramic micro-ultrafiltration system and the ceramic nanofiltration system have the advantages of high physical/maintainability chemical cleaning efficiency, long recovery chemical cleaning period, low medicine consumption and the like.
Compare in traditional ceramic membrane and filter, this application pottery micro ultrafiltration membrane goes out water and directly inserts pottery system of straining through short-flow conduit, need not security personnel filtration system.
And all matched pipelines and the like are food-grade stainless steel and glass, so that the risk of adding micro plastic in the water making process can be effectively avoided. The low-carbon high-efficiency short-flow advanced treatment device and the method have the functions of reducing the energy consumption, the medicine consumption, the investment/operation cost of the system, avoiding the risk of newly-increased plastic in the effluent quality and the like.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the application and, together with the description, serve to explain the application and are not intended to limit the application. In the drawings: fig. 1 is a schematic flow diagram of a low-carbon, high-efficiency, short-flow, all-ceramic membrane filtration water treatment apparatus according to a preferred embodiment of the present invention.
Detailed Description
The invention provides a low-carbon high-efficiency short-flow full ceramic membrane filtration water treatment device and a method, and in order to make the purpose, technical scheme and effect of the invention clearer and clearer, the invention is further described in detail by referring to the attached drawings and examples. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
It should be noted that the terms "first," "second," and the like in the description and claims of the present invention and in the drawings described above are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order, it being understood that the data so used may be interchanged under appropriate circumstances. Furthermore, the terms "comprises," "comprising," and any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed, but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
The first embodiment is as follows:
as shown in figure 1, the low-carbon high-efficiency short-flow all-ceramic membrane filtration water treatment device comprises a ceramic membrane micro-ultrafiltration device 2 and a ceramic membrane nanofiltration device 3; the ceramic membrane micro-ultrafiltration device 2 comprises a micro-ultrafiltration water inlet 21 positioned at the bottom and a micro-ultrafiltration water outlet 22 positioned at the top, and the ceramic membrane nano-filtration device comprises a nano-filtration water inlet 31 positioned at the bottom and a nano-filtration water outlet 32 positioned at the top;
wherein, the micro-ultrafiltration water outlet 22 is communicated with the nanofiltration water inlet 31, and the nanofiltration outlet 32 is a water production outlet.
The micro-ultrafiltration water inlet 21 is communicated with a micro-ultrafiltration cleaning device which comprises a first cleaning agent dosing container 4 and a first dosing pump 41, and the first dosing container 4 is communicated with the micro-ultrafiltration water inlet 21 through the first dosing pump 41; the nanofiltration water inlet 31 is communicated with a nanofiltration cleaning device which comprises a second cleaning agent feeding container 5, a second feeding pump 51, a scale inhibitor feeding container 6 and a third feeding pump 61, the second cleaning agent feeding container 5 is communicated with the nanofiltration water inlet 31 through the second feeding pump 51, and the scale inhibitor feeding container 6 is communicated with the nanofiltration water inlet 31 through the third feeding pump 61.
The Chinese medicine in the scale inhibitor feeding container 6 is scale inhibitor bactericide/biological dispersant, and is continuously fed, and the feeding amount is 0.10ppm.
The first medicine adding container 4 pumps chemical cleaning agent into the ceramic membrane micro-ultrafiltration device 2 and is used for cleaning the ceramic membrane micro-ultrafiltration device 2, the cleaning agent is sodium hypochlorite, and the concentration of the cleaning agent is 200mg/L.
An ozone water production device 1 is further arranged at the upstream of the first dosing pump 41 for carrying out ozone treatment on inlet water, wherein the ozone water production device 1 can be an ozone generator or an ozone pretreatment device and is positioned at or at the upstream of the micro-ultrafiltration water inlet 21 for carrying out ozone pretreatment before raw water 7 enters the ceramic membrane micro-ultrafiltration device 2 through the micro-ultrafiltration water inlet 21, wherein more preferably, the ozone water production device has the ozone adding amount of 4.5mg/L and ensures that the ozone content in outlet water entering the ozone water production device is more than or equal to 0.5mg/L.
Therefore, when the ceramic membrane micro-ultrafiltration device 2 is cleaned, the ozone water producing device 1 can be further included to directly enter the ceramic micro-ultrafiltration membrane filtering device 2 within 10s at the water inlet flow rate of 1.5 times, and positive diffusion cleaning is carried out, wherein the interval time of the positive diffusion cleaning is 6 hours.
