CN104591999A - Long chain organic acid purifying method - Google Patents

Long chain organic acid purifying method Download PDF

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Publication number
CN104591999A
CN104591999A CN201310529517.5A CN201310529517A CN104591999A CN 104591999 A CN104591999 A CN 104591999A CN 201310529517 A CN201310529517 A CN 201310529517A CN 104591999 A CN104591999 A CN 104591999A
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organic acid
organic
liquid
accordance
ether
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李晓姝
高大成
张霖
师文静
王领民
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China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
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China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
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Priority to CN201310529517.5A priority Critical patent/CN104591999A/en
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/47—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/48—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention discloses a fermentation organic acid purifying method. The method comprises the following steps: 1, carrying out heating inactivation on a fermentation ending liquid; 2, acidifying to crystallize an organic acid in order to obtain an organic acid crystal liquid; 3, mixing the organic acid crystal liquid or a water-containing organic acid filter cake obtained after filtration with an ether organic solvent to dissolve the above organic acid, adding a proper amount of a cationic surfactant, and carrying out organic phase and water phase separation; 4, washing the separated organic phase, adding an adsorbent, and filtering to remove solids; and 5, cooling the organic phase obtained in step 4 to crystallize the organic acid, filtering, and drying to obtain a purified organic acid product. The method uses the ether organic solvent and the cationic surfactant to purify the organic acid, so the process flow is shortened, device, time and energy investment is saved, the polymer grade product with high purity and low total nitrogen content is obtained, and the method is suitable for industrial production.

