CN107890686A - A kind of high performance membrane dilution crystallization method of double unit coupling cycles - Google Patents
A kind of high performance membrane dilution crystallization method of double unit coupling cycles Download PDFInfo
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- CN107890686A CN107890686A CN201711277970.6A CN201711277970A CN107890686A CN 107890686 A CN107890686 A CN 107890686A CN 201711277970 A CN201711277970 A CN 201711277970A CN 107890686 A CN107890686 A CN 107890686A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/005—Selection of auxiliary, e.g. for control of crystallisation nuclei, of crystal growth, of adherence to walls; Arrangements for introduction thereof
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0063—Control or regulation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D2009/0086—Processes or apparatus therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
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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
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/362—Pervaporation
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- Crystallography & Structural Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention provides a kind of high performance membrane dilution crystallization method of double unit coupling cycles, belong to crystallization field of engineering technology.Treat that material liquid is added in material liquid tank, dissolved agent is added in storage tank, after the dissolved that brings into operation agent is recycled to system stabilization, open the peristaltic pump of head tank, making dissolved agent and material liquid, fully contact produces crystal product in membrane module, and the mixed liquor for carrying crystal flows into formation solid and mother liquor after filtration drying device.Mother liquor goes out neat solvent, solute and pure dissolved agent, recycling design solute through osmotic evaporation film components apart, and pure dissolved agent returns in dissolved agent storage tank and carries out secondary use.The addition of dissolved agent is systematically regulated and controled by the control to film and operating condition, and process of pervaporation, efficiency, the feature of environmental protection and the greenization of coupling process are further improved on the premise of preferable crystal product is obtained, cost is reduced, increases the rate of recovery and yield of crystal product.
Description
Technical field
The invention belongs to crystallize field of engineering technology, particularly suitable for the continuous process of dilution crystallization, further increase
Industrialization, high efficiency and the feature of environmental protection of dilution crystallization.New road has been opened up for green crystal industrial expansion.
Background technology
Dilution crystallization is a kind of by adding dissolved agent into solution, and then changes solute solubility in former solvent, so as to
Produce the common separation method of crystal.The process has the advantage of uniqueness, and due to no temperature change, it is special to go for some
The preparation of different product, dilution crystallization are more and more extensive in the application of pharmaceutical industry.With the development of science and technology, various technologies and dissolved
The coupling process of crystallization has also obtained more concerns.Its quality optimization to crystal product has great significance.
With the development of membrane science technology, in numerous coupling process, the dilution crystallization process of film auxiliary is dissolved knot
Brilliant development provides wide space, dilution crystallization process is more added the characteristics of the efficient of membrane technology, energy-saving and environmental protection
Kind, the addition of membrane technology improves crystal product quality while dilution crystallization process control precision is improved.
During dilution crystallization, a certain amount of dissolved agent must be added, crystal product is obtained in order to as much as possible,
Need to add substantial amounts of dissolved agent in the solution.Either traditional dilution crystallization process or new film auxiliary dilution crystallization
Process, the problem of a large amount of dissolved agent recycle all be present.In CN106166400A, CN105753728A and the medicine of correlation
In thing dilution crystallization patent, do not mention the process problem on mixed liquor after filtering, patent CN106430110A,
In the coupling process such as CN107098935A, CN106831337A and CN106946655A, the mixed liquor after filtering is all to pass through steaming
Evaporate, the process desolvation such as rectifying, the agent of recovery dissolved recycle.But traditional rectifying still-process has its intrinsic limitation
Property, and equipment is complicated, power consumption is big, not environmentally, so as to add the industrialized cost of dilution crystallization on the whole, reduces life
Produce efficiency.
It in the industrial processes of dilution crystallization, should consider, only optimize dilution crystallization process, optimization crystallization production
Quality, the technological process without considering follow-up liquid waste processing and entirety is worthless.Inherently improving dissolved knot
On the basis of brilliant process, coupling process is thoroughly improved, the secondary cycle for improving dilution crystallization liquid waste processing and dissolved agent utilizes, right
High efficiency and the greenization for coupling dilution crystallization process are particularly important.
