CN212263278U - Liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system - Google Patents
Liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system Download PDFInfo
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- CN212263278U CN212263278U CN202021500944.2U CN202021500944U CN212263278U CN 212263278 U CN212263278 U CN 212263278U CN 202021500944 U CN202021500944 U CN 202021500944U CN 212263278 U CN212263278 U CN 212263278U
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Abstract
The utility model discloses a liquid phase hydrocarbon sulfur dioxide adsorbent regeneration system. The liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system comprises: the system comprises a sulfur dioxide adsorption tank, a regenerated gas heater, a regenerated gas heat exchanger, a first cooler and a regenerated gas compressor; the sulfur dioxide adsorption tank is used for containing an adsorbent of sulfur dioxide; the regenerated gas is heated by a regenerated gas heater and then enters a sulfur dioxide adsorption tank; the regenerated gas output from the sulfur dioxide adsorption tank is cooled by the first cooler after being subjected to heat exchange by the regenerated gas heat exchanger, then compressed by the regenerated gas compressor and enters the cold side of the regenerated gas heat exchanger to serve as a refrigerant, and the refrigerant enters the regenerated gas heater to be heated again after heat exchange. The utility model discloses to liquid phase hydrocarbons absorption desorption sulfur dioxide technology characteristics, provide a liquid phase hydrocarbons sulfur dioxide adsorbent regeneration system, its advantage mainly has: high-temperature nitrogen and air are used for regeneration, the operation is simple and practical, the operation is reliable, the control is simple and convenient, and the like.
Description
Technical Field
The utility model relates to a petrochemical technical field, concretely relates to liquid phase hydrocarbons sulfur dioxide adsorbent regeneration system.
Background
With the development of the petrochemical industry, liquid-phase hydrocarbons are increasingly regarded as a basic raw material and a chemical fuel. Meanwhile, with the development of economy in China, hydrocarbons have irreplaceable effects in the civil and industrial fields, and the demand is increasing. The hydrocarbons produced in the refinery still contain some sulfur dioxide, which not only poisons the catalyst, but also corrodes the equipment. The existing adsorption method technology can effectively remove sulfur dioxide in liquid-phase hydrocarbon. The adsorption method for removing sulfur dioxide has the greatest advantages of high desulfurization precision and easy regeneration of the adsorbent, and becomes the best choice for liquid-phase light hydrocarbon desulfurization.
However, the existing adsorbent regeneration technology can not realize the regeneration of the liquid-phase hydrocarbon sulfur dioxide adsorbent with high efficiency and reliability.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a liquid phase hydrocarbons sulfur dioxide adsorbent regeneration system to solve and adopt the adsorption process desorption sulfur dioxide regeneration problem in the system in the liquid phase hydrocarbons.
In order to realize the above purpose, the utility model adopts the following technical scheme:
the utility model discloses an aspect provides a liquid hydrocarbon sulfur dioxide adsorbent regeneration system, this regeneration system includes:
the system comprises a sulfur dioxide adsorption tank, a regenerated gas heater, a regenerated gas heat exchanger, a first cooler and a regenerated gas compressor;
the sulfur dioxide adsorption tank is used for containing an adsorbent adsorbed with sulfur dioxide; the outlet of the regenerated gas heater is connected with the inlet of the sulfur dioxide adsorption tank; the outlet of the sulfur dioxide adsorption tank is connected with the hot side inlet of the regenerated gas heat exchanger; the hot side outlet of the regeneration gas heat exchanger is connected with the inlet of the first cooler; the outlet of the first cooler is connected with the inlet of a regeneration gas compressor, the outlet of the regeneration gas compressor is connected with the cold side inlet of the regeneration gas heat exchanger, and the cold side outlet of the regeneration gas heat exchanger is connected with the inlet of the regeneration gas heater.
Based on the utility model discloses a regeneration system, each device that involves is the conventional equipment in this field.
Based on the utility model discloses a regeneration system, preferably, this regeneration system still includes the pans for depositing the liquid that comes from among the sulfur dioxide adsorption tanks.
Based on the regeneration system of the utility model, preferably, a dryer is connected in parallel on the connecting pipeline of the first cooler and the regeneration gas compressor; so as to dry the gas in the system if necessary and remove part of saturated water;
the outlet of the first cooler is respectively connected with the inlet of the regeneration gas compressor and the inlet of the dryer, and the outlet of the dryer is connected with the inlet of the regeneration gas compressor.
