Gasification furnace for producing oil gas and water gas

Abstract

The invention discloses a gasification furnace for producing oil gas and water gas, which is characterized in that hydrogen with methane content of less than 5% and temperature of normal temperature to 200 DEG C is subjected to hydrogenation reaction with a high-temperature coke hydrogenation gasification layer, a low-temperature coke hydrogenation gasification layer and semicoke in sequence; according to the method, the methane-hydrogen-rich coal gas with relatively high methane concentration is obtained, more methanation reaction heat is also obtained, the methane-hydrogen-rich coal gas carrying heat is used for heating, hydrogenation and dry distillation of the dried coal, and the methane yield is weakened by the partial pressure of gas-phase methane, so that the yield of oil is increased, the oil-rich coal gas is obtained, and the energy consumption is reduced. Meanwhile, the heat consumption of the system is also reduced. Raw material coal is firstly prepared into oil gas, and then oxygen-enriched water vapor gasification is carried out to produce water gas; water gas condensate is reduced, phenolic compounds are not contained, and the treatment cost is low; the oil gas and water gas production method can be used for industries such as coal natural gas, coal fuel oil, IGCC (integrated gasification combined cycle) coal-fired power generation and the like.

Description

Technical Field

[0001] The invention relates to the field of coal-based energy chemical industry, and in particular to a gasifier for producing oil gas and water gas. Background Art

[0003] The current coal-to-oil and coal-to-natural gas, whether it is the two-step method of coal gasification followed by synthesis of oil and gas, or the one-step method of direct coal hydrogenation to produce oil and gas, are all due to the complex process route and low energy conversion efficiency of the process. The coal-to-oil rate is only 43%, consuming 3.4 tons of standard coal per ton of oil; the coal-to-natural gas rate is only 50%, consuming 2.5 tons of standard coal per km. 3 ; Equipment investment is high, coal-to-oil 160 billion yuan / 10 million tons, coal-to-natural gas 28 billion yuan / 4 billion m 3 ; High water consumption, coal-to-oil consumes 6 tons of water per ton of oil, coal-to-natural gas consumes 6 tons / km 3 ; Severe environmental pollution, high sewage treatment costs and high CO2 emissions.

[0004] The reasons for the low efficiency of the current one-step coal direct hydrogenation oil production are: first, the process pressure is as high as 20MPa, and the equipment investment is large; second, the carbon conversion rate is low, and the residue contains up to 40% carbon, which needs to be reheated in a special gasifier to generate CO again; third, the entrained flow coal gasification hydrogen production, because in the entrained flow gasification process, the hydrogen element in the coal is in the form of hydrocarbons, which are first pyrolyzed into gaseous hydrocarbons below 700°C, and then react with O2 in the air flow to generate CO2 and H2O to release heat, so that the furnace temperature reaches 1300-1700°C. Therefore, a considerable part of the high furnace temperature of the entrained flow is contributed by the combustion of hydrogen, resulting in a low molar fraction of hydrogen in the coal gas and a particularly high CO component, and CO must be converted to hydrogen after conversion, that is, this hydrogen production process is essentially to first burn the H2 in the coal, and then use the C element in the coal to produce CO, and CO can only be converted to H2 after conversion, so the current one-step coal direct hydrogenation process to produce C n H 2n+2 There are also many disadvantages mentioned above.

[0005] CN110358579B discloses a production method capable of simultaneously obtaining oil gas and water gas. Although a residual coke downward movement channel is provided between the water gas section and the oil gas section so as to unload the residual coke from the oil gas section into the water gas section, there is no control device for the amount of residual coke downward movement in the residual coke downward movement channel, and thus the amount of residual coke downward movement cannot be controlled according to production needs. Since the invention requires the use of a gasifying agent of ≥15% methane and 30-80% hydrogen, and since the initial concentration of methane is too high, in order to obtain the heat required for pyrolysis of raw coal to produce oil gas, the pressure must be increased to 6-12MPa. In order to increase the yield of C+2H2=CH4, the heat must be increased, which will undoubtedly greatly increase the investment in the device, or the temperature of the hydrogen gasifying agent entering the furnace must be increased to above 300°C, which is obviously not economical; in the oil-coal gas section, a stirrer and a sieve plate are respectively set to break the adhesion of the raw coal. Due to the interaction between the static sieve plate and the rotating stirrer, a large amount of coal foam is generated, which increases the bed resistance and the resistance difference in the same plane, thereby causing gas deviation. Summary of the invention

[0006] The purpose of the present invention is to provide a gasifier for producing oil gas and water gas in view of the above-mentioned deficiencies. Through this scheme, the generation of coal foam in the oil gas section can be greatly reduced, and at the same time, the residual coke flowing down from the oil gas section into the water gas section can be controlled; thereby, the material layer height in the water gas section can be controlled; the temperature of the hydrogen gasifying agent entering the furnace can adopt the intake air of room temperature and methane concentration less than 5%, which not only reduces the heat energy consumption in the production of oil gas, but also effectively reduces the process pressure and thus reduces the investment in the device.

[0007] The present invention is achieved through the following scheme:

[0008] A gasifier for producing oil gas and water gas, comprising an oxygen and water vapor gasification agent inlet, a grate, a raw coal gasification bed, a stirrer, a coal distributor and a coal lock, a pressurized water jacket shell, a crude coal gas outlet and a hydrocarbon-rich coal gas outlet, wherein the raw coal gasification bed is divided into an ash layer, an oxygen combustion layer, a water gas generation layer, a methane generation layer and a raw coal drying layer from bottom to top, and oxygen and water vapor react with the raw coal from bottom to top to generate water gas;

[0009] The pressurized moving bed gasifier is designed to be a structure of upper and lower sections connected by a pressure-bearing cylinder (8) of a residual coke downward moving channel in which an isolation area (8B) and a circumferentially driven spiral pusher (8A) are arranged;

[0010] The lower section is designed as a water-gas section that uses a mixed gasification agent of oxygen and water vapor to produce hydrogen and carbon monoxide using the residual coke from the oil-gas section as a raw material;

[0011] The upper section is designed to use methane ≤ 5%, hydrogen 80-95%, CO+CO2+H2O+N2 ≤ 5%, H2S ≤ 2%, i.e., a normal temperature hydrogen gasification agent with hydrogen as the main component, to directly produce an oil-coal gas section with oil as the main product from raw coal, and the height-to-diameter ratio of the gasified raw coal bed is 3-6;

[0012] The oil, coal and gas sections are designed from bottom to top as follows:

[0013] A high-temperature coke hydrogenation gasification layer (13) is provided at the bottom with a hydrogen gasification agent bottom inlet (11), an annular channel (10A), a conical gas distribution component (10), a central bottom gas inlet pipe (11A), and a central bottom gas distribution component (12);

[0014] A low-temperature coke hydrogenation gasification layer (13A) is provided at the lower part thereof with a central inlet for hydrogen gasification agent (11B), an annular pipe (11D), a central annular gas distribution component (11F), a central central gas inlet sleeve (11C), and a central central gas distribution component (11E);

[0015] Semi-coke hydrogenation rapid gasification layer (14);

