CN1560023A - Process of separating DL-alpha lactamic acid by ion membrane electric dialysis method - Google Patents
Process of separating DL-alpha lactamic acid by ion membrane electric dialysis method Download PDFInfo
- Publication number
- CN1560023A CN1560023A CNA2004100164173A CN200410016417A CN1560023A CN 1560023 A CN1560023 A CN 1560023A CN A2004100164173 A CNA2004100164173 A CN A2004100164173A CN 200410016417 A CN200410016417 A CN 200410016417A CN 1560023 A CN1560023 A CN 1560023A
- Authority
- CN
- China
- Prior art keywords
- membrane
- chamber
- ionic membrane
- exchange membrane
- tripping device
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 35
- 230000008569 process Effects 0.000 title claims abstract description 30
- 239000012528 membrane Substances 0.000 title claims description 84
- 239000002253 acid Substances 0.000 title 1
- 238000000502 dialysis Methods 0.000 title 1
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims abstract description 75
- 235000019270 ammonium chloride Nutrition 0.000 claims abstract description 37
- 238000000909 electrodialysis Methods 0.000 claims abstract description 37
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000000243 solution Substances 0.000 claims abstract description 20
- 239000011259 mixed solution Substances 0.000 claims abstract description 14
- 125000002091 cationic group Chemical group 0.000 claims description 21
- 239000007788 liquid Substances 0.000 claims description 20
- 238000005516 engineering process Methods 0.000 claims description 18
- 239000003011 anion exchange membrane Substances 0.000 claims description 17
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 11
- 150000001413 amino acids Chemical class 0.000 claims description 10
- 150000003839 salts Chemical class 0.000 claims description 8
- 239000003014 ion exchange membrane Substances 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 5
- 230000001476 alcoholic effect Effects 0.000 claims description 3
- 239000007864 aqueous solution Substances 0.000 claims description 3
- 230000005012 migration Effects 0.000 claims description 3
- 238000013508 migration Methods 0.000 claims description 3
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims description 2
- 238000002425 crystallisation Methods 0.000 claims description 2
- 230000008025 crystallization Effects 0.000 claims description 2
- 230000005685 electric field effect Effects 0.000 claims description 2
- 239000012530 fluid Substances 0.000 claims description 2
- 239000000047 product Substances 0.000 abstract description 9
- 150000002500 ions Chemical class 0.000 abstract description 7
- 239000006227 byproduct Substances 0.000 abstract description 3
- QNAYBMKLOCPYGJ-UHFFFAOYSA-N Alanine Chemical compound CC([NH3+])C([O-])=O QNAYBMKLOCPYGJ-UHFFFAOYSA-N 0.000 abstract 6
- -1 NH4+ ions Chemical class 0.000 abstract 1
- 238000005349 anion exchange Methods 0.000 abstract 1
- 238000005341 cation exchange Methods 0.000 abstract 1
- 150000001768 cations Chemical class 0.000 abstract 1
- 230000005684 electric field Effects 0.000 abstract 1
- 231100000331 toxic Toxicity 0.000 abstract 1
- 230000002588 toxic effect Effects 0.000 abstract 1
- 238000002156 mixing Methods 0.000 description 8
- 238000000926 separation method Methods 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 239000013078 crystal Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000010612 desalination reaction Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 208000036142 Viral infection Diseases 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 125000003275 alpha amino acid group Chemical group 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- TWJVNKMWXNTSAP-UHFFFAOYSA-N azanium;hydroxide;hydrochloride Chemical compound [NH4+].O.[Cl-] TWJVNKMWXNTSAP-UHFFFAOYSA-N 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- VKYKSIONXSXAKP-UHFFFAOYSA-N hexamethylenetetramine Chemical compound C1N(C2)CN3CN1CN2C3 VKYKSIONXSXAKP-UHFFFAOYSA-N 0.000 description 1
- 230000008595 infiltration Effects 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Images
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention is an process of separating DL-alpha-alanine by ion film electrodialysis method, and its characteristic: it leads the synthesized DL-alpha-alanine-ammonium chloride mixed solution into an ion film electrodialytic device; it applies cation and anion exchange films to make ion film electrodialytic by arrangement in different sequences, under the action of a DC electric field, NH4+ ions migrate through the ion film exchange films to cathode, but Cl- ions migrate through the ion film exchange films to anode, and they are circularly speared so as to obtain DL-alpha-alanine solution and ammonium chloride solution, respectively, and then it crystallizes and separates out the products of DL-alpha-alanine and ammonium chloride. It can remarkably reduce energy source consumption, need not adopt large amount of combustible toxic methanol, improves product quality, and can obtain high-quality by-product ammonium chloride.
