CN217568762U - Tower-type gas-liquid-phase chloroethylene production device - Google Patents
Tower-type gas-liquid-phase chloroethylene production device Download PDFInfo
- Publication number
- CN217568762U CN217568762U CN202221389596.5U CN202221389596U CN217568762U CN 217568762 U CN217568762 U CN 217568762U CN 202221389596 U CN202221389596 U CN 202221389596U CN 217568762 U CN217568762 U CN 217568762U
- Authority
- CN
- China
- Prior art keywords
- catalyst
- gas
- liquid
- tower
- chloroethylene
- 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
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provides a tower gas-liquid looks chloroethylene apparatus for producing. The structure of the device comprises a chloroethylene synthetic tower, a condenser, a catalyst storage tank, a catalyst circulating pump and a heat exchanger. The chloroethylene synthetic tower is used for gas-liquid phase countercurrent or cocurrent contact reaction, and is divided into a gas-phase area, a gas-liquid reaction area and a gas-liquid separation area from top to bottom; the raw material gas and the liquid catalyst react in the gas-liquid reaction zone, the reacted liquid catalyst enters the catalyst storage tank, the reacted crude product gas enters the condenser, and the condenser is used for condensing and separating the liquid catalyst carried in the crude product gas. The utility model discloses the gas-liquid phase contact reaction takes place on regular packing surface, and the reaction heat is directly absorbed by liquid catalyst, improves catalyst temperature to directly take out the chloroethylene synthetic tower along with the flow of catalyst, solved among the prior art catalyst surface carbon deposit and blockked up, reaction area of contact diminishes, local temperature runaway, catalyst easily deactivates, product refining process technical problem such as complicated.
Description
Technical Field
The utility model belongs to the technical field of chloroethylene production technique and specifically relates to a tower gas-liquid phase chloroethylene production device.
Background
Vinyl Chloride (VCM), also known as Vinyl chloride (Vinyl chloride), is an important monomer used in polymer chemistry, and is colorless and easily liquefied gas. The vinyl chloride monomer is mainly used for producing polyvinyl chloride resin, and the polyvinyl chloride is a universal plastic with the largest yield in the world, and has wide application in building materials, industrial products, daily necessities, floor leathers, floor tiles, artificial leather, pipes, electric wires and cables, packaging films, bottles, foaming materials, sealing materials, fibers and the like.
Vinyl chloride monomer is industrialized in 1931, and currently, the global VCM production process mainly comprises an ethylene method and a calcium carbide method. According to the natural resources and the productivity structure of China, the calcium carbide method is still a main production technology in the polyvinyl chloride industry of China for a long time. The traditional calcium carbide method is to utilize calcium carbide (calcium carbide) to generate acetylene in water and load HgCl on activated carbon 2 Using acetylene and hydrogen chloride as catalyst to synthesize chloroethyleneA monomer. The reaction is a strong exothermic reaction, and the production of chloroethylene by adopting a fixed bed reactor can cause the activated carbon to load HgCl 2 The surface of the catalyst is locally overheated, carbon deposition blocks a pore channel, the contact area of the catalyst and gas is reduced, the catalyst is quickly inactivated, and the catalytic efficiency of the catalyst is reduced. In addition, local temperature runaway and side reactions are increased, the variety and the number of byproducts are increased, subsequent product refining is difficult, and the product quality is influenced. In addition, the reaction medium for vinyl chloride synthesis is strongly acidic, the reaction temperature is high, all materials in the reactor, which are in contact with the reaction medium, are required to resist strong acid corrosion and high temperature, the cost of the reaction device is high, and the use of the mercury catalyst can cause environmental pollution. The development of a device based on mercury-free catalysts and superior to the existing fixed bed reactors is therefore a research focus of the person skilled in the art.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a tower gas-liquid looks chloroethylene apparatus for producing aims at solving the problem such as the catalysis inefficiency that the tower preparation difficulty, reactor temperature runaway phenomenon and surface carbon deposit of carbide legal system preparation chloroethylene in-process equipment cost height, short-lived, major diameter result in.
The utility model discloses a realize like this: a tower-type gas-liquid phase chloroethylene production device comprises a chloroethylene synthetic tower, a condenser, a catalyst storage tank, a catalyst circulating pump and a heat exchanger.
