CN1235955A - Purifying technology for aromatic carboxylic acid - Google Patents
Purifying technology for aromatic carboxylic acid Download PDFInfo
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- CN1235955A CN1235955A CN 99113666 CN99113666A CN1235955A CN 1235955 A CN1235955 A CN 1235955A CN 99113666 CN99113666 CN 99113666 CN 99113666 A CN99113666 A CN 99113666A CN 1235955 A CN1235955 A CN 1235955A
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Abstract
Available liquid film process for purifying aromatic carboxylic acid has the demerits of heavy extractant loss and narrow selection range. The present invention greatly improves the purification effect of the said compound through selecting proper hollow fiber film to produce extraction- counter extraction column, utilizing extraction-counter extraction technology to control the pH value of the carboxylic acid mother liquor, and adopting neutral phosphorous extractant, acetate extractant, amine extractant and alkali counter extractant. The present invention uses simple equipment and simple operation process and has low technological cost and high efficiency.
Description
The present invention relates to the purification of aromatic carboxylic acid.
Aromatic series such as benzene series, naphthalene are carboxylic acid, as Whitfield's ointment, 2,3 acid, are the important intermediates of a class.The generation of intermediate in the modern chemistry industrial production, has been played the effect that centralized production, dispersion are used, thereby promoted developing rapidly of industry such as dyestuff, pigment, medicine, agricultural chemicals, to guaranteeing quality product, improve technical level simultaneously, vital role has reduced production costs.The aromatic carboxylic acid intermediate is of many uses, has versatility.On dyestuffs industries, can make substantive dyestuff and matching stain as Whitfield's ointment, on medicine industry, can make acetylsalicylic acid, sodium salicylate etc., also can in foodstuffs industry, make sanitas etc.2,3 acid can be synthesized azoic coupling component, also can be used as pigment and medicine intermediate.Aromatic carboxylic acid purity requirement as medicine intermediate the time is high especially, and its production technique is generally made through technologies such as salify, hydroxylation, neutralization, acid outs by phenol or naphthols, contains small amount of phenol or naphthols inevitably.Phenol, naphthols benzene series corresponding with it, naphthalene are that the carboxylic acid physicochemical property are extremely close, belong to an extremely difficult isolating class system, and successful isolation technique is not arranged at present as yet.
The objective of the invention is to design a kind of efficient height, cost is low, device is simple, the purification techniques of non-secondary pollution.
Adopt membrane extraction-back extraction integration apparatus, select suitable extraction agent and reverse-extraction agent for use, control certain pH condition, realize the purification of aromatic carboxylic acid.
Membrane extraction-back extraction equipment mainly is that three parts are formed: tubular fibre extraction (reextraction) post, the hollow-fibre membrane pencil is closely arranged, and sleeve pipe is arranged outward, and the film inner chamber has a pair of import and export, intermembrane space has a pair of import and export by sleeve pipe, forms film inner chamber and two passages of intermembrane space.Extraction agent circulation device and reverse-extraction agent circulation device.Their following circulation series connection: extraction agent storage tank → column extractor → re-extraction column → extraction agent storage tank; Another circulation is: reverse-extraction agent storage tank → re-extraction column → reverse-extraction agent storage tank.Be that extract flow is through column extractor, extraction liquid flows into the re-extraction column that connects after flowing out column extractor through extraction again, entering column extractor through the arrival of the extraction agent after back extraction extraction agent storage tank again through recycle pump recycles, the extraction agent storage tank is connected an import of column extractor, at any time add extraction agent, reverse-extraction agent storage tank one end is connected with an import of re-extraction column, strip liquor is through after the back extraction, flow out from an outlet of re-extraction column, flow back to the strip liquor storage tank through the re-extraction column outlet, extract gives displacement after reaching finite concentration again in the strip liquor.Another of re-extraction column is import and export that extraction liquid that above-mentioned column extractor comes out enters re-extraction column to import and export.
In the purification process of aromatic carboxylic acid, the control of the pH value of carboxylic acid mother liquor is extremely important, and suitable pH is controlled between this 3.5-8.0, helps refining effect.