Description
Technical field
The present invention separates DL-α-Bing Ansuan novel process for a kind of in preparation DL-α-Bing Ansuans such as utilizing the α-Lv Bingsuan ammoniation process is produced, its characteristics are to use cationic exchange membrane and anion-exchange membrane, arrange by different order, form ionic membrane electrodialysis tripping device, DL-α-Bing Ansuan and ammonium chloride mixed solution are carried out membrane sepn, relate to technology and operating parameters that the electrodialysis of utilization ionic membrane separates DL-α-Bing Ansuan and ammonium chloride.
Background technology
The DL-α-Bing Ansuan is a kind of important amino acid, be the important source material and the intermediate in fields such as medicine industry, agro-industry, organic synthesis and biochemical research, as foodstuff additive, fodder additives, daily use chemicals auxiliary agent etc., also be widely used in the industries such as food, feed, daily use chemicals.
Existing DL-α-Bing Ansuan is synthetic with separation method to be: with α-Lv Bingsuan, liquefied ammonia (or ammoniacal liquor) is raw material, is catalyzer with the urotropine, synthetic DL-α-Bing Ansuan and the ammonium chloride mixed solution of obtaining in the aqueous solution or alcohol solution or alcoholic solution; Utilize DL-α-Bing Ansuan undissolved characteristics in methyl alcohol, with a large amount of methyl alcohol the DL-α-Bing Ansuan separated to separate out, filter, make with extra care, drying obtains the DL-α-Bing Ansuan.Mother liquor is methyl alcohol and ammonium chloride mixt, reclaims methyl alcohol through rectifying, and the rectifying resistates obtains part through evaporation and is worth very low low-grade ammonium chloride, all the other dischargings.
The shortcoming that separating out alcohol method separates DL-α-Bing Ansuan technology is: 1, a large amount of mother liquors need rectifying to reclaim, and steam consumption is very big, and product per ton needs 9-12 ton steam.2, the methyl alcohol volatilization is big, consumes height, causes production cost to rise.3, use a large amount of inflammable virose methyl alcohol, cause production environment seriously polluted, also increased the production insecurity.4, ammonium chloride concentration height in the mother liquor, corrodibility is strong, rectifying tower requirement for anticorrosion height, investment is big, the maintenance cost height.5, separation yield is low.6, by-product ammonium chloride purity is low, is worth not high.
Summary of the invention
Purpose of the present invention is exactly at above-mentioned all kinds of shortcoming, adopt the ionic membrane electroosmose process that DL-α-Bing Ansuan and ammonium chloride mixed solution are carried out membrane sepn, have at the bar of normal temperature, no phase transformation and mix following realization separating substances and separation yield height, do not produce pollution characteristics.
Ionic membrane electroosmose process of the present invention separates DL-α-Bing Ansuan technology, it is characterized in that synthesizing the DL-α-Bing Ansuan and the ammonium chloride mixed solution that obtain introduces in the ionic membrane electrodialysis tripping device, utilization cationic exchange membrane and anion-exchange membrane, arrange by different order, form the ionic membrane electrodialysis under the DC electric field effect, NH
4 +Move Cl to cathode direction by cationic exchange membrane
-By the migration of anion-exchange membrane anode direction, circulation can obtain DL-α-Bing Ansuan solution and ammonium chloride solution respectively after separating, and DL-α-Bing Ansuan and ammonium chloride product are separated out in crystallization.
The above-mentioned employing in the ionic membrane electrodialysis tripping device, its cationic exchange membrane and anionresin film put in order with difference, form multi-cavity chamber repeated arrangement, and the chamber number can be 2-5.
A kind of priority scheme of ionic membrane electrodialysis tripping device of the present invention is 2 chamber structures, be spaced by cationic exchange membrane and anion-exchange membrane, the chamber that the positive and negative ion-exchange membrane is formed is to mix liquid chamber, anion-exchange membrane is the salt chamber with organizing the cationic exchange membrane composition down, mix liquid chamber near negative electrode, the salt chamber is near anode, can carry out pH value to the DL-α-Bing Ansuan introduced and ammonium chloride mixed solution and be controlled at 5.5-6.5, prevent the partial ionization of DL-α-Bing Ansuan and move escape, see Fig. 1.Make when mixing liquid chamber ammonium chloride and reaching certain little concentration when the ionic membrane electrodialysis separates desalination, can obtain DL-α-Bing Ansuan solution and ammonium chloride solution respectively, separate out DL-α-Bing Ansuan and ammonium chloride product through condensing crystal.