The chloroethylene synthetic tower is used for gas-liquid phase countercurrent or cocurrent contact reaction, and the interior of the chloroethylene synthetic tower is respectively provided with a gas-phase area, a gas-liquid reaction area and a gas-liquid separation area from top to bottom; the tower wall corresponding to the gas-phase zone is provided with a gas upper interface and a catalyst inlet, a liquid distributor is arranged between the gas-phase zone and the gas-liquid reaction zone and is connected with the catalyst inlet on the tower wall, the tower wall corresponding to the gas-liquid separation zone is provided with a gas lower interface, and the tower wall at the bottom side of the gas-liquid separation zone is provided with a catalyst outlet; the gas upper interface and the gas lower interface are connected with a gas inlet pipeline provided with a control valve, acetylene and hydrogen chloride mixed gas introduced from the gas inlet pipeline enters the chloroethylene synthesis tower through the gas upper interface or the gas lower interface, the mixed gas and a liquid catalyst introduced from a catalyst inlet generate gas-liquid parallel flow or gas-liquid countercurrent reaction in a gas-liquid reaction area to generate chloroethylene, the gas-liquid separation area is separated to obtain a liquid catalyst, the liquid catalyst is discharged from a catalyst outlet of the chloroethylene synthesis tower, and the obtained crude product gas is discharged to a condenser through the gas lower interface or the gas upper interface.
The top of condenser is equipped with the condenser upper shed, is equipped with the product gas export near the lateral wall at the top at the condenser, is equipped with condensate export and condenser end opening in the bottom of condenser, the condenser upper shed links to each other with the outside pipeline of interface and gas end opening on the chloroethylene synthetic tower through the pipeline that has the control valve respectively with the condenser end opening, the condenser is arranged in the liquid catalyst that the condensation separation carried in the crude product gas, and the condensate that obtains sends into the catalyst storage tank.
The top of the catalyst storage tank is provided with a circulating catalyst inlet and a catalyst charging port, the bottom of the catalyst storage tank is provided with a circulating catalyst outlet, and the catalyst storage tank is used for storing liquid catalyst introduced from the circulating catalyst inlet and the catalyst charging port; the circulating catalyst inlet is connected with the catalyst outlet through a pipeline, a circulating catalyst control valve is arranged on the pipeline outside the circulating catalyst outlet, a branch pipeline with a control valve is arranged behind the circulating catalyst control valve, one pipeline is used for circulating heat exchange of the catalyst, and the other pipeline is used for discharging the liquid catalyst.
The catalyst circulating pump is arranged at the downstream of the catalyst storage tank and connected with a pipeline for circulating heat exchange of the catalyst, and the catalyst circulating pump is used for conveying the liquid catalyst in the catalyst storage tank to return to the vinyl chloride synthesis tower for continuously participating in the reaction.
The heat exchanger is arranged on a downstream pipeline of the catalyst circulating pump, and the outlet of the heat exchanger is connected with the catalyst inlet on the chloroethylene synthetic tower through a pipeline and used for adjusting the temperature of the liquid catalyst.
The chloroethylene synthesizing tower adopts a tower shell and lining structure provided with an expansion joint, the tower shell is made of stainless steel or carbon steel, and the lining is a complete acid-resistant ceramic tile lining.
The gas-liquid reaction zone is filled with filler, and the lower part of the gas-liquid reaction zone is provided with a filler supporting device which plays the roles of supporting the filler and uniformly distributing gas.
The chloroethylene synthetic tower is higher than the catalyst storage tank, no liquid is stored at the bottom of the catalyst storage tank, and the liquid catalyst flows into the catalyst storage tank from the catalyst outlet under the action of gravity.
The outer wall of the catalyst storage tank is provided with a jacket, the jacket is provided with a cold and heat source inlet and outlet, and a heat source or a cold source is introduced into the jacket through the cold and heat source inlet and outlet to maintain the temperature of the reaction system and the liquid catalyst constant.
The utility model discloses a tower gas-liquid looks chloroethylene apparatus for producing's beneficial effect as follows:
(1) The utility model discloses a vinyl chloride synthetic tower body adopts tower shell + acidproof ceramic tile lining structure, sets up the expansion joint and has solved the problem of the expend with heat and contract with cold that arouses by normal atmospheric temperature to service temperature 200 ℃ steel shell and inside lining anticorrosive material coefficient of expansion difference. The liquid is not stored at the bottom of the chloroethylene synthetic tower, compared with the traditional fixed bed reactor, the device has the advantage that the production capacity of a single device can be multiplied, the equipment investment is lower than that of the traditional fixed bed chloroethylene synthetic device and tetrafluoro or graphite lining anticorrosion equipment, and the service life is as long as more than 10 years. The production capacity of single equipment of the chloroethylene synthetic fixed bed reactor reaches 7000 tons/year, and the gas-liquid chloroethylene synthetic tower can realize the production capacity of the single equipment of 3 ten thousand tons/year, 5 ten thousand tons/year and 12 ten thousand tons/year.
