CN202606034U - Continuous nanofiltration concentrating device - Google Patents
Continuous nanofiltration concentrating device Download PDFInfo
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- CN202606034U CN202606034U CN 201220296946 CN201220296946U CN202606034U CN 202606034 U CN202606034 U CN 202606034U CN 201220296946 CN201220296946 CN 201220296946 CN 201220296946 U CN201220296946 U CN 201220296946U CN 202606034 U CN202606034 U CN 202606034U
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Abstract
The utility model provides a continuous nanofiltration concentrating device and belongs to the technical field of nanofiltration devices. The continuous nanofiltration concentrating device comprises a feed pump, a safety filter, a high-pressure pump, a first section membrane stack, a second section membrane stack, a circulating pump, a third section membrane stack, a three-section concentrated solution regulating valve, a three-section concentrated solution flowmeter and a main penetrating fluid flowmeter. The continuous nanofiltration concentrating device has the advantages of being simple and reasonable in structure and low in installed power, and can be widely used in continuous concentration processing of clean materials. By arranging a proper programmable logic controller (PLC), a sensor and an actuator, the continuous nanofiltration concentrating device can achieve automatic operation.
Description
Technical field
The utility model belongs to the nanofiltration device technical field, and a kind of continuous nanofiltration enrichment facility particularly is provided.
Background technology
NF membrane belongs to the pellicle of counter-infiltration category, and its aperture is between counter-infiltration and milipore filter, and it is several to several nanometers to be often referred to zero point.Compare with reverse osmosis membrane; NF membrane has the effect that selectivity is held back to ion, and to organic matter, NF membrane arrives several thousand material to the molecular weight hundreds of; It is fine to hold back effect; Therefore, since the invention NF membrane, obtained fast development in the application of industries such as chemical industry, pharmacy, food and drink, water treatment, environmental protection.The application of NF membrane mainly concentrates on concentrated and separates.
In unit scale and configuration, the NF membrane separator is divided into unit piece system, single hop system and multistratum system.
The unit piece system is minimum nanofiltration system, only comprises a pressure vessel and a membrane component (all pressure vessels and membrane component are claimed membrane stack together).Because this system only adopts a membrane component; And the membrane component concentrated water drainage of single 40 inches long of designing requirements is 5:1 (being equivalent to 18% the rate of recovery approximately) with the minimum of a value of aquifer yield ratio high-volume, and therefore single membrane component system is difficult to reach the higher system rate of recovery.In order to improve the rate of recovery, the more membrane component of can in each pressure vessel, connecting.
Single pressure vessel is together in parallel and arranges just to have become the single hop system.At least comprise two pressure vessels and two membrane components in the single hop system.The membrane component quantity of connecting in single hop system recoveries rate and single the pressure vessel is relevant, generally between 15～50 %.Single original paper system and single hop system adopt the operation of infinite reflux pattern usually, and promptly material comes out from the nanofiltration circulating tank, get into nanofiltration system and carry out once concentration, and concentrate is back to the nanofiltration circulating tank again, so repeatedly, and to reach the cycles of concentration that needs.Adopt the infinite reflux mode to operate, operating cost is higher.
When requiring the system recoveries rate to surpass 50%, should adopt multistratum system.Multistratum system is meant first section dense water as second section water inlet, and second section dense water is as the 3rd section water inlet, by that analogy.Multistratum system can be divided into two kinds from the design of pressure vessel arrangement architecture: a kind of is Christmas tree structure design (Christmas Tree Design), and another kind is recirculation structure design (Recirculation Design).
