CN1629112A - Clean reclaiming process for byproduct chloromethane of glyphosate acid - Google Patents
Clean reclaiming process for byproduct chloromethane of glyphosate acid Download PDFInfo
- Publication number
- CN1629112A CN1629112A CN 200410097717 CN200410097717A CN1629112A CN 1629112 A CN1629112 A CN 1629112A CN 200410097717 CN200410097717 CN 200410097717 CN 200410097717 A CN200410097717 A CN 200410097717A CN 1629112 A CN1629112 A CN 1629112A
- Authority
- CN
- China
- Prior art keywords
- methyl chloride
- technology
- methylal
- methyl
- 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.)
- Granted
Links
Landscapes
- Treating Waste Gases (AREA)
Abstract
The discharged exhaust gas during the glyphosate acid production process through phosphorous acid alkyl acid includes 20-90% of methyl chloride, methanol, formaldehyde dimethyl acetal, water, hydrogen chloride and other foreign matter, by solvent absorption of foreign matter, condensation impurity or charging part of the foreign matter such as methanol, formaldehyde dimethyl acetal into hydrochloride-containing liquid and converting it into methyl chloride, high purity of methyl chloride can be obtained. The process not only solves the problem of environmental pollution in the glyphosate acid production, the production cost can also be lowered substantially.
Description
The application is to be on July 23rd, 2002, open day to be that October 8, application number in 2003 are dividing an application of 02125282.3 Chinese patent application the applying date.
Technical field
The present invention relates to the method for purifying and recovering of hydrolysis tail gas in the glyphosphonic acid building-up process, more particular words is to produce the high yield recovery by product methyl chloride the tail gas that discharges from glyphosphonic acid, and this process does not produce secondary pollution.
Background technology
Glyphosate is the maximum and the fastest steriland herbicide of rate of growth of sales volume in the world, whole world glyphosate technicals ultimate production reaches 260,000 tons, and along with the succeeding in developing and promoting the use of of the genetically modified crops of resistance glyphosate, for the continuation development of glyphosate provides new opportunity.The two kinds of methods that mainly contain are produced in whole world glyphosate industrialization: the one, and the IDA method promptly is starting raw material with the diethanolamine, U.S. Meng Shan waits offshore company generally to adopt this technology; Another kind method is an alkyl esterification method, domestic big multiple enterprises adopts this technology, alkyl esterification method glyphosate preparation method is open at document DEOLSNO.P 2942898.6, method commonly used is with Paraformaldehyde 96 or formaldehyde in containing the methanol solvate of triethylamine heating for dissolving 5-15 minute, again glycine is added heating for dissolving in this solution, add dimethylphosphite after 30 minutes, under 60-70 ℃, carry out condensation reaction, finish through 30-120 minute afterreaction, adding hydrochloric acid then is hydrolyzed (being called hydrolyzing process), generate the hydrochloride of glyphosphonic acid, the glyphosphonic acid crystallization was separated out after underpressure distillation removed solvent methanol and excessive hydrochloric acid again, filter after scouring, filter cake is glyphosphonic acid, the glyphosate that contains triethylamine hydrochloride and minimal amounts of dissolved in mother liquor and the washing lotion is used to prepare 10% sodium glyphosate aqua in liquid caustic soda and after reclaiming triethylamine.With the solution rectifying (being called the solvent recuperation operation) that underpressure distillation steams, isolate wherein solvent methanol and by product methylal, raffinate carries out biochemical treatment.If produce glyphosphonic acid with trimethyl phosphite, technology is similar.
