CN113457585B - Fluidized bed system for producing chloroethylene by acetylene method - Google Patents
Fluidized bed system for producing chloroethylene by acetylene method Download PDFInfo
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- CN113457585B CN113457585B CN202110727880.2A CN202110727880A CN113457585B CN 113457585 B CN113457585 B CN 113457585B CN 202110727880 A CN202110727880 A CN 202110727880A CN 113457585 B CN113457585 B CN 113457585B
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- fluidized bed
- bed reactor
- catalyst
- cyclone separator
- pipe
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- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 title claims abstract description 24
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical group ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000003054 catalyst Substances 0.000 claims abstract description 59
- 239000007789 gas Substances 0.000 claims abstract description 41
- 239000002245 particle Substances 0.000 claims abstract description 24
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000004480 active ingredient Substances 0.000 claims abstract description 12
- FDWREHZXQUYJFJ-UHFFFAOYSA-M gold monochloride Chemical group [Cl-].[Au+] FDWREHZXQUYJFJ-UHFFFAOYSA-M 0.000 claims abstract description 12
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 11
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 11
- ORTQZVOHEJQUHG-UHFFFAOYSA-L copper(II) chloride Chemical compound Cl[Cu]Cl ORTQZVOHEJQUHG-UHFFFAOYSA-L 0.000 claims abstract description 9
- 239000007788 liquid Substances 0.000 claims description 32
- 238000000926 separation method Methods 0.000 claims description 25
- 239000006227 byproduct Substances 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 7
- 239000011148 porous material Substances 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 12
- 239000003513 alkali Substances 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 20
- 239000007795 chemical reaction product Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 238000011143 downstream manufacturing Methods 0.000 description 4
- 238000005299 abrasion Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000005484 gravity Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/07—Preparation of halogenated hydrocarbons by addition of hydrogen halides
- C07C17/08—Preparation of halogenated hydrocarbons by addition of hydrogen halides to unsaturated hydrocarbons
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention belongs to the technical field of chlor-alkali chemical industry, and particularly relates to a fluidized bed system for producing chloroethylene by an acetylene method. The technical proposal is as follows: a fluidized bed system for producing chloroethylene by an acetylene method comprises a fluidized bed reactor, wherein a carrier of a catalyst is alumina particles, an active ingredient of the catalyst is gold chloride or copper chloride, and an air inlet pipe and a distributor for introducing mixed gas of acetylene and hydrogen chloride are arranged at the bottom of the fluidized bed reactor. The invention provides a fluidized bed system for producing chloroethylene by an acetylene method with high production efficiency.
Description
Technical Field
The invention belongs to the technical field of chlor-alkali chemical industry, and particularly relates to a fluidized bed system for producing chloroethylene by an acetylene method.
Background
The conventional acetylene-method vinyl chloride process adopts a fixed bed reactor, and the fixed bed reactor Shan Taisheng has small capacity and needs a large number of devices in industrial devices due to the limitations of equipment manufacture, heat transfer capacity and catalyst activity.
At present, the low-mercury catalyst used by the industrial device of vinyl chloride by acetylene method and the mercury-free catalyst under development are both carried by active carbon, the wear resistance is very poor, and only a fixed bed reactor can be adopted, but not a fluidized bed reactor. Therefore, the production efficiency of the existing acetylene method chloroethylene is lower.
Disclosure of Invention
In order to solve the problems in the prior art, the invention aims to provide a fluidized bed system for producing vinyl chloride by an acetylene method with high production efficiency.
The technical scheme adopted by the invention is as follows:
A fluidized bed system for producing chloroethylene by an acetylene method comprises a fluidized bed reactor, wherein a catalyst is arranged in the fluidized bed reactor, a carrier of the catalyst is alumina particles, an active ingredient of the catalyst is gold chloride or copper chloride, and an air inlet pipe for introducing a mixed gas of acetylene and hydrogen chloride is arranged at the bottom of the fluidized bed reactor.
