CN217464095U - Low-pressure gas energy-saving consumption-reducing recycling device - Google Patents
Low-pressure gas energy-saving consumption-reducing recycling device Download PDFInfo
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Abstract
The utility model provides a low-pressure gas energy-saving consumption-reducing recycling device, which belongs to the technical field of petrochemical industry and structurally comprises a screw compressor and a desulfurizing tower; the process end section low-pressure gas pipeline is communicated with a low-pressure gas collecting pipe through a collecting pipe in a converging way; the low-pressure gas collecting pipe and a diesel oil pipe of the cooling diesel oil tank are communicated with the inlet of the screw compressor; a high-pressure gas pipeline at the top of the high-pressure gas liquid separation tank is communicated to the bottom of the desulfurization tower, and high-pressure gas ascends in the tower body of the desulfurization tower; introducing a methyldiethanolamine MDEA barren solution pipeline at the top of a tower body of the desulfurizing tower, and enabling the methyldiethanolamine MDEA barren solution to descend in the tower body of the desulfurizing tower; and a desulfurization high-pressure gas output pipeline at the top of the desulfurization tower is communicated with an amine liquid recoverer, and the top of the amine liquid recoverer is communicated with an amine-removing high-pressure gas pipeline to a high-pressure gas pipe network. On the basis of realizing the recycling of low-pressure gas to high-pressure gas, the recycling of the desulfurization solvent and the recycling of cooling diesel oil are simultaneously tested.
Description
Technical Field
The utility model belongs to the technical field of petrochemical technology and specifically relates to a low pressure gas energy saving and consumption reduction recycling apparatus.
Background
In recent years, with the strictness of environmental protection measures, the awareness of environmental protection on production is increasing, and oil refining enterprises face unprecedented challenges. The gas recovery technology is an important link for reducing gas emission, can help enterprises to meet the requirements of stricter environmental protection and energy conservation indexes, and the treatment of the vent gas generated by each production device of a refinery is a more serious problem. In the work of energy saving and consumption reduction, the treatment of the emptying gas becomes the most important link.
The method is used for recovering the vent gas of process units such as a continuous reforming integrated unit with high production capacity, a diesel oil upgrading unit, a gasoline hydrogenation and gasoline etherification unit, a PSA (pressure swing adsorption) unit, a hydrogen production unit, a sulfur recovery integrated unit and the like of a refining project. In the traditional design, the vented gas is guided into the gas holder, and the hydrogen content is high, so that the technical requirement of a glue film under the gas holder cannot be met, and further improvement on the recycling of the vented gas is needed.
SUMMERY OF THE UTILITY MODEL
The technical task of the utility model is to solve the not enough of prior art, provide a low pressure gas energy saving and consumption reduction recycling device.
The technical scheme of the utility model is realized in the following way, the low-pressure gas energy-saving consumption-reducing recycling device of the utility model structurally comprises a screw compressor and a desulfurizing tower;
the process end section low-pressure gas pipeline is communicated with a low-pressure gas collecting pipe through a collecting pipe in a converging way;
the low-pressure gas collecting pipe and a diesel oil pipe of the cooling diesel oil tank are communicated with the inlet of the screw compressor together;
a high-pressure gas discharge pipe of the screw compressor is sequentially connected in series with a high-pressure gas aftercooler and a high-pressure gas liquid separation tank;
a high-pressure gas pipeline at the top of the high-pressure gas liquid separation tank is communicated to the bottom of the desulfurization tower, and high-pressure gas ascends in the tower body of the desulfurization tower;
introducing a methyldiethanolamine MDEA barren solution pipeline at the top of a tower body of the desulfurizing tower, and enabling the methyldiethanolamine MDEA barren solution to descend in the tower body of the desulfurizing tower;
enriching a methyldiethanolamine MDEA rich solution at the bottom of the desulfurizing tower, and discharging the methyldiethanolamine MDEA rich solution through a methyldiethanolamine MDEA rich solution pipeline;
and a desulfurization high-pressure gas output pipeline at the top of the desulfurization tower is communicated with an amine liquid recoverer, and the top of the amine liquid recoverer is communicated with an amine-removing high-pressure gas pipeline to a high-pressure gas pipe network.