Christmas tree structure design (Christmas Tree Design): because a water inlet part of every section becomes product water; The flow of inlet water that the back is one section can reduce; In order to guarantee the normal flow of inlet water of every membrane component; So the pressure vessel quantity of back segment is lacked than the pressure vessel quantity of the preceding paragraph, form the inverted pyramid shape and arrange.Concrete arrangement mode is relevant with factors such as single pressure vessel membrane component quantity, material properties (concentration, viscosity etc.), the design rate of recovery.The arrangement mode of common four～six core membrane pressure vessels is 2:1 or 4:2:1.To multistratum system, because membrane component self pressure drop and concentration raise, the hypodynamic phenomenon of clean drive pressure can appear in the back segment system, and it is unbalanced to cause leading portion and rear end to produce water, often need between per two sections, add booster pump, to improve the driving force of back segment.Two sections system recoveries rates of Christmas tree structure design can reach 50～70 %, and three sections system recoveries rates can reach 75～80 %.The Christmas tree structure design advantage is a structure and simple to operate, reduced investment.The system of this structure only needs a high-pressure pump (needing intersegmental booster pump sometimes) and process pipe seldom and control valve usually, and is simple to operation, is convenient to realize automatic control.Its disadvantage is to receive factor affecting such as material properties, the rate of recovery; The feed rate of membrane component is selected can be in too high or too low edge usually; The fluctuation of any point point feed rate all may cause system unstable, and system's once concentration multiple of this arrangement can only reach 4～5 times at most in addition.When system's cycles of concentration was less demanding, the multistratum system of Christmas tree structure design can be realized continued operation; If do not reach the cycles of concentration requirement, also must adopt total reflux operation through once concentration.
Recirculation structure design (Recirculation Design): its maximum is characterised in that every section system all is equipped with a circulating pump, and feed pipe is connected to pump entry, and each section membrane stack outlet conduit also is connected to pump entry simultaneously.Circulating pump and membrane stack, associated conduit form an inner loop circle.The effect of circulating pump provides every needed feed rate of pressure vessel, overcomes mould and falls.The recirculation structure design is generally 2 above circulating ring parallel connections, the pump entry of each circulating ring and membrane stack concentrated solution outlet mounted valve.Its great advantage is that each circulating ring can be distinguished independent operating, through controlling each circulating ring terminal valve, is producing under unbroken situation, realizes cleaning, thereby realizes continuous concentration truly; In addition, owing to adopted inner circulation structure, system recoveries rate can reach very high (can reach more than 95%), and can on a large scale, adjust according to material properties and production needs.Recirculation structure design major defect is that investment and operating cost are high.Under the situation that cycles of concentration and processing speed are confirmed, hop count is few more, and employed membrane component can be many more.Increase hop count, though can reduce membrane component quantity, can increase the quantity of circulating pump simultaneously, installed power improves, and operating cost increases.Influenced by the one-time investment expense, the recirculation structure design is generally used for the bigger system of treatment scale.
Summary of the invention
The purpose of the utility model is to provide a kind of continuous nanofiltration enrichment facility; With few membrane component and the few installed power of trying one's best of trying one's best; Can reach very high cycles of concentration (can reach more than 20 times); It is low to have solved traditional Christmas tree structure design cycles of concentration, recirculation structure design investment and the high problem of operating cost; Realized reduced investment, operating flexibility is big, operating cost is low, applicability is good.
The utility model comprises charging pump 1, security filter 2, high-pressure pump 3, one section membrane stack 4, two-segment film heap 9, circulating pump 13, three sections membrane stacks 14, three sections concentrate control valves 16, three sections concentrated solution discharge meters 17, total permeate flow meter 18.Charging pump 1 is connected with security filter 2; Security filter 2 is connected with high-pressure pump 3, and high-pressure pump 3 is connected with one section membrane stack 4, and one section membrane stack 4 concentration side is connected with two-segment film heap 9; Two-segment film heap 9 is connected with circulating pump 13 inlets; The outlet of the inlet of three sections membrane stacks 14 and concentration side is connected with inlet with the outlet of circulating pump 13 respectively, forms the inner loop circle, and three sections concentrate control valves of three sections membrane stack 14 concentration sides connections 16, three sections concentrate control valves 16 are connected with three sections concentrated solution discharge meters 17; One section outlet of membrane stack 4 per-meate side, two-segment film are piled the outlet of 9 per-meate side and three sections membrane stack 14 per-meate side outlet merging, connect total permeate flow meter 18.
This nanofiltration device is a multistratum system, is generally three sections systems, and wherein latter end adopts inner circulation structure, and former sections are adopted the Christmas tree structure design.This design has combined the advantage of two kinds of traditional design schemes, with less membrane component, realizes the production needs of once concentration to higher cycles of concentration (can reach 10～20 times), has practiced thrift disposable apparatus investment and operating cost.
As further optimization to the utility model, between one section membrane stack 4, two-segment film heap 9, increase an intersegmental booster pump 8, its position is between one section membrane stack 4 concentration side and two-segment film heap 9.