Carboxylic acid mother liquor and extraction liquid, extraction liquid and strip liquor all are countercurrent flows in post during extraction, and carboxylic acid mother liquor, extraction liquid, anti-stripping agent are fully contacted, and improve extraction efficiency.
Extraction agent is a neutral phosphorus extractant, as: tributyl phosphate (TBP), trioctyl phosphate (TOP), triphenylphosphate (TPP) etc.; The acetate esters extraction agent is as propyl acetate, butylacetate, n-amyl acetate; Amine extractant, as trioctylamine (TOA), N, N-two (1-methyl-heptyl)-ethanamide (N503), dilaurylamine etc.Also available mixture between them.Reverse-extraction agent is alkali or basic salt, as sodium hydroxide, yellow soda ash etc.
Generally all add proper amount of diluting in extraction agent during extraction, ratio is 50-90%, and thinner of the present invention is that routine is used thinner, and they are kerosene, sulfonated kerosene, toluene, dimethylbenzene, n-Octanol, chloroform or their mixed solution increase mobile to reduce viscosity.
Then effect is better between 4.8-6.0 for above-mentioned carboxylic acid mother liquor pH.
Be hollow fiber film assembly in column extractor and the stripping column, promptly tubular fibre is closely arranged, is fixed, and its import and export are drawn from post.Column extractor and stripping column respectively have two pairs of import and export, be respectively film inner chamber and film outer wall wait to come together the import and export of liquid and extraction liquid or extraction liquid and strip liquor.Communicate between the film inner chamber of two posts, also communicate between the intermembrane space.
During this device work, walk pending liquid in the column extractor in the hollow-fibre membrane, film is walked extraction liquid outward, like this then also be that film is walked from column extractor the extraction liquid that comes outward in the re-extraction column, walk strip liquor in the film, pending liquid is through so circulation, and extract wherein enters in the strip liquor.Also can move towards that opposite approach extracts and back extraction with above-mentioned.Wait in the film to come together liquid and the countercurrent flow of film outer extraction liquid fully contact it, improve extraction efficiency.
The present invention is in order to carry extraction agent and reverse-extraction agent, therefore in the device extraction agent circulation device and reverse-extraction agent circulation device are arranged, it is the control device when extraction liquid enters column extractor in the extraction agent storage tank, they are that recycle pump is arranged when the extraction agent storage tank enters column extractor, valve and tensimeter, the extraction liquid that comes out from stripping column enters the extraction agent storage tank behind under meter and valve; In like manner, the reverse-extraction agent storage tank also has with sampling device one cover.This device is used for carboxylic acid purifies, and as shown in Figure 1, the carboxylic acid mother liquor enters in the membrane fiber from the column extractor lower end, flows out from the upper end; Extraction agent flows into intermembrane space from the upper end, flows out from the lower end to enter re-extraction column, and in like manner, the carboxylic acid mother liquor also needs valve, tensimeter and under meter one covering device into and out of column extractor.
In various types of membrane modules, hollow fiber film assembly can provide maximum membrane area in unit volume.Material requires acidproof, alkaline-resisting, organic solvent-resistant.Alternative mould material has polysulfones (PS), cellulose acetate (CA), polypropylene (PP), polyethylene (PE), polyvinylidene difluoride (PVDF) (PVDF), polypropylene cyanogen (PAN), the length of tubular fibre is 150-1200mm, the best is 400-800mm, and the internal diameter of tubular fibre is 0.15-1.2mm, and the best is 0.3-0.8mm.The hollow-fibre membrane wall thickness is 20-500um, and the best is 40-80um.The tubular fibre micropore size is 0.01-0.8um, and the best is 0.03-0.2um.
