Decarburization system and method for reducing operation energy consumption of hydrogen-rich carbon circulating oxygen blast furnace

Abstract

The invention belongs to the technical field of steel smelting low-carbon ironmaking, and particularly discloses a decarburization system and method for reducing operation energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace. The decarburization system comprises a compressor, an absorption tower, a flash tank, a regeneration tower and a reboiler, the compressor is communicated with the absorption tower, the absorption tower is communicated with the flash tank, and the flash tank is communicated with the regeneration tower; the regeneration tower is communicated with the reboiler, the gas-liquid separator is communicated with an amine liquid heat exchanger, the amine liquid heat exchanger is communicated with the regeneration tower and the reboiler, regenerated gas is recycled in a regenerated gas recycling unit, flash steam is recycled in a gas pipeline, and high-pressure decarburized gas released from the absorption tower drives a transmission assembly; and the liquid spraying cooling water and the amine barren liquor flowing out of the compressor and the regeneration tower are subjected to heat absorption and heat exchange respectively. According to the system and the method, waste heat after compression of the compressor is recycled while decarburization treatment of the coal gas in the hydrogen-rich carbon cycle oxygen blast furnace is achieved, consumption of water energy, electric energy and steam is reduced, the operation cost is saved, and repeated utilization of resources is achieved.

Description

Technical Field

[0001] The present invention relates to the technical field of low-carbon ironmaking in steel smelting, and in particular to a decarbonization system and method for reducing operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace. Background Art

[0002] The hydrogen-rich carbon circulating oxygen blast furnace (HyCROF) is a smelting process that uses oxygen blast instead of traditional heated air blast. In order to compensate for the thermodynamic conditions required in the blast furnace caused by full oxygen blast, reduction of N2 and sharp reduction of furnace gas volume, it is necessary to remove CO2 from the top gas to form a reducing gas medium with a higher concentration of reducing components (CO and H2) and spray it into the blast furnace.

[0003] In the prior art, the decarbonization system, one of the important components of the hydrogen-rich carbon cycle oxygen blast furnace, is the main energy medium consumption of the hydrogen-rich carbon cycle oxygen blast furnace. The hydrogen-rich carbon cycle oxygen blast furnace gas contains 28%-32% of CO2 acidic gas. Removing CO2 from the gas can improve its gas reducibility and gas calorific value. The decarbonization system is mainly based on electricity consumption, which is mainly used to pressurize the blast furnace gas to provide the high-pressure environment required for the MDEA solution to absorb carbon dioxide. Therefore, in the decarbonization system, the compressor compression power consumption accounts for about 85% of the total power consumption. The power consumption of the compressor is mainly used for pressurizing the raw gas and the heat generated during the pressurization process. There is no reasonable way to utilize the waste heat of the compressor in the traditional MDEA decarbonization system. Most of them only use circulating cooling water to cool the waste heat generated by the compressor. The heat energy generated by the compressor is not fully utilized. While consuming cooling water, the waste heat energy of the compressor is also wasted. The flash gas from the flash tank is directly discharged because the hot spot is too low. At the same time, improper treatment of the amine liquid entrained in the regenerated coal gas and purified gas also causes the loss of amine liquid. The high-pressure decarbonized coal gas needs to be reduced by the pressure regulating valve group before it can be used by the subsequent user's blast furnace. The use of the pressure regulating valve group to directly reduce the pressure leads to energy waste. These factors lead to the problems of high operating costs, waste of resources, and high energy consumption during the operation of the decarbonization system. Summary of the invention

[0004] The purpose of the present invention is to provide a decarbonization system and method for reducing the operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace, so as to solve the problems of high operating costs, waste of resources and large energy consumption caused by factors such as improper treatment of amine liquid in the regenerated gas and direct discharge of flash steam during the operation of the decarbonization system.