The another kind of priority scheme of ionic membrane electrodialysis tripping device of the present invention is 3 chamber structures, by putting in order of cationic exchange membrane, cationic exchange membrane, anion-exchange membrane, the ionic membrane electrodialysis tripping device of forming 3 chamber repeated arrangement, the chamber that sun, cationic exchange membrane are formed is amino acid feedback chamber, the chamber that the positive and negative ion-exchange membrane is formed is to mix liquid chamber, DL-α-Bing Ansuan and the ammonium chloride mixed solution introduced, anion-exchange membrane is the salt chamber with organizing the cationic exchange membrane composition down.Amino acid feedback chamber is near negative electrode, and the salt chamber is near anode.The DL-α-Bing Ansuan of introducing and the PH of ammonium chloride mixed solution are can be controlled in PH between 2-7, and preferred PH is between the 4.5-6; Amino acid feedback chamber PH can be controlled between the 5-8.5, and preferred PH is between the 6-7.The DL-α-Bing Ansuan has partial ionization in the mixing liquid chamber, and the DL-α-Bing Ansuan that ionization is moved out can enter into amino acid feedback chamber, can turn back to the mixing liquid chamber during to finite concentration, sees Fig. 2.Make when mixing liquid chamber ammonium chloride and reaching certain little concentration when the ionic membrane electrodialysis separates desalination, can obtain DL-α-Bing Ansuan solution and ammonium chloride solution respectively, separate out DL-α-Bing Ansuan and ammonium chloride product through condensing crystal.
Cationic exchange membrane and anion-exchange membrane that described ionic membrane electrodialysis tripping device is selected for use can be heterogeneous membrane or homogeneous membrane.The sum of separate unit electrodialysis tripping device intermediate ion exchange membrane can be in 1200, the size dimension of film is long 100mm-2000mm, wide 100mm-1200mm, the combination of separate unit ionic membrane electrodialysis tripping device can be one section one-level or one section multistage (secondary or more than the secondary), but serial or parallel connection between every grade.
Ionic membrane electroosmose process of the present invention separates DL-α-Bing Ansuan technology, and institute's ionic membrane electrodialysis tripping device that adopts is an ionic membrane electrodialysis tripping device, also available (contain two) more than two and carry out serial or parallel connection make up, with raising throughput.
The significant parameter that should control in operating process comprises current density, liquid flow velocity and temperature in each chamber, pH value.The current density increase helps improving the product segregation rate, but the selection of current density should be taken into account employed ion selective membrane ability to bear and limit current density, greater than limit current density the time, dissociating of water can be taken place, influence current efficiency, general current density should be at 1mA/cm
2-100mA/cm
2In the scope; Each chamber liquid circular flow increases and helps increasing the velocity of flow of liquid in chamber, reduce resistance to mass transfer and polarization phenomena, but liquid flow rate is excessive, easily makes between each chamber pressure equilibrium control improper, causes the pressure reduction infiltration.Therefore general controlled liq speed is in 0.1cm/s~100cm/s scope.Service temperature suitably raising helps accelerating ion migration speed, the ionic membrane electrodialysis process is accelerated, but the selection of service temperature should be considered the ability to bear of the film that uses, and general temperature should be between 5 ℃~100 ℃.
In the described circulating sepn process, the circulation fluid of each chamber is the aqueous solution or alcohol solution or alcoholic solution, and selected alcohol is methyl alcohol or ethanol or Virahol.
Advantage of the present invention:
First: avoided using a large amount of methyl alcohol and the serious methyl alcohol volatile emission that causes is polluted and the production insecurity.Second: the ionic membrane sepn process is no phase transition process, and is lower than the phase transition process power consumption, and ionic membrane electroosmose process separating technology reduces power consumption more than 50% than separating out alcohol method technology.The 3rd; In the ionic membrane tripping device, except that small portions such as fastening piece are made of metal, being various macromolecular materials makes, these insulated with material and erosion resistance are all fine, there is not the such heavy corrosion problem of distillation method, the membrane separation unit long service life, operating maintenance is convenient, invest relatively for a short time, easily realize automatization control.The the 4th: the separation yield height.The 5th: by-product ammonium chloride purity is also high, and the added value height has reduced the three wastes.
