CN210831944U - Solvent regeneration waste heat recycling system - Google Patents
Solvent regeneration waste heat recycling system Download PDFInfo
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- CN210831944U CN210831944U CN202020842728.XU CN202020842728U CN210831944U CN 210831944 U CN210831944 U CN 210831944U CN 202020842728 U CN202020842728 U CN 202020842728U CN 210831944 U CN210831944 U CN 210831944U
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Abstract
The utility model discloses a solvent regeneration waste heat recycling system, which comprises a solvent regeneration tower, a low-pressure rich liquid flash tank, a first lean and rich solvent heat exchanger, a second lean and rich solvent heat exchanger, a solvent buffer tank, an acid gas liquid separating tank, a tower bottom reboiler and a steam generator; the inlet end of the solvent regeneration tower is connected with the first lean-rich solvent heat exchanger through a second lean-rich solvent heat exchanger, a low-pressure rich solution flash tank and the first lean-rich solvent heat exchanger in sequence; the tower bottom outlet end of the solvent regeneration tower is connected with a solvent buffer tank through a second lean and rich solvent heat exchanger and a first lean and rich solvent heat exchanger in sequence; the tower top outlet and the tower bottom outlet of the solvent regeneration tower are respectively connected with the acid gas liquid separation tank and the solvent regeneration tower; the medium inlet of the tower bottom reboiler is connected with a steam temperature and pressure reducer, the outlet of the tower bottom reboiler is connected with a steam generator, and the steam outlet of the steam generator is connected with the steam inlet of the steam temperature and pressure reducer. The utility model discloses rational in infrastructure, can practice thrift the deoxidization water, can reduce the energy consumption with heat reuse simultaneously.
Description
Technical Field
The utility model relates to a petrochemical technical field, concretely relates to solvent regeneration waste heat recovery utilizes system.
Background
Solvent regeneration is one of the technological processes for recovering and using sulfur in petroleum refining, and utilizes alcohol amine to remove H by means of chemical absorption2S (acid gas) and then containing H by stripping2And regenerating the rich solution of S. In the process of solvent regeneration, a large amount of heat is generated, and after the heat is cooled by an air cooler and the like, on one hand, the part of heat is lost, and on the other hand, the energy consumption of a heating furnace, the air cooler and the like is large, so that the energy consumption is increased, and a large amount of heat is discarded, so that the cost is increased; in addition, the water injection of the temperature and pressure reducer of the reboiler at the bottom of the solvent regeneration tower generally adopts deoxygenated water, so that a large amount of deoxygenated water is needed, and the energy consumption is increased.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a defect to prior art existence, provide a rational in infrastructure, can practice thrift the oxygen-removed water, can reduce the solvent regeneration waste heat recovery system of energy consumption with heat reuse simultaneously.
The technical scheme of the utility model as follows:
the solvent regeneration waste heat recycling system comprises a solvent regeneration tower, a low-pressure rich solution flash tank, a first lean and rich solvent heat exchanger, a second lean and rich solvent heat exchanger, a solvent buffer tank, an acid gas liquid separation tank, a tower bottom reboiler and a steam generator; the inlet end of the solvent regeneration tower is connected with the first lean and rich solvent heat exchanger through a second lean and rich solvent heat exchanger, a low-pressure rich solution flash tank and the first lean and rich solvent heat exchanger in sequence, and the first lean and rich solvent heat exchanger and the second lean and rich solvent heat exchanger are respectively arranged on an inlet pipeline and an outlet pipeline of the low-pressure rich solution flash tank; the outlet end of the tower bottom of the solvent regeneration tower is connected with the inlet of a solvent buffer tank through a second lean and rich solvent heat exchanger and a first lean and rich solvent heat exchanger in sequence by pipelines through a tower bottom pump, and the outlet of the solvent buffer tank is connected with a lean solution hydrogenation pipeline through a solvent pump;
the outlet of the tower top of the solvent regeneration tower is connected with an acid gas liquid separation tank through a pipeline, the gas phase outlet of the acid gas liquid separation tank is connected with a sulfur recovery device through a pipeline, and the liquid phase outlet of the acid gas liquid separation tank is connected with the solvent regeneration tower through a reflux pump;
the tower bottom reboiler is arranged at the lower part of the solvent regeneration tower, a medium inlet of the tower bottom reboiler is connected with a steam temperature and pressure reducer, a medium outlet of the tower bottom reboiler is connected with a steam generator through a condensation water tank, and a steam outlet of the steam generator is connected with a steam inlet of the steam temperature and pressure reducer.
