Hydrogen sulfide purification system for coal chemical industry production

Abstract

The utility model relates to a hydrogen sulfide purification system for coal chemical industry production, which comprises heat exchange equipment connected with the top of a methanol regeneration tower and a gas-liquid separation tank, the top of the gas-liquid separation tank is connected with a first acid gas conveying pipeline, and an inlet, close to the tower top, of a hydrogen sulfide purification tower is communicated with the tower bottom of a hydrogen sulfide concentration tower; an inlet, close to the tower bottom, of the hydrogen sulfide purification tower is communicated with an acid gas conveying pipeline, the top of the hydrogen sulfide purification tower is communicated with the hydrogen sulfide concentration tower, and the bottom of the hydrogen sulfide purification tower is connected with a second booster pump and a sulfur-rich methanol conveying pipe; an inlet of a sulfur-rich methanol regeneration tower is communicated with a sulfur-rich methanol conveying pipe, the bottom of the sulfur-rich methanol regeneration tower is communicated with a methanol regeneration tower, the top of the sulfur-rich methanol regeneration tower is connected with a heat exchanger and a gas-liquid separation tank, and a top outlet of the gas-liquid separation tank is respectively connected with a first H2S conveying pipe and a second H2S conveying pipe. And a bottom outlet of the gas-liquid separation tank is communicated with the hydrogen sulfide purification tower. According to the device, hydrogen sulfide gas is purified, and high-concentration hydrogen sulfide gas is produced as a byproduct.

Description

Technical Field

[0001] The utility model relates to the technical field of coal chemical equipment, in particular to a hydrogen sulfide purification system used in coal chemical production. Background Art

[0002] The low temperature methanol washing device (such as Figure 1 (as shown) When the Linde process technology is used for hydrogen sulfide purification, the rich methanol flowing out of the bottom of the hydrogen sulfide concentration tower is usually pressurized by a first booster pump and then sent to a methanol regeneration tower through a pipeline connected to the output end of the first booster pump for methanol regeneration. After the acid gas output from the top of the methanol regeneration tower after regeneration is subjected to three heat exchanges and secondary gas-liquid separation, the separated rich methanol is sent to the hydrogen sulfide concentration tower again, and the separated acid gas is partially returned to the hydrogen sulfide concentration tower for re-concentration. In this process, H2S and CO2 in the conversion gas are absorbed at a relatively high pressure through the selectivity of low-temperature methanol absorption, and the treated purified gas is free of acid gases in the conversion gas, so as to produce purified gas that meets the requirements of methanol synthesis production.

[0003] When the lean methanol from the low-temperature methanol washing unit enters the methanol washing tower (7.5MPa), it absorbs H2S and CO2 in the conversion gas. The rich methanol after absorption is regenerated into lean methanol through decompression, gasification and distillation, and then enters the methanol washing tower for recycling again.

[0004] The regeneration process of the 7.5MPa rich methanol that absorbs H2S and CO2 in the conversion gas is as follows: the 7.5MPa rich methanol that absorbs H2S and CO2 in the conversion gas is depressurized to 0.08MPa and enters the T103 hydrogen sulfide concentration tower, where a large amount of CO2 is decomposed through nitrogen stripping, and the rich methanol is pumped to the T104 methanol regeneration tower through P103A / B, and acid gas is produced at the top of the methanol regeneration tower.

[0005] However, the acid gas contains a large amount of CO2, while the H2S content is relatively low (the acid gas component percentage is CO2: 65%, H2S: 25%, N2: 7%, CH3: 3%). If it is directly discharged, it will cause air pollution. Therefore, the generally used process now is to send it to a sulfur recovery device to produce industrial sulfur. However, due to its low H2S content, directly using it as a raw material to produce industrial sulfur cannot meet the requirements of industrial sulfur production and has low economic benefits. Therefore, increasing the H2S content is of great significance. Utility Model Content

[0006] The purpose of the utility model is to overcome the above-mentioned problems existing in the prior art and to provide a hydrogen sulfide purification system for coal chemical production. The system uses low-temperature methanol rich in carbon dioxide to purify hydrogen sulfide gas in low-concentration acidic gas based on the different solubilities of hydrogen sulfide and carbon dioxide in low-temperature methanol, and produces high-concentration hydrogen sulfide gas as a by-product. The hydrogen sulfide gas is then sent to an industrial sulfur production device, thereby solving the problem that the economic benefit is low and cannot meet the requirements of industrial sulfur production.