Employing is in the production of alkyl phosphite technology (comprising with the phosphorus trichloride being raw material synthesizing phosphorous acid dimethyl ester operation) synthesizing glyphosate acid of starting raw material with dimethylphosphite or trimethyl phosphite, produce a large amount of tail gas that contains methyl chloride at dimethylphosphite synthesis procedure and the synthetic hydrolyzing process of glyphosphonic acid, can be used as the production of products such as carboxymethyl cellulose, chloroprene rubber behind the methyl chloride reclaiming clean wherein.Patent of invention 99119970.7 (franchise the applicant) discloses a kind of industrial method that reclaims the methyl chloride that produces in the alkyl phosphite method glyphosphonic acid building-up process, adopt be hydrolysis tail gas through washing, alkali cleaning, dry tertiary treatment, the storage of recompression condensation liquefaction.But this technology comes with some shortcomings in the rate of recovery and environmental protection: 1. the rate of recovery is low.Owing to contain saturated or oversaturated methylal and methyl alcohol under the normal pressure in this tail gas, if can not when washing, be removed, bring dehumidification system into after, can cause the consumption of siccative higher, and the quality of methyl chloride is reclaimed in influence.But be subjected to the influence of methylal and methyl alcohol solubleness and rate of mass transfer in water, in order to guarantee to reclaim the quality of methyl chloride, need to wash with a large amount of water (6 tons of/ton methyl chloride), and there is certain solubility (0.38 grams per liter) in methyl chloride in water, the washing water yield causes that greatly the solution loss of methyl chloride in water increases, and influenced the rate of recovery; 2. contaminate environment.Though this technology can be with the most of recovery of the methyl chloride in the discharging tail gas, reduced the pollution of glyphosphonic acid production to environment, but making, the defective of this technology itself can not thoroughly solve environmental issue, organic compound such as the methylal in the tail gas, methyl alcohol, methyl chloride have been dissolved in a large amount of bath wateies, and these materials of low levels can't adopt economic method to reclaim, can only carry out biochemical treatment or discharging, cause pollution environment; If carry out biochemical treatment, because methylal is embarrassed biochemical substances with methyl chloride, it is higher that it is carried out processing cost.3. it is not good to reclaim the methyl chloride quality.The impurity (moisture content, methylal, methyl alcohol) that also contains in the byproduct chloromethane of glyphosate acid that adopts the described tertiary treatment technology of this technology to reclaim is too high, in methyl chlorosilane is synthetic, can form polymkeric substance or thermo-cracking at catalyst surface coking, knot charcoal with the target product reaction, thus influence production.
Summary of the invention
The objective of the invention is to for solving the above-mentioned problem that exists, a kind of novel method of alkyl phosphite method glyphosphonic acid hydrolysis tail gas clean-up is provided, and whole recovery technology is environmental protection, can realize cleaner production, thoroughly solves the influence of glyphosphonic acid suitability for industrialized production discharging tail gas to environment.
Glyphosphonic acid production discharging tail gas consists of:
| Methyl chloride | Air | Methyl alcohol | Methylal | Water | Hydrogenchloride | Other |
| 20-90 | ??8-20 | ??2-15 | 4-20 | ??2-10 | 1-5 | ??1-5 |
Methyl alcohol wherein, methylal are in saturated or hypersaturated state, the boiling point of methyl alcohol, methylal, methyl chloride is respectively 64.5 ℃ under normal pressure, 42.3 ℃,-23.73 ℃, the emergent pressure of methyl alcohol, methylal is 240 ℃, 215 ℃, far above 143 ℃ of methyl chloride, the method that therefore can adopt compression is with methyl alcohol in the gas phase and the most of condensation of methylal, thereby the absorption that can reduce subsequent handling is significantly loaded.Methyl chloride saturated vapor pressure at normal temperatures is 506.63kpa (absolute pressure), therefore tail gas can be compressed to 0.11-1Mpa (absolute pressure), for guaranteeing that methyl alcohol separates with the most economical of methyl chloride with methylal, preferred pressure is 0.45-0.55Mpa (absolute pressure), the separation that is liquefied of methyl alcohol more than 80% and methylal will be arranged this moment, this phlegma mainly contains methyl alcohol and methylal, can return the solvent recuperation operation in the glyphosphonic acid production, separate the 60-95% methylal, can be used as commodity selling, 〉=98% methyl alcohol can be as the solvent of synthesizing glyphosate acid.
