CN113912236A - Method for recovering glycolic acid from CMC wastewater - Google Patents

Method for recovering glycolic acid from CMC wastewater Download PDF

Info

Publication number
CN113912236A
CN113912236A CN202111270790.1A CN202111270790A CN113912236A CN 113912236 A CN113912236 A CN 113912236A CN 202111270790 A CN202111270790 A CN 202111270790A CN 113912236 A CN113912236 A CN 113912236A
Authority
CN
China
Prior art keywords
glycolic acid
waste water
cmc
recovering
wastewater
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.)
Pending
Application number
CN202111270790.1A
Other languages
Chinese (zh)
Inventor
蔡亲荫
张芳
李宇翔
舒俭
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.)
Guangzhou Rand Environmental Protection Resources Technology Co ltd
Original Assignee
Guangzhou Rand Environmental Protection Resources Technology 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 Guangzhou Rand Environmental Protection Resources Technology Co ltd filed Critical Guangzhou Rand Environmental Protection Resources Technology Co ltd
Priority to CN202111270790.1A priority Critical patent/CN113912236A/en
Publication of CN113912236A publication Critical patent/CN113912236A/en
Pending legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/04—Chlorides
    • C01D3/06—Preparation by working up brines; seawater or spent lyes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
    • C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/285—Treatment of water, waste water, or sewage by sorption using synthetic organic sorbents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
    • C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)

Abstract

The invention discloses a method for recovering glycolic acid from CMC waste water, which relates to the field of chemical industry and water treatment environmental protection, and aims to solve the problems that the technology for separating sodium chloride from sodium glycolate to obtain sodium glycolate in the prior art is too complex, the process reliability is not high, the cost is too high, and the practical application is difficult, the following scheme is proposed, and the method comprises the following working procedures: a first step of pretreating wastewater to remove cellulose ether residues and pigments; the second process comprises the following steps: separating organic impurities by resin adsorption; a third step of evaporating and desalting by an MVR technology; a fourth step of acidifying, electrodialyzing and desalting, wherein sodium glycolate is converted into glycolic acid by adding a certain amount of acid, and simultaneously, residual sodium chloride is separated; and a fifth step of obtaining a glycolic acid product with higher purity by distillation and concentration. The method has the advantages of simple process, high resource utilization rate and low cost, can obtain a glycolic acid product with higher purity, and is effectively used for the treatment and resource utilization of various CMC wastewater.