In the acetylene-method vinyl chloride production system, the catalyst with the carrier of alumina particles and the active ingredient of gold chloride or copper chloride is adopted, and the carrier has good wear resistance. When a fluidized bed is used as the reactor, the catalyst having alumina particles as a carrier is resistant to attrition. Therefore, the invention adopts the catalyst with the carrier of alumina particles and uses the fluidized bed as a reactor, the reaction is continuously carried out, the reaction efficiency can be greatly improved, and the production capacity of a single fluidized bed reactor can reach 30 ten thousand tons of chloroethylene per year.
As a preferable scheme of the invention, a gas distributor is fixed in the fluidized bed reactor, a plurality of air holes are formed in the gas distributor, the gas distributor is positioned above the air inlet pipe, and a catalyst is arranged on the gas distributor. In the fluidized bed process, dehydrated mixed gas of acetylene and hydrogen chloride enters from the bottom of the fluidized bed reactor, and a gas distributor is arranged at the bottom of the fluidized bed reactor, so that the radial distribution effect of the mixed gas in the fluidized bed reactor can be enhanced, and the mixed gas can be fully contacted with a catalyst.
As a preferred embodiment of the present invention, the plurality of air holes are uniformly arranged on the gas distributor.
As a preferable scheme of the invention, a heat removing coil is arranged in the fluidized bed reactor, a vapor-liquid separation tank is arranged outside the fluidized bed reactor, the lower end of the heat removing coil is communicated with the lower end of the vapor-liquid separation tank through a pipeline, and the upper end of the heat removing coil is communicated with the upper end of the vapor-liquid separation tank through a pipeline. And a heat removal coil is arranged in the reaction section, hot water is introduced into the heat removal coil, so that the reaction heat can be taken away through circulating hot water in the tube, and the continuous reaction is ensured.
As a preferable mode of the invention, a byproduct steam pipe for discharging byproduct steam is connected to the top of the vapor-liquid separation tank.
As a preferable scheme of the invention, the upper end of the vapor-liquid separation tank is higher than the top of the heat removal coil pipe. The outside of the fluidized bed reactor is provided with a vapor-liquid separation tank, and the arrangement height of the vapor-liquid separation tank is slightly higher than the top of a heat removing coil in the fluidized bed reactor. The hot water in the heat-removing coil pipe is partially vaporized after being heated, and the density of the hot water is less than that of the hot water in the vapor-liquid separation tank. Under the pressure pushing generated by the density difference, hot water and water/steam mixed liquid naturally circulate between the heat removal coil pipe and the steam-liquid separation tank, the steam-water mixed liquid is separated in the steam-liquid separation tank, and byproduct steam is output from the top of the steam-liquid separation tank.
As a preferred embodiment of the present invention, a cyclone group is installed at the top of the fluidized bed reactor. The cyclone separator group is arranged outside the top of the fluidized bed reactor, and the reaction product gas enters the cyclone separator group after coming out of the top of the fluidized bed reactor. The catalyst particles are separated in a cyclone separator set which is arranged vertically above the fluidized bed reactor, a discharging pipe of the separated catalyst particles is directly inserted into the fluidized bed reactor, the separated catalyst particles return to the fluidized bed reactor by means of gravity, and the product gas from the cyclone separator set is further processed in a downstream process.
As a preferable scheme of the invention, the cyclone separator group comprises a first cyclone separator and a second cyclone separator, the upper section of the first cyclone separator is connected with the top of the fluidized bed reactor through a pipeline, the bottom of the first cyclone separator is connected with a first blanking pipe, and the first blanking pipe is inserted into the fluidized bed reactor; the upper section of the second cyclone separator is connected with the top of the first cyclone separator through a pipeline, a second blanking pipe is arranged at the bottom of the second cyclone separator, and the second blanking pipe is inserted into the fluidized bed reactor. The reaction product gas sequentially passes through the first cyclone separator and the second cyclone separator, so that the catalyst in the reaction product gas can be fully separated.
As a preferable scheme of the invention, the top of the second cyclone separator is connected with an exhaust pipe, and the product gas from the second cyclone separator is further processed by a downstream process.
As a preferable scheme of the invention, the shape of the carrier of the catalyst is spherical, a plurality of pores are arranged on the carrier of the catalyst, and the active ingredients of the catalyst are filled in the pores of the carrier of the catalyst.