Based on the utility model discloses a regeneration system, preferably, still including first buffer tank on the connecting pipeline of the entry front end of regeneration gas compressor to stabilize compressor inlet pressure and isolate a small amount of liquid in the regeneration gas.
An outlet of the first cooler is respectively connected with an inlet of a first buffer tank and an inlet of a dryer, and an outlet of the dryer is connected with an inlet of the first buffer tank; the outlet of the first buffer tank is connected with the inlet of the regeneration gas compressor.
Based on the utility model discloses a regeneration system, preferably, the regeneration gas compressor with still including the second cooler on the connecting line of regeneration gas heat exchanger to the reduction causes the medium temperature to rise because of the compressor pressurization.
The outlet of the regenerated gas compressor is connected with the inlet of the second cooler, and the outlet of the second cooler is connected with the cold side inlet of the regenerated gas heat exchanger.
Based on the utility model discloses a regeneration system, preferably, the second cooler with still including the second buffer tank on the connecting line of regeneration gas heat exchanger to stabilize compressor outlet pressure and isolate a small amount of liquid in the regeneration gas.
The outlet of the second cooler is connected with the inlet of the second buffer tank, and the outlet of the second buffer tank is connected with the cold side inlet of the regeneration gas heat exchanger.
Based on the utility model discloses a regeneration system, preferably, the second buffer tank with including the lateral line on the connecting line of regeneration gas heat exchanger, the lateral line is connected to the caustic wash tower.
Based on the regeneration system of the utility model, preferably, the connection pipeline of the first cooler and the regeneration gas compressor comprises a regeneration gas inlet;
the regeneration gas inlet includes a nitrogen inlet and an air inlet.
The regeneration gas inlet may be placed after the dryer if the nitrogen and air have a small water content, and the moisture in the gas may be absorbed by the dryer if the nitrogen and air have a large water content.
The utility model discloses another aspect provides a method for regenerating liquid phase hydrocarbon sulfur dioxide adsorbent that liquid phase hydrocarbon sulfur dioxide adsorbent regeneration system goes on according to above, this regeneration method includes following step:
1) pouring out the liquid in the sulfur dioxide adsorption tank;
a nitrogen gas analysis step:
2) introducing nitrogen heated by the regenerated gas heater from the top of the sulfur dioxide adsorption tank and outputting from the bottom of the sulfur dioxide adsorption tank; to carry out most of the liquid hydrocarbons remaining on the sulfur dioxide adsorbent and part of the adsorbed sulfur dioxide;
3) nitrogen output from the bottom of the sulfur dioxide adsorption tank enters a first cooler for cooling to the required temperature after exchanging heat with a cold-side medium through a regenerated gas heat exchanger;
4) mixing the nitrogen cooled by the first cooler with fresh nitrogen, and then boosting the pressure by a regeneration gas compressor;
5) part of the nitrogen after pressure rise is led out of the liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system, and part of the nitrogen enters the cold side of the regenerated gas heat exchanger through the regenerated gas to serve as a cold side medium, exchanges heat with a hot side medium and then enters a regenerated gas heater;
6) and (5) repeating the steps 2) and 5) until the content of sulfur dioxide in the nitrogen output from the inlet at the bottom of the adsorption tank is less than 10 ppm.
An air scorching process:
7) changing nitrogen into air, and repeating the steps 2) to 5) until all coke generated by the sulfur dioxide adsorbent in the adsorption process is burnt by the air;
by detecting CO at the outlet of the sulfur dioxide adsorption tank2When the concentration of the coke is not substantially changed, the coke is completely burnt by the air.
A nitrogen cooling procedure:
8) and (4) closing the regeneration gas heater, changing the air into nitrogen again, and repeating the steps 2) -5) until the temperature of the sulfur dioxide adsorption tank meets the requirement.
Based on the utility model discloses a regeneration method, preferably, in step 1), pour the liquid in the sulfur dioxide adsorption tank, let in 0.6-1.0 MPaG's low pressure nitrogen gas in to the sulfur dioxide adsorption tank.