Present technique adopts membrane extraction-back extraction integration apparatus, can overcome the problem of conventional extraction plant, also can overcome the deficiency of liquid-film method, has the advantage of himself, is mainly reflected in following several respects: (1) non-secondary pollution.Do not have other pollutents in the purification process and produce, a small amount of phenols in the carboxylic acid can be by being back to production after the back extraction; (2) do not have the dispersion and the agglomeration process of phase, can reduce extraction agent at the entrainment loss of feed liquid in mutually; (3) it is moving not form the liquid-liquid diphasic flow of direct contact, can make the scope of slective extraction agent and the requirement of its rerum natura (as density, viscosity, interfacial tension etc.) is relaxed greatly; (4) two-phase flows respectively in the film both sides, makes process avoid the influence of " back-mixing " and the restriction of " liquid flooding " condition; (5) can bring into play some advantage in the chemical engineering unit operation, improve the mass-transfer efficiency of process, as have huge two-phase contact area, can realize extraction at the same level and reextraction process, adopt the extracted species carrier to promote migration etc.; (6) compare with liquid film technology, feed liquid exists in the film both sides simultaneously with extraction phase, has avoided in the liquid film losing issue of film internal solvent in the breakdown of emulsion operation and immobilized liquid membrane.
Because membrane extraction has above various advantage, make the good separating effect of membrane extraction, easy and simple to handle, be easy to realize industrialization.In the purification process, the carboxylic acid loss is few, and phenol removal efficient is very high, and single-stage extraction efficient can reach more than 90%, and the phenol that reclaims can be back to production.The utility model technical project simple to operation, the extracting-back extraction device that cost is low and efficient is high is to adapt to the needs of purifying industrialization.
Fig. 1 is a using appts synoptic diagram of the present invention.Wherein 1 is column extractor, the 2nd, and re-extraction column, the 3rd, extraction agent storage tank, the 4th, reverse-extraction agent storage tank, the 5th, pending waste liquid import, the 6th, pending waste liquid outlet, the 7th, the extraction agent import of column extractor, the 8th, the outlet of the extraction agent of column extractor, the 9th, re-extraction column wait the liquid import of coming together, the 10th, re-extraction column wait the liquid outlet of coming together, the 11st, the strip liquor import of re-extraction column, the 12nd, the strip liquor outlet of re-extraction column, the 13rd, pump, the 14th, valve, the 15th, tensimeter, the 16th, under meter, the A after the numeral, B, C, D, E, F represent the same accessory of different positions.
Example
Carry out the purification of aromatic carboxylic acid with the utility model technology, can reach good effect, be exemplified below: 1, the removal of beta naphthal impurity in 2,3 acid
Be encapsulated in the ABS plastic cylindrical shell that length is 600mm with 20,000 PP hollow-fibre membranes, make hollow fiber film assembly.Membrane module has two mouths to communicate with hollow fiber cavity up and down, and also there are two mouths the cylindrical shell side.Get two membrane modules, one is column extractor, and another is a re-extraction column.
Making diameter with stainless material is 300mm, highly is the storage tank of the sharp end of 500mm.End has a drain hole under the point, and a side lower part has a discharge port, and middle side part is had a feedback outlet.Get two stainless steel storage tanks, one is the extraction agent storage tank, and another is the reverse-extraction agent storage tank.
With column extractor, re-extraction column, extraction agent storage tank, reverse-extraction agent storage tank are fixed on the stainless steel stent, connect into the extraction agent recycle system and the reverse-extraction agent recycle system with ABS pipe fitting, plastic pump, under meter, valve.As shown in Figure 1.Wherein 1 is column extractor, the 2nd, and re-extraction column, the 3rd, extraction agent storage tank, the 4th, reverse-extraction agent storage tank, the 5th, pending waste liquid import, the 6th, pending waste liquid outlet, the 7th, the extraction agent import of column extractor, the 8th, the outlet of the extraction agent of column extractor, the 9th, re-extraction column wait the liquid import of coming together, the 10th, the waiting of the re-extraction column liquid outlet of coming together, the 11st, the strip liquor import of re-extraction column, the 12nd, the strip liquor outlet of re-extraction column, the 13rd, pump, the 14th, valve, the 15th, tensimeter, the 16th, under meter.
With this technology to chemical plant, Shanghai 2-hydroxyl-3 how in formic acid (2, the 3 acid) production technique removal of beta naphthal impurity carried out pilot scale research.2,3 acid are a kind of important dyestuff, pigment, medicine intermediate.There is a spot of beta naphthal to remain in 2,3 acid products in its production process, is difficult to remove with ordinary method.