The low-pressure gas collecting pipe is provided with a shunting branch which is sequentially communicated with the low-pressure gas shunting tank and the low-pressure gas water sealing tank, and the tail end of the shunting branch is communicated to the torch.
The screw compressor is provided with a compressor oil-gas cooler and a compressor oil-gas separator;
the compressor oil-gas separator is provided with a compressor liquid separation tank, and a cooling diesel oil return pipe at the bottom of the compressor liquid separation tank is connected to an inlet of the screw compressor in a backflow mode to form a cooling diesel oil circulation loop.
A methyldiethanolamine MDEA desulfurization system is arranged between the methyldiethanolamine MDEA rich liquid pipeline and the methyldiethanolamine MDEA poor liquid pipeline;
the downstream of the methyldiethanolamine MDEA rich solution pipeline is communicated with a rich solution filter and a lean-rich solution secondary heat exchanger in sequence and is communicated to a rich solution flash tank finally;
a flash evaporation outlet pipeline at the top of the rich liquid flash evaporation tank empties the flash evaporation hydrocarbon to a torch through a safety valve;
a rich liquid pipe at the bottom of the rich liquid flash tank is pressurized by a rich liquid pressurizing pump, and the downstream of the rich liquid pipe after heat exchange by the lean rich liquid first-stage heat exchanger is communicated to the top of the tower body of the solvent regeneration tower;
descending the methyldiethanolamine MDEA rich solution in the tower body of the solvent regeneration tower;
the bottom of the tower body of the solvent regeneration tower is connected with a reboiler, and the reboiler is communicated to the bottom of the tower body of the solvent regeneration tower in a reflux manner;
the tower top of the solvent regeneration tower is connected with an acid gas distillation pipeline, an overhead air cooler, an overhead aftercooler and an acid gas liquid separation tank are sequentially arranged on the acid gas distillation pipeline, the bottom of the acid gas liquid separation tank is communicated with an overhead return pipe, and the overhead return pipe is communicated to the tower top of the solvent regeneration tower through an overhead return pump in a backflow mode; the top of the acid gas liquid separation tank is communicated with an acid gas outlet pipe, and the acid gas outlet pipe is discharged to the outside for treatment; a deoxygenated water filling pipe is arranged on the acid gas liquid separation tank;
the tower bottom of the solvent regeneration tower is communicated with a tower bottom lean liquid pipe;
pumping a lean liquid pipe at the bottom of the tower by a lean liquid booster pump, exchanging heat with a methyldiethanolamine MDEA rich liquid by a lean-rich liquid primary heat exchanger, a lean-rich liquid secondary heat exchanger, then transferring to a lean liquid air cooler and a lean liquid aftercooler, and finally communicating to a solvent buffer tank;
a Methyl Diethanolamine (MDEA) solvent replenishing pipeline is arranged on the solvent buffer tank;
the solvent buffer tank is communicated with a methyldiethanolamine MDEA barren solution pipeline to the top of the desulfurizing tower.
A steam heat exchange and condensation device is arranged on the reboiler;
the steam heat exchange and condensation device is structurally characterized in that an external steam pipeline of an external steam pipeline network is communicated to a steam flow of a reboiler through a steam desuperheater, the steam flow is communicated with a condensation water tank after exiting the reboiler, and the condensation water tank is communicated with a condensation water pump and a condensation water cooler and then enters a condensation water outlet device to the outside.
The underground solvent tank is filled with the methyldiethanolamine MDEA solvent, a solvent submerged pump is configured in the underground solvent tank, and the solvent submerged pump is communicated with a methyldiethanolamine MDEA solvent supplement pipeline and finally reaches the solvent buffer tank.
Compared with the prior art, the utility model produced beneficial effect is:
the utility model discloses a low pressure gas energy saving and consumption reduction retrieves recycling device, with low pressure gas directly get into desulfurization system behind the compressor pressure boost and send into high-pressure gas pipe network after the desulfurization and use as the fuel gas. And recycling and reusing. The gas is recycled and enters a high-pressure gas pipe network for utilization, so that the consumption of gas and steam is reduced and the environment-friendly emission is realized.
The method realizes the reduction of various consumptions and saves energy. The recycling of the low-pressure gas effectively reduces the emission of the overhead torch, realizes the recycling, saves the cost, reduces the energy consumption, reduces the gas consumption, reduces the emission of the waste gas of the torch and has good experimental operation effect; can bring considerable economic benefits.
