CN107837653B - Method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by tail gas treatment system - Google Patents

Method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by tail gas treatment system Download PDF

Info

Publication number
CN107837653B
CN107837653B CN201711324225.2A CN201711324225A CN107837653B CN 107837653 B CN107837653 B CN 107837653B CN 201711324225 A CN201711324225 A CN 201711324225A CN 107837653 B CN107837653 B CN 107837653B
Authority
CN
China
Prior art keywords
tail gas
absorbent
methyl
chlorosilane
tower
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201711324225.2A
Other languages
Chinese (zh)
Other versions
CN107837653A (en
Inventor
郑士朋
刘勇
何君
万文峰
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.)
Jiangxi Bluestar Xinghuo Silicone Co Ltd
Original Assignee
Jiangxi Bluestar Xinghuo Silicone 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 Jiangxi Bluestar Xinghuo Silicone Co Ltd filed Critical Jiangxi Bluestar Xinghuo Silicone Co Ltd
Priority to CN201711324225.2A priority Critical patent/CN107837653B/en
Publication of CN107837653A publication Critical patent/CN107837653A/en
Application granted granted Critical
Publication of CN107837653B publication Critical patent/CN107837653B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1418—Recovery of products
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1487—Removing organic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B01D53/185—Liquid distributors
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/205—Other organic compounds not covered by B01D2252/00 - B01D2252/20494
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/206—Organic halogen compounds
    • B01D2257/2064—Chlorine
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention discloses a tail gas treatment system and a method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by using the same, wherein the treatment system comprises a methyl chloride recovery tower, a condenser, an absorbent storage tank and a circulating pump, the methyl chloride recovery tower is provided with a tail gas inlet, a packing layer, a circulating absorption liquid outlet and a tower top spray header, and the other end of the circulating recovery liquid outlet is connected with an inlet of the circulating pump; the condenser is provided with an absorbent inlet and an absorbent outlet, wherein the other end of the methylchlorosilane inlet is connected with an absorbent storage tank, the absorbent storage tank is provided with a circulating absorption liquid inlet, and the other end of the circulating absorption liquid inlet is connected with an outlet of a circulating pump. The invention applies the similarity and intermiscibility principle, utilizes low-temperature methyl chlorosilane as an absorbent to absorb methyl chloride in the methyl chlorosilane synthesis tail gas in the filler absorption tower, can reduce the content of the methyl chloride in the methyl chlorosilane synthesis tail gas from 10-80wt% to less than 0.1wt%, has good absorption effect and better economic value, and is suitable for popularization and application.