When the ceramic membrane micro-ultrafiltration device 2 is used for cleaning, the low-carbon high-efficiency short-flow full ceramic membrane filtration water treatment device can further comprise a gas storage tank, backwashing washing power is provided by the gas storage tank, backwashing water is ceramic nanofiltration membrane produced water to form steam-water backwashing, the backwashing water enters the ceramic membrane micro-ultrafiltration device 2 from a water outlet, the backwashing pressure is 0.15MPa, the backwashing water amount is 5L, the backwashing time is 1s, and the backwashing time interval is 0.5h.
And a chemical cleaning agent is pumped into the ceramic membrane nanofiltration device 3 by the second medicine adding container 5 and is used for cleaning the ceramic membrane nanofiltration device 3, the cleaning agent is sodium hypochlorite or citric acid, and the concentration of the cleaning agent is 200mg/L.
When the ceramic membrane nanofiltration device is cleaned, the driving direction of the flushing pump is that the water produced by the ceramic micro-ultrafiltration system flows out from the upper part, the water produced by the ceramic micro-ultrafiltration system directly enters the ceramic micro-ultrafiltration membrane filtration system within 5s at the flow rate of 6.0 times of the water inlet flow rate, and the interval time between forward diffusion cleaning is 5hrs. Backwash flushing power is provided by the gas storage tank, backwash water is ceramic nanofiltration membrane produced water, backwash pressure is 0.2MPa, backwash water quantity is 8L, backwash time is 0.2s, and backwash time interval is 0.5h.
The top of the ceramic membrane micro-ultrafiltration device 2 is also provided with a micro-ultrafiltration return port 23, and the top of the ceramic membrane nanofiltration device 3 is also provided with a nanofiltration return port 33. The micro ultrafiltration return port 23 and the nanofiltration return port 33 return to a water inlet pipeline at the upstream of the micro ultrafiltration water inlet 22 together, the concentrated water and the physical cleaning and maintenance chemical cleaning return water of the ceramic micro ultrafiltration device 2, and the concentrated water and the physical cleaning and maintenance chemical cleaning return water of the ceramic nanofiltration device 3 (including cleaning water, vapor-water backwashing water and wastewater generated by filtration of chemical cleaning agents of the first chemical adding container 4 and the second chemical adding container 5) can be at least partially communicated with the micro ultrafiltration water inlet 22 together with the raw water 7 to perform mixed water inlet, wherein the volume proportion of the returned water to the total mixed water inlet can be 1%.
The water inlet pressure of the micro-ultrafiltration water inlet 21 is 0.05MPa, and the concentrated water discharging and flushing water inlet pressure of the micro-ultrafiltration return port 23 at the right upper end is 0.2MPa. And (3) filtering the dead end, closing a concentrated water valve, and refluxing the wastewater to the micro-ultrafiltration inlet 21 through a reflux pump during physical cleaning and maintenance chemical cleaning.
The water inlet pressure of the nanofiltration water inlet 31 is 0.2MPa, and the concentrated water discharging and flushing water inlet pressure of the nanofiltration return port 33 at the upper end is 0.5MPa. The dead end is filtered, the dense water valve is closed, and when the physical cleaning and the maintenance chemical cleaning are carried out, the wastewater flows back to the micro-ultrafiltration inlet 21 through the reflux pump. During cross-flow filtration, the concentrated water valve is opened, and during concentrated water, physical cleaning and maintenance chemical cleaning, the wastewater flows back to the micro-ultrafiltration inlet 21 through the reflux pump.
Example two:
as shown in figure 1, the low-carbon high-efficiency short-flow all-ceramic membrane filtration water treatment device comprises a ceramic membrane micro-ultrafiltration device 2 and a ceramic membrane nanofiltration device 3; the ceramic membrane micro-ultrafiltration device 2 comprises a micro-ultrafiltration water inlet 21 positioned at the bottom and a micro-ultrafiltration water outlet 22 positioned at the top, and the ceramic membrane nano-filtration device comprises a nano-filtration water inlet 31 positioned at the bottom and a nano-filtration water outlet 32 positioned at the top;
wherein, the micro-ultrafiltration water outlet 22 is communicated with the nanofiltration water inlet 31, and the nanofiltration outlet 32 is a water production outlet.