(2) The gas-liquid phase contact reaction is carried out on the surface of the structured packing, the contact area is large, the reaction efficiency is high, the contact area is stable and unchanged for a long time, the reaction heat is directly absorbed by the liquid catalyst, the temperature of the catalyst is increased, and the catalyst is directly taken out of the chloroethylene synthesis tower along with the flowing of the catalyst, so that the technical problems of carbon deposition blockage on the surface of the catalyst of active carbon loaded by gas-solid phase reaction active carbon, small reaction contact area, local temperature runaway, easy inactivation of the catalyst, complex product refining process and the like in the prior art are solved.
(3) The device can be used for gas-liquid parallel flow reaction and gas-liquid countercurrent reaction, the production capacity of a single device is multiplied, the synthesis reaction temperature is high and stable, convenient conditions are created for the utilization of chloroethylene synthesis reaction heat, 0.6 ton of steam can be produced as a byproduct in the production of 1 ton of chloroethylene, and a new way is provided for the energy conservation and emission reduction of the chloroethylene industry.
Drawings
FIG. 1 is a schematic view of a tower-type gas-liquid phase vinyl chloride production apparatus of the present invention.
FIG. 2 is a schematic view of the vinyl chloride synthesizing tower of the present invention.
Fig. 3 is a schematic structural diagram of the liquid distributor of the present invention.
The various reference numbers in the figures are schematic: A. hydrogen chloride; B. acetylene; C. a crude product gas; D. a liquid catalyst; 1. a vinyl chloride synthesis column; 101. a catalyst outlet; 102. a tower shell; 103. a liner; 104. a gas-liquid separation zone; 105. a packing support means; 106. A gas-liquid reaction zone; 107. a catalyst inlet; 108. a gas phase zone; 109. an upper gas interface; 110. a liquid distributor; 1101. a main pipe; a straight pipe 1102; 1103. a branch pipe; 1104. bending a pipe; 111. a gas lower interface; 2. a condenser; 201. an upper opening of the condenser; 202. a product gas outlet; 203. a condensate outlet; 204. a lower opening of the condenser; 3. a catalyst storage tank; 301. a recycle catalyst inlet; 302. a catalyst charging port; 303. a jacket; 304. a circulating catalyst outlet; 4. a catalyst circulation pump; 5. a heat exchanger; v1, a first control valve; v2, a second control valve; v3, a third control valve; v4, a fourth control valve; v5, a fifth control valve; v6, a catalyst discharge valve; v7, a circulating catalyst control valve.
Detailed Description
Referring to fig. 1, the utility model provides a tower gas-liquid phase chloroethylene production device, including chloroethylene synthetic tower 1, condenser 2, catalyst storage tank 3, catalyst circulating pump 4 and heat exchanger 5.
Referring to fig. 1, 2: the chloroethylene synthesizing tower 1 adopts a tower shell and lining structure provided with an expansion joint, the tower shell is made of stainless steel or carbon steel, and the lining is a complete acid-resistant ceramic tile lining. The vinyl chloride synthesizing tower 1 is divided into three sections from top to bottom, namely a gas phase section 108, a gas-liquid reaction section 106 and a gas-liquid separation section 104. The gas upper interface 109 and the catalyst inlet 107 are arranged on the tower wall corresponding to the gas phase zone 108, and the gas upper interface 109 is positioned at the upper part of the catalyst inlet 107. A liquid distributor 110 is arranged between the gas phase zone 108 and the gas-liquid reaction zone 106, and the liquid distributor 110 is connected with a catalyst inlet 107; a filler supporting device 105 is arranged between the gas-liquid reaction zone 106 and the gas-liquid separation zone 104; the gas-liquid separation zone 104 is provided with a gas lower interface 111 and a catalyst outlet 101 on the tower wall, and the gas lower interface 111 is positioned at the upper part of the catalyst outlet 101.