[0016] The hydrogenation pyrolysis distillation layer (17) is provided with a low-temperature stirring blade (16), a debonding component (15), a rotating disk (15D), a supporting wheel, a rib plate, a support, and a transmission shaft (15E); the low-temperature stirring blade (16), the debonding component (15) and the rotating disk (15D) connected thereto are driven to rotate by the transmission shaft (15E), so as to break the adhesion formed by the pyrolysis distillation of the coal; the weight of the raw coal is finally carried on the pressure-bearing shell (20) of the oil-coal-gas section through the debonding component (15) and the rotating disk (15D) connected thereto, the rotatable supporting wheel, and the stationary rib plate and the support; the transmission shaft (15E) for driving the low-temperature stirring blade (16), the debonding component (15) and the rotating disk (15D) to rotate is tubular so as to be inserted into the stationary central bottom air inlet pipe (11A) and the hydrogen central middle air inlet sleeve (11C);

[0017] A drying layer (18);

[0018] 60-70% of the total amount of hydrogen gasifying agent is uniformly introduced into the lower circular section of the high-temperature coke hydrogenation gasification layer (13) through the bottom inlet (11) of the oil-coal gas section, the annular channel (10A), the conical gas distribution component (10), the central bottom gas inlet pipe (11A), and the central bottom gas distribution component (12), and then reversely exchanges heat with the descending high-temperature coke at 1050°C, heating the normal-temperature hydrogen gasifying agent to 850°C, causing the hydrogen in the gasifying agent to undergo an exothermic methanogenic reaction of C+2H2→CH4 with the active carbon element in the high-temperature coke, while increasing the methane content in the gaseous phase gasifying agent, and also increasing the temperature of the top of the high-temperature coke hydrogenation gasification layer (13) to 1050°C, or a temperature below the ash melting point of coal, so that the gaseous phase methane concentration reaches The gas moves upward and mixes with the room temperature hydrogen gasifying agent which accounts for 30-40% of the total amount of hydrogen gasifying agent from the middle annular gas distributing member (11F) and the central middle gas distributing member (11E), and then the temperature drops to 800°C and enters the low temperature coke hydrogenation gasification layer (13A), where the hydrogen in the gas phase continues to react with the active carbon element in the coke to undergo an exothermic methanogenic reaction of C+2H2→CH4, thereby increasing the methane content in the gas phase gasifying agent to 25-30% and also increasing the temperature of the top of the low temperature coke hydrogenation gasification layer (13A) to 900-950°C; the gas phase gas continues to move upward and enters the semi-coke hydrogenation rapid gasification layer (14), where the hydrogen in the gas phase reacts with the solid unsaturated hydrocarbon C containing abundant active carbon elements in the semi-coke to react with the solid unsaturated hydrocarbon C containing abundant active carbon elements. X H Y Rapid hydrogenation reaction: C X H Y +(2X-0.5Y)H2→XCH4, so that the gas phase methane concentration rises to 35-45%, and the 600°C semi-coke from the hydropyrolysis and distillation layer (17) is heated to 800°C; the gas phase gas continues to ascend and enters the hydropyrolysis and distillation layer (17), and the gas phase gas heats the coal particles from the drying layer (18) and causes them to be pyrolyzed and distilled, and while precipitating and gasifying coal tar and realizing the production of oil and coal gas, it also pyrolyzes part of methane, so that the gas phase methane concentration rises to 40 -50%; the oil-coal gas continues to ascend and enter the drying layer (18), bringing heat into the drying layer (18), raising the temperature of the drying layer, causing the physical water carried by the coal particles to vaporize in the drying layer (18) and enter the gas phase, thereby drying the raw coal; at this point, the oil-coal gas rich in methane, coal tar gas, hydrogen, and water vapor leaves the drying layer (18), and leaves the oil-coal gas section successively through the annular space between the coal distributor (19) and the water-jacketed pressure shell (20) of the oil-coal gas section, and the oil-coal gas outlet (21).

[0019] Based on the above-mentioned gasification furnace for producing oil gas and water gas, the raw coal enters the drying layer after entering the furnace from the top of the furnace. After being heated by the rising hydrocarbon-rich oil gas to precipitate water, the temperature rises to 300-350°C and moves downward to the hydrogenation pyrolysis distillation layer. The polycarbons in the coal are softened, fused, cracked, and gasified by heat. Due to the constraints of its phase equilibrium, the amount of methane generated will be relatively reduced, and the hydrogen element in the coal will not be pyrolyzed into single H2 molecules and enter the gas phase, thereby increasing the generation of gaseous polycarbons and further improving the yield of gaseous polycarbons; the raw coal becomes semi-coke with a large amount of activated carbon elements attached at 600°C;

[0020] The semi-coke enters the semi-coke hydrogenation rapid gasification layer under the push of the debonding component, and contacts with the oil and coal gas containing methane and polycarbons from bottom to top in countercurrent. The aromatic hydrocarbons and unsaturated hydrocarbons containing active carbon elements attached to the semi-coke rapidly undergo hydrogenation saturation reaction with the hydrogen elements in the gas phase and release heat, generating a large amount of saturated hydrocarbon methane that enters the gas phase, turning the semi-coke into coke with a temperature of 750-800℃.

[0021] The coke continues to move slowly downward under the action of gravity, enters the low-temperature coke hydrogenation gasification layer, and contacts with the methane hydrogen gasification agent from bottom to top in countercurrent. While heating the upward methane hydrogen gasification agent, the actual concentration of gaseous methane is still less than the chemical equilibrium concentration of C+2H2=CH4, and the high temperature increases the molecular activation kinetic energy of coke and hydrogen, which in turn promotes the exothermic reaction of C+2H2=CH4 to generate methane, and makes the hot spot temperature of the low-temperature coke hydrogenation gasification layer reach 900-950℃;

[0022] The coke continues to move slowly downward under the action of gravity, and after exchanging part of its heat with the low-methane hydrogen gasifier mixed with the room-temperature hydrogen gasifier from the middle annular gas distribution component and the central middle gas distribution component, it enters the high-temperature coke hydrogenation gasification layer. Since the methane content in the hydrogen gasifier entering the high-temperature coke hydrogenation gasification layer is less than 5%, its gas phase concentration is still much lower than the equilibrium concentration under its designed process temperature and pressure. Therefore, in the high-temperature coke hydrogenation gasification layer, an exothermic reaction of C+2H2=CH4 to generate methane will inevitably occur, and the hot spot temperature of the high-temperature coke hydrogenation gasification layer will reach 1050°C, or a temperature below the ash melting point of coal;

[0023] The residual coke continues to move downward, and after countercurrent contact and heat exchange with the hydrogen gasifying agent from the conical gas distribution component and the center bottom gas distribution component, the temperature is reduced to 200-400℃, and then it enters the water-gas section through the isolation area and the spiral pusher; in the water vapor gasification layer, it reacts with the high-temperature water vapor from bottom to top to form C+H2O=CO+H2 water-gas, so that most of the carbon elements in the residual coke are converted into CO; the residual coke containing a small amount of carbon elements continues to move downward and enters the oxidation combustion layer; due to the strong oxidizing properties of oxygen, the remaining carbon elements in the residual coke burn rapidly, so that the temperature of the oxidation layer reaches a temperature above 1000℃ and below the ash melting point, which not only provides huge heat for the endothermic water-gas reaction, but also burns the residual coke into ash.

[0024] Based on the above-mentioned gasifier for producing oil gas and water gas, the temperature of the hydrogen gasifying agent is 50-200°C; the raw coal entering the furnace undergoes drying, carbonization, rapid gasification of semi-coke hydrogenation, low-temperature coke hydrogenation gasification, and high-temperature coke hydrogenation gasification from top to bottom in the oil gas section, and the total mass is reduced by 40-50% depending on the type of coal, ash content, and moisture content, and the carbon element is reduced by 30-50% to become residual coke.

