CN113354505A - Separation device and separation method for preventing catalytic gas fractionation device from coking at bottom of depropanizer - Google Patents
Separation device and separation method for preventing catalytic gas fractionation device from coking at bottom of depropanizer Download PDFInfo
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Abstract
The invention provides a separation device for preventing the bottom of a depropanizer of a catalytic gas fractionation device from coking, which comprises a high-pressure depropanizer and a low-pressure depropanizer; an inlet pipeline is arranged in the middle of the high-pressure depropanizing tower, a first tower top gas phase delivery pipeline is arranged at the top of the high-pressure depropanizing tower, and a first tower top condenser and a first tower top reflux tank are sequentially arranged on the first tower top gas phase delivery pipeline along the gas phase flowing direction; according to the invention, a high-pressure and low-pressure double-tower depropanization process is adopted, hot water at 80-95 ℃, low-temperature process material waste heat or low-pressure steam in a factory is used as a heat source at the tower bottom, so that the operation temperature at the tower bottom of the depropanization tower is effectively reduced, the problem of coking and blockage at the tower bottom of the depropanization tower is fundamentally solved, and the problems of processing load reduction and unplanned shutdown of a catalytic gas separation device caused by coking and blockage at the tower bottom of the depropanization tower are avoided; meanwhile, the steam consumption at the bottom of the depropanizing tower is saved, and the energy consumption of the device is reduced.
Description
Technical Field
The invention relates to a separation device for double-tower depropanization in a catalytic gas fractionation device, in particular to a separation device and a separation method for preventing the bottom of a depropanization tower of the catalytic gas fractionation device from coking.
Background
The gas fractionation device is a matched production unit for catalytic cracking and catalytic cracking, and mainly aims to recover and separate propylene and propane products in catalytic liquefied gas (liquid hydrocarbon). The catalytic cracking is higher than the conventional catalytic cracking unit in propylene yield and butadiene content due to higher severity. Liquid hydrocarbons produced by catalytic cracking and catalytic cracking devices are treated by a refining unit (alkali washing, desulfurization and mercaptan removal) and then are sent to a downstream gas fractionation device for fractionation.
Catalytic gas fractionation plants at home and abroad are usually designed according to a three-tower process (depropanizer, deethanizer and propylene rectifier). The feed to the depropanizer contains unsaturated hydrocarbons with C4 and above C4, wherein the butadiene polymerization activity is very high, and the polymer is easily generated at a higher temperature, so that a reboiler at the bottom of the depropanizer is coked and blocked, the heat exchange effect of the reboiler is deteriorated, and the processing load of a device is influenced and the device is shut down unplanned in severe cases. At present, the operation pressure at the top of a depropanizing tower is generally 1.8-2.0MPag, the temperature at the bottom of the depropanizing tower is about 104 ℃, a reboiler at the bottom of the depropanizing tower adopts 0.5MPa steam as a heat source, the steam consumption is high, the energy consumption is high, and the reboiler is easy to be blocked by polymerization coking of butadiene in materials in the reboiler at the bottom of the depropanizing tower.
The problem of coking and blocking at the bottom of a depropanizer of a catalytic cracking and catalytic cracking gas fractionation device is solved by adopting a method of injecting a polymerization inhibitor into a depropanizer feeding material or a tower bottom material. The problem of coking and blocking at the bottom of the depropanizing tower can be relieved to a certain extent by injecting the polymerization inhibitor, but the problem of butadiene polymerization and coking in materials in a reboiler at the bottom of the depropanizing tower cannot be fundamentally solved, and the production and operation cost is increased.
Disclosure of Invention
The invention aims to provide a separation device and a separation method for preventing the bottom of a depropanizer of a catalytic gas fractionation device from coking, so as to solve the problems in the background technology.