In to this production technique, earlier 2,3 acid mother liquor pH values are adjusted between the 5.2-5.8, enter membrane extraction equipment as shown in Figure 1 then.2,3 acid mother liquors pass through from the inside of column extractor one side hollow-fibre membrane, and extraction agent (kerosin of TOA) is in the hollow-fibre membrane outer loop, and the impurity beta naphthal in the mother liquor enters oil phase by film mutually from waste water.The extraction agent circulation enters re-extraction column one side hollow-fibre membrane outside, and reverse-extraction agent (sodium hydroxide solution) is in the hollow-fibre membrane internal recycling, and beta naphthal enters the alkali lye phase by film from oil phase, forms the beta naphthal sodium salt with the sodium hydroxide reaction.In the whole service process, because the beta naphthal of alkali lye in mutually kept lower concentration all the time, the beta naphthal of mother liquor in mutually constantly enters oil phase, enters the alkali lye phase then, generates beta naphthal sodium salt direct reuse in production.This method is reduced to 0.03% with the beta naphthal impurity in 2,3 acid from 0.6%, and removal of impurity reaches 95%.This technology had both improved the purity of 2,3 acid, had reclaimed useful matter (beta naphthal) again, did not produce secondary pollution in the whole purification process.2, the removal of phenol impurity in the Whitfield's ointment
Use 20,000 PP and PS hollow-fibre membrane to be encapsulated in the ABS plastic cylindrical shell that length is 600mm respectively, make column extractor and re-extraction column respectively.And connect into membrane extraction device as shown in Figure 1.With this device Whitfield's ointment is purified.
Whitfield's ointment is a kind of important medicine intermediate.There is a spot of phenol to remain in the Whitfield's ointment product in its production process, is difficult to remove with ordinary method.
In this purifying technique, earlier Whitfield's ointment mother liquor pH value is adjusted between the 5.0-5.8, advance membrane extraction equipment then.The Whitfield's ointment mother liquor passes through from the inside of column extractor one side hollow-fibre membrane, and extraction agent (kerosin of N503) is in the hollow-fibre membrane outer loop, and the impurity phenol in the mother liquor enters oil phase by film mutually from waste water.The extraction agent circulation enters re-extraction column one side hollow-fibre membrane outside, and reverse-extraction agent (sodium carbonate solution) is in the hollow-fibre membrane internal recycling, and phenol enters the alkali lye phase by film from oil phase, forms the phenol sodium salt with the yellow soda ash reaction.In the whole service process, because the phenol of alkali lye in is mutually kept lower concentration all the time, the phenol of mother liquor in mutually constantly enters oil phase, enters the alkali lye phase then, generates phenol sodium salt direct reuse in production.This method is reduced to 0.05% with the phenol impurity in the Whitfield's ointment from 1.2%, and removal of impurity reaches 95%.This technology had both improved salicylic purity, had reclaimed useful matter (phenol) again, did not produce secondary pollution in the whole purification process.3, the removal of phenol impurity in the phenylformic acid
Use 20,000 PE and PS hollow-fibre membrane to be encapsulated in the ABS plastic cylindrical shell that length is 600mm respectively, make column extractor and re-extraction column respectively.And connect into membrane extraction device as shown in Figure 1.The para Toluic Acid purifies with this device.
Phenylformic acid is a kind of important food, medical sanitas.There is a spot of phenol to remain in the phenylformic acid product in its production process, is difficult to remove with ordinary method.
In this purifying technique, earlier Whitfield's ointment mother liquor pH value is adjusted between the 5.5-6.0, advance membrane extraction equipment then.The Whitfield's ointment mother liquor passes through from the inside of column extractor one side hollow-fibre membrane, and extraction agent (the sulfonated kerosene solution of N-BUTYL ACETATE) is in the hollow-fibre membrane outer loop, and the impurity phenol in the mother liquor enters oil phase by film mutually from waste water.The extraction agent circulation enters re-extraction column one side hollow-fibre membrane outside, and reverse-extraction agent (sodium hydroxide solution) is in the hollow-fibre membrane internal recycling, and phenol enters the alkali lye phase by film from oil phase, forms the phenol sodium salt with the sodium hydroxide reaction.In the whole service process, because the phenol of alkali lye in is mutually kept lower concentration all the time, the phenol of mother liquor in mutually constantly enters oil phase, enters the alkali lye phase then, generates phenol sodium salt direct reuse in production.This method is reduced to 5ppm with the phenol impurity in the phenylformic acid from 100ppm, and removal of impurity reaches 95%.This technology had both improved benzoic purity, had reclaimed useful matter (phenol) again, did not produce secondary pollution in the whole purification process.