Description of drawings
Fig. 1 is the structure iron of the ionic membrane electrodialysis tripping device of 2 chamber structures
Among the figure: CM is a cationic exchange membrane; AM is an anion-exchange membrane; R1 is for mixing liquid chamber; R2 is the salt chamber; RC is a cathode compartment; RA is the anolyte compartment; (+) is anode; (-) is negative electrode.
Fig. 2 is the structure iron of the ionic membrane electrodialysis tripping device of 3 chamber structures
Among the figure: CM is a cationic exchange membrane; AM is an anion-exchange membrane; R1 is for mixing liquid chamber; R2 is the salt chamber; R3 is amino acid feedback chamber; RC is a cathode compartment; RA is the anolyte compartment; (+) is anode; (-) is negative electrode.
Embodiment
Embodiment 1
Referring to Fig. 1, present embodiment is for adopting the ionic membrane electrodialysis tripping device of 2 chamber structures, and membrane area is 150mm * 300mm, 31 pairs of positive and negative ion-exchange membrane 2 chamber repeated arrangement.In operating process, the water mixed liquid of DL-α-Bing Ansuan and ammonium chloride is entered into electrodialysis tripping device chamber R1 after secondary filter, can carry out pH value to the DL-α-Bing Ansuan introduced and ammonium chloride mixed solution and be controlled at 6.The significant parameter current density 10mA/cm that in operating process, should control
2, liquid flow velocity is 3cm/s in each chamber, temperature is 30 ℃.When separating desalination, the ionic membrane electrodialysis makes when mixing liquid chamber ammonium chloride and reaching certain little concentration, can obtain DL-α-Bing Ansuan solution and ammonium chloride solution respectively, separate out DL-α-Bing Ansuan and ammonium chloride product through condensing crystal, DL-α-Bing Ansuan yield is 91.0%
Embodiment 2
Referring to Fig. 2, adopt, the ionic membrane electrodialysis tripping device of 3 chamber structures, the ion-exchange membrane size is 200mm * 400mm, 3 chamber structure repeated arrangement are 100 groups.In operating process, introduce DL-α-Bing Ansuan and ammonium chloride water mixed solution among the electrodialysis tripping device chamber R1, carry out circulation type membrane and separate, actuating current density control 15mA/cm
2, liquid flow velocity is 2.8cm/s in each chamber, temperature is 35 ℃; The DL-α-Bing Ansuan of introducing and the PH of ammonium chloride mixed solution are controlled between the 5-6; Amino acid feedback chamber PH is controlled between the 6-7.5, and the DL-α-Bing Ansuan that ionization is moved out can enter into amino acid feedback chamber, can turn back to the mixing liquid chamber during to finite concentration.Behind circulation membrane sepn 5.5h, obtain DL-α-Bing Ansuan solution and ammonium chloride solution, separate out DL-α-Bing Ansuan and ammonium chloride product through condensing crystal, DL-α-Bing Ansuan yield is 97.5%.
Claims (10)
1, a kind of ionic membrane electroosmose process separates DL-α-Bing Ansuan technology, it is characterized in that synthetic DL-α-Bing Ansuan that obtains and ammonium chloride mixed solution are introduced in the ionic membrane electrodialysis tripping device, and under the DC electric field effect, NH
4 +Move Cl to cathode direction by cationic exchange membrane
-By the migration of anion-exchange membrane anode direction, through behind the circulation membrane sepn of certain hour, obtain DL-α-Bing Ansuan solution and ammonium chloride solution respectively, DL-α-Bing Ansuan and ammonium chloride product are separated out in crystallization.
2, ionic membrane electroosmose process according to claim 1 separates DL-α-Bing Ansuan technology, it is characterized in that described ionic membrane electrodialysis tripping device is by cationic exchange membrane and anion-exchange membrane, put in order as difference, form multi-cavity chamber repeated arrangement, the chamber number can be 2-5.
3, ionic membrane electroosmose process according to claim 1 separates DL-α-Bing Ansuan technology, it is characterized in that described ionic membrane electrodialysis tripping device is spaced by cationic exchange membrane and anion-exchange membrane, the ionic membrane electrodialysis tripping device of forming 2 chamber structures, to the DL-α-Bing Ansuan of introducing and the pH value of ammonium chloride mixed solution, be controlled at 5.5-6.5, preferred PH is 6.