In order to achieve the purpose, the invention provides the following technical scheme:
a separation device for preventing the bottom of a depropanizer of a catalytic gas fractionation device from coking comprises a high-pressure depropanizer and a low-pressure depropanizer;
an inlet pipeline is arranged in the middle of the high-pressure depropanizing tower, a first tower top gas phase delivery pipeline is arranged at the top of the high-pressure depropanizing tower, and a first tower top condenser and a first tower top reflux tank are sequentially arranged on the first tower top gas phase delivery pipeline along the gas phase flowing direction;
the top of the first tower top reflux tank is provided with a fuel gas discharge pipeline, the bottom of the first tower top reflux tank is respectively provided with a first liquid phase reflux pipeline and a liquid phase delivery pipeline, and the outlet of the first liquid phase reflux pipeline is communicated and connected with the top of the high-pressure depropanizing tower;
a first tower bottom liquid phase delivery pipeline is arranged at the bottom of the high-pressure depropanizing tower, and an outlet of the first tower bottom liquid phase delivery pipeline is communicated with the low-pressure depropanizing tower; a first reboiler is arranged on a liquid phase delivery pipeline at the bottom of the first tower, and an outlet of the first reboiler is communicated and connected with the bottom of the high-pressure depropanizing tower;
a second tower top gas phase delivery pipeline is arranged at the top of the low-pressure depropanizing tower, and a second tower top condenser and a second tower top reflux tank are sequentially arranged on the second tower top gas phase delivery pipeline along the gas phase flowing direction;
a second liquid phase reflux pipeline and a circulating pipeline are respectively arranged at the bottom of the second tower top reflux tank, the outlet of the second liquid phase reflux pipeline is in conduction connection with the top of the low-pressure depropanizing tower, and the outlet of the circulating pipeline is in conduction connection with the high-pressure depropanizing tower;
and a second tower bottom liquid phase delivery pipeline is arranged at the bottom of the low-pressure depropanizing tower, a second reboiler is arranged on the second tower bottom liquid phase delivery pipeline, and an outlet of the second reboiler is communicated and connected with the bottom of the low-pressure depropanizing tower.
As a further scheme of the invention: the theoretical plates of the high-pressure depropanizer are 15-80 layers, the operation pressure at the top of the tower is 1.3-1.6MPag, the temperature at the top of the tower is 30-45 ℃, and the temperature at the bottom of the tower is 60-90 ℃.
As a further scheme of the invention: the theoretical plates of the low-pressure depropanizing tower are 15-80 layers, the operation pressure at the top of the tower is 0.5-1.0MPag, the temperature at the top of the tower is 30-50 ℃, and the temperature at the bottom of the tower is 60-90 ℃.
As a further scheme of the invention: the first reboiler adopts hot water at 80-95 ℃ in a factory, waste heat of low-temperature-level process materials or low-pressure steam as a heat source; the second reboiler adopts hot water of 80-95 ℃ in a factory, waste heat of low-temperature-level process materials or low-pressure steam as a heat source.
A separation method for preventing the bottom of a depropanizer of a catalytic gas fractionation plant from coking comprises the following steps:
s1, feeding the liquid hydrocarbon material from the upstream device into a high-pressure depropanizing tower through an inlet pipeline;
s2, cooling the gas-phase material at the top of the high-pressure depropanizing tower by a first tower top condenser to form condensate, and feeding the condensate into a first tower top reflux tank; the condensate in the first tower top reflux tank is pressurized by a pump and then is divided into two parts, one part returns to the top of the high-pressure depropanizing tower through a first liquid phase reflux pipeline, and the other part is sent to a downstream device for continuous fractionation through a liquid phase delivery pipeline; the non-condensable gas in the first tower top reflux tank is discharged by a fuel gas discharge pipeline;
s3, heating a part of the liquid phase material at the bottom of the high-pressure depropanizing tower in a first reboiler, returning the heated part of the liquid phase material to the bottom of the high-pressure depropanizing tower, and sending the other part of the liquid phase material to the low-pressure depropanizing tower for continuous fractionation;
s4, cooling the gas-phase material from the top of the low-pressure depropanizing tower by a second tower top condenser to form condensate, and feeding the condensate into a second tower top reflux tank; the condensate in the reflux tank at the top of the second tower is pressurized by a pump and then is divided into two parts, one part returns to the top of the low-pressure depropanizing tower through a second liquid phase reflux pipeline, and the other part returns to the upper part of the high-pressure depropanizing tower through a circulating pipeline in a circulating way;
s5, feeding a part of the liquid phase material at the bottom of the low-pressure depropanizing tower into a second reboiler for heating and then returning to the bottom of the low-pressure depropanizing tower, and feeding the other part of the liquid phase material to a downstream device for continuous separation after the other part of the liquid phase material is pressurized by a pump.