As further optimization to the utility model, between 9, three sections membrane stacks 14 of two-segment film heap, increase an intersegmental booster pump 8, pile between 9 concentration sides and the circulating pump 13 at two-segment film its position.
Increase intersegmental booster pump 8, can improve the operating pressure of each section membrane stack behind the booster pump, improve the operating efficiency of back segment film, thereby effectively reduce membrane component quantity, reduce equipment investment.
As further optimization to the utility model; When between one section membrane stack 4 concentration side and two-segment film heap 9, increasing intersegmental booster pump 8; Between one section membrane stack 4 concentration side and intersegmental booster pump 8, increase by one section concentrating return-flow liquid control valve 6, connect one section phegma flow meter 7 afterwards; Simultaneously; Total permeate flow meter 18 is removed; Connect one section permeate flow meter 5 one section membrane stack 4 per-meate side outlet; Pile the outlet of 9 per-meate side at two-segment film and connect two sections permeate flow meters 10, connect three sections permeate flow meters 15, remerge behind each section of each section penetrating fluid process permeate flow meter at three sections membrane stack 14 side outlets; Remove total permeate flow meter 18.
As further optimization to the utility model; Two-segment film pile between 9 concentration sides and the circulating pump 13 increase intersegmental booster pump 8 in; Pile two sections concentrating return-flow liquid control valves 11 of increase between 9 concentration sides and the intersegmental booster pump 8 at two-segment film, connect two sections phegma flow meters 12 afterwards; Simultaneously; Total permeate flow meter 18 is removed; Connect one section permeate flow meter 5 one section membrane stack 4 per-meate side outlet; Pile the outlet of 9 per-meate side at two-segment film and connect two sections permeate flow meters 10, connect three sections permeate flow meters 15, remerge behind each section of each section penetrating fluid process permeate flow meter at three sections membrane stack 14 side outlets; Remove total permeate flow meter 18.
As further optimization to the utility model; Two-segment film pile between 9 concentration sides and the circulating pump 13 increase intersegmental booster pump 8 in; Between one section membrane stack 4 concentration side and two-segment film heap 9, increase by one section concentrating return-flow liquid control valve 6, connect one section phegma flow meter 7 afterwards; Simultaneously; Total permeate flow meter 18 is removed; Connect one section permeate flow meter 5 one section membrane stack 4 per-meate side outlet; Pile the outlet of 9 per-meate side at two-segment film and connect two sections permeate flow meters 10, connect three sections permeate flow meters 15, remerge behind each section of each section penetrating fluid process permeate flow meter at three sections membrane stack 14 side outlets.
Through above-mentioned optimization; Can reduce the type selecting configuration difficulty of each section membrane stack; The actual motion that can intuitively show simultaneously each section membrane stack situation of exerting oneself, and aperture that can be through regulating one section and two sections phegma control valve and the frequency of high-pressure pump and intersegmental booster pump are regulated the working flow of controlling each section membrane stack.
The beneficial effect of the utility model is: use less membrane component (perhaps less membrane filtration area) and lower installed power, realize the continuous concentration of the material of handling, practice thrift equipment one-time investment expense and operating cost.Simultaneously, this equipment once concentration multiple can be adjustable between 4～20 times (even higher), and applicability is good, and operating flexibility is big.
The utility model is simple and reasonable, and installed power is little, and the continuous concentration that can be widely used in cleaning material is handled.Be equipped with appropriate PLC, sensor and executing agency, can realize automatic operation.
Description of drawings
Fig. 1 is continuous nanofiltration enrichment facility structural representation.
Fig. 2 is a kind of structural representation of continuous nanofiltration enrichment facility with intersegmental booster pump.
Fig. 3 is with the another kind of structural representation of the continuous nanofiltration enrichment facility of intersegmental booster pump.
Fig. 4 is a kind of structural representation of continuous nanofiltration enrichment facility with intersegmental backflow and intersegmental booster pump.
Fig. 5 is with the another kind of structural representation of the continuous nanofiltration enrichment facility of intersegmental backflow and intersegmental booster pump.
Fig. 6 is continuous another structural representation of nanofiltration enrichment facility with intersegmental backflow and intersegmental booster pump.
Fig. 7 is three sections recirculation structure collating unit structural representations of tradition.
Fig. 8 is three sections Christmas tree structure collating unit structural representations of tradition.
