Staged reformer gasifier

Abstract

The utility model belongs to the coal gasification technical field, concretely relates to a kind of sectional conversion gasification furnace, including pyrolysis gasification reactor, fused aggregate separation unit and material leg fine powder circulating unit;The pyrolysis gasification reactor includes cylindrical furnace body, and the lower end of the cylindrical furnace body is fixedly connected with lower dense phase fluidized bed furnace body, and there is coal feeding pipe, oven coal gas pipe and second gasification nozzle on the lower dense phase fluidized bed furnace body, and the lower dense phase fluidized bed furnace body, coal feeding pipe, oven coal gas pipe and second gasification nozzle jointly constitute lower dense phase fluidized bed gasification section, and there is quenching water pipe and gasification furnace coal gas outlet on the top of the cylindrical furnace body, and the quenching water pipe and gasification furnace coal gas outlet constitute upper particle sedimentation separation section.The utility model uses sectional conversion process, improves gas-solid contact rate, increases residence time, and unconverted fly ash fine powder returns center tube high-temperature zone efficient conversion by center burner.

Description

Technical Field

[0001] This utility model belongs to the field of coal gasification technology, specifically relating to a staged conversion gasifier. Background Technology

[0002] my country's resource endowment of "abundant coal, scarce oil, and limited gas" dictates that coal will remain a crucial basic energy source for the foreseeable future. Coal gasification technology is one of the core technologies for achieving efficient and clean coal utilization. Reports indicate that low-rank coal, primarily lignite and long-flame coal, accounts for approximately 45% of my country's remaining recoverable coal reserves. However, the "two highs and three lows" (high volatile matter, high moisture, low ash fusion point, low density, and low calorific value) of lignite and other low-rank coals lead to severe environmental pollution, making large-scale utilization difficult.

[0003] Fluidized bed gasifiers are widely used in coal gasification due to their uniform temperature field, excellent heat and mass transfer between particles and gas, wide adaptability to different coal types, and low cost. Many coal gasification reactions utilize fluidized bed gasification devices. A search reveals numerous published patents related to fluidized bed gasification systems. Chinese utility model patent application CN1114976A discloses a method and apparatus for ash agglomeration fluidized bed gasification. This technology employs a dense-phase fluidized bed gasification process with ash agglomeration for ash removal. Based on the jet principle, an ash separation device is designed at the bottom of the fluidized bed, creating localized high temperatures within the bed that cause ash to agglomerate into spheres. The ash spheres are then separated from the material by weight difference. Chinese utility model patent application CN103911179A discloses a coal gasification method and apparatus. Pulverized coal and a gasifying agent are fed into a circulating fluidized bed gasifier for reaction. The generated gasifier flue gas is separated into return pulverized coal and a pulverized coal-laden gas stream by a first gas-solid separator. The return pulverized coal is recycled back to the circulating fluidized bed gasifier for further reaction, while the pulverized coal-laden gas stream is separated into coal gas and carbonaceous fly ash by a second gas-solid separator. The carbonaceous fly ash is fed into a hot blast stove and burned at a temperature above 1300°C. The resulting hot blast stove flue gas is returned to the circulating fluidized bed gasifier to participate in the reaction. The liquid slag generated from combustion is cooled and discharged. Chinese utility model patent application CN113088336A discloses a staged gasification pure oxygen circulating fluidized bed coal gas generator and its operating method. This method has several nozzles set in the main gasification core area, with the centerline of each nozzle extended to be tangent to the central circle, and a steam injection component is provided in the slag discharge mechanism. Chinese utility model patent application CN112824502A discloses a circulating fluidized bed gasification device and method, developed based on circulating fluidized bed boiler technology. Chinese utility model patent application CN105779008A discloses a method and system for treating pulverized coal. This method combines a circulating fluidized bed gasification system with an entrained gasification system, utilizing the fly ash generated by the circulating fluidized bed gasification system as raw material. It aims to solve the problems of low coal utilization and large fly ash volume in circulating fluidized bed gasification, thereby improving coal conversion efficiency.

[0004] However, with increasing industrial demands, the required gas production capacity of a single gasifier has increased (currently, the maximum gas production capacity of a single industrial gasifier is 80,000 Nm³ / h). Uneven gas distribution inevitably occurs during fluidized bed scale-up, leading to a decline in localized fluidization quality and even the emergence of dead zones. This directly affects the gasification reaction, reduces carbon conversion efficiency, and becomes a significant limiting factor for fluidized bed gasifier scale-up. Furthermore, the crude gas discharged from the fluidized bed gasifier outlet contains a high dust content, and the produced gas contains unreacted fly ash with a high carbon content, resulting in a loss of some of the coal's calorific value. These problems have yet to be effectively resolved.