[0025] Based on the above-mentioned gasifier for producing oil gas and water gas, the raw coal is lignite, bituminous coal, coke, anthracite, or various carbon-containing solid materials with a bonding index G≤20.

[0026] Based on the above-mentioned gasification furnace for producing oil gas and water gas, when non-caking coal is used, low-temperature stirring blades (16) are not provided in the gasification furnace.

[0027] Based on the above-mentioned gasification furnace for producing oil gas and water gas, the height-to-diameter ratio of the gasification bed in the oil gas section is inversely proportional to the gasification activity of the raw coal. The height-to-diameter ratio of high-activity coal coke is small, and the height-to-diameter ratio of low-activity coal coke is large. The inner diameter of the pressurized moving bed gasifier is 1.2 to 2 meters, or 2.2 to 4 meters, or 4.2 to 6 meters; the working pressure is 3 to 5 MPa, or 5.1 to 8 MPa.

[0028] Based on the above-mentioned gasifier for producing oil gas and water gas, the particle size of the raw coal or briquette is 3-10 mm, or 11-40 mm, or 41-80 mm.

[0029] Based on the above-mentioned gasifier for producing oil gas and water gas, 2-5% water vapor is added to the hydrogen gasifying agent (11) entering the oil gas section; the cooling water of the pressure shell jacket of the oil gas section and the cooling water of the pressure shell jacket of the water gas section are circulated separately.

[0030] Based on the above-mentioned gasification furnace for producing oil gas and water gas, a medium-temperature coke hydrogenation gasification layer is set between the high-temperature coke hydrogenation gasification layer (13) and the low-temperature coke hydrogenation gasification layer (13A) to increase the contact time between hydrogen and coke and improve the methane generation rate.

[0031] Based on the above-mentioned gasifier for producing oil gas and water gas, the slag removal method of the water gas section is a dry slag removal gasification method below the ash melting point temperature, or a molten slag gasification method above the ash melting point temperature.

[0032] In summary, due to the adoption of the above technical solution, the beneficial effects of the present invention are:

[0033] 1. The stationary sieve plate in CN110358579B is eliminated, thus greatly reducing the coal foam generated in the oil, coal and gas section;

[0034] 2. Since the coke hydrogenation gasification layer in CN110358579B is designed as a high-temperature coke hydrogenation gasification layer and a low-temperature coke hydrogenation gasification layer, not only the methane yield is increased, but also due to the increase in the heat of the methanation reaction, the temperature of the hydrogen gasifier can be reduced from the original more than 300°C to room temperature and the methane concentration of less than 5% of the inlet gas, which effectively reduces the heat energy consumption of oil and coal gas production, effectively reduces the process pressure and thus reduces the investment in the device;

[0035] 3. Since the residual coke downward movement channel in CN110358579B is designed as a residual coke downward movement channel structure with an isolation zone and a circumferentially driven spiral pusher arranged therein, not only can the residual coke flowing down from the oil-gas section into the water-gas section be controlled, thereby controlling the material layer height in the water-gas section, but also the probability of gas blowby between the oil-gas section and the water-gas section is greatly reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 It is a schematic diagram of the structure of the invention as a whole;

[0037] Markings in the figure: 1, ash lock bucket; 2, oxygen and water vapor gasification agent inlet; 3, grate; 4, ash layer; 5, oxygen combustion layer; 6, water vapor gasification layer; 6a, water jacket pressure shell of water gas section; 7, water gas collection space; 8, residual coke downward passage pressure cylinder; 8A, spiral pusher; 8B, isolation area; 9, water gas outlet; 10, conical gas distribution component; 10A, annular channel; 11, hydrogen gasification agent and oil gas section bottom inlet; 11A, center bottom air inlet pipe; 11B, hydrogen gasification agent middle inlet; 11C, center middle air inlet sleeve; 11D, annular Tube; 11E, central middle gas distribution component; 11F, central annular gas distribution component; 12, central bottom gas distribution component; 13, high-temperature coke hydrogenation gasification layer; 13A, low-temperature coke hydrogenation gasification layer; 14, semi-coke hydrogenation rapid gasification layer; 15, debonding component; 15E, transmission shaft; 15F, driving device; 16, low-temperature stirring blade; 17, hydrogenation pyrolysis distillation layer; 18, drying layer; 19, coal distributor; 20, water jacket pressure shell of oil-coal gas section; 21, oil-coal gas outlet; 22, raw coal lock bucket; 23, water vapor gasification layer thermocouple insertion port; 24, thermocouple insertion port. DETAILED DESCRIPTION

[0038] All features disclosed in this specification, or steps in all methods or processes disclosed, except mutually exclusive features and / or steps, can be combined in any manner.

[0039] Any feature disclosed in this specification (including any additional claims and abstract), unless otherwise stated, may be replaced by other equivalent or alternative features having similar purposes. That is, unless otherwise stated, each feature is only an example of a series of equivalent or similar features.

[0040] In the description of the present invention, it is necessary to understand that the directions or positional relationships indicated by the terms "up", "down", "left", "right", etc. are based on the directions or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a predetermined direction, be constructed and operated in a predetermined direction, and therefore cannot be understood as a limitation on the present invention.

[0041] In addition, the terms "first", "second", etc. are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first", "second", etc. may explicitly or implicitly include one or more of the features.

[0042] Example 1

[0043] like Figure 1 As shown, the present invention provides a technical solution:

[0044] A gasifier for producing oil-coal gas and water-coal gas, which at least includes but is not limited to a water-coal gas section and an oil-coal gas section. A pressure-bearing cylinder 8 for a residual coke downward passage is provided at the bottom of the oil-coal gas section, an assembly hole cooperating with the pressure-bearing cylinder 8 for the residual coke downward passage is provided on the water-coal gas section, a spiral pusher 8A for pushing the residual coke is provided in the pressure-bearing cylinder 8 for the residual coke downward passage, and the residual coke accumulated on the spiral pusher 8A forms an isolation zone 8B for blocking the water-coal gas section and the oil-coal gas section; at least two layers of coke hydrogenation gasification layers are provided in the oil-coal gas section, at least three air intake structures are provided along the gas flow direction of the oil-coal gas section, and a gas distribution structure is provided along at least part of the air intake structure, so that there is sufficient hydrogen at the location where the chemical reaction occurs to react with coal to generate methane.

[0045] Based on the above structure, in this scheme, a detachable residual coke downward movement channel pressure cylinder 8 is provided in the water-gas section and the oil-gas section to simplify the overall installation. At the same time, a spiral pusher 8A is provided inside the residual coke downward movement channel pressure cylinder 8. On the one hand, by controlling the speed of the spiral pusher 8A, the amount of residual coke entering the water-gas section can be adjusted, thereby controlling the material layer height of the water-gas section. In another scheme, the residual coke accumulated on the spiral pusher 8A can form an isolation zone 8B to reduce and eliminate gas blowby between the oil-gas section and the water-gas section.