On the basis of realizing the recycling of low-pressure gas to high-pressure gas, the recycling of the desulfurization solvent and the recycling of cooling diesel oil are simultaneously tested.
The utility model discloses a low pressure gas energy saving and consumption reduction retrieves and recycles device reasonable in design, simple structure, safe and reliable, convenient to use, easy to maintain have fine using value widely.
Drawings
FIG. 1 is a schematic view of the overall structure layout of the present invention;
FIG. 2 is a schematic structural view of the low-pressure gas energy-saving consumption-reducing recycling device of the present invention;
FIG. 3 is a schematic structural diagram of a methyldiethanolamine MDEA desulfurization system of the utility model.
The reference numerals in the drawings denote:
1. a low-pressure gas energy-saving consumption-reducing recycling device,
2. a process end low-pressure gas pipeline 3, a collecting pipe 4, a low-pressure gas collecting pipe 5, a diesel oil pipe for cooling a diesel oil tank 6 and a screw compressor,
7. a high-pressure gas discharge pipe 8, a high-pressure gas aftercooler 9, a high-pressure gas liquid separation tank,
10. a high-pressure gas pipeline,
11. a desulfurizing tower,
12. a methyl diethanol amine MDEA barren liquor pipeline,
13. a methyl diethanol amine MDEA rich liquid pipeline,
14. a desulfurization high-pressure gas output pipeline 15, an amine liquid recoverer 16, a deaminization high-pressure gas pipeline 17, a high-pressure gas pipe network,
18. a branch, 19, a low-pressure gas liquid separating tank, 20, a low-pressure gas water-sealed tank, 21 and a torch,
22. a compressor oil-gas cooler 23, a compressor oil-gas separator 24, a compressor liquid separation tank,
25. the cooling of the diesel oil circulation loop is carried out,
26. a methyl diethanol amine MDEA desulfurization system,
27. a rich solution filter 28, a lean and rich solution secondary heat exchanger 29, a rich solution flash tank 30, a flash evaporation outlet pipeline,
31. a safety valve is arranged on the upper portion of the safety valve,
32. a rich liquor pipe at the bottom of the tank, 33, a rich liquor booster pump, 34, a lean and rich liquor first-stage heat exchanger,
35. a solvent regeneration tower is arranged at the bottom of the tower,
36. a reboiler is arranged at the bottom of the reaction kettle,
37. an acid gas distillation pipeline 38, an overhead air cooler 39, an overhead aftercooler 40, an acid gas liquid separation tank 41, an overhead return pipe 42, an overhead return pump 43, an acid gas outlet pipe 44, a deoxygenated water filling pipe,
45. a lean liquid pipe at the bottom of the tower,
46. a barren liquor pressure pump 47, a barren liquor air cooler 48, a barren liquor aftercooler,
49. a solvent buffer tank is arranged in the container,
50. a methyl diethanol amine MDEA solvent replenishing pipeline,
51. a steam heat exchange condensing device 52, an external steam pipe network 53, an external steam pipeline 54, a steam desuperheater 55, a steam flow path 56, a condensed water tank 57, a condensed water pump 58, a condensed water cooler 59 and a condensed water outlet device,
60. an underground solvent tank, 61, methyldiethanolamine MDEA solvent, 62 and a solvent submerged pump.
Detailed Description
The following detailed description will be made on the low-pressure gas energy-saving consumption-reducing recycling device of the present invention with reference to the accompanying drawings.