Description

Method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by tail gas treatment system
Technical Field
The invention relates to the technical field of tail gas recovery and environmental protection, in particular to a method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by a tail gas treatment system.
Background
The direct method for synthesizing methyl chlorosilane adopts silicon powder and chloromethane as raw materials, and carries out gas-solid two-phase reaction in a fluidized bed reactor, after the reaction, a crude monomer contains chloromethane of about 10-60 percent, the crude monomer usually uses a crude monomer tower to separate the chloromethane and the monomer, a pure monomer is discharged from the belly of the tower, the chloromethane is discharged from the top of the tower, the chloromethane is removed from the purification tower of chloromethane at the top of the tower, and the purified chloromethane is discharged from the top of the tower. The tail gas at the top of the crude monomer tower and the chloromethane purification tower is generally subjected to deep cooling (-10 to-20 ℃) to recover the monomers and the chloromethane carried by the tail gas, and then the tail gas is discharged to be burned. The boiling point of the chloromethane is-23.7 ℃ (101 KPa), the tail gas is difficult to be completely condensed by deep cooling, the incineration tail gas test shows that the content of the chloromethane in the tail gas is about 10-80wt%, and the emission to an incinerator can increase the unit consumption of the chloromethane and cause the increase of the production cost.
Disclosure of Invention
The invention aims to solve the problem of incomplete recovery of methyl chloride in the prior art, and provides a method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by using a tail gas treatment system.
In order to achieve the purpose, the invention adopts the following technical scheme:
a tail gas treatment system comprises a methyl chloride recovery tower, a condenser, an absorbent storage tank and a circulating pump, wherein the methyl chloride recovery tower is provided with a tail gas inlet, a packing layer, a circulating absorption liquid outlet and a tower top spray header, and the other end of the circulating recovery liquid outlet is connected with an inlet of the circulating pump; the condenser is provided with an absorbent inlet and an absorbent outlet, wherein the other end of the absorbent inlet is connected with an absorbent storage tank, the absorbent storage tank is provided with a circulating absorption liquid inlet, and the other end of the circulating absorption liquid inlet is connected with an outlet of the circulating pump.
Further, the condenser is a tube type heat exchanger with a heat exchange area of 50-200m2。
Further, the temperature at the outlet of the condenser is-10 to-25 ℃.
Furthermore, the number of the filler layers is 10-25, and the filler layers are made of metal wire mesh corrugated fillers.
The method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by using the tail gas treatment system specifically comprises the following steps: methyl chlorosilane synthesis tail gas enters the bottom of a methyl chloride recovery tower through a tail gas inlet, an absorbent coming out of an absorbent storage tank enters a condenser through an absorbent inlet, after cooling, the absorbent is sprayed from the top of the tower through an absorbent outlet and a spray header at the top of the tower, the methyl chlorosilane synthesis tail gas and the absorbent are fully contacted under the action of a packing layer, and circulating absorption liquid flows out from a circulating recovery liquid outlet at the bottom of the tower, passes through a circulating pump and returns to the absorbent storage tank through a circulating absorption liquid inlet.
Further, the mass ratio of the spraying amount of the absorbent sprayed out of the spray header at the top of the tower to the tail gas is 5: 1-20: 1.
further, the absorbent in the absorbent storage tank is methyl chlorosilane.
Furthermore, the methyl chlorosilane is formed by mixing 5-15 wt% of the monomethyl chlorosilane and 85-95 wt% of the dimethyl chlorosilane.
Furthermore, the content of chloromethane in the tail gas of the synthesis of methyl chlorosilane is 10-80 wt%.
Furthermore, the methyl chlorosilane in the absorbent storage tank (30) is formed by mixing 13 wt% of the methyl chlorosilane and 87 wt% of the dimethyl chlorosilane, and the methyl chlorosilane synthesis tail gas contains 55wt% of methyl chloride, 25wt% of methane, 12wt% of propylene, 5wt% of propane and 3wt% of ethyl chloride.
The invention has the beneficial effects that: the invention applies the similarity and intermiscibility principle, utilizes low-temperature methyl chlorosilane as an absorbent to absorb methyl chloride in the methyl chlorosilane synthesis tail gas in the filler absorption tower, can reduce the content of the methyl chloride in the methyl chlorosilane synthesis tail gas from 10-80wt% to less than 0.1wt%, has good absorption effect and better economic value, and is suitable for popularization and application.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
Reference numerals: the system comprises a 10 chloromethane recovery tower, a 11 tail gas inlet condenser, a 12 packing layer, a 13 circulating absorption liquid outlet, a 14 tower top spray header, a 20 condenser, a 21 absorbent inlet, a 22 absorbent outlet, a 30 absorbent storage tank, a 31 circulating absorption liquid inlet and a 40 circulating pump.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it is to be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
Example 1:
a tail gas treatment system comprises a methyl chloride recovery tower 10, a condenser 20, an absorbent storage tank 30 and a circulating pump 40, wherein the methyl chloride recovery tower 10 is provided with a tail gas inlet 11, a packing layer 12, a circulating absorption liquid outlet 13 and a tower top spray header 14, and the other end of the circulating recovery liquid outlet 13 is connected with an inlet of the circulating pump 40; the condenser 20 is provided with an absorbent inlet 21 and an absorbent outlet 22, wherein the other end of the absorbent inlet 21 is connected with the absorbent storage tank 30, the absorbent storage tank 30 is provided with a circulating absorption liquid inlet 31, and the other end of the circulating absorption liquid inlet 31 is connected with an outlet of the circulating pump 40.
The condenser 20 is a shell and tube heat exchanger with a heat exchange area of 50m2。