[0007] The utility model provides a hydrogen sulfide purification system for coal chemical production, comprising: a hydrogen sulfide concentration tower and a methanol regeneration tower, the top of the methanol regeneration tower is connected with a heat exchange device and a gas-liquid separation tank, the top of the gas-liquid separation tank is connected with a first acid gas transmission pipeline, and also includes:

[0008] A hydrogen sulfide purification tower, wherein the inlet near the top of the tower is connected to the bottom of the hydrogen sulfide concentration tower through a first booster pump and a pipeline, the inlet near the bottom of the tower is connected to the acid gas delivery pipeline through a pipeline, the top is connected to the hydrogen sulfide concentration tower through a hydrogen sulfide pipeline, and the bottom is connected to a second booster pump and a sulfur-rich methanol delivery pipe;

[0009] The inlet of the sulfur-rich methanol regeneration tower is connected with the sulfur-rich methanol delivery pipe, the bottom of the tower is connected with the methanol regeneration tower through the third booster pump and the lean methanol delivery pipe, the top of the tower is connected with a heat exchanger and a gas-liquid separation tank, the top outlet of the gas-liquid separation tank is connected with the first H2S delivery pipe and the second H2S delivery pipe, and the bottom outlet of the gas-liquid separation tank is connected with the hydrogen sulfide purification tower.

[0010] Preferably, the top of the gas-liquid separation tank is connected to a hydrogen sulfide purification tower.

[0011] Preferably, valves are provided on both the first H2S delivery pipe and the second H2S delivery pipe, the first H2S delivery pipe is connected to a hydrogen sulfide recovery device, and the second H2S delivery pipe is connected to a hydrogen sulfide production device.

[0012] Preferably, the bottom of the hydrogen sulfide purification tower is connected to the hydrogen sulfide purification tower through a sulfur-rich methanol reflux pipe.

[0013] Preferably, the bottom of the methanol regeneration tower is connected with a depleted methanol storage tank delivery pipe.

[0014] Preferably, the top of the hydrogen sulfide concentration tower is connected with a tail gas venting tube delivery pipe.

[0015] Preferably, the first H2S delivery pipe and the second H2S delivery pipe are connected to the top outlet of the gas-liquid separation tank through an H2S delivery main pipe, and an H2S analyzer is provided on the H2S delivery main pipe.

[0016] Preferably, the hydrogen sulfide concentration tower is also connected to a low-pressure nitrogen delivery pipe.

[0017] Preferably, the heat exchange equipment includes a first heat exchanger, the gas-liquid separation tank includes a first separation tank, the top of the methanol regeneration tower is connected to the first heat exchanger, the first heat exchanger is connected to the first separation tank, the bottom outlet of the first separation tank is connected to a fourth booster pump, and the fourth booster pump is connected to the methanol regeneration tower through a pipeline.

[0018] Preferably, the top of the sulfur-rich methanol regeneration tower is connected to a fifth heat exchanger and a third separation tank, the fifth heat exchanger is connected to the third separation tank, the bottom outlet of the third separation tank is connected to a fifth booster pump, and the fifth booster pump is connected to the sulfur-rich methanol regeneration tower through a pipeline.

[0019] Preferably, the top of the gas-liquid separation tank is connected with a second acid gas delivery pipe, and the second acid gas delivery pipe is respectively connected with the acid gas flare pipeline and the sulfur recovery device.

[0020] Compared with the prior art, the beneficial effects of the utility model are:

[0021] 1. The present invention can ensure the normal operation of the existing low-temperature methanol washing device: in the low-temperature methanol washing device, low-temperature methanol is used to absorb hydrogen sulfide and carbon dioxide gas, and the solubility of hydrogen sulfide is six times that of carbon dioxide; therefore, a small amount of rich methanol in the low-temperature methanol washing system is sent to the hydrogen sulfide purification tower, and the small amount of rich methanol can absorb the hydrogen sulfide in the acidic gas again at a low temperature; finally, the rich methanol rich in hydrogen sulfide in the hydrogen sulfide purification tower is sent to the sulfur-rich methanol regeneration tower, and the top of the regeneration tower can produce more than 90% high-concentration hydrogen sulfide gas.