And a barren liquor filtering device is arranged at the inlet end of the first barren rich solvent heat exchanger.
The inlet of the steam temperature and pressure reducer is also connected with a deoxygenation water pipeline.
And a condensate pump is arranged on a pipeline between the condensate tank and the steam generator.
And an air cooler and a water cooler are sequentially arranged on a pipeline between the first lean-rich solvent heat exchanger and the solvent buffer tank.
Compared with the prior art, the utility model has the advantages of it is following: it is rational in infrastructure, utilize the heat exchanger, can realize waste heat and recycle to reduce cost, in addition, through combining together steam generator and reboiler at the bottom of the tower, the comdenstion water that can produce reboiler at the bottom of the tower is used for steam generator, thereby practices thrift the deoxidization water, reduces the energy consumption.
Drawings
Fig. 1 is a schematic structural view of the present invention;
in the figure: 1. the system comprises a solvent regeneration tower, 2, a low-pressure rich liquid flash tank, 3, a first lean and rich solvent heat exchanger, 4, a second lean and rich solvent heat exchanger, 5, a solvent buffer tank, 6, an acid gas liquid separation tank, 7, a tower bottom reboiler, 8, a steam generator, 9, a tower bottom pump, 10, a solvent pump, 11, a lean liquid hydrogenation pipeline, 12, a rich solvent pump, 13, an air cooler, 14, a water cooler, 15, a reflux pump, 16, a steam temperature and pressure reducer, 17, a deaerated water pipeline, 18, a condensate water tank, 19, a lean liquid filtering device, 20 and a condensate water pump.
Detailed Description
The present invention will be further explained with reference to the drawings and examples.
Referring to fig. 1, the solvent regeneration waste heat recycling system includes a solvent regeneration tower 1, a low-pressure rich solution flash tank 2, a first lean and rich solvent heat exchanger 3, a second lean and rich solvent heat exchanger 4, a solvent buffer tank 5, an acid gas liquid separation tank 6, a tower bottom reboiler 7, and a steam generator 8. Wherein, the inlet end of the solvent regeneration tower 1 is connected with the first lean rich solvent heat exchanger 3 through the second lean rich solvent heat exchanger 4, the low-pressure rich solution flash tank 2 in turn, and the first lean rich solvent heat exchanger 3 and the second lean rich solvent heat exchanger 4 are respectively arranged on the inlet and outlet pipelines of the low-pressure rich solution flash tank 2; the outlet end of the tower bottom of the solvent regeneration tower 1 is connected with the inlet of a solvent buffer tank 5 through a tower bottom pump 9 and a second lean and rich solvent heat exchanger 4 and a first lean and rich solvent heat exchanger 3 in sequence through pipelines, and the outlet of the solvent buffer tank 5 is connected with a lean solution hydrogenation pipeline 11 through a solvent pump 10; an air cooler 13 and a water cooler 14 are sequentially arranged on a pipeline between the first lean-rich solvent heat exchanger 3 and the solvent buffer tank 5. Thus, rich liquor from the hydrogenation part enters a low-pressure rich liquor flash tank 2 after heat exchange and temperature rise through a first lean rich solvent heat exchanger 3, flash hydrocarbon is discharged into a torch system after flash evaporation through the rich liquor flash tank 2, and the rich liquor enters a solvent regeneration tower 1 for regeneration after temperature rise through a rich solvent pump 12 and a second lean rich solvent heat exchanger 4; and the barren solution regenerated by the solvent regeneration tower 1 is subjected to heat release and temperature reduction through the second barren rich solvent heat exchanger 4 and the first barren rich solvent heat exchanger 3 in sequence, and is subjected to temperature reduction through the air cooler 13 and the water cooler 14, and then enters the solvent buffer tank 5 to exchange heat through the two heat exchangers respectively, so that waste heat is recovered, and meanwhile, the cooling consumption is reduced, so that the energy consumption is reduced, and the cost is reduced.
