Device for preparing synthesis gas through gasification coupling high-temperature thermal reforming

Abstract

The utility model discloses a device for preparing synthesis gas through gasification coupling high-temperature thermal reforming, and belongs to the technical field of gasification. The device comprises a gasification raw material feeder, a low-temperature gasification furnace, a high-temperature thermal reforming reactor, a deslagging lock hopper, a steam pocket, a synthesis gas cooler, an ash remover, a washing tower, a gas-liquid separator and a waste liquid collector, the low-temperature gasification furnace comprises a combustion area and a reduction area from bottom to top, and the high-temperature thermal reforming reactor comprises a step-by-step combustion area, a high-temperature reduction area and an ash collecting area from top to bottom; slag is discharged from a slag outlet at the bottom of the high-temperature thermal reforming reactor, and a gas outlet is connected with a synthesis gas cooler; the cooled synthesis gas sequentially passes through an ash remover, a washing tower and a gas-liquid separator for purification treatment; according to the utility model, the high-temperature thermal reforming reactor is adopted to reform and purify the crude gasified gas generated by gasification, tar and methane in the crude gasified gas are converted into CO and H2, and the problems of low energy utilization rate and low synthesis gas quality in the gasification technology are solved.

Description

Technical Field

[0001] The utility model belongs to the technical field of gasification, and in particular relates to a device for producing synthesis gas by coupling gasification with high-temperature thermal reforming. Background Art

[0002] Gasification is a thermochemical process that converts solid or liquid carbonaceous raw materials into combustible gases. This technology has been widely used in the fields of energy, chemical industry and clean energy development. The typical process of producing synthesis gas by gasification is: the gasification raw materials and gasifying agents (water, air, oxygen or carbon dioxide) undergo a gasification reaction at high temperature, and then the raw gas discharged from the gasifier is provided to the downstream process section after heat exchange, purification, dust removal and other steps. At present, gasifiers have high requirements for gasification raw materials. At the same time, the raw synthesis gas contains a large amount of impurities such as methane and tar. These impurities not only make the synthesis gas unstable, but also reduce the energy efficiency and carbon conversion rate of the entire gasification process.

[0003] After searching, patent CN219385071U discloses a low-rank coal gasification system, which realizes efficient utilization of low-rank coal by combining mainstream fluidized bed gasifier, fluidized bed combustion furnace and fluidized bed combustion furnace, but the gasification system has the disadvantages of high investment cost and difficulty in equipment maintenance, and the conversion effect of the gasification system on high-rank coal and biomass is not ideal. Patent CN216378071U discloses an entrained bed gasification device, which uses an entrained bed gasifier with a temperature between 1200 and 1600 to gasify pulverized coal. Although the gasification efficiency and stability of the device are high, the device directly cools and purifies the raw gasification gas containing a large amount of methane and tar from the gasifier, which leads to the technology facing problems such as low energy utilization, low carbon conversion rate, poor economic benefits, and serious secondary pollution. Patent CN111073711A discloses a low-tar biomass gasification method and system. The invention uses the low-temperature condensation characteristics of tar to pass the fuel gas through a heat exchanger and a material bed, thereby achieving gasification of the biomass raw material and adsorption of the tar. This method does not effectively treat methane, and the use of a heat exchanger and a material bed leads to increased investment and operating costs, and also makes it impossible to scale up the device. As can be seen from the above, the current gasification technology has problems such as high raw material requirements, large fluctuations in product composition and quality, serious secondary pollution, low gasification efficiency, and low carbon conversion rate.

[0004] As mentioned above, in view of the technical problems of existing gasification technology such as low gasification efficiency, poor operating stability, high environmental pressure, poor economic benefits, and limited production capacity, it is necessary to develop a large-scale, low-cost, clean and efficient gasification device. Utility Model Content

[0005] In view of the above problems in the prior art, the utility model provides a large-scale gasification device with high gasification efficiency, good economic benefits, stable operation, cleanliness and high efficiency.