[0005] To achieve the above-mentioned purpose, the basic scheme provided by the present invention is: a decarbonization system for reducing the operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace, comprising a gas pipeline, a main compressor, an absorption tower, a flash tank, a regeneration tower, a reboiler, a hydrogen-rich carbon circulating oxygen blast furnace and a regeneration gas recovery unit, the gas pipeline is connected to the main compressor, the compressor is connected to a gas-liquid separator, the gas outlet of the gas-liquid separator is connected to the absorption tower, the water outlet of the gas-liquid separator is connected to an amine-liquid heat exchanger, the absorption tower is connected to the flash tank, the absorption tower is connected to a decarbonized gas pipe, the decarbonized gas pipe is connected to a pipeline one, a gas expander is provided on the pipeline one, a transmission assembly is connected to the gas expander, the free end of the decarbonized gas pipe is connected to the decarbonized gas gas-liquid separator, the decarbonized gas gas-liquid separator is connected to the hydrogen-rich carbon circulating oxygen blast furnace, the bottom of the decarbonized gas gas-liquid separator is connected to a pipeline three, the free end of the pipeline three is connected to the absorption tower, a booster pump is provided on the pipeline three, and the water outlet of the flash tank The outlet is connected to the water inlet of the regeneration tower, the amine liquid heat exchanger is connected with an amine liquid inlet pipe and an amine liquid outlet pipe, the free end of the amine liquid inlet pipe is connected to the regeneration tower, the free end of the amine liquid outlet pipe is connected with an amine liquid outlet pipe 1 and an amine liquid outlet pipe 2, the amine liquid outlet pipe 1 is connected to the reboiler, the amine liquid outlet pipe 1 is provided with a reboiler control valve, the top of the reboiler is connected with a pipeline 2, the amine liquid outlet pipe 2 is connected with the pipeline 2, the amine liquid outlet pipe 2 is provided with a heat exchange bypass valve, the free end of the pipeline is connected to the regeneration tower, and the reboiler A steam inlet and a steam outlet are provided, a lean liquid pipe is connected to the bottom of the regeneration tower, a free end of the lean liquid pipe is connected to the absorption tower, a lean liquid pump is provided on the lean liquid pipe, a regeneration gas pipe is connected to the top of the regeneration tower, a free end of the regeneration gas pipe is connected to a regeneration gas cooler and a regeneration gas separation tank in sequence, a water outlet pipe is provided on the regeneration gas separation tank, a free end of the water outlet pipe is connected to the regeneration tower, a regeneration gas-liquid separation pump is provided on the water outlet pipe, and the gas outlet of the regeneration gas separation tank is connected to the regeneration gas recovery unit.

[0006] The working principle of the present invention is as follows: coal gas enters the compressor for compression, during which the compressor generates heat, and the spray cooling water in the spray cooler cools the compressor. The cooled cooling water enters the gas-liquid separator for gas-liquid separation, and the separated liquid phase enters the amine liquid heat exchanger for heat exchange. The gas phase enters the absorption tower to react with the amine liquid lean liquid to form decarbonized coal gas and amine liquid rich liquid, and the amine liquid rich liquid enters the flash tank and the regeneration tower for flash evaporation and regeneration. The regenerated amine liquid rich liquid enters the amine liquid heat exchanger and the reboiler for heating, and returns to the regeneration tower for regeneration after heating. The regenerated amine liquid lean liquid enters the absorption tower for recycling, the analytical gas in the regeneration tower enters the regeneration gas cooler and the regeneration gas separator for cooling and separation, the separated liquid phase returns to the regeneration tower for recycling, the gas phase is led to the regeneration gas recovery unit for recycling, and the CO2 released in the flash tank is led to the gas pipeline network for recycling.

[0007] The beneficial effects of the present invention are as follows: the decarbonization treatment of the raw gas released from the hydrogen-rich carbon circulating oxygen blast furnace is realized, the spray cooling water after the compressor is cooled enters the amine liquid heat exchanger to exchange heat with the regenerated amine liquid lean liquid, so that the spray cooling water is reused for a second time, and the spray cooling water after the heat exchange is circulated to the spray cooler again to cool the compressor. In this process, the spray cooling water is recycled, and after the analytical gas is separated by the regeneration gas separator, the liquid phase returns to the regeneration tower for regeneration, the regeneration gas enters the regeneration gas recovery unit, and the decarbonized coal gas enters the hydrogen-rich carbon circulating oxygen blast furnace, and the cooling water and steam are fully utilized, saving production resources.

[0008] Option 2, which is the preferred basic option, is that the top of the flash tank is connected to a flash steam pipe, the free end of the flash steam pipe is connected to a gas pipeline, and a flash steam pressure valve is provided on the flash steam pipe. The top of the flash tank is connected to the gas pipeline so that the flash steam to be discharged can directly enter the gas pipeline for recycling.

