CN113354504B - Separation device and separation method for preventing bottom coking of catalytic depropanizer - Google Patents
Separation device and separation method for preventing bottom coking of catalytic depropanizer Download PDFInfo
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- CN113354504B CN113354504B CN202110293929.8A CN202110293929A CN113354504B CN 113354504 B CN113354504 B CN 113354504B CN 202110293929 A CN202110293929 A CN 202110293929A CN 113354504 B CN113354504 B CN 113354504B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
Abstract
The invention provides a separation device for preventing bottom coking of a catalytic depropanizer, which comprises the depropanizer, wherein an inlet pipeline is arranged in the middle of the depropanizer, a tower top gas phase delivery pipeline is arranged at the top of the depropanizer, and a tower top condensing mechanism and a tower top reflux tank are sequentially arranged on the tower top gas phase delivery pipeline along the gas phase flowing direction; the invention adopts a low-pressure depropanization process to separate, effectively reduces the bottom operating temperature, fundamentally solves the problem of coking and blocking at the bottom of the depropanizer, and avoids the reduction of the processing load and unplanned shutdown of the catalytic gas separation device caused by coking and blocking at the bottom of the depropanizer; the bottom temperature is lower, and the bottom reboiler can adopt hot water at 80-95 ℃ of a factory, waste heat of low-temperature process materials or low-pressure steam as a heat source, so that the steam consumption at the bottom of the depropanizer is saved, and the energy consumption of the device is reduced.
Description
Technical Field
The invention relates to a separation device for low-pressure depropanization in a catalytic gas fractionation device, in particular to a separation device and a separation method for preventing bottom coking of a catalytic depropanizer.
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 in severity, and the propylene yield and butadiene content are also higher than those of a conventional catalytic cracking device. Liquid hydrocarbon produced by the catalytic cracking device is treated by a refining unit (alkali washing, desulfurization and mercaptan removal) and then sent to a downstream gas fractionation device for fractionation.
Catalytic gas fractionation units at home and abroad are generally designed in a three column process (depropanizer, deethanizer and propylene rectifier). The depropanizer feed contains C4 and above C4 unsaturated hydrocarbons, wherein the polymerization activity of butadiene is very high, and polymers are easily generated at higher temperature, so that a reboiler at the bottom of the depropanizer is coked and blocked, the heat exchange effect of the reboiler is poor, and the processing load of the device is influenced and the device is stopped in an unplanned way under severe conditions. At present, the operation pressure at the top of the depropanizer is generally 1.8-2.0MPag, the bottom temperature is about 104 ℃, 0.5MPa steam is adopted as a heat source in a reboiler at the bottom of the depropanizer, the steam consumption is large, the energy consumption is high, and butadiene in materials in the reboiler at the bottom of the depropanizer is easy to polymerize and coke to block the reboiler.
The existing problem of coking and blocking at the bottom of a depropanizer of a catalytic cracking gas fractionation device is generally solved by adopting a method of injecting a polymerization inhibitor into the feed or bottom material of the depropanizer. The injection of polymerization inhibitor can alleviate the coking and blocking problems at the bottom of the depropanizer to a certain extent, but the problem of polymerization and coking of butadiene in materials in a reboiler at the bottom of the depropanizer can not 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 bottom coking of a catalytic depropanizer, so as to solve the problems in the prior art.
In order to achieve the above purpose, the present invention provides the following technical solutions:
the separation device for preventing the bottom of the catalytic depropanizer from coking comprises a depropanizer, wherein an inlet pipeline is arranged in the middle of the depropanizer, a tower top gas phase delivery pipeline is arranged at the top of the depropanizer, and a tower top condensing mechanism and a tower top reflux tank are sequentially arranged on the tower top gas phase delivery pipeline along the gas phase flowing direction;
the top of the tower top reflux tank is provided with a fuel gas discharge pipeline, the bottom of the tower top reflux tank is respectively provided with a tower top liquid phase reflux pipeline and a tower top liquid phase delivery pipeline, and the outlet of the tower top liquid phase reflux pipeline is connected with the top of the depropanizer in a conducting way;
the bottom of the depropanizer is provided with a bottom liquid phase delivery pipeline, the bottom liquid phase delivery pipeline is provided with a bottom reboiler, and the outlet of the bottom reboiler is connected with the depropanizer in a conducting way.