Wherein, charging pump 1, security filter 2, high-pressure pump 3, one section membrane stack 4, one section permeate flow meter 5, one section concentrating return-flow liquid control valve 6, one section phegma flow meter 7, intersegmental booster pump 8,9, two sections permeate flow meters of two-segment film heap 10, two sections concentrating return-flow liquid control valves 11, two sections phegma flow meters 12, circulating pump 13, three sections membrane stacks 14, three sections permeate flow meters 15, three sections concentrate control valves 16, three sections concentrated solution discharge meters 17, total permeate flow meter 18.
The specific embodiment
Below in conjunction with accompanying drawing the utility model is done further explanation.
Embodiment 1:
The utility model embodiment 1 comprises charging pump 1, security filter 2,3, one sections membrane stacks 4 of high-pressure pump, two- segment film heap 9,16, three sections concentrated solution discharge meters 17 of 14, three sections concentrate control valves of 13, three sections membrane stacks of circulating pump, total permeate flow meter 18.
Wherein, one section membrane stack, two-segment film heap and three sections membrane stacks are composed in parallel by a pressure vessel or many pressure vessels, load membrane component in the pressure vessel; Membrane component adopts rolling NF membrane element, coiled reverse osmosis membrane element or rolling ultrafiltration membrane elements, and the membrane component specification comprises 8040,4040, and 2540 etc.; Pressure vessel can adopt 8 cun 1-6 cores of fiberglass, stainless steel or other material, 4 cun 1-4 cores, 2.5 cun 1-4 core putaminas.
Material liquid gets into security filter 2 through charging pump 1, and graininess impurity is fallen in interception, after high-pressure pump 3 pressurizations, gets into one section membrane stack 4, carries out preliminary pre-concentration; One section concentrate directly gets into two-segment film heap 9, carries out secondary concentration; Two sections concentrates get into circulating pump 13 as three sections material liquid, get into three sections membrane stacks 14 again, carry out final circulation and concentrate; Three sections concentrates get into subsequent processing and handle through three sections concentrated flowmeter 17 meterings; One section, two sections, three sections penetrating fluids merge after 18 meterings of total permeate flow meter are reclaimed or emission treatment.
More than three sections films adopt cascaded structures, wherein three sections membrane stack 14 concentrated solution outlets are communicated with the inlet of three sections circulating pumps 13, the formation inner loop, thereby guarantee the feed rate of three sections membrane stacks, 14 needs.
Through regulating the aperture of three sections concentrate control valves 16, can be free the cycles of concentration of control system, cycles of concentration calculates through meter readings.
One section is adopted Christmas tree structure to arrange with two-segment film, that is to say that one section membrane stack compares with the two-segment film heap, adopts more pressure vessel.Pressure vessel with 8 cun 6 core is an example, can adopt 2:1 usually, 3:2 (3:1) or 5:3 arrangement modes such as (5:2).Through to the type selecting of charging pump, high-pressure pump with to the calculating of film to arrangement architecture, the feed rate of every pressure vessel when guaranteeing operation.
Three sections inner circulation structures for the band circulating pump through Selection of Cycle Pump, can guarantee the suitable feed rate of three sections pressure vessels.
In the present embodiment 1, per-meate side has adopted a total permeate flow meter, and cost is low, but can not describe the rate of recovery situation of every section film.Can a flowmeter be installed every section film per-meate side outlet, cancel total permeate flow meter, thus, can calculate the rate of recovery of each section film according to each meter readings.
Embodiment 2:
Basic identical with embodiment 1, different is between one section membrane stack 4 concentration side and two-segment film heap 9, has increased intersegmental booster pump 8.
One, increase intersegmental booster pump between two sections after, two sections, three sections operating pressure is improved, thereby improve the operating efficiency of two sections and three sections films, reduction system membranes component population amount perhaps improves the total cycles of concentration of system.
Embodiment 3:
Basic identical with embodiment 2, different is that pile between 9 concentration sides and the circulating pump 13 at two-segment film the position of intersegmental booster pump 8.
Two, increase intersegmental booster pump between three sections after, three sections operating pressure is improved, thereby improve the operating efficiency of three sections films, reduce by three sections membrane component quantity, perhaps improve the total cycles of concentration of system.