Based on the regeneration method of the utility model, preferably, when the nitrogen heated by the regeneration gas heater is introduced, part of the nitrogen after the pressure rise is led out of the liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system in the step 5) and is conveyed to the alkaline tower; when the air heated by the regeneration gas heater is introduced and the regeneration gas heater is closed to introduce nitrogen, part of the air or nitrogen after being pressurized in the step 5) is led out of the liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system and is directly discharged to the atmosphere.
Based on the utility model discloses a regeneration method, preferably, in the analytic operating mode of nitrogen gas, when letting in the nitrogen gas after the heating of regeneration gas heater, the temperature of nitrogen gas is 100-.
Based on the utility model discloses a regeneration method, preferably, in the air burnt operating mode, when letting in the air after regeneration gas heater heating, the temperature of air is 300-; at the end, the temperature reached 450-.
Based on the regeneration method of the utility model, preferably, the inlet pressure of the regeneration gas compressor is 0.1-0.4MPaG, and the outlet pressure is 0.2-0.6 MPaG; more preferably, the inlet pressure of the regeneration gas compressor is 0.2MPaG and the outlet pressure is 0.4 MPaG.
Based on the regeneration method of the utility model, preferably, the first cooler adopts circulating water cooling and cools to 30-60 ℃.
In accordance with the regeneration method of the present invention, it is preferable to remove part of the saturated water when the gas contains saturated water after the nitrogen and/or air is discharged from the first cooler before entering the regeneration gas compressor.
The carbon number in the liquid phase hydrocarbon molecule in the utility model is in the range of 1-60, preferably 3-12, and can be one or the combination of more than two of alkane, cyclane or arene, etc.
The utility model discloses to liquid phase hydrocarbons absorption desorption sulfur dioxide technology characteristics, provide a liquid phase hydrocarbons sulfur dioxide adsorbent regeneration system and method, its advantage mainly has: high-temperature nitrogen and air are used for regeneration, the operation is simple and practical, the operation is reliable, the control is simple and convenient, and the like.
Drawings
Fig. 1 is a schematic view of a liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system of the present invention.
Fig. 2 is a schematic view of a liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system according to a preferred embodiment of the present invention.
Description of reference numerals:
1-sulfur dioxide adsorption tank;
2-regeneration gas heat exchanger;
3-first cooler;
4-a first buffer tank;
5-regeneration gas compressor;
6-second cooler;
7-a second buffer tank;
8-regeneration gas heater;
9-dryer;
10-fresh nitrogen;
11-fresh air;
12-gas outlet.
Detailed Description
In order to illustrate the invention more clearly, the invention is further described below with reference to preferred embodiments. It is to be understood by persons skilled in the art that the following detailed description is illustrative and not restrictive, and is not to be taken as limiting the scope of the invention.
As shown in fig. 1, the liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system of the present invention comprises:
sulfur dioxide adsorption tank 1, regeneration gas heater 8, regeneration gas heat exchanger 2, first cooler 3 and regeneration gas compressor 5.
The sulfur dioxide adsorption tank 1 comprises an adsorbent adsorbing sulfur dioxide; the outlet of the regenerated gas heater 8 is connected with the inlet of the sulfur dioxide adsorption tank 1; the outlet of the sulfur dioxide adsorption tank 1 is connected with the hot side inlet of the regenerated gas heat exchanger 2; the hot side outlet of the regeneration gas heat exchanger 2 is connected with the inlet of the first cooler 3; the outlet of the first cooler 3 is connected with the inlet of a regeneration gas compressor 5, the outlet of the regeneration gas compressor 5 is connected with the cold side inlet of the regeneration gas heat exchanger 2, and the cold side outlet of the regeneration gas heat exchanger 2 is connected with the inlet of the regeneration gas heater 8.