As shown in the attached drawings, the low-pressure gas energy-saving consumption-reducing recycling device 1 of the utility model structurally comprises a screw compressor and a desulfurizing tower;
the process end section low-pressure gas pipeline 2 is communicated with a low-pressure gas collecting pipe 4 through a collecting pipe 3 in a converging way;
the low-pressure gas collecting pipe 4 and a diesel oil pipe 5 for cooling the diesel oil tank are communicated with the inlet of a screw compressor 6;
a high-pressure gas discharge pipe 7 of the screw compressor 6 is sequentially connected in series with a high-pressure gas aftercooler 8 and a high-pressure gas liquid separation tank 9;
a high-pressure gas pipeline 10 at the top of the high-pressure gas liquid separation tank 9 is communicated to the bottom of the desulfurizing tower 11, and high-pressure gas ascends in the tower body of the desulfurizing tower 11;
introducing a methyldiethanolamine MDEA barren solution pipeline 12 into the top of the body of the desulfurizing tower 11, and allowing the methyldiethanolamine MDEA barren solution to descend in the body of the desulfurizing tower;
the tower bottom of the desulfurizing tower 11 is enriched with methyldiethanolamine MDEA rich liquid and discharged through a methyldiethanolamine MDEA rich liquid pipeline 13;
a desulfurization high-pressure gas output pipeline 14 at the top of the desulfurization tower 11 is communicated with an amine liquid recoverer 15, and the top of the amine liquid recoverer 15 is communicated with a deaminization high-pressure gas pipeline 16 to a high-pressure gas pipe network 17.
The low-pressure gas collecting pipe 4 is provided with a flow dividing branch 18, the downstream of the flow dividing branch 18 is sequentially communicated with a low-pressure gas flow dividing tank 19 and a low-pressure gas water-sealed tank 20, and the tail end of the flow dividing branch is communicated to a torch 21.
The screw compressor 6 is provided with a compressor oil-gas cooler 22 and a compressor oil-gas separator 23;
the compressor oil-gas separator 23 is provided with a compressor liquid separation tank 24, and a cooling diesel oil return pipe at the bottom of the compressor liquid separation tank 24 is connected to the inlet of the screw compressor in a backflow manner to form a cooling diesel oil circulation loop 25.
A methyldiethanolamine MDEA desulfurization system 26 is arranged between the methyldiethanolamine MDEA rich liquid pipeline 13 and the methyldiethanolamine MDEA poor liquid pipeline 12;
the downstream of the methyldiethanolamine MDEA rich solution pipeline 13 is communicated with a rich solution filter 27 and a lean-rich solution secondary heat exchanger 28 in sequence and is finally communicated to a rich solution flash tank 29;
a flash outlet line 30 at the top of the rich liquid flash tank 29 empties the flashed hydrocarbon to a torch 21 through a safety valve 31;
a tank bottom rich liquid pipe 32 of the rich liquid flash tank 29 is pressurized by a rich liquid pressurizing pump 33, and then is communicated to the top of the tower body of the solvent regeneration tower 35 through the downstream of the lean rich liquid first-stage heat exchanger 34 after heat exchange;
allowing the methyldiethanolamine MDEA rich solution to descend in a tower body of a solvent regeneration tower 35;
the bottom of the tower body of the solvent regeneration tower 35 is connected with a reboiler 36, and the reboiler 36 is communicated with the bottom of the tower body of the solvent regeneration tower 35 in a reflux manner;
the top of the solvent regeneration tower 35 is connected with an acid gas distillation pipeline 37, the acid gas distillation pipeline 37 is sequentially provided with a tower top air cooler 38, a tower top aftercooler 39 and an acid gas knockout drum 40, the bottom of the acid gas knockout drum 40 is communicated with a tower top return pipe 41, and the tower top return pipe 41 is communicated to the top of the solvent regeneration tower 35 through a tower top reflux pump 42 in a reflux manner; the top of the acid gas liquid separation tank 40 is communicated with an acid gas outlet pipe 43, and the acid gas outlet pipe 43 is discharged to the outside for treatment; a deoxygenated water filling pipe 44 is arranged on the acid gas liquid separation tank 40;
the tower bottom of the solvent regeneration tower 35 is communicated with a tower bottom lean liquid pipe 45;
a tower bottom lean liquid pipe 45 is pumped by a lean liquid pressurizing pump 46, exchanges heat with a methyldiethanolamine MDEA rich liquid through a lean-rich liquid primary heat exchanger 34 and a lean-rich liquid secondary heat exchanger 28, then is sent to a lean liquid air cooler 47 and a lean liquid aftercooler 48, and finally is communicated to a solvent buffer tank 49;
a methyl diethanolamine MDEA solvent replenishing pipeline 50 is arranged on the solvent buffer tank 49;
the solvent buffer tank 49 is communicated with a methyldiethanolamine MDEA barren solution pipeline 12 to the top of the desulfurizing tower 11.