Description

Method for recovering glycolic acid from CMC wastewater
Technical Field
The invention relates to the fields of chemical industry and water treatment environment protection, in particular to a method for recovering glycolic acid from CMC wastewater.
Background
Carboxymethyl cellulose ether (CMC) is an important cellulose ether product and is widely applied to industries such as petroleum, chemical engineering, detergents, ceramics, cigarettes, printing and dyeing, textiles, foods, medicines and the like. But the production wastewater mainly contains sodium glycolate, sodium chloride, a small amount of cellulose ether, ethanol and other pollutants, the COD and the salt content of the wastewater are both high, the sodium chloride content is up to more than 10%, and the COD content is up to 60000 mg/L. The conventional treatment is difficult to meet the emission requirements and the treatment cost is high. In recent years, many studies have been made to recover sodium chloride industrial salt and sodium glycolate as by-products from waste water, from the viewpoint of recycling. Several patent technologies have been successively disclosed therein. These include chromatographic separation techniques (a chromatographic separation method of sodium chloride and sodium glycolate in wastewater from sodium carboxymethyl cellulose production, patent application No. CN103214113A), extraction techniques (a process for treating and comprehensively utilizing wastewater from sodium carboxymethyl cellulose production, patent application No. 102206014A; a method for extracting high-purity sodium glycolate from diclofenac sodium wastewater, patent application No. CN20140124840.9), and acidification-esterification-hydrolysis techniques (a technique for extracting sodium glycolate from wastewater, patent application No. CN 201610346449.2).
Although these patent publications can separate sodium chloride and sodium glycolate to different degrees and obtain sodium glycolate, the technology is too complicated, the process reliability is not high and the cost is too high to be practically applied, and therefore, in order to solve such problems, we propose a method for recovering glycolic acid from CMC waste water.
Disclosure of Invention
The invention provides a method for recovering glycolic acid from CMC wastewater, which aims to solve the problems that in the prior art provided by the background art, sodium chloride and sodium glycolate can be separated to different degrees, and sodium glycolate is obtained, but the technology is too complex, the process reliability is not high, the cost is too high, and the practical application is difficult.
In order to achieve the purpose, the invention adopts the following technical scheme:
a method for recovering glycolic acid from CMC waste water comprises the following steps:
the first procedure, the wastewater is pretreated to remove cellulose ether residues, suspended matters, pigments and the like;
a second step of separating organic impurities by resin adsorption;
a third procedure, namely separating and desalting by an MVR technology;
a fourth procedure, desalting by an electrodialysis technology;
and fifthly, distilling and concentrating to obtain a glycolic acid product with higher purity.
Preferably, in the first step, the CMC wastewater is pretreated to remove suspended matters, sediments and the like in the wastewater, and the CMC wastewater is pretreated according to the size of the suspended matters in the wastewater, the used processes include grating, filtration, air flotation, flocculation and sedimentation and the like, and are combined with an ultrafiltration membrane separation technology, and the ultrafiltration membrane can adopt a roll-type membrane with the molecular weight cutoff of 1000 daltons, so that most of CMC residues and pigments can be effectively removed.
Preferably, in the second step, the resin used for adsorbing other organic impurities in the wastewater is a macroporous adsorption resin.
Preferably, the resin is activated for 1-4 h, then adsorbed for 1-4 h, and then desorbed for 2-4 h.
Preferably, the resin activating solvent is methanol or sodium hydroxide solution, and the resolving solution is methanol or sodium hydroxide solution.
Preferably, in the third step, the desalination is performed at 50-80 ℃ and under a vacuum degree of-0.085 MPa or less, wherein the desalination degree is based on the following characteristics: the content of sodium chloride in the desalting mother liquor is not more than 15 percent, or the content of sodium glycolate exceeds 40 percent.
Preferably, in the fourth step, in order to remove residual salts from the wastewater collected in the third step, the wastewater is acidified before entering the electrodialysis device to convert sodium glycolate into glycolic acid, the acidifying agent is hydrochloric acid or sulfuric acid, and the ratio of sodium glycolate to acid is 1-1.1: 1.
Preferably, the acidification process is to pump the desalted CMC wastewater into a reaction kettle, slowly add a certain amount of acid liquid under stirring, continuously stir for 1-2h at normal temperature and normal pressure, and obtain a glycolic acid crude solution after removing inorganic salt crystals by centrifugation or filtration.