[0005] Therefore, there is an urgent need to design a gasification system that produces high gas volume and can efficiently utilize carbon-containing fly ash. This system should not only overcome the shortcomings of large-scale coal utilization but also improve the utilization efficiency of carbon-containing fly ash, enhance the reaction thermal efficiency of the gasifier, and achieve efficient energy conversion. Utility Model Content

[0006] This invention provides a segmented conversion gasifier to address the aforementioned problems.

[0007] To achieve the above objectives, the present invention adopts the following technical solution: The segmented conversion gasifier includes a pyrolysis gasification reactor, a molten aggregate ash separation unit, and a feed leg fine powder circulation unit. The pyrolysis gasification reactor includes a cylindrical furnace body. A lower dense-phase fluidized bed furnace body is fixedly connected to the lower end of the cylindrical furnace body. A crushed coal feed pipe, a furnace gas pipe, and a second-stage gasification nozzle are connected to the lower dense-phase fluidized bed furnace body. The lower dense-phase fluidized bed furnace body, the crushed coal feed pipe, the furnace gas pipe, and the second-stage gasification nozzle together constitute the lower dense-phase fluidized bed gasification section. A quench water pipe and a gasifier gas outlet are provided at the top of the cylindrical furnace body. The quench water pipe and the gasifier gas outlet constitute the upper particle settling and separation section. The fused agglomerate ash separation unit includes a gas chamber shell, which is fixedly connected to the lower end of the lower dense phase fluidized bed furnace body. A conical distributor, shaped like an inverted cone, is installed on the upper part of the gas chamber shell. Gas outlets are evenly distributed on the conical distributor. An annular separation pipe is connected to the lower end of the conical distributor, with the lower end of the annular separation pipe located outside the gas chamber shell. The gas chamber shell, conical distributor, and annular separation pipe together constitute an inlet chamber. A distributor gasifying agent inlet pipe communicating with the inlet chamber is provided on the gas chamber shell. An ash discharge port is provided at the lower part of the annular separation pipe, and a separation outlet is provided at the lower end of the annular separation pipe. The device includes a gasifying agent inlet and a central gasifying burner inside the annular separation tube. The central gasifying burner coincides with the central axis of the annular separation tube, and the outlets of both the annular separation tube and the central gasifying burner are at the same height as the bottom of the conical distributor. The central gasifying burner is provided with a protective water jacket, a fly ash channel, and a gasifying agent channel from the outside to the inside. The central gasifying burner is provided with a protective water jacket inlet, a protective water jacket outlet, a central fly ash feed pipe, and a central gasifying agent inlet pipe. The protective water jacket inlet and outlet are connected to the protective water jacket, the central fly ash feed pipe is connected to the fly ash channel, and the central gasifying agent inlet pipe is connected to the gasifying agent channel. The feed leg fine powder circulation unit includes a primary cyclone separator. The inlet of the primary cyclone separator is connected to the gas outlet of the gasifier. A semi-coke fine powder circulation riser is connected to the lower part of the primary cyclone separator. The lower end of the semi-coke fine powder circulation riser is connected to the lower part of the semi-coke fine powder circulation control pneumatic valve via an inclined pipe. The lower end of the semi-coke fine powder circulation control pneumatic valve is connected to a pneumatic valve steam blower. A fine powder return steam blower is connected to the upper part of the inclined pipe. A semi-coke fine powder feed pipe is connected to the upper part of the semi-coke fine powder circulation control pneumatic valve. The semi-coke fine powder feed pipe is connected to the lower dense phase fluidized bed furnace body.

[0008] Furthermore, a thermal insulation material layer is provided on the inner wall of the cylindrical furnace body, the lower dense phase fluidized bed furnace body, the gas chamber shell, the conical distributor, the annular separation pipe, and the ash discharge port of the separation pipe, and a refractory lining is provided on the inner side of the thermal insulation material layer.

[0009] Furthermore, the lower dense-phase fluidized bed furnace body is inverted conical in shape, and the angle Ω between its conical generatrix and the central axis is 10 to 30°.

[0010] Furthermore, the outer diameter of the fly ash channel is 1 / 3 to 2 / 3 of the inner diameter of the lower end of the conical distributor, and the diameter of the gasifying agent channel is 1 / 4 to 1 / 2 of the inner diameter of the lower end of the conical distributor.

[0011] Furthermore, the cone distributor has an opening ratio of 0.5% to 2%, an aperture of 3 to 8 mm, and an angle α between its cone generatrix and the central axis of 30 to 50°.

[0012] Furthermore, the angle β between the conical generatrix of the upper throat of the annular separation tube and the central axis is 5 to 12°, and the angle θ between the conical generatrix of the lower throat of the annular separation tube and the central axis is 15 to 20°.