[0006] In order to achieve the above purpose, the utility model adopts the following technical solutions:

[0007] A device for producing synthesis gas by gasification coupled with high-temperature thermal reforming, comprising a gasification raw material feeder, a low-temperature gasification furnace, a high-temperature thermal reforming reactor, a slag lock hopper, a steam drum, a synthesis gas cooler, an ash remover, a scrubber, a gas-liquid separator and a waste liquid collector;

[0008] A crude gasification gas outlet is provided on the upper side wall of the low-temperature gasifier, and a gasification raw material feed port and a gasification agent inlet are provided on the lower side wall; a crude gasification gas inlet and a plurality of first air inlets are provided on the top of the high-temperature thermal reforming reactor, and a plurality of second air inlets and a plurality of third air inlets are provided on the upper part of the side wall; a cooling water inlet and an air outlet are provided on the lower part of the side wall; a slag outlet is provided on the bottom; and a slag discharge lock bucket is connected to the slag outlet;

[0009] The outlet of the gasification raw material feeder is connected to the low-temperature gasifier through the gasification raw material feed port; the low-temperature gasifier is connected to the crude gasification gas inlet at the top of the high-temperature thermal reforming reactor through the crude gasification gas outlet; the high-temperature thermal reforming reactor is connected to the feed port of the synthesis gas cooler through the gas outlet; the discharge port of the synthesis gas cooler is connected to the feed port of the ash remover through a pipeline; the gas outlet of the ash remover is connected to the gas inlet of the washing tower through a pipeline, and fine ash is discharged from the bottom of the ash remover; process condensed water is injected into the top of the washing tower, and the gas outlet of the washing tower is connected to the gas inlet of the gas-liquid separator through a pipeline; the liquid outlets of the washing tower and the gas-liquid separator are both connected to the liquid inlet of the waste liquid collector through a pipeline, and the liquid outlet of the waste liquid collector is connected to the cooling water inlet of the high-temperature thermal reforming reactor through a pipeline;

[0010] The steam drum is connected to the heat exchange medium of the synthesis gas cooler through a pipeline to form a circulation loop, and at the same time, the boiler feed water transported from another pipeline is converted into high-pressure steam and discharged from the outlet.

[0011] Furthermore, the interior of the low-temperature gasifier is composed of a combustion zone and a reduction zone from bottom to top; the interior of the high-temperature thermal reforming reactor is composed of an ash collection zone, a high-temperature reduction zone and a step-by-step combustion zone from bottom to top.

[0012] Furthermore, the pipeline between the gasification raw material feeder and the low-temperature gasification furnace is inclined to the furnace wall so that the outlet of the gasification raw material feeder is higher than the gasification raw material feed inlet of the low-temperature gasification furnace.

[0013] Furthermore, the height difference between the second air inlet and the first air inlet accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor, and the height difference between the second air inlet and the third air inlet accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor, forming a uniform temperature field to promote the conversion of methane and tar.

[0014] Furthermore, the low-temperature gasification furnace is cast by a pressure-resistant steel shell and refractory materials, with an operating temperature of 600° C. to 900° C. and a working pressure of 0.1 MPa to 3 MPa.

[0015] Furthermore, the high-temperature thermal reforming reactor adopts a water-cooled wall structure, with an operating temperature of 1200° C. to 1600° C. and an operating pressure of 0.1 MPa to 3 MPa.

[0016] Furthermore, the dust collector is a bag dust collector.