Compared with the prior art, the invention has the beneficial effects that:
1. compared with the high-pressure depropanizing tower separation technology and the separation method adopted by the existing catalytic cracking and catalytic cracking gas fractionation device, the method can effectively prevent the tower bottom of the depropanizing tower from coking and blocking and reduce the energy consumption of the gas fractionation device under the condition of meeting the separation precision requirement of the depropanizing tower of the gas fractionation device.
2. According to the invention, a high-pressure and low-pressure double-tower depropanization process is adopted, hot water at 80-95 ℃, low-temperature process material waste heat or low-pressure steam in a factory is used as a heat source at the tower bottom, so that the operation temperature at the tower bottom of the depropanization tower is effectively reduced, the problem of coking and blockage at the tower bottom of the depropanization tower is fundamentally solved, and the problems of processing load reduction and unplanned shutdown of a catalytic gas separation device caused by coking and blockage at the tower bottom of the depropanization tower are avoided; meanwhile, the steam consumption at the bottom of the depropanizing tower is saved, and the energy consumption of the device is reduced.
3. The method has the advantages that the separation effect of C3 and C4 in the catalytic liquid hydrocarbon is not affected, the operation temperature at the bottom of the depropanizing tower is reduced by adopting a high-pressure and low-pressure double-tower depropanizing system, the problem of polymerization coking blockage at the bottom of the depropanizing tower is effectively solved, the production operation period of a gas separation device is prolonged, and the decoking cost is saved; meanwhile, the steam consumption of a reboiler at the bottom of the depropanizing tower is saved, and the energy conservation and the efficiency improvement are realized.
Drawings
FIG. 1 is a schematic structural diagram of a separation device and a separation method for preventing the bottom of a depropanizer of a catalytic gas fractionation device from coking.
In the figure: 1. a high pressure depropanizer; 2. a low pressure depropanizer; 3. an inlet line; 4. a first overhead vapor phase export line; 5. a first overhead condenser; 6. a first overhead reflux drum; 7. a fuel gas discharge line; 8. a first liquid phase return line; 9. a liquid phase delivery line; 10. a first bottoms liquid phase export line; 11. a first reboiler; 12. a second overhead vapor phase export line; 13. a second overhead condenser; 14. a second overhead reflux drum; 15. a second liquid phase return line; 16. a recycle line; 17. a second bottoms liquid phase export line; 18. a second reboiler.
Detailed Description
The technical solution of the present patent will be described in further detail with reference to the following embodiments.
Referring to fig. 1, a separation apparatus for preventing coking at the bottom of a depropanizer of a catalytic gas fractionation plant comprises a high pressure depropanizer 1 and a low pressure depropanizer 2; the middle part of the high-pressure depropanizing tower 1 is provided with an inlet pipeline 3 for inputting materials; a first tower top gas phase delivery pipeline 4 is arranged at the top of the high-pressure depropanizing tower 1, and a first tower top condenser 5 and a first tower top reflux tank 6 are sequentially arranged on the first tower top gas phase delivery pipeline 4 along the gas phase flowing direction; the first tower top condenser 5 adopts circulating water or refrigerant water as a cold source to cool the gas-phase material. A fuel gas discharge pipeline 7 is arranged at the top of the first tower top reflux tank 6, a first liquid phase reflux pipeline 8 and a liquid phase delivery pipeline 9 are respectively arranged at the bottom of the first tower top reflux tank 6, and an outlet of the first liquid phase reflux pipeline 8 is communicated and connected with the top of the high-pressure depropanizer 1; a first tower bottom liquid phase delivery pipeline 10 is arranged at the bottom of the high-pressure depropanizing tower 1, and an outlet of the first tower bottom liquid phase delivery pipeline 10 is communicated with the low-pressure depropanizing tower 2; a first reboiler 11 is arranged on the first tower bottom liquid phase delivery pipeline 10, and an outlet of the first reboiler 11 is communicated and connected with the bottom of the high-pressure depropanizing tower 1; a second tower top gas phase delivery pipeline 12 is arranged at the top of the low-pressure depropanizing tower 2, a second tower top condenser 13 and a second tower top reflux tank 14 are sequentially arranged on the second tower top gas phase delivery pipeline 12 along the gas phase flowing direction, and the second tower top condenser 13 adopts circulating water or refrigerant water as a cold source to cool gas phase materials; a second liquid phase reflux pipeline 15 and a circulating pipeline 16 are respectively arranged at the bottom of the second tower top reflux tank 14, an outlet of the second liquid phase reflux pipeline 15 is in conduction connection with the top of the low-pressure depropanizing tower 2, and an outlet of the circulating pipeline 16 is in conduction connection with the high-pressure depropanizing tower 1; a second tower bottom liquid phase delivery pipeline 17 is arranged at the bottom of the low-pressure depropanizing tower 2, a second reboiler 18 is arranged on the second tower bottom liquid phase delivery pipeline 17, and an outlet of the second reboiler 18 is communicated and connected with the bottom of the low-pressure depropanizing tower 2.