[0046] As an example, the oil-coal-gas section may include, from bottom to top, a high-temperature coke hydrogenation gasification layer 13, a low-temperature coke hydrogenation gasification layer 13A, a semi-coke hydrogenation fast gasification layer 14, a hydrogenation pyrolysis distillation layer 17 and a drying layer 18; a coal distributor 19 is also provided above the drying layer 18, and the coal distributor 19 is connected to the raw coal lock hopper 22; an air intake structure and an air distribution structure are provided in both the high-temperature coke hydrogenation gasification layer 13 and the low-temperature coke hydrogenation gasification layer 13A, a rotating part extending to the hydrogenation pyrolysis distillation layer 17 is provided from the top center position of the oil-coal-gas section, and a supporting wheel for bearing pressure on the rotating part is provided in the hydrogenation pyrolysis distillation layer 17; at the same time, a central bottom air distribution component 12 extending to the central position of the high-temperature coke hydrogenation gasification layer 13 is provided in the rotating part, and the central bottom air distribution component 12 is connected to the central bottom air inlet pipe 11A, and the central middle air inlet sleeve 11C is provided on the central bottom air inlet pipe 11A.

[0047] Based on the above structure, the coal flows downward evenly from the coal distributor 19 and is broken in the rotating part. At the same time, part of the weight of the carbon layer is transferred to the inner wall of the furnace body through the supporting wheel, thereby greatly reducing the bearing pressure of the coal particles in the semi-coke hydrogenation rapid gasification layer 14, the low-temperature coke hydrogenation gasification layer 13A, and the high-temperature coke hydrogenation gasification layer 13 below, thereby effectively reducing the pulverization of the coal particles; the coal reacts with gases of different temperatures in the process of falling to obtain different products, thereby maximizing resource utilization.

[0048] As an example, in the high-temperature coke hydrogenation gasification layer 13, a bottom inlet of a hydrogen gasifying agent, an annular channel 10A and a conical gas distribution component 10 are arranged at its lower part; part of the hydrogen enters the annular channel 10A from the bottom inlet of the hydrogen gasifying agent, and finally the hydrogen is evenly arranged through the conical gas distribution component 10, so that the bottom circumference of the high-temperature coke hydrogenation gasification layer 13 can reach a preset concentration of hydrogen; part of the hydrogen is distributed from the central bottom gas distribution component 12 to the center position of the high-temperature coke hydrogenation gasification layer 13, so that the bottom center position of the high-temperature coke hydrogenation gasification layer 13 can reach a preset concentration of hydrogen, which is beneficial to the overall reaction.

[0049] As an example, in the low-temperature coke hydrogenation gasification layer 13A, a middle inlet 11B of hydrogen gasifying agent, an annular pipe 11D, a middle annular gas distribution component 11F and a central middle gas distribution component 11E are arranged at its lower part; the middle inlet 11B of hydrogen gasifying agent is connected with the annular pipe 11D, the annular pipe 11D is connected with the middle annular gas distribution component 11F, the central middle gas distribution component 11E is connected with the gas pipeline of the central bottom gas distribution component 12, part of the hydrogen passes through the annular pipe 11D and the middle annular gas distribution component 11F to evenly distribute the predetermined concentration of hydrogen in the circumferential position of the low-temperature coke hydrogenation gasification layer 13A, and the central middle gas distribution component 11E evenly distributes the predetermined concentration of hydrogen in the central position of the low-temperature coke hydrogenation gasification layer 13A, which is beneficial to the overall reaction.

[0050] As an example, the hydropyrolysis distillation layer 17 may specifically include a low-temperature stirring blade 16, a debonding component 15, a turntable, a supporting wheel, a rib plate, a support and a transmission shaft 15E; the low-temperature stirring blade 16, the debonding component 15 and the turntable connected thereto are driven by the transmission shaft 15E to rotate, so as to break the adhesion formed by the pyrolysis distillation of the coal; the weight of the raw coal can be finally carried on the oil by the debonding component 15 and the turntable connected thereto, the rotatable supporting wheel and the stationary rib plate and the support. On the pressure-bearing shell of the coal gas section, the load-bearing pressure of the coal particles in the semi-coke hydrogenation rapid gasification layer 14, the low-temperature coke hydrogenation gasification layer 13A, and the high-temperature coke hydrogenation gasification layer 13 below is greatly reduced, thereby effectively reducing the pulverization of the coal particles; the transmission shaft 15E that drives the low-temperature stirring blades 16, the debonding component 15, and the turntable to rotate is tubular, so as to be inserted into the stationary center bottom air inlet pipe 11A and the hydrogen center middle air inlet sleeve 11C; a thermocouple insertion port 24 is also provided in the oil and coal gas section.

[0051] As an example, the water gas section comprises, from the bottom, an oxygen and water vapor gasification agent inlet 2, a grate 3, an ash layer 4, an oxygen combustion layer 5, a water vapor gasification layer 6, a water gas collection space 7 and a water gas outlet 9; an ash lock hopper 1 is also connected to the bottom of the water gas section, and a water vapor gasification layer thermocouple insertion port 23 is also provided throughout the water gas section. The water gas section is prior art and will not be described in detail here.

[0052] In this scheme, the water-gas section uses oxygen and water vapor mixed gasifying agent, and uses the residual coke from the oil-gas section as raw material to produce hydrogen and carbon monoxide;

[0053] The oil-coal gas section uses methane ≤5%, hydrogen 80-95%, CO+CO2+H2O+N2≤5%, H2S≤2%, that is, room temperature hydrogen gasification agent with hydrogen as the main component, and uses raw coal to directly produce the oil-coal gas section with oil as the main product. The height-to-diameter ratio of the gasification raw coal bed is 3-6.

[0054] In this scheme, 60-70% of the total amount of hydrogen gasifying agent in the oil-coal gas section is uniformly introduced into the lower circular section of the high-temperature coke hydrogenation gasification layer 13 through the bottom inlet of the oil-coal gas section, the annular channel 10A, the conical gas distribution component 10, the central bottom air inlet pipe 11A, and the central bottom gas distribution component 12, and then counter-flows with the high-temperature coke at about 1050°C to exchange heat, so that the room temperature hydrogen gasifying agent is heated to 850°C, so that the hydrogen in the gasifying agent and the active carbon element in the high-temperature coke undergo an exothermic methanogenic reaction of C+2H2→CH4, and while increasing the methane content in the gaseous phase gasifying agent, the temperature of the top of the high-temperature coke hydrogenation gasification layer 13 is also increased to 1050°C, or a temperature below the ash melting point of coal, so that the gaseous phase methane concentration The gas goes up and mixes with the room temperature hydrogen gasifier which accounts for 30-40% of the total amount of hydrogen gasifier from the middle annular gas distribution component 11F and the central middle gas distribution component 11E, and then the temperature drops to about 800°C and enters the low temperature coke hydrogenation gasification layer 13A, where the hydrogen in the gas phase continues to react with the active carbon element in the coke to undergo an exothermic methanogenic reaction of C+2H2→CH4, which increases the methane content in the gas phase gasifier to 25-30% and also increases the temperature at the top of the low temperature coke hydrogenation gasification layer 13A to 900-950°C; the gas phase gas continues to go up and enters the semi-coke hydrogenation rapid gasification layer 14, where the hydrogen in the gas phase reacts with the solid unsaturated hydrocarbon C containing abundant active carbon element in the semi-coke to react ... hydrogen in the gas phase. X H Y Rapid hydrogenation reaction: C X H Y +(2X-0.5 Y)H2→XCH4, so that the gas phase methane concentration rises to 35-45%, and the 600℃ semi-coke from the hydropyrolysis and distillation layer 17 is heated to 800℃; the gas phase gas continues to ascend and enter the hydropyrolysis and distillation layer 17, and the gas phase gas heats the coal particles from the drying layer 18, and pyrolyzes and distills them, and while precipitating and gasifying coal tar and realizing the production of oil and coal gas, it will also pyrolyze part of methane, so that the gas phase methane concentration rises to 40-50%; the oil and coal gas continues to ascend and enter the drying layer 18, and while bringing heat into the drying layer 18, the temperature of the drying layer 18 is increased, and the physical water carried by the coal particles is vaporized in the drying layer 18 and enters the gas phase, thereby drying the raw coal; at this point, the oil and coal gas rich in methane, coal tar gas, hydrogen, and water vapor leaves the drying layer 18, and successively leaves the oil and coal gas section through the annular space between the coal distributor 19 and the water jacket pressure shell 20 of the oil and coal gas section, and the oil and coal gas outlet 21;