Description

A kind of method of purification of long chain organic acid
Technical field
The present invention relates to a kind of process for purification of long chain organic acid, from fermented liquid, particularly obtain high purity long chain organic acid method.
Background technology
Long chain organic acid general formula is generally C nh 2n-2o 4, wherein n is 10-18, is that microorganism utilizes the fermentation such as liquid wax and the meta-bolites that obtains.Its fermented liquid is complicated heterogeneous system, secretory product etc. wherein containing unreacted carbon source, microorganism cells and fragment, the substratum do not utilized and meta-bolites and microorganism, especially wherein to grade impurity containing a large amount of protein, pigment and ash, have a strong impact on purity and the application of product, and bring difficulty to this kind organic acid Extractive technology.
At present, very high to this kind organic acid purity requirement on market, particularly the purity requirement of polymerization-grade is higher, general requirement organic acid list acid purity is at more than 98.5wt%, total nitrogen < 30 μ g/g, only has at present and could obtain with organic solvent method purification the polymerization-grade product meeting this and require, and generally, even if purity reaches requirement, its total nitrogen content is still more difficult reaches requirement.
In long-chain biatomic acid process for purification disclosed in CN01142806.6, with long-chain biatomic acid dry powder for raw material, alcohols is used to make solvent treatment long-chain biatomic acid.The diprotic acid of this method first in fermented liquid is first after charcoal absorption, then acidizing crystal, filtration, washing and dry diprotic acid crystalli-zation cake obtain long-chain biatomic acid dry powder, then adopts organic solvent to refine.In the method, the solvent that refining diprotic acid adopts is alcohols, and when heating for dissolving, alcohol easily and diprotic acid generation esterification, causes the reduction of the finished product purity, limits the application in polymerization.The raw material that the method is refined is that moisture filter cake obtains diprotic acid dry powder after drying, raw aqueous quantitative limitation is reduced to the turndown ratio of the method, adds the equipment that thick acid is dry, causes this technical process longer, add production cost.When organic solvent refines diprotic acid, adopt sorbent material generally can reach the requirement of decolouring, but still the more difficult small molecular protein removed wherein, make total nitrogen content undesirable.
In long-chain biatomic acid process for purification disclosed in CN200410018255.7, first pre-treatment is carried out to fermentation method reaction solution, to remove thalline wherein and residual alkane or lipid acid, obtain organic acid clear liquid, then carry out acidizing crystal, acidizing crystal liquid obtains organic acid crude product through filter press again; Finally the crude product obtained refined in high vacuum conditions by wiped film vaporization, short course distillation device or adopt organic solvent to refine.After the diprotic acid crude product that the method obtains and solvent are dissolved, filtration etc. is not taked to remove the operation steps of insoluble impurities, in decrease temperature crystalline process, insoluble impurities must adsorb crystal surface like this, have impact on product purity, brings bad impact to the application of product.And the solvent treatment diprotic acid process in the method, include the solvent recrystallization operation of twice, solvent consumption is larger, add the burden that solvent recuperation is refining, cause operating process comparatively complicated, and the diprotic acid purity adopting solvent method to refine to obtain is the highest only 98.75wt%, produce slightly fluctuate time, just may can not get qualified product.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of method of purification of long chain organic acid.Compared with prior art, the inventive method technique is simple, and energy consumption is low, and supplies consumption is few, and the organic acid purity obtained is high, and the foreign matter content such as small protein and pigment is low, is suitable for suitability for industrialized production.
The method of purification of a kind of long chain organic acid of the present invention, comprising:
I, fermented liquid heat inactivation will be stopped;
II, acidifying make organic acid crystallization separate out, and obtain organic acid crystallization liquid;
III, organic acid filter cake organic acid crystallization liquid or filtration obtained mixes with organic solvent that organic acid is dissolved, described organic solvent to be carbon number be 2 ~ 8 ethers, the cationic surfactant solution that mass concentration is 0.03 ~ 2% is added in above-mentioned system, be preferably 0.05 ~ 1 wt%, the add-on of cationic surfactant solution is 5 ~ 100% of organic acid butt weight, be preferably 10 ~ 50 %, after mixing, carry out organic phase and aqueous phase separation;
After organic phase washed with water after IV, separation, add sorbent material, filtering and removing solid substance;
The organic phase that V, step IV obtain is cooled to organic acid crystallization and separates out, and after filtration, drying obtains the organic acid production refined.
In the inventive method, stopping fermented liquid described in step I is that microorganism utilizes liquid wax to ferment the meta-bolites obtained, and the organic acid molecule general formula wherein contained is C nh 2n-2o 4, wherein n is 10-18, and organic acid can be single a kind of organic acid, also can be mixed organic acid.After stopping fermented liquid heat inactivation, can carry out the impurity such as filtering and removing thalline, filtration can adopt the ordinary methods such as membrane filtration and equipment.Also can in Step II I the impurity such as separation removal thalline.Heat inactivation temperature is generally 75 DEG C ~ 100 DEG C.