Further, the theoretical plates of the high-pressure depropanizing tower 1 are 15-80 layers, the operation pressure at the top of the tower is 1.3-1.6MPag, the temperature at the top of the tower is 30-45 ℃, and the temperature at the bottom of the tower is 60-90 ℃.
Further, the theoretical plate of the low-pressure depropanizing tower 2 is 15-80 layers, the operation pressure at the top of the tower is 0.5-1.0MPag, the temperature at the top of the tower is 30-50 ℃, and the temperature at the bottom of the tower is 60-90 ℃.
Further, the first reboiler 11 adopts hot water at 80-95 ℃ in a factory, waste heat of low-temperature-level process materials or low-pressure steam as a heat source; the second reboiler 18 adopts hot water of 80-95 ℃ in a factory, waste heat of low-temperature-level process materials or low-pressure steam as a heat source.
A separation method for preventing the bottom of a depropanizer of a catalytic gas fractionation plant from coking comprises the following steps:
s1, feeding the liquid hydrocarbon material from the upstream device into a high-pressure depropanizing tower 1 through an inlet pipeline 3;
s2, cooling the gas-phase material at the top of the high-pressure depropanizing tower 1 by a first tower top condenser 5 to form condensate, and feeding the condensate into a first tower top reflux tank 6; the condensate in the first tower top reflux tank 6 is pressurized by a pump and then divided into two parts, one part returns to the top of the high-pressure depropanizing tower 1 through a first liquid phase reflux pipeline 8, and the other part is sent to a downstream device deethanizing tower or a propylene rectifying tower through a liquid phase delivery pipeline 9 for continuous fractionation; the non-condensable gas in the first tower top reflux tank 6 is discharged by a fuel gas discharge pipeline 7;
s3, heating a part of the liquid phase material at the bottom of the high-pressure depropanizing tower 1 in a first reboiler 11, returning the heated part of the liquid phase material to the bottom of the high-pressure depropanizing tower 1, and sending the other part of the liquid phase material to the low-pressure depropanizing tower 2 for continuous fractionation;
s4, cooling the gas-phase material from the top of the low-pressure depropanizing tower 2 by a second tower top condenser 13 to form condensate, and feeding the condensate into a second tower top reflux tank 14; the condensate in the second tower top reflux tank 14 is pressurized by a pump and then divided into two parts, one part returns to the top of the low-pressure depropanizing tower 2 through a second liquid phase reflux pipeline 15, and the other part returns to the upper part of the high-pressure depropanizing tower 1 through a circulating pipeline 16 in a circulating way;
s5, feeding a part of the liquid phase material at the bottom of the low-pressure depropanizing tower 2 into the second reboiler 18 for heating and then returning to the bottom of the low-pressure depropanizing tower 2, and feeding the other part of the liquid phase material to a downstream device for continuous separation after being pressurized by a pump.
In this example, the high pressure depropanizer 1 had 35 theoretical plates, an operating pressure at the top of the column of 1.6MPag, a temperature at the top of the column of 41 ℃, a temperature at the condenser of 40 ℃ and a temperature at the bottom of the column of 73.4 ℃. The inlet line 3 is located above the tray 36 level of the high pressure depropanizer 1. The first overhead condenser 5 uses circulating water as a cold source. The fuel gas is discharged to the plant fuel gas network through a fuel gas discharge line 7. The first reboiler 11 uses hot water of 90 c as a heat source.