4, ionic membrane electroosmose process according to claim 1 separates DL-α-Bing Ansuan technology, it is characterized in that described ionic membrane electrodialysis tripping device is by cationic exchange membrane, cationic exchange membrane, putting in order of anion-exchange membrane, the ionic membrane electrodialysis tripping device of forming 3 chamber repeated arrangement, sun, the chamber that cationic exchange membrane is formed is amino acid feedback chamber, sun, the chamber that anion-exchange membrane is formed is to mix liquid chamber, anion-exchange membrane is the salt chamber with organizing the cationic exchange membrane composition down, amino acid feedback chamber is near negative electrode, the salt chamber is near anode, the DL-α-Bing Ansuan of introducing and the PH of ammonium chloride mixed solution are can be controlled in PH between 2-7, preferred PH is between the 4.5-6, amino acid feedback chamber PH can be controlled between the 5-8.5, and preferred PH is between the 6-7.
5, ionic membrane electroosmose process according to claim 1 separates DL-α-Bing Ansuan technology, it is characterized in that described ionic membrane electrodialysis tripping device, and selected cationic exchange membrane and anion-exchange membrane are heterogeneous membrane or homogeneous membrane.
6, ionic membrane electroosmose process according to claim 1 separates DL-α-Bing Ansuan technology, the ion-exchange membrane size that it is characterized in that described ionic membrane electrodialysis tripping device is: long 100mm-2000mm, wide 100mm-1200mm, the ion-exchange membrane sum of separate unit ionic membrane electrodialysis tripping device can be in 1200.
7, ionic membrane electroosmose process according to claim 1 separates DL-α-Bing Ansuan technology, it is characterized in that described ionic membrane electrodialysis tripping device, by separate unit ionic membrane electrodialysis tripping device be combined as one section one-level or one section multistage (secondary or more than the secondary), can make serial or parallel connection between every grade.
8, ionic membrane electroosmose process according to claim 1 separates DL-α-Bing Ansuan technology, it is characterized in that adopting platform ionic membrane electrodialysis tripping device, or two above ionic membrane electrodialysis tripping devices carry out the serial or parallel connection combination.
9, separate DL-α-Bing Ansuan technology according to the said ionic membrane electroosmose process of claim 1, it is characterized in that in the described circulating sepn process, galvanic current density is 1mA/cm
2-100mA/cm
2, flow rate of liquid is 0.1cm/s-10cm/s in the chamber, service temperature is 5 ℃-100 ℃.
10, separate DL-α-Bing Ansuan technology according to the said ionic membrane electroosmose process of claim 1, it is characterized in that in the described circulating sepn process, the circulation fluid of each chamber is the aqueous solution or alcohol solution or alcoholic solution, and selected alcohol is methyl alcohol or ethanol or Virahol.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN 200410016417 CN1240670C (en) | 2004-02-16 | 2004-02-16 | Process of separating DL-alpha lactamic acid by ion membrane electric dialysis method |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN 200410016417 CN1240670C (en) | 2004-02-16 | 2004-02-16 | Process of separating DL-alpha lactamic acid by ion membrane electric dialysis method |
Publications (2)
Publication Number | Publication Date |
---|---|
CN1560023A true CN1560023A (en) | 2005-01-05 |
CN1240670C CN1240670C (en) | 2006-02-08 |
Family
ID=34440463
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN 200410016417 Expired - Fee Related CN1240670C (en) | 2004-02-16 | 2004-02-16 | Process of separating DL-alpha lactamic acid by ion membrane electric dialysis method |
Country Status (1)
Country | Link |
---|---|
CN (1) | CN1240670C (en) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101851016A (en) * | 2010-07-07 | 2010-10-06 | 浙江华友钴业股份有限公司 | Method for processing ammonium chloride waste water |
CN106349131A (en) * | 2016-08-26 | 2017-01-25 | 宁夏紫光天化蛋氨酸有限责任公司 | Separation and purification method of methionine |
CN110372496A (en) * | 2019-08-30 | 2019-10-25 | 河南师范大学 | A kind of method of electrodialysis purification neopentyl glycol sodium formate mixed liquor |
CN110746019A (en) * | 2019-09-27 | 2020-02-04 | 杭州蓝然环境技术股份有限公司 | Method for extracting free L-lysine in ammonia water eluent by membrane method |