[0017] The method for producing synthesis gas by gasification coupled with high temperature thermal reforming according to the above device comprises the following steps:

[0018] Step 1, the pre-treated gasification raw material is continuously and evenly added from the gasification raw material feed port to the lower part of the low-temperature gasification furnace through the gasification raw material feeder;

[0019] Step 2, introducing the pre-mixed gasifying agent into the gasifying agent inlet of the low-temperature gasifier;

[0020] Step 3, the gasification raw material and the gasifying agent are burned at 600°C to 900°C in the lower part of the low-temperature gasifier to generate semi-coke and a mixed gas of CO2 and H2O; the mixed gas rises to the upper part of the low-temperature gasifier, and then undergoes a reduction reaction at 700°C to 900°C to generate a crude gasification gas, and the crude gasification gas enters the high-temperature thermal reforming reactor through the crude gasification gas outlet at the top of the low-temperature gasifier;

[0021] Step 4, the crude gas is subjected to a reduction reaction in a high-temperature thermal reforming reactor at 1200° C. to 1500° C. to convert methane and tar into CO and H2, thereby completing the reforming of the crude gas;

[0022] Step 5, the crude gas reformed in step 4 is passed into a synthesis gas cooler to recover waste heat, and the heat is converted into high-temperature and high-pressure steam in a steam drum through a pipeline; the reformed crude gas is cooled from an inlet temperature of 1200°C to 1500°C to an outlet temperature of 300°C to 600°C;

[0023] Step 6, the cooled crude gas enters the ash remover to remove fine ash contained therein, and then further removes impurities in the scrubber, and finally passes into the gas-liquid separator to remove trace moisture contained therein, thereby obtaining synthesis gas;

[0024] Step 7: the liquid discharged from the washing tower and the gas-liquid separator flows into a waste liquid collector, and then is transported from the waste liquid collector to the bottom of the high-temperature thermal reforming reactor to cool the slag.

[0025] Furthermore, the mass percentage content of moisture in the gasification raw material is ≤15%; the mass percentage content of ash is ≤10%; the mass percentage content of volatile matter is <80%; the mass percentage content of fixed carbon is ≥10%; and the low calorific value is ≥12MJ / kg;

[0026] Further, the flow rate of oxygen in the gasifying agent is 0.20 kg / kg (biomass), and the flow rate of water vapor is 0.70 kg / kg (biomass);

[0027] Furthermore, the H2 content in the crude gasification gas is 20 mol% to 40 mol%; the CO content is 15 mol% to 30 mol%; the methane content is 7 mol% to 15 mol%; and the tar content is 5 g / Nm 3 ~50g / Nm 3 ;

[0028] Furthermore, the H2 content in the synthesis gas is 35mol% to 52mol%, the CO content is 39mol% to 63mol%, the methane content is ≤0.15mol%, and the tar content is ≤9mg / Nm 3 .

[0029] Furthermore, the molar ratio of oxygen delivered by the first air inlet to the oxygen required for complete combustion of the crude gas is 0.05-0.09, the molar ratio of oxygen delivered by the second air inlet to the oxygen required for complete combustion of the crude gas is 0.02-0.07, and the molar ratio of oxygen delivered by the third air inlet to the oxygen required for complete combustion of the crude gas is 0.06-0.10.

[0030] Compared with the prior art, the utility model has the following advantages:

[0031] 1. The utility model has a high carbon conversion rate. By subjecting the crude gasification gas to a high-temperature thermal reforming reaction, the carbon conversion rate of the gasification process can reach more than 96%, effectively reducing the generation of CO2, methane and tar.

[0032] The gasification-coupled high-temperature thermal reforming synthesis gas production device of the utility model further performs high-temperature thermal reforming on the raw gas obtained after gasification to stably produce high-purity synthesis gas, which can effectively solve the problems of low carbon conversion rate, poor economic benefits, and high environmental pressure of current gasification technology.

[0033] 2. The utility model has the potential for large-scale production. Without changing the number of gasifiers, by adjusting the sizes of the gasifiers and the high-temperature thermal reforming reactors, the production capacity of a single gasifier can reach 15-70t / h.

[0034] 3. The utility model has strong adaptability to raw materials. The function of the gasifier is only to produce raw gasification gas, so the gasifier of the device can adapt to different biomass, different coal or other gasification raw materials at the same time.

[0035] 4. The utility model is simple and flexible to operate and runs stably. Compared with the traditional gasification technology, the utility model only needs to combine with the control system to maintain the stable feed ratio of the gasification raw material and the gasification agent to achieve efficient and stable operation of the gasification.

