CN103113248A - Method for recycling DL-aspartic acid from aspartame production wastewater - Google Patents
Method for recycling DL-aspartic acid from aspartame production wastewater Download PDFInfo
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- CN103113248A CN103113248A CN2013100539173A CN201310053917A CN103113248A CN 103113248 A CN103113248 A CN 103113248A CN 2013100539173 A CN2013100539173 A CN 2013100539173A CN 201310053917 A CN201310053917 A CN 201310053917A CN 103113248 A CN103113248 A CN 103113248A
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- Prior art keywords
- aspartame
- production wastewater
- aspartic acid
- feed liquid
- reflux
- Prior art date
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Links
- 108010011485 Aspartame Proteins 0.000 title claims abstract description 45
- IAOZJIPTCAWIRG-QWRGUYRKSA-N aspartame Chemical compound OC(=O)C[C@H](N)C(=O)N[C@H](C(=O)OC)CC1=CC=CC=C1 IAOZJIPTCAWIRG-QWRGUYRKSA-N 0.000 title claims abstract description 45
- 239000000605 aspartame Substances 0.000 title claims abstract description 45
- 229960003438 aspartame Drugs 0.000 title claims abstract description 45
- 235000010357 aspartame Nutrition 0.000 title claims abstract description 45
- 239000002351 wastewater Substances 0.000 title claims abstract description 45
- CKLJMWTZIZZHCS-UHFFFAOYSA-N Aspartic acid Chemical compound OC(=O)C(N)CC(O)=O CKLJMWTZIZZHCS-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000004064 recycling Methods 0.000 title abstract 2
- 238000010992 reflux Methods 0.000 claims abstract description 35
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 27
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 56
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 48
- 238000002425 crystallisation Methods 0.000 claims description 16
- 230000008025 crystallization Effects 0.000 claims description 16
- 230000000994 depressogenic effect Effects 0.000 claims description 16
- 238000004821 distillation Methods 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 8
- 230000000630 rising effect Effects 0.000 claims description 8
- 238000003756 stirring Methods 0.000 claims description 8
- 238000011084 recovery Methods 0.000 abstract description 3
- 238000001816 cooling Methods 0.000 abstract 1
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 238000003786 synthesis reaction Methods 0.000 description 4
- WFDIJRYMOXRFFG-UHFFFAOYSA-N Acetic anhydride Chemical compound CC(=O)OC(C)=O WFDIJRYMOXRFFG-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 235000001014 amino acid Nutrition 0.000 description 3
- 150000001413 amino acids Chemical class 0.000 description 3
- 235000003599 food sweetener Nutrition 0.000 description 3
- 239000003765 sweetening agent Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 239000010815 organic waste Substances 0.000 description 2
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- AHRFRRASJMTTQU-UHFFFAOYSA-N 6-methyl-2,2-dioxooxathiazin-4-one;potassium Chemical class [K].CC1=CC(=O)NS(=O)(=O)O1 AHRFRRASJMTTQU-UHFFFAOYSA-N 0.000 description 1
- UDIPTWFVPPPURJ-UHFFFAOYSA-M Cyclamate Chemical compound [Na+].[O-]S(=O)(=O)NC1CCCCC1 UDIPTWFVPPPURJ-UHFFFAOYSA-M 0.000 description 1
- CKLJMWTZIZZHCS-REOHCLBHSA-N L-aspartic acid Chemical compound OC(=O)[C@@H](N)CC(O)=O CKLJMWTZIZZHCS-REOHCLBHSA-N 0.000 description 1
- COLNVLDHVKWLRT-QMMMGPOBSA-N L-phenylalanine Chemical compound OC(=O)[C@@H](N)CC1=CC=CC=C1 COLNVLDHVKWLRT-QMMMGPOBSA-N 0.000 description 1
- 229930006000 Sucrose Natural products 0.000 description 1
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- -1 asccharin Substances 0.000 description 1
- 235000003704 aspartic acid Nutrition 0.000 description 1
- OQFSQFPPLPISGP-UHFFFAOYSA-N beta-carboxyaspartic acid Natural products OC(=O)C(N)C(C(O)=O)C(O)=O OQFSQFPPLPISGP-UHFFFAOYSA-N 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000625 cyclamic acid and its Na and Ca salt Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000001835 salubrious effect Effects 0.000 description 1
- 229960001462 sodium cyclamate Drugs 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000005720 sucrose Substances 0.000 description 1
- 235000019605 sweet taste sensations Nutrition 0.000 description 1
- 238000010189 synthetic method Methods 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for recycling DL-aspartic acid from aspartame production wastewater. The method comprises the following steps of: infiltrating aspartame production wastewater to a reflux kettle for being heated up and refluxed; infiltrating the heated and refluxed aspartame production wastewater to a concentration kettle for being distilled under normal pressure and concentrated, adding water to dilute the aspartame production wastewater when the aspartame production wastewater is thick; distilling and concentrating the thick aspartame production wastewater under normal pressure, adding hydrochloric acid to heat up, reflux and hydrolyze the distilled and concentrated aspartame production wastewater; regulating a pH value of the aspartame production wastewater by sodium hydroxide after the refluxing is completed, cooling and crystallizing the aspartame production wastewater; and centrifuging the aspartame production wastewater to obtain the DL-aspartic acid. According to the method disclosed by the invention, the aspartame production wastewater can be treated, the DL-aspartic acid is recycled, the environment pollution is reduced and the production cost is saved; moreover, the method is simple in process, the device investment is less, the operation is easy and the recovery rate is high.
Description
[technical field]
The present invention relates to technical field of waste water processing, relate in particular to a kind of method that reclaims the DL-aspartic acid from production aspartame waste water.
[background technology]
Aspartame (Aspartame, C
14H
18N
2O
5), chemistry α by name-L-aspartoyl-L-Phe methyl esters is commonly called as sweetener, is a kind of emerging synthetic sweetener.Nineteen sixty-five U.S. GD Searle company is the synthetic aspartame first, patents.Aspartame is a kind of white crystalline powder, has salubrious sweet taste, and its sugariness is 180～200 times of sucrose.Because it is compared with synthetic sweeteners such as asccharin, Sodium Cyclamate, 3,4-Dihydro-6-methyl-1,2,3-oxathiazin-4-one 2,2-dioxide potassium salts, the advantage that has that flavor matter is good, safe, heat is low etc., make it in the eighties in last century with regard to fashionable European ﹠ American Market, be widely used in food, beverage and pharmaceutical industry.More than 100 granted use in countries and regions in the world again and again at present, and confirmed as international A (I) level sweeting agent by " the joint council of foodstuff additive " that the World Health Organization and Food and Argriculture OrganizationFAO are subordinate to.
At present the synthetic method of aspartame mainly contains biological synthesis process and chemical synthesis two classes, and wherein biological synthesis process is only used in minority external producer.The method of chemosynthesis aspartame is more, and Technology is also relatively ripe, therefore is widely used in most of producers.The chemical synthesis of widely using now is to obtain N-formyl-a-L-aspartic anhydride by ASPARTIC ACID and formic acid, aceticanhydride reaction, reacting with L-Phe, synthetic N-formyl-a-L-aspartic acid-L-Phe, then produce a-L-aspartic acid-L-Phe methyl ester hydrochloride with its reaction at low temperatures with concentrated hydrochloric acid and methyl alcohol, generation aspartame at last neutralizes.
But can produce in the synthetic aspartame process of chemical method and contain in a large number amino acid whose organic waste water, seldom have in existing factory technics synthetic aspartame waste water processed, therefore containing in a large number amino acid whose organic waste water is discharged, serious environment pollution not only, and greatly wasted resource, increase production cost, also do not met the aim of energy-saving and emission-reduction.
Treatment process and the treatment system thereof of the high saliferous amino acid wastewater of a kind of aspartame are disclosed in Chinese patent 201210112035.5, although can necessarily process aspartame waste water, but it need to set up a new filtration treatment system of cover, not only facility investment is large, complex process, complex operation is not suitable for the factory of all production aspartame, nor can directly reclaims the DL-aspartic acid from aspartame waste water.
[summary of the invention]
Purpose of the present invention solves exactly in prior art and seldom aspartame waste water is processed, and the treatment facility investment is large, and the problem that technique is loaded down with trivial details provides a kind of method that reclaims the DL-aspartic acid from production aspartame waste water.
A kind of method that reclaims the DL-aspartic acid from production aspartame waste water, the method comprise the steps,
(1) production aspartame waste water is driven in the backflow still with pump, opens and stir, open steam valve, temperature rising reflux is controlled reflux temperature at 100～120 ℃, return time 2～4 hours,
(2) backflow is complete, utilizes pneumatics that feed liquid is depressed into concentration kettle, and the acetic acid in waste water is distilled away in the heating air distillation,
(3) feed liquid is thick in still, and when the liquid outlet quantity of condenser liquid outlet obviously reduced, adding mass ratio was the water of initial aspartame wastewater flow rate 35%～100%, continues to add thermal distillation, steams acetic acid,
(4) again be distilled to when being thick when feed liquid in still, adding mass ratio is that the mass concentration of initial aspartame wastewater flow rate 20%～30% is 31% hydrochloric acid, reflux, be hydrolyzed, control reflux temperature at 100～120 ℃, return time 3～6 hours
(5) backflow is complete, utilizes pneumatics that feed liquid is depressed into crystallization kettle, is 32% sodium hydroxide adjusting material liquid pH value to 2.5～3.5 with mass concentration,
(6) decrease temperature crystalline when the crystallization kettle temperature is down to 20～30 ℃, is transferred to whizzer with material and carries out centrifugally, obtains the DL-aspartic acid.
Reclaim the DL-aspartic acid by the method, the rate of recovery can reach 20%.
The method can not only be processed production aspartame waste water, reclaims the DL-aspartic acid, reduces environmental pollution, save production cost, and the method technique is simple, and facility investment is few, and easy handling and the rate of recovery are high.
[description of drawings]
Fig. 1 reclaims the process flow sheet of DL-aspartic acid from production aspartame waste water
[embodiment]
Embodiment one
(1) production aspartame waste water 4000Kg is driven in the backflow still with pump, opens and stir, open steam valve, temperature rising reflux is controlled reflux temperature at 100 ℃, return time 4 hours,
(2) backflow is complete, utilizes pneumatics that feed liquid is depressed into concentration kettle, and the acetic acid in waste water is distilled away in the heating air distillation,
(3) feed liquid is thick in still, when the liquid outlet quantity of condenser liquid outlet obviously reduces, adds the water of 1500Kg, continues to add thermal distillation, steams acetic acid,
(4) again be distilled to when being thick when feed liquid in still, adding the 800Kg mass concentration is 31% hydrochloric acid, and reflux is hydrolyzed, and controls reflux temperature at 100 ℃, return time 6 hours,
(5) backflow is complete, utilizes pneumatics that feed liquid is depressed into crystallization kettle, is 32% sodium hydroxide adjusting material liquid pH value to 2.5～3.5 with mass concentration,
(6) decrease temperature crystalline when the crystallization kettle temperature is down to 20 ℃, is transferred to whizzer with material and carries out centrifugally, obtains the DL-aspartic acid.
Embodiment two
(1) production aspartame waste water 4000Kg is driven in the backflow still with pump, opens and stir, open steam valve, temperature rising reflux is controlled reflux temperature at 120 ℃, return time 2 hours,
(2) backflow is complete, utilizes pneumatics that feed liquid is depressed into concentration kettle, and the acetic acid in waste water is distilled away in the heating air distillation,
(3) feed liquid is thick in still, when the liquid outlet quantity of condenser liquid outlet obviously reduces, adds the water of 4000Kg, continues to add thermal distillation, steams acetic acid,
(4) again be distilled to when being thick when feed liquid in still, adding the 1200Kg mass concentration is 31% hydrochloric acid, and reflux is hydrolyzed, and controls reflux temperature at 120 ℃, return time 3 hours,
(5) backflow is complete, utilizes pneumatics that feed liquid is depressed into crystallization kettle, is 32% sodium hydroxide adjusting material liquid pH value to 2.5～3.5 with mass concentration,
(6) decrease temperature crystalline when the crystallization kettle temperature is down to 30 ℃, is transferred to whizzer with material and carries out centrifugally, obtains the DL-aspartic acid.
