Synthetic gas hydrogen production device and synthetic gas hydrogen production method

Abstract

The invention discloses a synthesis gas hydrogen production device which comprises a gas-water separator, a coal gas preheater, a self-heating purification furnace, a first conversion furnace, a second conversion furnace, a third conversion furnace, a waste heat boiler, a desalted water heater, a water cooler and an ammonia washing tower which are sequentially connected through a plurality of pipelines, the first conversion furnace is connected with a steam pocket through a second gas outlet pipe, the steam pocket is connected with a coal gas preheater through a return pipe, a first connecting pipe is connected between the self-heating purification furnace and the gas-water separator, the waste heat boiler is connected with a condenser pipe, a water inlet pipe is connected between the desalted water heater and the ammonia washing tower, and the gas-water separator is connected with a gas inlet pipe; the invention also discloses a method for producing hydrogen from synthesis gas. According to the invention, the depth of the conversion reaction can be effectively controlled, the waste heat generated by the conversion reaction is efficiently recycled, the production energy consumption is effectively reduced, the energy conversion rate is improved, the conversion reaction efficiency is high, and the process flow is short.

Description

Technical Field

[0001] The present invention belongs to the technical field of coal chemical plants, and relates to a syngas hydrogen production device. The present invention also relates to a syngas hydrogen production method. Background Art

[0002] The dry basis content of carbon monoxide in the raw syngas produced by the gasification technology is between 45% and 60%. In order to improve the driving force of the raw syngas shift reaction and avoid the methanation side reaction, most current shift devices adopt a high steam-to-gas ratio shift process, and the steam-to-gas ratio is generally greater than 1.2. In order to increase the steam-to-gas ratio, a large amount of steam needs to be introduced into the shift furnace, which not only consumes a large amount of energy, but also makes it difficult to control the reaction depth, and is prone to the adverse result of "temperature runaway" in the shift furnace bed. At the same time, a high steam-to-gas ratio is also prone to cause the performance of the catalyst to age and decay, shorten the catalyst life, increase the production operation cost, and it is difficult to achieve long-term stable operation of the production device. Chinese patent document with publication number CN101050391A discloses a pulverized coal gasification low water / gas sulfur-tolerant shift process. The shift process adopts a one-stage low steam-to-gas ratio sulfur-tolerant shift process with a steam-to-gas ratio of 0.15 to 0.2, but fails to fully recover the waste heat generated by the shift reaction, has a low driving force for the shift reaction, a shallow shift depth, and low production energy efficiency; Chinese patent document with publication number CN108203077A discloses a raw coal gas shift process. The shift process adopts a conventional shift process, and the process flow is cumbersome and the waste heat recovery utilization rate is low; Therefore, it is of great significance for the production operation of coal chemical plants to invent a low steam-to-gas ratio shift process that can effectively control the shift reaction depth, efficiently recover and utilize the waste heat generated by the shift reaction, effectively reduce production energy consumption, and improve the energy conversion rate. Summary of the Invention

[0003] The purpose of the present invention is to provide a syngas hydrogen production device, which solves the problems in the prior art that a large amount of steam needs to be introduced into the shift furnace in the syngas hydrogen production device and the catalyst bed "temperature runaway" occurs during start-up and shutdown.

[0004] The second purpose of the present invention is a syngas hydrogen production method.

[0005] The first technical solution adopted by the present invention is a syngas hydrogen production device, which includes a gas-water separator, a coal gas preheater, a self-heating purification furnace, a first shift furnace, a second shift furnace, a third shift furnace, a waste heat boiler, a demineralized water heater, a water cooler, and a wash ammonia tower connected in sequence through several pipelines. The wash ammonia tower is connected with a first gas outlet pipe. The first shift furnace is connected with a steam drum through a second gas outlet pipe. The steam drum is connected with the coal gas preheater through a reflux pipe. A first connecting pipe is connected between the self-heating purification furnace and the gas-water separator. The waste heat boiler is connected with a condensate pipe. A water inlet pipe is connected between the demineralized water heater and the wash ammonia tower. The gas-water separator is connected with a gas inlet pipe.

[0006] The features of the first technical solution of the present invention also lie in: The gas-water separator is connected with an intake pipe, a condensation pump is arranged on the condensation pipe, the steam drum is connected with a first water supply pipe, a fifth regulating valve is arranged on the first water supply pipe, the water cooler is connected with a second water supply pipe, a sixth regulating valve is arranged on the second water supply pipe, the second shift converter is connected with a third water supply pipe, a seventh regulating valve is arranged on the third water supply pipe, the third shift converter is connected with a fourth water supply pipe, an eighth regulating valve is arranged on the fourth water supply pipe, the first water supply pipe, the second water supply pipe, the third water supply pipe and the fourth water supply pipe are jointly connected with a self-pipeline network, a first regulating valve is arranged on each pipeline, a second regulating valve is arranged on the first connecting pipe, a third regulating valve is arranged on the reflux pipe, and a pressure regulating valve is arranged on the second gas outlet pipe.

[0007] An exhaust pipe is connected to the pipeline of the reflux pipe between the third regulating valve and the gas preheater, a fourth regulating valve is arranged on the exhaust pipe, the steam drum is connected with a first chemical dosing device through a second connecting pipe, a first metering pump is arranged on the second connecting pipe, the waste heat boiler is connected with a second chemical dosing device through a third connecting pipe, and a second metering pump is arranged on the third connecting pipe.

[0008] The first shift converter is a temperature-controlled shift converter, the second shift converter and the third shift converter are both axial-radial shift converters, the demineralized water heater is connected with a fourth water outlet pipe, a fifth connecting pipe is connected between the gas preheater and the waste heat boiler, a heat exchanger is arranged in the first shift converter, the heat exchanger is connected with the second gas outlet pipe, the waste heat boiler is respectively connected with a third gas outlet pipe and a water supply pipe, and a ninth regulating valve is arranged on the water supply pipe.

[0009] The second technical solution adopted by the present invention is a method for producing hydrogen from syngas, which includes the following steps: Step 1: Feed the syngas into the gas-water separator to separate the liquid water. A part of the gas is preheated by the gas preheater and then sent to the autothermal purification furnace, and the remaining gas is directly introduced into the autothermal purification furnace to remove impurities and preheat the mixed gas to generate the first shift gas; Step 2: Feed the first shift gas into the first shift converter for a shift reaction to generate the second shift gas; Step 3: Feed the second shift gas into the second shift converter for temperature reduction, humidity increase and shift reaction to generate the third shift gas; Step 4: Feed the third shift gas into the third shift converter for temperature reduction, humidity increase and shift reaction to generate the fourth shift gas; Step 5: Cool the fourth shift gas successively through the waste heat boiler, the demineralized water heater and the water cooler, and then perform gas-liquid separation, ammonia washing and methanol cleaning in the ammonia washing tower to collect hydrogen.

[0010] The features of the second technical solution of the present invention also lie in: Step 1 is specifically carried out according to the following steps: Step 1.1: Feed the syngas through the inlet pipe to the gas-water separator. The gas-water separator separates the liquid water and adjusts the first regulating valve and the second regulating valve to send 20%-30% of the gas into the gas preheater. Step 1.2: Preheat the gas entering the gas preheater to 250°C - 265°C and then send it to the catalyst section of the autothermal purification furnace. At the same time, the gas preheater sends the generated steam condensate to the waste heat boiler through the fifth connecting pipe. Step 1.3: Control the temperature of the autothermal purification furnace at 350°C - 400°C. A cobalt-molybdenum based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is installed in the catalyst section of the autothermal purification furnace. The gas undergoes a shift reaction under the action of the cobalt-molybdenum catalyst. The space velocity of the shift reaction is 3200h -1 -6000h -1 , generating converted gas. The converted gas and the remaining gas from the gas-water separator are simultaneously introduced into the detoxification section of the autothermal purification furnace. The detoxification section is provided with a detoxifying agent, which is QBS-02 sulfur-tolerant shift protective agent. The carbon black, oxygen, tar, dust, arsenic, phosphorus, and chlorine are removed through the detoxifying agent. The autothermal purification furnace preheats the mixed gas to 255°C - 275°C, generating the first converted gas.

[0011] Step 2 is specifically carried out as follows: Step 2.1: Feed the first converted gas into the catalyst section of the first conversion furnace. The water-gas ratio in the first converted gas is 0.2 - 1.2. A cobalt-molybdenum based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is installed in the catalyst section of the first conversion furnace. Set the bed temperature of the first conversion furnace at 280°C - 310°C. Step 2.2: The carbon monoxide and water vapor in the first converted gas undergo a shift reaction and generate heat simultaneously. The space velocity of the shift reaction is 3200h -1 -6000h -1 , and the heat is sent to the steam drum through the heat exchanger and the second outlet pipe. Water is sent to the steam drum from the pipe network through the first water supply pipe. Steam at 5.8MPa - 7MPa is generated in the steam drum. Part of the steam is introduced into the gas preheater to continue participating in the preheating, and the remaining steam is collected through the exhaust pipe. Step 2.3: Measure the temperature of the first converted gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the first converted gas is not more than 2.34mol% and the temperature of the mixed gas reaches 270°C - 310°C, the second converted gas is generated. The second converted gas is introduced into the water spraying section of the second conversion furnace, and water spraying is provided from the pipe network through the third water supply pipe at the same time.

[0012] Step 3 is specifically carried out as follows: Step 3.1: Set the bed temperature of the second shift converter to 240°C - 300°C. Cool down and humidify by spraying water to make the temperature of the second shifted gas reach 230°C - 250°C, and then introduce the second shifted gas into the catalyst section of the second shift converter. Step 3.2: A cobalt-molybdenum based sulfur-tolerant wide-temperature carbon monoxide shift catalyst is provided in the catalyst section of the second shift converter. The second shifted gas undergoes a shift reaction and generates heat. The space velocity of the shift reaction is 3200 h -1 -6000 h -1 . Measure the temperature of the second shifted gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the second shifted gas is not more than 1% and the temperature of the mixed gas reaches 210°C - 240°C, the third shifted gas is generated. The third shifted gas is introduced into the water spraying section of the third shift converter, and at the same time, water spraying is provided from the pipe network through the fourth water supply pipe.

[0013] Step 4 is specifically carried out according to the following steps: Step 4.1: Set the bed temperature of the third shift converter to 220°C - 270°C. Cool down and humidify by spraying water to make the temperature of the third shifted gas reach 220°C, and then introduce the third shifted gas into the catalyst section of the third shift converter. A cobalt-molybdenum based sulfur-tolerant wide-temperature carbon monoxide shift catalyst is provided in the catalyst section of the third shift converter. The third shifted gas undergoes a shift reaction. The space velocity of the shift reaction is 3200 h -1 -6000 h -1 ; Step 4.2: Measure the temperature of the third shifted gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the third shifted gas is not more than 0.6% and the temperature of the mixed gas reaches 223°C, the fourth shifted gas is generated. The fourth shifted gas is introduced into the waste heat boiler.

[0014] Step 5 is specifically carried out according to the following steps: Step 5.1: The fourth shifted gas is cooled to 168°C - 172°C by the steam condensate of the waste heat boiler, and the by-product steam of 0.5 MPa is collected through the third outlet pipe. Step 5.2: The fourth shifted gas is introduced into the demineralized water heater to be further cooled to 75°C, and then the fourth shifted gas is introduced into the water cooler to be cooled to 40°C. Water is sent from the pipe network through the second water supply pipe to the inlet of the water cooler to wash the dissolved salts. Step 5.3: The steam condensate of the waste heat boiler is pressurized to 7.8 MPa by a condensate pump and then sent into the ammonia washing tower. The fourth shifted gas is introduced into the ammonia washing tower for gas-liquid separation, steam condensate ammonia washing, and methanol cleaning in sequence, and the generated hydrogen is collected through the first outlet pipe.

[0015] The beneficial effects of the present invention are: The present invention can effectively control the depth of the shift reaction, efficiently recover and utilize the waste heat generated by the shift reaction, effectively reduce the production energy consumption, improve the energy conversion rate, has a high shift reaction efficiency and a short process flow, and is of great significance to the production operation of the coal chemical plant. By setting a chemical dosing device and a metering pump, scale inhibitors can be added to the steam drum and the waste heat boiler to prevent scaling. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 It is a structural diagram of the syngas-to-hydrogen production device of the present invention.

[0017] In the figure, 1. gas-water separator, 2. coal gas preheater, 3. autothermal purification furnace, 4. steam drum, 5. first shift furnace, 6. second shift furnace, 7. third shift furnace, 8. waste heat boiler, 9. desalted water heater, 10. water cooler, 11. ammonia washing tower, 12. first chemical dosing device, 13. first metering pump, 14. first regulating valve, 15. fourth regulating valve, 16. second chemical dosing device, 17. second metering pump, 18. inlet pipe, 19. first outlet pipe, 20. second outlet pipe, 21. return pipe, 22. exhaust pipe, 23. first connecting pipe, 24. first outlet water pipe, 25. first outlet water pipe, 26. second connecting pipe, 27. third connecting pipe, 28. second regulating valve, 29. third regulating valve, 30. pressure regulating valve, 31. condenser pipe, 32. condensate pump, 33. eighth regulating valve, 34. third outlet water pipe, 35. second outlet water pipe, 36. fourth connecting pipe, 37. fifth regulating valve, 38. seventh regulating valve, 39. sixth regulating valve, 40. fifth connecting pipe, 41. heat exchanger, 42. third outlet pipe, 43. self-pipeline network, 44. ninth regulating valve, 45. water supply pipe, 46. inlet water pipe. DETAILED DESCRIPTION OF THE INVENTION

[0018] The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments.

[0019] The syngas-to-hydrogen production device, referring to Figure 1 , includes a gas-water separator 1, a coal gas preheater 2, an autothermal purification furnace 3, a first shift furnace 5, a second shift furnace 6, a third shift furnace 7, a waste heat boiler 8, a desalted water heater 9, a water cooler 10, and an ammonia washing tower 11 that are sequentially connected through a plurality of pipelines. The ammonia washing tower 11 is connected with a first outlet pipe 19. The first shift furnace 5 is connected with a steam drum 4 through a second outlet pipe 20. The steam drum 4 is connected with the coal gas preheater 2 through a return pipe 21. A first connecting pipe 23 is connected between the autothermal purification furnace 3 and the gas-water separator 1. The waste heat boiler 8 is connected with a condenser pipe 31. An inlet water pipe 46 is connected between the desalted water heater 9 and the ammonia washing tower 11. The gas-water separator 1 is connected with an inlet pipe 18.

[0020] A condensate pump 32 is provided on the condenser pipe 31. The steam drum 4 is connected to a first water supply pipe 24, and a fifth regulating valve 37 is provided on the first water supply pipe 24. The water cooler 10 is connected to a second water supply pipe 35, and a sixth regulating valve 39 is provided on the second water supply pipe 35. The second shift converter 6 is connected to a third water supply pipe 34, and a seventh regulating valve 38 is provided on the third water supply pipe 34. The third shift converter 7 is connected to a fourth water supply pipe 36, and an eighth regulating valve 33 is provided on the fourth water supply pipe 36. The first water supply pipe 24, the second water supply pipe 35, the third water supply pipe 34, and the fourth water supply pipe 36 are jointly connected to a self-pipe network 43, and a first regulating valve 14 is provided on each pipe. A second regulating valve 28 is provided on the first connecting pipe 23, a third regulating valve 29 is provided on the return pipe 21, a pressure regulating valve 30 is provided on the second outlet gas pipe 20. An exhaust pipe 22 is connected to the return pipe 21 between the third regulating valve 29 and the gas preheater 2, and a fourth regulating valve 15 is provided on the exhaust pipe 22. The steam drum 4 is connected to a first chemical dosing device 12 through a second connecting pipe 26, and a first metering pump 13 is provided on the second connecting pipe 26. The waste heat boiler 8 is connected to a second chemical dosing device 16 through a third connecting pipe 27, and a second metering pump 17 is provided on the third connecting pipe 27. The scale inhibitor can be added to the steam drum 4 and the waste heat boiler 8 through the chemical dosing device and the metering pump to prevent scaling. The first shift converter 5 is a temperature-controlled shift converter, the second shift converter 6 and the third shift converter 7 are both axial-radial shift converters. The desalted water heater 9 is connected to a fourth water outlet pipe 25. A fifth connecting pipe 40 is connected between the gas preheater 2 and the waste heat boiler 8. A heat exchanger 41 is provided in the first shift converter 5, and the heat exchanger 41 is connected to the second outlet gas pipe 20. The waste heat boiler 8 is respectively connected to a third outlet gas pipe 42 and a water supply pipe 45, and a ninth regulating valve 44 is provided on the water supply pipe 45. The water supply pipe 45 is used to supplement low-pressure boiler water to the waste heat boiler 8.

[0021] The method for producing hydrogen from syngas includes the following steps: Step 1: Send the syngas through the inlet pipe 18 to the gas-water separator 1. The gas-water separator 1 separates the liquid water, and 20%-30% of the gas is sent to the gas preheater 2 by adjusting the first regulating valve 14 and the second regulating valve 28. The gas entering the gas preheater 2 is preheated to 250°C - 265°C and then sent to the catalyst section of the autothermal purification furnace 3. At the same time, the steam condensate generated by the gas preheater 2 is sent to the waste heat boiler 8 through the fifth connecting pipe 40. The temperature of the autothermal purification furnace 3 is controlled at 350°C - 400°C. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is provided in the catalyst section of the autothermal purification furnace 3. The gas undergoes a shift reaction under the action of the cobalt-molybdenum catalyst. The space velocity of the shift reaction is 3200h -1 -6000h -1, produce conversion gas, and simultaneously introduce the conversion gas and the remaining gas in the gas-water separator 1 into the detoxification section of the autothermal purification furnace 3. The detoxification section is provided with a detoxifying agent, and the detoxifying agent is QBS-02 sulfur-tolerant shift protective agent. Carbon black, oxygen, tar, dust, arsenic, phosphorus, and chlorine are removed through the detoxifying agent. The autothermal purification furnace 3 preheats the mixed gas to 255°C - 275°C to generate the first conversion gas; Step 2: Send the first conversion gas into the catalyst section of the first conversion furnace 5. The water-gas ratio in the first conversion gas is 0.2 - 1.2. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is provided in the catalyst section of the first conversion furnace 5. Set the bed temperature of the first conversion furnace 5 to 280°C - 310°C. The carbon monoxide and water vapor in the first conversion gas undergo a shift reaction and generate heat simultaneously. The space velocity of the shift reaction is 3200h -1 -6000h -1 , send the heat into the steam drum 4 through the heat exchanger 41 and the second outlet pipe 20. The self-pipeline network 43 sends water to the steam drum 4 through the first water supply pipe 24. Steam at 5.8MPa - 7MPa will be generated in the steam drum 4. Send a part of the steam into the gas preheater 2 to continue participating in preheating, and the rest of the steam is collected through the exhaust pipe 22. Measure the temperature of the first conversion gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the first conversion gas is not more than 2.34mol% and the temperature of the mixed gas reaches 270°C - 310°C, generate the second conversion gas, and send the second conversion gas into the water spraying section of the second conversion furnace 6. At the same time, the self-pipeline network 43 provides water spraying through the third water supply pipe 34; Step 3: Set the bed temperature of the second conversion furnace 6 to 240°C - 300°C. Cool down and humidify by water spraying to make the temperature of the second conversion gas reach 230°C - 250°C. Send the second conversion gas into the catalyst section of the second conversion furnace 6. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is provided in the catalyst section of the second conversion furnace 6. The second conversion gas undergoes a shift reaction and generates heat. The space velocity of the shift reaction is 3200h -1 -6000h -1 , measure the temperature of the second conversion gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the second conversion gas is not more than 1% and the temperature of the mixed gas reaches 210°C - 240°C, generate the third conversion gas, and send the third conversion gas into the water spraying section of the third conversion furnace 7. At the same time, the self-pipeline network 43 provides water spraying through the fourth water supply pipe 36; Step 4: Set the bed temperature of the third conversion furnace 7 to 220°C - 270°C. Cool down and humidify by water spraying to make the temperature of the third conversion gas reach 220°C. Send the third conversion gas into the catalyst section of the third conversion furnace 7. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is provided in the catalyst section of the third conversion furnace 7. The third conversion gas undergoes a shift reaction. The space velocity of the shift reaction is 3200h -1 -6000h-1 , measure the temperature of the third converted gas and the dry-based content of carbon monoxide. When the dry-based content of carbon monoxide in the third converted gas is not more than 0.6% and the temperature of the mixed gas reaches 223 °C, generate the fourth converted gas and introduce the fourth converted gas into the waste heat boiler 8; Step 5: Cool the fourth converted gas to 168 °C - 172 °C by the steam condensate of the waste heat boiler 8, collect the by-product steam of 0.5 MPa through the third outlet pipe 42, introduce the fourth converted gas into the demineralized water heater 9 to further cool it to 75 °C, and then introduce the fourth converted gas into the water cooler 10 to cool it to 40 °C. Send water from the pipe network 43 to the inlet of the water cooler 10 through the second water supply pipe 35 to wash the dissolved salt. Pressurize the steam condensate of the waste heat boiler 8 to 7.8 MPa by the condensate pump 32 and then send it to the ammonia washing tower 11. Introduce the fourth converted gas into the ammonia washing tower 11 to perform gas-liquid separation, steam condensate ammonia washing, and methanol cleaning in sequence, and collect the generated hydrogen through the first outlet pipe 19.

[0022] The QBS-02 sulfur-tolerant conversion protective agent can be used in combination with the cobalt-molybdenum-based sulfur-tolerant wide-temperature carbon monoxide conversion catalyst. It not only has high strength but also high porosity, has certain organic sulfur hydrolysis performance itself, can extend the service life of the cobalt-molybdenum-based sulfur-tolerant wide-temperature carbon monoxide conversion catalyst. When in use, only raise the temperature to the operating conditions, no reduction sulfidation is required, and it does not contain substances harmful to equipment and the human body.

[0023] Example 1: Syngas hydrogen production device, including a gas-water separator 1, a coal gas preheater 2, an autothermal purification furnace 3, a first converter 5, a second converter 6, a third converter 7, a waste heat boiler 8, a desalted water heater 9, a water cooler 10, and an ammonia washing tower 11 connected in sequence through a number of pipelines. The ammonia washing tower 11 is connected with a first gas outlet pipe 19. The first converter 5 is connected with a steam drum 4 through a second gas outlet pipe 20. The steam drum 4 is connected with the coal gas preheater 2 through a return pipe 21. A first connecting pipe 23 is connected between the autothermal purification furnace 3 and the gas-water separator 1. The waste heat boiler 8 is connected with a condensate pipe 31. A water inlet pipe 46 is connected between the desalted water heater 9 and the ammonia washing tower 11. The gas-water separator 1 is connected with a gas inlet pipe 18. A condensate pump 32 is arranged on the condensate pipe 31. The steam drum 4 is connected with a first water supply pipe 24. A fifth regulating valve 37 is arranged on the first water supply pipe 24. The water cooler 10 is connected with a second water supply pipe 35. A sixth regulating valve 39 is arranged on the second water supply pipe 35. The second converter 6 is connected with a third water supply pipe 34. A seventh regulating valve 38 is arranged on the third water supply pipe 34. The third converter 7 is connected with a fourth water supply pipe 36. An eighth regulating valve 33 is arranged on the fourth water supply pipe 36. The first water supply pipe 24, the second water supply pipe 35, the third water supply pipe 34, and the fourth water supply pipe 36 are jointly connected with a self-pipeline network 43. A first regulating valve 14 is arranged on each pipeline. A second regulating valve 28 is arranged on the first connecting pipe 23. A third regulating valve 29 is arranged on the return pipe 21. A pressure regulating valve 30 is arranged on the second gas outlet pipe 20.

[0024] Example 2: Syngas hydrogen production device, including a gas-water separator 1, a coal gas preheater 2, an autothermal purification furnace 3, a first converter 5, a second converter 6, a third converter 7, a waste heat boiler 8, a desalted water heater 9, a water cooler 10, and an ammonia washing tower 11 connected in sequence through a number of pipelines. The ammonia washing tower 11 is connected with a first gas outlet pipe 19. The first converter 5 is connected with a steam drum 4 through a second gas outlet pipe 20. The steam drum 4 is connected with the coal gas preheater 2 through a return pipe 21. A first connecting pipe 23 is connected between the autothermal purification furnace 3 and the gas-water separator 1. The waste heat boiler 8 is connected with a condensate pipe 31. A water inlet pipe 46 is connected between the desalted water heater 9 and the ammonia washing tower 11. The gas-water separator 1 is connected with a gas inlet pipe 18. A condensate pump 32 is arranged on the condensate pipe 31. The steam drum 4 is connected with a first water supply pipe 24. A fifth regulating valve 37 is arranged on the first water supply pipe 24. The water cooler 10 is connected with a second water supply pipe 35. A sixth regulating valve 39 is arranged on the second water supply pipe 35. The second converter 6 is connected with a third water supply pipe 34. A seventh regulating valve 38 is arranged on the third water supply pipe 34. The third converter 7 is connected with a fourth water supply pipe 36. An eighth regulating valve 33 is arranged on the fourth water supply pipe 36. The first water supply pipe 24, the second water supply pipe 35, the third water supply pipe 34, and the fourth water supply pipe 36 are jointly connected with a self-pipeline network 43. A first regulating valve 14 is arranged on each pipeline. A second regulating valve 28 is arranged on the first connecting pipe 23. A third regulating valve 29 is arranged on the return pipe 21. A pressure regulating valve 30 is arranged on the second gas outlet pipe 20. An exhaust pipe 22 is connected to the pipeline of the return pipe 21 between the third regulating valve 29 and the coal gas preheater 2. A fourth regulating valve 15 is arranged on the exhaust pipe 22. The steam drum 4 is connected with a first chemical dosing device 12 through a second connecting pipe 26. A first metering pump 13 is arranged on the second connecting pipe 26. The waste heat boiler 8 is connected with a second chemical dosing device 16 through a third connecting pipe 27. A second metering pump 17 is arranged on the third connecting pipe 27.

[0025] Example 3: Syngas hydrogen production device, including a gas-water separator 1, a coal gas preheater 2, an autothermal purification furnace 3, a first converter 5, a second converter 6, a third converter 7, a waste heat boiler 8, a desalted water heater 9, a water cooler 10, and an ammonia washing tower 11 connected in sequence through several pipelines. The ammonia washing tower 11 is connected with a first gas outlet pipe 19. The first converter 5 is connected with a steam drum 4 through a second gas outlet pipe 20. The steam drum 4 is connected with the coal gas preheater 2 through a reflux pipe 21. A first connecting pipe 23 is connected between the autothermal purification furnace 3 and the gas-water separator 1. The waste heat boiler 8 is connected with a condensate pipe 31. A water inlet pipe 46 is connected between the desalted water heater 9 and the ammonia washing tower 11. The gas-water separator 1 is connected with an inlet gas pipe 18. A condensate pump 32 is arranged on the condensate pipe 31. The steam drum 4 is connected with a first water supply pipe 24. A fifth regulating valve 37 is arranged on the first water supply pipe 24. The water cooler 10 is connected with a second water supply pipe 35. A sixth regulating valve 39 is arranged on the second water supply pipe 35. The second converter 6 is connected with a third water supply pipe 34. A seventh regulating valve 38 is arranged on the third water supply pipe 34. The third converter 7 is connected with a fourth water supply pipe 36. An eighth regulating valve 33 is arranged on the fourth water supply pipe 36. The first water supply pipe 24, the second water supply pipe 35, the third water supply pipe 34, and the fourth water supply pipe 36 are jointly connected with a self-pipeline network 43. A first regulating valve 14 is arranged on each pipeline. A second regulating valve 28 is arranged on the first connecting pipe 23. A third regulating valve 29 is arranged on the reflux pipe 21. A pressure regulating valve 30 is arranged on the second gas outlet pipe 20. The first converter 5 is a temperature-controlled converter. The second converter 6 and the third converter 7 are both axial-radial converters. The desalted water heater 9 is connected with a fourth water outlet pipe 25. A fifth connecting pipe 40 is connected between the coal gas preheater 2 and the waste heat boiler 8. A heat exchanger 41 is arranged in the first converter 5. The heat exchanger 41 is connected with the second gas outlet pipe 20. The waste heat boiler 8 is respectively connected with a third gas outlet pipe 42 and a water supply pipe 45. A ninth regulating valve 44 is arranged on the water supply pipe 45. Example 4: Syngas hydrogen production method, including the following steps: Step 1: Send the syngas through the inlet gas pipe 18 to the gas-water separator 1. The gas-water separator 1 separates the liquid water. Adjust the first regulating valve 14 and the second regulating valve 28 to send 20% of the gas into the coal gas preheater 2. Preheat the gas entering the coal gas preheater 2 to 250 °C and then send it to the catalyst section of the autothermal purification furnace 3. At the same time, the coal gas preheater 2 sends the generated steam condensate to the waste heat boiler 8 through the fifth connecting pipe 40. Control the temperature of the autothermal purification furnace 3 at 350 °C. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant conversion catalyst is arranged in the catalyst section of the autothermal purification furnace 3. The gas undergoes a conversion reaction under the action of the cobalt-molybdenum catalyst. The space velocity of the conversion reaction is 3200 h -1, generate conversion gas, and simultaneously introduce the conversion gas and the remaining gas in the gas-water separator 1 into the detoxification section of the autothermal purification furnace 3. The detoxification section is provided with a detoxifying agent, which is the QBS-02 sulfur-resistant shift protective agent. Through the detoxifying agent, carbon black, oxygen, tar, dust, arsenic, phosphorus, and chlorine are removed. The autothermal purification furnace 3 preheats the mixed gas to 255 °C to generate the first conversion gas; Step 2: Feed the first conversion gas into the catalyst section of the first conversion furnace 5. The water-gas ratio in the first conversion gas is 0.2. A cobalt-molybdenum-based wide-temperature sulfur-resistant shift catalyst is provided in the catalyst section of the first conversion furnace 5. Set the bed temperature of the first conversion furnace 5 to 280 °C. The carbon monoxide and water vapor in the first conversion gas undergo a shift reaction and generate heat simultaneously. The space velocity of the shift reaction is 3200 h -1 , send the heat into the steam drum 4 through the heat exchanger 41 and the second outlet pipe 20. The self-pipeline network 43 sends water to the steam drum 4 through the first water supply pipe 24. Steam at 5.8 MPa will be generated in the steam drum 4. Send a part of the steam into the gas preheater 2 to continue to participate in preheating, and the remaining steam is collected through the exhaust pipe 22. Measure the temperature of the first conversion gas and the dry-base content of carbon monoxide. When the dry-base content of carbon monoxide in the first conversion gas is not more than 2.34 mol% and the temperature of the mixed gas reaches 270 °C, generate the second conversion gas, and feed the second conversion gas into the water spraying section of the second conversion furnace 6. At the same time, the self-pipeline network 43 provides water spraying through the third water supply pipe 34; Step 3: Set the bed temperature of the second conversion furnace 6 to 240 °C, and cool down and humidify by spraying water to make the temperature of the second conversion gas reach 230 °C. Feed the second conversion gas into the catalyst section of the second conversion furnace 6. A cobalt-molybdenum-based wide-temperature sulfur-resistant shift catalyst is provided in the catalyst section of the second conversion furnace 6. The second conversion gas undergoes a shift reaction and generates heat. The space velocity of the shift reaction is 3200 h -1 , measure the temperature of the second conversion gas and the dry-base content of carbon monoxide. When the dry-base content of carbon monoxide in the second conversion gas is not more than 1% and the temperature of the mixed gas reaches 210 °C, generate the third conversion gas, and feed the third conversion gas into the water spraying section of the third conversion furnace 7. At the same time, the self-pipeline network 43 provides water spraying through the fourth water supply pipe 36; Step 4: Set the bed temperature of the third conversion furnace 7 to 220 °C, and cool down and humidify by spraying water to make the temperature of the third conversion gas reach 220 °C. Feed the third conversion gas into the catalyst section of the third conversion furnace 7. A cobalt-molybdenum-based wide-temperature sulfur-resistant shift catalyst is provided in the catalyst section of the third conversion furnace 7. The third conversion gas undergoes a shift reaction. The space velocity of the shift reaction is 3200 h -1 , measure the temperature of the third conversion gas and the dry-base content of carbon monoxide. When the dry-base content of carbon monoxide in the third conversion gas is not more than 0.6% and the temperature of the mixed gas reaches 223 °C, generate the fourth conversion gas, and feed the fourth conversion gas into the waste heat boiler 8; Step 5: The fourth converted gas is cooled to 168°C by the steam condensate of the waste heat boiler 8, the by-product steam of 0.5 MPa is collected through the third outlet pipe 42, the fourth converted gas is further cooled to 75°C by passing through the demineralized water heater 9, and then the fourth converted gas is cooled to 40°C by passing through the water cooler 10. Water is sent from the pipe network 43 to the inlet of the water cooler 10 through the second water supply pipe 35 to wash and dissolve salts. The steam condensate of the waste heat boiler 8 is pressurized to 7.8 MPa by the condensate pump 32 and then sent to the ammonia washing tower 11. The fourth converted gas is sent into the ammonia washing tower 11 for gas-liquid separation, steam condensate ammonia washing, and methanol cleaning in sequence, and the generated hydrogen is collected through the first outlet pipe 19.

[0026] Example 5: A method for producing hydrogen from syngas, comprising the following steps: Step 1: The syngas is sent to the gas-water separator 1 through the inlet pipe 18. The gas-water separator 1 separates the liquid water. 25% of the gas is sent into the gas preheater 2 by adjusting the first regulating valve 14 and the second regulating valve 28. The gas entering the gas preheater 2 is preheated to 258°C and then sent to the catalyst section of the autothermal purification furnace 3. At the same time, the gas preheater 2 sends the generated steam condensate to the waste heat boiler 8 through the fifth connecting pipe 40. The temperature of the autothermal purification furnace 3 is controlled at 375°C. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant conversion catalyst is provided in the catalyst section of the autothermal purification furnace 3. The gas undergoes a conversion reaction under the action of the cobalt-molybdenum catalyst. The space velocity of the conversion reaction is 4600 h -1 , generating converted gas. The converted gas and the remaining gas of the gas-water separator 1 are simultaneously sent into the detoxification section of the autothermal purification furnace 3. A detoxifying agent is provided in the detoxification section. The detoxifying agent is QBS-02 sulfur-tolerant conversion protective agent. Carbon black, oxygen, tar, dust, arsenic, and phosphorus and chlorine are removed through the detoxifying agent. The autothermal purification furnace 3 preheats the mixed gas to 265°C, generating the first converted gas; Step 2: The first converted gas is sent into the catalyst section of the first conversion furnace 5. The water-gas ratio in the first converted gas is 0.7. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant conversion catalyst is provided in the catalyst section of the first conversion furnace 5. The bed temperature of the first conversion furnace 5 is set at 295°C. Carbon monoxide and steam in the first converted gas undergo a conversion reaction and generate heat at the same time. The space velocity of the conversion reaction is 4600 h -1, heat is sent into the steam drum 4 through the heat exchanger 41 and the second outlet pipe 20, water is sent to the steam drum 4 from the pipe network 43 through the first water supply pipe 24, steam at 6.4 MPa is generated in the steam drum 4, a part of the steam is introduced into the gas preheater 2 to continue participating in preheating, and the rest of the steam is collected through the exhaust pipe 22. Measure the temperature of the first converted gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the first converted gas is not more than 2.34 mol% and the temperature of the mixed gas reaches 290 °C, the second converted gas is generated. The second converted gas is introduced into the water spraying section of the second conversion furnace 6, and at the same time, water spraying is provided from the pipe network 43 through the third water supply pipe 34; Step 3: Set the bed temperature of the second conversion furnace 6 to 270 °C, cool down and humidify by spraying water to make the temperature of the second converted gas reach 240 °C, introduce the second converted gas into the catalyst section of the second conversion furnace 6. A cobalt-molybdenum-based sulfur-tolerant wide-temperature carbon monoxide conversion catalyst is arranged in the catalyst section of the second conversion furnace 6. The second converted gas undergoes a conversion reaction and generates heat. The space velocity of the conversion reaction is 4600 h -1 , measure the temperature of the second converted gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the second converted gas is not more than 1% and the temperature of the mixed gas reaches 225 °C, the third converted gas is generated. The third converted gas is introduced into the water spraying section of the third conversion furnace 7, and at the same time, water spraying is provided from the pipe network 43 through the fourth water supply pipe 36; Step 4: Set the bed temperature of the third conversion furnace 7 to 245 °C, cool down and humidify by spraying water to make the temperature of the third converted gas reach 220 °C, introduce the third converted gas into the catalyst section of the third conversion furnace 7. A cobalt-molybdenum-based sulfur-tolerant wide-temperature carbon monoxide conversion catalyst is arranged in the catalyst section of the third conversion furnace 7. The third converted gas undergoes a conversion reaction. The space velocity of the conversion reaction is 4600 h -1 , measure the temperature of the third converted gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the third converted gas is not more than 0.6% and the temperature of the mixed gas reaches 223 °C, the fourth converted gas is generated. The fourth converted gas is introduced into the waste heat boiler 8; Step 5: The fourth converted gas is cooled to 170 °C by the steam condensate of the waste heat boiler 8, the by-product steam at 0.5 MPa is collected through the third outlet pipe 42, the fourth converted gas is introduced into the demineralized water heater 9 to be further cooled to 75 °C, and then the fourth converted gas is introduced into the water cooler 10 to be cooled to 40 °C. Water is sent to the inlet of the water cooler 10 from the pipe network 43 through the second water supply pipe 35 to wash and dissolve salts. The steam condensate of the waste heat boiler 8 is pressurized to 7.8 MPa by the condensate pump 32 and then sent into the ammonia washing tower 11. The fourth converted gas is introduced into the ammonia washing tower 11 for gas-liquid separation, steam condensate ammonia washing, and methanol cleaning in sequence, and the generated hydrogen is collected through the first outlet pipe 19.

[0027] Example 6: A method for producing hydrogen from syngas, comprising the following steps: Step 1: Feed the syngas through the inlet pipe 18 to the gas-water separator 1. The gas-water separator 1 separates the liquid water and sends 30% of the gas into the coal gas preheater 2 by adjusting the first regulating valve 14 and the second regulating valve 28. The gas entering the coal gas preheater 2 is preheated to 265°C and then sent to the catalyst section of the autothermal purification furnace 3. At the same time, the steam condensate generated by the coal gas preheater 2 is sent to the waste heat boiler 8 through the fifth connecting pipe 40. Control the temperature of the autothermal purification furnace 3 at 400°C. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is provided in the catalyst section of the autothermal purification furnace 3. The gas undergoes a shift reaction under the action of the cobalt-molybdenum catalyst. The space velocity of the shift reaction is 6000 h -1 , generating converted gas. The converted gas and the remaining gas in the gas-water separator 1 are simultaneously introduced into the detoxification section of the autothermal purification furnace 3. A detoxifying agent is provided in the detoxification section. The detoxifying agent is QBS-02 sulfur-tolerant shift protective agent. Carbon black, oxygen, tar, dust, arsenic, phosphorus, and chlorine are removed by the detoxifying agent. The autothermal purification furnace 3 preheats the mixed gas to 275°C, generating the first converted gas; Step 2: Feed the first converted gas into the catalyst section of the first conversion furnace 5. The water-gas ratio in the first converted gas is 1.2. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is provided in the catalyst section of the first conversion furnace 5. Set the bed temperature of the first conversion furnace 5 to 310°C. Carbon monoxide and steam in the first converted gas undergo a shift reaction and generate heat at the same time. The space velocity of the shift reaction is 6000 h -1 , and the heat is sent to the steam drum 4 through the heat exchanger 41 and the second outlet pipe 20. Water is sent from the pipe network 43 to the steam drum 4 through the first water supply pipe 24. Steam at 7 MPa is generated in the steam drum 4. Part of the steam is introduced into the coal gas preheater 2 to continue participating in the preheating, and the remaining steam is collected through the exhaust pipe 22. Measure the temperature of the first converted gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the first converted gas is not more than 2.34 mol% and the temperature of the mixed gas reaches 310°C, the second converted gas is generated. The second converted gas is introduced into the water spraying section of the second conversion furnace 6, and at the same time, the pipe network 43 provides water spraying through the third water supply pipe 34; Step 3: Set the bed temperature of the second conversion furnace 6 to 300°C. Cool and humidify by spraying water to make the temperature of the second converted gas reach 250°C. Feed the second converted gas into the catalyst section of the second conversion furnace 6. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is provided in the catalyst section of the second conversion furnace 6. The second converted gas undergoes a shift reaction and generates heat. The space velocity of the shift reaction is 6000 h -1, measure the temperature of the second converted gas and the dry-base content of carbon monoxide. When the dry-base content of carbon monoxide in the second converted gas is not more than 1% and the temperature of the mixed gas reaches 240 °C, the third converted gas is generated. The third converted gas is introduced into the water spraying section of the third conversion furnace 7, and at the same time, water spraying is provided through the fourth water supply pipe 36 from the pipe network 43; Step 4: Set the bed temperature of the third conversion furnace 7 to 270 °C, and cool and humidify by water spraying to make the temperature of the third converted gas reach 220 °C. The third converted gas is introduced into the catalyst section of the third conversion furnace 7. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant conversion catalyst is provided in the catalyst section of the third conversion furnace 7. The third converted gas undergoes a conversion reaction, and the conversion reaction space velocity is 6000 h -1 , measure the temperature of the third converted gas and the dry-base content of carbon monoxide. When the dry-base content of carbon monoxide in the third converted gas is not more than 0.6% and the temperature of the mixed gas reaches 223 °C, the fourth converted gas is generated. The fourth converted gas is introduced into the waste heat boiler 8; Step 5: The fourth converted gas is cooled to 172 °C by the steam condensate of the waste heat boiler 8. The by-product steam of 0.5 MPa is collected through the third outlet pipe 42. The fourth converted gas is introduced into the desalted water heater 9 to be further cooled to 75 °C, and then the fourth converted gas is introduced into the water cooler 10 to be cooled to 40 °C. Water is sent from the pipe network 43 through the second water supply pipe 35 to the inlet of the water cooler 10 to wash and dissolve salts. The steam condensate of the waste heat boiler 8 is pressurized to 7.8 MPa by the condensate pump 32 and then sent to the ammonia washing tower 11. The fourth converted gas is introduced into the ammonia washing tower 11 for gas-liquid separation, steam condensate ammonia washing, and methanol cleaning in sequence, and the generated hydrogen is collected through the first outlet pipe 19.

Claims

1. A syngas-to-hydrogen production device, characterized in that, It includes a gas-water separator (1), a gas preheater (2), an autothermal purification furnace (3), a first converter (5), a second converter (6), a third converter (7), a waste heat boiler (8), a demineralized water heater (9), a water cooler (10), and an ammonia washing tower (11) connected in sequence through a number of pipelines. The ammonia washing tower (11) is connected with a first gas outlet pipe (19). The first converter (5) is connected with a steam drum (4) through a second gas outlet pipe (20). The steam drum (4) is connected with the gas preheater (2) through a reflux pipe (21). A first connecting pipe (23) is connected between the autothermal purification furnace (3) and the gas-water separator (1). The waste heat boiler (8) is connected with a condensate pipe (31). A water inlet pipe (46) is connected between the demineralized water heater (9) and the ammonia washing tower (11). The gas-water separator (1) is connected with a gas inlet pipe (18).

2. The syngas hydrogen production device according to claim 1, characterized in that A condensate pump (32) is arranged on the condensate pipe (31). The steam drum (4) is connected with a first water supply pipe (24). A fifth regulating valve (37) is arranged on the first water supply pipe (24). The water cooler (10) is connected with a second water supply pipe (35). A sixth regulating valve (39) is arranged on the second water supply pipe (35). The second converter (6) is connected with a third water supply pipe (34). A seventh regulating valve (38) is arranged on the third water supply pipe (34). The third converter (7) is connected with a fourth water supply pipe (36). An eighth regulating valve (33) is arranged on the fourth water supply pipe (36). The first water supply pipe (24), the second water supply pipe (35), the third water supply pipe (34), and the fourth water supply pipe (36) are jointly connected with a self-pipeline network (43). A first regulating valve (14) is arranged on each pipeline. A second regulating valve (28) is arranged on the first connecting pipe (23). A third regulating valve (29) is arranged on the reflux pipe (21). A pressure regulating valve (30) is arranged on the second gas outlet pipe (20).

3. The syngas hydrogen production device according to claim 2, characterized in that, An exhaust pipe (22) is connected to the pipeline of the reflux pipe (21) between the third regulating valve (29) and the gas preheater (2). A fourth regulating valve (15) is arranged on the exhaust pipe (22). The steam drum (4) is connected with a first chemical dosing device (12) through a second connecting pipe (26). A first metering pump (13) is arranged on the second connecting pipe (26). The waste heat boiler (8) is connected with a second chemical dosing device (16) through a third connecting pipe (27). A second metering pump (17) is arranged on the third connecting pipe (27).

4. The syngas hydrogen production device according to any one of claims 1-3, characterized in that, The first converter (5) is a temperature-controlled converter. The second converter (6) and the third converter (7) are both axial-radial converters. The demineralized water heater (9) is connected with a fourth water outlet pipe (25). A fifth connecting pipe (40) is connected between the gas preheater (2) and the waste heat boiler (8). A heat exchanger (41) is arranged in the first converter (5). The heat exchanger (41) is connected with the second gas outlet pipe (20). The waste heat boiler (8) is respectively connected with a third gas outlet pipe (42) and a water supply pipe (45). A ninth regulating valve (44) is arranged on the water supply pipe (45).

5. A method for producing hydrogen from syngas, characterized in that, Using the syngas hydrogen production device described in claim 4, the following steps are included: Step 1: Feed the syngas into the gas-water separator (1) to separate the liquid water. Part of the gas is preheated by the coal gas preheater (2) and then sent to the autothermal purification furnace (3), and the remaining gas is directly introduced into the autothermal purification furnace (3) to remove impurities and preheat the mixed gas, generating the first shifted gas. Step 2: Feed the first shifted gas into the first shift furnace (5) for a shift reaction to generate the second shifted gas. Step 3: Send the second shifted gas into the second shift furnace (6) for temperature reduction, humidity increase, and a shift reaction to generate the third shifted gas. Step 4: Carry out temperature reduction, humidity increase, and a shift reaction on the third shifted gas in the third shift furnace (7) to generate the fourth shifted gas. Step 5: Cool the fourth shifted gas successively through the waste heat boiler (8), the demineralized water heater (9), and the water cooler (10), and then carry out gas-liquid separation, ammonia washing, and methanol cleaning in the ammonia washing tower (11) to collect hydrogen.

6. The method for producing hydrogen from syngas according to claim 5, characterized in that, The specific implementation of Step 1 is carried out according to the following steps: Step 1.1: Feed the syngas through the inlet pipe (18) to the gas-water separator (1). The gas-water separator (1) separates the liquid water, and 20%-30% of the gas is sent to the coal gas preheater (2) by adjusting the first regulating valve (14) and the second regulating valve (28). Step 1.2: Preheat the gas entering the coal gas preheater (2) to 250°C - 265°C and then send it to the catalyst section of the autothermal purification furnace (3). At the same time, the steam condensate generated by the coal gas preheater (2) is sent to the waste heat boiler (8) through the fifth connecting pipe (40). Step 1.3, control the temperature of the autothermal purification furnace (3) at 350°C - 400°C. A cobalt-molybdenum-based sulfur-tolerant shift catalyst for wide temperature range is provided in the catalyst section of the autothermal purification furnace (3). The gas undergoes a shift reaction under the action of the cobalt-molybdenum catalyst, and the space velocity of the shift reaction is 3200 h -1 -1 -1 -6000 h to generate converted gas. The converted gas and the remaining gas in the gas-water separator (1) are simultaneously introduced into the detoxification section of the autothermal purification furnace (3). A detoxifying agent is provided in the detoxification section, and the detoxifying agent is QBS-02 sulfur-tolerant shift protective agent. Carbon black, oxygen, tar, dust, arsenic, phosphorus, and chlorine are removed through the detoxifying agent. The autothermal purification furnace (3) preheats the mixed gas to 255°C - 275°C to generate the first converted gas.

7. The method for producing hydrogen from syngas according to claim 6, wherein The specific implementation of Step 2 is carried out according to the following steps: Step 2.1: Feed the first shifted gas into the catalyst section of the first shift furnace (5). The steam-gas ratio in the first shifted gas is 0.2 - 1.

2. A cobalt-molybdenum-based carbon monoxide wide-temperature sulfur-tolerant shift catalyst is provided in the catalyst section of the first shift furnace (5), and the bed temperature of the first shift furnace (5) is set to 280°C - 310°C. Step 2.2, carbon monoxide and steam in the first shift gas undergo a shift reaction, generating heat simultaneously. The space velocity of the shift reaction is 3200 h -1 -6000 h -1 . The heat is sent into the steam drum (4) through the heat exchanger (41) and the second outlet pipe (20). Water is sent to the steam drum (4) from the pipe network (43) through the first water supply pipe (24). Steam at 5.8 MPa - 7 MPa is generated in the steam drum (4). Part of the steam is introduced into the gas preheater (2) to continue participating in preheating, and the remaining steam is collected through the exhaust pipe (22); Step 2.3: Measure the temperature of the first shifted gas and the dry-base content of carbon monoxide. When the dry-base content of carbon monoxide in the first shifted gas is not more than 2.34 mol% and the temperature of the mixed gas reaches 270°C - 310°C, generate the second shifted gas, and introduce the second shifted gas into the water spraying section of the second shift furnace (6). At the same time, water spraying is provided from the pipe network (43) through the third water supply pipe (34).

8. The method for producing hydrogen from syngas according to claim 7, wherein The specific implementation of Step 3 is carried out according to the following steps: Step 3.1: Set the bed temperature of the second shift furnace (6) to 240°C - 300°C, cool and humidify the second shifted gas by water spraying to make the temperature of the second shifted gas reach 230°C - 250°C, and introduce the second shifted gas into the catalyst section of the second shift furnace (6). Step 3.2, a cobalt-molybdenum-based sulfur-tolerant shift catalyst with a wide temperature range is provided in the catalyst section of the second shift converter (6). The second shift gas undergoes a shift reaction and generates heat. The space velocity of the shift reaction is 3200 h -1 -6000 h -1 . Measure the temperature of the second shift gas and the dry basis content of carbon monoxide. When the dry basis content of carbon monoxide in the second shift gas is not more than 1% and the temperature of the mixed gas reaches 210°C - 240°C, the third shift gas is generated. The third shift gas is introduced into the water spraying section of the third shift converter (7), and at the same time, water spraying is provided from the pipe network (43) through the fourth water supply pipe (36).

9. The method for producing hydrogen from syngas according to claim 8, wherein The specific implementation of Step 4 is carried out according to the following steps: Step 4.1, set the bed temperature of the third shift converter (7) to 220°C - 270°C, cool down and humidify by spraying water to make the temperature of the third shifted gas reach 220°C, and introduce the third shifted gas into the catalyst section of the third shift converter (7). A cobalt-molybdenum based sulfur-tolerant shift catalyst for wide temperature range of carbon monoxide is set in the catalyst section of the third shift converter (7). The third shifted gas undergoes a shift reaction, and the space velocity of the shift reaction is 3200h -1 -6000h -1 ; Step 4.2: Measure the temperature of the third shifted gas and the dry-base content of carbon monoxide. When the dry-base content of carbon monoxide in the third shifted gas is not more than 0.6% and the temperature of the mixed gas reaches 223°C, generate the fourth shifted gas, and introduce the fourth shifted gas into the waste heat boiler (8).

10. The method for producing hydrogen from syngas according to claim 9, wherein The specific implementation of Step 5 is carried out according to the following steps: Step 5.1, the fourth converted gas is cooled to 168°C - 172°C by the steam condensate of the waste heat boiler (8), and the by-product steam of 0.5 MPa is collected through the third outlet pipe (42); Step 5.2, the fourth converted gas is further cooled to 75°C by passing it through the demineralized water heater (9), and then the fourth converted gas is cooled to 40°C by passing it through the water cooler (10). Water is sent from the pipe network (43) to the inlet of the water cooler (10) through the second water supply pipe (35) to wash the dissolved salts; Step 5.3, the steam condensate of the waste heat boiler (8) is pressurized to 7.8 MPa by the condensate pump (32) and then sent to the ammonia washing tower (11). The fourth converted gas is passed into the ammonia washing tower (11) for gas-liquid separation, steam condensate ammonia washing, and methanol cleaning in sequence, and the generated hydrogen is collected through the first outlet pipe (19).

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