[0013] Furthermore, the second-stage gasification nozzle is located at the lower part of the dense phase fluidized bed furnace body, between the lower part of the crushed coal feed pipe and the upper edge of the distributor. The second-stage gasification nozzle is inclined upwards, and the angle ε between the second-stage gasification nozzle and the horizontal line is 10-20°. The extension of its center line is tangent to the central circle. The center of the central circle is located on the axis of the gasifier. A tangent line is drawn at the intersection of the center line of the second-stage gasification nozzle and the outer wall of the lower dense phase fluidized bed furnace body. The angle ʎ between this tangent line and the center line of the second-stage gasification nozzle is 45-75°.

[0014] Compared with the prior art, the present invention has the following advantages: The gasifier of this invention can operate at a pressure of up to 3.0 MPa, has a large processing capacity, and low compression energy consumption. This invention employs selective ash separation and dry slag discharge, resulting in low carbon content in the discharged ash. The gas entrains fine powder and increases the residence time through a high circulation ratio, thereby improving the overall gasification carbon conversion rate. This invention adopts a segmented conversion process to improve the gas-solid contact rate and increase the residence time. Unconverted fly ash fine powder is returned to the high-temperature zone of the central tube through the central burner for efficient conversion. Crushed coal can be used directly, reducing coal grinding power consumption. The overall energy consumption and oxygen consumption of the system are low. This invention employs segmented gasification, resulting in high gasifier volume utilization, high carbon conversion rate, and low risk of slagging. The gasifier in this invention has a simple structure, requires no special refractory materials, is low in cost, is easy to operate, and has a long service life. This invention is applicable to a wide range of coal types and can gasify most coal types in China. Attached Figure Description

[0015] Figure 1 This is a schematic diagram of the gasification furnace of this utility model; Figure 2 This is a schematic diagram of the structure of the fused alumina separation unit of this utility model; Figure 3 This utility model Figure 2 A magnified view of a portion of circle A in the center; Figure 4 This is a schematic diagram showing the tangency between the two-stage gasification nozzle and the central circle of this utility model; Figure 5 This is a flowchart of the coal gasification process of this utility model; In the diagram, 1 is a cylindrical furnace body, 2 is a lower dense-phase fluidized bed furnace body, 3 is a crushed coal feed pipe, 4 is a furnace gas pipe, 5 is a secondary gasification nozzle, 6 is a quench water pipe, 7 is a gasifier gas outlet, 8 is a gas chamber shell, 9 is a conical distributor, 10 is an annular separator, 11 is a distributor gasifying agent inlet pipe, 12 is a separator ash discharge port, 13 is a separator gasifying agent inlet, 14 is a central gasification burner, 15 is a protective water jacket, 16 is a fly ash channel, 17 is a gasifying agent channel, 18 is a protective water jacket inlet, 19 is a protective water jacket outlet, 20 is a central fly ash feed pipe, 21 is a central gasifying agent inlet pipe, 22 is a primary cyclone separator, 23 is a semi-coke fine powder circulation riser, 24 is an inclined pipe, 25 is a semi-coke fine powder circulation control pneumatic valve, 26 is a pneumatic valve steam blower, and 27 is a fine powder return steam blower. 28 Semi-coke fine powder feed pipe, 29 Coal conveyor belt, 30 Vibrating screen, 31 Raw coal crusher, 32 Dryer, 33 No. 1 hoist, 34 Dry crushed coal storage silo, 35 Dry crushed coal conveyor, 36 No. 2 hoist, 37 Crushed coal feed hopper, 38 Rotary feeder, 39 Gasifier, 40 Slag cooler, 41 Ash discharge hopper, 42 Fly ash conveyor, 43 Fly ash collection / cooling tank, 44 Air separator, 45 Air preheater, 46 Superheated steam separator, 47 Coal gas separator, 48 Secondary cyclone separator, 49 Waste heat boiler, 50 Steam superheater, 51 Deoxygenated water preheater, 52 Venturi scrubber, 53 Tray-type water washing tower, 54 Gas-water separator, 55 Coal desulfurization tower, 56 Coal gas pressure regulating valve, 57 Flash evaporator. Detailed Implementation

[0016] To further illustrate the technical solution of this utility model, the following embodiments will be used to further explain this utility model. Example 1