As a further scheme of the invention: the tower top condensation mechanism comprises a first branch, a second branch and a third branch which are respectively connected with the tower top gas phase delivery pipeline in a conducting way;
a condenser is arranged on the first branch, and an outlet of the condenser is connected with the tower top reflux tank;
the second branch is sequentially provided with a first tower top gas booster and a cooler along the gas phase flowing direction, and the outlet of the cooler is connected with a tower top reflux tank;
the third branch is sequentially provided with a second tower top gas booster and a tower top gas aftercooler along the gas phase flowing direction, and the outlet of the second tower top gas booster is connected with the tower bottom reboiler; the outlet of the tower bottom reboiler is connected with the tower top gas aftercooler, and the outlet of the tower top gas aftercooler is connected with the tower top reflux tank; the second tower top gas booster, the tower bottom reboiler and the tower top gas aftercooler are matched to form a heat pump system.
As a further scheme of the invention: 15-80 layers of theoretical plates of the depropanizer, wherein the operating pressure of the tower top is 0.5-1.2MPag, the temperature of the tower top is 0-30 ℃, and the temperature of the tower bottom is 60-95 ℃.
As a further scheme of the invention: the bottom reboiler adopts 80-95 ℃ hot water, low temperature process material waste heat or low pressure steam as a heat source.
A separation method for preventing the bottom coking of a catalytic depropanizer, comprising the following steps:
s1, introducing catalytic liquefied gas materials from an upstream device into a depropanizer through an inlet pipeline;
s2, cooling a gas phase material from the top of the depropanizer by a tower top condensing mechanism to form condensate, and enabling the condensate to enter a tower top reflux tank; the condensate in the tower top reflux tank is pressurized by a pump and then is divided into two parts, one part of condensate is returned to the top of the depropanizer as reflux through a tower top liquid phase reflux pipeline, and the other part of condensate is sent to a downstream device from a tower top liquid phase delivery pipeline for continuous separation; the non-condensing steam in the tower top reflux tank is discharged by a fuel gas discharge pipeline;
s3, a part of liquid phase materials at the bottom of the depropanizer enters a reboiler at the bottom of the tower to be heated and then returns to the bottom of the depropanizer, and the other part of the liquid phase materials is pressurized by a pump and then is sent to a downstream device for continuous separation through a liquid phase sending pipeline at the bottom of the tower.
As a further scheme of the invention: in step S2, after the gas phase material at the top of the depropanizer enters the condensing mechanism at the top of the tower, there are three condensing modes:
in the first mode, gas phase materials at the top of the depropanizer enter a first branch and are cooled by a condenser to form condensate;
in the second mode, the gas phase material at the top of the depropanizer enters a second branch, is pressurized by a first tower top gas booster and then enters a cooler to be cooled to form condensate;
and in the third mode, the gas phase material at the top of the depropanizer enters a third branch, is pressurized by a second tower top gas booster, and is cooled by a tower bottom reboiler and a tower top gas aftercooler in sequence to form condensate.
Compared with the prior art, the invention has the beneficial effects that:
1. compared with the separation technology and the separation method of a high-pressure depropanizer adopted by the existing catalytic cracking and catalytic cracking gas fractionation device, the method can effectively prevent coking and blocking at the bottom of the depropanizer and reduce the energy consumption of the catalytic gas fractionation device under the condition of meeting the separation precision requirement of the depropanizer of the gas fractionation device.
2. The invention adopts a low-pressure depropanization process to separate, effectively reduces the bottom operating temperature, fundamentally solves the problem of coking and blocking at the bottom of the depropanizer, and avoids the reduction of the processing load and unplanned shutdown of the catalytic gas separation device caused by coking and blocking at the bottom of the depropanizer; the bottom temperature is lower, the bottom reboiler can adopt hot water at 80-95 ℃ of a factory, waste heat of low-temperature process materials or low-pressure steam as a heat source (or a heat pump system is formed by the bottom reboiler and the top gas booster), so that the steam consumption at the bottom of the depropanizer is saved, and the energy consumption of the device is reduced.