To wash the methyl chloride solution loss that is caused with water or reduce contained organic substance influence problem of environment in the washing water that cause therefrom in order to reduce, also having a kind of technical scheme is that the tail gas that will contain methyl chloride makes its almost completely condensation except that contained non-condensable gasess such as air by pressurization and refrigerative method, this moment, pressure can be 0.4-2Mpa (absolute pressure), and temperature is-50-40 ℃ (technical professional can also adopt the combination of multiple pressure and temperature to reach same effect certainly).Components such as contained methyl chloride, methyl alcohol, methylal are separated from phlegma by the method for rectifying again, because the boiling point of methyl chloride is minimum, can at first obtain from cat head, bottom product is the mixture of components such as methyl alcohol, methylal, and this mixture is again through separating methyl alcohol and the methylal to obtain higher concentration.
Because most methyl alcohol and methylal separated (being called pre-treatment), can significantly reduce the consumption of washing water, in order to strengthen rate of mass transfer and to improve the content of methyl alcohol and methylal in the washing water, adopt the circulation absorption technique, single tower can be adopted according to tolerance in the absorption tower, perhaps multitower serial or parallel connection, working pressure is 0.08-0.3Mpa (absolute pressure).Contain methyl alcohol and methylal that weight concentration is 10-30% in the washing water, the solvent recuperation operation that also can return in the glyphosphonic acid production is separated.
Still contain carbonic acid gas, hydrogenchloride or vaporific hydrochloric acid in the gas after washing, can also be that potassium hydroxide, carbonate (sodium, the potassium) aqueous solution etc. of 10-40% absorbs with weight concentration except that the liquid caustic soda of patent of invention 99119970.7 disclosed 30% weight concentrations, factor preferred weight concentration such as comprehensive cost be the aqueous sodium hydroxide solution of 25-35%.
The water that still contains the 100-20000ppm that has an appointment in the gas after above-mentioned processing, still do not meet the requirement of industry standard, patent of invention 99119970.7 adopts the vitriol oil to carry out drying, but only use this method, still contain the water that is about 30ppm in the methyl chloride after the processing, though meet the industry standard of methyl chloride, very harsh to the requirement of the used methyl chloride of synthesizing methyl-chloro-silane, water content is low more favourable more to synthesizing methyl-chloro-silane.It is considered herein that and can also adopt other method that can remove micro-moisture, simple to operate, effective as adopting the solid matter that can absorb moisture to absorb moisture.Therefore can adopt behind vitriol oil drying process again with or the solid adsorbent that directly can absorb moisture with copper sulfate, calcium sulfate, calcium chloride, yellow soda ash, water glass, Vanadium Pentoxide in FLAKES, calcium oxide, 3A aluminum oxide molecular sieve etc. dewater, moisture content can be reduced to below the 15ppm after this art breading.
Also the tail gas of tail gas or treated mistake can be absorbed methyl chloride by organic solvent, method by stripping or rectifying obtains comparatively purified methyl chloride again, used organic solvent can be halogenated hydrocarbons, as first chlorination carbon, ethylene dichloride chlorinated aliphatic hydrocarbon, chlorination aromatic hydrocarbons such as mono chloro benzene, dichlorobenzene, m-chlorotoluene; Alcohols is as methyl alcohol, ethanol etc.; Ketone such as acetone, butanone etc.Require solvent for use higher boiling point concerning methyl chloride has higher solubleness and relative methyl chloride, can think that tetracol phenixin is to select preferably.
Contain impurity such as more methyl alcohol, methylal in the synthetic discharging of the glyphosphonic acid tail gas, and the purpose product is high-load methyl chloride, except that the method for above-mentioned separating impurity, the method of another efficient and cost-effective is by chemical reaction impurity conversion to be become the purpose product, huge separating device can be save on the one hand, more purpose product can also be obtained on the other hand.Methylal can be converted into methyl chloride, formaldehyde and water in the presence of hydrogenchloride; Methyl alcohol also can be converted into methyl chloride in the presence of the zinc chloride in hydrochloric acid or hydrogen chloride gas.Therefore carry out other handle before earlier with described tail gas by containing zine ion hydrochloric acid soln or mix laggard promoting the circulation of qi solid catalysis reaction with hydrogenchloride methyl alcohol and methylal are converted into methyl chloride also be a kind of method preferably, used catalyzer is the particulate alumina that contains zinc chloride.