Preliminary use of the membrane science in dilution crystallization has fully demonstrated its huge superiority, and pervaporation is made
It is a kind of efficient organic liquid treatment technology using more and more common, its efficient separating capacity and the extensive scope of application make
It can replace rectifying distillation to complete water-oil separating.The present invention takes full advantage of the advantage of membrane technology, overall to consider under film auxiliary
The coupling process of dilution crystallization, application of membrane is being produced and post-processing two key links, is fundamentally changing dissolved knot
Brilliant circulating system, early stage utilize the regulation and control of operating condition, form homogeneous dissolved agent infiltration, crystal product are produced, after filtering
The mother liquor of formation enters pervaporation membrane module, carries out secondary separation, obtains crystal and dissolved agent again while output solvent
Mixed liquor, obtain the dissolved agent of crystal and high-purity into secondary filter, flow into production system and carry out secondary use.The invention
Coupling dilution crystallization process is greatly simplify, realizes continuous production and green production, reduces dilution crystallization industrialization cost,
Improve production efficiency.
The content of the invention
The present invention proposes a kind of high performance membrane dilution crystallization method of double unit coupling cycles, and two kinds of membrane technologies are used in technology
For core, production section carries out dilution crystallization using film auxiliary, and production membrane module side is crystallization solution, and opposite side is molten
Agent is analysed, obtains ideal crystal by regulating and controlling the operating conditions such as concentration, pressure, temperature, the mother liquor after filtering enters osmotic evaporation film
Component, carry out secondary separation crystallization.Outlet respectively obtains three kinds of neat solvent, pure solute, pure dissolved agent materials, and pure dissolved agent is again
Production system secondary use is flowed into, neat solvent can be recovered.
A kind of system used in high performance membrane dilution crystallization method of double unit coupling cycles, including production membrane module 1, infiltration
Evaporate membrane module 2, filter 3, drying device 4, flowmeter 5, thermometer 6, pressure gauge 7, peristaltic pump 8, valve 9, heat exchanger
10th, material liquid tank 11, dissolved agent storage tank 12 and vavuum pump 13；
Material liquid tank 11 enters the side of production membrane module 1 by peristaltic pump 8 and valve 9, its pipeline be provided with flowmeter 5,
Thermometer 6 and pressure gauge 7, the production membrane module 1 side upper outlet are connected with dissolved agent storage tank 12；Produce the opposite side of membrane module 1
It is connected by valve 9 with filter 3；The port of export connection drying device 4 of filter 3, another port of export pass through preheating
Device 10, peristaltic pump 8 and valve 9 are connected with the side of pervaporation membrane module 2, and its pipeline is provided with thermometer 6 and flowmeter 5, oozes
The right outlet in evaporation membrane module 2 side thoroughly is connected with filter 3 and drying device 4 successively, and is controlled by valve 9；Infiltration is steamed
The hair opposite side of membrane module 2 is connected by pressure gauge 7, condenser 10 with vavuum pump 13；Dissolved agent storage tank 12 passes through peristaltic pump 8 and valve
Door 9 is connected with producing the lower inlet of membrane module 1, and its pipeline is provided with thermometer 6, pressure gauge 7 and flowmeter 5；
Comprise the following steps that：
(1) prepare solution to be crystallized, according under the conditions of certain temperature solute in the solubility of solvent, prepare nearly saturation point
Uniform solution；
(2) solution prepared is added into stable 30min in material liquid tank 11；
(3) dissolved agent is added in dissolved agent storage tank 12；
(4) peristaltic pump 8 of control dissolved agent storage tank 12 is opened, adjusts flow, dissolved agent is flowed through production membrane module 1, it
After flow out, return in dissolved agent storage tank 12, form circulation loop；
(5) after dissolved agent is stable, the peristaltic pump 8 being connected with material liquid tank 11 is opened, makes raw material flow velocity higher than molten
Analyse agent flow velocity；
(6) material liquid contacts with dissolved agent in membrane module 1 is produced, and reaches supersaturation, production by the regulation of operating condition
Raw crystal, mixed liquor carry crystal and obtain solid and mother liquor into filter 3；Solid is dried to obtain crystalline substance into drying device 4
Body product, evacuated pervaporation membrane module 2 is entered by peristaltic pump 8 after the preheated preheating of device 10 of mother liquor, due to mixed
Liquid desolventizing is closed so further crystallization, the solvent of removing enter the condensation recovery of condenser 10, carry the dissolved agent of solute successively
Into filter 3 and drying device 4, crystal product is dried to obtain, the pure dissolved agent being filtrated to get returns to dissolved agent storage tank 12
Middle carry out secondary use；Dissolved dosage in dissolved agent storage tank is detected, is supplemented in good time.