[0009] Scheme 3, which is the preferred basic scheme, is provided with a regeneration gas pressure valve on the regeneration gas pipe, and the pressure in the regeneration tower is adjusted by the regeneration gas pressure valve.

[0010] Option 4, which is the preferred option of the basic option, is a decarbonized gas pressure valve provided on the decarbonized gas pipe.

[0011] Option 5 is the preferred option of Option 5, and a thermocouple is provided on the amine liquid outlet pipe.

[0012] Scheme 6, a method for reducing the operating energy consumption of a hydrogen-rich carbon cycle oxygen blast furnace, the steps of reducing the operating energy consumption are as follows:

[0013] S1: Use the main compressor to pressurize the gas input from the gas pipeline from 0.15-0.2MPa to 1.2-2.0MPa;

[0014] S2: injecting liquid cooling water into the low-pressure end of the compressor through the liquid cooling device for heat exchange and cooling, reducing the temperature of the main compressor from 240℃ to 80-90℃, and the temperature of the liquid cooling water after heat exchange increases from 30-40℃ to 80-88℃;

[0015] S3: The compressed coal gas and the spray cooling water are separated by a gas-liquid separator, the separated coal gas enters the absorption tower, and the spray cooling water enters the amine liquid heat exchanger;

[0016] S4: The coal gas enters the absorption tower and contacts fully with the lean amine liquid to form rich amine liquid and decarbonized coal gas. The rich amine liquid enters the flash tank, and the decarbonized coal gas rises for recovery;

[0017] S5: Divide the decarbonized coal gas into two routes:

[0018] When the gas volume of the gas expander does not reach the maximum volume or the gas expander does not need to be shut down for maintenance, the decarbonized gas pressure valve is closed, and the decarbonized gas enters pipeline 1 first. The decarbonized gas is depressurized by the gas expander, and the pressure of the decarbonized gas is reduced from 1.2-2.0MPa to 0.3-0.5MPa. The decarbonized gas after decompression enters the decarbonized gas gas-liquid separator. At this time, the gas expander directly drives the transmission assembly;

[0019] When the gas volume of the gas expander reaches the maximum volume or the gas expander needs to be shut down for maintenance, the decarbonized gas pressure valve is opened to reduce the decarbonized gas pressure from 1.2-2.0MPa to 0.3-0.5MPa. The decarbonized gas enters the decarbonized gas gas-liquid separator through the decarbonized gas pipe for gas-liquid separation. The separated gas enters the hydrogen-rich carbon circulating oxygen blast furnace, and the liquid is pressurized by the booster pump and returned to the absorption tower;

[0020] S6: Use the flash steam pressure regulating valve to control the flash tank pressure at 0.15-0.35MPa, and the amine liquid rich liquid after flashing enters the regeneration tower;

[0021] S6: Use the flash steam pressure valve to control the flash tank pressure at 0.15-0.35MPa, and the amine liquid rich liquid after flashing enters the regeneration tower;

[0022] S7: Use the regeneration gas pressure valve to adjust the pressure in the regeneration tower to 0.02-0.05MPa. The amine rich liquid in the regeneration tower flows from the amine liquid inlet pipe to the amine liquid heat exchanger, and is heated by the spray cooling water. The spray cooling water that has completed the heat exchange is pressed from the high-pressure side of the main compressor into the low-pressure side to continue the heat exchange.

[0023] S8: The CO2 released in the regeneration tower is cooled and separated by the regeneration gas cooler and the regeneration gas separation tank. The separated gas enters the regeneration gas recovery unit, and the liquid returns to the regeneration tower for further regeneration;

[0024] S9: The lean liquid amine solution from which CO2 is removed in the regeneration tower is extracted through a lean liquid pump and led to the absorption tower for further use.

[0025] Scheme 7, which is a preferred embodiment of Scheme 6, the amine lean liquid heat exchange step in S7 comprises:

[0026] Measured by thermocouple:

[0027] If the temperature of the lean amine liquid reaches 65-85℃ after heat exchange with the spray cooling water, the heat exchange bypass valve is opened through the PLC control end, the reboiler control valve is closed, and the heated lean amine liquid enters the regeneration tower through the amine liquid pipe 2;

[0028] If the temperature of the lean amine liquid does not reach 65-85°C after heat exchange with the spray cooling water, the heat exchange bypass valve is closed through the PLC control end, and the reboiler control valve is opened. The lean amine liquid enters the reboiler for secondary heating. After the temperature of the lean amine liquid is heated to 65-85°C, it enters the regeneration tower.