The upper gas connector 109 and the lower gas connector 111 are both connected with a gas inlet pipeline, a second control valve V2 is arranged on the gas inlet pipeline connected with the upper gas connector 109, and a third control valve V3 is arranged on the gas inlet pipeline connected with the lower gas connector 111. The gases fed in through the inlet duct are hydrogen chloride and acetylene, namely: the hydrogen chloride and acetylene may enter the vinyl chloride synthesis column 1 through the gas upper connection 109 or the gas lower connection 111.
Referring to fig. 3, the liquid distributor 110 includes a header pipe 1101 connected to the catalyst inlet 107, wherein one end of the header pipe 1101 extending into the vinyl chloride synthesis tower 1 is located on the axial line of the vinyl chloride synthesis tower 1 and is connected to two opposite bent pipes 1104 bent downward, and the lower ends of the two bent pipes 1104 are connected to a straight pipe 1102; the straight pipe 1102 is connected with a plurality of branch pipes 1103 on both sides, and the branch pipes 1103 are provided with downward openings for distribution of the liquid catalyst. The manifold 1101, straight tubes 1102, and branch tubes 1103 are all arranged laterally. The liquid catalyst enters the header 1101 from the catalyst inlet 107, then enters the straight pipe 1102 through two bent pipes 1104, and finally is sprayed downward through the openings of the branch pipes 1103.
The gas-liquid reaction zone 106 is filled with filler, and the filler supporting device 105 is positioned below the filler in the gas-liquid reaction zone 106 and plays a role in supporting the filler and uniformly distributing gas. The packing support device 105 is a spherical arch with uniformly distributed through holes through which gas and liquid can pass.
The condenser 2 is sequentially provided with a condenser upper opening 201, a product gas outlet 202, a condensate outlet 203 and a condenser lower opening 204 from top to bottom, the condenser upper opening 201 is connected with a gas upper interface 109 on the chloroethylene synthetic tower 1 through a pipeline, and a first control valve V1 is arranged on the pipeline connected with the condenser upper opening 201 and the gas upper interface 109; the lower port 204 of the condenser is connected with the lower gas port 111 of the vinyl chloride synthesizing tower 1 through a pipeline, and a fourth control valve V4 is arranged on the pipeline connecting the lower port and the gas port.
The catalyst tank 3 is located below the vinyl chloride synthesis column 1, i.e.: the vinyl chloride synthesis tower 1 is positioned higher than the catalyst storage tank 3 so that no liquid is stored at the bottom of the vinyl chloride synthesis tower 1 and the liquid catalyst flows into the catalyst storage tank 3 from the catalyst outlet 101 by gravity.
A circulating catalyst inlet 301 and a catalyst feed inlet 302 are provided at the top of the catalyst storage tank 3, and a circulating catalyst outlet 304 is provided at the bottom thereof. The circulating catalyst inlet 301 is connected with the catalyst outlet 101 on the chloroethylene synthetic tower 1 through a pipeline; the circulating catalyst outlet 304 is externally connected with a pipeline, a fifth control valve V5 is arranged on the external pipeline, two branch pipelines are arranged behind the fifth control valve V5, a catalyst discharge valve V6 is arranged on one pipeline, and a circulating catalyst control valve V7 is arranged on the other pipeline.
The outer wall of the catalyst storage tank 3 is provided with a jacket 303, and the jacket 303 is provided with a cold and heat source inlet and outlet, so that when the liquid catalyst is connected with a heat source, the liquid catalyst is prevented from being too low in temperature and becoming viscous to influence the fluidity; when the cold source is connected, the device is used for cooling when the temperature of the liquid catalyst is high.
The catalyst circulating pump 4 is arranged at the downstream of the catalyst storage tank 3, and the catalyst circulating pump 4 is connected with a pipeline provided with a circulating catalyst control valve V7 to provide power for the circulation of the liquid catalyst in the device.
The heat exchanger 5 is arranged on a downstream pipeline of the catalyst circulating pump 4, two ends of the heat exchanger 5 are respectively connected with the catalyst circulating pump 4 and a catalyst inlet 107 on the chloroethylene synthesizing tower 1 through pipelines, the heat exchanger 5 is used for providing heat required by catalytic reaction at the initial stage of the reaction, and after the reaction is stable, the removal of redundant reaction heat is carried out.
