CN105622332A - Recovery method for chloroethane tail gas in fosetyl-aluminum production - Google Patents
Recovery method for chloroethane tail gas in fosetyl-aluminum production Download PDFInfo
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- CN105622332A CN105622332A CN201511010043.9A CN201511010043A CN105622332A CN 105622332 A CN105622332 A CN 105622332A CN 201511010043 A CN201511010043 A CN 201511010043A CN 105622332 A CN105622332 A CN 105622332A
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- Prior art keywords
- monochloroethane
- gas
- tail gas
- recovery method
- chloroethane
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
Abstract
The invention provides a recovery method for chloroethane tail gas in fosetyl-aluminum production. The recovery method comprises the following steps that the chloroethane tail gas in fosetyl-aluminum production is subjected to gas-liquid separation through a gas-liquid separator; the chloroethane tail gas after being subjected to gas-liquid separation enters a first-stage condenser to be subjected to condensation treatment, so that the chloroethane tail gas is obtained; the chloroethane tail gas is subjected to alkali washing, drying and compressing; compressed chloroethane enters a second-stage condenser to be subjected to subzero treatment, so that a finished product chloroethane is obtained. The recovery method is environmentally friendly, and moreover, the influence on the environment from production exhaust tail gas is thoroughly avoided. The flow of the method is simple, operation is convenient, cost can be reduced, the recovery rate is increased, recovery quality is improved, and the method has good economic benefits and social benefits.
Description
Technical field
The present invention relates to the method for purifying and recovering of monochloroethane, it relates to the recovery method of monochloroethane tail gas in the production of a kind of second phosphine aluminium.
Background technology
The current domestic second total production capacity of phosphine aluminium reaches more than 30,000 ton, more than 5,000 ton, annual by-product monochloroethane, but is limited to state of the art. The tail gas monochloroethane of its by-product can not effectively be recycled by current domestic most second phosphine aluminium and diethyl phosphite manufacturing enterprise, along with domestic pesticide synthesis is fast-developing, the demand of monochloroethane also increases fast, the monochloroethane reclaimed and make good use of in second phosphine aluminium/diethyl phosphite tail gas not only brings considerable economic benefit, objectively also turn waste into wealth, monochloroethane is that one is colourless taste gas, human body is poisonous, the not treated discharge of this tail gas, enterprise will be decreased an income, more importantly ambient air is caused serious impact.
In prior art, the recovery method of monochloroethane tail gas mainly contains following two kinds:
The main flow that pressurization condensation method reclaims monochloroethane comprises: through gas condenser, most of water vapor condensation separation is got off by tail gas, reenter sulphuric acid desiccator dehydration, Nash pump is forced through the thick monochloroethane condenser entering two series connection after separator removes acid mist successively, condensed thick monochloroethane liquid enters storage tank, finally entering distillation tower to refine, tower top gaseous component out is through finished product condenser laggard essence monochloroethane storage tank.
Low temperature absorption method reclaim monochloroethane main flow be: tail gas is entered two series connection bubble absorption devices absorb, the monochloroethane in solution absorption tail gas is carried out as absorption agent with the raffinate after cooling, after again absorbing liquid is put into storage tank, finally entering distillation tower to refine, tower top gaseous component out is through finished product condenser condenses laggard essence monochloroethane storage tank.
Adopting above-mentioned pressurization condensation method and low temperature absorption method to reclaim monochloroethane, the rate of recovery is lower, and generally at about 50-60%, and monochloroethane quality is also unstable after reclaiming.
Summary of the invention
In order to solve the deficiency that prior art exists, it is an object of the invention to provide the recovery method of monochloroethane tail gas in the production of a kind of second phosphine aluminium, its technique is simple, rate of recovery height, free from environmental pollution, recovery quality height, and cost recovery is low.
For achieving the above object, the recovery method of monochloroethane tail gas in second phosphine aluminium provided by the invention production, comprises the following steps:
1) in being produced by second phosphine aluminium, monochloroethane tail gas carries out gas-liquid separation through gas-liquid separator;
2) monochloroethane tail gas after gas-liquid separation enters first-stage condenser and carries out condensation process, obtains monochloroethane gas;
3) monochloroethane gas is carried out alkali cleaning, drying, then compress;
4) monochloroethane after compressing enters secondary condenser and carries out sub-zero treatment, obtains finished product monochloroethane.
Further, the condensing temperature of described first-stage condenser is 0 DEG C��-2 DEG C.
