CN109651182B - Clean treatment method of ammonium chloride production wastewater - Google Patents

Clean treatment method of ammonium chloride production wastewater Download PDF

Info

Publication number
CN109651182B
CN109651182B CN201910130583.2A CN201910130583A CN109651182B CN 109651182 B CN109651182 B CN 109651182B CN 201910130583 A CN201910130583 A CN 201910130583A CN 109651182 B CN109651182 B CN 109651182B
Authority
CN
China
Prior art keywords
evaporation system
water
temperature
evaporation
ammonium chloride
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201910130583.2A
Other languages
Chinese (zh)
Other versions
CN109651182A (en
Inventor
彭春雪
郝晓斌
刘三六
李跃军
马万志
覃华龙
喻飞
张凯
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hubei Taisheng Chemical Co Ltd
Original Assignee
Hubei Taisheng Chemical Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hubei Taisheng Chemical Co Ltd filed Critical Hubei Taisheng Chemical Co Ltd
Priority to CN201910130583.2A priority Critical patent/CN109651182B/en
Publication of CN109651182A publication Critical patent/CN109651182A/en
Application granted granted Critical
Publication of CN109651182B publication Critical patent/CN109651182B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C227/00Preparation of compounds containing amino and carboxyl groups bound to the same carbon skeleton
    • C07C227/38Separation; Purification; Stabilisation; Use of additives
    • C07C227/40Separation; Purification
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01CAMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00Ammonia; Compounds thereof
    • C01C1/02Preparation, purification or separation of ammonia
    • C01C1/022Preparation of aqueous ammonia solutions, i.e. ammonia water
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01CAMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00Ammonia; Compounds thereof
    • C01C1/16Halides of ammonium
    • C01C1/162Ammonium fluoride
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of bulk chemicals

Abstract

The invention relates to a clean treatment method of ammonium chloride production wastewater. The method comprises the following specific steps: in the process of separating and purifying ammonium chloride, residual liquid after rectifying methanol respectively passes through a double-effect evaporation system, a first-effect evaporation system and a reduced-pressure flash evaporation system, and condensed water with high ammonia nitrogen content and high COD content obtained by the double-effect evaporation system and the reduced-pressure flash evaporation system is directly recycled to the glycine production process by the chloroacetic acid method. Treating water obtained by the primary evaporation system through a vacuum low-temperature evaporation system, using the obtained low-ammonia-nitrogen condensate water as a raw material for industrial-grade ammonia water production, and directly recycling the residual liquid into a chloroacetic acid-method glycine production process. The method has the advantages of small equipment investment, harmless treatment of evaporated condensed water, energy conservation and environmental protection, and is suitable for the glycine production process by a chloroacetic acid method.