In the inventive method, the acidifying described in Step II can adopt ordinary method to carry out.The pH value of described acidifying is 2.0 ~ 4.0, and Heating temperature is 80 ~ 100 DEG C.The above-mentioned acidifying of the present invention acid used can be the H of any concentration 2sO 4, HNO 3, HCl or H 3pO 4.
Step II I organic solvent used is ethers, the carbon number of described ethers is 2 ~ 8, be preferably one or more of ether, propyl ether, isopropyl ether, butyl ether, ethyl isobutyl ether, amyl ether, isoamyl oxide, hexyl ether etc., one or more of more preferably positive propyl ether, isopropyl ether, n-butyl ether, ethyl isobutyl ether, isoamyl oxide etc.
Step II I cats product used is quaternary cationics, preferably four decyl trimethyl ammonium halogenide, cetyltrimethyl ammonium halogenide, dodecyl trimethyl ammonium halogenide, one or more in cetyl pyridinium drone halogenide.
In the inventive method, the weight ratio of organic solvent and organic acid butt is 1:1 ~ 15:1, is preferably 2:1 ~ 7:1.Organic acid crystallization liquid or organic acid filter cake and organic solvent preferably dissolve in a heated condition, and Heating temperature is generally 80 DEG C ~ 150 DEG C, preferably 90 ~ 120 DEG C, concrete according to selecting the boiling point of solvent to determine, generally lower than the boiling temperature of used solvent.
In the inventive method, can add in step IV deionized water wash organic phase once or once more than, and isolate aqueous phase.
In the inventive method, sorbent material in step IV is one or more in gac, atlapulgite etc., and be preferably gac, add-on is the 0.01wt% ~ 2.0wt% of organic acid butt weight, be preferably 0.01wt% ~ 1.0wt%, adsorption time is 30min ~ 60min.
In the inventive method, till in step V, crystallisation by cooling temperature is generally and makes organic acid sufficient crystallising, temperature is generally 10 DEG C ~ 30 DEG C.
In the inventive method, the organic solvent filtrate obtained in step V, can recycle.
The inventive method can obtain the organic acid production of highly purified single kind, also can obtain mixed organic acid product.
Although it is this area ordinary method that organic solvent method refines this kind organic acid, but the optimum solvent used in existing method and best operational path, also purity requires (98.5%) purity a little more than product quality indicator can only be obtained, this is disadvantageous to the stably manufactured of full scale plant, when production is slightly fluctuated, just qualified product may be can not get.The ether solvent that the inventive method adopts and the synergy of cats product can make the small molecules organonitrogen in solvent phase and pigment etc. efficiently be transferred in the aqueous solution, and only use the sorbent material of minute quantity just can obtain purity be greater than 99.5% and total nitrogen be less than the organic acid production of 30 μ g/g.In the art, it has been very difficult that object quality product reaches polymerization-grade index request, purity often improves 0.1 percentage point and total nitrogen to reduce by 1 μ g/g is all very difficult on this basis, and be also all significant and value, this is to the steady running of guarantee full scale plant, improve the aspects such as conforming product rate, having important effect, is also obviously to the quality influence of the polymerization products such as follow-up synthesizing engineering plastic.
The inventive method, while acquisition high purity organic acid production, the advantages such as also have technological process simple, energy consumption is low, and supplies consumption is few.
Embodiment
Process for purification of the present invention is further illustrated below by embodiment.In the present invention, wt% is massfraction.
In the inventive method, containing liquid wax, thalline, the substratum do not utilized, meta-bolites and microorganism secretion thing etc. in fermented liquid, especially wherein containing impurity such as a large amount of protein, pigments.Organic acid crystallization liquid can adopt this area usual method to obtain, as adopted following at least one scheme:
(1) will stop fermented liquid heat and leave standstill, and divide the liquid wax going to upper strata, then cooling also filtration sterilization, obtains filtrate and is acidified with acid to pH2.0 ~ 4.0, and heat simultaneously, obtain organic acid crystallization liquid, or organic acid solution filtration is obtained filter cake;
Actual conditions is: termination fermented liquid is heated 75 DEG C ~ 100 DEG C, leave standstill, then the liquid wax that upper strata is residual is divided, be cooled to 60 DEG C ~ 90 DEG C again, through micro-filtration and/or ultrafiltration apparatus, filtering the impurity such as thalline obtains clear liquid excessively, the clear liquid obtained is added acid for adjusting pH value to 2.0 ~ 4.0, and be heated to 80 DEG C ~ 100 DEG C, obtain organic acid crystallization liquid, or organic acid solution filtration is obtained filter cake.
(2) fermented liquid is heated to 75 DEG C ~ 100 DEG C, and is acidified to pH value 2.0 ~ 4.0, leave standstill, Separation and Recovery liquid wax, obtains organic acid crystallization liquid.
(3) fermented liquid is heated to 75 DEG C ~ 90 DEG C, enters micro-filtration or ultra-filtration equipment, remove thalline and liquid wax etc., the acidification of filtrate obtained to pH value 2.0 ~ 4.0, and is heated to 80 DEG C ~ 100 DEG C, obtains organic acid crystallization liquid, or aqueous solutions of organic acids filtration is obtained filter cake.
Embodiment 1
Get 200ml and obtain C by Candida tropicalis fermentation 12h 22o 4organic acid fermentation liquid, concentration is 160g/l.Be heated to 80 DEG C, use H 2sO 4pH value is adjusted to 3.0, leaves standstill 2h, point liquid wax going solution residual, obtains the C of mycetome 12h 22o 4organic acid crystallization liquid.