When the regeneration system is used for regenerating the liquid-phase hydrocarbon sulfur dioxide adsorbent, the process is as follows:
a) closing an inlet valve and an outlet valve of the sulfur dioxide adsorption tank 1, and pouring out the liquid in the sulfur dioxide adsorption tank 1; meanwhile, low-pressure nitrogen of 0.6-1.0MPaG can be introduced into the sulfur dioxide adsorption tank to pour out the liquid in the adsorption tank as much as possible.
b) A nitrogen gas analysis step:
1) introducing nitrogen heated by the regeneration gas heater 8 from the top of the sulfur dioxide adsorption tank 1, and outputting from the bottom; to carry out most of the liquid hydrocarbons remaining on the sulfur dioxide adsorbent and part of the adsorbed sulfur dioxide;
2) nitrogen output from the bottom of the sulfur dioxide adsorption tank 1 enters a first cooler 3 to be cooled to 40-60 ℃ after heat exchange with a cold-side medium through a regenerated gas heat exchanger 2;
3) the nitrogen cooled by the first cooler 3 is mixed with fresh nitrogen 10 and then is subjected to pressure boosting by a regeneration gas compressor 5;
4) a part of the acid-containing waste gas of the nitrogen after the pressure rise is discharged to an alkaline tower at a gas outlet 12, and a part of the acid-containing waste gas enters the cold side of a regenerated gas heat exchanger 2 through regenerated gas to be used as a cold side medium, exchanges heat with a hot side medium and then enters a regenerated gas heater 8;
5) and (4) repeating the steps 1) and 4) until the content of sulfur dioxide in the nitrogen output from the bottom of the sulfur dioxide adsorption tank is less than 10 ppm. c) An air scorching process:
changing nitrogen into air to repeat steps 1) -4) in the nitrogen desorption procedure until all coke generated by the sulfur dioxide adsorbent in the adsorption process is burnt by the air; in the process, the air cooled by the first cooler 3 is mixed with the fresh air 11 and then is subjected to pressure boosting by the regeneration gas compressor 5; in the process, one part of the air after pressure boosting is directly discharged to the atmosphere at the gas outlet 12, and the other part of the air enters the cold side of the regenerated gas heat exchanger 2 to be used as a cold side medium.
d) A nitrogen cooling procedure:
and (4) closing the regeneration gas heater, changing the air into nitrogen again, and repeating the steps 2) -5) until the temperature of the sulfur dioxide adsorption tank meets the requirement. In the process, part of the nitrogen after pressure rise is directly discharged to the atmosphere at the gas outlet 12, and the other part of the nitrogen enters the cold side of the regenerated gas heat exchanger 2 to be used as a cold side medium.
The present invention provides a preferred embodiment, as shown in fig. 2, the liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system comprises: sulfur dioxide adsorption tank 1, regeneration gas heat exchanger 2, first cooler 3, first buffer tank 4, regeneration gas compressor 5, second cooler 6, second buffer tank 7, regeneration gas heater 8, desicator 9 and pans.
The sulfur dioxide adsorption tank 1 comprises an adsorbent adsorbing sulfur dioxide; the outlet of the regenerated gas heater 8 is connected with the inlet of the sulfur dioxide adsorption tank 1; the outlet of the sulfur dioxide adsorption tank 1 is connected with the hot side inlet of the regenerated gas heat exchanger 2; the hot side outlet of the regeneration gas heat exchanger 2 is connected with the inlet of the first cooler 3; the outlet of the first cooler 3 is connected with the inlet of the first buffer tank 4, the outlet of the first buffer tank 4 is connected with the inlet of the regeneration gas compressor 5, the outlet of the regeneration gas compressor 5 is connected with the inlet of the second cooler 6, the outlet of the second cooler 6 is connected with the inlet of the second buffer tank 7, the outlet of the second buffer tank 7 is connected with the cold side inlet of the regeneration gas heat exchanger 2, and the cold side outlet of the regeneration gas heat exchanger 2 is connected with the inlet of the regeneration gas heater 8.
A drier 9 is connected in parallel on a connecting pipeline between the first cooler 3 and the first buffer tank 4; so that the gas in the system is dried, if necessary, to remove part of the saturated water. The outlet of the first cooler 3 is connected with the inlet of the first buffer tank 4 and the inlet of the dryer 9, and the outlet of the dryer 9 is connected with the inlet of the first buffer tank 4. The dryer 9 can be based on the condensation principle or on the absorption principle, for example an adsorption dryer.
And a gas outlet 12 is also arranged on a connecting pipeline between the second buffer tank 7 and the regenerated gas heat exchanger 2.