Hollow-fibre membrane or Flat Membrane can be used in described production membrane module 1, organic film can be used, such as：Polytetrafluoroethyl-ne
Alkene (PTFE), Kynoar (PVDF), polyether sulfone (PES), polyvinyl alcohol (PVA), polyacrylic acid (PAA) etc.；Composite membrane, example
Such as：Vinyl alcohol/micro- sodium cellulose, PVA/PAN etc.；Inoranic membrane, such as：Ceramic membrane, zeolite membrane, metal oxide film, molecular sieve
Film etc..
Hollow-fibre membrane or Flat Membrane can be used in described pervaporation membrane module 2, is selected according to different system for handling
Select different films.Preferential water permeable membrane mainly has：(1) non-ionic polyalcohol film, such as：Polyvinyl alcohol (PVA), gather through base methylene
(PHM), methoxymethylated nylon -3 (N-Methoxymethylated Nylon-3), cross-linked poly-methyl methacrylate vinegar
(Poly- (methyl acrylate)) etc..(2) cation type polymer film, such as：Chitosan, polyallyl money chloride
Deng；(3) anionic polymer film, such as：Sulfonated polyethylene, through methylcellulose (CMC), alginic acid etc..
Preferential organic matter film thoroughly has：(1) non-organic silicon polymer, such as：Dimethyl silicone polymer (PDMS), poly- trimethyl
Silicon propine (PTMSP), polyvinyl trimethyl silane (PVTMS) etc.；(2) fluoropolymer, such as：Polytetrafluoroethylene (PTFE)
(PTFE), Kynoar (PVDF), poly- hexafluoro-propylene (PHEP), polysulfonate fluorovinyl ether and teflon-copolymers
(Nafion) etc..
Described heat exchanger is preheater or condenser.
In order to ensure production efficiency and quality, two sets of membrane modules and in-service pipeline are required to fixed time cleaning, and cleaning fluid is pre-
Heat, higher than 5-35 DEG C of operation temperature, using being cleaned in peristaltic pump adition process system, circular flow 30-60min.
Beneficial effects of the present invention：
(1) traditional mother liquor processing method is changed, reduces energy consumption and cost of investment, crystallization production process is more green
Environmental protection；
(2) high efficiency of membrane process, disposing mother liquor reuse ratio is added, reduces dissolved agent and the loss of material liquid,
Crystal yield is added, while can be carried out under process of pervaporation low temperature, has expanded the category of recovery mother liquor；
(3) production efficiency is high, and working condition is content with very little and regulated and controled.Double coupling membrane modules are easy to amplify and reduced.For
The reluctant feed liquid of some conventional procedures has good adaptability, is more widely applied.
The present invention makes full use of the advantage of membrane technology, with reference to auxiliary equipments such as heat exchanger, peristaltic pumps, forms complete double
The high performance membrane dilution crystallization method of unit coupling cycle.Compared to traditional coupling process, production link and mother liquor are post-processed
Link is thoroughly changed, and greatly simplify the process of coupling dilution crystallization, is improving crystal product quality and quantity
On the basis of realize that dissolved agent and the high efficiente callback of solvent utilize, make production process more green.Other pervaporation ring
Crystal product also occurs in section, improves the rate of recovery and yield of solute.Whole production process does not have the discharge of waste liquid waste gas, equipment
Simply, cost investment is few more suitable for new industrialization process.
Brief description of the drawings
Fig. 1 is the high performance membrane dilution crystallization method installation drawing of double unit coupling cycles.
In figure：1 production membrane module；2 pervaporation membrane modules；3 filters；4 drying devices；5 flowmeters；6 thermometers；
7 pressure gauges；8 peristaltic pumps；9 valves；10 heat exchangers (preheating/condensation)；11 material liquid tanks；12 dissolved agent storage tanks；13 vavuum pumps.
Embodiment
Below in conjunction with accompanying drawing and process regimes, embodiment of the invention is further illustrated.
Embodiment 1
Take PES hollow-fibre membranes that production membrane module is made, pervaporation membrane module is made in PVA Flat Membranes.Take 72g NaCl
Add in deionized water, the stable uniform saturated solution being formulated as at 25 DEG C.The crystallization solution prepared is added in head tank,
Stable 30min.Enough ethanol is added into dissolved agent storage tank, opens ethanol storage tank valve, regulation peristaltic pump is 70rpm, makes second
Alcohol flows through production membrane module.After ethanol is stable, the valve of head tank is opened, adjusts peristaltic pump, makes the flow of NaCl solution
For 2 times of ethanol flow, NaCl solution flows into production membrane module, just there is crystal generation, carries the mixed liquor of crystal by filtering
Device output solid and mother liquor, solid form crystal product by drying device, and mother liquor is preheated to 40 DEG C, through peristaltic pump with 2L/h
Flow enter the pervaporation membrane module that pressure is 2KPa, process of pervaporation preferentially sloughs the water in mother liquor, in mother liquor again
Secondary generation NaCl crystal, the side mixed liquor flows into filtering, drying device forms ethanol and a small amount of NaCl crystal, and dissolved agent imports storage
Secondary use is carried out in tank；The vapor of membrane module opposite side forms pure water outflow by 0 DEG C of condenser.
Embodiment 2
Take PES Flat Membranes that production membrane module is made, take PHM hollow-fibre membranes that pervaporation membrane module is made.Take 72g's
NaCl is added in deionized water, the stable uniform saturated solution being formulated as at 25 DEG C, and the crystallization solution prepared is added into raw material
In tank, stable 30min.Sufficient isopropanol is added into dissolved agent storage tank, opens isopropanol storage tank valve, regulation peristaltic pump is
10rpm, isopropanol is set to slowly flow across production membrane module.After isopropanol is stable, the valve of head tank is opened, regulation is wriggled
Pump, the flow of NaCl solution is set to be higher than 10 times of isopropanol, NaCl solution flows into production membrane module, just there is crystal generation, carries brilliant
The mixed liquor of body passes through filter output solid and mother liquor, and solid forms crystal product by drying device, and mother liquor is preheated
Device is preheated to 30 DEG C, enters pressure as 2KPa pervaporation membrane module, process of pervaporation using 1L/h flow through peristaltic pump
The water in mother liquor is preferentially sloughed, NaCl crystal is produced again in mother liquor, the side mixed liquor flows into filtering, drying device forms isopropyl
Alcohol and a small amount of NaCl crystal, dissolved agent import in storage tank and carry out secondary use；The vapor of membrane module opposite side is cold by 0 DEG C
Condenser forms pure water outflow.
Embodiment 3
Take PTFE hollow-fibre membranes that production membrane module is made, take PDMS Flat Membranes that pervaporation membrane module is made.Take 36g third
Olefin(e) acid resin is added in acetone, the stable uniform saturated solution being formulated as at 25 DEG C, and the crystallization solution prepared is added into raw material
In tank, stable 30min.Enough water is added into dissolved agent storage tank, opens water storage tank valve, regulation, which is wriggled, arrives 70rpm, leads to water
Cross production membrane module.After stable, the valve of head tank is opened, peristaltic pump is adjusted, the flow of acrylic resin is higher than water
10 times of flow, material solution flow into production membrane module, just have crystal generation, the mixed liquor for carrying crystal passes through filter output
Solid and mother liquor, solid form crystal product by drying device, and the preheated device of mother liquor is preheated to 50 DEG C, through peristaltic pump with 4L/h
Flow enter the pervaporation membrane module that pressure is 1KPa, process of pervaporation preferentially sloughs the acetone in mother liquor, in mother liquor
Acrylic resin crystal is produced again, and the side mixed liquor flows into filtering, drying device forms pure water and a small amount of acrylic resin is brilliant
Body, pure water import in storage tank and carry out secondary use；The acetone of membrane module opposite side forms neat solvent stream by 0 DEG C of condenser
Go out.
Claims (10)
- A kind of 1. high performance membrane dilution crystallization method of double unit coupling cycles, it is characterised in that described high performance membrane dilution crystallization System used in method, including production membrane module (1), pervaporation membrane module (2), filter (3), drying device (4), stream Gauge (5), thermometer (6), pressure gauge (7), peristaltic pump (8), valve (9), heat exchanger (10), material liquid tank (11), dissolved agent storage Tank (12) and vavuum pump (13)；Material liquid tank (11) enters the side of production membrane module (1) by peristaltic pump (8) and valve (9), and its pipeline is provided with flow (5), thermometer (6) and pressure gauge (7) are counted, production membrane module (1) side upper outlet is connected with dissolved agent storage tank (12)；Produce film The opposite side of component (1) is connected by valve (9) with filter (3)；The port of export connection drying device of filter (3) (4), another port of export is connected by preheater (10), peristaltic pump (8) and valve (9) with pervaporation membrane module (2) side, its Pipeline is provided with thermometer (6) and flowmeter (5), the right outlet in pervaporation membrane module (2) side successively with filter (3) and Drying device (4) connects, and is controlled by valve (9)；Pervaporation membrane module (2) opposite side passes through pressure gauge (7), condenser (10) it is connected with vavuum pump (13)；Dissolved agent storage tank (12) is by peristaltic pump (8) and valve (9) with producing under membrane module (1) Entrance is connected, and its pipeline is provided with thermometer (6), pressure gauge (7) and flowmeter (5)；Comprise the following steps that：(1) prepare solution to be crystallized, according under the conditions of certain temperature solute in the solubility of solvent, prepare the equal of nearly saturation point One solution；(2) solution prepared is added into stable 30min in material liquid tank (11)；(3) dissolved agent is added in dissolved agent storage tank (12)；(4) peristaltic pump (8) of control dissolved agent storage tank (12) is opened, adjusts flow, dissolved agent is flowed through production membrane module (1), Flow out, returned in dissolved agent storage tank (12) afterwards, form circulation loop；(5) after dissolved agent is stable, the peristaltic pump (8) being connected with material liquid tank (11) is opened, makes raw material flow velocity higher than molten Analyse agent flow velocity；(6) material liquid contacts with dissolved agent in production membrane module (1), reaches supersaturation by the regulation of operating condition, produces Crystal, mixed liquor carry crystal and obtain solid and mother liquor into filter (3)；Solid is dried to obtain into drying device (4) Crystal product, evacuated pervaporation membrane module is entered by peristaltic pump (9) after the preheated device of mother liquor (10) preheating (2), due to mixed liquor desolventizing so further crystallization, the solvent of removing enter condenser (10) condensation recovery, carry solute Dissolved agent sequentially enter filter (3) and drying device (4), be dried to obtain crystal product, the pure dissolved agent being filtrated to get Return and secondary use is carried out in dissolved agent storage tank (12)；Dissolved dosage in dissolved agent storage tank is detected, is supplemented in good time.
- 2. the high performance membrane dilution crystallization method of double unit coupling cycles according to claim 1, it is characterised in that described Produce and hollow-fibre membrane or Flat Membrane are used in membrane module (1).
- 3. the high performance membrane dilution crystallization method of double unit coupling cycles according to claim 1 or 2, it is characterised in that institute Organic film, composite membrane or inoranic membrane are used in the production membrane module (1) stated.
- 4. the high performance membrane dilution crystallization method of double unit coupling cycles according to claim 3, it is characterised in that described Organic film is polytetrafluoroethylene (PTFE), Kynoar, polyether sulfone, polyvinyl alcohol or polyacrylic acid；Described composite membrane be vinyl alcohol/ Micro- sodium cellulose, PVA/PAN；Described inoranic membrane is ceramic membrane, zeolite membrane, metal oxide film or molecular screen membrane.
