CN1861569A - Tech. of separating purifying 3,3-dichlorobenzidine hydrochloride - Google Patents
Tech. of separating purifying 3,3-dichlorobenzidine hydrochloride Download PDFInfo
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- CN1861569A CN1861569A CN 200610085497 CN200610085497A CN1861569A CN 1861569 A CN1861569 A CN 1861569A CN 200610085497 CN200610085497 CN 200610085497 CN 200610085497 A CN200610085497 A CN 200610085497A CN 1861569 A CN1861569 A CN 1861569A
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- hydrochloric acid
- dichlorobenzidine hydrochloride
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Abstract
A process for separating and refining 3,3'-dichlorobiphenyl amine hydrochloride includes such steps as mixing 3,3'-dichlorobiphenyl amine hydrochloride with hydrochloric acid, water and arylhydrocarbon for washing and dissolving, oil-water separation, evaporating for removing hydrochloric acid, decoloring, removing impurities, filtering, cooling while crystallizing to educe out 3,3'-dichlorobiphenylamine hydrochloride, filtering, and treating filtered cake.
Description
Technical field
The present invention relates to a kind of Crystallization Separation process for refining, particularly a kind of 3, the separation and purification 3 of 3 '-dichlorobenzidine hydrochloride, hydrochloric acid, water and aromatic hydrocarbons mixture material, 3 '-dichlorobenzidine hydrochloride technology belongs to the fine chemical technology field.
Background technology
3,3 '-dichlorobenzidine (being called for short DCB) hydrochloride (C
12H
10Cl
2N
22HCl), water-soluble slightly, dissolve in alcohol, easily oxidation, more stable in dilute hydrochloric acid solution, be a kind of important pigment, dyestuff intermediate, diarylide yellow, the Wu Erkang fast red of producing with this intermediate, azoic dyestuff is better, strong than the acid resistance of producing with p-diaminodiphenyl, look green.Occupy about 27% of machine pigment total amount with its serial pigment dyestuff that is main body makes, it can also the good substantive dyestuff of processability in addition.Present 3,3 '-dichlorobenzidine hydrochloride adopts 2 usually, translocation reaction takes place with hydrochloric acid and makes in 2 '-dichlorohydrazobenzene (being called for short DHB) in solution such as benzene, toluene or dimethylbenzene, also anhydrochloric consumption in the DHB transposition process, but in the DCB salification process, consumed hydrochloric acid, in the translocation reaction process, in order to improve speed of response and reaction preference, satisfy the requirement of translocation reaction technological process, added excessive hydrochloric acid in the translocation reaction process.Therefore, translocation reaction still has in the material to be about a large amount of hydrochloric acid surpluses after finishing.Present 3, the separation and purification technology of 3 '-dichlorobenzidine reactant salt material is to adopt traditional technology, regulating concentration hydrochloric acid by the moisturizing dilution is 2%～6%, stirs, heats up, material is dissolved at aqueous hydrochloric acid, standing demix, upper strata oil reservoir reclaim benzene, toluene or dimethylbenzene through separation processes such as neutralization, desalinations again.Lower floor's water is 3, and 3 '-dichlorobenzidine hydrochloride aqueous solution is produced 3,3 '-dichlorobenzidine hydrochloride product through unit operations such as decolouring, filtration, crystallizations.Defectives such as this separation and purification processing method has product cost height, seriously polluted, and crystallization cooling is difficult, wastewater flow rate is big, 3, and the loss of 3 '-dichlorobenzidine hydrochloride is more.
Summary of the invention
The objective of the invention is at the deficiencies in the prior art, provide that a kind of yield height, cost are low, the separation and purification 3 of environmental protection, 3 '-dichlorobenzidine hydrochloride technology.