Description

Clean treatment method of ammonium chloride production wastewater
Technical Field
The invention belongs to the technical field of glycine production by a chloroacetic acid method, and particularly relates to a clean treatment method of ammonium chloride production wastewater.
Background
At present, the separation and purification technology of ammonium chloride adopts the invention patent with the publication number of CN1033303942A and the name of 'a method and equipment for recovering ammonium chloride from glycine mother liquor', and mainly comprises the steps of respectively passing raffinate after rectifying methanol through a two-effect evaporation system, a one-effect evaporation system and a reduced pressure flash evaporation system, and centrifuging through a centrifugal machine to obtain an ammonium chloride product and an evaporation condensate in the separation process of ammonium chloride. Because the ammonium chloride evaporation condensate has complex components, high ammonia nitrogen and high COD, no economic and environment-friendly treatment method and technology exist at present.
The invention discloses a method for recycling wastewater in the process of producing glycine by chloroacetic acid, which is disclosed by CN107573252A, utilizes the difference of condensed water components in the separation and purification process of ammonium chloride, and recycles the condensed water components to different processes of glycine synthesis.
The invention discloses a method for cleaning glycine production wastewater with the publication number of CN108658374A, which is named as 'a method for cleaning glycine production wastewater', ammonium chloride mother liquor is adjusted by hydrochloric acid, primary and secondary evaporation condensate is directly recycled to a glycine production procedure, the flash evaporation condensate is subjected to a low-temperature evaporation system, evaporation liquid is discharged through membrane treatment and biochemical treatment, and residual liquid is returned to a glycine production process. The method has the defects of high investment cost, high treatment cost and the like after membrane treatment and biochemical treatment.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a clean treatment method of ammonium chloride production wastewater, in the process of separating and purifying ammonium chloride, residual liquid after rectifying methanol respectively passes through a two-effect evaporation system, a one-effect evaporation system and a reduced pressure flash evaporation system, a part of condensate can be used in a chloroacetic acid method glycine production system, a part of condensate passes through a vacuum low-temperature evaporation system, low ammonia nitrogen condensate is used as an industrial grade ammonia water production raw material, and the residual liquid is directly recycled in a chloroacetic acid method glycine production process to realize clean production.
The implementation of the invention comprises the following steps:
(1) in the process of separating and purifying ammonium chloride, residual liquid after rectifying methanol is produced from glycine is respectively passed through a two-effect evaporation system, a one-effect evaporation system and a reduced-pressure flash evaporation system to obtain three different evaporation condensate liquids, and the evaporation condensate liquids of the two-effect evaporation system and the reduced-pressure flash evaporation system are directly returned to a chloroacetic acid method glycine production system to be used as catalyst urotropine material water or glycine synthesis process water supplement. Two effect evaporation system: one-effect evaporation system: the ratio of the amount of water used in the flash evaporation system is =3:5-6: 1-2.
(2) When the ammonium chloride mother liquor passes through the primary-effect evaporation system, the temperature of a heater in the primary-effect evaporation system is controlled to be 100-130 ℃, the vacuum degree is controlled to be-0.02-0.08 Mpa, and the temperature of the generated primary-effect evaporation condensate is controlled to be 50-75 ℃. And mixing the evaporation condensate of the two-effect evaporation system and the evaporation condensate of the flash evaporation system in a mass ratio of 3:1-2, and then using the mixture to produce glycine.
(3) The one-effect evaporation condensate is evaporated in vacuum at low temperature, the temperature is controlled to be 50-75 ℃ of the water inlet temperature of the one-effect evaporation condensate, and the vacuum degree is-0.05-0.1 Mpa. Obtaining low ammonia nitrogen evaporating liquid and residual liquid. The residual liquid is directly returned to a chloroacetic acid method glycine production system to be used as catalyst urotropine chemical material water or glycine synthesis process water supplement.
(4) Conveying the evaporated liquor with low ammonia nitrogen to a condensation kettle for preparing the atropine by formaldehyde by a pump to produce ammonia water, controlling the reaction temperature to be 30-50 ℃, and prolonging the ammonia introducing time by measuring the specific gravity of the reaction liquor to obtain 1-38% ammonia water.
The method has the following advantages:
(1) the problem of unbalanced water consumption in the production of the glycine after the ammonium chloride evaporation condensate is recycled for a long time is solved, and the clean production of the glycine by the chloroacetic acid method is realized.