[0029] The decarbonization treatment of the raw gas released from the hydrogen-rich carbon circulating oxygen blast furnace is realized, and the spray cooling water after the compressor is cooled enters the amine liquid heat exchanger for heat exchange with the regenerated amine liquid lean liquid, so that the spray cooling water is reused for the second time. The spray cooling water after heat exchange is circulated to the spray cooler again to cool the compressor. In this process, the spray cooling water is recycled, and the analyzed gas is separated by the regeneration gas separator, and the liquid phase returns to the regeneration tower for regeneration. The reboiler heat exchanger is used to exchange heat with the amine liquid rich liquid in the regeneration tower, thereby reducing the steam usage in the reboiler. After the decarbonized coal gas is purified by the purifier separation tank, it is decompressed and expanded by the gas expander. The gas expander directly drives the compressor to operate, which reduces the power consumption generated by the compressor during operation. The water energy consumption, steam consumption and electricity consumption are reduced in the whole process. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 It is a process flow chart of a decarbonization system and method for reducing operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace according to the present invention; DETAILED DESCRIPTION

[0031] The present invention is further described in detail below through specific embodiments:

[0032] The reference numerals in the drawings of the specification include: 1. gas pipeline, 2. main compressor, 3. absorption tower, 4. flash tank, 5. regeneration tower, 6. reboiler, 7. hydrogen-rich carbon circulating oxygen blast furnace, 8. regeneration gas recovery unit, 9. gas-liquid separator, 10. amine liquid heat exchanger, 11. decarbonized gas pipeline, 12. pipeline one, 13. gas expander, 14. amine liquid inlet pipe, 15. amine liquid outlet pipe, 16. amine liquid outlet pipe one, 17. amine liquid outlet pipe two, 18. reboiler control valve, 19. .Pipeline 2, 20. Heat exchange bypass valve, 21. Thermocouple, 22. Decarbonized gas pressure valve, 23. Lean liquid pipe, 24. Lean liquid pump, 25. Regeneration gas pipe, 26. Regeneration gas cooler, 27. Regeneration gas separation tank, 28. Decarbonized gas gas-liquid separator, 29. Transmission assembly, 30. Flash steam pipe, 31. Gas pipeline, 32. Flash steam pressure valve, 33. Regeneration gas pressure valve, 34. Water outlet pipe, 35. Regeneration gas-liquid separation pump, 36. Pipeline 3, 37. Booster pump.