The beneficial effects of the invention are as follows:
in the acetylene-method vinyl chloride production system, the catalyst with the carrier of alumina particles and the active ingredient of gold chloride or copper chloride is adopted, and the carrier has good wear resistance. When a fluidized bed is used as the reactor, the catalyst with alumina particles as the carrier can meet the abrasion resistance requirement in the fluidized bed. Therefore, the invention adopts the catalyst with the carrier of alumina particles and uses the fluidized bed as a reactor, the reaction is continuously carried out, the reaction efficiency can be greatly improved, and the production capacity of a single fluidized bed reactor can reach 30 ten thousand tons of chloroethylene per year.
Drawings
Fig. 1 is a schematic structural view of the present invention.
In the figure, 1-fluidized bed reactor; 2-an air inlet pipe; 3-gas distributor; 4-heat removal coil pipe; 5-a vapor-liquid separation tank; a 6-cyclone separator set; 51-a byproduct steam pipe; 61-a first cyclone; 62-a second cyclone; 63-a first blanking pipe; 64-a second blanking pipe; 65-exhaust pipe.
Detailed Description
Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are illustrative and intended to explain the present invention and should not be construed as limiting the invention.
As shown in fig. 1, the fluidized bed system for producing vinyl chloride by an acetylene method in this embodiment comprises a fluidized bed reactor 1, wherein a catalyst is arranged in the fluidized bed reactor 1, the carrier of the catalyst is alumina particles, the active ingredient of the catalyst is gold chloride or copper chloride, and an air inlet pipe 2 for introducing a mixed gas of acetylene and hydrogen chloride is arranged at the bottom of the fluidized bed reactor 1.
The shape of the carrier of the catalyst is spherical, a plurality of pores are arranged on the carrier of the catalyst, and the active ingredients of the catalyst are filled in the pores of the carrier of the catalyst.
In the acetylene-method vinyl chloride production system, the catalyst with the carrier of alumina particles and the active ingredient of gold chloride or copper chloride is adopted, and the carrier has good wear resistance. When a fluidized bed is used as the reactor, the catalyst having alumina particles as a carrier is resistant to attrition. Therefore, the invention adopts the catalyst with the carrier of alumina particles and uses the fluidized bed as a reactor, the reaction is continuously carried out, the reaction efficiency can be greatly improved, and the production capacity of a single fluidized bed reactor 1 can reach 30 ten thousand tons of chloroethylene per year.
Furthermore, a gas distributor 3 is fixed in the fluidized bed reactor 1, a plurality of air holes are uniformly distributed on the gas distributor 3, the gas distributor 3 is positioned above the air inlet pipe 2, and the catalyst is arranged on the gas distributor 3. In the fluidized bed process, dehydrated mixed gas of acetylene and hydrogen chloride enters from the bottom of the fluidized bed reactor 1, and a gas distributor 3 is arranged at the bottom of the fluidized bed reactor 1, so that the radial distribution effect of the mixed gas in the fluidized bed reactor 1 can be enhanced, and the mixed gas can be fully contacted with a catalyst.
Still further, install in the fluidized bed reactor 1 and remove hot coil pipe 4, fluidized bed reactor 1 outside is provided with vapour and liquid knockout drum 5, removes the lower extreme of hot coil pipe 4 and the lower extreme of vapour and liquid knockout drum 5 through the pipeline intercommunication, removes the upper end of hot coil pipe 4 and the upper end of vapour and liquid knockout drum 5 through the pipeline intercommunication. A byproduct steam pipe 51 for discharging byproduct steam is connected to the top of the vapor-liquid separation tank 5. And a heat removal coil 4 is arranged in the reaction section, hot water is introduced into the heat removal coil 4, so that the reaction heat can be taken away through circulating hot water in the tube, and the continuous reaction is ensured.
Wherein the upper end of the vapor-liquid separation tank 5 is higher than the top of the heat removal coil 4. Outside the fluidized bed reactor 1, a vapor-liquid separation tank 5 is arranged at a height slightly higher than the top of the heat removal coil 4 in the fluidized bed reactor 1. The hot water in the heat-removing coil 4 is partially vaporized after being heated, and the density of the hot water is less than that of the hot water in the vapor-liquid separation tank 5. Under the pressure pushing generated by the density difference, hot water and water/steam mixed liquid naturally circulate between the heat removal coil pipe 4 and the steam-liquid separation tank 5, the steam-water mixed liquid is separated in the steam-liquid separation tank 5, and byproduct steam is output from the top of the steam-liquid separation tank 5.