The theoretical plate of the low-pressure depropanizer 2 is 25 layers, the operation pressure at the top of the tower is 0.8MPag, the temperature at the top of the tower is 43 ℃, the condenser at the top of the tower is 30.6 ℃, and the temperature at the bottom of the tower is 73 ℃. The outlet of the first bottom liquid phase sending-out line 10 is connected to a position above the tray 12 layer of the low-pressure depropanizer 2. The second reboiler 18 uses 90 c hot water as a heat source. The second tower top condenser 13 adopts circulating water and 7 ℃ refrigerant water as cold sources to be connected in series for gradual cooling.
The separation device and the separation method have the advantages that the separation effect of C3 and C4 in the catalytic liquid hydrocarbon is not affected, the operation temperature at the bottom of the depropanizing tower is reduced by adopting a high-pressure and low-pressure double-tower depropanizing system, the problem of polymerization, coking and blockage at the bottom of the depropanizing tower is effectively solved, the production operation period of the gas separation device is prolonged, and the decoking cost is saved; meanwhile, the reboiler at the bottom of the depropanization tower saves steam of 0.5MPa by about 22t/h, thereby realizing energy conservation and efficiency improvement.
Although the preferred embodiments of the present patent have been described in detail, the present patent is not limited to the above embodiments, and various changes can be made without departing from the spirit of the present patent within the knowledge of those skilled in the art.
Claims (5)
1. A separation device for preventing the bottom of a depropanizer of a catalytic gas fractionation device from coking is characterized by comprising a high-pressure depropanizer (1) and a low-pressure depropanizer (2);
an inlet pipeline (3) is arranged in the middle of the high-pressure depropanizing tower (1), a first tower top gas phase delivery pipeline (4) is arranged at the top of the high-pressure depropanizing tower (1), and a first tower top condenser (5) and a first tower top reflux tank (6) are sequentially arranged on the first tower top gas phase delivery pipeline (4) along the gas phase flowing direction;
a fuel gas discharge pipeline (7) is arranged at the top of the first tower top reflux tank (6), a first liquid phase reflux pipeline (8) and a liquid phase delivery pipeline (9) are respectively arranged at the bottom of the first tower top reflux tank (6), and an outlet of the first liquid phase reflux pipeline (8) is in conduction connection with the top of the high-pressure depropanizing tower (1);
a first tower bottom liquid phase delivery pipeline (10) is arranged at the bottom of the high-pressure depropanizing tower (1), and an outlet of the first tower bottom liquid phase delivery pipeline (10) is communicated with the low-pressure depropanizing tower (2); a first reboiler (11) is arranged on the first tower bottom liquid phase delivery pipeline (10), and an outlet of the first reboiler (11) is communicated and connected with the bottom of the high-pressure depropanizing tower (1);
a second tower top gas phase delivery pipeline (12) is arranged at the top of the low-pressure depropanizing tower (2), and a second tower top condenser (13) and a second tower top reflux tank (14) are sequentially arranged on the second tower top gas phase delivery pipeline (12) along the gas phase flowing direction;
a second liquid phase reflux pipeline (15) and a circulating pipeline (16) are respectively arranged at the bottom of the second tower top reflux tank (14), the outlet of the second liquid phase reflux pipeline (15) is communicated and connected with the top of the low-pressure depropanizing tower (2), and the outlet of the circulating pipeline (16) is communicated and connected with the high-pressure depropanizing tower (1);
a second tower bottom liquid phase delivery pipeline (17) is arranged at the bottom of the low-pressure depropanizing tower (2), a second reboiler (18) is arranged on the second tower bottom liquid phase delivery pipeline (17), and an outlet of the second reboiler (18) is communicated and connected with the bottom of the low-pressure depropanizing tower (2).
2. The separation apparatus for preventing the bottom of the depropanizer of the catalytic gas fractionation plant from coking according to claim 1, wherein the high pressure depropanizer (1) has 15-80 theoretical plates, the top operating pressure is 1.3-1.6MPag, the top temperature is 30-45 ℃ and the bottom temperature is 60-90 ℃.
3. The separation apparatus for preventing bottom coking of depropanizer of catalytic gas fractionation plant according to claim 1, wherein said low pressure depropanizer (2) has a theoretical plate 15-80 layers, an operating pressure at the top of the column of 0.5-1.0MPag, a temperature at the top of the column of 30-50 ℃ and a temperature at the bottom of the column of 60-90 ℃.