[0022] 2. The present invention produces high-purity hydrogen sulfide gas, which can be used to produce sodium hydrosulfide to generate higher economic benefits than producing sulfur. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 This is an actual production process flow chart of the prior art.

[0024] Figure 2 This is the actual production process flow chart of the utility model

[0025] Description of reference numerals:

[0026] 1. Hydrogen sulfide concentration tower, 2. Methanol regeneration tower, 3. First heat exchanger, 4. First separation tank, 5. Second heat exchanger, 6. Third heat exchanger, 7. Second separation tank, 8. Hydrogen sulfide purification tower, 9. Fourth heat exchanger, 10. Sulfur-rich methanol regeneration tower, 11. Fifth heat exchanger, 12. Third separation tank, 13. Sixth heat exchanger, 14. Seventh heat exchanger, 15. Fourth separation tank. DETAILED DESCRIPTION

[0027] The following is combined with Figure 2 , the specific implementation of the utility model is described in detail, but it should be understood that the protection scope of the utility model is not limited by the specific implementation. Based on the embodiments of the utility model, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the utility model.

[0028] Due to existing technologies, such as Figure 1 In the hydrogen sulfide purification system for coal chemical production provided, during the hydrogen sulfide concentration and methanol purification process, the acid gas obtained contains a large amount of CO2, while the H2S content is relatively low (the acid gas component percentage is CO2: 65%, H2S: 25%, N2: 7%, CH3: 3%). If it is directly discharged, it will cause air pollution and does not meet environmental protection requirements. Therefore, it is sent to a sulfur recovery device to produce industrial sulfur. However, due to its low H2S content, it cannot meet the requirements for producing industrial sulfur by directly using it as a raw material, and the economic benefit is low.

[0029] In view of this, it is necessary to improve the hydrogen sulfide purification system used in coal chemical production in the prior art to reduce the problems of low purity of the product sodium hydrosulfide and high consumption of sodium hydroxide due to the large amount of CO2 contained in the acid gas.

[0030] like Figure 2 As shown, the utility model provides a hydrogen sulfide purification system for coal chemical production, comprising: a hydrogen sulfide concentration tower 1, a methanol regeneration tower 2, a hydrogen sulfide purification tower 8 and a methanol-rich regeneration tower 10, wherein the bottom of the hydrogen sulfide concentration tower 1 is connected to a first delivery pipe and a first booster pump, and the first booster pump is respectively connected to a second delivery pipe and a third delivery pipe through a first tee; the middle of the methanol regeneration tower 2 is connected to the second delivery pipe, the top of the methanol regeneration tower 2 is connected to a fourth delivery pipe and a first heat exchanger 3, and the first heat exchanger 3 is connected to a fifth delivery pipe. , the fifth delivery pipe is connected to the first separation tank 4, the top of the first separation tank 4 is connected to the sixth delivery pipe and the second heat exchanger 5, the second heat exchanger 5 is connected to the seventh delivery pipe and the third heat exchanger 6, the third heat exchanger 6 is connected to the second separation tank 7, the top of the second separation tank 7 is respectively connected to the eighth delivery pipe and the ninth delivery pipe through the second tee, wherein the ninth delivery pipe is the second acid gas delivery pipe, the eighth delivery pipe is connected to the hydrogen sulfide concentration tower 1, the bottom of the second separation tank 7 is connected to the tenth delivery pipe, and the tenth delivery pipe is connected to the hydrogen sulfide concentration tower 1;

[0031] The upper middle portion of the hydrogen sulfide purification tower 8 is connected to the third delivery pipe, the lower middle portion of the hydrogen sulfide purification tower 8 is connected to the ninth delivery pipe, the top of the hydrogen sulfide purification tower 8 is connected to the eleventh delivery pipe, the eleventh delivery pipe is connected to the hydrogen sulfide concentration tower 1, the bottom of the hydrogen sulfide purification tower 8 is connected to the twelfth delivery pipe and the second booster pump, the second booster pump is respectively connected to the thirteenth delivery pipe and the fourteenth delivery pipe through the third three-way, the thirteenth delivery pipe is connected to the upper middle portion of the hydrogen sulfide purification tower 8 (the thirteenth delivery pipe is the sulfur-rich methanol reflux pipe), the fourteenth delivery pipe is connected to the shell side inlet of the fourth heat exchanger 9, and the shell side outlet of the fourth heat exchanger 9 is connected to the fifteenth delivery pipe;

[0032] The upper middle portion of the rich methanol regeneration tower 10 is connected to the fifteenth delivery pipe, the top of the rich methanol regeneration tower 10 is connected to the sixteenth delivery pipe and the fifth heat exchanger 11, the fifth heat exchanger 11 is connected to the seventeenth delivery pipe, the seventeenth delivery pipe is connected to the third separation tank 12, the top of the third separation tank 12 is connected to the eighteenth delivery pipe, the eighteenth delivery pipe is connected to the sixth heat exchanger 13, the sixth heat exchanger 13 is connected to the nineteenth delivery pipe and the seventh heat exchanger 14, the seventh heat exchanger 14 is connected to the twentieth delivery pipe and the fourth separation tank 15, the top of the fourth separation tank 15 is connected to the The fourth three-way pipe is respectively connected to the twenty-first delivery pipe and the twenty-second delivery pipe, the twenty-first delivery pipe is connected to the hydrogen sulfide purification tower 8, the twenty-second delivery pipe is connected to the tube side inlet of the sixth heat exchanger 13, the bottom of the fourth separation tank 15 is connected to the hydrogen sulfide purification tower 8 through the twenty-third delivery pipe, the bottom of the methanol-rich regeneration tower 10 is connected to the twenty-fourth delivery pipe and the third pressure pump, the third pressure pump is connected to the tube side inlet of the fourth heat exchanger 9, the tube side outlet of the fourth heat exchanger 9 is connected to the twenty-fifth delivery pipe, and the twenty-fifth delivery pipe is connected to the methanol regeneration tower 2.

[0033] Specifically, the top of the gas-liquid separation tank is communicated with the hydrogen sulfide purification tower 8 .

[0034] Specifically, the bottom of the first separation tank 4 is connected with a twenty-sixth delivery pipe and a fourth pressure pump, and the fourth pressure pump is connected with the methanol regeneration tower 2 through a twenty-seventh delivery pipe.

[0035] Specifically, a twenty-eighth delivery pipe and a fifth pressure pump are connected to the bottom of the third separation tank 12 , and the fifth pressure pump is connected to the methanol-rich regeneration tower 10 through a twenty-ninth delivery pipe.

[0036] Specifically, the tube outlet of the sixth heat exchanger 13 is connected to the 30th delivery pipe, and the 30th delivery pipe is respectively connected to the first H2S delivery pipe and the second H2S delivery pipe through the fifth tee, and the second H2S delivery pipe is connected to the desulfurization recovery device.

[0037] Specifically, the ninth delivery pipe is connected to the thirty-first delivery pipe, the thirty-first delivery pipe is communicated with the tube side inlet of the second heat exchanger 5, the tube side outlet of the second heat exchanger 5 is connected to the thirty-second delivery pipe, and the thirty-second delivery pipe is respectively connected to the deacidified gas flare pipeline and the sulfur recovery device through the sixth tee.

[0038] Specifically, the bottom of the methanol regeneration tower 2 is connected with a depleted methanol storage tank delivery pipe.

[0039] Specifically, valves are provided on the low-pressure nitrogen delivery pipe, the second delivery pipe, the third delivery pipe, the eighth delivery pipe, the tenth delivery pipe, the eleventh delivery pipe, the thirteenth delivery pipe, the fifteenth delivery pipe, the twenty-first delivery pipe, the twenty-fifth delivery pipe, the twenty-seventh delivery pipe, the first H2S delivery pipe, the second H2S delivery pipe, the acid gas flare pipeline and the delivery pipeline connecting to the sulfur recovery unit.

[0040] Specifically, a low-pressure nitrogen delivery pipe is connected to the lower middle portion of the hydrogen sulfide concentration tower 1 , and a tail gas delivery pipe to a vent cylinder is connected to the top of the hydrogen sulfide concentration tower 1 .