Embodiment
It is considered herein that easily the technical scheme of industrializing implementation is: (1) pre-treatment: after described hydrolysis tail gas is sent into the gas holder buffering, with compressor compresses and cooling, the control compressor delivery pressure does not liquefy with methyl chloride and is advisable, be generally 0.1-1Mpa (absolute pressure), methylal and methyl alcohol in the hydrolysis tail gas are liquefied because of being in hypersaturated state, separate with the methylal and the methyl alcohol of separator, get pre-treatment gas liquefaction.The present invention is preferably 0.35-0.4Mpa (absolute pressure), and the washing hydration of isolated methylal and methyl alcohol and a step operation is also handled.(2) circulation washing: pre-treatment gas is removed the not methylal and the methyl alcohol of liquefaction in the pre-treatment gas by single-stage washing or plural serial stage washing, must wash gas.The washing of should pressurizeing of this step to improve methylal and the solubleness of methyl alcohol in water, reduces washing water consumption (can reduce to 1-2 ton/ton), and working pressure is 0.08-0.3Mpa (absolute pressure), is preferably 0.15-0.2Mpa (absolute pressure).Methylal and methanol content are higher in the washing water after the absorption, can with send methanol recovery system to separate purification after the methylal of pre-treatment discharging and methyl alcohol merge with rectifying tower, the methyl alcohol of recovery is used for the synthetic of glyphosphonic acid, methylal is as commodity selling.(3) alkali lye absorbs: with the liquid caustic soda washing of above-mentioned gas by 10-40%, remove acidic substance, used absorption agent also can for the hydrogen of 10-40% according to yellow soda ash or the salt of wormwood of changing potassium or 10-40%, from considering economically, the present invention is preferably sodium hydroxide, and concentration is 25-35%.(4) drying: will handle that back gas passes through vitriol oil plural serial stage drying after molecular sieve adsorption or anhydrous metal salt drying through the last step, compressed again condensation promptly gets the methyl chloride finished product.
Characteristics of the present invention are the methyl chloride rate of recovery height in the glyphosphonic acid tail gas, quality better, and methyl alcohol in the tail gas and methylal can be made full use of.
The method that is used for removing the impurity component of the synthetic discharging of glyphosphonic acid tail gas described in the invention can be carried out multiple combination, do not do the limit explanation in the present invention, should be included within the present invention yet even the combination of the processing scheme of being done on basis of the present invention is different from the described scheme of embodiment.
Embodiment: it is 4M that the exhaust emissions point from glyphosphonic acid and dimethylphosphite production respectively draws pipeline to a volume
3Surge tank through spinner-type flowmeter, adopts down routine scheme to handle methyl chloride and methylal weight content in the usefulness gas spectrum analysis exit gas of back respectively, in each experimentation from surge tank sampling analysis methyl chloride content wherein.
Embodiment 1: adopt patent of invention 99119970.7 described tertiary treatment, both earlier through big water gaging spray washing, washing is to be 89mm at four groups of diameters, high 1000mm, in fill out in the packing tower of glass rectangular saddle ring and carry out, washing gas absorbs through 30% liquid caustic soda, 85% vitriol oil again.
Embodiment 2: be compressed to 0.3Mpa (absolute pressure) earlier, be cooled to 15 ℃ through condenser, gas phase washes with water through two groups of above-mentioned packing towers again, and washing gas absorbs through 35% liquid caustic soda, 90% vitriol oil again, keeps system pressure and is not less than 0.2Mpa (absolute pressure).
Embodiment 3: be compressed to 5Mpa (absolute pressure) earlier, be cooled to-5 ℃ with chilled brine, get rid of the experiment of again phlegma being introduced through being incubated processing behind the non-condensable gases and use in the distillation tower, keep tower still temperature and be no more than 5 ℃, the tower internal pressure is 0.2Mpa (absolute pressure), analyzes the overhead gas phase composite.