4. The separation device for preventing the bottom of the depropanizer of the catalytic gas fractionation plant from coking according to claim 1, wherein the first reboiler (11) adopts hot water at 80-95 ℃, waste heat of low-temperature-level process materials or low-pressure steam as a heat source; the second reboiler (18) adopts hot water at the temperature of 80-95 ℃ in a factory, waste heat of low-temperature-level process materials or low-pressure steam as a heat source.
5. A separation method for preventing the bottom of a depropanizer of a catalytic gas fractionation plant from coking is characterized by comprising the following steps:
s1, feeding the liquid hydrocarbon material from the upstream device into a high-pressure depropanizing tower (1) through an inlet pipeline (3);
s2, cooling a gas phase material at the top of the high-pressure depropanizing tower (1) by a first tower top condenser (5) to form a condensate, and feeding the condensate into a first tower top reflux tank (6); the condensate in the first tower top reflux tank (6) is pressurized by a pump and then divided into two parts, one part returns to the top of the high-pressure depropanizing tower (1) through a first liquid phase reflux pipeline (8), and the other part is sent to a downstream device for continuous fractionation through a liquid phase delivery pipeline (9); the non-condensable gas in the first tower top reflux tank (6) is discharged by a fuel gas discharge pipeline (7);
s3, heating a part of liquid phase material at the bottom of the high-pressure depropanizing tower (1) in a first reboiler (11), returning the heated part of liquid phase material to the bottom of the high-pressure depropanizing tower (1), and sending the other part of liquid phase material to the low-pressure depropanizing tower (2) for continuous fractionation;
s4, cooling the gas-phase material from the top of the low-pressure depropanizing tower (2) by a second tower top condenser (13) to form condensate, and feeding the condensate into a second tower top reflux tank (14); the condensate in the second tower top reflux tank (14) is pressurized by a pump and then divided into two parts, one part returns to the top of the low-pressure depropanizing tower (2) through a second liquid phase reflux pipeline (15), and the other part returns to the upper part of the high-pressure depropanizing tower (1) through a circulating pipeline (16);
s5, feeding a part of the liquid phase material at the bottom of the low-pressure depropanizing tower (2) into a second reboiler (18) for heating and then returning to the bottom of the low-pressure depropanizing tower (2), and pumping the other part of the liquid phase material to a downstream device for continuous separation.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102464546A (en) * | 2011-08-17 | 2012-05-23 | 中国寰球工程公司 | Double-tower depropanization process for reducing reboiler scaling |
| CN103304358A (en) * | 2013-05-29 | 2013-09-18 | 中建安装工程有限公司 | Separating method and equipment of low-carbon olefins beneficial to product recovery |
| CN103724147A (en) * | 2013-12-27 | 2014-04-16 | 中国天辰工程有限公司 | Desorption method for butadiene in reaction product of methanol to olefin |
| CN103896702A (en) * | 2012-12-27 | 2014-07-02 | 中国石油天然气股份有限公司 | Light hydrocarbon separation method and system for pre-cutting from middle of fractions |
| CN110092701A (en) * | 2018-01-31 | 2019-08-06 | 中国寰球工程有限公司 | The lighter hydrocarbons separation system and method for MTO product mix gas |
-
2021
- 2021-03-19 CN CN202110293963.5A patent/CN113354505A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102464546A (en) * | 2011-08-17 | 2012-05-23 | 中国寰球工程公司 | Double-tower depropanization process for reducing reboiler scaling |
| CN103896702A (en) * | 2012-12-27 | 2014-07-02 | 中国石油天然气股份有限公司 | Light hydrocarbon separation method and system for pre-cutting from middle of fractions |
| CN103304358A (en) * | 2013-05-29 | 2013-09-18 | 中建安装工程有限公司 | Separating method and equipment of low-carbon olefins beneficial to product recovery |
| CN103724147A (en) * | 2013-12-27 | 2014-04-16 | 中国天辰工程有限公司 | Desorption method for butadiene in reaction product of methanol to olefin |
| CN110092701A (en) * | 2018-01-31 | 2019-08-06 | 中国寰球工程有限公司 | The lighter hydrocarbons separation system and method for MTO product mix gas |
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