Further, the cryogenic temperature of described secondary condenser is-10 DEG C ~-15 DEG C.
Further, described monochloroethane gas is dried and is by step 3): adopt specification be �� 900 �� 6000, inside install �� 25 Pall ring additional sulfuric acid as siccative.
Further, dried monochloroethane carry out described in step 3) compression is adopt monochloroethane dedicated compressor; Described monochloroethane dedicated compressor is oil-free lubricatoin water-cooled piston formula compressor, and its exhaust pressure to be 0.8-1.2MPa, pressure of inspiration(Pi) be normal pressure, type of drive are resilient coupling.
The recovery method of monochloroethane tail gas in the second phosphine aluminium production of the present invention, it is not necessary to zeolite fixed-bed reactor is de-except moisture content, reduces cost; By adopting monochloroethane dedicated compressor to carry out after the tentatively de-moisture removal of first-stage condenser pressurized liquefied, it is to increase the rate of recovery; Carrying out dark cold recovery monochloroethane by secondary condenser, flow process is simple, easy to operate; Adopt the vitriol oil to dewater, make the monochloroethane content reach more than 99.8%, it is to increase the rate of recovery.
The recovery method of monochloroethane tail gas in the second phosphine aluminium production of the present invention, recovery process environmental protection, and thoroughly solve and produce emission to the impact of environment, this technical process is simple, easy to operate, and can reduce costs, improve the rate of recovery, the advantage that high quality reclaims and increases economic efficiency.
Other features and advantages of the present invention will be set forth in the following description, and, partly become apparent from specification sheets, or understand by implementing the present invention.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for specification sheets, and together with embodiments of the present invention, for explaining the present invention, is not construed as limiting the invention. In the accompanying drawings:
Fig. 1 is the process flow sheet that the second phosphine aluminium according to the present invention produces monochloroethane recovery method in emission.
Embodiment
Below in conjunction with accompanying drawing, the preferred embodiments of the present invention are described, it will be appreciated that preferred embodiment described herein, only for instruction and explanation of the present invention, is not intended to limit the present invention.
Fig. 1 is the process flow sheet that the second phosphine aluminium according to the present invention produces monochloroethane recovery method in emission, below with reference to Fig. 1, is described in detail by monochloroethane recovery method in the second phosphine aluminium production emission of the present invention.
First, in step 101, by the exhaust collection containing monochloroethane of discharge in second phosphine aluminium production process in tail gas buffer.
In step 102, the tail gas containing monochloroethane is transported to gas-liquid separator from tail gas buffer, carries out gas-liquid separation process, isolate moisture.
In step 103, the monochloroethane tail gas processed through gas-liquid separation is sent into first-stage condenser and carries out condensation, condensing temperature 0��-2 DEG C, make the moisture content condensation separation of gas, collect monochloroethane gas.
In step 104, through the monochloroethane gas that first-stage condenser process obtains, through alkali cleaning, then through three grades of vitriol oil drying tower drying treatment, remove the trace water in monochloroethane further. Vitriol oil specification is �� 900 �� 6000, and inside installs �� 25 Pall ring additional.
In step 105, monochloroethane gas after drying treatment carries out processed compressed through monochloroethane dedicated compressor, and the structure formation of this dedicated compressor to be oil-free lubricatoin water-cooled piston formula, exhaust pressure be 0.8-1.2MPa, pressure of inspiration(Pi) are normal pressure, type of drive is resilient coupling.
In step 106, through the monochloroethane of processed compressed, enter secondary condenser and carry out sub-zero treatment, obtain finished product monochloroethane. Compression obtains monochloroethane, in secondary condenser, is the sub-zero treatment of-10��-15 DEG C through condensing temperature, finally obtains finished product monochloroethane.
In step 107, the finished product monochloroethane obtained through sub-zero treatment is transported to monochloroethane liquid storage vessel, completes the recovery of monochloroethane tail gas in second phosphine aluminium production process.
The second phosphine aluminium of the present invention produces monochloroethane recovery method in emission, and the rate of recovery of monochloroethane reaches more than 99.6%, and content reaches more than 99.8%.