All water produced in the prior glycine production is clear water, and the produced wastewater is used for sewage treatment plants except for a small amount of urotropine preparation; after all the waste water is recycled, in order to ensure the qualified rate and the yield of the glycine production (the yield of the glycine can be ensured due to the addition of more water, but the yield of the glycine is reduced due to the addition of more water, so that the water addition amount needs to be ensured to be balanced), the water used in the glycine production process is a certain amount, the total amount of the waste water is surplus except the recycled waste water amount every day, namely the surplus water amount of the waste water is used as ammonia water, and the water consumption in the glycine production can be kept balanced. The wastewater amount of 1 ton of glycine production is 1.33 tons, the water amount of 1 ton of glycine recycled methenamine and process water is 1.16 tons, and the residual wastewater amount of 1 ton of glycine is 0.17 ton.
(2) The method has the advantages of simple process and equipment, low investment cost and low wastewater treatment cost, and a part of the treated wastewater is used for producing industrial-grade ammonia water for sale.
In the technical scheme of the invention, the residual liquid after rectifying the methanol contains about 1.6 to 1.8 percent of methanol and about 5 to 7 percent of methanol
27-30% of ammonium chloride and 62-66% of water, so that the amount of double-effect evaporated water is as follows: the first effect of the evaporated water amount: the flash evaporation water amount =3:5-6: 1-2.
The water content mainly evaporated by the double-effect evaporation system is about 0.8-1 percent of methanol, which is not suitable for being used as ammonia water,
used as process water supplement. The single-effect evaporation system mainly evaporates urotropine with the concentration of about 2-3% of water, the ammonia nitrogen is about 9000PPm, water with the ammonia nitrogen lower than 100PPm is obtained after low-temperature flash evaporation, the low-temperature flash evaporation water is used as ammonia water, and the water left after the low-temperature flash evaporation is used as urotropine chemical materials and water for production process.
The ammonia nitrogen in the water of the flash evaporation system is about 4000ppm, the temperature is low, the continuous low-temperature evaporation is not facilitated, and the ammonia nitrogen can be directly used
The urotropine compound and the water for the production process are used.
The mixed liquid of the double-effect evaporation system and the flash evaporation system is used for producing the glycine because the ammonia nitrogen content of the water is lower
And a certain amount of methanol can be recovered, the mixing ratio of the two is about 3:1-2, the purity of the glycine is not influenced, the content of wet powder glycine is more than 95%, and about 5% of water and methanol are also contained, after a large amount of waste water is used, the process water consumption is increased, the glycine taken away from water is increased due to the increase of the water consumption, and the yield of the glycine is reduced from the original 85% to the current 83%.
Because the water quantity of the one-effect evaporation system is large and the temperature of the evaporated water is higher (the temperature of the one-effect heater is 120 ℃, the evaporation temperature is high)
The temperature of the generated condensed water is about 60 ℃, and the temperature of other evaporated condensed water is below 50 ℃), and the content of the urotropine can be increased from 3% to about 6% by the residual solution after low-temperature vacuum evaporation, which is beneficial to preparing the concentration of the urotropine. The obtained ammonia water is white transparent liquid, the solubility is more than 20% (other indexes are not detected), and the ammonia water is mainly applied to the denitration process of fire coal. Therefore, the single-effect evaporation system is adopted for low-temperature vacuum evaporation and is used for producing ammonia water products.
Drawings
FIG. 1 is a flow chart of a cleaning treatment process of ammonium chloride production wastewater.
DETAILED DESCRIPTION OF EMBODIMENT (S) OF INVENTION
Example 1
Production of 120 tons of glycine can produce 1560m methanol mother liquor, wherein the process water consumption is 140m (the sum of water consumption for urotropine and process water supplementation), the residue liquid quantity after rectification of methanol during production of glycine is 230m, the mother liquor is obtained by respectively passing through a double-effect evaporation system, a first-effect evaporation system and a reduced-pressure flash evaporation system, the temperature of a first-effect heater is controlled to 115 ℃, the vacuum degree is controlled to-0.06 Mpa, the temperature of the generated first-effect evaporation condensate is 60 ℃, and the water quantity is 80.53 m. The volume of evaporated condensate from the dual-effect evaporation system and the reduced-pressure flash evaporation system was obtained by ethanol flash evaporation at 72.27m, and the other volumes were all obtained by ethanol flash evaporation at 7.2 m. Carrying out vacuum low-temperature evaporation on the first-effect evaporation condensate with the temperature of 60 ℃ and the water amount of 80.53m, carrying out thin-film high-temperature evaporation on the first-effect evaporation condensate with the vacuum degree controlled to-0.095 MPa, carrying out low-temperature evaporation on the first-effect evaporation condensate with the water amount of 34.52m, and carrying out thin-film high-temperature evaporation on the second-effect evaporation condensate with the remaining amount of 46.01 m. Conveying the low-temperature evaporated water to a formaldehyde-made tropine condensation kettle by a pump to produce ammonia water, and controlling the reaction temperature to be 41-45 ℃ to obtain 20.2% ammonia water.