The outlet of the tower top of the solvent regeneration tower 1 is connected with the acid gas liquid separation tank 6 through a pipeline, so that the gas at the tower top of the solvent regeneration tower 1 is mixed with deoxygenated water before entering the acid gas liquid separation tank 6, is cooled and then enters the acid gas liquid separation tank 6, the gas phase outlet of the acid gas liquid separation tank 6 is connected with a sulfur recovery device through a pipeline, and the acid gas enters the sulfur recovery device for preparing sulfur; the liquid phase outlet of the acid gas liquid separation tank 6 is connected with the solvent regeneration tower 1 through a reflux pump 15, so that the liquid separated from the acid gas liquid separation tank 6 is sent to the top of the solvent regeneration tower 1 through the reflux pump 15 to realize reflux.
The tower bottom reboiler 7 is arranged at the lower part of the solvent regeneration tower 1, a medium inlet of the tower bottom reboiler 7 is connected with a steam temperature and pressure reducing device 16, a medium outlet of the tower bottom reboiler 7 is connected with the steam generator 8 through a condensation water tank 18, a steam outlet of the steam generator 8 is connected with a steam inlet of the steam temperature and pressure reducing device 16, and a condensation water pump 20 is arranged on a pipeline between the condensation water tank 18 and the steam generator 8. The comdenstion water that reboiler 7 produced at the bottom of the tower produced like this is through condensation water tank 18 buffer storage back, sends it into steam generator 8 production steam through condensate pump 20, reduces the use of oxygen-free water on the one hand like this, has practiced thrift the energy, and on the other hand can directly be used for steam pressure reducer 16 reuse through the steam that the water injection retrieval and utilization produced, has reduced the energy consumption.
The inlet end of the first lean-rich solvent heat exchanger 3 is provided with a lean solution filtering device 19, and the rich solution needs to be filtered by the lean solution filtering device 19 before entering the low-pressure rich solution flash tank 2.
The inlet of the steam temperature and pressure reducing device 16 is also connected with a deoxygenated water pipeline 17. The deoxygenated water enters the steam temperature and pressure reducer 16 through a deoxygenated water pipeline 17 to be mixed with steam for temperature reduction and pressure reduction.
After being filtered by a lean solution filtering device 19, rich solution from a hydrogenation part firstly exchanges heat and is heated by a first lean and rich solvent heat exchanger 3, then enters a low-pressure rich solution flash tank 2, flash hydrocarbon flashed by the rich solution flash tank 2 is discharged into a torch system through a torch pipeline, and the rich solution exchanges heat and is heated by a second lean and rich solvent heat exchanger 4 through a rich solvent pump 12 and then enters a solvent regeneration tower 1 for regeneration; after being regenerated by the solvent regeneration tower 1, the gas enters an acid gas liquid separation tank 6 through a gas phase outlet at the top of the tower after being respectively air-cooled and water-cooled, and after being separated by the acid gas liquid separation tank 6, the acid gas enters a sulfur recovery device for preparing sulfur; the liquid is sent into the top of the solvent regeneration tower 1 again through a reflux pump 15 to be refluxed; the barren liquor regenerated by the solvent regeneration tower 1 is subjected to heat release and cooling by the second barren and rich solvent heat exchanger 4 and the first barren and rich solvent heat exchanger 3 in sequence, and is cooled by the air cooler 13 and the water cooler 14 and then enters the solvent buffer tank 5, so that heat exchange is carried out through the two heat exchangers respectively, waste heat recovery is realized, and cooling consumption is reduced, so that energy consumption and cost are reduced. The lean solution entering the solvent buffer tank 5 is sent to a lean solution hydrogenation line 11 through a solvent pump 10 to the hydrogenation process.
A part of liquid circulates through the reboiler 7 at the bottom of the tower, and after the condensed water produced in the process is buffered and stored through the condensed water tank 18, the condensed water is sent into the steam generator 8 through the condensed water pump 20 to produce steam, so that the use of the deaerated water is reduced, the energy is saved, and on the other hand, the steam produced through water injection recycling can be directly used for recycling the steam temperature and pressure reducer 16, and the energy consumption is reduced.