[0017] like Figures 1 to 5 As shown, the method for staged conversion fluidized bed coal gasification includes the following steps: Preparation of raw coal for gasification: Raw coal is fed into vibrating screen 30 via coal conveyor belt 29. Raw coal with a particle size greater than 20mm is crushed into crushed coal with a particle size less than 20mm by raw coal crusher 31. The crushed coal and the raw coal under the screen of vibrating screen 30 are then fed into dryer 32 for drying to make the moisture content <25wt%. The crushed coal with a particle size less than 20mm is fed into dry crushed coal storage silo 34 via No. 1 elevator 33 as raw coal for fluidized bed gasification. First stage of gasification: a. The gasifier 39 is preheated. The preheating air comes from the air distribution cylinder 44, and the preheating gas comes from the gas distribution cylinder 47. The air enters the gasifier 39 through the distributor gasifying agent inlet pipe 11, the separator gasifying agent inlet 13, and the central gasifying agent inlet pipe 21. The gas enters the gasifier 39 through the preheating gas pipe 4. When the temperature at the bottom of the gasifier 39 exceeds 900℃, 1000 Nm³ / h of air and 100 kg / h of steam are introduced through the distributor gasifying agent inlet pipe 11, the separator gasifying agent inlet 13, and the central gasifying agent inlet pipe 21. The steam comes from the superheated steam distribution cylinder 46. The rotary feeder 38 is turned on to feed the crushed coal from the gasifier 39. a) Continuously add gasified pulverized coal through feed pipe 3, operating at an air-to-coal ratio of 2.5–3.5 Nm³ / kg and a steam-to-coal ratio of 0.3–0.6 kg / kg, so that the pulverized coal burns in gasifier 39 to obtain semi-coke oven feed, gradually building up the material inside gasifier 39; b) When the bed pressure drop of the semi-coke oven feed in gasifier 39 reaches 5–10 kPa, switch to air / oxygen-enriched / pure oxygen and steam blast, controlling the temperature at 800–900℃ during the switching process; c) Perform gasification operation at an oxygen-to-coal ratio of 0.4–0.5 Nm³ / kg and a steam-to-coal ratio of 0.5–1.0 kg / kg, stabilizing the bottom temperature of gasifier 39 in the range of 900–1100℃; Second-stage gasification: After the first-stage gasification operation is stable, that is, when the bed pressure drop reaches 5-10 kPa and the bottom temperature of gasifier 39 is stable at 900-1100℃, increase the amount of crushed coal feed until the bed pressure drop of the furnace charge in gasifier 39 reaches 10-15 kPa. Then, open the second-stage gasification nozzle 5 to blow air / oxygen-enriched / pure oxygen and steam. During the opening process, the temperature is controlled at 900-1100℃. Three-stage gasification: The crude coal gas generated from the gasifier 39 enters the secondary cyclone separator 48 through the primary cyclone separator 22. The collected fly ash is sent to the fly ash channel 16 on the central gasification burner 14 through the fly ash collection / cooling tank 43 and the fly ash conveyor 42. During the fly ash feeding process, the air / oxygen-enriched / pure oxygen and steam intake in the central gasification agent intake pipe 21 are increased to ensure that the temperature at the bottom of the gasifier 39 is controlled at 950-1100℃. Ash discharge from the gasifier: During the gasification process, the gas velocity in the conical distributor 9 is 1-3 m / s, and the oxygen concentration in the gas is 10-15 vol; the gas velocity in the annular separator 10 is 4-6 m / s, and the oxygen concentration in the gas is 0-10 vol; the gas velocity in the gasifying agent channel 17 of the central gasification burner 14 is 20-60 m / s, and the oxygen concentration in the gas is 15-60 vol; the gas velocity in the second-stage gasification nozzle 5 is 80-120 m / s, and the oxygen concentration in the gas is 15-60 vol; by controlling the rotation speed of the ash cooler 40, the ash discharge rate is controlled, so that the bed pressure drop of the semi-coke oven material in the gasifier 39 is maintained between 10-15 kPa; Purification and waste heat recovery of crude gas: Quenching water is injected into the gas outlet 7 of the gasifier to ensure the inlet temperature of the primary cyclone separator 22 is <900℃. The crude gas is separated by the primary cyclone separator 22, and the collected semi-coke fine powder is returned to the lower dense-phase fluidized bed gasification section of the gasifier 39 via the semi-coke fine powder circulation riser 23, the semi-coke fine powder circulation control pneumatic valve 25, and the semi-coke fine powder feed pipe 28 to participate in the reaction again. The crude gas enters the secondary cyclone separator 48, where the collected... Fly ash is sent to the fly ash channel 16 on the central gasification burner 14 via fly ash collection / cooling tank 43 and fly ash conveyor 42; the high-temperature coal gas from coarse separation passes through waste heat boiler 49, steam superheater 50, and deoxygenated water preheater 51, and the coal gas temperature is reduced to 50-170℃ before entering Venturi scrubber 52 and tray-type water washing tower 53, gas-water separator 54 and coarse desulfurization tower 55, and after further cooling and dust removal, it is output to the coal gas purification section via coal gas pressure regulating valve 56. Gasifier shutdown: During normal shutdown, first stop the supply of air / oxygen-enriched / pure oxygen into the gasifier 39; close the central fly ash feed pipe 20 on the central gasification burner 14, stop adding fly ash into the gasifier 39, and stop adding crushed coal into the gasifier 39; disconnect the pipeline between the secondary cyclone separator 48 and the waste heat boiler 49, and vent the crude coal gas from the secondary cyclone separator 48 to reduce the pressure inside the gasifier 39 to atmospheric pressure; then, increase the speed of the slag cooler 40, increase the ash discharge, and simultaneously increase the fluidized bed steam consumption, keeping the furnace temperature below 900℃. After the furnace charge is discharged, stop the steam supply, and finally, purge and clean the gasifier 39 with steam and air in succession.