[0055] In the scheme, in the water-gas section, the oxygen-containing gasifying agent composed of a mixture of oxygen and water vapor enters the furnace from the oxygen and water vapor gasifying agent inlet 2 at the bottom of the furnace, passes through the grate 3 and passes through the ash layer 4 from bottom to top, absorbs the heat carried by it, and the temperature rises to about 600°C before entering the oxygen combustion layer 5. The oxygen in the gasifying agent causes the remaining carbon elements in the residual coke to burn and gasify rapidly, generating CO2 and releasing a large amount of heat, so that the water vapor in the gasifying agent and the bed temperature reach above 1000°C, below the ash melting point; The high-temperature water vapor containing CO2 transfers heat to the residual coke in the water vapor gasification layer 6 from bottom to top, and at the same time reacts with the carbon elements in the residual coke to undergo an endothermic water vapor gasification reaction C+H2O=CO+H2, so that most of the carbon elements in the residual coke react with 30-40% of water molecules in the water vapor and are converted into CO and H2 in the raw gas. The raw gas becomes hot and humid with a temperature of about 700°C and enters the water gas collection space 7 at the top of the water gas reaction layer, and then flows out of the water gas section through the water gas outlet 9.

[0056] In this scheme, temperature measuring thermocouples are set at a vertical interval of 250mm in the furnace of the oil-gas section and the water-gas section to monitor their temperature; pressure detection points are set in the isolation area 8B and the water-gas collection space 7 to accurately control the pressure difference between the upper and lower ends of the isolation area 8B to reduce and eliminate gas blowby between the oil-gas section and the water-gas section.

[0057] In this scheme, the raw coal enters the furnace from the top and enters the drying layer 18. It contacts and exchanges heat with the rising hydrocarbon-rich oil gas in reverse while slowly moving downward. After being heated by the rising hydrocarbon-rich oil gas to precipitate water, the temperature rises to 300-350°C and moves downward into the hydrogenation pyrolysis distillation layer 17. While the raw coal is further heated, the polycarbons in the coal are softened, fused, cracked, and gasified by the heat, causing the coal particles to expand and a large number of micropores to appear, and its specific surface area increases rapidly. Since the coal gas from the semi-coke hydrogenation layer is rich in methane, and hydrogen, the tar in the coal is restricted by its phase equilibrium, and the amount of methane generated will be relatively reduced, and the hydrogen element in the coal will not be pyrolyzed into single H2 molecules to enter the gas phase, thereby increasing the generation of gaseous polycarbons (oil), and then improving the yield of gaseous polycarbons (oil or tar); with the increase of distillation time and the increase of temperature, the raw coal completes pyrolysis and distillation, and the precipitated coal tar completes cracking and gasification. The raw coal becomes semi-coke with a huge specific surface area at about 600°C, and a large amount of solid products of distillation and cracking are attached, that is, activated carbon elements;

[0058] The semi-coke is driven by the debonding component 15 to enter the semi-coke hydrogenation fast gasification layer 14, and countercurrently contacts the oil and coal gas containing methane and polycarbons from bottom to top. The aromatic hydrocarbons and unsaturated hydrocarbons containing active carbon elements attached to the semi-coke rapidly undergo hydrogenation saturation reaction with the hydrogen elements in the gas phase and release heat, generating a large amount of saturated hydrocarbons methane and ethane that enter the gas phase, turning the semi-coke into coke with a temperature of 750-800°C.

[0059] The coke continues to move slowly downward under the action of gravity and enters the low-temperature coke hydrogenation gasification layer 13A, and contacts the methane hydrogen gasification agent from bottom to top in countercurrent. While heating the upward methane hydrogen gasification agent, since the partial pressure of hydrogen in the methane hydrogen gasification agent accounts for the vast majority of the total pressure, although the bed temperature is relatively high, the actual concentration of gas phase methane is still less than the chemical equilibrium concentration of C+2H2=CH4. In addition, the high temperature increases the molecular activation kinetic energy of coke and hydrogen, which greatly increases the active molecular fraction in coke and hydrogen, which is very conducive to promoting the exothermic reaction of C+2H2=CH4 to generate methane, and makes the hot spot temperature of the low-temperature coke hydrogenation gasification layer 13A reach 900-950℃;

[0060] The coke continues to move slowly downward under the action of gravity, and after exchanging part of its heat with the low-methane hydrogen gasifier mixed with the room-temperature hydrogen gasifier from the middle annular gas distribution component 11F and the central middle gas distribution component 11E, it enters the high-temperature coke hydrogenation gasification layer 13, and undergoes a methanation reaction with the hydrogen gasifier from the conical gas distribution component 10 and the central bottom gas distribution component 12. Since the methane content in the hydrogen gasifier entering the high-temperature coke hydrogenation gasification layer 13 is less than 5%, its gas phase concentration is still much lower than the equilibrium concentration under its designed process temperature and pressure. Therefore, in the high-temperature coke hydrogenation gasification layer 13, an exothermic reaction of C+2H2=CH4 to generate methane will inevitably occur, and the hot spot temperature of the high-temperature coke hydrogenation gasification layer 13 will reach 1050°C, or a temperature below the ash melting point of coal.

[0061] After the raw coal enters the furnace and goes through drying, carbonization, rapid gasification of semi-coke hydrogenation, low-temperature coke hydrogenation and high-temperature coke hydrogenation from top to bottom in the oil-coal gas section, the total mass is reduced by 40-50% and the carbon element is reduced by 30-50% according to the type of coal, ash content and moisture content, and becomes residual coke.

[0062] The residual coke continues to move downward, and after countercurrent contact and heat exchange with the hydrogen gasifying agent from the conical gas distribution component 10 and the central bottom gas distribution component 12, the temperature is reduced to 200-400℃, and then it enters the water-gas section through the isolation area 8B and the spiral pusher 8A; in the water vapor gasification layer 6, it reacts with the high-temperature water vapor from bottom to top in C+H2O=CO+H2 water-gas reaction, so that most of the carbon elements in the residual coke are converted into CO; the residual coke containing a small amount of carbon elements continues to move downward and enters the oxidation combustion layer; it contacts with the oxygen-containing water vapor from bottom to top in countercurrent, and due to the strong oxidizing property of oxygen, the remaining carbon elements in the residual coke are rapidly burned, and a large amount of heat is released while generating CO2, so that the temperature of the oxidation layer reaches a temperature above 1000℃ and below the ash melting point, which not only provides huge heat for the endothermic water-gas reaction, but also burns the residual coke into ash.