Example 2
Production of 120 tons of glycine can produce 1560m methanol mother liquor, wherein the process water consumption is 140m (the sum of water consumption for urotropine and process water supplementation), the residue liquid amount after rectification of methanol during glycine production is 230m, the mother liquor is obtained by respectively passing through a double-effect evaporation system, a first-effect evaporation system and a reduced-pressure flash evaporation system, the temperature of a first-effect heater is controlled to 120 ℃, the vacuum degree is controlled to-0.08 Mpa, the temperature of the generated first-effect evaporation condensate is 65 ℃, and the water amount is 86.2 m. And (4) carrying out 66.6m high-speed harvest on the evaporation condensate liquid of the double-effect evaporation system and the reduced-pressure flash evaporation system, and carrying out 7.2m high-speed harvest on the ammonium chloride product by using other water quantities. Carrying out vacuum low-temperature evaporation on the first-effect evaporation condensate with the temperature of 65 ℃ and the water amount of 86.2m, carrying out thin-film high-temperature evaporation on the first-effect evaporation condensate with the vacuum degree of-0.095 MPa, carrying out low-temperature evaporation on the first-effect evaporation condensate with the water amount of 45.4m for cultivation, and carrying out thin-film high-temperature evaporation on the second-effect evaporation condensate with the remaining amount of 40.8m for cultivation. Conveying the low-temperature evaporated water to a formaldehyde-made tropine condensation kettle by a pump to produce ammonia water, and controlling the reaction temperature to 38-43 ℃ to obtain 21.4% ammonia water.
Example 3
Production of 120 tons of glycine can produce 1560m methanol mother liquor, wherein the process water consumption is 140m (the sum of water consumption for urotropine and process water supplementation), the residue liquid amount after rectification of methanol during glycine production is 230m, the mother liquor is obtained by respectively passing through a double-effect evaporation system, a first-effect evaporation system and a reduced-pressure flash evaporation system, the temperature of a first-effect heater is controlled to 130 ℃, the vacuum degree is controlled to-0.08 Mpa, the temperature of the generated first-effect evaporation condensate is 75 ℃, and the water amount is 82.55 m. The volume of evaporated condensate in the double-effect evaporation system and the reduced-pressure flash evaporation system is 74.85m under heavy load, and the other water volumes are all 7.2m under heavy load in the ammonium chloride product. Carrying out vacuum low-temperature evaporation on the first-effect evaporation condensate with the temperature of 55 ℃ and the water amount of 82.55m, carrying out thin-film high-temperature evaporation on the first-effect evaporation condensate with the vacuum degree of-0.05 Mpa, carrying out low-temperature evaporation on the first-effect evaporation condensate with the water amount of 30.52m, and carrying out thin-film high-temperature evaporation on the second-effect evaporation condensate with the residual amount of 42. Conveying the low-temperature evaporated water to a formaldehyde-made tropine condensation kettle by a pump to produce ammonia water, and controlling the reaction temperature to be 40-43 ℃ to obtain 24.6% ammonia water.
Example 4
Production of 120 tons of glycine can produce 1560m methanol mother liquor, wherein the process water consumption is 140m (the sum of water consumption for urotropine and process water supplementation), the residue liquid amount after rectification of methanol during glycine production is 230m, the mother liquor is obtained by respectively passing through a double-effect evaporation system, a first-effect evaporation system and a reduced-pressure flash evaporation system, the temperature of a first-effect heater is controlled to 125 ℃, the vacuum degree is controlled to-0.02 Mpa, the temperature of the generated first-effect evaporation condensate is 50 ℃, and the water amount is 88 m. The volume of evaporated condensate from the dual-effect evaporation system and the reduced-pressure flash evaporation system was obtained by ethanol flash evaporation at 68.35m, and the other volumes were all obtained by ethanol flash evaporation at 7.2 m. Carrying out vacuum low-temperature evaporation on the first-effect evaporation condensate with the temperature of 60 ℃ and the water amount of 88.5m, carrying out thin-film high-temperature evaporation on the first-effect evaporation condensate with the vacuum degree controlled at-0.08 MPa, carrying out thin-film high-temperature evaporation on the first-effect evaporation condensate with the water amount of 42.35m, and carrying out thin-film high-temperature evaporation on the second-effect evaporation condensate with the residual amount of 41.5 m. Conveying the low-temperature evaporated water to a formaldehyde-made tropine condensation kettle by a pump to produce ammonia water, and controlling the reaction temperature to 39-42 ℃ to obtain 22.7% ammonia water.