[0018] The segmented conversion gasifier includes a pyrolysis gasification reactor, a molten aggregate ash separation unit, and a feed leg fine powder circulation unit. The pyrolysis gasification reactor includes a cylindrical furnace body 1. A lower dense-phase fluidized bed furnace body 2 is fixedly connected to the lower end of the cylindrical furnace body 1. The lower dense-phase fluidized bed furnace body 2 is inverted conical in shape, with an angle Ω between its generatrix and central axis of 10–30°. A pulverized coal feed pipe 3, a furnace gas pipe 4, and a secondary gasification nozzle 5 are connected to the lower dense-phase fluidized bed furnace body 2. The lower dense-phase fluidized bed furnace body 2, pulverized coal feed pipe 3, furnace gas pipe 4, and secondary gasification nozzle 5 together constitute the lower dense-phase fluidized bed gasification section. The secondary gasification nozzle 5 is located at the lower part of the lower dense-phase fluidized bed furnace body 2 and is located at the lower end of the pulverized coal feed pipe 3. Between the lower part and the upper edge of the distributor, the two-stage gasification nozzle 5 is inclined upwards, and the angle ε between the two-stage gasification nozzle 5 and the horizontal line is 10-20°. The extension of its center line is tangent to the central circle. The center of the central circle is located on the axis of the gasifier. A tangent line is drawn at the intersection of the center line of the two-stage gasification nozzle 5 and the outer wall of the lower dense phase fluidized bed furnace body 2. The angle ʎ between the tangent line and the center line of the two-stage gasification nozzle 5 is 45-75°. A quench water pipe 6 and a gasifier gas outlet 7 are provided at the top of the cylindrical furnace body 1. The quench water pipe 6 and the gasifier gas outlet 7 constitute the upper particle settling and separation section. The fused agglomerate ash separation unit includes a gas chamber shell 8, which is fixedly connected to the lower end of the lower dense phase fluidized bed furnace body 2. A conical distributor 9 is installed on the upper part of the gas chamber shell 8. The conical distributor 9 is inverted conical in shape and has gas outlets evenly distributed on it. The opening ratio of the conical distributor 9 is 0.5% to 2%, the aperture is 3 to 8 mm, and the angle α between its conical generatrix and the central axis is 30 to 50°. An annular separation pipe 10 is connected to the lower end of the conical distributor 9, and the lower end of the annular separation pipe 10 is located outside the gas chamber shell 8. The gas chamber shell 8, the conical distributor 9, and the annular separator 10 together constitute the air inlet chamber. The angle β between the generatrix of the cone at the upper throat of the annular separator 10 and the central axis is 5–12°, and the angle θ between the generatrix of the cone at the lower throat of the annular separator 10 and the central axis is 15–20°. A distributor gasifying agent inlet pipe 11 communicating with the air inlet chamber is provided on the gas chamber shell 8. A separator ash discharge port 12 is provided at the lower part of the annular separator 10, and a separator gasifying agent inlet 13 is provided at the lower end of the annular separator 10. A gasifying agent inlet 13 is provided inside the annular separator 10. A central gasification burner 14 is provided, with its central axis coinciding with that of the annular separation pipe 10. The outlets of both the annular separation pipe 10 and the central gasification burner 14 are at the same height as the bottom of the conical distributor 9. The central gasification burner 14 is provided with a protective water jacket 15, a fly ash channel 16, and a gasifying agent channel 17 arranged sequentially from the outside to the inside. A protective water jacket inlet 18, a protective water jacket outlet 19, a central fly ash feed pipe 20, and a central gasifying agent inlet pipe 21 are also provided on the central gasification burner 14. The protective water jacket inlet 18 and the protective water jacket outlet 19 are connected to the protective water... The jacket 15 is connected, the central fly ash feed pipe 20 is connected to the fly ash channel 16, and the central gasifying agent inlet pipe 21 is connected to the gasifying agent channel 17. The outer diameter of the fly ash channel 16 is 1 / 3 to 2 / 3 of the inner diameter of the lower end of the conical distributor 9, and the diameter of the gasifying agent channel 17 is 1 / 4 to 1 / 2 of the inner diameter of the lower end of the conical distributor 9. Thermal insulation material layers are provided on the inner walls of the cylindrical furnace body 1, the lower dense phase fluidized bed furnace body 2, the gas chamber shell 8, the conical distributor 9, the annular separation pipe 10, and the ash discharge port 12 of the separation pipe. A refractory lining is provided on the inner side of the thermal insulation material layer.