3. When the gas phase material at the top of the depropanizer is condensed, three condensing modes are provided: the first mode is that a supercharger is not used, so that the electricity consumption can be saved, the method is suitable for factories with more sufficient coolant water quantity, and the energy consumption of the device is reduced; in the second mode, after the first tower top gas booster is pressurized, air cooling or circulating water cooling is used, so that the consumption of coolant water can be saved, and the energy consumption of the device is further reduced; and in the third mode, the second tower top gas booster, the tower bottom reboiler and the tower top gas aftercooler form a heat pump system, the tower bottom does not need external heat sources any more, and the energy consumption of the device is reduced more.
4. According to the separation device and the separation method, the separation effect of C3 and C4 in the catalytic liquid hydrocarbon is not affected, and the low-pressure depropanization is adopted, so that the operating temperature at the bottom of the depropanization tower is reduced, the problem of polymerization coking blockage at the bottom of the depropanization tower is effectively solved, the production operation period of the gas separation device is prolonged, and the decoking cost is saved; meanwhile, the steam consumption of the reboiler at the bottom of the depropanizer is saved, and the essential energy conservation and synergy are realized.
Drawings
FIG. 1 is a schematic diagram of a separation apparatus and separation method for preventing coking at the bottom of a catalytic depropanizer.
In the figure: 1. a depropanizer; 2. an inlet line; 3. a gas phase outgoing line at the top of the tower; 4. a tower top condensing mechanism; 401. a first branch; 402. a second branch; 403. a third branch; 404. a condenser; 405. a first overhead gas booster; 406. a cooler; 407. a second overhead gas booster; 408. an overhead gas aftercooler; 5. a top reflux drum; 6. a fuel gas discharge line; 7. an overhead liquid phase reflux line; 8. a tower top liquid phase delivery pipeline; 9. a bottom liquid phase delivery line; 10. a bottom reboiler.
Detailed Description
The technical scheme of the patent is further described in detail below with reference to the specific embodiments.
Referring to fig. 1, a separation device for preventing coking at the bottom of a catalytic depropanizer comprises a depropanizer 1, wherein an inlet pipeline 2 is arranged in the middle of the depropanizer 1 and used for inputting materials; the top of the depropanizer 1 is provided with a tower top gas phase delivery pipeline 3, and the tower top gas phase delivery pipeline 3 is sequentially provided with a tower top condensing mechanism 4 and a tower top reflux tank 5 along the gas phase flowing direction; the top of the tower top reflux tank 5 is provided with a fuel gas discharge pipeline 6 which can directly discharge fuel gas into a torch or be integrated into a fuel gas pipe network; the bottom of the tower top reflux tank 5 is respectively provided with a tower top liquid phase reflux pipeline 7 and a tower top liquid phase delivery pipeline 8, and the outlet of the tower top liquid phase reflux pipeline 7 is connected with the top of the depropanizer 1 in a conducting way; a bottom liquid phase delivery pipeline 9 is arranged at the bottom of the depropanizer 1, a bottom reboiler 10 is arranged on the bottom liquid phase delivery pipeline 9, and an outlet of the bottom reboiler 10 is connected with the depropanizer 1 in a conducting way.
Further, the overhead condensing mechanism 4 comprises a first branch 401, a second branch 402 and a third branch 403 which are respectively connected with the overhead gas-phase delivery pipeline 3 in a conducting way;
a condenser 404 is arranged on the first branch 401, an outlet of the condenser 404 is connected with the tower top reflux tank 5, and chilled water or propylene at 0 ℃ is used as a cold source;
a first tower top gas booster 405 and a cooler 406 are sequentially arranged on the second branch 402 along the gas phase flowing direction, and an outlet of the cooler 406 is connected with the tower top reflux tank 5; the first overhead gas booster 405 boosts the overhead gas to 1.5-2.0MPag and the cooler 406 is air cooled or circulating water cooled.
A second tower top gas booster 407 and a tower top gas aftercooler 408 are sequentially arranged on the third branch 403 along the gas phase flowing direction, and an outlet of the second tower top gas booster 407 is connected with the tower bottom reboiler 10; the outlet of the tower bottom reboiler 10 is connected with a tower top gas aftercooler 408, and the outlet of the tower top gas aftercooler 408 is connected with a tower top reflux tank 5; the second overhead gas booster 407, the bottom reboiler 10, and the overhead gas aftercooler 408 cooperate to form a heat pump system. The second overhead gas booster 407 boosts the overhead gas to 2.5-3.0MPag
Further, the theoretical plate of the depropanizer 1 is 15-80 layers, the tower top operation pressure is 0.5-1.2MPag, the tower top temperature is 0-30 ℃, and the tower bottom temperature is 60-95 ℃.
Further, the bottom reboiler 10 uses 80-95 ℃ hot water, low temperature process material waste heat or low pressure steam as a heat source.
A separation method for preventing the bottom coking of a catalytic depropanizer, comprising the following steps:
s1, introducing catalytic liquefied gas materials from an upstream device into a depropanizer 1 through an inlet pipeline 2;
s2, cooling a gas phase material from the top of the depropanizer 1 through a tower top condensing mechanism 4 to form condensate, and enabling the condensate to enter a tower top reflux tank 5; the condensate in the tower top reflux tank 5 is divided into two parts after being pressurized by a pump, one part of condensate is returned to the top of the depropanizer 1 as reflux through a tower top liquid phase reflux pipeline 7, and the other part of condensate is sent to a downstream device (a deethanizer or a propylene rectifying tower) from a tower top liquid phase sending pipeline 8 for continuous separation; the non-condensing steam in the tower top reflux tank 5 is discharged by a fuel gas discharge pipeline 6;
and S3, heating one part of liquid phase materials at the bottom of the depropanizer 1 in a tower bottom reboiler 10, returning the heated liquid phase materials to the bottom of the depropanizer 1, pressurizing the other part of the liquid phase materials by a pump, and sending the pressurized liquid phase materials to a downstream device through a tower bottom liquid phase delivery pipeline 9 for continuous separation.
Further, in step S2, after the top gas phase material of the depropanizer 1 enters the top condensing mechanism 4, there are three condensing modes:
in the first mode, the gas phase material at the top of the depropanizer 1 enters a first branch 401 and is cooled by a condenser 404 to form condensate;
in the second mode, the gas phase material at the top of the depropanizer 1 enters a second branch 402, is pressurized by a first tower top gas booster 405 and then enters a cooler 406 to be cooled to form condensate;
in the third mode, the gas phase material at the top of the depropanizer 1 enters the third branch 403, is pressurized by the second tower top gas booster 407, and then is cooled by the tower bottom reboiler 10 and the tower top gas aftercooler 408 in sequence to form condensate.
Example 1:
in this example, the depropanizer 1 had 30 theoretical plates, a column top operating pressure of 0.85MPag, a column top temperature of 16℃and a column bottom temperature of 74.3 ℃. The inlet line 2 is located at a position above the deck 10 of the depropanizer 1. The fuel gas directly discharges the flare. The tower top condensing mechanism 4 adopts a first mode, the gas phase material at the tower top is condensed by a condenser 404, and the condenser 404 adopts 7 ℃ chilled water as a cold source. The bottom reboiler 10 employs hot water at 90 c as a heat source.
The separation method comprises the following steps:
the material from the upstream device enters the depropanizer 1 through a side line inlet pipeline 2; the gas phase material from the top of the depropanizer 1 is cooled by a tower top condenser 404 to form condensate, the condensate enters a tower top reflux tank 5, after being pressurized by a pump, one part of condensate is used as reflux liquid and returns to the top of the depropanizer 1 through a tower top liquid phase reflux pipeline 7, and the other part of tower top liquid phase is sent to a downstream deethanizer (or propylene rectifying tower) from a tower top liquid phase sending pipeline 8 for continuous separation. The non-condensing steam in the tower top reflux tank 5 is discharged by a fuel gas discharge pipeline 6; part of liquid phase materials at the bottom of the depropanizer 1 enter a tower bottom reboiler 10 to be heated and then return to the bottom of the depropanizer 1, and the other part is pressurized by a pump and then sent to a downstream device for continuous separation through a tower bottom liquid phase sending pipeline 9.
Example 2:
in this example, the depropanizer 1 had 30 theoretical plates, the overhead operating pressure of 0.6MPag, the overhead temperature of 6.5℃and the bottom temperature of 63.3 ℃. The side inlet line 2 is located at a position above the deck 10 of the depropanizer 1. The second mode is adopted by the tower top condensation mechanism 4, and the tower top gas phase material is pressurized to 1.7MPag through the first tower top gas booster 405 and then enters the cooler 406, and the cooler 406 is cooled by adopting an air cooler. The bottom reboiler 10 uses 85 ℃ hot water as a heat source.
The separation method comprises the following steps:
the material from the upstream device enters the depropanizer 1 through a side line inlet pipeline 2; the gas phase material from the top of the depropanizer 1 is pressurized by a first tower top gas booster 405, enters a cooler 406, is cooled by an air cooler, and forms condensate after cooling, and enters a tower top reflux tank 5. After the condensate is pressurized by a pump, one part of the condensate is used as reflux liquid to be returned to the top of the depropanizer 1 through a tower top liquid phase reflux pipeline 7, and the other part of the tower top liquid phase is sent to a downstream deethanizer (or propylene rectifying tower) from a tower top liquid phase sending pipeline 8 to be continuously separated. The non-condensing steam in the tower top reflux tank 5 is discharged by a fuel gas discharge pipeline 6; part of liquid phase materials at the bottom of the depropanizer 1 enter a tower bottom reboiler 10 to be heated and then return to the bottom of the depropanizer 1, and the other part is pressurized by a pump and then sent to a downstream device for continuous separation through a tower bottom liquid phase sending pipeline 9.
Example 3:
in this example, the depropanizer 1 had 30 theoretical plates, a column top operating pressure of 0.65MPag, a column top temperature of 8.8℃and a column bottom temperature of 65.2 ℃. The side inlet line 2 is located at the level of the tray 10. The tower top condensing mechanism 4 adopts a mode III, the tower top gas phase is pressurized to 2.85MPag through the second tower top gas booster 407, enters the tower bottom reboiler 10, exchanges heat with the tower bottom material, is condensed through the tower top gas post-cooler 408, and completely forms condensate to enter the tower top reflux tank 5. The bottom reboiler 10 does not require an external heat source.
The separation method comprises the following steps:
the material from the upstream device enters the depropanizer 1 through a side line inlet pipeline 2; the gas phase material coming out from the top of the depropanizer 1 is pressurized by a second tower top gas booster 407, enters a tower bottom reboiler 10, exchanges heat with the tower bottom material, is condensed by a tower top gas aftercooler 408, and completely forms condensate to enter a tower top reflux tank 5. After the condensate is pressurized by a pump, one part of the condensate is used as reflux liquid to be returned to the top of the depropanizer 1 through a tower top liquid phase reflux pipeline 7, and the other part of the condensate is sent to a downstream deethanizer (or propylene rectifying tower) from a tower top liquid phase sending pipeline 8 to be continuously separated. The non-condensing steam in the tower top reflux tank 5 is discharged by a fuel gas discharge pipeline 6; part of liquid phase materials at the bottom of the depropanizer 1 enter a tower bottom reboiler 10 to be heated and then return to the bottom of the depropanizer 1, and the other part is pressurized by a pump and then sent to a downstream device for continuous separation through a tower bottom liquid phase sending pipeline 9.
According to the separation device and the separation method, the separation effect of C3 and C4 in the catalytic liquid hydrocarbon is not affected, and the low-pressure depropanization is adopted, so that the operating temperature at the bottom of the depropanization tower is reduced, the problem of polymerization coking blockage at the bottom of the depropanization 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 depropanizer saves about 22t/h of 0.5MPa steam, and achieves essential energy conservation and synergy.
While 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 may be made without departing from the spirit of the present patent within the knowledge of those skilled in the art.
Claims (5)
1. The separation device for preventing the bottom coking of the catalytic depropanizer comprises a depropanizer (1) and is characterized in that an inlet pipeline (2) is arranged in the middle of the depropanizer (1), a tower top gas phase delivery pipeline (3) is arranged at the top of the depropanizer (1), and a tower top condensing mechanism (4) and a tower top reflux tank (5) are sequentially arranged on the tower top gas phase delivery pipeline (3) along the gas phase flowing direction;
the top of the tower top reflux tank (5) is provided with a fuel gas discharge pipeline (6), the bottom of the tower top reflux tank (5) is respectively provided with a tower top liquid phase reflux pipeline (7) and a tower top liquid phase delivery pipeline (8), and the outlet of the tower top liquid phase reflux pipeline (7) is connected with the top of the depropanizer (1) in a conducting way;
a bottom liquid phase delivery pipeline (9) is arranged at the bottom of the depropanizer (1), a bottom reboiler (10) is arranged on the bottom liquid phase delivery pipeline (9), and an outlet of the bottom reboiler (10) is connected with the depropanizer (1) in a conducting way;
15-80 layers of theoretical plates of the depropanizer (1), the operating pressure at the top of the tower is 0.5-1.2MPag, the temperature at the top of the tower is 0-30 ℃, and the temperature at the bottom of the tower is 60-95 ℃.
2. A separation device for preventing bottom coking of catalytic depropanizer according to claim 1, characterized in that the overhead condensing means (4) comprises a first branch (401), a second branch (402) and a third branch (403) in conductive connection with the overhead gas phase outgoing line (3), respectively;
a condenser (404) is arranged on the first branch (401), and an outlet of the condenser (404) is connected with the tower top reflux tank (5);
a first tower top gas booster (405) and a cooler (406) are sequentially arranged on the second branch (402) along the gas phase flowing direction, and an outlet of the cooler (406) is connected with the tower top reflux tank (5);
a second tower top gas booster (407) and a tower top gas aftercooler (408) are sequentially arranged on the third branch (403) along the gas phase flowing direction, and an outlet of the second tower top gas booster (407) is connected with a tower bottom reboiler (10); the outlet of the tower bottom reboiler (10) is connected with a tower top gas aftercooler (408), and the outlet of the tower top gas aftercooler (408) is connected with a tower top reflux tank (5); the second tower top gas booster (407), the tower bottom reboiler (10) and the tower top gas aftercooler (408) are matched to form a heat pump system.
3. A separation device for preventing bottom coking of catalytic depropanizer according to claim 1, characterized in that the bottom reboiler (10) uses 80-95 ℃ hot water, low temperature process material waste heat or low pressure steam as heat source.
4. The separation method for preventing the bottom of the catalytic depropanizer from coking is characterized by comprising the following steps:
s1, introducing catalytic liquefied gas materials from an upstream device into a depropanizer (1) through an inlet pipeline (2);
s2, cooling a gas phase material coming out of the top of the depropanizer (1) through a tower top condensing mechanism (4) to form condensate, and then enabling the condensate to enter a tower top reflux tank (5); the condensate in the tower top reflux tank (5) is divided into two parts after being pressurized by a pump, one part of condensate is returned to the top of the depropanizer (1) as reflux through a tower top liquid phase reflux pipeline (7), and the other part of condensate is sent to a downstream device from a tower top liquid phase delivery pipeline (8) for continuous separation; the non-condensing steam in the tower top reflux tank (5) is discharged by a fuel gas discharge pipeline (6);
s3, a part of liquid phase materials at the bottom of the depropanizer (1) enter a tower bottom reboiler (10) to be heated and then return to the bottom of the depropanizer (1), and the other part of the liquid phase materials are pressurized by a pump and then sent to a downstream device for continuous separation through a tower bottom liquid phase delivery pipeline (9);
15-80 layers of theoretical plates of the depropanizer (1), the operating pressure at the top of the tower is 0.5-1.2MPag, the temperature at the top of the tower is 0-30 ℃, and the temperature at the bottom of the tower is 60-95 ℃.
5. The separation method for preventing bottom coking of catalytic depropanizer according to claim 4, wherein in step S2, after the gaseous material in the top of the depropanizer (1) enters the top condensing mechanism (4), there are three condensing modes:
in the first mode, the gas phase material at the top of the depropanizer (1) enters a first branch (401) and is cooled by a condenser (404) to form condensate;
in the second mode, the gas phase material at the top of the depropanizer (1) enters a second branch (402), is pressurized by a first tower top gas booster (405) and then enters a cooler (406) to be cooled to form condensate;
in the third mode, the gas phase material at the top of the depropanizer (1) enters a third branch (403), is pressurized by a second tower top gas booster (407), and then is cooled by a tower bottom reboiler (10) and a tower top gas aftercooler (408) in sequence to form condensate.
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| CN106495980A (en) * | 2016-09-29 | 2017-03-15 | 大连理工大学 | Gas separation unit and method based on forward and backward depropanization double-column process |
| WO2019071869A1 (en) * | 2017-10-12 | 2019-04-18 | 中国石油工程建设有限公司 | Device and method using stepped cooling to recover ethane from natural gas |
| WO2021050627A1 (en) * | 2019-09-10 | 2021-03-18 | Kellogg Brown & Root Llc | Process for recovery of propylene from propane dehydrogenation process |
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