The utility model discloses in, raw materials gas is hydrogen chloride and acetylene, and the catalyst is liquid catalyst, and the reaction product is gaseous chloroethylene. The utility model can be used for gas-liquid parallel flow reaction and gas-liquid countercurrent reaction. The operation of these two cases is described separately below.
The utility model discloses can realize that raw material gas adds from the gaseous interface 109 that goes up of the gaseous phase district 108 of chloroethylene synthetic tower 1, liquid catalyst adds from catalyst entry 107, realizes the gas-liquid cocurrent flow reaction, and its working process is as follows:
as shown in fig. 1 and 2, the first control valve V1, the third control valve V3, the fifth control valve V5, and the catalyst discharge valve V6 are kept closed, and the second control valve V2, the fourth control valve V4, and the circulating catalyst control valve V7 are opened. Fresh liquid catalyst D is added into the catalyst storage tank 3 through the catalyst feed port 302, when the liquid level in the catalyst storage tank 3 reaches a certain height, the fifth control valve V5 is opened, so that the liquid catalyst sequentially passes through the fifth control valve V5 and the circulating catalyst control valve V7, is conveyed by the catalyst circulating pump 4 sequentially passes through the heat exchanger 5 and the catalyst inlet 107, is fed into the vinyl chloride synthesizing tower 1, and is uniformly distributed in the gas-liquid reaction zone 106 through the liquid distributor 110. The mixed gas of acetylene B and hydrogen chloride A introduced from the gas inlet pipeline sequentially passes through the second control valve V2 and the gas upper interface 109 to enter the chloroethylene synthetic tower 1, and performs gas-liquid parallel flow reaction with the liquid catalyst in the gas-liquid reaction zone 106 to generate chloroethylene, and the crude product gas C and the liquid catalyst D enter the gas-liquid separation zone 104 for gas-liquid separation. The liquid catalyst D after the temperature rise of the reaction is discharged from a catalyst outlet 101 and is sent into a catalyst storage tank 3 through a circulating catalyst inlet 301; the crude product gas C carrying a small amount of atomized catalyst droplets is discharged from the gas lower interface 111, enters the condenser 2 from the condenser lower port 204 through a pipeline of the fourth control valve V4, is discharged from the product gas outlet 202, condenses a small amount of atomized catalyst droplets carried in the crude product gas C, discharges condensate through the condensate outlet 203, sends the discharged condensate into the catalyst storage tank 3 through the catalyst feed opening 302, mixes with the reacted liquid catalyst entering the circulating catalyst inlet 301, and continues to participate in the circulating reaction after being cooled by the heat exchanger 5 under the conveying of the catalyst circulating pump 4. When the activity of the liquid catalyst has decreased to a certain level, the circulating catalyst control valve V7 is closed, and the catalyst discharge valve V6 is opened to discharge the catalyst.
The utility model discloses still can realize that raw materials gas adds from the gas of the gas-liquid separation zone 104 of chloroethylene synthetic tower 1 interface 111 down, and liquid catalyst adds from catalyst entry 107, realizes the gas-liquid reaction against current, and its working process is as follows:
as shown in fig. 1 and 2, the second control valve V2, the fourth control valve V4, the fifth control valve V5, and the catalyst discharge valve V6 are kept closed, and the first control valve V1, the third control valve V3, and the circulating catalyst control valve V7 are opened. Fresh liquid catalyst D is added into the catalyst storage tank 3 through the catalyst feed port 302, when the liquid level in the catalyst storage tank 3 reaches a certain height, the fifth control valve V5 is opened, so that the liquid catalyst sequentially passes through the fifth control valve V5 and the circulating catalyst control valve V7, is conveyed by the catalyst circulating pump 4 sequentially passes through the heat exchanger 5 and the catalyst inlet 107, is sent into the vinyl chloride synthesizing tower 1, and is uniformly distributed in the gas-liquid reaction zone 106 through the liquid distributor 110. The acetylene B and hydrogen chloride A mixed gas introduced from the gas inlet pipeline sequentially passes through the third control valve V3 and the gas lower interface 111 to enter the chloroethylene synthetic tower 1, and performs gas-liquid countercurrent reaction with the liquid catalyst in the gas-liquid reaction zone 106 to generate chloroethylene. The liquid catalyst D after the temperature rise of the reaction enters a gas-liquid separation zone 104 under the action of gravity, is discharged from a catalyst outlet 101, and is sent into a catalyst storage tank 3 from a circulating catalyst inlet 301; the crude product gas C carrying a small amount of atomized catalyst droplets enters the gas phase area 108 under the action of pressure, is discharged from a gas upper interface 109, enters the condenser 2 from a condenser upper port 201 through a pipeline of a first control valve V1, is discharged from a product gas outlet 202, is condensed by a small amount of atomized catalyst droplets carried in the crude product gas C, is discharged from a condensate outlet 203, is sent into the catalyst storage tank 3 through a catalyst feeding port 302, is mixed with the reacted liquid catalyst entering from the circulating catalyst inlet 301, and is cooled by a heat exchanger 5 under the conveying of a catalyst circulating pump 4 to continue to participate in the circulating reaction. When the activity of the liquid catalyst has decreased to a certain level, the circulating catalyst control valve V7 is closed, and the catalyst discharge valve V6 is opened to discharge the catalyst.