[0019] The feed fine powder circulation unit includes a primary cyclone separator 22. The inlet of the primary cyclone separator 22 is connected to the gas outlet 7 of the gasifier. The lower part of the primary cyclone separator 22 is connected to a semi-coke fine powder circulation riser 23. The lower end of the semi-coke fine powder circulation riser 23 is connected to the lower part of the semi-coke fine powder circulation control pneumatic valve 25 through an inclined pipe 24. The lower end of the semi-coke fine powder circulation control pneumatic valve 25 is connected to a pneumatic valve steam blowing pipe 26. The upper part of the inclined pipe 24 is connected to a fine powder return steam blowing pipe 27. The upper part of the semi-coke fine powder circulation control pneumatic valve 25 is connected to a semi-coke fine powder feed pipe 28. The semi-coke fine powder feed pipe 28 is connected to the lower dense phase fluidized bed furnace body 2. Example 2

[0020] In the first stage of gasification, the air-to-coal ratio in step a is 3.5 Nm³ / kg, and the steam-to-coal ratio is 0.6 kg / kg. In step c, the oxygen-to-coal ratio is 0.4 Nm³ / kg, and the steam-to-coal ratio is 0.5 kg / kg.

[0021] In the slag discharge step of the gasifier, the gas velocity in the conical distributor 9 is 3 m / s, and the oxygen concentration in the gas is 10 vol; the gas velocity in the annular separator 10 is 6 m / s, and the oxygen concentration in the gas is 0 vol; the gas velocity in the gasifying agent channel 17 of the central gasifying burner 14 is 60 m / s, and the oxygen concentration in the gas is 15 vol%. The gas velocity in the second-stage gasifying nozzle 5 is 120 m / s, and the oxygen concentration in the gas is 15 vol.

[0022] The cone distributor 9 in the segmented conversion gasifier has an opening ratio of 0.5%, an aperture of 8 mm, and an included angle α of 30°.

[0023] The angle β between the conical generatrix of the upper throat of the annular separation tube 10 and the central axis is 12°, and the angle θ between the conical generatrix of the lower throat of the annular separation tube 10 and the central axis is 15°.

[0024] The angle Ω between the generatrix of the lower dense phase fluidized bed furnace body 2 and the central axis is 30°, and the angle ε between the second-stage gasification nozzle 5 and the horizontal line is 10°.

[0025] A tangent is drawn at the intersection of the centerline of the second-stage gasification nozzle 5 and the outer wall of the lower dense fluidized bed furnace body 2. The angle ʎ between the tangent and the centerline of the second-stage gasification nozzle 5 is 45°. Example 3

[0026] In the first stage of gasification, the air-to-coal ratio in step a is 2.5 Nm³ / kg, and the steam-to-coal ratio is 0.3 kg / kg. In step c, the oxygen-to-coal ratio is 0.5 Nm³ / kg, and the steam-to-coal ratio is 1.0 kg / kg.

[0027] In the slag discharge step of the gasifier, the gas velocity in the conical distributor 9 is 1 m / s, and the oxygen concentration in the gas is 15 vol; the gas velocity in the annular separator 10 is 4 m / s, and the oxygen concentration in the gas is 10 vol; the gas velocity in the gasifying agent channel 17 of the central gasifying burner 14 is 20 m / s, and the oxygen concentration in the gas is 60 vol; the gas velocity in the second-stage gasifying nozzle 5 is 80 m / s, and the oxygen concentration in the gas is 60 vol.

[0028] The cone distributor 9 in the segmented conversion gasifier has an opening ratio of 2%, an aperture of 3 mm, and an included angle α of 50°.

[0029] The angle β between the conical generatrix of the upper throat of the annular separation tube 10 and the central axis is 5°, and the angle θ between the conical generatrix of the lower throat of the annular separation tube 10 and the central axis is 20°.

[0030] The angle Ω between the generatrix of the lower dense phase fluidized bed furnace body 2 and the central axis is 10°, and the angle ε between the second-stage gasification nozzle 5 and the horizontal line is 20°.

[0031] A tangent is drawn at the intersection of the centerline of the second-stage gasification nozzle 5 and the outer wall of the lower dense fluidized bed furnace body 2. The angle ʎ between the tangent and the centerline of the second-stage gasification nozzle 5 is 60°. Example 4

[0032] In the first stage of gasification, the air-to-coal ratio in step a is 0.4 Nm³ / kg, and the steam-to-coal ratio is 0.5 kg / kg. In step c, the oxygen-to-coal ratio is 0.45 Nm³ / kg, and the steam-to-coal ratio is 0.7 kg / kg.

[0033] In the slag discharge step of the gasifier, the gas velocity in the conical distributor 9 is 2 m / s, and the oxygen concentration in the gas is 13 vol; the gas velocity in the annular separator 10 is 5 m / s, and the oxygen concentration in the gas is 6 vol; the gas velocity in the gasifying agent channel 17 of the central gasifying burner 14 is 40 m / s, and the oxygen concentration in the gas is 50 vol; the gas velocity in the second-stage gasifying nozzle 5 is 100 m / s, and the oxygen concentration in the gas is 40 vol.