[0033] Embodiment 1

[0034] The embodiment is basically as shown in the attached Figure 1As shown: a decarbonization system for reducing the operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace, comprising a gas pipeline 1, a main compressor 2, an absorption tower 3, a flash tank 4, a regeneration tower 5, a reboiler 6, a hydrogen-rich carbon circulating oxygen blast furnace 7 and a regeneration gas recovery unit 8, the gas pipeline 1 is connected to the main compressor 2, the compressor 2 is connected to a gas-liquid separator 9, the gas outlet of the gas-liquid separator 9 is connected to the absorption tower 3, the water outlet of the gas-liquid separator 9 is connected to an amine liquid heat exchanger 10, the absorption tower 3 is connected to the flash tank 4, the absorption tower 3 is connected to a decarbonization gas pipe 11, the decarbonization gas pipe 11 is connected to a pipeline 12, and the pipeline 12 is provided with a gas expansion The gas expander 13 is connected with a transmission assembly 29, which may be a secondary compressor or a water pump. The gas expander 13 directly drives the transmission assembly 29. The free end of the decarbonized coal gas pipe 11 is connected with a decarbonized coal gas-liquid separator 28, which is connected with the hydrogen-rich carbon circulating oxygen blast furnace 7. The bottom of the decarbonized coal gas-liquid separator 28 is connected with a pipeline 3 36, and the free end of the pipeline 3 36 is connected with the absorption tower 3. A booster pump 37 is provided on the pipeline 3 36. The water outlet of the flash tank 4 is connected with the water inlet of the regeneration tower 5. The amine liquid heat exchanger 10 is connected with an amine liquid inlet pipe 14 and an amine liquid outlet pipe 15. The free end of the amine liquid inlet pipe 14 is connected to the regeneration tower 5, the free end of the amine liquid outlet pipe 15 is connected to the amine liquid outlet pipe 16 and the amine liquid outlet pipe 2 17, the amine liquid outlet pipe 15 is provided with a thermocouple 21, the amine liquid outlet pipe 16 is connected to the reboiler 6, the amine liquid outlet pipe 16 is provided with a reboiler control valve 18, the top of the reboiler 6 is connected to the pipeline 2 19, the amine liquid outlet pipe 2 17 is connected to the pipeline 2 19, the amine liquid outlet pipe 2 17 is provided with a heat exchange bypass valve 20, the free end of the pipeline 2 19 is connected to the regeneration tower 5, the bottom of the regeneration tower 5 is connected to the lean liquid pipe 23, the free end of the lean liquid pipe 23 is connected to the absorption tower 3, the lean liquid pipe 23 is provided with a There is a lean liquid pump 24, the top of the regeneration tower 5 is connected to a regeneration gas pipe 25, the regeneration gas pipe 25 is provided with a regeneration gas pressure valve 33, the free end of the regeneration gas pipe 25 is connected to a regeneration gas cooler 26 and a regeneration gas separation tank 27 in sequence, the regeneration gas separation tank 27 is provided with a water outlet pipe 34, the free end of the water outlet pipe 34 is connected to the regeneration tower 5, the water outlet pipe 34 is provided with a regeneration gas-liquid separation pump 35, the gas outlet of the regeneration gas separation tank 27 is connected to the regeneration gas recovery unit 8, the top of the flash tank 4 is connected to a flash steam pipe 30, the free end of the flash steam pipe 30 is connected to a gas pipeline 31, and the flash steam pipe 30 is provided with a flash steam pressure valve 32.

[0035] The implementation method of this embodiment is as follows:

[0036] First, the coal gas is input into the compressor 2 through the gas pipeline 1 for pressurization, and the pressurized coal gas enters the absorption tower 3. During the compression process, liquid cooling water is sprayed to exchange heat and cool the compressor. The cooled cooling water and coal gas enter the gas-liquid separator 9 to separate the gas phase and the liquid phase. The liquid phase enters the amine liquid heat exchanger 10 to exchange heat with the amine liquid, and the gas phase enters the absorption tower 3. The decarbonized coal gas in the absorption tower 3 is preferentially driven by the gas expander 13 to directly drive the secondary compressor 29. The redundant decarbonized coal gas enters the hydrogen-rich carbon circulating oxygen blast furnace 7 through the decarbonized coal gas pipe 11 for recycling. Then, the rich amine liquid that has completed CO2 absorption in the absorption tower 3 enters the flash tank 4 for flash evaporation, and the flash steam from the flash evaporation enters the gas pipeline 31 for recycling. The amine liquid after flash evaporation enters the regeneration tower 5, and the rich amine liquid flows out from the lower part of the regeneration tower 5 through the amine liquid inlet pipe 14 and enters the amine liquid heat exchanger 10. Heat is exchanged with the spray cooling water to increase the temperature. If the spray cooling water increases the temperature of the amine rich liquid to 65-85°C, the heat exchange bypass valve 20 is opened, the reboiler control valve 18 is closed, and the amine rich liquid flows through the amine outlet pipe 2 to the pipeline 2 19 and directly enters the regeneration tower 5. If the temperature is less than 65-85°C, the heat exchange bypass valve 20 is closed, the reboiler control valve 18 is opened, and the amine rich liquid enters the reboiler 6 through the amine outlet pipe 1 for further temperature increase and then enters the regeneration tower 5 through the pipeline 2 19. The amine rich liquid after temperature increase enters the regeneration tower 5 and quickly releases CO2 gas, and is discharged from the top of the regeneration tower 5 to the regeneration gas cooler 26 and the regeneration gas separation tank 27 for cooling and separation, and finally input into the regeneration gas recovery unit 8 for recycling. The lean amine liquid after CO2 removal in the regeneration tower 5 flows out from the bottom of the regeneration tower 5, and is pressurized by the lean liquid pump 24 and then pumped into the absorption tower 3 for recycling.