The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.
Claims (7)
1. A tower-type gas-liquid phase chloroethylene production device is characterized by comprising a chloroethylene synthetic tower, a condenser, a catalyst storage tank, a catalyst circulating pump and a heat exchanger;
the interior of the chloroethylene synthetic tower is divided into three areas from top to bottom, namely a gas phase area, a gas-liquid reaction area and a gas-liquid separation area; a gas upper interface and a catalyst inlet are arranged on the tower wall corresponding to the gas phase area, and the gas upper interface is positioned at the upper part of the catalyst inlet; a gas lower interface and a catalyst outlet are arranged on the tower wall corresponding to the gas-liquid separation zone, and the gas lower interface is positioned at the upper part of the catalyst outlet; a liquid distributor is arranged between the gas phase zone and the gas-liquid reaction zone and is connected with the catalyst inlet; a filler is filled in the gas-liquid reaction zone;
the gas upper connector and the gas lower connector are respectively connected with the gas inlet pipeline through two branch pipes on one hand, and are respectively connected with the condenser through two branch pipes on the other hand, and the branch pipes connected with the gas upper connector and the gas lower connector are respectively provided with a control valve; raw material gas enters a chloroethylene synthesis tower from a gas inlet pipeline through a gas upper connector or a gas lower connector, and reacts with a liquid catalyst entering the chloroethylene synthesis tower from a catalyst inlet in a gas-liquid reaction zone, and crude product gas after reaction enters a condenser from the gas lower connector or the gas upper connector; the condenser is used for condensing and separating a liquid catalyst carried in the crude product gas;
the catalyst storage tank is arranged below the chloroethylene synthetic tower, and after raw material gas and the liquid catalyst react in the gas-liquid reaction zone, the liquid catalyst enters the catalyst storage tank from the catalyst outlet;
the catalyst circulating pump is arranged at the downstream of the catalyst storage tank and is used for conveying the liquid catalyst in the catalyst storage tank to return to the vinyl chloride synthesis tower for continuously participating in the reaction;
the heat exchanger is arranged on a downstream pipeline of the catalyst circulating pump, and an outlet of the heat exchanger is connected with a catalyst inlet on the chloroethylene synthetic tower through a pipeline and is used for adjusting the temperature of the liquid catalyst.
2. The tower-type gas-liquid-phase vinyl chloride production device according to claim 1, wherein the liquid distributor comprises a header pipe connected with the catalyst inlet, one end of the header pipe extending into the vinyl chloride synthesis tower is connected with two opposite bent pipes bent downwards, and the lower ends of the two bent pipes are connected with a straight pipe; the two sides of the straight pipe are connected with a plurality of branch pipes, each branch pipe is provided with a downward opening, the liquid catalyst can enter the main pipe from the catalyst inlet, then enters the straight pipe through the two bent pipes, then enters each branch pipe, and finally is sprayed downwards through the openings on the branch pipes.
3. The tower-type gas-liquid-phase vinyl chloride production device as claimed in claim 1, wherein a packing support device is provided between the gas-liquid reaction zone and the gas-liquid separation zone; the filler supporting device is a spherical arch uniformly distributed with through holes, and gas and liquid can penetrate through the through holes.
4. The tower-type gas-liquid-phase vinyl chloride production device as claimed in claim 1, wherein a jacket is provided on an outer wall of the catalyst storage tank, and a cold and heat source inlet and outlet is provided on the jacket, through which a heat source or a cold source can be introduced into the jacket.