One of ordinary skill in the art will appreciate that: the foregoing is only the preferred embodiments of the present invention, it is not limited to the present invention, although with reference to previous embodiment to invention has been detailed description, for a person skilled in the art, the technical scheme that foregoing embodiments is recorded still can be modified by it, or wherein part technology feature carries out equivalent replacement. Within the spirit and principles in the present invention all, any amendment of doing, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (5)
1. a second phosphine aluminium produce in the recovery method of monochloroethane tail gas, it is characterised in that, comprise the following steps:
1) in being produced by second phosphine aluminium, monochloroethane tail gas carries out gas-liquid separation through gas-liquid separator;
2) monochloroethane tail gas after gas-liquid separation enters first-stage condenser and carries out condensation process, obtains monochloroethane gas;
3) monochloroethane gas is carried out alkali cleaning, drying, then compress;
4) monochloroethane after compressing enters secondary condenser and carries out sub-zero treatment, obtains finished product monochloroethane.
2. second phosphine aluminium according to claim 1 produce in the recovery method of monochloroethane tail gas, it is characterised in that, the condensing temperature of described first-stage condenser is 0 DEG C��-2 DEG C.
3. second phosphine aluminium according to claim 1 produces the recovery method of monochloroethane in emission, it is characterised in that, the cryogenic temperature of described secondary condenser is-10 DEG C ~-15 DEG C.
4. second phosphine aluminium according to claim 1 produce in the recovery method of monochloroethane tail gas, it is characterized in that, described monochloroethane gas is dried and is by described step 3): adopt specification be �� 900 �� 6000, inside install �� 25 Pall ring additional sulfuric acid as siccative.
5. second phosphine aluminium according to claim 1 produce in the recovery method of monochloroethane tail gas, it is characterised in that, it is adopt monochloroethane dedicated compressor that dried monochloroethane carries out described in step 3) compression; Described monochloroethane dedicated compressor is oil-free lubricatoin water-cooled piston formula compressor, and its exhaust pressure to be 0.8-1.2MPa, pressure of inspiration(Pi) be normal pressure, type of drive are resilient coupling.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201511010043.9A CN105622332A (en) | 2015-12-30 | 2015-12-30 | Recovery method for chloroethane tail gas in fosetyl-aluminum production |
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| CN201511010043.9A CN105622332A (en) | 2015-12-30 | 2015-12-30 | Recovery method for chloroethane tail gas in fosetyl-aluminum production |
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| CN105622332A true CN105622332A (en) | 2016-06-01 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114322458A (en) * | 2022-01-20 | 2022-04-12 | 河南隆鑫高纯新材料科技有限公司 | Sufficient and environment-friendly tail gas treatment process and device |
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|---|---|---|---|---|
| JPS5016766A (en) * | 1973-06-01 | 1975-02-21 | ||
| CN101407444A (en) * | 2008-11-25 | 2009-04-15 | 湖北泰盛化工有限公司 | Method for recovering methyl chloride in discharged tail gas of glyphosate / dimethyl phosphate production |
| CN102643156A (en) * | 2012-04-11 | 2012-08-22 | 天津林圣金海化工有限公司 | Chloroethane purification process |
| CN102766157A (en) * | 2012-09-05 | 2012-11-07 | 利民化工股份有限公司 | Method for producing technical-grade fosetyl-aluminum |
| CN204025015U (en) * | 2014-08-05 | 2014-12-17 | 杭州高成机电设备有限公司 | Water-cooled is pure without oily adjusting piston air compressor |
-
2015
- 2015-12-30 CN CN201511010043.9A patent/CN105622332A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5016766A (en) * | 1973-06-01 | 1975-02-21 | ||
| CN101407444A (en) * | 2008-11-25 | 2009-04-15 | 湖北泰盛化工有限公司 | Method for recovering methyl chloride in discharged tail gas of glyphosate / dimethyl phosphate production |
| CN102643156A (en) * | 2012-04-11 | 2012-08-22 | 天津林圣金海化工有限公司 | Chloroethane purification process |
| CN102766157A (en) * | 2012-09-05 | 2012-11-07 | 利民化工股份有限公司 | Method for producing technical-grade fosetyl-aluminum |
| CN204025015U (en) * | 2014-08-05 | 2014-12-17 | 杭州高成机电设备有限公司 | Water-cooled is pure without oily adjusting piston air compressor |
Non-Patent Citations (1)
| Title |
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| 刘克斌等: "氯油尾气中氯乙烷的回收新工艺研究", 《化工科技市场》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114322458A (en) * | 2022-01-20 | 2022-04-12 | 河南隆鑫高纯新材料科技有限公司 | Sufficient and environment-friendly tail gas treatment process and device |
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