Further, a cyclone group 6 is installed at the top of the fluidized bed reactor 1. The cyclone separator group 6 is arranged outside the top of the fluidized bed reactor 1, and the reaction product gas enters the cyclone separator group 6 after coming out of the top of the fluidized bed reactor 1. The catalyst particles are separated in a cyclone group 6, the cyclone group 6 is arranged vertically above the fluidized bed reactor 1, a discharging pipe of the separated catalyst particles is directly inserted into the fluidized bed reactor 1, the separated catalyst particles return to the fluidized bed reactor 1 by means of gravity, and the product gas from the cyclone group 6 is further processed in a downstream process.
The cyclone separator group 6 comprises a first cyclone separator 61 and a second cyclone separator 62, wherein the upper section of the first cyclone separator 61 is connected with the top of the fluidized bed reactor 1 through a pipeline, the bottom of the first cyclone separator 61 is connected with a first blanking pipe 63, and the first blanking pipe 63 is inserted into the fluidized bed reactor 1; the upper section of the second cyclone 62 is connected with the top of the first cyclone 61 through a pipeline, a second discharging pipe 64 is arranged at the bottom of the second cyclone 62, and the second discharging pipe 64 is inserted into the fluidized bed reactor 1. The reaction product gas sequentially passes through the first cyclone separator 61 and the second cyclone separator 62, so that the catalyst in the reaction product gas can be fully separated. An exhaust pipe 65 is connected to the top of the second cyclone 62, and the product gas from the second cyclone 62 is further processed in a downstream process.
The invention relates to a method for producing chloroethylene by acetylene method, which comprises the following steps:
S1: adding a catalyst in the fluidized bed reactor 1; wherein, the carrier of the catalyst is alumina particles, and the active ingredient of the catalyst is gold chloride or copper chloride;
S2: introducing a mixed gas of acetylene and hydrogen chloride into the bottom of the fluidized bed reactor 1;
S3: after the mixed gas reacts in the fluidized bed reactor 1, the product gas is discharged from the cyclone separator group 6; the reaction heat in the fluidized bed reactor 1 is absorbed by the heat removal coil 4 and transferred to the vapor-liquid separation tank 5.
In the invention, the reactor is a fluidized bed, so that the production efficiency of the invention is higher. The catalyst has the advantages that the carrier of the catalyst is alumina particles, the active ingredient of the catalyst is gold chloride or copper chloride, and the catalyst with the carrier of the alumina particles has good abrasion resistance, so that the catalyst meets the abrasion resistance requirement in a fluidized bed.
The molar ratio of the hydrogen chloride to the acetylene in the mixed gas is 1.01-1.08; the reaction temperature is 150-260 ℃; the pressure at the top of the reactor is 10-100 kPaG; the temperature of the hot water for removing heat is 140-200 ℃. The alumina particles have an average particle diameter of 50 to 150 mu m and an active ingredient content of 0.001 to 0.5% by weight.
The specific implementation cases are as follows:
Case 1: the molar ratio of hydrogen chloride to acetylene in the reaction feed mixture is 1.05; the reaction temperature is 200 ℃; the reactor head pressure was 40kPaG; the temperature of the hot water for heat removal is 170 ℃. Gold chloride in the catalyst 0.2% wt.
Case 2: the molar ratio of hydrogen chloride to acetylene in the reaction feed mixture is 1.01; the reaction temperature is 150 ℃; the reactor head pressure was 100kPaG; the temperature of the hot water for heat removal is 140 ℃. Gold chloride in the catalyst 0.5% wt.
Case 3: the molar ratio of hydrogen chloride to acetylene in the reaction feed mixture is 1.08; the reaction temperature is 260 ℃; the reactor head pressure was 10kPaG; the temperature of the hot water for heat removal is 200 ℃. Gold chloride in the catalyst 0.001% wt.