[0063] In this scheme, the ash lock bucket 1 is used to discharge the ash remaining after the coal discharged from the furnace is gasified; the grate 3 is used to remove the ash and the gasifying agent flowing upward uniformly; the ash layer 4 is both a heat insulation protection layer of the grate 3 and a heat source for recovering the waste heat of the ash to heat the gasifying agent;

[0064] Oxygen combustion layer 5, where the oxygen in the gasifier first burns the residual carbon in the ash, and heats the gasifier and the carbon layer to above 1000°C, below the ash melting point, to provide heat energy for the endothermic water-gas reaction;

[0065] Water vapor gasification layer 6, mainly C+H2O=CO+H2;

[0066] The water-gas collecting space 7 is where the water-gas produced in the carbon layer below is collected;

[0067] The residual coke moves down the pressure-bearing cylinder 8 of the channel to discharge the residual coke into the water vapor reaction layer;

[0068] The screw pusher 8A adopts circular drive;

[0069] The isolation area 8B uses the residual coke accumulated in this area and the screw pusher 8A to achieve the isolation of different gases between the oil gas section and the water gas section;

[0070] A conical gas distribution member 10, through which the hydrogen gasifying agent entering the furnace is evenly distributed on the circular cross section in the furnace and flows upward;

[0071] The annular channel 10A is composed of a conical gas distribution component 10 and a concave surface of the head, so that the hydrogen added from the bottom inlet of the hydrogen gasifier can be distributed in the circular cross-section of the carbon layer in the furnace through the conical gas distribution component 10, and flow upward in the gaps between the coal particles.

[0072] The bottom inlet 11 of the hydrogen gasifying agent and oil and coal gas section, from which the hydrogen added can be distributed to the circular cross section of the furnace through the conical gas distribution member 10;

[0073] The center bottom air inlet pipe 11A delivers hydrogen gasification agent to the center bottom;

[0074] The central bottom gas distribution component 12 distributes the hydrogen sent through the central air inlet pipe to the central area of ​​the bottom;

[0075] The high-temperature coke hydrogenation gasification layer 13 mainly performs the C+2H2=CH4 reaction at a temperature of 900-1100°C to convert the carbon element in the coke into methane;

[0076] The low-temperature coke hydrogenation gasification layer 13A mainly performs the C+2H2=CH4 reaction at a temperature of 800-950°C to convert the carbon element in the coke into methane;

[0077] The semi-coke hydrogenation fast gasification layer 14 mainly performs fast 2CH+3H2=2CH4, 2CH2+2H2=2CH4, 2CH3+H2=2CH4 reactions at a temperature of 700-800°C to convert the solid unsaturated hydrocarbons in the semi-coke into methane;

[0078] The sticking breaking member 15 rotates together with the turntable under the drive of the transmission shaft 15E to break the sticking raw coal and prevent the oversized semi-coke from entering the semi-coke hydrogenation gasification layer;

[0079] The lower annular surface of the rotating disk is supported by the supporting wheel, so that the weight of the carbon layer is transferred to the inner wall of the furnace body through the supporting wheel, the bracket and the rib plate; the structural design of the rotating disk has the functions of breaking adhesion, bearing weight and discharging carbon materials;

[0080] The transmission shaft 15E drives the turntable to rotate. The shaft is tubular so as to be inserted into the stationary center bottom air intake pipe 11A and the hydrogen center middle air intake sleeve 11C;

[0081] The driving device 15F drives the transmission shaft 15E and the turntable to rotate;

[0082] Low temperature stirring blade 16, to break the coal adhesion during the dry distillation process and reduce the degree of agglomeration;

[0083] Hydropyrolysis and distillation layer 17, where the coal is heated, distilled, pyrolyzed, and gasified by the rising hot air flow to produce polycarbons;

[0084] Drying layer 18, where the coal is heated by the rising hot air flow, drying the moisture inside it and decomposing the adsorbed gas;

[0085] The coal distributor 19 evenly distributes the raw coal / coal briquettes from the coal lock hopper in the cross section of the furnace.

[0086] The oil gas outlet 21 contains gaseous hydrocarbons.

[0087] Example 2

[0088] The present embodiment discloses a gasifier for producing oil gas and water gas, which is composed of an oxygen and water vapor gasification agent inlet, a grate 3, a raw coal gasification bed, a stirrer, a coal distributor and a coal lock, a pressurized water jacket shell, a crude gas outlet and a hydrocarbon-rich gas outlet, wherein the raw coal gasification bed is divided into an ash layer 4, an oxygen combustion layer 5, a water gas generation layer, a methane generation layer, and a raw coal drying layer 18 from bottom to top, and oxygen and water vapor react with the raw coal from bottom to top to generate water gas, and the pressurized moving bed gasifier is designed to be an upper and lower structure connected by a pressure cylinder 8 with a residual coke downward movement channel having an isolation zone 8B and a circumferentially driven spiral pusher 8A disposed therein;

[0089] The lower section is designed as a water-gas section that uses a mixed gasification agent of oxygen and water vapor to produce hydrogen and carbon monoxide using the residual coke from the oil-gas section as a raw material;

[0090] The upper section is designed to use methane ≤5%, hydrogen 80-95%, CO+CO2+H2O+N2≤5%, H2S≤2%, that is, a room temperature hydrogen gasification agent with hydrogen as the main component, and use raw coal to directly produce an oil-coal gas section with oil as the main product. The height-to-diameter ratio of the gasification raw coal bed is 3-6.

[0091] First, the water-gas section and the oil-gas section with an inner diameter of 3.8 meters are manufactured separately and then transported to the installation site. After being connected as a solid whole by the pressure-bearing cylinder 8 of the residual coke downward movement channel equipped with a spiral pusher 8A, the internal components of the water-gas section and the oil-gas section are installed, and the leak and pressure tests are passed. After the installation is in place, the process piping, electrical instrumentation, anti-corrosion and insulation, system leak and pressure tests, and commissioning are passed, desalted water is added to the jackets of the water-gas section and the oil-gas section of the gasifier, so that they have the structure and function of graded production of hydrocarbon-rich oil gas and water gas.

[0092] Then, 300mm thick coal gasifier ash and 2000mm thick coke of the water gasification layer 6 are sequentially laid on the grate 3 of the water gas section; 20-80mm thick coke of the coke hydrogenation gasification layer of the oil gas section is added; 3000mm thick semi-coke of the semi-coke hydrogenation gasification layer is added; 20-80mm thick weakly sticky coal of the coke hydrogenation gasification layer is added; 2000mm thick weakly sticky coal of the coke hydrogenation gasification layer is added; 20-80mm thick weakly sticky coal of the coke hydrogenation gasification layer is added; 2000mm thick weakly sticky coal of the coke hydrogenation gasification layer is added; 2000mm thick weakly sticky coal of the coke hydrogenation gasification layer is added; 2000mm thick weakly sticky coal of the coke hydrogenation gasification layer is added; 2000mm thick weakly sticky coal of the coke hydrogenation gasification layer is added; 1000mm thick weakly sticky coal of the coke hydrogenation gasification layer is added;

[0093] ①Press the air at 5000~10000Nm per hour 3 The flow rate is sent into the furnace at a temperature rise rate of 50℃ / h and is discharged at the oil gas outlet 21; in about 6 hours, since the ignition point of coke is about 350℃, the temperature of the oxygen combustion layer 5 in the water gas section will begin to exceed the temperature of the air entering the furnace. When the oxygen combustion layer 5 rises rapidly to about 700℃, the venting is changed to venting after the water gas outlet 9 of the water gas section; nitrogen can be added to the air entering the furnace in an appropriate amount to reduce its O2 content so as to control the heating rate of the oxygen combustion layer 5 at about 100℃ / h. When the temperature of the oxygen combustion layer 5 reaches 900-1000℃, the air heating is gradually changed to oxygen-water vapor mixed gasification agent, and its temperature is controlled not to rise any more so as to prevent over-temperature scarring in the water gas section.