[0034] The cone distributor 9 in the segmented conversion gasifier has an opening ratio of 1%, an aperture of 4 mm, and an included angle α of 40°.

[0035] The angle β between the conical generatrix of the upper throat of the annular separation tube 10 and the central axis is 8°, and the angle θ between the conical generatrix of the lower throat of the annular separation tube 10 and the central axis is 18°.

[0036] The angle Ω between the generatrix of the lower dense phase fluidized bed furnace body 2 and the central axis is 20°, and the angle ε between the second-stage gasification nozzle 5 and the horizontal line is 15°.

[0037] A tangent is drawn at the intersection of the centerline of the second-stage gasification nozzle 5 and the outer wall of the lower dense fluidized bed furnace body 2. The angle ʎ between the tangent and the centerline of the second-stage gasification nozzle 5 is 50°. Example 5

[0038] In the first stage of gasification, the air-to-coal ratio in step a is 0.5 Nm³ / kg, and the steam-to-coal ratio is 1.0 kg / kg. In step c, the oxygen-to-coal ratio is 0.4 Nm³ / kg, and the steam-to-coal ratio is 0.6 kg / kg.

[0039] In the slag discharge step of the gasifier, the gas velocity in the conical distributor 9 is 3 m / s, and the oxygen concentration in the gas is 13 vol; the gas velocity in the annular separator 10 is 5 m / s, and the oxygen concentration in the gas is 5 vol; the gas velocity in the gasifying agent channel 17 of the central gasifying burner 14 is 50 m / s, and the oxygen concentration in the gas is 50 vol; the gas velocity in the second-stage gasifying nozzle 5 is 90 m / s, and the oxygen concentration in the gas is 55 vol.

[0040] The cone distributor 9 in the segmented conversion gasifier has an opening ratio of 1.5%, an aperture of 6 mm, and an included angle α of 45°.

[0041] The angle β between the conical generatrix of the upper throat of the annular separation tube 10 and the central axis is 10°, and the angle θ between the conical generatrix of the lower throat of the annular separation tube 10 and the central axis is 20°.

[0042] The angle Ω between the generatrix of the lower dense phase fluidized bed furnace body 2 and the central axis is 15°, and the angle ε between the second-stage gasification nozzle 5 and the horizontal line is 15°.

[0043] A tangent is drawn at the intersection of the centerline of the second-stage gasification nozzle 5 and the outer wall of the lower dense fluidized bed furnace body 2. The angle ʎ between the tangent and the centerline of the second-stage gasification nozzle 5 is 75°.

[0044] The raw coal parameters under the conditions of Examples 2-5 are listed in Table 1.

[0045] Table 1 shows the parameters for different types of raw coal.

[0046] The synthesis gas produced by segmented conversion fluidized bed coal gasification under the conditions of Examples 2-5 is listed in Table 2.

[0047] Table 2 shows the composition of syngas produced by staged conversion fluidized bed coal gasification under different conditions.

[0048] The foregoing has shown and described the main features and advantages of this utility model. It will be apparent to those skilled in the art that this utility model is not limited to the details of the exemplary embodiments described above, and that it can be implemented in other specific forms without departing from the spirit or essential characteristics of this utility model. Therefore, the embodiments should be considered exemplary and non-limiting in all respects. The scope of this utility model is defined by the appended claims rather than the foregoing description, and thus all variations falling within the meaning and scope of equivalents of the claims are intended to be included within this utility model.

[0049] Furthermore, it should be understood that although this specification describes embodiments, not every embodiment contains only one independent technical solution. This narrative style is merely for clarity. Those skilled in the art should consider the specification as a whole, and the technical solutions in each embodiment can also be appropriately combined to form other embodiments that can be understood by those skilled in the art.

Claims

1. A staged reformer gasifier, applied to a staged reformer fluidized bed coal gasification method, characterized in that: It includes a pyrolysis gasification reactor, a melt-polymerized ash separation unit, and a feed leg fine powder recycling unit; The pyrolysis gasification reactor includes a cylindrical furnace body (1), and a lower dense fluidized bed furnace body (2) is fixedly connected to the lower end of the cylindrical furnace body (1). A crushed coal feed pipe (3), a furnace gas pipe (4), and a second-stage gasification nozzle (5) are connected to the lower dense fluidized bed furnace body (2). The lower dense fluidized bed furnace body (2), the crushed coal feed pipe (3), the furnace gas pipe (4), and the second-stage gasification nozzle (5) together constitute the lower dense fluidized bed gasification section. A quench water pipe (6) and a gasifier gas outlet (7) are provided at the top of the cylindrical furnace body (1). The quench water pipe (6) and the gasifier gas outlet (7) constitute the upper particle settling and separation section. The fused agglomerate ash separation unit includes a gas chamber shell (8), which is fixedly connected to the lower end of the lower dense phase fluidized bed furnace body (2). A conical distributor (9) is installed on the upper part of the gas chamber shell (8). The conical distributor (9) is inverted cone shape, and gas outlets are evenly distributed on the conical distributor (9). An annular separation pipe (10) is connected to the lower end of the conical distributor (9). The lower end of the annular separation pipe (10) is located outside the gas chamber shell (8). The gas chamber shell (8), the conical distributor (9), and the annular separation pipe (10) together constitute the inlet chamber. A distributor gasifying agent inlet pipe (11) communicating with the inlet chamber is provided on the gas chamber shell (8). A separation pipe ash discharge port (12) is provided at the lower part of the annular separation pipe (10). A separation pipe gasifying agent inlet port (13) is provided at the lower end of the annular separation pipe (10). A central gasification burner (14) is installed inside the annular separation tube (10). The central gasification burner (14) coincides with the central axis of the annular separation tube (10), and the outlets of the annular separation tube (10) and the central gasification burner (14) are at the same height as the bottom of the conical distributor (9). The central gasification burner (14) is provided with a protective water jacket (15), a fly ash channel (16), and a gasifying agent channel (17) from the outside to the inside. The gasification burner (14) is provided with a protective water jacket inlet (18), a protective water jacket outlet (19), a central fly ash feed pipe (20), and a central gasifying agent inlet pipe (21). The protective water jacket inlet (18) and the protective water jacket outlet (19) are connected to the protective water jacket (15). The central fly ash feed pipe (20) is connected to the fly ash channel (16). The central gasifying agent inlet pipe (21) is connected to the gasifying agent channel (17). The material leg fine powder circulation unit includes a primary cyclone separator (22). The inlet of the primary cyclone separator (22) is connected to the gas outlet (7) of the gasifier. The lower part of the primary cyclone separator (22) is connected to a semi-coke fine powder circulation riser (23). The lower end of the semi-coke fine powder circulation riser (23) is connected to the lower part of the semi-coke fine powder circulation control pneumatic valve (25) through an inclined pipe (24). The lower end of the semi-coke fine powder circulation control pneumatic valve (25) is connected to a pneumatic valve steam blow pipe (26). The upper part of the inclined pipe (24) is connected to a fine powder return steam blow pipe (27). The upper part of the semi-coke fine powder circulation control pneumatic valve (25) is connected to a semi-coke fine powder feed pipe (28). The semi-coke fine powder feed pipe (28) is connected to the lower dense phase fluidized bed furnace body (2).

2. The segmented conversion gasifier according to claim 1, characterized in that: A thermal insulation material layer is provided on the inner walls of the cylindrical furnace body (1), the lower dense phase fluidized bed furnace body (2), the gas chamber shell (8), the conical distributor (9), the annular separation pipe (10), and the ash discharge port (12) of the separation pipe, and a refractory lining is provided on the inner side of the thermal insulation material layer.

3. The segmented conversion gasifier according to claim 1, characterized in that: The lower dense fluidized bed furnace body (2) is inverted cone shape, and the angle Ω between its cone generatrix and the central axis is 10 to 30°.

4. The segmented conversion gasifier according to claim 1, characterized in that: The outer diameter of the fly ash channel (16) is 1 / 3 to 2 / 3 of the inner diameter of the lower end of the conical distributor (9), and the diameter of the gasifying agent channel (17) is 1 / 4 to 1 / 2 of the inner diameter of the lower end of the conical distributor (9).

5. The segmented conversion gasifier according to claim 1, characterized in that: The cone distributor (9) has an opening ratio of 0.5% to 2%, an aperture of 3 to 8 mm, and an angle α between its cone generatrix and the central axis of 30 to 50°.

6. The segmented conversion gasifier according to claim 1, characterized in that: The angle β between the conical generatrix of the upper throat of the annular separation tube (10) and the central axis is 5 to 12°, and the angle θ between the conical generatrix of the lower throat of the annular separation tube (10) and the central axis is 15 to 20°.

7. The staged conversion gasifier according to claim 1, characterized in that: The second-stage gasification nozzle (5) is located at the lower part of the lower dense phase fluidized bed furnace body (2), and between the lower part of the crushed coal feed pipe (3) and the upper part of the distributor. The second-stage gasification nozzle (5) is inclined upwards, and the angle ε between the second-stage gasification nozzle (5) and the horizontal line is 10-20°. The extension of its center line is tangent to the center circle. The center of the center circle is located on the axis of the gasifier. A tangent line is drawn at the intersection of the center line of the second-stage gasification nozzle (5) and the outer wall of the lower dense phase fluidized bed furnace body (2). The angle ʎ between the tangent line and the center line of the second-stage gasification nozzle (5) is 45-75°.

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