- 5. the high performance membrane dilution crystallization method of double unit coupling cycles according to claim 1,2 or 4, it is characterised in that Hollow-fibre membrane or Flat Membrane are used in described pervaporation membrane module (2), it is different according to different system for handling selections Film.
- 6. the high performance membrane dilution crystallization method of double unit coupling cycles according to claim 3, it is characterised in that described Hollow-fibre membrane or Flat Membrane are used in pervaporation membrane module (2), different films is selected according to different system for handling.
- 7. the high performance membrane dilution crystallization method of double unit coupling cycles according to claim 5, it is characterised in that described Water permeable membrane or saturating organic matter film are used in pervaporation membrane module (2).
- 8. the high performance membrane dilution crystallization method of double unit coupling cycles according to claim 6, it is characterised in that described Water permeable membrane or saturating organic matter film are used in pervaporation membrane module (2).
- 9. the high performance membrane dilution crystallization method of double unit coupling cycles according to claim 7 or 8, it is characterised in that institute The water permeable membrane stated is：(1) non-ionic polyalcohol film, (2) cation type polymer film, (3) anionic polymer film；It is described Saturating organic matter film be：(1) non-organic silicon polymer, (2) fluoropolymer.
- 10. the high performance membrane dilution crystallization method of double unit coupling cycles according to claim 9, it is characterised in that described Heat exchanger (10) be preheater or condenser.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109794078A (en) * | 2019-03-21 | 2019-05-24 | 大连理工大学 | A kind of method and system of the automatic nucleus screening of membrane interface regulation |
| CN109833641A (en) * | 2019-04-04 | 2019-06-04 | 上海电气集团股份有限公司 | A kind of strong brine crystal system and application method |
| CN115259113A (en) * | 2021-04-29 | 2022-11-01 | 浙江蓝天环保高科技股份有限公司 | Method and device for continuously purifying lithium bis (fluorosulfonyl) imide |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106166400A (en) * | 2016-08-05 | 2016-11-30 | 大连理工大学 | A kind of dilution crystallization device and method of film assist control |
| CN106512737A (en) * | 2016-10-27 | 2017-03-22 | 华南理工大学 | Particle controllable preparation method and device based on ultrasonic auxiliary continuous anti-solvent film dialysis process |
| CN106946655A (en) * | 2017-04-17 | 2017-07-14 | 武汉科技大学 | A kind of continuous anti-dissolved membrane crystallization method of antierythrite |
| CN107233744B (en) * | 2017-06-12 | 2019-04-05 | 大连理工大学 | A kind of cooling crystallization method of film auxiliary nucleation |
-
2017
- 2017-12-06 CN CN201711277970.6A patent/CN107890686A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106166400A (en) * | 2016-08-05 | 2016-11-30 | 大连理工大学 | A kind of dilution crystallization device and method of film assist control |
| CN106512737A (en) * | 2016-10-27 | 2017-03-22 | 华南理工大学 | Particle controllable preparation method and device based on ultrasonic auxiliary continuous anti-solvent film dialysis process |
| CN106946655A (en) * | 2017-04-17 | 2017-07-14 | 武汉科技大学 | A kind of continuous anti-dissolved membrane crystallization method of antierythrite |
| CN107233744B (en) * | 2017-06-12 | 2019-04-05 | 大连理工大学 | A kind of cooling crystallization method of film auxiliary nucleation |
Non-Patent Citations (1)
| Title |
|---|
| 刘丽娅: "溶析结晶辅助膜分离技术纯化药用右旋糖酐的研究", 《中国优秀硕士学位论文全文数据库》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109794078A (en) * | 2019-03-21 | 2019-05-24 | 大连理工大学 | A kind of method and system of the automatic nucleus screening of membrane interface regulation |
| CN109833641A (en) * | 2019-04-04 | 2019-06-04 | 上海电气集团股份有限公司 | A kind of strong brine crystal system and application method |
| CN115259113A (en) * | 2021-04-29 | 2022-11-01 | 浙江蓝天环保高科技股份有限公司 | Method and device for continuously purifying lithium bis (fluorosulfonyl) imide |
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