Preferably, in the fifth step, the purpose is to purify the glycolic acid crude product by distillation and concentration, and the glycolic acid distillation process is completed in a system consisting of an evaporator, a circulating pump, a condenser and a vacuum pump; the main purpose of the process is to remove most of water through evaporation and separation so as to achieve the purpose of concentration; the specific process is that the low-concentration glycolic acid enters an evaporator for evaporation, wherein water forms water vapor, and condensed water is formed after condensation, so that the water vapor is removed; the concentration of the glycolic acid distillate left at the bottom of the kettle is gradually increased along with the evaporation of water until reaching 70 percent, and the pressure and the temperature in the distillation and concentration process are less than or equal to-0.093 MPa and less than or equal to 56 ℃.
Preferably, the process method is applied to the treatment and resource utilization of various CMC production wastewater.
The invention has the beneficial effects that: the invention provides a method for recovering glycolic acid from CMC wastewater, which has simple process and low cost, can obtain a glycolic acid product with higher purity, is effectively used for the treatment and resource utilization of various CMC wastewater, can not only efficiently treat the CMC wastewater, but also realize the recovery and utilization of byproducts.
Drawings
FIG. 1 is a process flow diagram of a method for recovering glycolic acid from CMC waste water according to the present invention.
In the figure: 1-1, acidifying the reaction kettle; 1-2 centrifuge; 1-3 intermediate tanks; 2-1, 3-1 circulating pump; 2-2 salt crystal separation tank; 2-3, 3-2 evaporators; 2-4 water-vapor separator; 2-5 and 3-3 condensers; 2-6, 3-4 vacuum pumps; 2-7 buffer tanks.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
The invention provides the following technical scheme: a method for recovering glycolic acid from CMC waste water comprises the following steps:
the first procedure, the wastewater is pretreated to remove cellulose ether residues, suspended matters and pigments;
a second step of separating organic impurities by resin adsorption;
a third procedure, namely separating and desalting by an MVR technology;
a fourth procedure, desalting by an electrodialysis technology;
and fifthly, distilling and concentrating to obtain a glycolic acid product with higher purity.
The method is completed by 5 procedures in two stages, wherein the first stage is a pretreatment stage which comprises the first to the third procedures and aims at removing CMC residues, suspended matters, pigments and sodium chloride so as to ensure the normal implementation of the second stage process; the second stage is the glycolic acid extraction stage, which includes the fourth and fifth steps (see fig. 1) for separating and purifying glycolic acid to form a product, which are carried out in complete sequence during the overall process.
More specifically, the first process is used for pretreating the CMC wastewater to remove suspended matters and sediments in the wastewater, and the CMC wastewater is pretreated according to the size of suspended matters in the wastewater by using the processes of grating, filtering, air flotation and flocculation sedimentation; the first process comprises three implementation steps: firstly, removing macromolecular components of CMC residues by an air floatation method; filtering through a bag type or filter element type filter to remove suspended matters; and thirdly, removing medium and small molecular components of the CMC residues through membrane ultrafiltration, wherein the molecular weight cut-off of the membrane is 1000 daltons, the working temperature is below 45 ℃, and the ultrafiltered light salt water enters the next working procedure.
The second procedure is to adsorb other organic impurities in the wastewater, the used resin is macroporous adsorption resin, the used resin is firstly activated for 1-4 h, then adsorbed for 1-4 h, and then desorbed for 2-4 h, the used resin activation solvent is methanol or sodium hydroxide solution, and the desorption solution is methanol or sodium hydroxide solution; the specific implementation process comprises the steps of soaking a certain amount of macroporous adsorption resin in methanol or sodium hydroxide for 2-4 hours, washing the macroporous adsorption resin with distilled water for multiple times after soaking is finished, then adding light salt water subjected to the first procedure, continuously adsorbing for 2-4 hours, collecting permeate, and entering the next procedure.
The third procedure is used for removing most of salt in the wastewater, and evaporation desalination is carried out at 50-80 ℃ and under the condition that the vacuum degree is less than or equal to-0.085 MPa; the specific implementation process is that the permeate after resin adsorption is added into an evaporator for evaporation, wherein water and some low-boiling point organic matters form steam in the process, condensed water is formed after the steam is condensed by a condenser and is removed, when the feed liquid is dehydrated and concentrated to reach the crystallization concentration of sodium chloride, namely more than 35 percent, the feed liquid containing salt crystals is pumped into a crystallization tank by a pump, and then the crystallized sodium chloride is separated and recovered by a centrifuge or by filtration. Because the concentration of sodium glycolate in the feed liquid is lower than that of sodium chloride, and the saturated concentration of the organic salt is far higher than that of sodium chloride and reaches more than 65%, during sodium chloride crystallization, sodium glycolate does not form crystals, and the sodium glycolate still remains in the mother liquid after solid-liquid separation.
