System and process for producing synthesis gas by coupling high-temperature gas cooled reactor with CO2 dry reforming and biomass gasification

Abstract

A high-temperature gas cooled reactor coupled CO2 dry reforming and biomass gasification synthesis gas production system comprises a high-temperature gas cooled reactor, a CO2 dry reforming device, a biomass gasification synthesis gas production device, pipelines and a heat exchanger, and the heat exchanger comprises a pipeline I and a pipeline II; the CO2 dry reforming device comprises a raw material preheater and a CO2 dry reforming reactor which are communicated with each other; the raw material preheater comprises a preheated gas pipeline and a reaction gas pipeline; the device for producing the synthesis gas through biomass gasification comprises a biomass gasification reactor, an acid gas remover and a gas separator, an outlet of the reactor is communicated with an inlet of the acid gas remover, the acid gas remover comprises an outlet I and an outlet II, the outlet I is communicated with an inlet of the gas separator, and the gas separator comprises an outlet IV; the outlet II is communicated with the reaction gas pipeline through a pipeline I; the outlet IV is communicated with the reaction gas pipeline through a pipeline II; gas I generated in the high-temperature gas cooled reactor enters the preheated gas pipeline from the pipeline I; and gas II discharged from the preheating pipeline returns to the high-temperature gas cooled reactor.

Description

Technical Field

[0001] The present invention relates to the technical field of energy conservation and emission reduction, and in particular to a system and process for producing synthesis gas by coupling CO2 dry reforming and biomass gasification with a high-temperature gas-cooled reactor. Background Art

[0002] At present, the development of the coal chemical industry is facing great pressure to reduce carbon emissions. How to improve energy efficiency and reduce resource consumption; how to deeply couple with new technologies such as new energy to reduce carbon emissions are issues facing the development of the coal chemical industry.

[0003] In order to achieve the goal of carbon emission reduction, the reforming reaction of methane and carbon dioxide is one of the effective means. The methane carbon dioxide reforming reaction converts the two main greenhouse gases, methane (CH4) and carbon dioxide (CO2), into synthesis gas (H2 and CO). While reducing carbon emissions and mitigating the greenhouse effect, it also provides an efficient, pollution-free clean energy hydrogen. Therefore, this reaction has extremely important research value and potential industrial application. In addition, compared with traditional steam reforming, the synthesis gas produced by this technology has a lower hydrogen-carbon ratio and is more suitable for processes such as Fischer-Tropsch synthesis and carbonyl synthesis.

[0004] In addition, as one of the most promising solutions in the fourth-generation nuclear power system, the high-temperature gas-cooled reactor has the advantages of outstanding safety features, high outlet temperature and modular system. It can not only generate electricity safely and efficiently, but also be widely used in non-electric fields such as high-temperature process heating and nuclear desalination. At the same time, it can provide high-temperature process heat, providing technical support for the wider application of nuclear energy. In the high-temperature gas-cooled reactor, helium is an ideal heat transfer medium with its excellent heat transfer characteristics and chemical inertness. The core outlet temperature of the high-temperature gas-cooled reactor is 700-1000℃, making nuclear hydrogen production technology possible. The high-temperature gas-cooled reactor is conducive to achieving clean energy transformation and reducing carbon emissions from fossil fuels in industries, transportation and heating.

[0005] Biomass energy is a clean energy source. The content of harmful substances (sulfur and ash, etc.) in biomass is only about 1 / 10 of that in coal. At the same time, the emission and absorption of carbon dioxide by biomass constitutes the carbon cycle in nature. Its energy utilization can almost achieve zero carbon dioxide emissions. Biomass gasification technology has gradually become one of the most efficient and practical methods for biomass energy conversion and utilization. Therefore, increasing the development and utilization of biomass energy plays an important role in improving energy utilization efficiency, reducing greenhouse gas emissions, protecting the environment, and achieving sustainable development.

[0006] Based on this, there is an urgent need in the prior art to provide a new advanced green carbon reduction process and system. Summary of the invention

[0007] In order to solve the above problems in the prior art, the present invention proposes a system and process for producing synthesis gas by coupling CO2 dry reforming and biomass gasification with a high temperature gas-cooled reactor.

[0008] In the first aspect, the present invention proposes a system for producing synthesis gas by coupling CO2 dry reforming and biomass gasification with a high temperature gas-cooled reactor.

[0009] Including high temperature gas-cooled reactor, CO2 dry reforming unit and biomass gasification production synthesis gas unit, pipelines and heat exchangers;

[0010] Pipe I and pipeline II are arranged inside the heat exchanger;

[0011] Specifically, the heat exchanger can be selected from one of a tubular heat exchanger, a plate heat exchanger, and a fin heat exchanger.

[0012] The CO2 dry reforming device includes a raw material preheater and a CO2 dry reforming reactor. A preheating gas pipeline and a reaction gas pipeline are arranged inside the raw material preheater; the gas discharged from the reaction gas pipeline enters the CO2 dry reforming reactor.

[0013] Specifically, the raw material preheater is an air preheater selected from one of plate type, rotary type and tubular type.

[0014] Specifically, the CO2 dry reforming reactor is selected from one of an updraft gasification reactor, a downdraft gasification reactor, a fixed bed gasification reactor, and a fluidized bed gasification reactor.

[0015] The biomass gasification synthesis gas production device includes a biomass gasification reactor, an acid gas remover and a gas separator; the outlet of the biomass gasification reactor is connected to the inlet of the acid gas remover, the acid gas remover includes an outlet I, an outlet II and an outlet III, the outlet I is connected to the inlet of the gas separator, and the gas separator includes an outlet IV and an outlet V;

[0016] Outlet II is connected to the reaction gas pipeline through pipeline I;

[0017] The outlet IV is connected to the reaction gas pipeline through the pipeline II;

[0018] The gas I generated in the high temperature gas-cooled reactor enters the pipeline I, and enters the preheating gas pipeline after being discharged from the pipeline I;

[0019] The gas II exhausted from the preheating pipeline enters the pipeline II through the pipeline III, and after being discharged from the pipeline II, enters the high temperature gas-cooled reactor through the pipeline IV.

[0020] Specifically, the biomass gasification reactor can be selected from a fixed bed gasification reactor or a fluidized bed gasification reactor.

[0021] Specifically, the acid gas remover is used to separate the mixed gas generated in the biomass gasification reactor into impurity gas, CO2 and effective gas. The effective gas includes synthesis gas I and methane. The synthesis gas in the present invention refers to a mixed gas composed of CO and H2. The effective gas is discharged through outlet I, the CO2 gas is discharged through outlet II, and the impurity gas is discharged through outlet III. The impurity gas in the present invention mainly includes acid gases other than CO2 generated by biomass in the biomass gasification reactor.

[0022] Specifically, the acid gas remover may be an MDEA device or a low-temperature methanol wash device.

[0023] Specifically, the gas separator adopts a membrane gas separation device or a cryogenic separation device to separate methane and synthesis gas I, and methane is discharged from outlet IV, and synthesis gas I is discharged from outlet V.

[0024] As a specific embodiment of the present invention, the high temperature gas-cooled reactor coupled with CO2 dry reforming and biomass gasification to produce synthesis gas system also includes a waste heat power generation device.

[0025] The waste heat power generation device includes a steam generator, a steam turbine generator and a condenser;

[0026] The steam generator is arranged in pipeline III, pipeline III and pipeline IV are arranged inside the steam generator, water is stored in pipeline IV, gas II enters pipeline III, under the action of gas II, water in pipeline IV generates steam I and steam II, gas III is discharged from pipeline III, gas III enters pipeline II, and enters the high temperature gas-cooled reactor through pipeline IV;

[0027] Steam I enters the steam turbine generator to drive the steam turbine generator to generate electricity. Steam III discharged from the steam turbine generator enters the condenser, where steam III is condensed into liquid. The liquid discharged from the condenser enters the pipeline IV through the pipeline V.

[0028] Steam II enters the reaction gas pipeline through pipeline VI.

[0029] Preferably, the waste heat power generation device further comprises a boiler feed water pump, which is arranged in the pipeline V. The liquid discharged from the condenser enters the pipeline IV under the drive of the boiler feed water pump.

[0030] As a specific embodiment of the present invention, the CO2 dry reforming device further includes a heat recovery device, which is connected to the outlet of the CO2 dry reforming reactor and is used to recover the heat of the gas discharged from the CO2 dry reforming reactor.

[0031] Specifically, the heat recovery device can be a partition type heat exchanger, such as a tube type or a plate fin type heat exchanger.

[0032] As a specific embodiment of the present invention, the biomass gasification synthesis gas production device also includes a biomass raw material preprocessor, which is connected to the biomass gasification reactor and is used to crush, extrude and granulate the biomass.

[0033] As a specific embodiment of the present invention, the biomass gasification synthesis gas system also includes a CO converter, which is arranged between the biomass gasification reactor and the acid gas remover. The CO converter is used to adjust the molar ratio of H2 and CO in the exhaust gas in the biomass gasification reactor.

[0034] Specifically, the raw material preprocessor adopts a device in the prior art that can crush, extrude and granulate the biomass raw materials.

[0035] Specifically, the CO converter can be selected from an adiabatic CO converter or an isothermal CO converter.

[0036] Specifically, the system further includes a gas compressor, which is arranged in pipeline IV and arranged between the high temperature gas-cooled reactor and the heat exchanger. The gas compressor is used to compress the gas discharged from the heat exchanger and then pass it into the high temperature gas-cooled reactor.

[0037] Specifically, the gas compressor may be a positive displacement compressor or a centrifugal compressor.

[0038] In a second aspect, the present invention provides a process for producing synthesis gas by coupling CO2 dry reforming and biomass gasification with a high temperature gas-cooled reactor, comprising the following steps:

[0039] Step 1: Biomass reacts in a biomass gasification reactor to generate a mixed gas, which is separated into effective gas, CO2 and impurity gas by an acid gas remover. The effective gas is discharged through outlet I and enters a gas separator. The effective gas includes synthesis gas I and methane; CO2 is discharged through outlet II and enters a reaction gas pipeline; impurity gas is discharged through outlet III, and the effective gas is separated into methane and synthesis gas I by a gas separator. Methane is discharged through outlet IV and enters a reaction gas pipeline, and synthesis gas I is discharged through outlet V;

[0040] Step 2: The high temperature gas-cooled reactor generates gas I, which enters the preheater pipeline through pipeline I. Gas I preheats CO2 and methane in the reaction gas pipeline, and the preheater pipeline discharges gas II, gas II, and gas II through pipeline III and pipeline II, and then returns to the high temperature gas-cooled reactor through pipeline IV for recycling. The CO2 and methane discharged from the reaction gas pipeline enter the CO2 dry reforming reactor;

[0041] Step 3: CO2 and methane react in a CO2 dry reforming reactor to generate synthesis gas II.

[0042] As a specific embodiment of the present invention, in step 2, gas II enters pipeline III through pipeline III, and under the action of gas II, water in pipeline IV generates steam I and steam II, gas III is discharged from pipeline III, steam I enters the steam turbine generator to generate electricity, steam III discharged from the steam turbine generator enters the condenser, steam III is condensed into liquid in the condenser, and the liquid generated in the condenser enters pipeline IV for recycling;

[0043] Steam II enters the reaction gas pipeline and mixes with CO2 and methane before entering the CO2 dry reforming reactor;

[0044] Steam II enters the CO2 dry reforming reactor and participates in the CO2 dry reforming reaction to prevent the catalyst in the CO2 dry reforming reactor from being carbonized and losing its activity.

[0045] Gas III enters pipeline II, is discharged from pipeline II, and then returns to the high temperature gas-cooled reactor through pipeline IV for recycling;

[0046] Preferably, the gas discharged from pipeline III is compressed by a gas compressor and then returned to the high temperature gas-cooled reactor for recycling.

[0047] As a specific embodiment of the present invention, the liquid in the condenser is introduced into the steam generator through a boiler feed water pump.

[0048] As a specific implementation of the present invention, the synthesis gas II enters the heat recovery device, recovers heat through the heat recovery device, and is then discharged.

[0049] As a specific embodiment of the present invention, the temperature of gas I is 700-750°C, the temperature of gas II is 600-650°C, and the temperature of gas III is 200-250°C.

[0050] As a specific embodiment of the present invention, in step 2, the temperature of CO2 and methane discharged from the reaction gas pipeline is 450-500°C.

[0051] As a specific embodiment of the present invention, in step 2, the temperature of CO2, methane and steam II discharged from the reaction gas pipeline is 450-500°C.

[0052] As a specific embodiment of the present invention, in step 1, the biomass is crushed and extruded and granulated by a biomass raw material preprocessor, and then enters a biomass gasification reactor for reaction.

[0053] Specifically, the biomass in the present invention can be wood cellulose such as straw and trees other than grains and fruits in the agricultural and forestry production process, waste materials from the agricultural and forestry processing industry, and livestock manure and waste in the animal husbandry production process.

[0054] As a specific embodiment of the present invention, the mixed gas enters the CO converter, the molar ratio of H2 and CO in the mixed gas is adjusted in the CO converter, and the mixed gas with the adjusted molar ratio of CO and H2 enters the acid gas remover. In the present invention, the molar ratio of H2 and CO in the mixed gas is adjusted according to the demand for synthesizing downstream products.

[0055] Preferably, when the synthetic downstream product is synthetic oil, the molar ratio of H2 and CO in the mixed gas is adjusted to 3.0-3.1.

[0056] Preferably, when the synthetic downstream product is methanol, the molar ratio of H2 and CO in the mixed gas is adjusted to 2.0-2.1.

[0057] Compared with the prior art, the present invention has the following beneficial effects.

[0058] The present invention designs a system and process for producing synthesis gas by coupling CO2 dry reforming and biomass gasification with a high-temperature gas-cooled reactor, which can improve the utilization efficiency of CO2 produced by biomass gasification and make full use of the heat generated by the high-temperature gas-cooled reactor. The high-temperature heat directly preheats the raw gas for dry reforming.

[0059] The waste heat generated by the system is used to generate electricity, which improves the heat recovery efficiency. In addition, the CO2 generated by the biomass gasification acid gas removal unit and the CH4 generated by the gas separator can fully react to generate synthesis gas, which not only reduces the carbon emissions of the entire device, but also improves the utilization efficiency of carbon atoms and improves economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0060] Figure 1 This is a schematic diagram of a synthesis gas production device provided by a high temperature gas-cooled reactor coupled with CO2 dry reforming and biomass gasification in Example 1 of the present invention;

[0061] Figure 2 This is a schematic diagram of a synthesis gas production device provided by a high temperature gas-cooled reactor coupled with CO2 dry reforming and biomass gasification in Example 2 of the present invention;

[0062] Among them, 1-high temperature gas-cooled reactor;

[0063] 2-CO2 dry reforming system, 21-feedstock preheater, 22-CO2 dry reforming reactor, 23-heat recovery device;

[0064] 3-biomass gasification synthesis gas production device, 31-biomass gasification reactor, 32-acid gas remover, 33-gas separator, 34-raw material pre-processor, 35-CO converter;

[0065] 4- pipeline, 41- pipeline I, 42- pipeline II, 43- pipeline III, 44- pipeline IV, 45- pipeline V, 46- pipeline VI;

[0066] 5-Heat exchanger;

[0067] 6-waste heat power generation device, 61-steam generator, 62-steam turbine generator, 63-condenser, 64-boiler feed pump;

[0068] 7- Gas compressor. DETAILED DESCRIPTION

[0069] The present invention will be further described below in conjunction with specific embodiments, but they do not constitute any limitation to the present invention.

[0070] Example 1

[0071] like Figure 1 As shown, a high temperature gas-cooled reactor coupled with CO2 dry reforming and biomass gasification synthesis gas production system includes a high temperature gas-cooled reactor 1, a CO2 dry reforming device 2, a biomass gasification synthesis gas production device 3, a pipeline 4 and a heat exchanger 5; the pipeline 4 includes a pipeline I41, a pipeline II42, a pipeline III43 and a pipeline IV44. The heat exchanger 5 is a tubular heat exchanger, and the heat exchanger 5 is provided with pipelines I and II.

[0072] The CO2 dry reforming device 2 includes a raw material preheater 21 and a CO2 dry reforming reactor 22. The raw material preheater 21 is a plate-type air preheater, and a preheating gas pipeline and a reaction gas pipeline are arranged inside the raw material preheater 21; the CO2 dry reforming reactor 22 is a fixed bed gasification reactor, and the gas discharged from the reaction gas pipeline enters the CO2 dry reforming reactor 22.

[0073] The biomass gasification synthesis gas production device 3 includes a biomass gasification reactor 31, an acid gas remover 32 and a gas separator 33. The outlet of the biomass gasification reactor 31 is connected to the inlet of the acid gas remover 32. The acid gas remover 32 includes outlets I, II and III. The outlet I is connected to the inlet of the gas separator 33. The gas separator 33 includes outlets IV and V. The outlet II is connected to the reaction gas pipeline through a pipeline I41. The outlet IV is connected to the reaction gas pipeline through a pipeline II42. The biomass gasification reactor 31 is a fixed bed gasification reactor. A mixed gas is generated in the biomass gasification reactor. The mixed gas is separated into effective gas, CO2 and impurity gas through the acid remover 32. The effective gas includes synthesis gas I and methane. The effective gas enters the gas separator 33 through the outlet I. The effective gas is separated into synthesis gas I and methane in the gas separator 33. CO2 is discharged into the reaction gas pipeline through the outlet II, and the impurity gas is discharged through the outlet III. The methane produced in the gas separator is discharged from outlet IV into the reaction gas pipeline, and the synthesis gas I is discharged from outlet V. The acid gas remover 32 is a low-temperature methanol washing device. The gas separator 33 adopts a membrane gas separation device.

[0074] The gas I generated in the high-temperature gas-cooled reactor enters the pipeline I, and enters the preheating gas pipeline after being discharged from the pipeline I. The gas I preheats the CO2 and methane in the reaction gas pipeline. The heated CO2 and methane enter the CO2 dry reforming reaction gas device 22, and the CO2 and methane react in the dry reforming reaction gas device 22 to generate synthesis gas II; the gas II discharged from the preheating pipeline enters the pipeline II through the pipeline III43, and after being discharged from the pipeline II, it returns to the high-temperature gas-cooled reactor 1 through the pipeline IV44.

[0075] Example 2

[0076] like Figure 2 As shown, the high temperature gas-cooled reactor coupled CO2 dry reforming and biomass gasification synthesis gas production system includes a high temperature gas-cooled reactor 1, a CO2 dry reforming device 2 and a biomass gasification synthesis gas production device 3, a pipeline 4 heat exchanger 5, a preheating power generation device 6 and a gas compressor 7; the pipeline 4 includes a pipeline I41, a pipeline II42, a pipeline III43, a pipeline IV44, a pipeline V45 and a pipeline VI6. The heat exchanger 5 is a tubular heat exchanger, and the heat exchanger 5 is provided with pipelines I and II.

[0077] The CO2 dry reforming device 2 includes a raw material preheater 21, a CO2 dry reforming reactor 22 and a heat recovery device 23. The CO2 dry reforming reactor 22 is a fixed bed gasification reactor, and the heat recovery device 23 is a partition heat exchanger. The raw material preheater 21 is a plate air preheater, and a preheating gas pipeline and a reaction gas pipeline are arranged inside the raw material preheater 21. The gas discharged from the reaction gas pipeline enters the CO2 dry reforming reactor 21, and the heat recovery device 23 is connected to the outlet of the CO2 dry reforming reactor 22. The gas discharged from the CO2 dry reforming reactor 22 enters the heat recovery device 23 to recover heat.

[0078] The biomass gasification synthesis gas production device 3 includes a biomass gasification reactor 31, an acid gas remover 32, a gas separator 33, a raw material preprocessor 34 and a CO converter 35. The outlet of the biomass gasification reactor 31 is connected to the inlet of the CO converter 35, and the outlet of the CO converter 35 is connected to the inlet of the acid gas remover 32. The acid gas remover 32 includes an outlet I, an outlet II and an outlet III. The outlet I is connected to the inlet of the gas separator 33, and the outlet II is connected to the reaction gas pipeline through a pipeline I41. The gas separator 33 includes an outlet IV and an outlet V; the outlet IV is connected to the reaction gas pipeline through a pipeline II42. After the biomass is crushed by the raw material preprocessor 34, it enters the biomass gasification reactor 31. The biomass gasification reactor 31 is a fixed bed gasification reactor. The biomass gasification reactor produces a mixed gas I, which enters the CO converter 35. The CO converter 35 adjusts the molar ratio of H2 and CO in the mixed gas I. The mixed gas II discharged from the CO converter 35 enters the acid remover 32. The acid remover 32 separates the mixed gas II into effective gas, CO2 and impurity gas. The effective gas includes synthesis gas I and methane. The effective gas enters the gas separator 33 through the outlet I. The effective gas is separated into synthesis gas I and methane in the gas separator 33. CO2 is discharged from the outlet II into the reaction gas pipeline, and the impurity gas is discharged from the outlet III. The methane generated in the gas separator is discharged from the outlet IV into the reaction gas pipeline; the synthesis gas I is discharged from the outlet V, and the synthesis gas I enters the synthesis pipeline network or the synthesis gas storage equipment for use in synthesizing downstream products. The acid gas remover 32 is a low-temperature methanol washing device. The gas separator 33 is a membrane gas separation device.

[0079] The gas I generated in the high-temperature gas-cooled reactor enters the pipeline I, and enters the preheating gas pipeline after being discharged through the pipeline I. The gas I preheats the CO2 and methane in the reaction gas pipeline. The heated CO2 and methane enter the CO2 dry reforming reaction gasifier 22. In the CO2 dry reforming reaction gasifier 22, CO2 and methane react to generate synthesis gas II. The synthesis gas II enters the heat recovery device 23 to recover heat and then is discharged; the gas II discharged from the preheating pipeline.

[0080] The steam generator 61 is arranged in the pipeline III43. The steam generator 51 includes a pipeline III and a pipeline IV. Water is stored in the pipeline IV. Gas II enters the pipeline III. Under the action of gas II, the water in the pipeline IV generates steam I and steam II. Gas III is discharged from the pipeline III. Gas III enters the pipeline II through the pipeline III43 and enters the high temperature gas-cooled reactor 1 after being compressed by the gas compressor 7 on the pipeline IV. Steam I enters the steam turbine generator 62 to drive the steam turbine generator 62 to generate electricity. Steam III discharged from the steam turbine generator 62 enters the condenser 63, and steam III is condensed into liquid in the condenser 63. The liquid discharged from the condenser 63 enters the pipeline IV through the pipeline V45. The boiler feed water pump 64 is arranged in the pipeline V45. The liquid discharged from the condenser enters the pipeline IV under the drive of the boiler feed water pump 64; steam II enters the reaction gas pipeline through the pipeline VI46 and enters the CO2 dry reforming reactor 22 after being preheated. The steam generator 61 is a partition-type heat exchanger, the steam turbine generator 62 is a condensing generator, the condenser 63 is a surface condenser, and the boiler feed water pump 64 is a centrifugal pump.

[0081] Example 3

[0082] The system in Example 2 is used, with a scale of 2.8 million tons / year of methanol produced by biomass gasification and CO2 dry reforming, and the thermal power of two reactor modules is 250MWth, and the power generation power is 210MWe as the calculation basis. The high temperature gas-cooled reactor used can provide 7MPaG, 700℃ high temperature helium 290.1t / h, i.e. gas I. After the biomass is crushed and extruded and granulated, a mixed gas is produced in the biomass gasification reactor, and the mixed gas enters the CO converter. The molar ratio of H2 to CO in the mixed gas is adjusted to 3.0-3.1 in the CO converter. The mixed gas can meet the requirements of synthesizing downstream products after the hydrogen-carbon ratio is adjusted. The crude synthesis gas after the hydrogen-carbon ratio is adjusted is separated into impurity gas, CO2 and effective gas in the acid gas remover, and the effective gas includes methane and synthesis gas I. Methane and synthesis gas I are separated into methane and synthesis gas I in the gas separator, and synthesis gas I is sent to the pipeline network for synthesizing downstream products. 3973 kmol / h methane produced in the gas separator and 2371 kmol / h CO2 produced in the acid gas remover are directly sent to the raw material preheater. In order to avoid carbon deposition in the CO2 reforming reactor, a small amount of water vapor, namely steam II, is added to the raw material preheater through the steam generator. The volume ratio of water vapor: CO2: CH4 is controlled to be 0.1:1:1. CO2, methane and water vapor are preheated to 450°C in the raw material preheater and then enter the CO2 reforming reactor for reaction, generating synthesis gas II after the reaction. The generated synthesis gas II is sent to the pipeline network after the heat is recovered by the heat recovery device for the synthesis of downstream products.

[0083] After the high-temperature helium passes through the raw material preheater, its temperature drops to 600°C and is discharged from the raw material preheater, namely, gas II. Gas II enters the steam generator. Under the action of the high-temperature helium, the steam generator produces 246.8t / h of 10.0MPaG steam, namely, steam I. Steam I enters the steam turbine generator to generate electricity. At this time, the power generation load is 18.23MW. The 200°C high-temperature helium after passing through the steam generator, namely, gas III, is returned to the high-temperature gas-cooled reactor for the next cycle. The steam discharged from the steam turbine generator, namely, steam III, enters the condenser and condenses into liquid. The liquid in the condenser is transported to the steam generator for recycling under the action of the boiler feed water pump.

[0084] Under this scale, not only can the annual consumption of CO2 raw materials be 818,000 tons / year, but also the heat and carbon emissions provided by the combustion of fuel gas required by the CO2 dry reforming device can be avoided. At the same time, an additional 146 million kWh of green electricity can be provided to the device or the external power grid.

[0085] It should be noted that the embodiments described above are only used to explain the present invention and do not constitute any limitation to the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory words, rather than restrictive words. The present invention may be modified as specified within the scope of the claims of the present invention, and the present invention may be revised without departing from the scope and spirit of the present invention. Although the present invention described therein relates to specific methods, materials and embodiments, it does not mean that the present invention is limited to the specific examples disclosed therein, on the contrary, the present invention can be extended to all other methods and applications with the same functions.

Claims

1. A system for producing synthesis gas by coupling CO2 dry reforming and biomass gasification with a high temperature gas-cooled reactor, characterized in that: Including high temperature gas-cooled reactor, CO2 dry reforming unit, biomass gasification production synthesis gas unit, pipelines and heat exchangers; Pipeline I and pipeline II are arranged inside the heat exchanger; The CO2 dry reforming device comprises a raw material preheater and a CO2 dry reforming reactor, wherein a preheating gas pipeline and a reaction gas pipeline are arranged inside the raw material preheater; the gas discharged from the reaction gas pipeline enters the CO2 dry reforming reactor; The biomass gasification synthesis gas production device comprises a biomass gasification reactor, an acid gas remover and a gas separator; the outlet of the biomass gasification reactor is connected to the inlet of the acid gas remover, the acid gas remover comprises an outlet I, an outlet II and an outlet III, the outlet I is connected to the inlet of the gas separator, and the gas separator comprises an outlet IV and an outlet V; The outlet II is connected to the reaction gas pipeline through pipeline I; The outlet IV is connected to the reaction gas pipeline through pipeline II; The gas I generated in the high temperature gas-cooled reactor enters the pipeline I, and enters the preheating gas pipeline after being discharged from the pipeline I; The gas II exhausted from the preheating pipeline enters the pipeline II through the pipeline III, and then enters the high temperature gas-cooled reactor through the pipeline IV after being exhausted from the pipeline II.

2. The system according to claim 1, characterized in that The system also includes a waste heat power generation device; The waste heat power generation device includes a steam generator, a steam turbine generator and a condenser; The steam generator is arranged in pipeline III, pipeline III and pipeline IV are arranged inside the steam generator, water is stored in pipeline IV, the gas II enters pipeline III, under the action of gas II, the water in pipeline IV generates steam I and steam II, gas III is discharged from pipeline III, gas III enters pipeline II, and then enters the high temperature gas-cooled reactor through pipeline IV; Steam I enters the steam turbine generator to drive the steam turbine generator to generate electricity. Steam III discharged from the steam turbine generator enters the condenser, where steam III is condensed into liquid. The liquid discharged from the condenser enters the pipeline IV through the pipeline V. Steam II enters the reaction gas pipeline through pipeline VI; Preferably, the waste heat power generation device further comprises a boiler feed pump, which is arranged in the pipeline V. The liquid discharged from the condenser enters the pipeline IV under the drive of the boiler feed pump.

3. The system according to claim 1 or 2, characterized in that: The CO2 dry reforming device further includes a heat recovery device, which is connected to the outlet of the CO2 dry reforming reactor and is used to recover the heat of the gas discharged from the CO2 dry reforming reactor.

4. The system according to claim 3, characterized in that The biomass gasification synthesis gas production device also includes a biomass raw material preprocessor, which is connected to the biomass gasification reactor and is used to crush, extrude and granulate the biomass; And / or, the biomass gasification synthesis gas system also includes a CO converter, which is arranged between the biomass gasification reactor and the acid gas remover. The gas exhausted from the biomass gasification synthesis gas system enters the CO converter, is discharged from the CO converter, and then enters the acid gas remover. The CO converter is used to adjust the molar ratio of H2 and CO in the exhaust gas from the biomass gasification reactor.

5. The system according to any one of claims 1 to 4, characterized in that: The system further comprises a gas compressor, which is arranged in pipeline IV and is located between the high temperature gas-cooled reactor and the heat exchanger.

6. A process for producing synthesis gas by coupling CO2 dry reforming and biomass gasification with a high temperature gas-cooled reactor, using the system of claim 5, characterized in that: The following steps are involved: Step 1: Biomass reacts in a biomass gasification reactor to generate a mixed gas, which is separated into effective gas, CO2 and impurity gas by an acid gas remover. The effective gas is discharged through outlet I and enters a gas separator. The effective gas includes synthesis gas I and methane; CO2 is discharged through outlet II and enters a reaction gas pipeline; impurity gas is discharged through outlet III, and the effective gas is separated into methane and synthesis gas I by a gas separator. Methane is discharged through outlet IV and enters a reaction gas pipeline, and synthesis gas I is discharged through outlet V; Step 2: The high temperature gas-cooled reactor generates gas I, which enters the preheater pipeline through pipeline I. Gas I preheats CO2 and methane in the reaction gas pipeline, and gas II is discharged from the preheater pipeline. Gas II enters pipeline II through pipeline III, and then returns to the high temperature gas-cooled reactor through pipeline IV for recycling. The CO2 and methane discharged from the reaction gas pipeline enter the CO2 dry reforming reactor; Step 3: CO2 and methane react in a CO2 dry reforming reactor to generate synthesis gas II.

7. The process according to claim 6, characterized in that In step 2, gas II enters pipeline III. Under the action of gas II, water in pipeline IV generates steam I and steam II. Gas III is discharged from pipeline III. Steam I enters the steam turbine generator to generate electricity. Steam III discharged from the steam turbine generator enters the condenser. Steam III is condensed into liquid in the condenser. The liquid generated in the condenser enters pipeline IV for recycling. Steam II enters the reaction gas pipeline and mixes with CO2 and methane before entering the CO2 dry reforming reactor; Gas III enters pipeline II, is discharged from pipeline II, and then returns to the high temperature gas-cooled reactor through pipeline IV for recycling; Preferably, the gas discharged from pipeline II is compressed by a gas compressor and then returned to the high temperature gas-cooled reactor for recycling.

8. The process according to claim 7, characterized in that The liquid discharged from the condenser is introduced into the steam generator through the boiler feed water pump; and / or the synthesis gas II enters the heat recovery device, recovers heat through the heat recovery device, and is then discharged.

9. The process according to claim 8, characterized in that The temperature of gas I is 700-750°C, the temperature of gas II is 600-650°C, and the temperature of gas III is 200-250°C; and / or, in step 2, the temperature of CO2 and methane discharged from the reaction gas pipeline is 450-500°C; preferably, the temperature of CO2, methane and steam II discharged from the reaction gas pipeline is 450-500°C.

10. The process according to claim 9, characterized in that The biomass in step 1 is crushed and extruded and granulated by a biomass raw material preprocessor, and then enters a biomass gasification reactor to react; and or, the mixed gas enters a CO converter, the molar ratio of H2 and CO in the mixed gas is adjusted in the CO converter, and the mixed gas with the adjusted molar ratio of CO and H2 enters an acid gas remover; Preferably, the molar ratio of H2 to CO in the mixed gas is adjusted to 3.0 to 3.1; Preferably, the molar ratio of H2 to CO in the mixed gas is adjusted to 2.0-2.1.

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