Embodiment three
(1) production aspartame waste water 4000Kg is driven in the backflow still with pump, opens and stir, open steam valve, temperature rising reflux is controlled reflux temperature at 110 ℃, return time 3 hours,
(2) backflow is complete, utilizes pneumatics that feed liquid is depressed into concentration kettle, and the acetic acid in waste water is distilled away in the heating air distillation,
(3) feed liquid is thick in still, when the liquid outlet quantity of condenser liquid outlet obviously reduces, adds the water of 3000Kg, continues to add thermal distillation, steams acetic acid,
(4) again be distilled to when being thick when feed liquid in still, adding the 1000Kg mass concentration is 31% hydrochloric acid, and reflux is hydrolyzed, and controls reflux temperature at 110 ℃, return time 5 hours,
(5) backflow is complete, utilizes pneumatics that feed liquid is depressed into crystallization kettle, is 32% sodium hydroxide adjusting material liquid pH value to 2.5～3.5 with mass concentration,
(6) decrease temperature crystalline when the crystallization kettle temperature is down to 30 ℃, is transferred to whizzer with material and carries out centrifugally, obtains the DL-aspartic acid.
Embodiment four
(1) production aspartame waste water 4000Kg is driven in the backflow still with pump, opens and stir, open steam valve, temperature rising reflux is controlled reflux temperature at 100 ℃, return time 4 hours,
(2) backflow is complete, utilizes pneumatics that feed liquid is depressed into concentration kettle, and the acetic acid in waste water is distilled away in the heating air distillation,
(3) feed liquid is thick in still, when the liquid outlet quantity of condenser liquid outlet obviously reduces, adds the water of 4000Kg, continues to add thermal distillation, steams acetic acid,
(4) again be distilled to when being thick when feed liquid in still, adding the 1000Kg mass concentration is 31% hydrochloric acid, and reflux is hydrolyzed, and controls reflux temperature at 120 ℃, return time 3 hours,
(5) backflow is complete, utilizes pneumatics that feed liquid is depressed into crystallization kettle, is 32% sodium hydroxide adjusting material liquid pH value to 2.7 with mass concentration,
(6) decrease temperature crystalline when the crystallization kettle temperature is down to 30 ℃, is transferred to whizzer with material and carries out centrifugally, obtains the DL-aspartic acid.
Embodiment five
(1) production aspartame waste water 4000Kg is driven in the backflow still with pump, opens and stir, open steam valve, temperature rising reflux is controlled reflux temperature at 120 ℃, return time 2 hours,
(2) backflow is complete, utilizes pneumatics that feed liquid is depressed into concentration kettle, and the acetic acid in waste water is distilled away in the heating air distillation,
(3) feed liquid is thick in still, when the liquid outlet quantity of condenser liquid outlet obviously reduces, adds the water of 2000Kg, continues to add thermal distillation, steams acetic acid,
(4) again be distilled to when being thick when feed liquid in still, adding the 1000Kg mass concentration is 31% hydrochloric acid, and reflux is hydrolyzed, and controls reflux temperature at 120 ℃, return time 4 hours,
(5) backflow is complete, utilizes pneumatics that feed liquid is depressed into crystallization kettle, is 32% sodium hydroxide adjusting material liquid pH value to 3.5 with mass concentration,
(6) decrease temperature crystalline when the crystallization kettle temperature is down to 20 ℃, is transferred to whizzer with material and carries out centrifugally, obtains the DL-aspartic acid.
Embodiment six
(1) production aspartame waste water 4000Kg is driven in the backflow still with pump, opens and stir, open steam valve, temperature rising reflux is controlled reflux temperature at 100 ℃, return time 4 hours,
(2) backflow is complete, utilizes pneumatics that feed liquid is depressed into concentration kettle, and the acetic acid in waste water is distilled away in the heating air distillation,
(3) feed liquid is thick in still, when the liquid outlet quantity of condenser liquid outlet obviously reduces, adds the water of 1500Kg, continues to add thermal distillation, steams acetic acid,
(4) again be distilled to when being thick when feed liquid in still, adding the 1000Kg mass concentration is 31% hydrochloric acid, and reflux is hydrolyzed, and controls reflux temperature at 100 ℃, return time 6 hours,
(5) backflow is complete, utilizes pneumatics that feed liquid is depressed into crystallization kettle, is 32% sodium hydroxide adjusting material liquid pH value to 2.7 with mass concentration,
(6) decrease temperature crystalline when the crystallization kettle temperature is down to 20 ℃, is transferred to whizzer with material and carries out centrifugally, obtains the DL-aspartic acid.
