CN106748637A - A kind of glyphosate hydrolyzing tail gas recovery method - Google Patents
A kind of glyphosate hydrolyzing tail gas recovery method Download PDFInfo
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- CN106748637A CN106748637A CN201610984916.4A CN201610984916A CN106748637A CN 106748637 A CN106748637 A CN 106748637A CN 201610984916 A CN201610984916 A CN 201610984916A CN 106748637 A CN106748637 A CN 106748637A
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- C07—ORGANIC CHEMISTRY
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- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
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Abstract
The invention discloses a kind of glyphosate hydrolyzing tail gas recovery method, belong to glyphosate production technical field.The described method comprises the following steps：A. alkali is added to be neutralized to alkalescent glyphosate hydrolyzing tail gas；B. the alkalescent gas for step A being obtained is passed through weight-removing column, and the mixed gas of tower top are condensed through first-stage condenser, obtain the mixing lime set of methyl alcohol and dimethoxym ethane；C. uncooled methyl chloride gas in step B and uncooled complete dimethoxym ethane gas are passed through secondary condenser, obtain the mixing lime set of dimethoxym ethane and chloromethanes；D. the methyl alcohol and the mixing lime set of dimethoxym ethane for step B being obtained are placed in product tower, obtain methanol product and dimethoxym ethane product；E. the dimethoxym ethane and the mixing lime set of chloromethanes for step C being obtained are placed in recovery tower, obtain dimethoxym ethane product and chloromethanes product；F. the uncooled methyl chloride gas of step C are entered into chloromethanes recovery system.The present invention has processing method simple, low cost, the product purity of recovery advantage high.
Description
Technical field
The present invention relates to a kind of glyphosate hydrolyzing tail gas recovery method, belong to glyphosate production technical field.
Background technology
Glyphosate is global sales maximum and the most fast herbicide kind of growth rate, and it is main that the country prepares glyphosate at present
There are alkyl esterification method and IDA methods.Alkyl esterification method technique is with paraformaldehyde, amion acetic acid, dimethylphosphite, methyl alcohol, triethylamine
Raw material, through depolymerization, addition, condensation reaction in synthesis reactor, is subsequently adding 30% hydrochloric acid solution and is hydrolyzed reaction.Hydrolysis
In presence of hydrochloric acid, methyl is broken two methoxyl groups in intensification desolvation process on phosphono with epoxide, produces methyl chloride gas,
Main component is chloromethanes, methyl alcohol, dimethoxym ethane and moisture in the hydrolysis tail gas, and a small amount of hydrogen chloride impurity.Traditional handicraft is led to
Cross to hydrolysis tail gas condensing, methyl alcohol, dimethoxym ethane, water turn into liquid phase, and chloromethanes is gas phase, and gas phase chloromethanes is through washing, alkali cleaning, sulphur
Sour drying reaches purification purpose and obtains methyl chloride gas, and byproduct chloromethane can be obtained after compressed, condensation, and tail gas condensing liquid phase is through adding
Alkali is neutralized as neutral or alkalescence enters dimethoxym ethane, methanol rectifying tower, obtains by-product dimethoxym ethane and methyl alcohol, and it is sweet that methyl alcohol is back to grass
In phosphine synthesis technique.Traditional handicraft is disadvantageous in that：Methyl alcohol, dimethoxym ethane, water etc. are all condensed, rectifying is reheated, significantly
Waste heat.
In the prior art, the disclosure of the invention such as Publication No. CN103752158A is grasped by partial condensation mode
Make, energy utilization increases compared with traditional approach capacity usage ratio, but secondly in level condensation process, due to dimethoxym ethane and methyl alcohol
Intersolubility, the more dimethoxym ethane of condensation process is dissolved in the methyl alcohol of condensation, cannot be separated in methanol rectifying tower distillation process, shadow
Ring methanol quality.
And for example, another exhaust gas treating method of the disclosure of the invention of Publication No. CN104353339B, by first using at alkali
Reason tail gas, adjusts pH value, then by after fore-running, dehydration fore-running, condensed device fore-running obtains methyl alcohol and gaseous mixture, gaseous state
Finished product dimethoxym ethane is obtained after the pressurized condensation of mixture, decompression；Fixed gas obtains finished product chloromethanes through drying, compression, condensation.Should
Although method is not first to condense, the mode of reheating rectifying, chloromethanes complex disposal process, dimethoxym ethane contains in methyl chloride gas
Amount is high, needs to consume a large amount of sulfuric acid in its drying process, and processing cost is high；Simultaneously the dimethoxym ethane purity that obtains also only 80~
90%, it is impossible to obtain high-purity methylal.
The content of the invention
Present invention seek to address that glyphosate hydrolyzing tail gas complex disposal process, high cost, dimethoxym ethane product in the prior art
A kind of not high enough problem of purity, there is provided new glyphosate hydrolyzing tail gas recovery method, low cost simple with processing method,
The product purity of recovery advantage high.
In order to realize foregoing invention purpose, technical scheme is as follows：
A kind of glyphosate hydrolyzing tail gas recovery method, it is characterised in that：Comprise the following steps：
A. neutralize
Glyphosate hydrolyzing tail gas plus alkali are neutralized to alkalescent, with protection equipment；
B. one-level condensation
The alkalescent gas that step A is obtained is passed through weight-removing column, and the mixed gas of tower top are condensed through first-stage condenser, obtain methyl alcohol
With the mixing lime set of dimethoxym ethane；
C. B-grade condensation
Uncooled methyl chloride gas in step B and uncooled complete dimethoxym ethane gas are passed through secondary condenser, first is obtained
The mixing lime set of acetal and chloromethanes；
D. the methyl alcohol and the mixing lime set of dimethoxym ethane for step B being obtained are placed in product tower, and bottom of towe obtains methanol product, methanol content
99.5%, the condensed device condensation of top gaseous phase obtains dimethoxym ethane product, dimethoxym ethane content 80~90%, and yield is that dimethoxym ethane product is total
The 30~40% of amount；
E. the dimethoxym ethane and the mixing lime set of chloromethanes for step C being obtained are placed in recovery tower, and bottom of towe obtains dimethoxym ethane product, tower top
The condensed device condensation of gas phase obtains chloromethanes product；
F. the uncooled methyl chloride gas of step C are entered into chloromethanes recovery system, finished product is obtained by drying, compression, condensation
Chloromethanes；It is the 20~50% of chloromethanes tail gas total amount not coagulate gas.
Further, in step A, described plus alkali is neutralized to alkalescent, and the pH value for hydrolyzing tail gas is 8~10.
In step B, the bottom of towe optimum temperature of the weight-removing column is 105~115 DEG C；62~70 DEG C of tower top optimum temperature.
In step B, the optimum temperature of the first-stage condenser is 40~60 DEG C.
In step C, the optimum temperature of the secondary condenser is -15~0 DEG C.
In step D, the bottom of towe optimum temperature of the product tower is 65~78 DEG C；42~50 DEG C of tower top optimum temperature.
In step E, 112-125 DEG C of the bottom of towe optimum temperature of the recovery tower；38~45 DEG C of tower top optimum temperature；Operation pressure
The Mpa of power 0.75~0.9.
In step E, the purity of the dimethoxym ethane product is 95~99.5%.
In step E, the purity of the chloromethanes product is 99.5~99.9%.
Beneficial effects of the present invention：
The improvement that the present invention passes through process, classification treatment waste gas, is condensed into mixing lime set, significantly by chloromethanes and dimethoxym ethane
The chloromethanes tail gas for entering recovery system is reduced, chloromethanes cost recovery is reduced；Dimethoxym ethane and chloromethanes are separated in recovery tower,
Solve containing chloromethanes in traditional handicraft dimethoxym ethane product, the technical barrier containing dimethoxym ethane in chloromethanes tail gas improves first contracting
The purity and the rate of recovery of aldehyde and chloromethanes；95~99.5% high-quality dimethoxym ethane is obtained in recovery tower simultaneously, product is enhanced
Added value.In addition, the recovery method is simple to operate, thermal energy consumption is low, greatly reduces production cost, improves enterprise competitiveness.
Specific embodiment
The present invention is described in further detail with reference to embodiment, but embodiments of the present invention not limited to this.
Embodiment 1
A kind of glyphosate hydrolyzing tail gas recovery method, comprises the following steps：
A. neutralize
Glyphosate hydrolyzing tail gas plus alkali are neutralized to alkalescent；
B. one-level condensation
The alkalescent gas that step A is obtained is passed through weight-removing column, and the mixed gas of tower top are condensed through first-stage condenser, obtain methyl alcohol
With the mixing lime set of dimethoxym ethane；
C. B-grade condensation
Uncooled methyl chloride gas in step B and uncooled complete dimethoxym ethane gas are passed through secondary condenser, first is obtained
The mixing lime set of acetal and chloromethanes；
D. the methyl alcohol and the mixing lime set of dimethoxym ethane for step B being obtained are placed in product tower, and bottom of towe obtains methanol product, top gaseous phase
Condensed device condensation obtains dimethoxym ethane product；
E. the dimethoxym ethane and the mixing lime set of chloromethanes for step C being obtained are placed in recovery tower, and bottom of towe obtains dimethoxym ethane product, tower top
The condensed device condensation of gas phase obtains chloromethanes product；
F. the uncooled methyl chloride gas of step C are entered into chloromethanes recovery system.
In the present embodiment, in step A, described plus alkali is neutralized to alkalescent, and the pH value for hydrolyzing tail gas is 8.
In step B, the column bottom temperature of the weight-removing column is 105 DEG C, and tower top temperature is 68 DEG C.
In step B, the temperature of the first-stage condenser is 50 DEG C.
In step C, the temperature of the secondary condenser is -15 DEG C.
In step D, the column bottom temperature of the product tower is 68 DEG C, and tower top temperature is 45 DEG C.
In step E, the column bottom temperature of the recovery tower is 115 DEG C, and tower top temperature is 45 DEG C, and operating pressure is 0.80MPa.
The product that the present embodiment is obtained：The purity of methyl alcohol is 99.8%, methyl alcohol water content 0.07%；The purity of dimethoxym ethane is
96.5%, dimethoxym ethane water content 0.15%；The purity of chloromethanes is more than 99.5%, moisture 0.030%, acidity 0.0050%.
Embodiment 2
A kind of glyphosate hydrolyzing tail gas recovery method, comprises the following steps：
A. neutralize
Glyphosate hydrolyzing tail gas plus alkali are neutralized to alkalescent；
B. one-level condensation
The alkalescent gas that step A is obtained is passed through weight-removing column, and the mixed gas of tower top are condensed through first-stage condenser, obtain methyl alcohol
With the mixing lime set of dimethoxym ethane；
C. B-grade condensation
Uncooled methyl chloride gas in step B and uncooled complete dimethoxym ethane gas are passed through secondary condenser, first is obtained
The mixing lime set of acetal and chloromethanes；
D. the methyl alcohol and the mixing lime set of dimethoxym ethane for step B being obtained are placed in product tower, and bottom of towe obtains methanol product, top gaseous phase
Condensed device condensation obtains dimethoxym ethane product；
E. the dimethoxym ethane and the mixing lime set of chloromethanes for step C being obtained are placed in recovery tower, and bottom of towe obtains dimethoxym ethane product, tower top
The condensed device condensation of gas phase obtains chloromethanes product；
F. the uncooled methyl chloride gas of step C are entered into chloromethanes recovery system.
In the present embodiment, in step A, described plus alkali is neutralized to alkalescent, and the pH value for hydrolyzing tail gas is 10.