[0037] Embodiment 2

[0038] The embodiment is basically as shown in the attached Figure 1 As shown:

[0039] A method for reducing the operating energy consumption of a hydrogen-rich carbon cycle oxygen blast furnace, wherein the steps of reducing the operating energy consumption are as follows:

[0040] S1: using the main compressor 2 to pressurize the gas input from the gas pipeline 1, and pressurizing the gas from 0.15-0.2MPa to 1.2-2.0MPa;

[0041] S2: inject liquid cooling water into the low-pressure end of compressor 2 for heat exchange and cooling, reducing the temperature of main compressor 2 from 240°C to 80-90°C, and the temperature of liquid cooling water after heat exchange increases from 30-40°C to 80-88°C;

[0042] S3: The compressed coal gas and the spray cooling water are separated by the gas-liquid separator 9, the separated coal gas enters the absorption tower 3, and the spray cooling water enters the amine liquid heat exchanger 10;

[0043] S4: The coal gas enters the absorption tower 3 and contacts fully with the lean amine liquid to form a rich amine liquid and decarbonized coal gas. The rich amine liquid enters the flash tank 4, and the decarbonized coal gas rises for recovery;

[0044] S5: Divide the decarbonized coal gas into two routes:

[0045] When the gas volume of the gas expander 13 does not reach the maximum volume or the gas expander 13 does not need to be shut down for maintenance, the decarbonized coal gas pressure valve 22 is closed, and the decarbonized coal gas enters the pipeline 12 first, and the decarbonized coal gas is depressurized by the gas expander 13, and the pressure of the decarbonized coal gas is reduced from 1.2-2.0MPa to 0.3-0.5MPa. The decarbonized coal gas after decompression enters the decarbonized coal gas-liquid separator 28, and the gas expander 13 directly drives the transmission component 29;

[0046] When the gas volume of the gas expander 13 reaches the maximum volume or the gas expander 13 needs to be shut down for maintenance, the decarbonized gas pressure valve 22 is opened, and the decarbonized gas pressure valve 22 is used to reduce the decarbonized gas pressure from 1.2-2.0 MPa to 0.3-0.5 MPa, and the decarbonized gas enters the decarbonized gas gas-liquid separator 28 through the decarbonized gas pipe 11 for gas-liquid separation, and the separated gas enters the hydrogen-rich carbon circulating oxygen blast furnace 7, and the liquid is pressurized by the booster pump 36 and returned to the absorption tower 3;

[0047] S6: Using the flash steam pressure regulating valve 32, the pressure of the flash tank 4 is controlled at 0.15-0.35 MPa, and the amine liquid rich liquid after flashing enters the regeneration tower 5;

[0048] S6: Using the flash steam pressure valve 32, the pressure of the flash tank 4 is controlled at 0.15-0.35 MPa, and the amine liquid rich liquid after flashing enters the regeneration tower 5;

[0049] S7: The pressure in the regeneration tower 5 is adjusted to 0.02-0.05 MPa by using the regeneration gas pressure valve 33. The amine liquid rich liquid in the regeneration tower 5 flows from the amine liquid inlet pipe 14 to the amine liquid heat exchanger 10, and is heated by the spray cooling water. The spray cooling water that has completed the heat exchange is pressed from the high-pressure side of the main compressor 2 into the low-pressure side to continue the heat exchange.

[0050] Measured by thermocouple 21:

[0051] If the temperature of the lean amine liquid reaches 65-85°C after heat exchange with the spray cooling water, the heat exchange bypass valve 20 is opened through the PLC control end, and the reboiler control valve 18 is closed, and the heated lean amine liquid enters the regeneration tower 5 through the amine liquid pipe 17;

[0052] If the temperature of the lean amine liquid does not reach 65-85°C after heat exchange with the spray cooling water, the heat exchange bypass valve 20 is closed through the PLC control end, and the reboiler control valve 18 is opened. The lean amine liquid enters the reboiler 6 for secondary heating. After the temperature of the lean amine liquid is heated to 65-85°C, it enters the regeneration tower 5.

[0053] S8: The CO2 released in the regeneration tower 5 is cooled and separated by the regeneration gas cooler 26 and the regeneration gas separation tank 27. The separated gas enters the regeneration gas recovery unit 8, and the liquid returns to the regeneration tower 5 for further regeneration;

[0054] S9: The lean liquid amine solution from which CO2 is removed in the regeneration tower 5 is extracted through the lean liquid pump 24 and introduced into the absorption tower 3 for further use.