A sodium glycolate extraction stage, as shown in fig. 1, namely a fourth process and a fifth process, wherein the fourth process is to remove residual salt in the wastewater collected from the third process, the wastewater is firstly acidified before entering an electrodialysis device to convert the sodium glycolate into the glycolic acid, a used acidifying reagent is hydrochloric acid or sulfuric acid, the ratio of the sodium glycolate to the acid is 1-1.1: 1, the acidification process is to pump the desalted CMC wastewater into a reaction kettle, slowly add a certain acid solution under stirring, continuously stir at normal temperature and normal pressure for 1-2 hours, and obtain a crude glycolic acid solution after removing inorganic salt crystals by centrifugation or filtration; the specific implementation mode of the acidification reaction is that the desalted mature mother liquor obtained in the third procedure is pumped into an acidification reaction kettle 1-1 through a pump, then a stirrer is started, concentrated hydrochloric acid is slowly added during stirring, stirring is continued for 1-2 hours under the conditions of normal temperature and normal pressure, sodium glycolate is converted into glycolic acid during the acidification reaction, meanwhile, the solubility of residual sodium chloride and sodium chloride generated during the acidification reaction is sharply reduced under the acidic condition to form crystals, the crystals are removed through a centrifugal machine 1-2, the separated liquid is crude liquid of glycolic acid, and the crude liquid is collected in an intermediate tank 1-3 and then enters the next procedure.
Further processing through a fifth process, namely distillation concentration, which comprises separating glycolic acid and water from the crude liquid, evaporating water to concentrate glycolic acid, and the specific implementation steps are that the crude liquid of glycolic acid is transferred to a salt crystal separation tank 2-2 through a circulating pump 2-1, flows into an evaporator 2-3, enters a condenser 2-5 through a water-vapor separator 2-4, starts a vacuum pump 2-6, obtaining low-concentration glycolic acid at 73-78 ℃ under-0.092 PMa-0.090 MPa, transferring the low-concentration glycolic acid in the buffer tank 2-7 to an evaporator 3-2 through a circulating pump 3-1, starting a vacuum pump 3-4, concentrating under the conditions that the pressure is lower than-0.093 MPa and the temperature is lower than 56 ℃ until the concentration of the glycolic acid reaches the requirement of a finished product of 70 percent.
The invention is further illustrated by the following examples.
Example 1
And (3) acidification reaction: 1000ml of desalted mature mother liquor is taken and added into a 2000ml beaker, 530ml of concentrated hydrochloric acid (36%) is slowly added during stirring, then stirring is carried out for 1 hour at normal temperature, then a suction bottle is used for suction filtration, filtrate is collected, and the concentration of glycolic acid, namely chloride, in the filtrate is sampled and analyzed. The results are shown in Table 1:
TABLE 1 Table of the concentrations of sodium glycolate and glycolic acid, i.e. chloride, before and after the acidification reaction
Figure BDA0003328682460000071
Example 2
Separation and distillation: from the experiment of example 1, 1000ml of filtered filtrate was taken and added to a water bath evaporator 2-3, a water bath heater was started to raise the temperature to 78 ℃, a vacuum pump 2-6 was started to adjust the negative pressure in the evaporator 2-3 to-0.092 PMa, then a cooling water inlet/outlet valve of a condenser 2-5 was opened to allow the evaporator 2-3 to evaporate continuously until no condensate flowed out, the amount of condensate and the remaining amount of unevaporated feed liquid remaining in a heating bottle of the evaporator 2-3 were collected and measured, and the glycolic acid content and the chloride content were sampled and analyzed. The results are shown in Table 2:
TABLE 2 Table for the quantification of condensate and residue in the separation and distillation and the analysis of the component contents
Serial number Sample (I) Quantity (V) Glycolic acid Chloride compound Crystalline sodium chloride
1 Condensate liquid 840ml 194.6g 1.45g Is free of
2 Residue of the reaction 125ml 48.4g 29.2g 78.3g
Example 3
Concentration and distillation: 700ml of the condensate collected in example 2 was taken out and added to a water bath evaporator 3-2, and the other operations were similar to those of example 2, except that the temperature of the water bath was adjusted to 56 ℃, the vacuum pump 3-4 was started, the negative pressure in the evaporator 3-2 was adjusted to-0.093 MPa, then the cooling water inlet/outlet valve of the condenser 3-3 was opened, and evaporation was continued until the concentration of glycolic acid in the concentrate reached 70%, and the condensate and the concentrate generated during evaporation were sampled and analyzed, respectively. The analytical results are shown in Table 3:
TABLE 3 table of the results of the concentration distillation analysis
Serial number Sample (I) Quantity (V) Glycolic acid (%) Chloride (%)
1 Concentrated solution 232ml 75 0.006
2 Condensed water 448ml 1.05 Is free of
In conclusion, the process method is applied to the treatment and resource utilization of various CMC production wastewater, has simple process and low cost, can obtain a glycolic acid product with higher purity, can not only efficiently treat the CMC wastewater, but also realize the recycling of byproducts.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.