Claims (4)

1. A clean treatment method of ammonium chloride production wastewater is characterized in that: the method comprises the following specific steps:
(1) in the ammonium chloride separation and purification process, the residual liquid after rectifying the methanol is respectively subjected to a double-effect evaporation system, a first-effect evaporation system and a reduced-pressure flash evaporation system to obtain three different evaporation condensates, the evaporation condensates of the double-effect evaporation system and the reduced-pressure flash evaporation system directly return to a chloroacetic acid method glycine production system, and the evaporation condensate of the first-effect evaporation system is treated by a vacuum low-temperature evaporation system, namely the double-effect evaporation system: one-effect evaporation system: the ratio of water used in the flash evaporation system is =3:5-6:1-2, the temperature in the primary evaporation system is controlled to be 100 ℃ and 130 ℃, the vacuum degree is controlled to be-0.02 to-0.08 Mpa, the temperature of the generated primary evaporation condensate is controlled to be 50-75 ℃, and the residual liquid after rectifying the methanol contains 1.6-1.8 percent of methanol, 5-7 percent of urotropine, 27-30 percent of ammonium chloride and 62-66 percent of water;
(2) and (2) directly using the low ammonia nitrogen water obtained by the vacuum low-temperature evaporation system treatment in the step (1) to produce ammonia water by using a condensation kettle, and returning the residual liquid to a glycine system of a chloroacetic acid method.
2. The method for cleaning and treating the ammonium chloride production wastewater according to claim 1, characterized in that: and (2) evaporating the condensate in the step (1) at a low temperature in vacuum, wherein the temperature is controlled to be 50-75 ℃ of the water inlet temperature of the condensate in the first-effect evaporation, and the vacuum degree is-0.05 to-0.1 Mpa.
3. The method for cleaning and treating the ammonium chloride production wastewater according to claim 1, characterized in that: and (3) directly using the low ammonia nitrogen water treated by the vacuum low-temperature evaporation system in the step (2) to produce ammonia water by using a condensation kettle, controlling the temperature to be 30-50 ℃, and returning the residual liquid to a glycine system of a chloroacetic acid method.
4. The method for cleaning and treating the ammonium chloride production wastewater according to claim 1, characterized in that: and (3) mixing the evaporation condensate of the two-effect evaporation system in the step (2) with the evaporation condensate of the flash evaporation system in a mass ratio of 3:1-2, and then using the mixture to produce glycine.
CN201910130583.2A 2019-02-21 2019-02-21 Clean treatment method of ammonium chloride production wastewater Active CN109651182B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201910130583.2A CN109651182B (en) 2019-02-21 2019-02-21 Clean treatment method of ammonium chloride production wastewater

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201910130583.2A CN109651182B (en) 2019-02-21 2019-02-21 Clean treatment method of ammonium chloride production wastewater

Publications (2)

Publication Number Publication Date
CN109651182A CN109651182A (en) 2019-04-19
CN109651182B true CN109651182B (en) 2021-09-07

Family

ID=66123552

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201910130583.2A Active CN109651182B (en) 2019-02-21 2019-02-21 Clean treatment method of ammonium chloride production wastewater

Country Status (1)

Country Link
CN (1) CN109651182B (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110980844A (en) * 2019-11-22 2020-04-10 天津乐科节能科技有限公司 Treatment method of glycine production wastewater

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101538269A (en) * 2009-04-15 2009-09-23 杜青旺 Recovery method for dealcoholizing waste water in glycine technology of chloroactic acid method
CN103011484A (en) * 2013-01-08 2013-04-03 石家庄东华金龙化工有限公司 Method for treating ammonium chloride wastewater during production of glycin prepared based on chloroacetic acid method
CN107573252A (en) * 2017-09-11 2018-01-12 宜昌金信化工有限公司 A kind of method that Sewage treatment utilizes during chloroactic acid method production glycine
CN108218089A (en) * 2018-03-09 2018-06-29 浙江新安化工集团股份有限公司 A kind of processing method of glycin waste water
CN108658374A (en) * 2018-05-18 2018-10-16 宜昌金信化工有限公司 A kind of cleaning method of glycine production waste water