The C obtaining mycetome 12h 22o 4organic acid crystallization liquid and positive propyl ether (positive propyl ether and C 12h 22o 4weight ratio is 7:1) mixing, be heated to 80 DEG C, after organic acid dissolves, in mixed solution, add 16 ml massfractions is the cetyltrimethylammonium chloride of 0.05%, after mixing, static 60min, point sub-cloud aqueous phase; In solvent phase, add 30ml deionized water wash organic phase again, again divide phase of anhydrating; Subsequently to adding 0.3g gac insulation decolouring 30min in organic phase, then cross and filter gac, the organic phase after decolouring is cooled to 30 DEG C of crystallizations and obtains C 12h 22o 4organic acid, then drying step obtains product after filtration.Quality product is in table 1.
Embodiment 2
Get 200ml and obtain C by Candida tropicalis fermentation 12h 22o 4organic acid fermentation liquid, concentration is 160g/l.Be heated to 80 DEG C, use H 2sO 4pH value is adjusted to 3.0, leaves standstill 2h, point liquid wax going solution residual, obtains the C of mycetome 12h 22o 4organic acid crystallization liquid.
The C obtaining mycetome 12h 22o 4organic acid crystallization liquid and n-butyl ether (n-butyl ether and C 12h 22o 4weight ratio is 6:1) mixing, be heated to 93 DEG C, after organic acid dissolves, in mixed solution, add 6.4 ml massfractions is the dodecyltrimethyl of 0.1%, after mixing, static 60min, point sub-cloud aqueous phase; In solvent phase, add 50ml deionized water wash organic phase again, again divide phase of anhydrating; In organic phase, add 0.2g gac insulation decolouring 30min, then cross and filter gac, the organic phase after decolouring is cooled to 30 DEG C of crystallizations and obtains C 12h 22o 4organic acid, then drying step obtains product after filtration.Quality product is in table 1.
Embodiment 3
Get 200ml and obtain C by Candida tropicalis fermentation 13h 24o 4organic acid fermentation liquid, concentration is 154g/l.Be heated to 70 DEG C, through ceramic micro filter membrane filtration, the liquid wax removing thalline and remnants obtains filtrate.H is added in filtrate 2sO 4adjust ph to 2.4, and be heated to 95 DEG C, obtain C 13h 24o 4organic acid crystallization liquid, is cooled to room temperature filtration and obtains organic acid filter cake.
The C obtained 13h 24o 4organic acid filter cake and n-butyl ether (n-butyl ether and C 13h 24o 4weight ratio is 2:1) mixing, be heated to 97 DEG C, after organic acid dissolves, in mixed solution, add the four decyl trimethyl ammonium halogenide that 12.5 ml massfractions are 0.3%, after mixing, static 60min, point sub-cloud aqueous phase; In solvent phase, add 60ml deionized water wash organic phase again, again divide phase of anhydrating; Add 0.15g gac insulation decolouring 30min to organic phase, then cross and filter gac, the organic phase after decolouring is cooled to 18 DEG C of crystallizations and obtains C 13h 24o 4organic acid, then drying step obtains product after filtration.Quality product is in table 1.
Embodiment 4
Get the C that 200ml concentration is 145g/l 14h 26o 4organic acid fermentation liquid, is heated to 70 DEG C, and through ceramic micro filter membrane filtration, the liquid wax removing thalline and remnants obtains filtrate.H is added in filtrate 2sO 4adjust ph to 2.4, and be heated to 95 DEG C, obtain C 14h 26o 4organic acid crystallization liquid.
The C obtained 14h 26o 4organic acid crystallization liquid and isopropyl ether (isopropyl ether and C 14h 26o 4weight ratio is 6:1) mixing, be heated to 58 DEG C, after organic acid dissolves, in mixed solution, add cetyl pyridinium drone the halogenide that 9 ml massfractions are 0.5%, after mixing, static 60min, point sub-cloud aqueous phase; In solvent phase, add 30ml deionized water wash organic phase again, again divide phase of anhydrating; In organic phase, add 0.20g gac insulation decolouring 30min, then cross and filter gac, the organic phase after decolouring is cooled to 28 DEG C of crystallizations and obtains C 14h 26o 4organic acid, then drying step obtains product after filtration.Quality product is in table 1.
Embodiment 5
Get the C that 200ml concentration is 165g/l 12h 22o 4organic acid fermentation liquid, is heated to 70 DEG C, and through ceramic micro filter membrane filtration, the liquid wax removing thalline and remnants obtains filtrate.H is added in filtrate 2sO 4adjust ph to 2.4, and be heated to 95 DEG C, obtain C 12h 22o 4organic acid crystallization liquid.
The C obtained 12h 22o 4organic acid crystallization liquid and propyl ether (propyl ether and C 12h 22o 4weight ratio is 5:1) mixing, be heated to 75 DEG C, after organic acid dissolves, in mixed solution, add the dodecyl trimethyl ammonium halogenide that 3.3 ml massfractions are 0.6%, after mixing, static 40min, point sub-cloud aqueous phase; In solvent phase, add 30ml deionized water wash organic phase again, again divide phase of anhydrating; In organic phase, add 0.20g gac insulation decolouring 30min, then cross and filter gac, the organic phase after decolouring is cooled to 28 DEG C of crystallizations and obtains C 12h 22o 4organic acid, then drying step obtains product after filtration.Quality product is in table 1.
Comparative example 1
Isopropyl ether in embodiment 4 is replaced with ethanol, and organic acid crystallization liquid makes organic acid dissolve with ethanol mixing post-heating to 65 DEG C, and all the other are with embodiment 4.Quality product is in table 1.
Comparative example 2
Isopropyl ether in embodiment 4 is replaced with acetone, and organic acid crystallization liquid makes organic acid dissolve with acetone mixing post-heating to 40 DEG C, and all the other are with embodiment 4.Quality product is in table 1.
Comparative example 3
With embodiment 4, just do not add tensio-active agent, quality product is in table 1.
 