[0041] Specifically, the eleventh delivery pipe is provided with a pressure gauge.

[0042] Specifically, a H2S analyzer is provided on the 22nd delivery pipe.

[0043] Process principle:

[0044] The principle of the low-temperature methanol washing process is based on the different solubilities of H2S and CO2 in low-temperature methanol. The CO2 and H2S in the conversion process gas are absorbed through a methanol washing tower under high pressure and low temperature. The upper tower of the methanol washing tower absorbs CO2, and the lower tower of the methanol washing tower absorbs H2S to obtain purified gas that meets the requirements of methanol synthesis. According to test data, the solubility of H2S in low-temperature methanol is about six times that of CO2.

[0045] At the same time, the rich methanol that has absorbed CO2 in the upper part of the methanol washing tower can enter the lower tower to absorb H2S again, and the dissolution heat released when absorbing H2S is compensated by the desorption heat of CO2 in methanol, so that the temperature of the desulfurization section of the methanol washing tower does not rise, which is conducive to the absorption of H2S.

[0046] In the prior art, such as Figure 1The process flow of the hydrogen sulfide purification system for coal chemical production is described as follows: the bottom of the hydrogen sulfide concentration tower 1 (T103) in the low-temperature methanol washing is rich in methanol, which is pressurized by the first pressure pump (P103 pump) and sent to the methanol regeneration tower 2 (T104). 0.5MPa low-pressure steam is introduced into the heat exchange gas (E112) for heating and regeneration. The acid gas regenerated at the top of the methanol regeneration tower 2 (T104) passes through the first heat exchanger 3 (E113)-water cooler, the second Heat exchanger 5 (E114) and the third heat exchanger 6 (E117) - propylene cryogenic cooler are used for cooling, and the methanol-rich gas separated by cooling is sent to hydrogen sulfide concentration tower 1 (T103) through the second gas-liquid separator (V107). The acid gas at the top of the second gas-liquid separator (V107) is sent to the hydrogen sulfide concentration tower 1 (T103) for concentration. After concentration, the regenerated acid gas concentration can reach 25-40%, and is sent to the sulfur recovery device to produce industrial sulfur.

[0047] like Figure 1 As shown, in the low-temperature methanol washing process, the H2S concentration in the acidic gas regenerated by the methanol regeneration tower 2 (T104) reaches up to about 40%, which is used for the sulfur recovery device to produce sulfur. Pure oxygen is required for combustion or liquefied gas is burned to maintain the temperature of the sulfur-making furnace, and the energy consumption is relatively high. 40% of the H2S gas is used to produce sodium hydrosulfide. Since it contains a large amount of CO2, the purity of the product sodium hydrosulfide is low, and the consumption of sodium hydroxide is large and cannot meet the requirements for the production of industrial sulfur, resulting in low economic benefits.

[0048] like Figure 2 As shown, the hydrogen sulfide purification system for coal chemical production provided by the present invention is an improvement made on the original hydrogen sulfide purification system for coal chemical production, and its process flow is described as follows:

[0049] The bottom of the hydrogen sulfide concentration tower 1 (T103) is rich in methanol during low-temperature methanol washing. After being pressurized by the first pressure pump (P103 pump), part of it is sent to the methanol regeneration tower 2 (T104), and part of it is sent to the hydrogen sulfide purification tower 8 (T113). 0.5MPa low-pressure steam is introduced into the heat exchange gas (E112) for heating and regeneration. Acidic gas (CO2: 65%, H2S: 25-40%, N2: 7%, CH3: 3%) is regenerated at the top of the methanol regeneration tower 2 (T104).

[0050] The temperature is lowered through the first heat exchanger 3 (E113)-water cooler, the second heat exchanger 5 (E114) and the third heat exchanger 6 (E117)-propylene deep cooler, and the methanol-rich gas separated by the lowering temperature is sent to the hydrogen sulfide concentration tower 1 (T103) through the second gas-liquid separator (V107). The acid gas at the top of the second gas-liquid separator (V107) is sent to the hydrogen sulfide concentration tower 1 (T103) for concentration, and the acid gas at the top of the second gas-liquid separator (V107) tank is sent to the bottom of the hydrogen sulfide concentration tower 1 (T103) for concentration, so that the H2S concentration in the regenerated acid gas can be reduced. When the temperature reaches 40%, the valve on the top of the second gas-liquid separator (V107) tank that is sent to the sulfur recovery device and the acid gas flare pipeline is closed. After being separated by cooling, the gas is drawn out from the second gas-liquid separator (V107) and sent to the bottom of the hydrogen sulfide purification tower 8 (T113); it is reversely contacted with a small amount of rich methanol at the bottom of the hydrogen sulfide concentration tower 1 (T103) sent to the top of the hydrogen sulfide purification tower 8 (T113) by the first booster pump (P103A / B), and the acid gas from the top of the second gas-liquid separator (V107) tank is washed and separated; since H2S is in the low-temperature methanol The solubility of H2S is about six times that of CO2. Therefore, the low-temperature rich methanol sent by the first booster pump (P103A / B) absorbs the H2S in the acidic gas sent by the second gas-liquid separator (V107), and at the same time analyzes the CO2 in the rich methanol. When the H2S in the sulfur-rich methanol in the hydrogen sulfide purification tower 8 (T113) reaches saturation, the sulfur-rich methanol after washing and separation is sent to the sulfur-rich methanol regeneration tower 10 (T114) for regeneration through the third booster pump (P113A / B). The regenerated acidic gas is cooled and separated by the propylene cooler 14 (E127) to obtain high-purity H2S acidic gas. The H2S concentration in the acidic gas can reach 90%; a large amount of CO2 gas analyzed from the top of the hydrogen sulfide purification tower 8 (T113) is sent to the middle section of the hydrogen sulfide concentration tower 1 (T103) for desulfurization treatment, so that trace amounts of hydrogen sulfide in the analyzed CO2 gas are absorbed by the low-temperature methanol in the hydrogen sulfide concentration tower 1 (T103), preventing the CO2 gas containing trace amounts of H2S at the top of the hydrogen sulfide purification tower 8 (T113) from being directly discharged to pollute the environment; a large amount of CO2 gas analyzed from the hydrogen sulfide purification tower 8 (T113) enters the exhaust gas in the hydrogen sulfide concentration tower 1 (T103) for emission that meets the emission standards.

[0051] After the lean methanol is regenerated at the bottom of the sulfur-rich methanol regeneration tower 10 (T114), in order to prevent high sulfide content in the lean methanol, the lean methanol at the bottom of the sulfur-rich methanol regeneration tower 10 (T114) is pressurized by the third pressure pump (P116A / B) and sent to the methanol regeneration tower 2 (T104) for regeneration again to ensure that the quality of the lean methanol entering the low-temperature methanol washing meets the standards.

[0052] When the sulfur-rich methanol at the bottom of the hydrogen sulfide purification tower 8 (T113) is sent out through P113A / B, part of the sulfur-rich methanol is refluxed to the upper part of the hydrogen sulfide purification tower 8 (T113), so that the sulfur-rich methanol is circulated again inside the hydrogen sulfide purification tower 8 (T113) to absorb H2S in the acid gas, thereby increasing the concentration of hydrogen sulfide absorbed by the rich methanol in the hydrogen sulfide purification tower 8 (T113), and is sent out to the sulfur-rich methanol regeneration tower 10 (T114) for regeneration to obtain high-purity H2S gas.

[0053] The top of the methanol regeneration tower 2 (T104) is sent to the first separation tank 4 for gas-liquid separation after heat exchange in the first heat exchanger 3, which can reduce the amount of methanol carried in the regenerated acid gas. The separated liquid is pumped to the top of the regeneration tower through P107A / B and recycled as the reflux liquid at the top of the regeneration tower.

[0054] The top of the methanol regeneration tower 10 (T114) is sent to the third separation tank 12 for gas-liquid separation after heat exchange in the fifth heat exchanger 11 to reduce the amount of methanol carried in the regenerated acid gas. The separated liquid is pumped to the top of the regeneration tower through P117A / B and recycled as regeneration tower top reflux liquid.

[0055] The acid gas regenerated from the top of the sulfur-rich methanol regeneration tower 10 (T114) is separated by gas-liquid separation by V117 and then detected by an online H2S analyzer at the top outlet of the V117 separator. When the H2S content in the regenerated acid gas reaches 90%, the self-regulating valve of the acid gas desulfurization recovery device is closed to produce high-purity H2S for recycling.

[0056] Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. A hydrogen sulfide purification system for coal chemical production, comprising: The hydrogen sulfide concentration tower (1) and the methanol regeneration tower (2) are characterized in that the top of the methanol regeneration tower (2) is connected to a heat exchange device and a gas-liquid separation tank, the top of the gas-liquid separation tank is connected to a first acid gas transmission pipeline, and further comprises: A hydrogen sulfide purification tower (8), wherein the inlet near the top of the tower is connected to the bottom of the hydrogen sulfide concentration tower (1) through a first booster pump and a pipeline, the inlet near the bottom of the tower is connected to the acid gas delivery pipeline through a pipeline, the top is connected to the hydrogen sulfide concentration tower (1) through a hydrogen sulfide pipeline, and the bottom is connected to a second booster pump and a sulfur-rich methanol delivery pipe; The inlet of the sulfur-rich methanol regeneration tower (10) is connected to the sulfur-rich methanol delivery pipe, the bottom of the tower is connected to the methanol regeneration tower (2) through the third booster pump and the lean methanol delivery pipe, the top of the tower is connected to the heat exchanger and the gas-liquid separation tank, the top outlet of the gas-liquid separation tank is connected to the first H2S delivery pipe and the second H2S delivery pipe, and the bottom outlet of the gas-liquid separation tank is connected to the hydrogen sulfide purification tower (8).

2. A hydrogen sulfide purification system for coal chemical production according to claim 1, characterized in that: The top of the gas-liquid separation tank is connected to the hydrogen sulfide purification tower (8).

3. A hydrogen sulfide purification system for coal chemical production according to claim 1, characterized in that: The first H2S delivery pipe and the second H2S delivery pipe are both provided with valves. The first H2S delivery pipe is connected to the hydrogen sulfide recovery device, and the second H2S delivery pipe is connected to the hydrogen sulfide production device.

4. A hydrogen sulfide purification system for coal chemical production according to claim 1, characterized in that: The bottom of the hydrogen sulfide purification tower (8) is connected to the hydrogen sulfide purification tower (8) via a sulfur-rich methanol reflux pipe.

5. A hydrogen sulfide purification system for coal chemical production according to claim 1, characterized in that: The bottom of the methanol regeneration tower (2) is connected to a depleted methanol storage tank delivery pipe, and the top of the hydrogen sulfide concentration tower (1) is connected to a tail gas venting cylinder delivery pipe.

6. A hydrogen sulfide purification system for coal chemical production according to claim 1, characterized in that: The first H2S delivery pipe and the second H2S delivery pipe are connected to the top outlet of the gas-liquid separation tank through the H2S delivery main pipe, and the H2S delivery main pipe is provided with an H2S analyzer.

7. A hydrogen sulfide purification system for coal chemical production according to claim 1, characterized in that: The hydrogen sulfide concentration tower (1) is also connected to a low-pressure nitrogen delivery pipe.

8. A hydrogen sulfide purification system for coal chemical production according to claim 1, characterized in that: The heat exchange equipment comprises a first heat exchanger (3), the gas-liquid separation tank comprises a first separation tank (4), the top of the methanol regeneration tower (2) is connected to the first heat exchanger (3), the first heat exchanger (3) is communicated with the first separation tank (4), the bottom outlet of the first separation tank (4) is connected to a fourth booster pump, and the fourth booster pump is communicated with the methanol regeneration tower (2) through a pipeline.

9. A hydrogen sulfide purification system for coal chemical production according to claim 1, characterized in that: The top of the sulfur-rich methanol regeneration tower (10) is connected to a fifth heat exchanger (11) and a third separation tank (12), the fifth heat exchanger (11) is connected to the third separation tank (12), the bottom outlet of the third separation tank (12) is connected to a fifth booster pump, and the fifth booster pump is connected to the sulfur-rich methanol regeneration tower (10) through a pipeline.

10. A hydrogen sulfide purification system for coal chemical production according to claim 1, characterized in that: The top of the gas-liquid separation tank is connected with a second acid gas delivery pipe, and the second acid gas delivery pipe is respectively connected with the acid gas flare pipeline and the sulfur recovery device.

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