In step B, the column bottom temperature of the weight-removing column is 115 DEG C, and tower top temperature is 59 DEG C.
In step B, the temperature of the first-stage condenser is 60 DEG C.
In step C, the temperature of the secondary condenser is 0 DEG C.
In step D, the column bottom temperature of the product tower is 72 DEG C, and tower top temperature is 48 DEG C.
In step E, the column bottom temperature of the recovery tower is 125 DEG C, and tower top temperature is 50 DEG C, and operating pressure is 0.9MPa.
The product that the present embodiment is obtained：The purity of methyl alcohol is 99.7%, methyl alcohol water content 0.09%；The purity of dimethoxym ethane is
97.0%, dimethoxym ethane water content 0.11%；The purity of chloromethanes is more than 99.5%, moisture 0.025%, acidity 0.0045%.
Embodiment 3
A kind of glyphosate hydrolyzing tail gas recovery method, comprises the following steps：
A. neutralize
Glyphosate hydrolyzing tail gas plus alkali are neutralized to alkalescent；
B. one-level condensation
The alkalescent gas that step A is obtained is passed through weight-removing column, and the mixed gas of tower top are condensed through first-stage condenser, obtain methyl alcohol
With the mixing lime set of dimethoxym ethane；
C. B-grade condensation
Uncooled methyl chloride gas in step B and uncooled complete dimethoxym ethane gas are passed through secondary condenser, first is obtained
The mixing lime set of acetal and chloromethanes；
D. the methyl alcohol and the mixing lime set of dimethoxym ethane for step B being obtained are placed in product tower, and bottom of towe obtains methanol product, top gaseous phase
Condensed device condensation obtains dimethoxym ethane product；
E. the dimethoxym ethane and the mixing lime set of chloromethanes for step C being obtained are placed in recovery tower, and bottom of towe obtains dimethoxym ethane product, tower top
The condensed device condensation of gas phase obtains chloromethanes product；
F. the uncooled methyl chloride gas of step C are entered into chloromethanes recovery system.
In the present embodiment, in step A, described plus alkali is neutralized to alkalescent, and the pH value for hydrolyzing tail gas is 9.
In step B, the column bottom temperature of the weight-removing column is 118 DEG C, and tower top temperature is 60 DEG C.
In step B, the temperature of the first-stage condenser is 40 DEG C.
In step C, the temperature of the secondary condenser is -10 DEG C.
In step D, the column bottom temperature of the product tower is 70 DEG C, and tower top temperature is 45 DEG C.
In step E, the column bottom temperature of the recovery tower is 118 DEG C, and tower top temperature is 47 DEG C, and operating pressure is 0.82MPa.
The product that the present embodiment is obtained：The purity of methyl alcohol is 99.8%, methyl alcohol water content 0.08%；The purity of dimethoxym ethane is
98.0%, dimethoxym ethane water content 0.10%；The purity of chloromethanes is more than 99.5%, moisture 0.030%, acidity 0.0040%.
Embodiment 4
A kind of glyphosate hydrolyzing tail gas recovery method, comprises the following steps：
A. neutralize
Glyphosate hydrolyzing tail gas plus alkali are neutralized to alkalescent；
B. one-level condensation
The alkalescent gas that step A is obtained is passed through weight-removing column, and the mixed gas of tower top are condensed through first-stage condenser, obtain methyl alcohol
With the mixing lime set of dimethoxym ethane；
C. B-grade condensation
Uncooled methyl chloride gas in step B and uncooled complete dimethoxym ethane gas are passed through secondary condenser, first is obtained
The mixing lime set of acetal and chloromethanes；
D. the methyl alcohol and the mixing lime set of dimethoxym ethane for step B being obtained are placed in product tower, and bottom of towe obtains methanol product, top gaseous phase
Condensed device condensation obtains dimethoxym ethane product；
E. the dimethoxym ethane and the mixing lime set of chloromethanes for step C being obtained are placed in recovery tower, and bottom of towe obtains dimethoxym ethane product, tower top
The condensed device condensation of gas phase obtains chloromethanes product；
F. the uncooled methyl chloride gas of step C are entered into chloromethanes recovery system.
In the present embodiment, in step A, described plus alkali is neutralized to alkalescent, and the pH value for hydrolyzing tail gas is 8.