Table 1 organic acid production quality

Claims (14)

1. a process for purification for fermentation organic acid, comprising:
I, fermented liquid heat inactivation will be stopped;
II, acidifying make organic acid crystallization separate out, and obtain organic acid crystallization liquid;
III, organic acid filter cake organic acid crystallization liquid or filtration obtained mixes with organic solvent that organic acid is dissolved, described organic solvent to be carbon number be 2 ~ 8 ethers, the cationic surfactant solution that mass concentration is 0.03 ~ 2% is added in above-mentioned system, be preferably 0.05 ~ 1 wt%, the add-on of cationic surfactant solution is 5 ~ 100 % of organic acid butt weight, be preferably 10 ~ 50 %, after mixing, carry out organic phase and aqueous phase separation;
After organic phase washed with water after IV, separation, add sorbent material, filtering and removing solid substance;
The organic phase that V, step IV obtain is cooled to organic acid crystallization and separates out, and after filtration, drying obtains the organic acid production refined.
2. in accordance with the method for claim 1, it is characterized in that described ethers be ether, propyl ether, isopropyl ether, butyl ether, ethyl isobutyl ether, amyl ether, isoamyl oxide, hexyl ether one or more.
3. in accordance with the method for claim 1, it is characterized in that described ethers be positive propyl ether, isopropyl ether, n-butyl ether, ethyl isobutyl ether, isoamyl oxide one or more.
4. in accordance with the method for claim 1, it is characterized in that described cats product is quaternary cationics, preferably four decyl trimethyl ammonium halogenide, cetyltrimethyl ammonium halogenide, dodecyl trimethyl ammonium halogenide, one or more in cetyl pyridinium drone halogenide.
5. in accordance with the method for claim 1, it is characterized in that described organic acid molecule general formula is C nh 2n-2o 4, wherein n is 10-18, and organic acid is single a kind of organic acid or is mixed organic acid.
6. in accordance with the method for claim 1, it is characterized in that step I heat inactivation temperature is 75 DEG C ~ 100 DEG C.
7. in accordance with the method for claim 1, it is characterized in that the pH value of acidifying described in Step II is 2.0 ~ 4.0, Heating temperature is 80 DEG C ~ 100 DEG C, and acidifying acid used is the H of any concentration 2sO 4, HNO 3, HCl or H 3pO 4.
8. in accordance with the method for claim 1, it is characterized in that in Step II I, the weight ratio of organic solvent and organic acid butt is 1:1 ~ 15:1.
9. in accordance with the method for claim 1, it is characterized in that in Step II I, the weight ratio of organic solvent and organic acid butt is 2:1 ~ 7:1.
10. in accordance with the method for claim 1, it is characterized in that in Step II I, organic acid crystallization liquid or organic acid filter cake and organic solvent dissolve in a heated condition, and Heating temperature is 80 DEG C ~ 150 DEG C.
11. in accordance with the method for claim 1, and the sorbent material that it is characterized in that in step IV is one or more in gac, atlapulgite, and add-on is the 0.01wt% ~ 2.0wt% of organic acid butt weight, and adsorption time is 30min ~ 60min.
12. in accordance with the method for claim 1, and the sorbent material add-on that it is characterized in that in step IV is the 0.01wt% ~ 1.0wt% of organic acid butt weight.
13. in accordance with the method for claim 1, it is characterized in that in Step II, and organic acid crystallization liquid adopts following at least one scheme:
(1) termination fermented liquid be heated to 75 DEG C ~ 100 DEG C and leave standstill, dividing the liquid wax going to upper strata, then cooling also filtration sterilization, obtains filtrate and is acidified with acid to pH2.0 ~ 4.0, and be heated to 80 DEG C ~ 100 DEG C simultaneously, obtain organic acid crystallization liquid;
(2) termination fermented liquid is heated to 75 DEG C ~ 100 DEG C, and is acidified to pH value 2.0 ~ 4.0, leave standstill, Separation and Recovery liquid wax, obtains organic acid crystallization liquid;
(3) fermented liquid is heated to 75 DEG C ~ 90 DEG C, enters micro-filtration or ultra-filtration equipment, remove thalline and liquid wax, the acidification of filtrate obtained to pH value 2.0 ~ 4.0, and is heated to 80 DEG C ~ 100 DEG C, obtains organic acid crystallization liquid.
14. in accordance with the method for claim 1, and to it is characterized in that in step V that crystallisation by cooling temperature is for till making organic acid sufficient crystallising, temperature is 10 DEG C ~ 30 DEG C.
CN201310529517.5A 2013-11-01 2013-11-01 Long chain organic acid purifying method Pending CN104591999A (en)