Claims (10)

1. A method for recovering glycolic acid from CMC waste water is characterized by comprising the following steps:
the first procedure, the wastewater is pretreated to remove cellulose ether residues, suspended matters and pigments;
a second step of separating organic impurities by resin adsorption;
a third procedure, namely separating and desalting by an MVR technology;
a fourth procedure, desalting by an electrodialysis technology;
and fifthly, distilling and concentrating to obtain a glycolic acid product with higher purity.
2. The method for recovering glycolic acid from CMC waste water as claimed in claim 1, wherein said first process is used to pretreat CMC waste water to remove suspended matter and sediment in the waste water, and the CMC waste water is pretreated according to the size of suspended matter in the waste water by using the processes of grating, filtering, air flotation, flocculation and sedimentation.
3. The method for recovering glycolic acid from CMC waste water as claimed in claim 1, wherein said second process is used for adsorbing other organic impurities in the waste water, and the used resin is macroporous adsorption resin.
4. The method for recovering glycolic acid from CMC waste water as claimed in claim 2, wherein the resin is activated for 1-4 h, then adsorbed for 1-4 h, and then desorbed for 2-4 h.
5. The method for recovering glycolic acid from CMC waste water as claimed in claim 4, wherein the resin activating solvent is methanol or sodium hydroxide solution, and the desorption solution is methanol or sodium hydroxide solution.
6. The method for recovering glycolic acid from CMC waste water as claimed in claim 1, wherein said third process is used to remove most of salt in the waste water, and evaporation desalination is performed at 50-80 ℃ and vacuum degree of-0.085 MPa.
7. The method for recovering glycolic acid from CMC waste water according to claim 1, characterized in that, the said fourth process removes the residual salt from the waste water collected from the third process, the waste water is acidified before entering the electrodialysis device to convert sodium glycolate into glycolic acid, the acidifying agent is hydrochloric acid or sulfuric acid, and the ratio of sodium glycolate to acid is 1-1.1: 1.
8. The method for recovering glycolic acid from CMC waste water as claimed in claim 7, wherein the acidification process comprises pumping the desalted CMC waste water into a reaction kettle, slowly adding a certain acid solution under stirring, continuously stirring for 1-2h at normal temperature and pressure, centrifuging or filtering to remove inorganic salt crystals to obtain a glycolic acid crude liquid.
9. The method for recovering glycolic acid from CMC waste water as claimed in claim 1, wherein said fifth process is to purify the glycolic acid crude product by distillation concentration, the glycolic acid distillation process is completed in the system composed of evaporator, circulating pump, condenser and vacuum pump; the specific process is that the low-concentration glycolic acid enters an evaporator for evaporation, wherein water forms water vapor, and condensed water is formed after condensation, so that the water vapor is removed; the concentration of the glycolic acid distillate left at the bottom of the kettle is gradually increased along with the evaporation of water until reaching 70 percent, and the pressure and the temperature in the distillation and concentration process are less than or equal to-0.093 MPa and less than or equal to 56 ℃.
10. The method for recovering glycolic acid from CMC waste water according to claim 1, characterized in that, the process method is applied to the treatment and resource utilization of various CMC production waste water.
CN202111270790.1A 2021-10-29 2021-10-29 Method for recovering glycolic acid from CMC wastewater Pending CN113912236A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202111270790.1A CN113912236A (en) 2021-10-29 2021-10-29 Method for recovering glycolic acid from CMC wastewater

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202111270790.1A CN113912236A (en) 2021-10-29 2021-10-29 Method for recovering glycolic acid from CMC wastewater

Publications (1)

Publication Number Publication Date
CN113912236A true CN113912236A (en) 2022-01-11

Family

ID=79243543

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202111270790.1A Pending CN113912236A (en) 2021-10-29 2021-10-29 Method for recovering glycolic acid from CMC wastewater

Country Status (1)

Country Link
CN (1) CN113912236A (en)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109160660A (en) * 2018-09-20 2019-01-08 浙江三和食品科技有限公司 A kind of sodium carboxymethylcellulose produces the recovery method of hydroxyacetic acid in waste water
CN109205904A (en) * 2018-10-12 2019-01-15 江苏盛勤环境工程有限公司 The producing wastewater treatment of sodium cellulose glycolate
CN209668842U (en) * 2019-01-30 2019-11-22 杭州匠容道环境科技有限公司 Cellulose waste water desalination system based on electrodialytic technique
CN111393281A (en) * 2020-04-10 2020-07-10 高春燕 Environment-friendly clean production method of high-purity glycolic acid

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109160660A (en) * 2018-09-20 2019-01-08 浙江三和食品科技有限公司 A kind of sodium carboxymethylcellulose produces the recovery method of hydroxyacetic acid in waste water
CN109205904A (en) * 2018-10-12 2019-01-15 江苏盛勤环境工程有限公司 The producing wastewater treatment of sodium cellulose glycolate
CN209668842U (en) * 2019-01-30 2019-11-22 杭州匠容道环境科技有限公司 Cellulose waste water desalination system based on electrodialytic technique
CN111393281A (en) * 2020-04-10 2020-07-10 高春燕 Environment-friendly clean production method of high-purity glycolic acid

Similar Documents

Publication Publication Date Title
CN111592136A (en) Method and device for efficiently utilizing components of corn soaking water
CN110526512B (en) High-salt high-COD wastewater recovery zero-discharge system and process
CN101085734A (en) Method for purifying itaconic acid fermentation liquor or extracting itaconic acid from itaconic acid mother liquid by film device
CN110713432A (en) Preparation method of anhydrous electronic grade ethanol
CN102557316B (en) Pretreatment method of epoxy resin desalinization wastewater
CN111591967A (en) Recovery processing method of phosphoric acid waste acid
WO2011076690A1 (en) Method for purifying 1,2-propanediol from a fermentation broth
CN111573950B (en) Recovery treatment method of organic solvent-containing wastewater
KR20190080840A (en) Apparatus for treating brine discharged from desalination process of sea water
CN110015796B (en) Zero-discharge treatment system and process for nickel hydrometallurgy wastewater of mixed high-salt system
CN113912236A (en) Method for recovering glycolic acid from CMC wastewater
CN109665659B (en) Treatment and recycling system and process for soybean oil-making wastewater
CN109456146B (en) Method for separating and preparing high-purity 1,2,4-butanetriol from recombinant escherichia coli fermentation liquor
CN116102589A (en) Method for extracting sodium phytate from corn steep liquor
CN211921110U (en) Device for efficiently utilizing components of corn soaking water
JP3434848B2 (en) Treatment method for phenol-containing wastewater
JP2022075844A (en) Method for recovery of ketone and glycol from fermentation
CN114230076A (en) Metal surface treatment liquid recycling system and operation method thereof
CN110787638B (en) Concentration system and concentration method of pentanediamine
CN1253461C (en) Method for treating waste water of chinese yam saporin and recovering gluocose and hydrochloric acid by membrane integrating technique
CN102134135A (en) Method for recovering and purifying tetra-alkylammonium hydroxide from waste liquor containing tetra-alkylammonium hydroxide
KR101256613B1 (en) Recovery of high purity phosphoric acid from mixed waste acid
CN214088113U (en) Landfill leachate's processing and separation extraction element of its salt
CN110229046B (en) Device and method for extracting glycerol and glycerol-like alcohol from epoxy wastewater evaporation mother liquor
CN114044755B (en) Decolorization and purification method for ionic liquid

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
RJ01 Rejection of invention patent application after publication

Application publication date: 20220111

RJ01 Rejection of invention patent application after publication