Embodiment 4: is the stainless steel tube of 25mm with exsiccant with the aluminium sesquioxide granular solids filling diameter that zinc chloride soaks, adopt the electric heating type of heating, gas is mixed the back feed this reactor with the hydrogenchloride that parses from hydrochloric acid, and to keep temperature of reaction be 120-180 ℃, adopts the method for embodiment 1 to handle exit gas again.
Embodiment 5: pass through the anhydrous cupric sulfate drying again after embodiment 2 handles.
Embodiment 6: adopt embodiment 1 described packing tower, replace water to absorb with tetracol phenixin, temperature is controlled at 20-30 ℃, pressure 0.6-1Mpa (absolute pressure).Through embodiment 3 described distillation tower distillations, the control tower internal pressure is 0.05Mpa (absolute pressure) to absorption liquid again, and cat head is controlled at 0-10 ℃ with chilled brine, adopts the method for embodiment 1 to handle exit gas again.
The experimental result tabulation
| Sequence number | Methyl chloride weight content (%) | Impurity weight content ppm | ||
| Surge tank | Outlet | Methylal | Water | |
| ????1 | ????62.2 | ????99.5 | ????35 | ????40 |
| ????2 | ????64.5 | ????99.8 | ????28 | ????32 |
| ????3 | ????62.3 | ????98.1 | ????80 | ????68 |
| ????4 | ????63.7 | ????99.7 | ????30 | ????35 |
| ????5 | ????62.8 | ????99.9 | ????26 | ????10 |
| ????6 | ????62.0 | ????99.7 | ????30 | ????27 |
Claims (12)
1. technology that reclaims the methyl chloride that produces in the glyphosphonic acid production process is characterized in that:
(1) collects discharge tail gas in the glyphosphonic acid production process;
(2) adopt isolating method to handle collected tail gas, methyl chloride content is wherein increased, wherein this separation method comprises that the fluid that will contain methyl chloride by organic solvent, adopts the method that absorbs that the methyl chloride in the described fluid is changed in the solvent.
2. according to the technology of claim 1, being characterized as of the methyl chloride that is reclaimed wherein: 1. the weight content of methyl chloride is 20-99.99%; 2. contain feature impurity methylal, its weight content is 0.1ppm-80%.
3. according to the technology of claim 1, being characterized as of the methyl chloride that is reclaimed wherein: 1. the weight content of methyl chloride is 99-99.99%; 2. the weight content of feature impurity methylal is 0.1-100ppm.
4. according to the technology of claim 1, being characterized as of wherein said glyphosphonic acid: adopting dimethylphosphite or trimethyl phosphite is that the alkyl phosphite method of one of main raw material is produced.
5. according to the technology of claim 3, wherein said glyphosphonic acid production technique comprises phosphorus trichloride synthesizing phosphorous acid dimethyl ester or trimethyl phosphite as one of glyphosphonic acid synthesis procedure.
6. according to the technology of claim 1, it further comprises and will contain the absorption liquid desorption of methyl chloride and other impurity component and separate.
7. according to the technology of claim 1 or 6, wherein implementing to carry out a kind of method for transformation before the described separation method, this method for transformation is the collected tail gas that contains methyl chloride to be fed in the solution that contains hydrogenchloride or with hydrogenchloride be mixed into reactor, and wherein methyl alcohol and methylal partly or entirely changed into methyl chloride.
8. according to the technology of claim 1, wherein said organic solvent is that carbonatoms is that halohydrocarbon, ketone, alcohol or the carbonatoms of 1-10 is the hydrocarbon of 4-16.
9. technology according to Claim 8, wherein said organic solvent is a tetracol phenixin.
10. according to the technology of claim 6, it comprises that also the fluid that will contain methyl chloride adopts the method for absorption to make the wherein aqueous content decline of institute by the solid adsorbent that can absorb water.
11. according to the technology of claim 10, wherein said solid adsorbent is oxide compound or the anhydrous metal salt that water sorption is arranged.