The temperature at the outlet of the condenser 20 was-10 ℃.
The number of the filler layers 12 is 10, and the material of the filler layers 12 is wire mesh corrugated filler.
The method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by using the tail gas treatment system specifically comprises the following steps: methyl chlorosilane synthesis tail gas enters the bottom of a methyl chloride recovery tower 10 through a tail gas inlet 11, an absorbent coming out of an absorbent storage tank 30 enters a condenser 20 through an absorbent inlet 21, after cooling, the absorbent is sprayed down from the top of the tower through an absorbent outlet 22 and a spray header 14 at the top of the tower, the methyl chlorosilane synthesis tail gas and the absorbent are fully contacted under the action of a packing layer 12, and circulating absorption liquid flows out from a circulating recovery liquid outlet 13 at the bottom of the tower, passes through a circulating pump 40 and returns to the absorbent storage tank 30 through a circulating absorption liquid inlet 31.
The mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header 14 to the tail gas is 5: 1.
the absorbent in the absorbent storage tank 30 is methyl chlorosilane.
The methylchlorosilane is formed by mixing 5% by weight of monomethylchlorosilane and 95% by weight of dimethylchlorosilane.
The content of chloromethane in the tail gas generated in the synthesis of methyl chlorosilane is 10 wt%.
Example 2:
the condenser 20 is a shell and tube heat exchanger with heat exchange area of 100m2The temperature at the outlet of the condenser 20 was-15 ℃.
The number of the filler layers 12 is 15, and the filler layers 12 are made of wire mesh corrugated filler.
The mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header 14 to the tail gas is 10: 1.
the absorbent in the absorbent storage tank 30 is methyl chlorosilane.
The methylchlorosilane is formed by mixing 10% by weight of monomethylchlorosilane and 90% by weight of dimethylchlorosilane.
The content of methyl chloride in the tail gas of the synthesis of methyl chlorosilane is 20 wt%.
The rest is the same as example 1.
Example 3:
the condenser 20 is a shell and tube heat exchanger with a heat exchange area of 150m2The temperature at the outlet of the condenser 20 was-20 ℃.
The number of the filler layers 12 is 20, and the material of the filler layers 12 is wire mesh corrugated filler.
The mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header 14 to the tail gas is 15: 1.
the absorbent in the absorbent storage tank 30 is methyl chlorosilane.
The methyl chlorosilane is formed by mixing 15% of monomethyl chlorosilane by weight and 85% of dimethyl chlorosilane by weight.
The content of chloromethane in the tail gas generated in the synthesis of methyl chlorosilane is 30 wt%.
The rest is the same as example 1.
Example 4:
the condenser 20 is a shell and tube heat exchanger with a heat exchange area of 200m2The temperature at the outlet of the condenser 20 was-25 ℃.
The number of the filler layers 12 is 25, and the material of the filler layers 12 is wire mesh corrugated filler.
The mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header 14 to the tail gas is 20: 1.
the absorbent in the absorbent storage tank 30 is methyl chlorosilane.
The methylchlorosilane is formed by mixing 5% by weight of monomethylchlorosilane and 95% by weight of dimethylchlorosilane.
The content of chloromethane in the tail gas generated in the synthesis of methyl chlorosilane is 40 wt%.
The rest is the same as example 1.
Example 5:
the condenser 20 is a shell and tube heat exchanger with a heat exchange area of 50m2The temperature at the outlet of the condenser 20 was-10 ℃.
The number of the filler layers 12 is 10, and the material of the filler layers 12 is wire mesh corrugated filler.
The mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header 14 to the tail gas is 5: 1.
the absorbent in the absorbent storage tank 30 is methyl chlorosilane.
The methylchlorosilane is formed by mixing 10% by weight of monomethylchlorosilane and 90% by weight of dimethylchlorosilane.
The chloromethane content in the tail gas of the synthesis of methyl chlorosilane is 50 wt%.
The rest is the same as example 1.
Example 6:
the condenser 20 is a shell and tube heat exchanger with heat exchange area of 100m2The temperature at the outlet of the condenser 20 was-15 ℃.
The number of the filler layers 12 is 16, and the material of the filler layers 12 is wire mesh corrugated filler.
The mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header 14 to the tail gas is 8: 1.
the absorbent in the absorbent storage tank 30 is methyl chlorosilane.
The methylchlorosilane is formed by mixing 12% by weight of monomethylchlorosilane and 88% by weight of dimethylchlorosilane.
The chloromethane content in the tail gas of the synthesis of methyl chlorosilane is 60 wt%.
The rest is the same as example 1.
Example 7:
the condenser 20 is a tube type heat exchanger with heat exchange area of 180m2The temperature at the outlet of the condenser 20 was-20 ℃.
The number of the filler layers 12 is 21, and the material of the filler layers 12 is wire mesh corrugated filler.
The mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header 14 to the tail gas is 16: 1.
the absorbent in the absorbent storage tank 30 is methyl chlorosilane.
The methylchlorosilane is formed by mixing 13% by weight of monomethylchlorosilane and 87% by weight of dimethylchlorosilane.
The chloromethane content in the tail gas of the synthesis of methyl chlorosilane is 70 wt%.
The rest is the same as example 1.
Example 8:
the condenser 20 is a shell and tube heat exchanger with a heat exchange area of 200m2The temperature at the outlet of the condenser 20 was-25 ℃.
The number of the filler layers 12 is 25, and the material of the filler layers 12 is wire mesh corrugated filler.
The mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header 14 to the tail gas is 20: 1.
the absorbent in the absorbent storage tank 30 is methyl chlorosilane.
The methyl chlorosilane is formed by mixing 15% of monomethyl chlorosilane by weight and 85% of dimethyl chlorosilane by weight.
The chloromethane content in the tail gas of the synthesis of methyl chlorosilane is 80 wt%.
The rest is the same as example 1.
Example 9:
a tail gas treatment system comprises a methyl chloride recovery tower 10, a condenser 20, an absorbent storage tank 30 and a circulating pump 40, wherein the methyl chloride recovery tower 10 is provided with a tail gas inlet 11, a packing layer 12, a circulating absorption liquid outlet 13 and a tower top spray header 14, and the other end of the circulating recovery liquid outlet 13 is connected with an inlet of the circulating pump 40; the condenser 20 is provided with an absorbent inlet 21 and an absorbent outlet 22, wherein the other end of the absorbent inlet 21 is connected with the absorbent storage tank 30, the absorbent storage tank 30 is provided with a circulating absorption liquid inlet 31, and the other end of the circulating absorption liquid inlet 31 is connected with an outlet of the circulating pump 40.
The condenser 20 is a shell and tube heat exchanger with a heat exchange area of 50m2。
The temperature at the outlet of the condenser 20 was-10 ℃.
The number of the filler layers 12 is 10, and the material of the filler layers 12 is wire mesh corrugated filler.
The method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by using the tail gas treatment system specifically comprises the following steps: methyl chlorosilane synthesis tail gas enters the bottom of a methyl chloride recovery tower 10 through a tail gas inlet 11, an absorbent coming out of an absorbent storage tank 30 enters a condenser 20 through an absorbent inlet 21, after cooling, the absorbent is sprayed down from the top of the tower through an absorbent outlet 22 and a spray header 14 at the top of the tower, the methyl chlorosilane synthesis tail gas and the absorbent are fully contacted under the action of a packing layer 12, and circulating absorption liquid flows out from a circulating recovery liquid outlet 13 at the bottom of the tower, passes through a circulating pump 40 and returns to the absorbent storage tank 30 through a circulating absorption liquid inlet 31.
The mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header 14 to the tail gas is 5: 1.
the absorbent in the absorbent storage tank 30 is methyl chlorosilane.
The methyl chlorosilane in the absorbent storage tank (30) is formed by mixing 13 wt% of methyl chlorosilane and 87 wt% of dimethyl chlorosilane, and the methyl chlorosilane synthesis tail gas contains 55wt% of methyl chloride, 25wt% of methane, 12wt% of propylene, 5wt% of propane and 3wt% of ethyl chloride.
Comparative example 1:
in the operation process of the example 1, the condenser is closed, the tail gas is directly absorbed by the absorbent at normal temperature, the other operations are consistent with the operation process of the example 1, and the methyl chloride absorption and recovery effect is observed.
Comparative example 2:
in the operation of example 2, the packing layer in the absorption tower was removed, and the remaining operation was kept in accordance with example 2, and the effect of absorbing and recovering methyl chloride was observed.
Comparative example 3:
in the operation process of example 3, the spraying amount of the absorbent sprayed from the tower top spray header 14 was changed so that the mass ratio of the spraying amount to the amount of the tail gas was 4: 1, the remaining operations were kept in accordance with example 3, and the effect of absorbing and recovering methyl chloride was observed.
Comparative example 4:
in the operation process of example 4, the spraying amount of the absorbent sprayed from the tower top spray header 14 was changed so that the mass ratio of the spraying amount to the amount of the tail gas was 3: 1, the remaining operations were kept in accordance with example 4, and the effect of absorbing and recovering methyl chloride was observed.
Comparative example 5:
in the operation process of example 5, the spraying amount of the absorbent sprayed from the tower top spray header 14 was changed so that the mass ratio of the spraying amount to the amount of the off-gas was 2: 1, the remaining operations were kept in accordance with example 5, and the effect of absorbing and recovering methyl chloride was observed.
Comparative example 6:
in the operation process of example 6, the spraying amount of the absorbent sprayed from the tower top spray header 14 was changed so that the mass ratio of the spraying amount to the amount of the off-gas was 1: 1, the remaining operations were kept in accordance with example 6, and the effect of absorbing and recovering methyl chloride was observed.
Comparative example 7:
in the operation process of example 7, the absorbent in the absorbent storage tank 30 is methylchlorosilane, and the methylchlorosilane is monomethylchlorosilane in a weight ratio of 100%, and the remaining operations are the same as those in example 7, and the effect of absorbing and recovering chloromethane is observed.
Comparative example 8:
in the operation process of example 8, the absorbent in the absorbent storage tank 30 is methylchlorosilane, and the methylchlorosilane is dimethylchlorosilane in a weight ratio of 100%, and the remaining operations are the same as those in example 8, and the effect of absorbing and recovering chloromethane is observed.
Comparative example 9:
the same tail gas raw material as in example 9 was used, methyl chloride was recovered by a conventional cryogenic process, and the effect of methyl chloride absorption and recovery was observed.
And collecting the treated tail gas, and detecting the content of the methyl chloride in the tail gas, wherein the detection result is shown in the table I.
Table one: and (4) treating the content of methyl chloride in the tail gas.
Figure DEST_PATH_IMAGE001
From the above data, it can be found that: 1. by adopting the system and the tail gas recovery method, the content of the methyl chloride in the treated tail gas can be reduced to be below 0.1wt%, most of the methyl chloride can be recycled, the environment is protected, and the recycled methyl chloride can reduce the production cost of enterprises; 2. comparative examples 1 to 8, which employ a system or method similar to the present invention but with some parameters changed, resulted in poor absorption, demonstrated that the system and method of the present invention were both creatively explored and provided significant progress; 3. comparative example 9 adopts the traditional cryogenic process to recover methyl chloride, but the method forms an azeotrope with methyl chloride due to the complexity of components in the synthesis tail gas, especially due to the coexistence of propylene (boiling point-47.4 ℃) and propane (boiling point-42.1 ℃) in the tail gas, so that the recovery of methyl chloride is extremely incomplete, the energy consumption is relatively large, and the raw material recycling and energy saving and consumption reduction of enterprises are not facilitated.