Claims (6)
1, a kind of purification techniques of aromatic carboxylic acid is by tubular fibre extraction and reextraction device, with extraction and reextraction method purifying aromatic family carboxylic acid, it is characterized in that:
(1) column extractor is connected with re-extraction column, is that the hollow-fibre membrane pencil is closely arranged in the post, and sleeve pipe is arranged outward, is two passages of film inner chamber and intermembrane space in the post, and they have two import and export respectively, and the extraction agent storage tank is connected with column extractor, is connected to the extraction agent storage tank through re-extraction column; The reverse-extraction agent storage tank is connected with re-extraction column and is connected to the reverse-extraction agent storage tank again, and the liquid transmitting power is a recycle pump;
(2) extraction agent is a neutral phosphorus extractant, the acetates extraction agent, amine extractant, strippant is alkali or basic salt, the diluent of extraction agent is conventional thinner, the pH of carboxylic acid mother liquor is 3.5-8.0 during extraction, and carboxylic acid mother liquor and extraction liquid, extraction liquid and anti-stripping agent be countercurrent flow between film inner chamber and intermembrane space respectively.
2, the purification techniques of aromatic carboxylic acid according to claim 1, the pH value 4.8-6.0 of carboxylic acid mother liquor when it is characterized in that extracting.
3, the purification techniques of aromatic carboxylic acid according to claim 1 is characterized in that the intermembrane space of column extractor is communicated with the intermembrane space of stripping column, and the film inner chamber of two posts is communicated with the film inner chamber.
4, the purification techniques of aromatic carboxylic acid according to claim 3 is characterized in that the carboxylic acid mother liquor stream through column extractor film inner chamber, the anti-stripping agent re-extraction column film inner chamber of flowing through.
5, the purification techniques of aromatic carboxylic acid according to claim 1 is characterized in that hollow-fibre membrane length is 150-1200mm, and inner chamber is 0.15-1.2mm, and membranous wall is thick to be 20-500um, and membrane pore size is 0.01-0.8um.
6, the purification techniques of aromatic carboxylic acid according to claim 1 is characterized in that hollow-fibre membrane length is 400-800mm, and inner chamber is 0.3-0.8mm, and membranous wall is thick to be 40-80um, and membrane pore size is 0.03-0.2um.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99113666A CN1086376C (en) | 1999-04-27 | 1999-04-27 | Purifying technology for aromatic carboxylic acid |
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| Application Number | Priority Date | Filing Date | Title |
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| CN99113666A CN1086376C (en) | 1999-04-27 | 1999-04-27 | Purifying technology for aromatic carboxylic acid |
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| CN1086376C CN1086376C (en) | 2002-06-19 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105017003B (en) * | 2014-04-30 | 2017-10-20 | 财团法人工业技术研究院 | Process for purifying organic acids |
| CN115368596A (en) * | 2021-10-22 | 2022-11-22 | 乐凯光电材料有限公司 | Solvent recovery method and application thereof in optical thin film |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU1473160A1 (en) * | 1987-01-20 | 1990-09-23 | Институт Неорганической Химии Ан Латвсср | Apparatus for conducting process of membrane extraction |
| US4891137A (en) * | 1989-03-03 | 1990-01-02 | Spectra-Physics, Inc. | Method and apparatus for membrane extraction of hydrolysis contaminates |
| CN1026232C (en) * | 1991-10-14 | 1994-10-19 | 上海新顺化工厂 | Process for preparing 2-hydroxy-3-naphthoic acid with 99% concentration |
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1999
- 1999-04-27 CN CN99113666A patent/CN1086376C/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105017003B (en) * | 2014-04-30 | 2017-10-20 | 财团法人工业技术研究院 | Process for purifying organic acids |
| CN115368596A (en) * | 2021-10-22 | 2022-11-22 | 乐凯光电材料有限公司 | Solvent recovery method and application thereof in optical thin film |
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| CN1086376C (en) | 2002-06-19 |
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