12. according to the technology of claim 11, wherein said oxide compound or anhydrous metal salt are copper sulfate, calcium sulfate, calcium chloride, yellow soda ash, water glass, Vanadium Pentoxide in FLAKES, calcium oxide or 3A aluminum oxide molecular sieve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410097717 CN1289448C (en) | 2002-07-23 | 2002-07-23 | Clean reclaiming process for byproduct chloromethane of glyphosate acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410097717 CN1289448C (en) | 2002-07-23 | 2002-07-23 | Clean reclaiming process for byproduct chloromethane of glyphosate acid |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02125282 Division CN1199921C (en) | 2002-07-23 | 2002-07-23 | Technique for cleanly recovering byproduct methyl chloride of glyphosate acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1629112A true CN1629112A (en) | 2005-06-22 |
| CN1289448C CN1289448C (en) | 2006-12-13 |
Family
ID=34847953
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200410097717 Expired - Lifetime CN1289448C (en) | 2002-07-23 | 2002-07-23 | Clean reclaiming process for byproduct chloromethane of glyphosate acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1289448C (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101337861B (en) * | 2007-12-26 | 2011-10-05 | 浙江新安化工集团股份有限公司 | Method for purifying and recovering methyl chloride of glyphosate byproduct |
| US8669396B2 (en) | 2009-05-18 | 2014-03-11 | Monsanto Technology Llc | Recovery of phosphorus values and salt impurities from aqueous waste streams |
| CN103691257A (en) * | 2013-12-25 | 2014-04-02 | 湖北泰盛化工有限公司 | Recycling process and equipment for glyphosate exhaust gas absorption liquid |
| CN105713038A (en) * | 2016-03-19 | 2016-06-29 | 安徽东至广信农化有限公司 | Chloromethane acid-pickling process used during glyphosate production |
| CN105753901A (en) * | 2016-03-19 | 2016-07-13 | 安徽东至广信农化有限公司 | Technology for recovering chloromethane washing wastewater in glyphosate production |
| CN108586190A (en) * | 2018-07-31 | 2018-09-28 | 山东海昆化工技术有限公司 | A method of recycling chloromethanes from chloromethanes exhaust gas |
| CN108863712A (en) * | 2018-08-15 | 2018-11-23 | 无锡智归科技有限公司 | A kind of glyphosate byproduct chloromethanes extracting and purifying method |
| CN110204416A (en) * | 2019-05-29 | 2019-09-06 | 华陆工程科技有限责任公司 | The recovery method of chloromethanes tail gas in a kind of chemical production process |
| CN111170826A (en) * | 2020-03-16 | 2020-05-19 | 浙江新安化工集团股份有限公司 | Clean recovery system and clean recovery process for chloromethane in glyphosate production tail gas |
| CN111269089A (en) * | 2020-03-16 | 2020-06-12 | 浙江新安化工集团股份有限公司 | Method and system for recovering hydrolysis tail gas of glyphosate synthetic liquid |
| CN112441872A (en) * | 2019-08-31 | 2021-03-05 | 浙江工业大学 | Method for treating waste sulfuric acid generated in industrial production of glyphosate by using glycine method |
-
2002
- 2002-07-23 CN CN 200410097717 patent/CN1289448C/en not_active Expired - Lifetime
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101337861B (en) * | 2007-12-26 | 2011-10-05 | 浙江新安化工集团股份有限公司 | Method for purifying and recovering methyl chloride of glyphosate byproduct |
| US8669396B2 (en) | 2009-05-18 | 2014-03-11 | Monsanto Technology Llc | Recovery of phosphorus values and salt impurities from aqueous waste streams |
| US9394173B2 (en) | 2009-05-18 | 2016-07-19 | Monsanto Technology Llc | Recovery of phosphorus values and salt impurities from aqueous waste streams |
| CN103691257B (en) * | 2013-12-25 | 2016-02-10 | 湖北泰盛化工有限公司 | Glyphosate tail gas absorption liquid utilization process and equipment thereof |
| CN103691257A (en) * | 2013-12-25 | 2014-04-02 | 湖北泰盛化工有限公司 | Recycling process and equipment for glyphosate exhaust gas absorption liquid |
| CN105713038A (en) * | 2016-03-19 | 2016-06-29 | 安徽东至广信农化有限公司 | Chloromethane acid-pickling process used during glyphosate production |