Claims (1)
1. method that reclaims the DL-aspartic acid from production aspartame waste water is characterized in that: the method comprises the steps,
(1) production aspartame waste water is driven in the backflow still with pump, opens and stir, open steam valve, temperature rising reflux is controlled reflux temperature at 100～120 ℃, return time 2～4 hours,
(2) backflow is complete, utilizes pneumatics that feed liquid is depressed into concentration kettle, and the acetic acid in waste water is distilled away in the heating air distillation,
(3) feed liquid is thick in still, and when the liquid outlet quantity of condenser liquid outlet obviously reduced, adding mass ratio was the water of initial aspartame wastewater flow rate 35%～100%, continues to add thermal distillation, steams acetic acid,
(4) again be distilled to when being thick when feed liquid in still, adding mass ratio is that the mass concentration of initial aspartame wastewater flow rate 20%～30% is 31% hydrochloric acid, reflux, be hydrolyzed, control reflux temperature at 100～120 ℃, return time 3～6 hours
(5) backflow is complete, utilizes pneumatics that feed liquid is depressed into crystallization kettle, is 32% sodium hydroxide adjusting material liquid pH value to 2.5～3.5 with mass concentration,
(6) decrease temperature crystalline when the crystallization kettle temperature is down to 20～30 ℃, is transferred to whizzer with material and carries out centrifugally, obtains the DL-aspartic acid.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100539173A CN103113248A (en) | 2013-02-20 | 2013-02-20 | Method for recycling DL-aspartic acid from aspartame production wastewater |
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| CN2013100539173A CN103113248A (en) | 2013-02-20 | 2013-02-20 | Method for recycling DL-aspartic acid from aspartame production wastewater |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116478055A (en) * | 2023-05-05 | 2023-07-25 | 新疆苏源生物工程有限公司 | Chiral refining method of aspartic acid |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4348317A (en) * | 1980-12-29 | 1982-09-07 | Monsanto Company | Recovery of L-phenylalanine and L-aspartic acid during preparation of α-L-aspartyl-L-phenylalanine methyl ester |
| JPS63159355A (en) * | 1986-12-23 | 1988-07-02 | Mitsui Toatsu Chem Inc | Method for recovering L-phenylalanine and L-aspartic acid |
| US5304671A (en) * | 1991-08-05 | 1994-04-19 | Ajinomoto Co., Inc. | Method for recovery of α-L-aspartyl-L-phenylalanine methyl ester, L-phenylalanine and L-aspartic acid |
| CN101284796A (en) * | 2008-05-30 | 2008-10-15 | 何关昌 | Process for preparing DL-phenylalanine and DL-asparaginic acid by mother liquor reclamation |
| CN102603090A (en) * | 2012-04-17 | 2012-07-25 | 常州大学 | Method and system for treating high-salinity amino acid waste water in aspartame industry |
| CN102875401A (en) * | 2012-10-30 | 2013-01-16 | 宜兴市前成生物有限公司 | Method for producing DL-aspartic acid from waste radix asparagi |
-
2013
- 2013-02-20 CN CN2013100539173A patent/CN103113248A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4348317A (en) * | 1980-12-29 | 1982-09-07 | Monsanto Company | Recovery of L-phenylalanine and L-aspartic acid during preparation of α-L-aspartyl-L-phenylalanine methyl ester |
| JPS63159355A (en) * | 1986-12-23 | 1988-07-02 | Mitsui Toatsu Chem Inc | Method for recovering L-phenylalanine and L-aspartic acid |
| US5304671A (en) * | 1991-08-05 | 1994-04-19 | Ajinomoto Co., Inc. | Method for recovery of α-L-aspartyl-L-phenylalanine methyl ester, L-phenylalanine and L-aspartic acid |
| CN101284796A (en) * | 2008-05-30 | 2008-10-15 | 何关昌 | Process for preparing DL-phenylalanine and DL-asparaginic acid by mother liquor reclamation |
| CN102603090A (en) * | 2012-04-17 | 2012-07-25 | 常州大学 | Method and system for treating high-salinity amino acid waste water in aspartame industry |
| CN102875401A (en) * | 2012-10-30 | 2013-01-16 | 宜兴市前成生物有限公司 | Method for producing DL-aspartic acid from waste radix asparagi |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116478055A (en) * | 2023-05-05 | 2023-07-25 | 新疆苏源生物工程有限公司 | Chiral refining method of aspartic acid |
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Application publication date: 20130522 |