The micro-ultrafiltration water inlet 21 is communicated with a micro-ultrafiltration cleaning device which comprises a first cleaning agent dosing container 4 and a first dosing pump 41, and the first dosing container 4 is communicated with the micro-ultrafiltration water inlet 21 through the first dosing pump 41; the nanofiltration water inlet 31 is communicated with a nanofiltration cleaning device which comprises a second cleaning agent adding container 5, a second dosing pump 51, a scale inhibitor adding container 6 and a third dosing pump 61, the second cleaning agent adding container 5 is communicated with the nanofiltration water inlet 31 through the second dosing pump 51, and the scale inhibitor adding container 6 is communicated with the nanofiltration water inlet 31 through the third dosing pump 61.
The Chinese medicament in the antisludging agent dosing container 6 is an antisludging bactericide/biological dispersant, and is continuously dosed, wherein the dosage is 0.30ppm.
The first medicine adding container 4 pumps chemical cleaning agent into the ceramic membrane micro-ultrafiltration device 2 for cleaning the ceramic membrane micro-ultrafiltration device 2, the cleaning agent is suggested to be sodium hypochlorite, and the cleaning agent concentration is suggested to be 600mg/L.
An ozone water production device 1 is further arranged at the upstream of the first dosing pump 41 for carrying out ozone treatment on inlet water, wherein the ozone water production device 1 can be an ozone generator or an ozone pretreatment device and is positioned at or at the upstream of the micro-ultrafiltration water inlet 21 for carrying out ozone pretreatment before raw water 7 enters the ceramic membrane micro-ultrafiltration device 2 through the micro-ultrafiltration water inlet 21, wherein more preferably, the ozone water production device has the ozone adding amount of 3.5mg/L and ensures that the ozone content in outlet water entering the ozone water production device is more than or equal to 0.5mg/L.
Therefore, when the ceramic membrane micro-ultrafiltration device 2 is cleaned, the ozone water producing device 1 can be further included to directly enter the ceramic micro-ultrafiltration membrane filtering device 2 within 20s at the water inlet flow rate of 4 times, and positive diffusion cleaning is carried out, wherein the interval time of the positive diffusion cleaning is 2 hours.
When the ceramic membrane micro-ultrafiltration device 2 is used for cleaning, the low-carbon high-efficiency short-flow full ceramic membrane filtration water treatment device can further comprise a gas storage tank, backwashing washing power is provided by the gas storage tank, backwashing water is ceramic nanofiltration membrane produced water to form steam-water backwashing, the backwashing water enters the ceramic membrane micro-ultrafiltration device 2 from a water outlet, the backwashing pressure is 0.45MPa, the backwashing water amount is 15L, the backwashing time is 5s, and the backwashing time interval is 5h.
And the second medicine adding container 5 pumps a chemical cleaning agent into the ceramic membrane nanofiltration device 3 for cleaning the ceramic membrane nanofiltration device 3, wherein the cleaning agent is sodium hypochlorite or citric acid, and the concentration of the cleaning agent is 400mg/L.
When the ceramic membrane nanofiltration device is cleaned, the driving direction of the flushing pump is that the water produced by the ceramic micro-ultrafiltration system flows out from the upper part, the water produced by the ceramic micro-ultrafiltration system directly enters the ceramic micro-ultrafiltration membrane filtration system within 10s at 4.0 times of the water inlet flow, and the interval time of forward diffusion cleaning is 2hrs. The backwashing flushing power is provided by the gas storage tank, backwashing water is ceramic nanofiltration membrane produced water, backwashing pressure is 0.5MPa, backwashing water quantity is 22L, backwashing time is 2s, and backwashing time interval is 5h.
The top of the ceramic membrane micro-ultrafiltration device 2 is also provided with a micro-ultrafiltration return port 23, and the top of the ceramic membrane nanofiltration device 3 is also provided with a nanofiltration return port 33. The micro-ultrafiltration return port 23 and the nanofiltration return port 33 return to a water inlet pipeline at the upstream of the micro-ultrafiltration water inlet 22, concentrated water and physical cleaning and maintenance chemical cleaning return water of the ceramic micro-ultrafiltration device 2, and concentrated water and physical cleaning and maintenance chemical cleaning return water of the ceramic nanofiltration device 3 can be at least partially communicated to the micro-ultrafiltration water inlet 22 together with raw water 7 to be mixed for water inlet, wherein the volume proportion of the returned water in the total mixed inlet water can be 1.5%.
The water inlet pressure of the micro-ultrafiltration water inlet 21 is 0.25MPa, and the concentrated water discharge and flushing water inlet pressure of the micro-ultrafiltration return port 23 at the right upper end is 0.4MPa. And (3) filtering the dead end, closing a concentrated water valve, and refluxing the wastewater to the micro-ultrafiltration inlet 21 through a reflux pump during physical cleaning and maintenance chemical cleaning.