In step B, the column bottom temperature of the weight-removing column is 112 DEG C, and tower top temperature is 55 DEG C.
In step B, the temperature of the first-stage condenser is 45 DEG C.
In step C, the temperature of the secondary condenser is -10 DEG C.
In step D, the column bottom temperature of the product tower is 70 DEG C, and tower top temperature is 46 DEG C.
In step E, the column bottom temperature of the recovery tower is 105 DEG C, and tower top temperature is 38 DEG C, and operating pressure is 0.75MPa.
The product that the present embodiment is obtained：The purity of methyl alcohol is 99.7%, methyl alcohol water content 0.07%；The purity of dimethoxym ethane is
96.8%, dimethoxym ethane water content 0.15%；The purity of chloromethanes is more than 99.5%, moisture 0.028%, acidity 0.0046%.
Embodiment 5
A kind of glyphosate hydrolyzing tail gas recovery method, comprises the following steps：
A. neutralize
Glyphosate hydrolyzing tail gas plus alkali are neutralized to alkalescent；
B. one-level condensation
The alkalescent gas that step A is obtained is passed through weight-removing column, and the mixed gas of tower top are condensed through first-stage condenser, obtain methyl alcohol
With the mixing lime set of dimethoxym ethane；
C. B-grade condensation
Uncooled methyl chloride gas in step B and uncooled complete dimethoxym ethane gas are passed through secondary condenser, first is obtained
The mixing lime set of acetal and chloromethanes；
D. the methyl alcohol and the mixing lime set of dimethoxym ethane for step B being obtained are placed in product tower, and bottom of towe obtains methanol product, top gaseous phase
Condensed device condensation obtains dimethoxym ethane product；
E. the dimethoxym ethane and the mixing lime set of chloromethanes for step C being obtained are placed in recovery tower, and bottom of towe obtains dimethoxym ethane product, tower top
The condensed device condensation of gas phase obtains chloromethanes product；
F. the uncooled methyl chloride gas of step C are entered into chloromethanes recovery system.
In the present embodiment, in step A, described plus alkali is neutralized to alkalescent, and the pH value for hydrolyzing tail gas is 10.
In step B, the column bottom temperature of the weight-removing column is 105 DEG C, and tower top temperature is 75 DEG C.
In step B, the temperature of the first-stage condenser is 55 DEG C.
In step C, the temperature of the secondary condenser is -5 DEG C.
In step D, the column bottom temperature of the product tower is 85 DEG C, and tower top temperature is 50 DEG C.
In step E, the column bottom temperature of the recovery tower is 122 DEG C, and tower top temperature is 48 DEG C, and operating pressure is .88MPa.
The product that the present embodiment is obtained：The purity of methyl alcohol is 99.9%, methyl alcohol water content 0.06%；The purity of dimethoxym ethane is
97.5%, dimethoxym ethane water content 0.11%；The purity of chloromethanes is more than 99.5%, moisture 0.030%, acidity 0.0050%.
The above, is only presently preferred embodiments of the present invention, not does any formal limitation to the present invention, it is every according to
Any simple modification, the equivalent variations made to above example according to technical spirit of the invention, each fall within protection of the invention
Within the scope of.