| CN105753901A (en) * | 2016-03-19 | 2016-07-13 | 安徽东至广信农化有限公司 | Technology for recovering chloromethane washing wastewater in glyphosate production |
| CN108586190A (en) * | 2018-07-31 | 2018-09-28 | 山东海昆化工技术有限公司 | A method of recycling chloromethanes from chloromethanes exhaust gas |
| CN108863712A (en) * | 2018-08-15 | 2018-11-23 | 无锡智归科技有限公司 | A kind of glyphosate byproduct chloromethanes extracting and purifying method |
| CN110204416A (en) * | 2019-05-29 | 2019-09-06 | 华陆工程科技有限责任公司 | The recovery method of chloromethanes tail gas in a kind of chemical production process |
| CN112441872A (en) * | 2019-08-31 | 2021-03-05 | 浙江工业大学 | Method for treating waste sulfuric acid generated in industrial production of glyphosate by using glycine method |
| CN111170826A (en) * | 2020-03-16 | 2020-05-19 | 浙江新安化工集团股份有限公司 | Clean recovery system and clean recovery process for chloromethane in glyphosate production tail gas |
| CN111269089A (en) * | 2020-03-16 | 2020-06-12 | 浙江新安化工集团股份有限公司 | Method and system for recovering hydrolysis tail gas of glyphosate synthetic liquid |
| CN111170826B (en) * | 2020-03-16 | 2023-08-22 | 浙江新安化工集团股份有限公司 | Clean recovery system and clean recovery process for chloromethane in tail gas from glyphosate production |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1289448C (en) | 2006-12-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1199921C (en) | Technique for cleanly recovering byproduct methyl chloride of glyphosate acid | |
| CN101012146B (en) | Method of separating and recovering methyl chloride from methyl chloride mixture gas | |
| CN1289448C (en) | Clean reclaiming process for byproduct chloromethane of glyphosate acid | |
| CN101337861B (en) | Method for purifying and recovering methyl chloride of glyphosate byproduct | |
| CN105503492A (en) | MTP (methanol to propylene) device and novel separation process thereof | |
| CN102101821A (en) | Recovery method of monochloro methane | |
| EA009531B1 (en) | Process for converting oxygenate feedstock to olefins and apparatus therefor | |
| CN104447198B (en) | Separation technology for preparation of isopropanol by acetone hydrogenation | |
| CN1288118C (en) | Clean reclaiming process for byproduct chloromethane of glyphosate acid | |
| CN102781890A (en) | Process for removing oxygenated contaminants from an hydrocarbon stream | |
| CN100447120C (en) | Technological process for refining trimethylolpropane | |
| EP1752433B1 (en) | Improved drying process for linear alpha-olefins | |
| CN112473314A (en) | Environment-friendly treatment method for 3-chloropropyltrichlorosilane synthesis tail gas | |
| CN113247862A (en) | High-purity electronic-grade hydrogen chloride production device and process | |
| CN105480948B (en) | Method and system for recycling byproduct hydrogen chloride in fatty acid or fatty acyl chloride chlorination production process | |
| CN216427170U (en) | Deep recovery system for chloromethane | |
| CN113929555B (en) | Method and device for recovering byproduct chloromethane for preparing glyphosate or dimethyl phosphite | |
| CN108383084B (en) | Hydrogen chloride emission each component recycling and reusing method in organic chlorination | |
| CN101318877B (en) | Process for recycling chloromethane generated in cartap production process | |
| CN109550359B (en) | Utilization method for recovering components in purge gas by using efficient absorbent | |
| CN209940867U (en) | Production system of high-purity 1, 4-butanediol | |
| CN115055132B (en) | Production process and device for preparing ethylene by ethanol dehydration | |
| CN216427171U (en) | Clean recovery system of methyl chloride in glyphosate and dimethyl phosphite production tail gas | |
| CN220861473U (en) | Device for synthesizing chloroethylene by mercury-free catalyst two-stage reaction | |
| CN112961026B (en) | Acetylene purification linkage control type trans-1, 2-dichloroethylene preparation system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20061213 |