The water inlet pressure of the nanofiltration water inlet 31 is 0.5MPa, and the concentrated water discharging and flushing water inlet pressure of the nanofiltration water return port 33 at the upper end is 0.7MPa. The dead end is filtered, the dense water valve is closed, and when the physical cleaning and the maintenance chemical cleaning are carried out, the wastewater flows back to the micro-ultrafiltration inlet 21 through the reflux pump. During cross-flow filtration, the concentrated water valve is opened, and during concentrated water, physical cleaning and maintenance chemical cleaning, the wastewater flows back to the micro-ultrafiltration inlet 21 through the reflux pump.
In the above embodiment of the present application, the outlet water of the ceramic micro-ultrafiltration membrane is directly connected to the ceramic nanofiltration system through a short-flow water pipeline, and the outlet water detection data is as follows: the total hardness of the effluent is between 90 and 110mg/L, the TOC is between 0.6 and 1.2mg/L, and the COD is Mn Is 0.42-0.81mg/L, and the sulfate radical is less than 10mg/L. In the above-mentioned embodiment of this application, supporting complete set pipeline etc. are food level stainless steel, glass, can effectively avoid making the little plastics risk of newly-increased among the water process. Therefore, the method and the device have the advantages of reducing the energy consumption, the medicine consumption, the investment/operation cost and the effluent quality of the systemNo risk of adding micro plastic and the like.
The embodiments of the present invention have been described in detail, but the embodiments are only examples, and the present invention is not limited to the embodiments described above. Any equivalent modifications and substitutions for the present invention are within the scope of the present invention for those skilled in the art. Accordingly, equivalent alterations and modifications are intended to be included within the scope of the present invention, without departing from the spirit and scope of the invention.
Claims (10)
1. A low-carbon high-efficiency short-flow full ceramic membrane filtered water treatment device is characterized by comprising a ceramic membrane micro-ultrafiltration device and a ceramic membrane nanofiltration device; the ceramic membrane micro-ultrafiltration device comprises a micro-ultrafiltration water inlet and a micro-ultrafiltration water outlet, and the ceramic membrane nano-filtration device comprises a nano-filtration water inlet and a nano-filtration water outlet;
wherein, the micro-ultrafiltration water outlet is communicated to the nanofiltration water inlet; the micro-ultrafiltration water inlet is communicated with a micro-ultrafiltration cleaning device which comprises a first cleaning agent dosing container and a first dosing pump, and the first dosing container is communicated with the micro-ultrafiltration water inlet through the first dosing pump; the nanofiltration water inlet is communicated with a nanofiltration cleaning device which comprises a second cleaning agent dosing container, a second dosing pump, a scale inhibitor dosing container and a third dosing pump, the second cleaning agent dosing container is communicated with the nanofiltration water inlet through the second dosing pump, and the scale inhibitor dosing container is communicated with the nanofiltration water inlet through the third dosing pump.
2. The apparatus of claim 1, wherein the all-ceramic membrane filtration water treatment apparatus further comprises an ozone water production apparatus for ozone treatment of the feed water, the ozone water production apparatus performing ozone pretreatment of the feed water at or upstream of the micro-ultrafiltration water inlet.
3. The apparatus of claim 2, wherein the full ceramic membrane filtration water treatment apparatus comprises a water inlet pipe, the water inlet pipe being connected to the micro-ultrafiltration water inlet; the first dosing container is connected to the water inlet pipe through a first dosing pump; the ozone water producing device is positioned at the upstream of the connection point of the first dosing pump and the water inlet pipe.
4. The apparatus of claim 1, wherein the ceramic membrane micro-ultrafiltration device comprises a micro-ultrafiltration return port, the ceramic membrane nanofiltration device comprises a nanofiltration return port, and the nanofiltration return port and the micro-ultrafiltration return port are independent from each other or return to the micro-ultrafiltration water inlet together; the return water of the nanofiltration water return port and the micro-ultrafiltration water return port at least partially flows back to the micro-ultrafiltration water inlet, and the volume ratio of the return water of the nanofiltration water return port and the micro-ultrafiltration water return port in the water entering the micro-ultrafiltration water inlet is preferably 0.1-1.5%.