Claims (9)
1. a kind of glyphosate hydrolyzing tail gas recovery method, it is characterised in that：Comprise the following steps：
A. neutralize
Glyphosate hydrolyzing tail gas plus alkali are neutralized to alkalescent；
B. one-level condensation
The alkalescent gas that step A is obtained is passed through weight-removing column, and the mixed gas of tower top are condensed through first-stage condenser, obtain methyl alcohol
With the mixing lime set of dimethoxym ethane；
C. B-grade condensation
Uncooled methyl chloride gas in step B and uncooled complete dimethoxym ethane gas are passed through secondary condenser, first is obtained
The mixing lime set of acetal and chloromethanes；
D. the methyl alcohol and the mixing lime set of dimethoxym ethane for step B being obtained are placed in product tower, and bottom of towe obtains methanol product, top gaseous phase
Condensed device condensation obtains dimethoxym ethane product；
E. the dimethoxym ethane and the mixing lime set of chloromethanes for step C being obtained are placed in recovery tower, and bottom of towe obtains dimethoxym ethane product, tower top
The condensed device condensation of gas phase obtains chloromethanes product；
F. the uncooled methyl chloride gas of step C are entered into chloromethanes recovery system, finished product is obtained by drying, compression, condensation
Chloromethanes.
2. a kind of glyphosate hydrolyzing tail gas recovery method as claimed in claim 1, it is characterised in that：In step A, described plus alkali
Alkalescent is neutralized to, the pH value for hydrolyzing tail gas is 8~10.
3. a kind of glyphosate hydrolyzing tail gas recovery method as claimed in claim 1, it is characterised in that：In step B, the de- weight
The column bottom temperature of tower is 105~120 DEG C, and tower top temperature is 55~75 DEG C.
4. a kind of glyphosate hydrolyzing tail gas recovery method as claimed in claim 1, it is characterised in that：In step B, the one-level
The temperature of condenser is 25~65 DEG C.
5. a kind of glyphosate hydrolyzing tail gas recovery method as claimed in claim 1, it is characterised in that：In step C, described two grades
The temperature of condenser is -15~15 DEG C.
6. a kind of glyphosate hydrolyzing tail gas recovery method as claimed in claim 1, it is characterised in that：In step D, the product
The column bottom temperature of tower is 65~85 DEG C, and tower top temperature is 40~55 DEG C.
7. a kind of glyphosate hydrolyzing tail gas recovery method as claimed in claim 1, it is characterised in that：In step E, the recovery
The column bottom temperature of tower is 100~130 DEG C, and tower top temperature is 35~50 DEG C, and operating pressure is 0.7~1MPa.
8. a kind of glyphosate hydrolyzing tail gas recovery method as claimed in claim 1, it is characterised in that：In step E, the first contracting
The purity of aldehyde product is 95~99.5%.
9. a kind of glyphosate hydrolyzing tail gas recovery method as claimed in claim 1, it is characterised in that：In step E, the chloromethane
The purity of alkane product is 99.5~99.9%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111068497A (en) * | 2019-12-13 | 2020-04-28 | 湖北泰盛化工有限公司 | Device and method for recovering solvent methanol in glyphosate production |
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| CN104353339A (en) * | 2014-10-30 | 2015-02-18 | 江西金龙化工有限公司 | Method for continuously recovering by-products from tail gas obtained by hydrolyzing glyphosate |
| CN104959002A (en) * | 2015-06-29 | 2015-10-07 | 江西金龙化工有限公司 | Method for removing hydrogen chloride by continuously recycling glyphosate hydrolyzed tail gas |
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| CN1260348A (en) * | 1999-11-08 | 2000-07-19 | 浙江新安化工集团股份有限公司 | Hydrolysis subsequent procedure in synthesis of glyphosphonic acid |
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| CN111068497A (en) * | 2019-12-13 | 2020-04-28 | 湖北泰盛化工有限公司 | Device and method for recovering solvent methanol in glyphosate production |
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Application publication date: 20170531 |