[0055] The above is only an embodiment of the present invention, and the common knowledge such as the known specific structure and characteristics in the scheme is not described in detail here. It should be pointed out that for those skilled in the art, several deformations and improvements can be made without departing from the structure of the present invention, which should also be regarded as the protection scope of the present invention, and these will not affect the effect of the implementation of the present invention and the practicality of the patent. The scope of protection required by this application shall be based on the content of its claims, and the specific implementation methods and other records in the specification can be used to interpret the content of the claims.

Claims

1. A decarbonization system for reducing the operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace, characterized in that: The invention comprises a coal gas pipeline (1), a main compressor (2), an absorption tower (3), a flash tank (4), a regeneration tower (5), a reboiler (6), a hydrogen-rich carbon circulating oxygen blast furnace (7) and a regeneration gas recovery unit (8), wherein the coal gas pipeline (1) is connected to the main compressor (2), the compressor (2) is connected to a gas-liquid separator (9), the gas outlet of the gas-liquid separator (9) is connected to the absorption tower (3), the water outlet of the gas-liquid separator (9) is connected to an amine liquid heat exchanger (10), the absorption tower (3) is connected to the flash tank (4), the absorption tower (3) is connected to a decarbonized coal gas pipe (11), and the decarbonized coal gas pipe (11) is connected to a pipeline (11). 2) The pipeline 1 (12) is provided with a gas expander (13), and the gas expander (13) is connected to a transmission assembly (29). The free end of the decarbonized coal gas pipe (11) is connected to a decarbonized coal gas liquid separator (28), and the decarbonized coal gas liquid separator (28) is connected to a hydrogen-rich carbon circulating oxygen blast furnace (7). The bottom of the decarbonized coal gas liquid separator (28) is connected to a pipeline 3 (36), and the free end of the pipeline 3 (36) is connected to an absorption tower (3). A booster pump (37) is provided on the pipeline 3 (36). The water outlet of the flash tank (4) is connected to the water inlet of the regeneration tower (5). The amine liquid heat exchanger (10) is connected to An amine liquid inlet pipe (14) and an amine liquid outlet pipe (15) are connected, the free end of the amine liquid inlet pipe (14) is connected to the regeneration tower (5), the free end of the amine liquid outlet pipe (15) is connected to an amine liquid outlet pipe 1 (16) and an amine liquid outlet pipe 2 (17), the amine liquid outlet pipe 1 (16) is connected to the reboiler (6), the amine liquid outlet pipe 1 (16) is provided with a reboiler control valve (18), the top of the reboiler (6) is connected to a pipeline 2 (19), the amine liquid outlet pipe 2 (17) is connected to the pipeline 2 (19), the amine liquid outlet pipe 2 (17) is provided with a heat exchange bypass valve (20), the free end of the pipeline 2 (19) is connected to the regeneration tower (5), the reboiler The bottom of the regeneration tower (5) is connected to a lean liquid pipe (23), the free end of the lean liquid pipe (23) is connected to the absorption tower (3), and a lean liquid pump (24) is provided on the lean liquid pipe (23). The top of the regeneration tower (5) is connected to a regeneration gas pipe (25), the free end of the regeneration gas pipe (25) is connected to a regeneration gas cooler (26) and a regeneration gas separation tank (27) in sequence, and a water outlet pipe (34) is provided on the regeneration gas separation tank (27). The free end of the water outlet pipe (34) is connected to the regeneration tower (5), and a regeneration gas-liquid separation pump (35) is provided on the water outlet pipe (34). The regeneration gas separation tank (27) is connected to a regeneration gas recovery unit (8).

2. A decarbonization system for reducing operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace according to claim 1, characterized in that: The top of the flash tank (4) is connected to a flash steam pipe (30), the free end of the flash steam pipe (30) is connected to a gas pipeline (31), and a flash steam pressure valve (32) is provided on the flash steam pipe (30).

3. A decarbonization system for reducing operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace according to claim 1, characterized in that: The regeneration gas pipe (25) is provided with a regeneration gas pressure valve (33).

4. A decarbonization system for reducing operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace according to claim 1, characterized in that: The decarbonized coal gas pipe (11) is provided with a decarbonized coal gas pressure regulating valve (22).

5. A decarbonization system for reducing operating energy consumption of a hydrogen-rich carbon circulating oxygen blast furnace according to claim 1, characterized in that: The amine liquid outlet pipe (15) is provided with a thermocouple (21).