CN113663517A (en) * | 2021-07-30 | 2021-11-19 | 中国科学技术大学 | Anion rectification system for fine screening of special anions and application thereof |
CN113663518A (en) * | 2021-07-30 | 2021-11-19 | 中国科学技术大学 | Ion cooperative distillation system for fine screening of special mixed ions and application thereof |
-
2004
- 2004-02-16 CN CN 200410016417 patent/CN1240670C/en not_active Expired - Fee Related
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101851016A (en) * | 2010-07-07 | 2010-10-06 | 浙江华友钴业股份有限公司 | Method for processing ammonium chloride waste water |
CN106349131A (en) * | 2016-08-26 | 2017-01-25 | 宁夏紫光天化蛋氨酸有限责任公司 | Separation and purification method of methionine |
CN106349131B (en) * | 2016-08-26 | 2018-04-20 | 宁夏紫光天化蛋氨酸有限责任公司 | A kind of isolation and purification method of methionine |
CN110372496A (en) * | 2019-08-30 | 2019-10-25 | 河南师范大学 | A kind of method of electrodialysis purification neopentyl glycol sodium formate mixed liquor |
CN110746019A (en) * | 2019-09-27 | 2020-02-04 | 杭州蓝然环境技术股份有限公司 | Method for extracting free L-lysine in ammonia water eluent by membrane method |
CN113663517A (en) * | 2021-07-30 | 2021-11-19 | 中国科学技术大学 | Anion rectification system for fine screening of special anions and application thereof |
CN113663518A (en) * | 2021-07-30 | 2021-11-19 | 中国科学技术大学 | Ion cooperative distillation system for fine screening of special mixed ions and application thereof |
Also Published As
Publication number | Publication date |
---|---|
CN1240670C (en) | 2006-02-08 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN104445755B (en) | A kind of method for ammonium chloride waste-water recycling treatment | |
CN109097408B (en) | Preparation method of nylon 56 salt | |
CN100345615C (en) | Electric deionisation method and apparatus for producing superpure water using bipolar membrane | |
US20120253069A1 (en) | Method for separation and purification of long-chain diacids | |
CN102531927A (en) | Method for preparing tetrapropyl ammonium hydroxide by utilizing bipolar membrane electrodialysis | |
CN103787471B (en) | A kind of device and technique processing tosic acid waste liquor of sodium | |
CN108997141A (en) | A kind of preparation method of 1,5- pentanediamine | |
CN110683693A (en) | Method for treating sodium sulfate type wastewater by electrodialysis and reverse osmosis integrated conversion method | |
CN1240670C (en) | Process of separating DL-alpha lactamic acid by ion membrane electric dialysis method | |
CN107973481A (en) | A kind of Treatment and recovery technique for the high salt high-COD waste water that preparing epoxy chloropropane by using glycerol method produces | |
CN102838497B (en) | Cleaning production process of glycine | |
CN109134317B (en) | Method for preparing L-10-camphorsulfonic acid by bipolar membrane electrodialysis | |
Zhong et al. | Sustainable production of lithium acetate by bipolar membrane electrodialysis metathesis | |
Boniardi et al. | Analysis of the sodium lactate concentration process by electrodialysis | |
CN100418905C (en) | Reverse osmosis membrane anti-scaling agent and its preparation method | |
CN1242986C (en) | Technique of ion membrane process for preparing taurine | |
CN103990382A (en) | Method for separating methoxamine from distillation liquid by using electrodialysis | |
CN203699994U (en) | High-salt wastewater electrodialysis device | |
CN111138390B (en) | Improved cleaning process for preparing vitamin C by membrane method | |
CN110272061A (en) | A kind of salt extraction process | |
Xiao et al. | Three-segmented counterflow pilot-scale electrodialysis for ammonia and potassium treatment in liquid anaerobic digestate: A trade-off among advanced ion removal, nutrients concentration limitation, and energy consumption | |
Xia et al. | An innovative beneficial reclamation of flue gas desulfurization brine using bipolar membrane electrodialysis technique | |
TWI639552B (en) | A method of synthesizing homogeneous barium perborate particles by using fluidized-bed crystallization technology | |
Trivedi et al. | Studies on bipolar membranes: Part III: Conversion of sodium phosphate to phosphoric acid and sodium hydroxide | |
CN1196710C (en) | Production of 5'-guanylate disodium. 5'-inosine disodium mixed crystals |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
C06 | Publication | ||
PB01 | Publication | ||
C10 | Entry into substantive examination | ||
SE01 | Entry into force of request for substantive examination | ||
C14 | Grant of patent or utility model | ||
GR01 | Patent grant | ||
C17 | Cessation of patent right | ||
CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20060208 Termination date: 20100216 |