Wherein:
the reboiler 36 is provided with a vapor heat exchange condenser 51;
the steam heat exchange and condensation device 51 is structurally characterized in that an external steam pipeline 53 of an external steam pipe network 52 is communicated to a steam flow 55 of a reboiler through a steam desuperheater 54, the steam flow 55 is communicated with a condensate tank 56 after exiting the reboiler, and the condensate tank 56 is communicated with a condensate pump 57 and a condensate water cooler 58 to a condensate water outlet device 59 to the outside.
The underground solvent tank 60 is filled with a methyldiethanolamine MDEA solvent 61, a solvent submerged pump 62 is arranged in the underground solvent tank, and the solvent submerged pump 62 is communicated with the methyldiethanolamine MDEA solvent replenishing pipeline 50 and finally reaches the solvent buffer tank 49.
The utility model discloses a low pressure gas energy saving and consumption reduction retrieves and recycles device adopts and is collected the low pressure gas of each way workshop section and get into high pressure gas pipe network after compressor pressure boost and desulfurization and retrieve and recycle, and reduce cost reduces the torch and discharges, reduces steam consumption, and is energy-concerving and environment-protective. The solvent liquid for desulfurization is provided with a solvent regeneration device, so that the solvent can be recycled and reused. The main process comprises the following three aspects:
1. gas flow:
the gas enters the screw compressor and is mixed with the sprayed cooling diesel at the inlet of the compressor. The compressed high-pressure gas with the temperature not higher than 80 ℃ and the carried cooling diesel oil enter an oil-gas cooler of the compressor unit for cooling. Then enters an oil-gas separator of a compressor unit, and realizes the separation of high-pressure gas and diesel oil therein. The diesel oil with the temperature of 40 ℃ at the lower part in the liquid separating tank of the compressor returns to the inlet of the screw compressor again by the pressure in the container for recycling. And the high-pressure gas at the upper part in the liquid separating tank of the compressor enters a fuel gas aftercooler and then enters the high-pressure gas liquid separating tank, so that the high-pressure gas is stably buffered, and diesel oil possibly carried in the gas is further removed. The high-pressure gas from the liquid separating tank enters the bottom of a desulfurizing tower and contacts with a Methyldiethanolamine (MDEA) barren solution entering from the upper part of the tower from bottom to top in the tower, and H in the high-pressure gas 2 S is absorbed. And (4) enabling the desulfurized high-pressure gas to come out from the top of the desulfurization tower and then enter an amine liquid recoverer to remove the methyldiethanolamine possibly carried in the gas. Qualified high-pressure gas is merged into a high-pressure gas pipeline of a whole plant system pipe network through the pressure regulating outlet device.
Condensed oil in the compressor area, condensed oil tanks at the inlet pipelines of the diesel station and the new compressor enters the condensed oil tanks, and when the condensed oil in the tanks is collected to a certain amount, the condensed oil is pressed to the flare liquid separating tank from the tanks by adopting condensed oil pumps or nitrogen of a factory system.
2. Cooling diesel oil flow:
when the screw compressor is started, the external diesel oil supply loop is started, firstly, diesel oil is injected into the inlet of the compressor by the diesel oil pump, and enters the compressor liquid separation tank together with gas after passing through the compressor and the gas-liquid cooler. The cooling diesel oil is continuously accumulated at the bottom of the compressor liquid separation tank, and meanwhile, the pressure in the compressor liquid separation tank is continuously increased to a designed pressure value. When the diesel oil liquid level in the compressor liquid separation tank reaches a certain level, a self circulation loop of the screw compressor unit for cooling the diesel oil is opened, namely the diesel oil is filtered from the bottom of the compressor liquid separation tank and injected into an inlet of the compressor, and then the diesel oil and gas pass through the compressor and a gas-liquid cooler together and enter the compressor liquid separation tank. At this point, a self-circulation of cooling diesel is established, and the external diesel supply circuit of the compressor can be closed.
When the performance index of the circulating diesel oil does not meet the requirement after long-term use, the circulating diesel oil in the liquid separation tank of the compressor can be gradually put into the gas holder condensation oil tank, and an external diesel oil supply loop is opened for supplement.
3. Methyldiethanolamine (MDEA) scheme:
the method comprises the steps of providing a Methyldiethanolamine (MDEA) barren solution by a desulfurization system of a gas holder device, enabling the Methyldiethanolamine (MDEA) barren solution to enter a barren solution secondary heat exchanger after the Methyldiethanolamine (MDEA) barren solution comes out from the bottom of a desulfurization tower, filtering impurities in the Methyldiethanolamine (MDEA) barren solution, enabling the Methyldiethanolamine (MDEA) barren solution to enter a barren solution flash tank after heat exchange of a barren solution secondary heat exchanger, enabling part of acid gas and other gases to be evaporated from the top of the flash tank, enabling the Methyldiethanolamine (MDEA) barren solution to pass through a barren solution primary heat exchanger after being pressurized by a barren solution pump and then enter the top of a regeneration tower, enabling the Methyldiethanolamine (MDEA) barren solution to flow downwards from the top of the regeneration tower, enabling the barren solution at the bottom of the regeneration tower to exchange heat with steam to enable the acid gas to overflow from the Methyldiethanolamine (MDEA) barren solution, enabling the produced by the Methyldiethanolamine (MDEA) barren solution to enter the bottom of the regeneration tower to reversely contact with the acid gas produced by the reboiler at the bottom of the regeneration tower, and the Methyl Diethanolamine (MDEA) barren solution at the tower bottom enters a barren and rich solution primary heat exchanger, is pressurized by a Methyl Diethanolamine (MDEA) barren solution pressure pump, enters a barren and rich solution secondary heat exchanger to exchange heat with the Methyl Diethanolamine (MDEA) barren solution, is cooled in air, enters a barren solution cooler and then enters a barren solution buffer tank. The Methyldiethanolamine (MDEA) barren solution at the top of the desulfurizing tower is pumped by a barren solution circulating tank, so that a cycle is established between the Methyldiethanolamine (MDEA) barren solution and the Methyldiethanolamine (MDEA) barren solution, the barren solution of the Methyldiethanolamine (MDEA) can be filtered by using a barren solution filtering facility when the Methyldiethanolamine (MDEA) barren solution contains more impurities, and fresh Methyldiethanolamine (MDEA) barren solution can be supplemented through an amine injection port if the liquid level of the barren solution buffering tank is lower.
Claims (6)
1. The low-pressure gas energy-saving consumption-reducing recycling device is characterized by comprising a screw compressor and a desulfurizing tower;
the process end section low-pressure gas pipeline is communicated with a low-pressure gas collecting pipe through a collecting pipe in a converging way;
the low-pressure gas collecting pipe and a diesel oil pipe of the cooling diesel oil tank are communicated with the inlet of the screw compressor together;
a high-pressure gas discharge pipe of the screw compressor is sequentially connected in series with a high-pressure gas aftercooler and a high-pressure gas liquid separation tank;
a high-pressure gas pipeline at the top of the high-pressure gas liquid separation tank is communicated to the bottom of the desulfurization tower, and high-pressure gas ascends in the tower body of the desulfurization tower;
introducing a methyldiethanolamine MDEA barren solution pipeline at the top of a tower body of the desulfurizing tower, and enabling the methyldiethanolamine MDEA barren solution to descend in the tower body of the desulfurizing tower;
enriching a methyldiethanolamine MDEA rich solution at the bottom of the desulfurizing tower, and discharging the methyldiethanolamine MDEA rich solution through a methyldiethanolamine MDEA rich solution pipeline;
and a desulfurization high-pressure gas output pipeline at the top of the desulfurization tower is communicated with an amine liquid recoverer, and the top of the amine liquid recoverer is communicated with a deamine high-pressure gas pipeline to a high-pressure gas pipe network.
2. The low-pressure gas energy-saving consumption-reducing recycling device as claimed in claim 1, characterized in that:
the low-pressure gas collecting pipe is provided with a shunting branch which is sequentially communicated with the low-pressure gas shunting tank and the low-pressure gas water sealing tank, and the tail end of the shunting branch is communicated to the torch.
3. The low-pressure gas energy-saving consumption-reducing recycling device as claimed in claim 1, wherein: the screw compressor is provided with a compressor oil-gas cooler and a compressor oil-gas separator;
the compressor oil-gas separator is provided with a compressor liquid separation tank, and a cooling diesel oil return pipe at the bottom of the compressor liquid separation tank is connected to an inlet of the screw compressor in a backflow mode to form a cooling diesel oil circulation loop.