Embodiment 4:
Basic identical with embodiment 2; Different is between one section membrane stack 4 concentration side and intersegmental booster pump 8; One section concentrating return-flow liquid control valve 6 and corresponding one section phegma flow meter 7 (one section return line) have been increased; Simultaneously, every section film per-meate side outlet has increased permeate flow meter 5,10,15 respectively, has cancelled total permeate flow meter 18.
One, increase by one section return line between two sections after; One, the type selecting free degree of the arrangement of two-segment film and charging pump, high-pressure pump can increase; Can be through regulating the aperture of one section concentrating return-flow liquid control valve 6; Regulate the feed rate of two-segment film and the seepage discharge of one section film, the operability of system increases greatly.
Embodiment 5:
Basic identical with embodiment 3; Different is to pile between 9 concentration sides and the intersegmental booster pump 8 at two-segment film; Two sections concentrating return-flow liquid control valves 11 and corresponding two sections phegma flow meters 12 (two sections return lines) have been increased; Simultaneously, every section film per-meate side outlet has increased a permeate flow meter 5,10,15 respectively, has cancelled total permeate flow meter 18.
Two, increase by two sections return lines between three sections after, can improve the free degree of lectotype selection.After lectotype selection is confirmed, can be through regulating the aperture of two sections concentrating return-flow liquid control valves 11, adjusting one, the feed rate and of two-segment film, the seepage discharge of two-segment film, the operability of improvement system.
Embodiment 6:
Basic identical with embodiment 5, different is between one section membrane stack 4 concentration side and two-segment film heap 9, has increased by one section concentrating return-flow liquid control valve 6 and corresponding one section phegma flow meter 7 (one section return line).
After increasing by one section return line, can improve the free degree of lectotype selection.After lectotype selection is definite, can be through regulating the aperture of one section concentrating return-flow liquid control valve 7, the seepage discharge of the feed rate and of adjusting one, two-segment film, section film, the operability of improvement system.
Embodiment 7:
System configuration for three sections recirculation arrangements of tradition.
Be equipped with 5 pumps altogether, other embodiment compares with the utility model, and investment obviously increases.
Embodiment 8:
System configuration for three sections Christmas trees arrangements of tradition.
Receive the specification and the operating characteristics influence of high-pressure pump and membrane component, the film device that Christmas tree structure is arranged, the cycles of concentration maximum can reach about 5 times.
Concrete realization approach of the utility model and mode also have a lot, and the above only is the preferred several kinds of embodiments of the utility model.Should be pointed out that for those skilled in the art, under the prerequisite that does not break away from the utility model basic principle, also can make some improvement and modification, these improvement and modification also should be regarded as the protection domain of the utility model.
Claims (6)
1. a continuous nanofiltration enrichment facility is characterized in that: comprise charging pump (1), security filter (2), high-pressure pump (3), one section membrane stack (4), two-segment film heap (9), circulating pump (13), three sections membrane stacks (14), three sections concentrate control valves (16), three sections concentrated solution discharge meters (17), total permeate flow meter (18); Charging pump (1) is connected with security filter (2); Security filter (2) is connected with high-pressure pump (3); High-pressure pump (3) is connected with one section membrane stack (4); One section membrane stack (4) concentration side is connected with two-segment film heap (9), and two-segment film heap 9 is connected with circulating pump (13) inlet, and the inlet of three sections membrane stacks (14) is connected with inlet with the outlet of circulating pump (13) respectively with the concentration side outlet; Form the inner loop circle; Three sections membrane stacks (14) concentration side connects three sections concentrate control valves (16), three sections concentrate control valves (16) are connected with three sections concentrated solution discharge meters (17), and the outlet of one section membrane stack (4) per-meate side, (9) per-meate side outlet of two-segment film heap and three sections membrane stacks (14) side outlet merge, and connect total permeate flow meter (18).
2. continuous nanofiltration enrichment facility according to claim 1 is characterized in that, between one section membrane stack (4), two-segment film heap (9), increases an intersegmental booster pump (8), and its position is between one section membrane stack (4) concentration side and two-segment film heap (9).
3. continuous nanofiltration enrichment facility according to claim 1 is characterized in that, between two-segment film heap (9), three sections membrane stacks (14), increases an intersegmental booster pump (8), and its position is between two-segment film heap (9) concentration side and circulating pump (13).
4. continuous nanofiltration enrichment facility according to claim 1 and 2; It is characterized in that; Increase by one one section concentrating return-flow liquid control valve (6) in the outlet of one section membrane stack (4) concentration side; Connect one section phegma flow meter (7) afterwards, its position is between one section membrane stack (4) concentration side and intersegmental booster pump (8).
5. according to claim 1 or 3 described continuous nanofiltration enrichment facilities; It is characterized in that; Increase by one two sections concentrating return-flow liquid control valves (11) in the outlet of two-segment film heap (9) concentration side and connect two sections phegma flow meters (12) afterwards, its position is between two-segment film heap (9) concentration side and intersegmental booster pump (8).
6. continuous nanofiltration enrichment facility according to claim 5; It is characterized in that; Increase by one one section concentrating return-flow liquid control valve (6) in the outlet of one section membrane stack (4) concentration side; Connect one section phegma flow meter (7) afterwards, its position is between one section membrane stack (4) concentration side and two-segment film heap (9).
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| CN 201220296946 CN202606034U (en) | 2012-06-19 | 2012-06-19 | Continuous nanofiltration concentrating device |
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| CN 201220296946 CN202606034U (en) | 2012-06-19 | 2012-06-19 | Continuous nanofiltration concentrating device |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103910442A (en) * | 2013-01-08 | 2014-07-09 | 株式会社日立制作所 | Fresh water system |
| CN104001423A (en) * | 2014-06-17 | 2014-08-27 | 沈阳新华环境工程有限公司 | Membrane separation device of series connection structure and control method thereof |
| WO2014139116A1 (en) * | 2013-03-14 | 2014-09-18 | General Electric Company | Membrane filtration system with concentrate staging and concentrate recirculation, switchable stages, or both |
| CN108793328A (en) * | 2017-04-26 | 2018-11-13 | 王涛 | A kind of intelligence varying duty film processing system and its application |
| CN109529625A (en) * | 2018-11-28 | 2019-03-29 | 宜宾丝丽雅股份有限公司 | Continuous nanofiltration process for alkali liquor |
| CN109663408A (en) * | 2019-01-11 | 2019-04-23 | 合肥科锐特环保工程有限公司 | Formic acid film reclaimer |
| CN113754137A (en) * | 2021-10-27 | 2021-12-07 | 北京鑫佰利科技发展有限公司 | Brine refining method and device for extracting lithium from salt lake |
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2012
- 2012-06-19 CN CN 201220296946 patent/CN202606034U/en not_active Expired - Lifetime
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103910442A (en) * | 2013-01-08 | 2014-07-09 | 株式会社日立制作所 | Fresh water system |
| WO2014139116A1 (en) * | 2013-03-14 | 2014-09-18 | General Electric Company | Membrane filtration system with concentrate staging and concentrate recirculation, switchable stages, or both |
| CN105026018B (en) * | 2013-03-14 | 2019-10-29 | Bl 科技公司 | Membrane filtration system with concentrate classification and concentrate recycling, convertible grade or both |
| US10532938B2 (en) | 2013-03-14 | 2020-01-14 | Bl Technologies, Inc. | Membrane filtration system with concentrate staging and concentrate recirculation, switchable stages, or both |
| US10995016B2 (en) | 2013-03-14 | 2021-05-04 | Bl Technologies, Inc. | Membrane filtration system with concentrate staging and concentrate recirculation, switchable stages, or both |
| US11027989B2 (en) | 2013-03-14 | 2021-06-08 | Bl Technologies, Inc. | Membrane filtration system with concentrate staging and concentrate recirculation, switchable stages, or both |
| CN104001423A (en) * | 2014-06-17 | 2014-08-27 | 沈阳新华环境工程有限公司 | Membrane separation device of series connection structure and control method thereof |
| CN108793328A (en) * | 2017-04-26 | 2018-11-13 | 王涛 | A kind of intelligence varying duty film processing system and its application |
| CN109529625A (en) * | 2018-11-28 | 2019-03-29 | 宜宾丝丽雅股份有限公司 | Continuous nanofiltration process for alkali liquor |
| CN109663408A (en) * | 2019-01-11 | 2019-04-23 | 合肥科锐特环保工程有限公司 | Formic acid film reclaimer |
| CN113754137A (en) * | 2021-10-27 | 2021-12-07 | 北京鑫佰利科技发展有限公司 | Brine refining method and device for extracting lithium from salt lake |
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Granted publication date: 20121219 |