5. The device according to claim 1, wherein the micro-ultrafiltration cleaning device and the nanofiltration cleaning device further comprise air sources respectively and independently, or the micro-ultrafiltration cleaning device and the nanofiltration cleaning device share the same air source, so as to provide back-flushing power for the micro-ultrafiltration cleaning device and the nanofiltration cleaning device, and form steam-water flushing with back-flushing water.
6. A low-carbon high-efficiency short-flow full ceramic membrane filtration water treatment method is characterized by comprising the following steps:
raw water enters a ceramic membrane micro-ultrafiltration device through a micro-ultrafiltration water inlet to carry out ceramic membrane micro-ultrafiltration;
then, the nano-filtration water enters a ceramic membrane nano-filtration device from a nano-filtration water inlet to carry out ceramic membrane nano-filtration;
the method comprises the following steps of cleaning a ceramic membrane micro-ultrafiltration device, and feeding a first cleaning agent into the ceramic membrane ultra-ultrafiltration device from a micro-ultrafiltration water inlet by a first pump;
the method comprises the following steps of cleaning a ceramic membrane nanofiltration device, conveying a second cleaning agent into the ceramic membrane nanofiltration device from a nanofiltration water inlet by a second medicine feeding pump, and conveying one or more of a scale inhibitor, a bactericide and a biological dispersant into the ceramic membrane nanofiltration device from the nanofiltration water inlet by a third medicine feeding pump.
7. The method as claimed in claim 6, wherein the ozone pretreatment is performed before the raw water enters the ceramic membrane micro-ultrafiltration device through the micro-ultrafiltration water inlet, wherein, more preferably, the ozone water production device has an ozone dosage of 2.5-5.5mg/L and ensures that the ozone content in the effluent entering the ozone water production device is more than or equal to 0.5mg/L.
8. The method according to claim 6, wherein the water inlet pressure of the water inlet of the ceramic membrane micro-ultrafiltration device is 0.01-0.35MPa, the discharge pressure of the return port of the ceramic membrane micro-ultrafiltration device is 0.1-0.45MPa, and the cleaning water inlet pressure of the ceramic membrane micro-ultrafiltration device is 0.1-0.45MPa;
the water inlet pressure of the water inlet of the ceramic membrane nanofiltration device is 0.18-0.85MPa, the discharge pressure of the return port of the ceramic membrane nanofiltration device is 0.25-1.0MPa, and the cleaning water inlet pressure of the ceramic membrane nanofiltration device is 0.25-1.0MPa.
9. The method according to claim 6, wherein before water enters the ceramic membrane nanofiltration device, a third dosing pump doses one or more of a scale inhibitor, a bactericide and a biological dispersant into the water; the dosage is 0.10-0.38ppm.
10. The method of claim 6,
the cleaning of the ceramic membrane nanofiltration device comprises the following steps: water generated by the ozone water generating device is delivered to the ceramic membrane micro-ultrafiltration device through a water inlet of the ceramic membrane micro-ultrafiltration device by a flushing pump, and is delivered to the ceramic membrane micro-ultrafiltration device within 5-30 seconds at the flow rate of 1.5-4.5 times of the water inlet flow rate for forward diffusion cleaning, wherein the forward diffusion cleaning interval time is 2-168 hours; the method also comprises a step of backwashing the ceramic membrane micro-ultrafiltration device, wherein a gas source provides backwashing power, and water used for backwashing is water filtered by the ceramic membrane nanofiltration device; the back washing pressure is 0.15-0.45MPa, the back washing water quantity is 5-20L, the back washing time is 0.5-5 seconds, and the back washing time interval is 0.5-10 hours; the first pump sends the chemical cleaning agent with the concentration of 100-1000mg/L into the water inlet of the ceramic membrane micro-ultrafiltration device;
the cleaning of the ceramic membrane nanofiltration device comprises the following steps: the water produced by the ceramic membrane nanofiltration device directly enters the ceramic membrane nanofiltration device for forward diffusion cleaning within 2-15 seconds at the flow rate of 2.0-6.0 times of the water inlet flow rate, and the forward diffusion cleaning interval time is 0.5-8 hours; the ceramic membrane nanofiltration device is used for backwashing, and water used for backwashing is water filtered by the ceramic membrane nanofiltration device; the back washing pressure is 0.2-0.6MPa, the back washing water quantity is 2-30L, the back washing time is 0.2-3 seconds, and the back washing time interval is 0.5-8 hours; the second pump sends the chemical cleaning agent with the concentration of 100-1000mg/L into the water inlet of the ceramic membrane nanofiltration device.
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