The invention is not limited to the above-described alternative embodiments, and any person who may derive other various forms of products in the light of the present invention, however, any changes in shape or structure thereof, all falling within the technical solutions defined in the scope of the claims of the present invention, fall within the scope of protection of the present invention.
Claims (1)
1. The fluidized bed system for producing chloroethylene by an acetylene method is characterized by comprising a fluidized bed reactor (1), wherein a catalyst is arranged in the fluidized bed reactor (1), the carrier of the catalyst is alumina particles, the active component of the catalyst is gold chloride or copper chloride, and an air inlet pipe (2) for introducing mixed gas of acetylene and hydrogen chloride is arranged at the bottom of the fluidized bed reactor (1);
A gas distributor (3) is fixed in the fluidized bed reactor (1), a plurality of air holes are formed in the gas distributor (3), the gas distributor (3) is positioned above the air inlet pipe (2), and a catalyst is arranged on the gas distributor (3);
the air holes are uniformly distributed on the gas distributor (3);
a heat removing coil pipe (4) is arranged in the fluidized bed reactor (1), a vapor-liquid separation tank (5) is arranged outside the fluidized bed reactor (1), the lower end of the heat removing coil pipe (4) is communicated with the lower end of the vapor-liquid separation tank (5) through a pipeline, and the upper end of the heat removing coil pipe (4) is communicated with the upper end of the vapor-liquid separation tank (5) through a pipeline;
The top of the vapor-liquid separation tank (5) is connected with a byproduct steam pipe (51) for discharging byproduct steam;
The upper end of the vapor-liquid separation tank (5) is higher than the top of the heat removal coil pipe (4);
the top of the fluidized bed reactor (1) is provided with a cyclone separator group (6);
The cyclone separator group (6) comprises a first cyclone separator (61) and a second cyclone separator (62), the bottom of the first cyclone separator (61) is connected with a first blanking pipe (63), and the first blanking pipe (63) is inserted into the fluidized bed reactor (1); the bottom of the second cyclone separator (62) is provided with a second blanking pipe (64), and the second blanking pipe (64) is inserted into the fluidized bed reactor (1); the upper section of the first cyclone separator (61) is connected with the top of the fluidized bed reactor (1) through a pipeline, and the upper section of the second cyclone separator (62) is connected with the top of the first cyclone separator (61) through a pipeline;
the top of the second cyclone separator (62) is connected with an exhaust pipe (65);
the shape of the carrier of the catalyst is spherical, a plurality of pores are arranged on the carrier of the catalyst, and the active ingredients of the catalyst are filled in the pores of the carrier of the catalyst.
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| CN202110727880.2A CN113457585B (en) | 2021-06-29 | 2021-06-29 | Fluidized bed system for producing chloroethylene by acetylene method |
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| CN202110727880.2A CN113457585B (en) | 2021-06-29 | 2021-06-29 | Fluidized bed system for producing chloroethylene by acetylene method |
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| CN215506701U (en) * | 2021-06-29 | 2022-01-14 | 中国成达工程有限公司 | Fluidized bed system for producing chloroethylene by acetylene method |
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| BE632044A (en) * | 1962-05-08 | |||
| BE848731A (en) * | 1975-11-28 | 1977-05-25 | CATALYTIC OXIDATION PROCESS OF VINYL CHLORIDE, | |
| CA1109853A (en) * | 1977-10-19 | 1981-09-29 | Michael F. Lemanski | Catalyst and process for production of vcm |
| KR101114363B1 (en) * | 2006-09-04 | 2012-02-13 | 주식회사 엘지화학 | Method for preparing vinyl chloride from 1,2-dichloroethane |
| CN101786939A (en) * | 2010-03-04 | 2010-07-28 | 大连化工研究设计院 | Method for preparing vinyl chloride by reacting ammonium chloride with acetylene |
| CN108786670B (en) * | 2017-04-27 | 2021-01-26 | 中国科学院大连化学物理研究所 | Method for preparing p-xylene and co-producing low-carbon olefin by methanol and/or dimethyl ether and toluene |
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| CN215506701U (en) * | 2021-06-29 | 2022-01-14 | 中国成达工程有限公司 | Fluidized bed system for producing chloroethylene by acetylene method |
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