6. A method for reducing the operating energy consumption of a hydrogen-rich carbon cycle oxygen blast furnace, characterized in that: Steps to reduce operating energy consumption are as follows: S1: using the main compressor (2) to pressurize the gas input from the gas pipeline (1) from 0.15-0.2 MPa to 1.2-2.0 MPa; S2: injecting liquid cooling water into the low-pressure end of the compressor (2) for heat exchange and cooling, reducing the exhaust temperature of the main compressor (2) to 80-90° C., while increasing the temperature of the liquid cooling water from 30-40° C. to 80-88° C.; S3: The compressed coal gas and the spray cooling water are separated by a gas-liquid separator (9), the separated coal gas enters the absorption tower (3), and the spray cooling water enters the amine liquid heat exchanger (10); S4: The coal gas enters the absorption tower (3) and is fully contacted with the lean amine liquid to form a rich amine liquid and decarbonized coal gas. The rich amine liquid enters the flash tank (4), and the decarbonized coal gas is recovered by rising; S5: Divide the decarbonized coal gas into two routes: When the gas volume of the gas expander (13) has not reached the maximum volume or the gas expander (13) does not need to be shut down for maintenance, the decarbonized coal gas pressure valve (22) is closed, and the decarbonized coal gas preferentially enters the pipeline 1 (12). The decarbonized coal gas is depressurized by the gas expander (13), and the pressure of the decarbonized coal gas is reduced from 1.2-2.0 MPa to 0.3-0.5 MPa. The decarbonized coal gas after decompression enters the decarbonized coal gas-liquid separator (28). At this time, the gas expander (13) directly drives the transmission component (29); When the gas volume of the gas expander (13) reaches the maximum volume or the gas expander (13) needs to be shut down for maintenance, the decarbonized coal gas pressure valve (22) is opened to reduce the decarbonized coal gas pressure from 1.2-2.0 MPa to 0.3-0.5 MPa, and the decarbonized coal gas enters the decarbonized coal gas-liquid separator (28) through the decarbonized coal gas pipe (11) for gas-liquid separation, and the separated gas enters the hydrogen-rich carbon circulating oxygen blast furnace (7), and the liquid is pressurized by the booster pump (36) and returned to the absorption tower (3); S6: Using the flash steam pressure regulating valve (32), the pressure of the flash tank (4) is controlled at 0.15-0.35 MPa, and the amine liquid rich liquid after flashing enters the regeneration tower (5); S7: The pressure in the regeneration tower (5) is adjusted to 0.02-0.05 MPa by using the regeneration gas pressure regulating valve (33). The rich amine liquid in the regeneration tower (5) releases part of the carbon dioxide and flows from the amine liquid inlet pipe (14) to the amine liquid heat exchanger (10). The temperature is increased by the spray cooling water. The spray cooling water that has completed the heat exchange is pressed from the high-pressure side of the main compressor (2) into the low-pressure side to continue the heat exchange. S8: The CO2 released in the regeneration tower (5) is cooled and separated into gas and liquid by a regeneration gas cooler (26) and a regeneration gas separation tank (27); the separated gas enters a regeneration gas recovery unit (8) for recycling, and the liquid is pumped back into the regeneration tower (5) for recycling via a regeneration gas-liquid separation pump (35); S9: The lean liquid amine solution from which CO2 has been removed in the regeneration tower (5) is pumped out through the lean liquid pump (24) and introduced into the absorption tower (3) for further use.

7. A method for reducing operating energy consumption of a hydrogen-rich carbon cycle oxygen blast furnace according to claim 6, characterized in that: The amine lean liquid heat exchange step in S7 includes: According to the thermocouple (21), it is measured: When the temperature of the amine liquid reaches 65-85°C after heat exchange with the spray cooling water, the heat exchange bypass valve (20) is opened through the PLC control end, the reboiler control valve (18) is closed, and the heated amine liquid enters the regeneration tower (5) through the amine liquid pipe 2 (17); If the temperature of the amine liquid does not reach 65-85°C after the heat exchange with the spray cooling water, the heat exchange bypass valve (20) is closed through the PLC control end, and the reboiler control valve (18) is opened, and the amine liquid enters the reboiler (6) again for secondary heating. After the amine liquid temperature is heated to 65-85°C, it enters the regeneration tower (5).

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