Claims (2)

1. A method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by a tail gas treatment system is characterized by comprising the following steps: methyl chlorosilane synthesis tail gas enters the bottom of a methyl chloride recovery tower (10) through a tail gas inlet (11), an absorbent coming out of an absorbent storage tank (30) enters a condenser (20) through an absorbent inlet (21), is sprayed from the top of the tower through an absorbent outlet (22) and a tower top spray header (14) after being cooled, the methyl chlorosilane synthesis tail gas and the absorbent are fully contacted under the action of a packing layer (12), and circulating absorption liquid flows out of a circulating recovery liquid outlet (13) at the bottom of the tower, passes through a circulating pump (40) and returns to the absorbent storage tank (30) through a circulating absorption liquid inlet (31); the mass ratio of the spraying amount of the absorbent sprayed out of the tower top spray header (14) to the tail gas amount is 5: 1-20: 1; the absorbent in the absorbent storage tank (30) is methyl chlorosilane; the methyl chlorosilane is formed by mixing 5-15 wt% of monomethyl chlorosilane and 85-95 wt% of dimethyl chlorosilane; the content of chloromethane in the tail gas of the synthesis of methyl chlorosilane is 10-80 wt%.
2. The method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by using the tail gas treatment system as claimed in claim 1, which is characterized in that: the methyl chlorosilane in the absorbent storage tank (30) is formed by mixing 13 wt% of methyl chlorosilane and 87 wt% of dimethyl chlorosilane, and the methyl chlorosilane synthesis tail gas contains 55wt% of methyl chloride, 25wt% of methane, 12wt% of propylene, 5wt% of propane and 3wt% of ethyl chloride.
CN201711324225.2A 2017-12-13 2017-12-13 Method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by tail gas treatment system Active CN107837653B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201711324225.2A CN107837653B (en) 2017-12-13 2017-12-13 Method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by tail gas treatment system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201711324225.2A CN107837653B (en) 2017-12-13 2017-12-13 Method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by tail gas treatment system