The technical scheme that realizes above-mentioned purpose is: a kind of separation and purification 3, and 3 '-dichlorobenzidine hydrochloride technology, described processing step is as follows:
(1). the washing dissolving, 3, add diluted hydrochloric acid aqueous solution and/or water in 3 '-dichlorobenzidine hydrochloride, hydrochloric acid, water and the aromatic hydrocarbons mixture material, to 3,3 '-dichlorobenzidine hydrochloride washs and dissolves;
(2). oily water separation, upper oil phase is mainly aromatic hydrocarbons, and lower floor's water is mainly 3, and 3 '-dichlorobenzidine hydrochloride, water enter next step operation
(3). the evaporation deacidification, lower floor's water steams hydrochloric acid, and the concentration of hydrochloric acid of control solution is 1.0%～4.0%, 3, and 3 '-dichlorobenzidine hydrochloride concentration is 4.0%～12.0%, makes it become solution;
(4). removal of impurities decolouring, decolour removal of impurities and filtration;
(5). crystallisation by cooling, the filtrate that previous step produces is carried out the adjustment of concentration of hydrochloric acid, adjusting concentration of hydrochloric acid is 4%～8%, crystallisation by cooling separates out 3,3 '-dichlorobenzidine hydrochloride then;
(6). solid-liquid separation, the material filtering with previous step produces carries out Processing of Preparation to filter cake and goes out 3,3 '-dichlorobenzidine hydrochloride product.
Further, described the first step washing dissolving and second relates in the oily water separation, and washing dissolving and oil water separation process can carry out one to three time.
Further, in the described the first step washing dissolving and the second step oily water separation, the diluted hydrochloric acid aqueous solution of adding and/or the temperature of water are 60 ℃～95 ℃.
Further, in described second step oily water separation and the removal of impurities decolouring of the 4th step, the service temperature of control is 80 ℃～95 ℃.
Further, in described the 3rd step evaporation deacidification, the red-tape operati temperature is 80 ℃～100 ℃.
Further, in described the 5th step crystallisation by cooling, filtrate is cooled to 20 ℃～60 ℃.
Further, in the described the first step washing dissolving, aromatic hydrocarbons is benzene, also can be toluene, also can be dimethylbenzene.
Further, described the 4th step removal of impurities decolouring, the removal of impurities discoloring agent is an activated carbon, also can be diatomite, also can be molecular sieve.
Further, the filtrate after described the 6th step solid-liquid separation recycles recyclable utilization after steaming hydrochloric acid under 80 ℃～100 ℃ temperature.
Realize that the main technique equipment that the present invention needs is: dissolution kettle, stirring tank, decolouring stirring tank, crystallization kettle, pressure filter, in and still etc.
Adopt the benefit of technique scheme to be: (1), product yield height, quality is good.The present invention utilizes 3,3 '-dichlorobenzidine hydrochloride dissolubility difference in different concns hydrochloric acid is big with 3,3 '-dichlorobenzidine hydrochloride more stable characteristics in dilute hydrochloric acid, adopt concentration of hydrochloric acid and the parallel method of heating and cooling of regulating, and utilize the volatile and characteristic that easily absorbed of hydrochloric acid by water, to 3,3 '-dichlorobenzidine hydrochloride carries out separation and purification, is 1%～3% o'clock as the control concentration of hydrochloric acid, and 3,3 '-dichlorobenzidine hydrochloride solubleness maximum, can improve throughput and production efficiency, be 4%～6% o'clock as the control concentration of hydrochloric acid, crystallisation by cooling, thereby improved separation and purification 3, the yield of 3 '-dichlorobenzidine hydrochloride product; (2), cost is low.Operational path of the present invention is short, and the material in the technology, energy etc. can both effectively utilize, can recycled as crystalline mother solution of the present invention, and this has significantly reduced wastewater treatment capacity and 3, the loss of 3 '-dichlorobenzidine hydrochloride and hydrochloric acid.These have all reduced cost widely, have avoided the waste of resource; (3), environmental protection, the present invention is provided with in the alkali lye and waits the waste water aftertreatment technology, greatly reduces pollution, very environmental protection is a kind of process for cleanly preparing.In a word; the present invention overcome in the existing technology that the crystallization cooling is difficult, wastewater flow rate is big, 3, defective such as the loss of 3 '-dichlorobenzidine hydrochloride is more is a kind of new separation and purification technology; being a technology that applicability is very strong, is a kind of technology that is suitable for industrially scalable production.
Description of drawings
Accompanying drawing is a process flow sheet of the present invention.
Embodiment
The present invention is further detailed explanation below in conjunction with drawings and Examples.
Main technique equipment is: washing dissolution kettle, decolouring still, crystallization kettle, evaporation deacidification still, filter, in and still etc.
Embodiment one
A kind of separation and purification 3,3 '-dichlorobenzidine hydrochloride technology, described processing step is as follows:
(1). washing dissolving and oily water separation, with 3,3 '-dichlorobenzidine hydrochloride, hydrochloric acid, water and toluene mixture material material add in the washing dissolution kettle, feed a certain amount of 90 ℃ of hot water and fully stirring, make 3,3 '-dichlorobenzidine hydrochloride is partly dissolved, under 80 ℃～95 ℃ temperature, standing separation then, isolating water layer continues to add 90 ℃ of hot water, standing separation again through pumping into the decolouring still in the oil reservoir of remainder under agitation condition, isolating water layer pumps into the decolouring still, and remaining oil reservoir can adopt intensification distillatory method to carry out toluene and reclaim.
(2). evaporation deacidification and removal of impurities decolouring, in the decolouring still, intensification is also stirred, under reduced pressure, temperature steams hydrochloric acid between 80 ℃～100 ℃, and the concentration of hydrochloric acid of control solution is 1.5%～2.5%, 3,3 '-dichlorobenzidine hydrochloride concentration is 6.0%～10.0%, make water become solution, add a certain amount of activated carbon, keeping the feed liquid temperature is 90 ℃～95 ℃, under agitation condition, the removal of impurities of decolouring, filtered while hot, filtrate pumps into crystallization kettle.
(3). crystallisation by cooling and solid-liquid separation, in crystallization kettle, add a certain amount of 32% technical hydrochloric acid, adjusting concentration of hydrochloric acid is 5%～6%, be cooled to 35 ℃, 3, the crystallization of 3 '-dichlorobenzidine hydrochloride is separated out, and filtration, filter cake go out 3 through conventional Processing of Preparation, 3 '-dichlorobenzidine hydrochloride finished product, filtrate pump into evaporation deacidification still.
(4). filtrate evaporation deacidification, in evaporation deacidification still, intensification is also stirred, and under reduced pressure, temperature steams hydrochloric acid between 80～100 ℃, and the concentration of hydrochloric acid of control solution is about 1.0%, and filtrate pumps into the dilute hydrochloric acid medial launder and prepares to use.
Embodiment two
A kind of separation and purification 3,3 '-dichlorobenzidine hydrochloride technology, described processing step is as follows:
(1). washing dissolving and oily water separation, with 3,3 '-dichlorobenzidine hydrochloride, hydrochloric acid, water and toluene mixture material material add in the washing dissolution kettle, feed dilute hydrochloric acid medial launder preparation dilute hydrochloric acid solution among a certain amount of 90 ℃ embodiment one, and fully stir, make 3,3 '-dichlorobenzidine hydrochloride is partly dissolved, under 80 ℃～95 ℃ temperature, standing separation then, isolating water layer is through pumping into the decolouring still, continuation adds 90 ℃ of dilute hydrochloric acid solutions in the oil reservoir of remainder, standing separation again, isolating water layer pumps into the decolouring still, and remaining oil reservoir can adopt intensification distillatory method to carry out toluene and reclaim.
(2). evaporation deacidification and removal of impurities decolouring, in the decolouring still, intensification is also stirred, under reduced pressure, temperature steams hydrochloric acid between 80 ℃～100 ℃, and the concentration of hydrochloric acid of control solution is 1.5%～2.5%, 3,3 '-dichlorobenzidine hydrochloride concentration is 6.0%～10.0%, make water become solution, add a certain amount of activated carbon, keeping the feed liquid temperature is 90 ℃～95 ℃, under agitation condition, the removal of impurities of decolouring, filtered while hot, filtrate pumps into crystallization kettle.
(3). crystallisation by cooling and solid-liquid separation, in crystallization kettle, add a certain amount of 32% technical hydrochloric acid, adjusting concentration of hydrochloric acid is 5%～6%, be cooled to 35 ℃, 3, the crystallization of 3 '-dichlorobenzidine hydrochloride is separated out, and filtration, filter cake go out 3 through conventional Processing of Preparation, 3 '-dichlorobenzidine hydrochloride finished product, filtrate pump into evaporation deacidification still.
(4). filtrate evaporation deacidification, in evaporation deacidification still, intensification is also stirred, and under reduced pressure, temperature steams hydrochloric acid between 80 ℃～100 ℃, and the concentration of hydrochloric acid of control solution is about 1.0%, and filtrate pumps into the dilute hydrochloric acid medial launder and prepares to use.
Embodiment three
A kind of separation and purification 3,3 '-dichlorobenzidine hydrochloride technology, described processing step is as follows:
(1). washing dissolving and oily water separation, with 3,3 '-dichlorobenzidine hydrochloride, hydrochloric acid, water and toluene mixture material material add in the washing dissolution kettle, feed dilute hydrochloric acid medial launder preparation dilute hydrochloric acid solution among a certain amount of 90 ℃ embodiment two, and fully stir, make 3,3 '-dichlorobenzidine hydrochloride is partly dissolved, under 80 ℃～95 ℃ temperature, standing separation then, isolating water layer is through pumping into the decolouring still, continuation adds 90 ℃ of dilute hydrochloric acid solutions in the oil reservoir of remainder, standing separation again, isolating water layer pumps into the decolouring still, and remaining oil reservoir can adopt intensification distillatory method to carry out toluene and reclaim.
(2). evaporation deacidification and removal of impurities decolouring, in the decolouring still, intensification is also stirred, under reduced pressure, temperature steams hydrochloric acid between 80 ℃～100 ℃, and the concentration of hydrochloric acid of control solution is 1.5%～2.5%, 3,3 '-dichlorobenzidine hydrochloride concentration is 6.0%～10.0%, make water become solution, add a certain amount of molecular sieve, keeping the feed liquid temperature is 90 ℃～95 ℃, under agitation condition, the removal of impurities of decolouring, filtered while hot, filtrate pumps into crystallization kettle.
(3). crystallisation by cooling and solid-liquid separation, in crystallization kettle, add the recovery hydrochloric acid among a certain amount of embodiment two, adjusting concentration of hydrochloric acid is 5%～6%, be cooled to 20 ℃, 3, the crystallization of 3 '-dichlorobenzidine hydrochloride is separated out, and filtration, filter cake go out 3 through conventional Processing of Preparation, 3 '-dichlorobenzidine hydrochloride finished product, filtrate pump into evaporation deacidification still.
(4). filtrate evaporation deacidification, in evaporation deacidification still, heat up and also stir, under reduced pressure, temperature steams hydrochloric acid between 80 ℃～100 ℃, and the concentration of hydrochloric acid of control solution is about 1.0%, during filtrate pumps into and still.
(5). wastewater treatment, in and still add a certain amount of CaCO
3In and hydrochloric acid, cooling, filtration, filter cake reclaims 3,3 '-dichlorobenzidine hydrochloric acid, filtrate waste water after treatment can go further processing with biochemical liquid.
In the present invention, filtrate after the solid-liquid separation can be reclaimed after removing acid treatment, hydrochloric acid can be done the supplemental acid of Crystallization Separation and apply mechanically, also the diluted hydrochloric acid aqueous solution of evaporation deacidification can be done washing dissolved make up water applies mechanically, after applying mechanically repeatedly, the too high levels of impurity in the dilute hydrochloric acid of evaporation deacidification, or the water system circulation is when superfluous, carry out neutralizing acid and handle, preferably adopt NaCO during neutralizing acid
3And CaCO
3, in and after-filtration, filter cake is recyclable 3,3 '-dichlorobenzidine hydrochloric acid, waste water can be done further biochemical treatment.Technological design of the present invention is ingenious, recycles acid, and is also recyclable 3, and 3 '-dichlorobenzidine hydrochloric acid utilizes recirculated water, and this all makes the technology cost reduce greatly, and the pollution that the three wastes caused is reduction greatly also, is a kind of process for cleanly preparing.
Claims (9)
1, a kind of separation and purification 3,3 '-dichlorobenzidine hydrochloride technology is characterized in that described processing step is as follows:
(1). the washing dissolving, 3, add diluted hydrochloric acid aqueous solution and/or water in 3 '-dichlorobenzidine hydrochloride, hydrochloric acid, water and the aromatic hydrocarbons mixture material, to 3,3 '-dichlorobenzidine hydrochloride washs and dissolves;
(2). oily water separation, upper oil phase is mainly aromatic hydrocarbons, and lower floor's water is mainly 3, and 3 '-dichlorobenzidine hydrochloride, water enter next step operation
(3). the evaporation deacidification, lower floor's water steams hydrochloric acid, and the concentration of hydrochloric acid of control solution is 1.0%～4.0%, 3, and 3 '-dichlorobenzidine hydrochloride concentration is 4.0%～12.0%, makes it become solution;
(4). removal of impurities decolouring, decolour removal of impurities and filtration;
(5). crystallisation by cooling, the filtrate that previous step produces is carried out the adjustment of concentration of hydrochloric acid, adjusting concentration of hydrochloric acid is 4%～8%, crystallisation by cooling separates out 3,3 '-dichlorobenzidine hydrochloride then;
(6). solid-liquid separation, the material filtering with previous step produces carries out Processing of Preparation to filter cake and goes out 3,3 '-dichlorobenzidine hydrochloride product.
2, separation and purification 3 according to claim 1,3 '-dichlorobenzidine hydrochloride technology is characterized in that: described the first step washing dissolving and second relates in the oily water separation, and washing dissolving and oil water separation process can carry out one to three time.
3, separation and purification 3 according to claim 1 and 2,3 '-dichlorobenzidine hydrochloride technology is characterized in that: in the described the first step washing dissolving and the second step oily water separation, the diluted hydrochloric acid aqueous solution of adding and/or the temperature of water are 60 ℃～95 ℃.
4, separation and purification 3 according to claim 1 and 2,3 '-dichlorobenzidine hydrochloride technology is characterized in that: in described second step oily water separation and the removal of impurities decolouring of the 4th step, the service temperature of control is 80 ℃～95 ℃.
5, separation and purification 3 according to claim 1 and 2,3 '-dichlorobenzidine hydrochloride technology is characterized in that: in described the 3rd step evaporation deacidification, the red-tape operati temperature is 80 ℃～100 ℃.
6, separation and purification 3 according to claim 1 and 2,3 '-dichlorobenzidine hydrochloride technology is characterized in that: in described the 5th step crystallisation by cooling, filtrate is cooled to 20 ℃～60 ℃.
7, separation and purification 3 according to claim 1 and 2,3 '-dichlorobenzidine hydrochloride technology is characterized in that: in the described the first step washing dissolving, aromatic hydrocarbons is benzene, also can be toluene, also can be dimethylbenzene.
8, separation and purification 3 according to claim 1 and 2,3 '-dichlorobenzidine hydrochloride technology is characterized in that: described the 4th step removal of impurities decolouring, the removal of impurities discoloring agent is an activated carbon, also can be diatomite, also can be molecular sieve.
9, separation and purification 3 according to claim 1 and 2,3 '-dichlorobenzidine hydrochloride technology is characterized in that: the filtrate after described the 6th step solid-liquid separation recycles recyclable utilization after steaming hydrochloric acid under 80 ℃～100 ℃ temperature.
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| CNB2006100854977A CN100354250C (en) | 2006-06-19 | 2006-06-19 | Tech. of separating purifying 3,3-dichlorobenzidine hydrochloride |
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| CNB2006100854977A CN100354250C (en) | 2006-06-19 | 2006-06-19 | Tech. of separating purifying 3,3-dichlorobenzidine hydrochloride |
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| CN100354250C CN100354250C (en) | 2007-12-12 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109836337A (en) * | 2019-03-08 | 2019-06-04 | 陕西大生制药科技有限公司 | A kind of method of purification of diphenyl amine compound |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4559160A (en) * | 1984-02-09 | 1985-12-17 | Bofors Nobel, Inc. | Highly stable dichlorobenzidine dihydrochloride slurry and a method for preparing such |
| DE3937320A1 (en) * | 1989-11-09 | 1991-05-16 | Hoechst Ag | METHOD FOR THE CONTINUOUS PRODUCTION OF 3,3'-DICHLOR-BENZIDINE DIHYDROCHLORIDE |
| DE4237816C1 (en) * | 1992-11-10 | 1993-10-14 | Hoechst Ag | Stable 3,3'-dichlorobenzidine dihydrochloride suspension |
| CN1280255C (en) * | 2004-08-31 | 2006-10-18 | 大连理工大学 | Process for comprehensive utilization of waste sulfuric acid from 3,3'-dichloro benzidine hydrochloride |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109836337A (en) * | 2019-03-08 | 2019-06-04 | 陕西大生制药科技有限公司 | A kind of method of purification of diphenyl amine compound |
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