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109485558B (en) * 2017-09-09 2021-02-05 中国石油化工股份有限公司 Purification method of long-chain dibasic acid
CN113429283A (en) * 2021-06-22 2021-09-24 湖北凌晟药业有限公司 Method for recovering phenylacetic acid from medical wastewater
CN113461514A (en) * 2020-03-31 2021-10-01 上海凯赛生物技术股份有限公司 Method for extracting long-chain dicarboxylic acid from fermentation liquor
CN115181020A (en) * 2021-04-02 2022-10-14 上海骆骐化学科技有限公司 Extraction method of long-chain dicarboxylic acid

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5296639A (en) * 1992-12-18 1994-03-22 E. I. Du Pont De Nemours And Company Adipic acid purification
CN101698859A (en) * 2009-09-11 2010-04-28 淄博广通化工有限责任公司 Production method of n-hexadecyl dibasic acid
CN102911036A (en) * 2011-08-01 2013-02-06 中国石油化工股份有限公司 Method for obtaining high pure dicarboxylic acid

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5296639A (en) * 1992-12-18 1994-03-22 E. I. Du Pont De Nemours And Company Adipic acid purification
CN101698859A (en) * 2009-09-11 2010-04-28 淄博广通化工有限责任公司 Production method of n-hexadecyl dibasic acid
CN102911036A (en) * 2011-08-01 2013-02-06 中国石油化工股份有限公司 Method for obtaining high pure dicarboxylic acid

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109485558B (en) * 2017-09-09 2021-02-05 中国石油化工股份有限公司 Purification method of long-chain dibasic acid
CN113461514A (en) * 2020-03-31 2021-10-01 上海凯赛生物技术股份有限公司 Method for extracting long-chain dicarboxylic acid from fermentation liquor
CN115181020A (en) * 2021-04-02 2022-10-14 上海骆骐化学科技有限公司 Extraction method of long-chain dicarboxylic acid
CN113429283A (en) * 2021-06-22 2021-09-24 湖北凌晟药业有限公司 Method for recovering phenylacetic acid from medical wastewater
CN113429283B (en) * 2021-06-22 2022-04-22 湖北凌晟药业有限公司 Method for recovering phenylacetic acid from medical wastewater

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Application publication date: 20150506