Publications (2)

Publication Number Publication Date
CN107837653A CN107837653A (en) 2018-03-27
CN107837653B true CN107837653B (en) 2021-03-19

Family

ID=61663825

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201711324225.2A Active CN107837653B (en) 2017-12-13 2017-12-13 Method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by tail gas treatment system

Country Status (1)

Country Link
CN (1) CN107837653B (en)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111632469A (en) * 2020-05-09 2020-09-08 山东东岳有机硅材料股份有限公司 Dust-containing waste gas interception process and device in organic silicon monomer production
CN112717640A (en) * 2020-12-14 2021-04-30 安徽国星生物化学有限公司 Intelligent and efficient methyl chloride tail gas recovery device and use method thereof
CN112675667A (en) * 2020-12-31 2021-04-20 江苏爱姆欧光电材料有限公司 Recovery and absorption system and method for chloromethane in alkyl metal production process

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101870709B (en) * 2010-06-25 2012-08-08 天津大学 Method for refining and reclaiming chloromethane from organic silicon production process
CN103816768B (en) * 2014-02-26 2016-01-20 重庆海洲化学品有限公司 From producing the method and system reclaiming hydrogen chloride chloromethanes or tetrachloro-ethylene tail gas

Also Published As

Publication number Publication date
CN107837653A (en) 2018-03-27

Similar Documents

Publication Publication Date Title
CN107837653B (en) Method for recovering methyl chloride from methyl chlorosilane synthesis tail gas by tail gas treatment system
CN106946669B (en) Environment-friendly insulating gas co-production process and industrial production device
CN106731482A (en) A kind of industrial blast-furnace gas hydrogen chloride Gas recovering method and device
CN104311383B (en) A kind of method of the hydrogen chloride production monochloro methane that utilizes by-product in tetrachloro-ethylene production process
CN101235160B (en) Hydrogen chloride whole reclaiming zero discharging technique and device for PVC producing process
CN107540020B (en) A kind of synthetic method of tungsten hexafluoride
CN106242944B (en) A kind of preparation method of electron level perfluoroethane
TWI740458B (en) Abstract of description nitrogen oxide absorption slurry and its preparation and use method thereof
CN103638688B (en) A kind of recoverying and utilizing method synthesizing phosgene in n-butyl isocyanate thermo-optical reaction end gas
JP5864770B2 (en) Method and apparatus for recovering ethylene in vinyl acetate production process
CN110252268A (en) A kind of regeneration method of chlorobenzene production waste water absorption resin
US20150290581A1 (en) Carbon dioxide absorbing composition including antisolvent, and method and apparatus for absorbing carbon dioxide using the same
CN102516022B (en) Comprehensive processing method of vinyl chloride synthetic gas
CN108821253B (en) Purification system and treatment method of electronic grade phosphane
CN103816768B (en) From producing the method and system reclaiming hydrogen chloride chloromethanes or tetrachloro-ethylene tail gas
CN103588220B (en) A kind of ammonium chloride decomposes soda acid joint process and the system of preparing ammonia and hydrochloric acid
CN207708810U (en) The recovery system of tail gas in a kind of production of chlorination toluene
CN110204416A (en) The recovery method of chloromethanes tail gas in a kind of chemical production process
CN102766019A (en) Catalytic cracking process for producing vinyl chloride by using active carbon as accelerant
CN104164577A (en) Method for recovering germanium from tail gas generated by distillation of germanium tetrachloride
CN111994873B (en) Method and device for producing high-purity hydrobromic acid by adopting industrial grade hydrogen bromide gas
Wang et al. Synthesis of glycerol carbonate from glycerol and dimethyl carbonate catalyzed by solid base catalyst derived from waste carbide slag
CN111701404A (en) Hydrogen chloride absorption treatment method and device and application
CN104230650B (en) A kind of light chlorination process prepares the technique of methyl chloride
CN205850525U (en) A kind of for processing the device of tail gas in benzene chloride production

Legal Events

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