4. The low-pressure gas energy-saving consumption-reducing recycling device as claimed in claim 1, wherein:
a methyldiethanolamine MDEA desulfurization system is arranged between the methyldiethanolamine MDEA rich liquid pipeline and the methyldiethanolamine MDEA poor liquid pipeline;
the downstream of the MDEA rich solution pipeline of the methyldiethanolamine is communicated with a rich solution filter and a lean-rich solution secondary heat exchanger in sequence and is finally communicated to a rich solution flash tank;
a flash evaporation outlet pipeline at the top of the rich liquid flash evaporation tank empties the flash evaporation hydrocarbon to a torch through a safety valve;
a rich liquid pipe at the bottom of the rich liquid flash tank is pressurized by a rich liquid pressurizing pump, and the downstream of the rich liquid pipe after heat exchange by the lean rich liquid first-stage heat exchanger is communicated to the top of the tower body of the solvent regeneration tower;
descending the methyldiethanolamine MDEA rich solution in the tower body of the solvent regeneration tower;
the bottom of the tower body of the solvent regeneration tower is connected with a reboiler, and the reboiler is communicated to the bottom of the tower body of the solvent regeneration tower in a reflux manner;
the top of the solvent regeneration tower is connected with an acid gas distillation pipeline, an overhead air cooler, an overhead aftercooler and an acid gas liquid separation tank are sequentially arranged on the acid gas distillation pipeline, the bottom of the acid gas liquid separation tank is communicated with an overhead return pipe, and the overhead return pipe is communicated to the top of the solvent regeneration tower through an overhead return pump in a backflow manner; the top of the acid gas liquid separation tank is communicated with an acid gas outlet pipe, and the acid gas outlet pipe is discharged to the outside for treatment; a deoxygenated water filling pipe is arranged on the acid gas separation tank;
the tower bottom of the solvent regeneration tower is communicated with a tower bottom lean liquid pipe;
pumping a lean liquid pipe at the bottom of the tower by a lean liquid booster pump, exchanging heat with a methyldiethanolamine MDEA rich liquid by a lean-rich liquid primary heat exchanger, a lean-rich liquid secondary heat exchanger, then transferring to a lean liquid air cooler and a lean liquid aftercooler, and finally communicating to a solvent buffer tank;
a methyl diethanolamine MDEA solvent replenishing pipeline is arranged on the solvent buffer tank;
the solvent buffer tank is communicated with a methyldiethanolamine MDEA barren solution pipeline to the top of the desulfurizing tower.
5. The low-pressure gas energy-saving consumption-reducing recycling device as claimed in claim 4, wherein:
a steam heat exchange and condensation device is arranged on the reboiler;
the steam heat exchange and condensation device is structurally characterized in that an external steam pipeline of an external steam pipeline network is communicated to a steam flow of a reboiler through a steam desuperheater, the steam flow is communicated with a condensation water tank after exiting the reboiler, and the condensation water tank is communicated with a condensation water pump and a condensation water cooler and then enters a condensation water outlet device to the outside.
6. The low-pressure gas energy-saving consumption-reducing recycling device as claimed in claim 4, wherein:
the underground solvent tank is filled with the methyldiethanolamine MDEA solvent, a solvent submerged pump is configured in the underground solvent tank, and the solvent submerged pump is communicated with a methyldiethanolamine MDEA solvent supplement pipeline and finally reaches the solvent buffer tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121024715.2U CN217464095U (en) | 2021-05-13 | 2021-05-13 | Low-pressure gas energy-saving consumption-reducing recycling device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121024715.2U CN217464095U (en) | 2021-05-13 | 2021-05-13 | Low-pressure gas energy-saving consumption-reducing recycling device |
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| Publication Number | Publication Date |
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| CN217464095U true CN217464095U (en) | 2022-09-20 |
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| CN202121024715.2U Active CN217464095U (en) | 2021-05-13 | 2021-05-13 | Low-pressure gas energy-saving consumption-reducing recycling device |
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2021
- 2021-05-13 CN CN202121024715.2U patent/CN217464095U/en active Active
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