When the regeneration system is used for regenerating the liquid-phase hydrocarbon sulfur dioxide adsorbent, the process is as follows:
(a) closing the inlet and outlet valves of the sulfur dioxide adsorption tank 1, pouring out the liquid in the tank, and simultaneously introducing low-pressure nitrogen of 0.6-1.0MPaG to transfer all liquid-phase hydrocarbons in the sulfur dioxide adsorption tank into an intermediate tank (not shown in the figure).
(b) A nitrogen gas analysis step:
nitrogen heated to 100-120 ℃ enters from the top of the sulfur dioxide adsorption tank 1, enters into the regeneration gas heat exchanger 2 after exiting from the bottom, exchanges heat with gas at an outlet at the top of the second buffer tank 7 to about 80-120 ℃, then enters into the first cooler 3 for water cooling to 30-60 ℃, when the gas contains saturated water, partial saturated water is removed through the dryer 9, the cooled nitrogen is mixed with fresh nitrogen 10 and then sequentially enters into the first buffer tank 4 and the regeneration gas compressor 5 for pressure boosting to 0.2-0.6MPaG, the nitrogen after pressure boosting enters into the second cooler 6 for cooling to 40-60 ℃ and then enters into the second buffer tank 7, wherein a part of acid-containing waste gas is discharged into the alkaline tower from the gas guide outlet 12, a part of the acid-containing waste gas is heated to 100-120 ℃ through the regeneration gas heater 8 and then enters into the sulfur dioxide adsorption tank for recycling, and meanwhile, slowly raising the temperature of the nitrogen to 300-400 ℃ until the content of the sulfur dioxide in the gas output from the bottom of the sulfur dioxide adsorption tank 1 is less than 10 ppm.
(c) Air-charring working condition:
air heated to the temperature of 300-, until the coke in the sulfur dioxide adsorption tank 1 is completely combusted (when the concentration of carbon dioxide in the gas output from the bottom of the sulfur dioxide adsorption tank 1 is basically not changed).
(d) Nitrogen cooling working condition:
and (2) closing the regeneration gas heater 8, allowing nitrogen to enter from the top of the sulfur dioxide adsorption tank 1, taking away heat in the sulfur dioxide adsorption tank 1, allowing the nitrogen to enter the regeneration gas heat exchanger 2 after coming out from the bottom, performing heat exchange with gas at an outlet at the top of the second buffer tank 7 to about 80-120 ℃, performing water cooling to 30-60 ℃ in the first cooler 3, removing partial saturated water through a dryer 9 if necessary, mixing the cooled nitrogen with fresh nitrogen 10, sequentially allowing the mixed nitrogen to enter the first buffer tank 4 and the regeneration gas compressor 5 to be boosted to 0.2-0.6MPaG, allowing the boosted nitrogen to enter the second cooler 6 to be cooled to 40-60 ℃, allowing the nitrogen to enter the second buffer tank 7, allowing the nitrogen to enter the sulfur dioxide adsorption tank 1, and performing recirculation until the temperature of the sulfur dioxide adsorption tank meets the requirement.
The utility model uses nitrogen and air to regenerate the sulfur dioxide adsorbent of liquid phase hydrocarbon, the operation pressure is 0.1-0.6MPaG, the operation temperature is 100-500 ℃, and the utility model has the advantages of simple and practical operation, reliable operation, simple and convenient control, etc.
Obviously, the above embodiments of the present invention are only examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention, and it is obvious for those skilled in the art to make other variations or changes based on the above descriptions, and all the embodiments cannot be exhausted here, and all the obvious variations or changes that belong to the technical solutions of the present invention are still in the protection scope of the present invention.
Claims (10)
1. A liquid phase hydrocarbon sulfur dioxide sorbent regeneration system, comprising:
the system comprises a sulfur dioxide adsorption tank, a regenerated gas heater, a regenerated gas heat exchanger, a first cooler and a regenerated gas compressor;
the sulfur dioxide adsorption tank is used for containing an adsorbent adsorbed with sulfur dioxide; the outlet of the regenerated gas heater is connected with the inlet of the sulfur dioxide adsorption tank; the outlet of the sulfur dioxide adsorption tank is connected with the hot side inlet of the regenerated gas heat exchanger; the hot side outlet of the regeneration gas heat exchanger is connected with the inlet of the first cooler; the outlet of the first cooler is connected with the inlet of a regeneration gas compressor, the outlet of the regeneration gas compressor is connected with the cold side inlet of the regeneration gas heat exchanger, and the cold side outlet of the regeneration gas heat exchanger is connected with the inlet of the regeneration gas heater.
2. The liquid phase hydrocarbon sulfur dioxide sorbent regeneration system of claim 1 further comprising an intermediate tank for holding liquid from the sulfur dioxide sorbent tank.
3. The liquid phase hydrocarbon sulfur dioxide adsorbent regeneration system as claimed in claim 1, wherein a dryer is connected in parallel to a connection line of the first cooler and the regeneration gas compressor;
the outlet of the first cooler is respectively connected with the inlet of the regeneration gas compressor and the inlet of the dryer, and the outlet of the dryer is connected with the inlet of the regeneration gas compressor.
4. The liquid phase sulfur dioxide adsorbent regeneration system as claimed in claim 3, wherein the connection piping of the inlet front end of the regeneration gas compressor further comprises a first buffer tank;
an outlet of the first cooler is respectively connected with an inlet of a first buffer tank and an inlet of a dryer, and an outlet of the dryer is connected with an inlet of the first buffer tank; the outlet of the first buffer tank is connected with the inlet of the regeneration gas compressor.
5. The liquid phase hydrocarbon sulfur dioxide adsorbent regeneration system as claimed in any one of claims 1 to 4, wherein a second cooler is further included in the connection line between said regeneration gas compressor and said regeneration gas heat exchanger,
the outlet of the regenerated gas compressor is connected with the inlet of the second cooler, and the outlet of the second cooler is connected with the cold side inlet of the regenerated gas heat exchanger.
6. The liquid phase hydrocarbon sulfur dioxide adsorbent regeneration system as claimed in claim 5, wherein a second buffer tank is further included in a connection line between said second cooler and said regeneration gas heat exchanger;
the outlet of the second cooler is connected with the inlet of the second buffer tank, and the outlet of the second buffer tank is connected with the cold side inlet of the regeneration gas heat exchanger.
7. The liquid phase hydrocarbon sulfur dioxide adsorbent regeneration system as claimed in claim 6, wherein a branch line is included in a connection line between said second buffer tank and said regeneration gas heat exchanger, and said branch line is connected to a caustic tower.
8. The liquid phase hydrocarbon sulfur dioxide sorbent regeneration system of any one of claims 1 to 4 wherein the regeneration gas inlet is included in the first cooler and regeneration gas compressor connection line;
the regeneration gas inlet includes a nitrogen inlet and an air inlet.
9. The liquid phase sulfur dioxide adsorbent regeneration system of claim 3, wherein said first cooler and regeneration gas compressor connection line includes a regeneration gas inlet;
the regeneration gas inlet is located before the dryer and comprises a nitrogen inlet and an air inlet.
10. The liquid phase hydrocarbon sulfur dioxide adsorbent regeneration system as claimed in claim 1, wherein a dryer is connected in parallel to a connection line of the first cooler and the regeneration gas compressor; the outlet of the first cooler is respectively connected with the inlet of a regeneration gas compressor and the inlet of a dryer, and the outlet of the dryer is connected with the inlet of the regeneration gas compressor;
the connecting pipeline at the front end of the inlet of the regeneration gas compressor also comprises a first buffer tank; an outlet of the first cooler is respectively connected with an inlet of a first buffer tank and an inlet of a dryer, and an outlet of the dryer is connected with an inlet of the first buffer tank; the outlet of the first buffer tank is connected with the inlet of the regeneration gas compressor;
the connecting pipeline of the regenerated gas compressor and the regenerated gas heat exchanger also comprises a second cooler, the outlet of the regenerated gas compressor is connected with the inlet of the second cooler, and the outlet of the second cooler is connected with the cold side inlet of the regenerated gas heat exchanger.
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| CN111774046A (en) * | 2020-07-27 | 2020-10-16 | 北京石油化工工程有限公司 | Liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system and method |
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| CN111774046A (en) * | 2020-07-27 | 2020-10-16 | 北京石油化工工程有限公司 | Liquid-phase hydrocarbon sulfur dioxide adsorbent regeneration system and method |
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