The present invention is not limited to the above-described embodiments, and various changes can be made within the knowledge range of those skilled in the art without departing from the spirit of the present invention, and the changed contents still belong to the protection scope of the present invention.
Claims (5)
1. Solvent regeneration waste heat recovery utilizes system, its characterized in that: the system comprises a solvent regeneration tower, a low-pressure rich solution flash tank, a first lean and rich solvent heat exchanger, a second lean and rich solvent heat exchanger, a solvent buffer tank, an acid gas liquid separation tank, a tower bottom reboiler and a steam generator; the inlet end of the solvent regeneration tower is connected with the first lean and rich solvent heat exchanger through a second lean and rich solvent heat exchanger, a low-pressure rich solution flash tank and the first lean and rich solvent heat exchanger in sequence, and the first lean and rich solvent heat exchanger and the second lean and rich solvent heat exchanger are respectively arranged on an inlet pipeline and an outlet pipeline of the low-pressure rich solution flash tank; the outlet end of the tower bottom of the solvent regeneration tower is connected with the inlet of a solvent buffer tank through a second lean and rich solvent heat exchanger and a first lean and rich solvent heat exchanger in sequence by pipelines through a tower bottom pump, and the outlet of the solvent buffer tank is connected with a lean solution hydrogenation pipeline through a solvent pump;
the outlet of the tower top of the solvent regeneration tower is connected with an acid gas liquid separation tank through a pipeline, the gas phase outlet of the acid gas liquid separation tank is connected with a sulfur recovery device through a pipeline, and the liquid phase outlet of the acid gas liquid separation tank is connected with the solvent regeneration tower through a reflux pump;
the tower bottom reboiler is arranged at the lower part of the solvent regeneration tower, a medium inlet of the tower bottom reboiler is connected with a steam temperature and pressure reducer, a medium outlet of the tower bottom reboiler is connected with a steam generator through a condensation water tank, and a steam outlet of the steam generator is connected with a steam inlet of the steam temperature and pressure reducer.
2. The solvent regeneration waste heat recovery system according to claim 1, characterized in that: and a barren liquor filtering device is arranged at the inlet end of the first barren rich solvent heat exchanger.
3. The solvent regeneration waste heat recovery system according to claim 2, characterized in that: the inlet of the steam temperature and pressure reducer is also connected with a deoxygenation water pipeline.
4. The solvent regeneration waste heat recovery system according to claim 2, characterized in that: and a condensate pump is arranged on a pipeline between the condensate tank and the steam generator.
5. The solvent regeneration waste heat recovery system according to claim 2, characterized in that: and an air cooler and a water cooler are sequentially arranged on a pipeline between the first lean-rich solvent heat exchanger and the solvent buffer tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020842728.XU CN210831944U (en) | 2020-05-20 | 2020-05-20 | Solvent regeneration waste heat recycling system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020842728.XU CN210831944U (en) | 2020-05-20 | 2020-05-20 | Solvent regeneration waste heat recycling system |
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| CN210831944U true CN210831944U (en) | 2020-06-23 |
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| CN202020842728.XU Active CN210831944U (en) | 2020-05-20 | 2020-05-20 | Solvent regeneration waste heat recycling system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114432887A (en) * | 2021-12-29 | 2022-05-06 | 江苏新海石化有限公司 | Amine liquid regeneration circulation system |
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2020
- 2020-05-20 CN CN202020842728.XU patent/CN210831944U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114432887A (en) * | 2021-12-29 | 2022-05-06 | 江苏新海石化有限公司 | Amine liquid regeneration circulation system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Haixing Chemical Co.,Ltd. Dongying City Assignor: Shandong Dongfang Hualong Industrial and Trade Group Co.,Ltd. Contract record no.: X2021980014437 Denomination of utility model: Solvent regeneration waste heat recovery and utilization system Granted publication date: 20200623 License type: Common License Record date: 20211209 |
|
| EE01 | Entry into force of recordation of patent licensing contract |