[0094] ② Pass hot nitrogen isothermally with the flue gas at the water gas outlet 9 at a rate of 5000~10000Nm 3 / h flow rate, added to the oil-gas section through the hydrogen inlet of the oil-gas section, and discharged at the oil-gas outlet 21. In order to further heat the coke, semi-coke and raw coal in the oil-gas section, a proper amount of air (actually oxygen, note: the maximum temperature of the coke hydrogenation gasification layer and the semi-coke hydrogenation gasification layer shall not exceed 700°C) can be added to the hot nitrogen to accelerate the heating rate by utilizing the combustion heat of oxygen and coke;

[0095] ③ When the temperature of the distillation layer of the oil and gas section is greater than 400℃, the agitator can be started to operate at a low speed in real time, and the coal adding device can start the automatic control loop to automatically add raw coal in time.

[0096] ④ When the maximum temperature of the coke hydrogenation gasification layer and the semi-coke hydrogenation gasification layer reaches above 600°C, start to increase the system pressure at a rate of 1MPa per hour. During the pressure increase process, pay attention to: reduce the pressure difference between the water gas outlet 9 and the hydrogen inlet to near zero, so as to prevent the gas in the oil gas section from flowing downward into the water gas collector and out from the water gas outlet 9.

[0097] ⑤ When the pressure rises to 2MPa, turn off the oxygen added to the hot nitrogen for 30 minutes, or turn off the oxygen, and after the hot spot temperature drops by 50℃, replace the hot nitrogen into the furnace with hot hydrogen at 5000~10000Nm 3 / h flow rate into the furnace, so that the oil gas section into the hydrogen gasification period, and gradually increase at a rate of 1MPa per hour, and finally stabilize the pressure at 3MPa.

[0098] Furnace temperature control: In the water-gas section, the temperature of the oxygen combustion layer 5 is controlled to be 30-80°C below the ash melting point by controlling the steam-oxygen ratio of the furnace; in the oil-gas section, the maximum temperature of the semi-coke hydrogenation section is controlled to be ≤1000°C by controlling the hydrogen temperature and the methane content in the hydrogen;

[0099] Oil and coal gas composition control: The methane content in the oil and coal gas is controlled at about 50% by controlling the hydrogen flow, temperature and methane content of the furnace according to the activity and volatility of the coal type, and other gaseous hydrocarbons are 100-200g / Nm 3 Oil, gas.

[0100] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A gasifier for producing oil gas and water gas, comprising an oxygen and water vapor gasification agent inlet, a grate, a raw coal gasification bed, a stirrer, a coal distributor and a coal lock, a pressurized water jacket shell, a crude gas outlet and a hydrocarbon-rich gas outlet, wherein the raw coal gasification bed is divided into an ash layer, an oxygen combustion layer, a water gas generation layer, a methane generation layer, and a raw coal drying layer from bottom to top, and oxygen and water vapor react with the raw coal from bottom to top to generate water gas, characterized in that: The pressurized moving bed gasifier is designed to be a structure of upper and lower sections connected by a pressure-bearing cylinder (8) of a residual coke downward moving channel in which an isolation area (8B) and a circumferentially driven spiral pusher (8A) are arranged; The lower section is designed as a water-gas section that uses a mixed gasification agent of oxygen and water vapor to produce hydrogen and carbon monoxide using the residual coke from the oil-gas section as a raw material; The upper section is designed to use methane ≤ 5%, hydrogen 80-95%, CO+CO2+H2O+N2 ≤ 5%, H2S ≤ 2%, i.e., a normal temperature hydrogen gasification agent with hydrogen as the main component, to directly produce an oil-coal gas section with oil as the main product from raw coal, and the height-to-diameter ratio of the gasified raw coal bed is 3-6; The oil, coal and gas sections are designed from bottom to top as follows: A high-temperature coke hydrogenation gasification layer (13) is provided at the bottom with a hydrogen gasification agent bottom inlet (11), an annular channel (10A), a conical gas distribution component (10), a central bottom gas inlet pipe (11A), and a central bottom gas distribution component (12); A low-temperature coke hydrogenation gasification layer (13A) is provided at the lower part thereof with a central inlet for hydrogen gasification agent (11B), an annular pipe (11D), a central annular gas distribution component (11F), a central central gas inlet sleeve (11C), and a central central gas distribution component (11E); Semi-coke hydrogenation rapid gasification layer (14); The hydrogenation pyrolysis distillation layer (17) is provided with a low-temperature stirring blade (16), a debonding component (15), a rotating disk (15D), a supporting wheel, a rib plate, a support, and a transmission shaft (15E); the low-temperature stirring blade (16), the debonding component (15) and the rotating disk (15D) connected thereto are driven to rotate by the transmission shaft (15E), so as to break the adhesion formed by the pyrolysis distillation of the coal; the weight of the raw coal is finally carried on the pressure-bearing shell (20) of the oil-coal-gas section through the debonding component (15) and the rotating disk (15D) connected thereto, the rotatable supporting wheel, and the stationary rib plate and the support; the transmission shaft (15E) for driving the low-temperature stirring blade (16), the debonding component (15) and the rotating disk (15D) to rotate is tubular so as to be inserted into the stationary central bottom air inlet pipe (11A) and the hydrogen central middle air inlet sleeve (11C); A drying layer (18); 60-70% of the total amount of hydrogen gasifying agent is uniformly introduced into the lower circular section of the high-temperature coke hydrogenation gasification layer (13) through the bottom inlet (11) of the oil-coal gas section, the annular channel (10A), the conical gas distribution component (10), the central bottom gas inlet pipe (11A), and the central bottom gas distribution component (12), and then reversely exchanges heat with the descending high-temperature coke at 1050°C, heating the normal-temperature hydrogen gasifying agent to 850°C, causing the hydrogen in the gasifying agent to undergo an exothermic methanogenic reaction of C+2H2→CH4 with the active carbon element in the high-temperature coke, while increasing the methane content in the gaseous phase gasifying agent, and also increasing the temperature of the top of the high-temperature coke hydrogenation gasification layer (13) to 1050°C, or a temperature below the ash melting point of coal, so that the gaseous phase methane concentration reaches The gas moves upward and mixes with the room temperature hydrogen gasifying agent which accounts for 30-40% of the total amount of hydrogen gasifying agent from the middle annular gas distributing member (11F) and the central middle gas distributing member (11E), and then the temperature drops to 800°C and enters the low temperature coke hydrogenation gasification layer (13A), where the hydrogen in the gas phase continues to react with the active carbon element in the coke to undergo an exothermic methanogenic reaction of C+2H2→CH4, thereby increasing the methane content in the gas phase gasifying agent to 25-30% and also increasing the temperature of the top of the low temperature coke hydrogenation gasification layer (13A) to 900-950°C; the gas phase gas continues to move upward and enters the semi-coke hydrogenation rapid gasification layer (14), where the hydrogen in the gas phase reacts with the solid unsaturated hydrocarbon C containing abundant active carbon elements in the semi-coke to react with the solid unsaturated hydrocarbon C containing abundant active carbon elements. X H Y Rapid hydrogenation reaction: C X H Y +(2X-0.5Y)H2→XCH4, so that the gas phase methane concentration rises to 35-45%, and the 600°C semi-coke from the hydropyrolysis and distillation layer (17) is heated to 800°C; the gas phase gas continues to ascend and enters the hydropyrolysis and distillation layer (17), and the gas phase gas heats the coal particles from the drying layer (18) and causes them to be pyrolyzed and distilled, and while precipitating and gasifying coal tar and realizing the production of oil and coal gas, it also pyrolyzes part of methane, so that the gas phase methane concentration rises to 40 -50%; the oil-coal gas continues to ascend and enter the drying layer (18), bringing heat into the drying layer (18), raising the temperature of the drying layer, causing the physical water carried by the coal particles to vaporize in the drying layer (18) and enter the gas phase, thereby drying the raw coal; at this point, the oil-coal gas rich in methane, coal tar gas, hydrogen, and water vapor leaves the drying layer (18), and leaves the oil-coal gas section successively through the annular space between the coal distributor (19) and the water-jacketed pressure shell (20) of the oil-coal gas section, and the oil-coal gas outlet (21).

2. A gasifier for producing oil gas and water gas as claimed in claim 1, characterized in that: The raw coal enters the furnace from the top and enters the drying layer. After being heated by the rising hydrocarbon-rich oil gas to precipitate water, the temperature rises to 300-350℃ and moves downward to the hydropyrolysis distillation layer. The polycarbons in the coal are softened, fused, cracked, and gasified by the heat. Due to the constraints of its phase equilibrium, the amount of methane generated will be relatively reduced, and the hydrogen element in the coal will not be pyrolyzed into single H2 molecules and enter the gas phase, thereby increasing the generation of gaseous polycarbons and further improving the yield of gaseous polycarbons. The raw coal turns into semi-coke with a large amount of active carbon elements at 600℃; The semi-coke enters the semi-coke hydrogenation rapid gasification layer under the push of the debonding component, and contacts with the oil and coal gas containing methane and polycarbons from bottom to top in countercurrent. The aromatic hydrocarbons and unsaturated hydrocarbons containing active carbon elements attached to the semi-coke rapidly undergo hydrogenation saturation reaction with the hydrogen elements in the gas phase and release heat, generating a large amount of saturated hydrocarbon methane that enters the gas phase, turning the semi-coke into coke with a temperature of 750-800℃. The coke continues to move slowly downward under the action of gravity, enters the low-temperature coke hydrogenation gasification layer, and contacts with the methane hydrogen gasification agent from bottom to top in countercurrent. While heating the upward methane hydrogen gasification agent, the actual concentration of gaseous methane is still less than the chemical equilibrium concentration of C+2H2=CH4, and the high temperature increases the molecular activation kinetic energy of coke and hydrogen, which in turn promotes the exothermic reaction of C+2H2=CH4 to generate methane, and makes the hot spot temperature of the low-temperature coke hydrogenation gasification layer reach 900-950℃; The coke continues to move slowly downward under the action of gravity, and after exchanging part of its heat with the low-methane hydrogen gasifier mixed with the room-temperature hydrogen gasifier from the middle annular gas distribution component and the central middle gas distribution component, it enters the high-temperature coke hydrogenation gasification layer. Since the methane content in the hydrogen gasifier entering the high-temperature coke hydrogenation gasification layer is less than 5%, its gas phase concentration is still much lower than the equilibrium concentration under its designed process temperature and pressure. Therefore, in the high-temperature coke hydrogenation gasification layer, an exothermic reaction of C+2H2=CH4 to generate methane will inevitably occur, and the hot spot temperature of the high-temperature coke hydrogenation gasification layer will reach 1050°C, or a temperature below the ash melting point of coal; The residual coke continues to move downward, and after countercurrent contact and heat exchange with the hydrogen gasifying agent from the conical gas distribution component and the center bottom gas distribution component, the temperature is reduced to 200-400℃, and then it enters the water-gas section through the isolation area and the spiral pusher; in the water vapor gasification layer, it reacts with the high-temperature water vapor from bottom to top to form C+H2O=CO+H2 water-gas, so that most of the carbon elements in the residual coke are converted into CO; the residual coke containing a small amount of carbon elements continues to move downward and enters the oxidation combustion layer; due to the strong oxidizing properties of oxygen, the remaining carbon elements in the residual coke burn rapidly, so that the temperature of the oxidation layer reaches a temperature above 1000℃ and below the ash melting point, which not only provides huge heat for the endothermic water-gas reaction, but also burns the residual coke into ash.

3. A gasifier for producing oil gas and water gas as claimed in claim 2, characterized in that: The temperature of the hydrogen gasifier is 50-200°C; after the raw coal entering the furnace undergoes top-down drying, carbonization, rapid gasification of semi-coke hydrogenation, low-temperature coke hydrogenation gasification, and high-temperature coke hydrogenation gasification in the oil-coal gas section, the total mass is reduced by 40-50% and the carbon element is reduced by 30-50% depending on the type of coal, ash content, and moisture content, and becomes residual coke.

4. A gasifier for producing oil gas and water gas as claimed in claim 3, characterized in that: The raw coal is lignite, bituminous coal, coke, anthracite, or various carbon-containing solid materials with a caking index G≤20.

5. A gasifier for producing oil gas and water gas as claimed in claim 4, characterized in that: When non-caking coal is used, no low-temperature stirring blade (16) is provided in the gasifier.

6. A gasifier for producing oil gas and water gas as claimed in claim 5, characterized in that: The height-to-diameter ratio of the gasification bed in the oil-coal gas section is inversely proportional to the gasification activity of the raw coal. The high-activity coal coke adopts a smaller height-to-diameter ratio, while the low-activity coal coke adopts a larger height-to-diameter ratio. The inner diameter of the pressurized moving bed gasifier is 1.2 to 2 meters, or 2.2 to 4 meters, or 4.2 to 6 meters; the working pressure is 3 to 5 MPa, or 5.1 to 8 MPa.

7. A gasifier for producing oil gas and water gas as claimed in claim 6, characterized in that: The particle size of raw coal or briquette coal is 3-10mm, or 11-40mm, or 41-80mm.

8. A gasifier for producing oil gas and water gas as claimed in claim 7, characterized in that: 2-5% water vapor is added to the hydrogen gasifying agent (11) entering the oil-gas section; the cooling water of the jacket of the pressure shell of the oil-gas section and the cooling water of the jacket of the pressure shell of the water-gas section are circulated separately.

9. A gasifier for producing oil gas and water gas as claimed in claim 8, characterized in that: A medium-temperature coke hydrogenation gasification layer is provided between the high-temperature coke hydrogenation gasification layer (13) and the low-temperature coke hydrogenation gasification layer (13A) to increase the contact time between hydrogen and coke and improve the methane generation rate.

10. A gasifier for producing oil gas and water gas as claimed in claim 9, characterized in that: The slag discharge method of the water-gas section is a dry slag discharge gasification method below the ash melting point temperature, or a molten slag gasification method above the ash melting point temperature.

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