[0036] 5. The utility model has a high energy utilization rate. By combining the use of a syngas cooler and a steam drum, the excess heat generated by gasification can be converted into kinetic energy and thermal energy, thereby effectively reducing the energy loss of the entire process.

[0037] 6. The secondary pollution of the utility model is small. Compared with the traditional gasification technology, the utility model can fully convert the carbon in the gasification raw material into CO in the synthesis gas, avoiding the formation of tar in the production process, thereby avoiding the environmental pressure caused by removing the tar. BRIEF DESCRIPTION OF THE DRAWINGS

[0038] Figure 1 This is a process flow chart of gasification coupled high temperature thermal reforming;

[0039] Figure 2 This is a structural diagram of a low-temperature gasification furnace in an embodiment of the utility model;

[0040] Figure 3 This is a structural diagram of a high temperature thermal reforming reactor in an embodiment of the utility model;

[0041] Figure numerals: 1. gasification raw material feeder; 2. low-temperature gasification furnace; 3. high-temperature thermal reforming reactor; 4. slag lock bucket; 5. steam drum; 6. synthesis gas cooler; 7. ash remover; 8. washing tower; 9. gas-liquid separator; 10. waste liquid collector; 11. combustion zone; 12. reduction zone; 13. ash outlet; 14. gasification raw material feed port; 15. gasification agent inlet; 16. crude gasification gas outlet; 17. ash collection zone; 18. high-temperature reduction zone; 19. step-by-step combustion zone; 20. slag outlet; 21. cooling water inlet; 22. air outlet; 23. third air inlet; 24. second air inlet; 25. first air inlet; 26. crude gasification gas inlet. DETAILED DESCRIPTION

[0042] In order to gain a deeper understanding of the present invention, we will provide a comprehensive and detailed description of the present invention. However, the present invention has multiple implementations and is not limited to the specific examples listed herein. The presentation of these examples is intended to deepen the comprehensive understanding of the disclosure of the present invention.

[0043] Example 1

[0044] A device for producing synthesis gas by gasification coupled with high-temperature thermal reforming, comprising a gasification raw material feeder 1, a low-temperature gasification furnace 2, a high-temperature thermal reforming reactor 3, a slag lock hopper 4, a steam drum 5, a synthesis gas cooler 6, an ash remover 7, a washing tower 8, a gas-liquid separator 9 and a waste liquid collector 10

[0045] The interior of the low-temperature gasification furnace 2 is composed of a combustion zone 11 and a reduction zone 12 from bottom to top; the interior of the high-temperature thermal reforming reactor 3 is composed of an ash collection zone 17, a high-temperature reduction zone 18 and a step-by-step combustion zone 19 from bottom to top.

[0046] A crude gasification gas outlet 16 is provided on the upper side wall of the low-temperature gasification furnace 2, and a gasification raw material feed port 14 and a gasification agent inlet 15 are provided on the lower side wall; a crude gasification gas inlet 26 and a plurality of first air inlets 25 are provided on the top of the high-temperature thermal reforming reactor 3, and a plurality of second air inlets 24 and a plurality of third air inlets 23 are provided on the upper side wall; a cooling water inlet 21 and an air outlet 22 are provided on the lower side wall; a slag outlet 20 is provided on the bottom; and the slag outlet 20 is connected to a slag discharge lock bucket 4;

[0047] The height difference between the second air inlet 24 and the first air inlet 25 accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor 3, and the height difference between the second air inlet 24 and the third air inlet 23 accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor 3, forming a uniform temperature field to promote the conversion of methane and tar.

[0048] The pipeline between the gasification raw material feeder 1 and the low-temperature gasification furnace 2 is inclined to the furnace wall so that the outlet of the gasification raw material feeder 1 is higher than the gasification raw material feed port 14 of the low-temperature gasification furnace 2 .

[0049] The outlet of the gasification raw material feeder 1 is connected to the low-temperature gasifier 2 through the gasification raw material feed port 14; the low-temperature gasifier 2 is connected to the crude gasification gas inlet 26 at the top of the high-temperature thermal reforming reactor 3 through the crude gasification gas outlet 16; the high-temperature thermal reforming reactor 3 is connected to the feed port of the synthesis gas cooler 6 through the gas outlet 22; the outlet of the synthesis gas cooler 6 is connected to the feed port of the ash remover 7 through a pipeline; the gas outlet of the ash remover 7 is connected to the gas inlet of the washing tower 8 through a pipeline, and the gas outlet of the washing tower 8 is connected to the gas inlet of the gas-liquid separator 9 through a pipeline; the liquid outlets of the washing tower 8 and the gas-liquid separator 9 are both connected to the liquid inlet of the waste liquid collector 10 through a pipeline, and the liquid outlet of the waste liquid collector 10 is connected to the cooling water inlet 21 of the high-temperature thermal reforming reactor 3 through a pipeline;

[0050] The steam drum 5 is connected to the heat exchange medium of the synthesis gas cooler 6 through a pipeline to form a circulation loop, and at the same time, the boiler feed water transported from another pipeline is converted into high-pressure steam and discharged from the gas outlet.

[0051] Furthermore, the low-temperature gasification furnace 2 is cast by a pressure-resistant steel shell and refractory materials, with an operating temperature of 600-900° C. and a working pressure of 0.1-3 MPa.

[0052] Furthermore, the high temperature thermal reforming reactor 3 adopts a water-cooled wall structure, with an operating temperature of 1200-1600° C. and an operating pressure of 0.1-3 MPa.

[0053] Furthermore, the dust collector 7 is a bag dust collector.

[0054] The low-temperature gasifier 2 is fed with gasification raw materials, steam and oxygen for gasification reaction, wherein the gasification raw materials undergo incomplete combustion reaction with oxygen, and undergo gasification reaction with the participation of steam to generate crude gas. A certain amount of oxygen is introduced into the high-temperature thermal reforming reactor 3, which can further convert the tar and methane contained in the crude gas, and convert the tar and methane in the crude gas into synthesis gas; the synthesis gas cooler 6 is used to introduce the high-temperature crude gas converted by the high-temperature thermal reforming reactor 3, and is used to provide the steam drum 5 with the heat source required to generate steam. The waste liquid collector 10 is used to collect and store waste water from the washing tower 8 and the gas-liquid separator 9.

[0055] In this embodiment, a combination of low-temperature gasification and high-temperature thermal reforming reactors is adopted to fully utilize the advantages of each device. The tower conversion rate of the gasification device can reach 99%. At the same time, the synthesis gas produced by the device does not contain tar and methane, which greatly reduces the environmental pressure in the production process and can generate higher economic benefits.

[0056] The method for producing synthesis gas by gasification coupled with high temperature thermal reforming according to the above device comprises the following steps:

[0057] Step 1, the pre-treated gasification raw material is continuously and evenly added to the lower part of the low-temperature gasification furnace 2 from the gasification raw material feed port 14 through the gasification raw material feeder 1; the mass percentage content of water in the gasification raw material is ≤15%; the mass percentage content of ash is ≤10%; the mass percentage content of volatile matter is <80%; the mass percentage content of fixed carbon is ≥10%; and the low calorific value is ≥12MJ / kg;

[0058] Step 2, introducing a pre-mixed gasifying agent into the gasifying agent inlet 15 of the low-temperature gasifier 2; the flow rate of oxygen in the gasifying agent is 0.20 kg / kg (biomass), and the flow rate of water vapor is 0.70 kg / kg (biomass);

[0059] Step 3, the gasified raw material and the gasifying agent are burned at 600°C to 900°C in the lower part of the low-temperature gasifier 2 to generate a mixture of semi-coke and CO2 and H2O; the mixed gas rises to the upper part of the low-temperature gasifier 2, and then undergoes a reduction reaction at 700°C to 900°C to generate a crude gas, which enters the high-temperature thermal reforming reactor 3 through the crude gasification gas outlet 16 at the top of the low-temperature gasifier 2; the H2 content in the crude gasification gas is 20mol% to 40mol%; the CO content is 15mol% to 30mol%; the methane content is 7mol% to 15mol%; the tar content is 5g / Nm 3 ~50g / Nm 3 ;

[0060] Step 4, the crude gasification gas is subjected to a reduction reaction in a high-temperature thermal reforming reactor 3 at 1200° C. to 1500° C. to convert methane and tar into CO and H2, thereby completing the reforming of the crude gasification gas;

[0061] Step 5, the crude gas reformed in step 4 is passed into the synthesis gas cooler 6 for waste heat recovery, and the heat is converted into high-temperature and high-pressure steam in the steam drum 5 through the pipeline; the reformed crude gas is cooled from the inlet 1200°C to 1500°C to the outlet 300°C to 600°C;

[0062] Step 6: The cooled crude gas enters the ash remover 7 to remove fine ash contained therein, and then further removes impurities in the scrubber 8, and finally enters the gas-liquid separator 9 to remove trace moisture contained therein to obtain synthesis gas; the synthesis gas contains H2 content of 35mol% to 52mol%, CO content of 39mol% to 63mol%, methane content ≤0.15mol%, and tar content ≤9mg / Nm 3 .

[0063] In step 7, the liquid discharged from the washing tower 8 and the gas-liquid separator 9 flows into the waste liquid collector 10, and then is transported from the waste liquid collector 10 to the bottom of the high-temperature thermal reforming reactor 3 to cool the slag.

[0064] Furthermore, the molar ratio of oxygen delivered by the first air inlet 25 to the oxygen required for complete combustion of the crude gas is 0.05-0.09, the molar ratio of oxygen delivered by the second air inlet 24 to the oxygen required for complete combustion of the crude gas is 0.02-0.07, and the molar ratio of oxygen delivered by the third air inlet 23 to the oxygen required for complete combustion of the crude gas is 0.06-0.10.

[0065] The chemical reaction formula of the gasification reaction in the low-temperature fluidized bed 2 is as follows:

[0066] C+CO2=2CO-Q; H2O+CO=2CO2+H2-Q

[0067] C + H2O = H2 + CO-Q;

[0068] C + 2H2O = CO2 + 2H2-Q;

[0069] 3H2+CO=CH4+H2O-Q;

[0070] The chemical reaction formula of the reforming reaction in the high temperature thermal reforming reactor 3 is as follows:

[0071] 2CH4+O2=2CO+4H2+Q;

[0072] C n H m +n / 2O2=nCO+m / 2H2+Q;

[0073] In this embodiment, the secondary combustion of tar and methane in the crude gasification gas not only reduces the content of tar and methane, greatly reduces the load of the subsequent synthesis gas purification section, but also improves the energy efficiency and carbon conversion rate of the entire system. Compared with traditional gasification technology, the utility model has been greatly improved in terms of process, economy and environmental protection.

[0074] The contents not described in detail in the specification of the utility model belong to the prior art known to the professional and technical personnel in the field. Although the above describes the illustrative specific implementation of the utility model to facilitate the understanding of the utility model by the technical personnel in the field, it should be clear that the utility model is not limited to the scope of the specific implementation. For the ordinary technical personnel in the field, as long as the various changes are within the spirit and scope of the utility model defined and determined by the attached claims, these changes are obvious, and all inventions and creations conceived by the utility model are protected.

Claims

1. A device for producing synthesis gas by gasification coupled with high temperature thermal reforming, characterized in that: It comprises a gasification raw material feeder (1), a low-temperature gasification furnace (2), a high-temperature thermal reforming reactor (3), a slag discharge lock hopper (4), a steam drum (5), a synthesis gas cooler (6), an ash remover (7), a washing tower (8), a gas-liquid separator (9) and a waste liquid collector (10); A crude gasification gas outlet (16) is provided on the upper side wall of the low-temperature gasification furnace (2), and a gasification raw material feed port (14) and a gasification agent inlet (15) are provided on the lower side wall; a crude gasification gas inlet (26) and a plurality of first air inlets (25) are provided on the top of the high-temperature thermal reforming reactor (3), and a plurality of second air inlets (24) and a plurality of third air inlets (23) are provided on the upper side wall; a cooling water inlet (21) and an air outlet (22) are provided on the lower side wall; a slag outlet (20) is provided on the bottom; and the slag outlet (20) is connected to a slag discharge lock bucket (4); The outlet of the gasification raw material feeder (1) is connected to the low-temperature gasification furnace (2) through the gasification raw material feed port (14); the low-temperature gasification furnace (2) is connected to the crude gasification gas inlet (26) at the top of the high-temperature thermal reforming reactor (3) through the crude gasification gas outlet (16); the high-temperature thermal reforming reactor (3) is connected to the feed port of the synthesis gas cooler (6) through the gas outlet (22); the outlet of the synthesis gas cooler (6) is connected to the feed port of the ash remover (7) through a pipeline. The gas outlet of the ash remover (7) is connected to the gas inlet of the washing tower (8) through a pipeline, and the gas outlet of the washing tower (8) is connected to the gas inlet of the gas-liquid separator (9) through a pipeline; the liquid outlets of the washing tower (8) and the gas-liquid separator (9) are both connected to the liquid inlet of the waste liquid collector (10) through a pipeline, and the liquid outlet of the waste liquid collector (10) is connected to the cooling water inlet (21) of the high-temperature thermal reforming reactor (3) through a pipeline; The steam drum (5) is connected to the heat exchange medium of the synthesis gas cooler (6) through a pipeline to form a circulation loop, and at the same time, the boiler feed water transported by another pipeline is converted into high-pressure steam and discharged from the gas outlet.

2. The device for producing synthesis gas by gasification coupled with high temperature thermal reforming according to claim 1, characterized in that: The interior of the low-temperature gasification furnace (2) is composed of a combustion zone (11) and a reduction zone (12) from bottom to top; the interior of the high-temperature thermal reforming reactor (3) is composed of an ash collection zone (17), a high-temperature reduction zone (18) and a step-by-step combustion zone (19) from bottom to top.

3. The device for producing synthesis gas by gasification coupled with high temperature thermal reforming according to claim 1, characterized in that: The pipeline between the gasification raw material feeder (1) and the low-temperature gasification furnace (2) is arranged to be inclined with respect to the furnace wall, so that the outlet of the gasification raw material feeder (1) is higher than the gasification raw material feed port (14) of the low-temperature gasification furnace (2).

4. The device for producing synthesis gas by gasification coupled with high temperature thermal reforming according to claim 1, characterized in that: The height difference between the second air inlet (24) and the first air inlet (25) accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor (3), and the height difference between the second air inlet (24) and the third air inlet (23) accounts for 1 / 5 to 1 / 3 of the height of the high-temperature thermal reforming reactor (3), forming a uniform temperature field for promoting the conversion of methane and tar.

5. The device for producing synthesis gas by gasification coupled with high temperature thermal reforming according to claim 1, characterized in that: The low-temperature gasification furnace (2) is formed by casting a pressure-resistant steel shell and refractory materials, with an operating temperature of 600° C. to 900° C. and an operating pressure of 0.1 MPa to 3 MPa.

6. The device for producing synthesis gas by gasification coupled with high temperature thermal reforming according to claim 1, characterized in that: The high-temperature thermal reforming reactor (3) adopts a water-cooled wall structure, with an operating temperature of 1200° C. to 1600° C. and an operating pressure of 0.1 MPa to 3 MPa.

7. The device for producing synthesis gas by gasification coupled with high temperature thermal reforming according to claim 1, characterized in that: The dust collector (7) is a bag dust collector.

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