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101717165A (en) * 2009-12-22 2010-06-02 大连水产学院 Method for treating wastewater from preparation of glycine by chloroacetic acid ammonolysis process
WO2018053071A1 (en) * 2016-09-16 2018-03-22 Heliae Development Llc Methods of treating wastewater with microalgae cultures supplemented with organic carbon

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101538269A (en) * 2009-04-15 2009-09-23 杜青旺 Recovery method for dealcoholizing waste water in glycine technology of chloroactic acid method
CN103011484A (en) * 2013-01-08 2013-04-03 石家庄东华金龙化工有限公司 Method for treating ammonium chloride wastewater during production of glycin prepared based on chloroacetic acid method
CN107573252A (en) * 2017-09-11 2018-01-12 宜昌金信化工有限公司 A kind of method that Sewage treatment utilizes during chloroactic acid method production glycine
CN108218089A (en) * 2018-03-09 2018-06-29 浙江新安化工集团股份有限公司 A kind of processing method of glycin waste water
CN108658374A (en) * 2018-05-18 2018-10-16 宜昌金信化工有限公司 A kind of cleaning method of glycine production waste water

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
Synthesis of glycine using two-step reaction approach in alcohol and its purification;Limin Yang,等;《Advanced Materials Research》;20111122;第1711-1715页 *
从生产甘氨酸废水中回收氯化铵工艺研究;杨春光,等;《无机盐工业》;20031231;第42-43页 *

Also Published As

Publication number Publication date
CN109651182A (en) 2019-04-19

Similar Documents

Publication Publication Date Title
CN102079512B (en) Process for recovering sulfuric acid and sulfate from waste acid generated in preparation of titanium dioxide by using sulfuric acid method
CN101117315B (en) Production method of citric acid
CN210084997U (en) Device for recycling cyclohexanone ammoximation device wastewater
CN109651182B (en) Clean treatment method of ammonium chloride production wastewater
CN104086362A (en) Method for recycling organic solvents of wastewater generated in synthesis of hydrazine hydrate by ketazine method
CN104058924A (en) Method for preparing chloromethane by utilizing alcohol-containing hydrochloric acid
CN103833050A (en) Treatment method of ammonium chloride-containing aminoacetic acid dealcoholization mother liquor
CN101121709B (en) Primary concentration and purification method for trioxymethylene after synthesizing
CN204400883U (en) Pentamethylene diamine purification system
CN103601616B (en) Alcohol-water separation recycling method of Fischer-Tropsch synthesis reaction water
CN209940877U (en) Utilize device of dimethyl phosphite accessory substance synthetic glyphosate
CN104876817B (en) A kind of method that use succinic acid fermentation liquor extracts succinic acid
CN108128829A (en) Taurine waste water zero discharge treatment process and taurine wastewater zero discharge processing unit
CN104974046A (en) Purifying method of pentanediamine
CN104418759A (en) Method for preparing glycine through alcohol phase synthesis, chromatographic separation, MVR evaporative crystallization
CN109650646B (en) Treatment method of glycine production wastewater
CN108640844B (en) Method for recovering triethylamine from industrial wastewater
CN107573252B (en) The method that Sewage treatment utilizes during a kind of chloroactic acid method production glycine
CN106349108B (en) A kind of isolation and purification method of cyanoacetic acid
CN106608832B (en) The process of liquid ammonia process for caustic soda purification and Ammonia Process co-producing ethanol amine
TW201434758A (en) Method of recycling ethylene glycol and acetaldehyde from polyester waste water
CN104478767B (en) Method for processing beta salt mother liquor through low temperature acid separation technology
CN102249889A (en) Method for extracting succinic acid from citric acid mother solution
Wang et al. A novel process to recycle the highly concentrated calcium and chloride ions in the gelatin acidification wastewater
CN210885671U (en) Recovery unit of metribuzin production waste acid water

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant