CN102816080A - Method of recovering paracetamol from mother solution - Google Patents
Method of recovering paracetamol from mother solution Download PDFInfo
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- CN102816080A CN102816080A CN2012103054767A CN201210305476A CN102816080A CN 102816080 A CN102816080 A CN 102816080A CN 2012103054767 A CN2012103054767 A CN 2012103054767A CN 201210305476 A CN201210305476 A CN 201210305476A CN 102816080 A CN102816080 A CN 102816080A
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- acamol
- ion exchange
- paracetamol
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- acetic acid
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Abstract
The invention provides a method of recovering paracetamol from a mother solution. The method comprises the steps of: 1) heating the mother solution to a temperature of 40-60 DEG C, and conducting filtration under the temperature so as to obtain a filtrate; 2) subjecting the filtrate to paracetamol adsorption by simulated moving bed ion exchange system loaded with macroporous resin, eluting the paracetamol adsorbed by the moving bed with an acetic acid solution, flushing the macroporous resin with water, and collecting the eluent outflowing from acetic acid elution; and 3) concentrating the eluent so as to obtain crystals. The method provided in the invention uses the simulated moving bed ion exchange system to effectively remove the residual paracetamol from the mother solution, and the recovered paracetamol has purity up to over 98.5%, so that the cost is saved, and good economic benefits are generated. The discharged waste water contains no organic solvent or other impurities, thus reducing environmental pollution.
Description
Technical field
The invention belongs to the preparation field of isocyclic compound, be specially a kind of recoverying and utilizing method that contains the mother liquor of acetoamidophenol.
Background technology
Acamol has another name called Paracetamol USP23,BP98, chemical name N-(4-carboxyl phenyl)-ethanamide.Product is white, off-white color crystallization or crystalline powder.Odorless, mildly bitter flavor.In hot water or ethanol, be prone to dissolve, in acetone, dissolve slightly soluble in water.Fusing point is 168-172 ℃, saturated aqueous solution pH value 5.5-6.5.Antipyretic-antalgic is had significant curative effect, is one of present widely used medicine.Paracetamol USP23,BP98 is Acetanilide or Phenacetin meta-bolites in vivo.Paracetamol USP23,BP98 has no stimulation to stomach, so patients with gastric disease should be used; The anaphylaxis of no Frosst), baby, children and women are used to bring down a fever, ease pain safer.To so far, not seeing has tangible harm and pathogenic report.Can be used for treating heating, headache, arthrodynia, myalgia and neurodynia etc., meta-bolites is mainly glucuronate and small amount of sulfur hydrochlorate in vivo, discharges in the urine certainly.
Producing the main compound method that Paracetamol USP23,BP98 adopts has: synthetic route, the phenol that with the Sodium p-nitrophenoxide is raw material is the synthetic route of raw material and is the route of raw material with oil of mirbane.
After building-up reactions is accomplished, need solvent evaporated, use acetone, water washing again, recrystallization obtains the acamol white crystal.Contain a large amount of acamols in the mother liquor of washing reaction product,, will cause the waste with product of significantly rising of Paracetamol USP23,BP98 production cost, and the mother liquor discharging also causes environmental pollution if can not efficient recovery.
Summary of the invention
To the weak point that prior art exists, the objective of the invention is to propose a kind of method that from mother liquor, reclaims acamol.
The technical scheme that realizes the object of the invention is:
A kind of method that from mother liquor, reclaims acamol comprises step:
The mother liquor that 1) will contain acamol is heated to 40-60 ℃, under this temperature, filter, filtrate;
2) filtrate is carried out the absorption to acamol with the simulation moving-bed ion exchange system that resin is housed, the acamol that moving-bed adsorbs is carried out wash-out, effusive elutriant behind the collection acetate wash-out with acetic acid soln;
3) elutriant is concentrated, obtain crystallization.
Wherein, acamol content is 10.0-20.0g/L in the said mother liquor, and solids content is 5-10%.Solvent is a water in the acamol mother liquor, and dry-matter is acamol and a small amount of other impurity (bringing in the raw material).
Wherein, it is filtration medium that the filtration in the said step 1) is to use zeyssatite, and normal pressure filters or vacuum filtration, preferred vacuum filtration.
Wherein, resin is that the aperture is the macroporous resin of 0.10-0.20 μ m said step 2).
Wherein, said step 2) in the acetic acid soln quality of acetic acid content be 40-60% (mass ratio).Said wash-out also comprises the step with water rinse resin after finishing, and makes residual acetate in the resin below 5%.
Wherein, said step 2) simulation moving-bed ion exchange system is the placed in-line system of 5-15 radical ion exchange column in, adsorbs respectively at ion exchange column described in the processing cycle, the step of wash-out and flushing.Every post is provided with opening for feed, water-in, advances the acetate mouth, goes out the waste water mouth, goes out the product mouth, goes out raw material waste liquid mouth; System's when operation charging with go out opening for feed that product space is respectively ion exchange column and go out one of product mouth, and opening for feed and to go out the relative position of product mouth constant.
Wherein, a said processing cycle is 30-120min.
Wherein, The condensing crystal of said step 3) is the activated carbon decolorizing 30-50min that in elutriant, adds mass and size specific mass 0.5-1% (being to add the 0.5-1kg gac in the 100L elutriant); Filter, the solution of simmer down to acamol mass content 50-90% then, leaving standstill then has crystallization to separate out; Spinning obtains crystallization.
Wherein, said obtaining also comprises use air stream drying gained crystalline step after the crystallization, and exsiccant air flow inlet temperature is 90 ℃-100 ℃, and temperature out is 40 ℃-80 ℃.
Wherein, during said air stream drying, the flow velocity of air-flow is 10-40m/s, and the exsiccant time is 1s-30s.
Beneficial effect of the present invention is:
Use simulation moving-bed ion exchange system, effectively remove acamol residual in the mother liquor, reclaim the acamol purity that obtains and reach more than 98.5%, compare traditional evaporation concentration and practice thrift cost, produced good economic benefit.Do not have impurity such as organic solvent in the waste water of discharging, reduced environmental pollution.
Description of drawings
Fig. 1 is the embodiment of the invention 1 a used simulation moving-bed ion exchange system schema.Figure intermediate ion exchange system is made up of five radical ion exchange columns.
Embodiment
With following most preferred embodiment the present invention is described, but is not used for limiting scope of the present invention at present.
In an embodiment of the present invention, used following reagent: macroporous resin D816 (Shanghai Hua Zhen) or LS200 (Xi'an is blue dark).
Simulation moving-bed ion exchange system of the present invention is in series by 5～15 radical ion exchange columns, opening for feed, water-in is arranged on the every post, advance the acetate mouth, goes out the waste water mouth, goes out the product mouth, goes out the diluted acid mouth.The switching of continuous ionic exchange column of the present invention realizes through computer controlled automatic.
Embodiment 1
Referring to Fig. 1.Use five post ion exchange systems, be filled with macroporous resin D816 in the post.The opening for feed of the 4th exchange column is the feed entrance point of system from the top down, the 3rd exchange column go out the discharging position that the product mouth is a system.Feed entrance point and the zone that goes out between the waste water mouth position are adsorption zone.Filtrate gets into system from opening for feed, leaves system from the waste water mouth that goes out of the 5th exchange column.Acetate gets into system from clockwise second exchange column, leaves system from going out the product mouth, and the regeneration wash water gets into from the water-in (system the top Fig. 1) of clockwise first exchange column, and the waste water mouth that goes out from last several first exchange column after the water flushing is discharged.
Charging in the system and discharging position move up through 30min, and next ion exchange column is arrived in the input and output material position and relative position is constant.Become the resin in the adsorption zone of next cycle by the resin after the water flushing.
Acetic acid soln gets into system from advancing the acetate mouth, leaves system from going out product mouth position, and that leaves is called elutriant.
With 50L concentration is that Paracetamol USP23,BP98 (acamol) mother liquor of 14.0g/L is heated to 40 ℃; Solids content 5wt% wherein; In 60 ℃ of vacuum filtration impurity screenings, filtrate is equipped with the simulation moving-bed from the friendship system of macroporous adsorbent resin with the speed entering of 1.5L/h with zeyssatite.Acetic acid concentration is 50%, and flow velocity is 0.2L/h, and the water of flushing resin uses the regeneration wash water, is 4wt% by residual acetate in the resin of water flushing back, and regeneration wash water flow velocity is 3.6L/h, and the regeneration wash water gets into environment-friendly disposal system behind the acetate that reclaims high density.Behind continuous macroporous resin adsorption and diluted acid wash-out, Paracetamol USP23,BP98 concentration is 40.5g/L in the elutriant that obtains.The burgy (Powdered Activated Carbon, every 100L elutriant adds 0.5kg) of acamol (Paracetamol USP23,BP98) elutriant being used its mass volume ratio 0.5% is in 55 ℃ of decolouring 50min, through the filtering charcoal; The strong solution of the destainer simmer down to mass ratio 30% that obtains leaves standstill crystallization, centrifugal removal liquid phase; Air stream drying is carried out in crystallization, and exsiccant air flow inlet temperature is 90 ℃, and temperature out is that 40 ℃, the flow velocity of air-flow are 30m/s; Dry 30s obtains content and is 99.2% acamol.
Embodiment 2
Use ten post ion exchange systems, in be filled with macroporous resin LS200.Each feed entrance point, Inlet and outlet water position are with embodiment 1.Charging in the system and discharging position every through 80min change to next ion exchange column and relative position constant.Being become the resin in the adsorption zone of next cycle by the resin after the water flushing, is 3wt% by residual acetate in the resin of water flushing back.
Embodiment 3
Use 15 post ion exchange systems, in be filled with macroporous resin LS200.Each feed entrance point, Inlet and outlet water position are with embodiment 1.Charging in the system and discharging position change to next ion exchange column through 120min and relative position constant.By residual acetate in the resin of water flushing back is 3wt%, is become the resin in the adsorption zone of next cycle by the resin after the water flushing.
Embodiment 4
Use and ion exchange system that embodiment 1 is same.
With 100L concentration is the Paracetamol USP23,BP98 mother liquor of 15.8g/L; Wherein solids content 7wt% is heated to 50 ℃, with zeyssatite in 60 ℃ of impurity screenings; Filtrate gets into the simulation moving-bed ion exchange system that macroporous adsorbent resin is housed with the speed of 2.5L/h, and the water flow velocity of drip washing resin is 1.4L/h.Acetic acid concentration is 45%, and flow velocity is 0.3L/h, and regeneration wash water flow velocity is 5.4L/h.After continuous macroporous resin adsorption and diluted acid system, the elutriant Paracetamol USP23,BP98 concentration that obtains is 44.1g/L.The burgy of the acamol elutriant being used its mass volume ratio 0.7% is in 60 ℃ of decolouring 35min, through filtering charcoal, the strong solution of the destainer simmer down to mass ratio 20% that obtains; Leave standstill crystallization, centrifugal removal liquid phase is carried out air stream drying to crystallization; Exsiccant air flow inlet temperature is 95 ℃; Temperature out is that 60 ℃, the flow velocity of air-flow are 40m/s, and dry 10s obtains content and be 98.7% acamol.
Embodiment 5
Use and ion exchange system that embodiment 1 is same.With wherein solids content 10wt%, 150L concentration is that the Paracetamol USP23,BP98 mother liquor of 17.3g/L is heated to 55 ℃; With zeyssatite in 60 ℃ of impurity screenings; Filtrate is equipped with the simulation moving-bed from the friendship system of macroporous adsorbent resin with the speed entering of 2.0L/h, and the washing water flow velocity is 1.4L/h.Acetic acid concentration is 50%, and flow velocity is 0.25L/h, and regeneration wash water flow velocity is 3.0L/h.After continuous macroporous resin adsorption and diluted acid system, the elutriant Paracetamol USP23,BP98 concentration that obtains is 50.2g/L.With the acamol elutriant with the burgy of mass volume ratio 0.5% in 63 ℃ of decolouring 40min, through filtering charcoal, the strong solution of the destainer simmer down to mass ratio 25% that obtains; Leave standstill crystallization; Centrifugal, air stream drying is carried out in crystallization, exsiccant air flow inlet temperature is 100 ℃; Temperature out is that 80 ℃, the flow velocity of air-flow are 10m/s, and it is 99.2% acamol that dry 20s obtains content.
Embodiment 6
Use the ion exchange system of embodiment 2.With 150L concentration is that the Paracetamol USP23,BP98 mother liquor of 17.3g/L is heated to 60 ℃, and in 60 ℃ of impurity screenings, filtrate gets into the speed of 2.0L/h the simulation moving-bed from the friendship system of macroporous adsorbent resin is housed with zeyssatite, and the washing water flow velocity is 1.4L/h.Acetic acid concentration is 50%, and flow velocity is 0.25L/h, and the water of flushing resin uses the regeneration wash water, and regeneration wash water flow velocity is 3.0L/h.After continuous macroporous resin adsorption and diluted acid system, the elutriant Paracetamol USP23,BP98 concentration that obtains is 50.2g/L.The burgy of the acamol elutriant being used its mass volume ratio 1% is in 63 ℃ of decolouring 40min, through filtering charcoal, the strong solution of the destainer simmer down to mass ratio 27% that obtains; Leave standstill crystallization; Centrifugal, air stream drying is carried out in crystallization, exsiccant air flow inlet temperature is 100 ℃; Temperature out is that 80 ℃, the flow velocity of air-flow are 10m/s, and it is 99.2% acamol that dry 10s obtains content.
Above embodiment describes preferred implementation of the present invention; Be not that scope of the present invention is limited; Design under the prerequisite of spirit not breaking away from the present invention; Various modification and improvement that the common engineering technical personnel in this area make technical scheme of the present invention all should fall in the definite protection domain of claims of the present invention.
Claims (10)
1. method that from mother liquor, reclaims acamol comprises step:
The mother liquor that 1) will contain acamol heats and filtration, gets filtrate;
2) filtrate is carried out the absorption to acamol with the simulation moving-bed ion exchange system that resin is housed, the acamol that adsorbs is carried out wash-out, effusive elutriant behind the collection acetate wash-out with acetic acid soln;
3) elutriant is concentrated, obtain crystallization.
2. the method for claim 1 is characterized in that, acamol content is 10.0-20.0g/L in the said mother liquor, and dry biomass content is 5-10%.
3. the method for claim 1 is characterized in that, being heated to be in the said step 1) is heated to 40-60 ℃, and under this temperature, filters; It is filtration medium that said filtration is to use zeyssatite, and normal pressure filters or vacuum filtration.
4. the method for claim 1 is characterized in that, said step 2) in resin be that the aperture is the macroporous resin of 0.10-0.20 μ m.
5. the method for claim 1 is characterized in that, said step 2) in the acetic acid soln quality of acetic acid content be 40-60%; Said wash-out also comprises the step with water rinse resin after finishing, and makes acetate residual in the resin below 5%.
6. the method for claim 1 is characterized in that, said step 2) in simulation moving-bed ion exchange system be the placed in-line system of 5-15 radical ion exchange column, in a processing cycle each ion exchange column adsorb respectively, the step of wash-out and flushing.
7. method as claimed in claim 6 is characterized in that, a said processing cycle is 30-120min.
8. the method for claim 1; It is characterized in that the condensing crystal of said step 3) is the activated carbon decolorizing 30-50min that in elutriant, adds mass volume ratio 0.5-1%, filters; The solution of simmer down to acamol mass content 50-90% then; Leave standstill, spinning obtains crystallization.
9. like claim 1 or 8 described methods, it is characterized in that said obtaining also comprises use air stream drying gained crystalline step after the crystallization, exsiccant air flow inlet temperature is 90 ℃-100 ℃, and temperature out is 40 ℃-80 ℃.
10. method as claimed in claim 9 is characterized in that, during said air stream drying, the flow velocity of air-flow is 10-40m/s, and the exsiccant time is 1s-30s.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012103054767A CN102816080A (en) | 2012-08-24 | 2012-08-24 | Method of recovering paracetamol from mother solution |
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| CN2012103054767A CN102816080A (en) | 2012-08-24 | 2012-08-24 | Method of recovering paracetamol from mother solution |
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| CN102816080A true CN102816080A (en) | 2012-12-12 |
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| CN2012103054767A Pending CN102816080A (en) | 2012-08-24 | 2012-08-24 | Method of recovering paracetamol from mother solution |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104529799A (en) * | 2014-11-26 | 2015-04-22 | 南京化学试剂有限公司 | Method for preparing (2-hydroxyphenylamino)acetyl chloride |
| RU2802285C1 (en) * | 2022-11-28 | 2023-08-24 | Общество с ограниченной ответственностью "ДЖИЭСЭМ КЕМИКЭЛ" | Installation for continuous production of purified paracetamol, method for continuous production of purified paracetamol |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0320484A2 (en) * | 1987-12-09 | 1989-06-14 | Rhone-Poulenc Chimie | Purification of N-acetyl aminophenols |
| CN101624352A (en) * | 2009-07-30 | 2010-01-13 | 浙江康乐药业股份有限公司 | Method for processing acetaminophen refined mother liquid |
| CN102351731A (en) * | 2011-08-18 | 2012-02-15 | 河北冀衡（集团）药业有限公司 | Acetaminophen refining mother liquid recycling device and recycling method |
| CN202186952U (en) * | 2011-08-18 | 2012-04-11 | 河北冀衡（集团）药业有限公司 | Acetaminophen refining mother liquid recycling device |
-
2012
- 2012-08-24 CN CN2012103054767A patent/CN102816080A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0320484A2 (en) * | 1987-12-09 | 1989-06-14 | Rhone-Poulenc Chimie | Purification of N-acetyl aminophenols |
| CN101624352A (en) * | 2009-07-30 | 2010-01-13 | 浙江康乐药业股份有限公司 | Method for processing acetaminophen refined mother liquid |
| CN102351731A (en) * | 2011-08-18 | 2012-02-15 | 河北冀衡（集团）药业有限公司 | Acetaminophen refining mother liquid recycling device and recycling method |
| CN202186952U (en) * | 2011-08-18 | 2012-04-11 | 河北冀衡（集团）药业有限公司 | Acetaminophen refining mother liquid recycling device |
Non-Patent Citations (1)
| Title |
|---|
| 刘晓莲 等: "树脂吸附法回收对乙酰氨基酚母液", 《河南化工》, vol. 35, no. 6, 30 June 2012 (2012-06-30) * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104529799A (en) * | 2014-11-26 | 2015-04-22 | 南京化学试剂有限公司 | Method for preparing (2-hydroxyphenylamino)acetyl chloride |
| RU2802285C1 (en) * | 2022-11-28 | 2023-08-24 | Общество с ограниченной ответственностью "ДЖИЭСЭМ КЕМИКЭЛ" | Installation for continuous production of purified paracetamol, method for continuous production of purified paracetamol |
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Application publication date: 20121212 |