5. The tower-type gas-liquid-phase vinyl chloride production device as claimed in claim 1, wherein the vinyl chloride synthesis tower has a combined structure of a tower shell provided with an expansion joint and a lining, the tower shell is made of stainless steel or carbon steel, and the lining is an acid-resistant ceramic tile lining.
6. The tower-type gas-liquid-phase vinyl chloride production device as claimed in claim 1, wherein a catalyst charging port is further provided at the top of the catalyst storage tank, and a liquid catalyst can be charged into the catalyst storage tank through the catalyst charging port.
7. The tower-type gas-liquid-phase vinyl chloride production apparatus according to claim 6, wherein the liquid catalyst condensed and separated by the condenser is fed into the catalyst storage tank through the catalyst feed port.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221389596.5U CN217568762U (en) | 2022-06-06 | 2022-06-06 | Tower-type gas-liquid-phase chloroethylene production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221389596.5U CN217568762U (en) | 2022-06-06 | 2022-06-06 | Tower-type gas-liquid-phase chloroethylene production device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN217568762U true CN217568762U (en) | 2022-10-14 |
Family
ID=83527112
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202221389596.5U Active CN217568762U (en) | 2022-06-06 | 2022-06-06 | Tower-type gas-liquid-phase chloroethylene production device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN217568762U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117065403A (en) * | 2023-10-17 | 2023-11-17 | 中盐吉兰泰氯碱化工有限公司 | Technology development and application treatment system and technology for removing VOCs gas in polymeric latex |
-
2022
- 2022-06-06 CN CN202221389596.5U patent/CN217568762U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117065403A (en) * | 2023-10-17 | 2023-11-17 | 中盐吉兰泰氯碱化工有限公司 | Technology development and application treatment system and technology for removing VOCs gas in polymeric latex |
| CN117065403B (en) * | 2023-10-17 | 2024-02-06 | 中盐吉兰泰氯碱化工有限公司 | Technology development and application treatment system and technology for removing VOCs gas in polymeric latex |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109134231B (en) | Device and process for continuously producing chloroacetic acid by differential circulation | |
| CN217568762U (en) | Tower-type gas-liquid-phase chloroethylene production device | |
| CN110218151B (en) | Device and method for preparing propyl propionate through tower kettle flash evaporation type heat pump reaction rectification | |
| CN1051075C (en) | Process and apparatus for producing urea with increased yield by stripping with CO2 | |
| CN102102040B (en) | Ash coal gasification low water/gas ratio total low temperature chilling CO sulfur resistant shifting technology | |
| CN108409526B (en) | Methane chloride energy-saving production system and method | |
| CN101492398B (en) | Urea production process of high-efficiency condensation, low-mounting height CO2 air stripping method and high-voltage lamp type full condensation reactor | |
| CN217313451U (en) | Tower type continuous preparation device for bis (fluorosulfonyl) imide | |
| CN109364868A (en) | A kind of continous way chloro thing process units | |
| CN104152198B (en) | Methanation reaction process | |
| CN205295183U (en) | Energy -saving ultra -large methanol synthesis device of production different brackets steam | |
| CN209772061U (en) | Normal-temperature feeding reaction hydrocarbon preparation equipment based on methanol | |
| CN207816054U (en) | A kind of heat exchanger, the four Hydrogenation iso-butane device of mixing carbon using the heat exchanger | |
| CN217016571U (en) | High-efficient photochlorination reactor | |
| CN107011163B (en) | The method that acetylene method gas phase produces vinylacetate | |
| CN215288579U (en) | Tower type countercurrent gas-liquid phase chloroethylene production device | |
| CN202715401U (en) | Fixed bed catalytic reaction device capable of adjusting temperature of material at inlet | |
| CN109456431B (en) | Clean closed-loop production method and system for polyolefin | |
| CN207391310U (en) | For the methyl alcohol vaporizing device of chloromethanes production | |
| CN113121303B (en) | Chloroethylene production process and special device thereof | |
| CN215428945U (en) | Chloroethylene production device | |
| CN105985217A (en) | Reaction system for increasing utilization ratio of reactants in chloromethane production and application of reaction system | |
| CN110327846A (en) | Isothermal reactor and the device and method for carrying out methanation reaction using it | |
| CN217796145U (en) | Device for synthesizing methanol | |
| CN110124590A (en) | A kind of production equipment and its technique of 3- chlorpromazine chloride |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |