Ultrafine particle gasification system and gasification process of carbonaceous materials

Abstract

The present invention discloses an ultrafine particle gasification system and a gasification process of carbonaceous materials, wherein the gasification system comprises a raw material conveying unit, a gasification unit and a synthesis gas purification unit; the raw material conveying unit, the gasification unit and the synthesis gas purification unit are connected in sequence; the raw material conveying unit comprises a carrier gas control system and a silo, and the carrier gas control system is used to control the adding mode and flow rate of the carrier gas added to the silo; the lower end of the silo is provided with 2 to 10 layers of annular pipe branches, and each layer of annular pipe branches is evenly provided with 4 to 20 air inlets, which are used as the entrance for loading the carrier gas into the silo; the synthesis gas purification unit comprises a cyclone separator, a particle layer filter, a convection waste pot and a scrubber in sequence. The present invention further improves the efficiency of entrained flow gasification, improves the processing capacity of the gasifier, reduces the reaction temperature, prolongs the service life of the gasifier lining, and saves the operating cost.

Description

Technical Field

[0001] The invention relates to an ultrafine particle gasification system and a gasification process of carbon-containing substances. Background Art

[0002] The process of converting solid carbon-containing substances into gaseous substances rich in CO, H2 (or containing CH4) is a process that uses oxygen (air, enriched oxygen or industrial pure oxygen) and water vapor as gasifying agents to convert the combustible part of coal or coal coke into gaseous substances rich in CO, H2 (or containing CH4) through chemical reactions.

[0003] The existing carbon-containing material gasification process can be divided into fixed bed atmospheric pressure (pressurized) gasification process, fluidized bed gasification process and entrained flow gasification process according to the size of the solid particles entering the reactor. In the fixed bed atmospheric pressure (pressurized) gasification process, solid materials enter the gasifier at a centimeter scale, and the conversion time is tens of minutes to hours; the fluidized bed gasification process uses millimeter-level solid particles as raw materials, and the conversion time is about minutes; the entrained flow gasification technology uses hundreds of micron-level particles as raw materials, and the conversion time is 10 seconds. The change in particle size leads to a huge change in the reaction time of the particles, which in turn makes the gasifier structure, processing capacity, and process flow very different. From the reaction performance of fixed bed gasifiers, fluidized bed gasifiers, and entrained flow gasifiers, it can be seen that the entrained flow gasifier has the largest unit volume processing capacity. Chinese patent document CN110257105A discloses a process for producing synthesis gas by gasification of ultrafine powder at low temperature fluidized bed, which uses solid carbonaceous particles with a particle size of less than 75 μm as gasification raw materials, and reacts with a gasifying agent at a gasification temperature below 1300°C to generate synthesis gas. The main problem is that the gasification efficiency is difficult to further improve, the unit volume processing capacity of the gasifier is not high, and the gasification temperature is still as high as 1300°C, the lining of the gasifier is greatly eroded, reducing the service life of the lining, and the enterprise has high operating costs.

[0004] Although those skilled in the art know that further refining the particle size of solid particles can increase the gasification rate of the fluidized bed, thereby reducing the gasification temperature and improving the unit volume processing capacity of the gasifier, to date, the particle size of raw materials for fluidized bed gasification still remains at the level of hundreds of microns. In addition to the technical difficulties of ultrafine particle grinding, there are two major technical difficulties in the gasification of ultrafine particles: one is the stability problem of pneumatic conveying of ultrafine particles. The finer the solid particles, the worse their fluidity, and the more unstable the pneumatic conveying flow rate. The existing pneumatic conveying system cannot convey ultrafine particles of carbon-containing substances; the second is the separation of synthesis gas, slag and fly ash. The solid particle size is further reduced. Although this brings about an improvement in gasification efficiency, it also further reduces the particle size of fly ash, and the difficulty of separating fly ash from synthesis gas is further increased. The carrier gas conveying system and synthesis gas purification system in the existing technology are no longer suitable for the gasification of ultrafine particles. Summary of the invention

[0005] The technical problem to be solved by the present invention is to overcome the defects that the gasification efficiency of the existing fluidized bed gasification process is difficult to further improve, the processing capacity of the gasifier per unit volume is not high, the gasification temperature is high, the service life of the refractory lining of the gasifier is short, the enterprise operation cost is high, and the carrier gas delivery system and synthesis gas purification system of the prior art are not suitable for ultrafine particle gasification. A superfine particle gasification system and gasification process of carbon-containing substances are provided, which further improve the gasification efficiency and the processing capacity of the gasifier by further refining the particle size of the carbon-containing substance, and reduce the gasification temperature. The service life of the refractory lining is extended, the operation cost of the enterprise is reduced, and at the same time the stability of ultrafine particle delivery is improved and the ash content in the synthesis gas is reduced to a lower level.

[0006] The present invention solves the above technical problems through the following technical solutions:

[0007] The present invention provides an ultrafine particle gasification system of carbonaceous matter, which comprises a raw material conveying unit, a gasification unit and a synthesis gas purification unit; the outlet of the raw material conveying unit is connected to the inlet of the gasification unit, and the outlet of the gasification unit is connected to the inlet of the synthesis gas purification unit;

[0008] The raw material conveying unit includes a carrier gas control system and a silo, wherein the lower end of the silo is provided with 2 to 10 layers of annular pipe branches, and each layer of the annular pipe branches is evenly provided with 4 to 20 gas inlets; the carrier gas control system includes a solenoid valve, a pulse power supply controller and a gas distributor, wherein the pulse power supply controller is electrically connected to the solenoid valve, the outlet of the solenoid valve is connected to the inlet of the gas distributor, and the outlet of the gas distributor is connected to each of the gas inlets;

[0009] The synthesis gas purification unit includes a cyclone separator, a particle layer filter, a convection waste boiler and a washing tower in sequence. The inlet of the cyclone separator is the inlet of the synthesis gas purification unit, the outlet of the cyclone separator is connected to the inlet of the particle layer filter, the outlet of the particle layer filter is connected to the inlet of the convection waste boiler, and the outlet of the convection waste boiler is connected to the inlet of the washing tower.

[0010] In the present invention, the number of layers of the annular tube branches is preferably 4-8, more preferably 6-7.

[0011] In the present invention, the number of air inlets of each layer of the annular tube branches is preferably 5-15, and more preferably 12.

[0012] In the present invention, the structural design of the silo, combined with the pulsed carrier gas addition method, can achieve uniform and smooth feeding of ultrafine particles. Combined with the pulse gas combination control, ultrafine particles can be smoothly and evenly fed, and the particle flow fluctuation is less than 5%. With the traditional silo structure and the existing carrier gas control method, ultrafine particles are easily blocked in the silo, and the feed flow of ultrafine particles fluctuates greatly, affecting the stable operation of the gasifier.

[0013] In the present invention, the gasification unit generally includes a gasification chamber and a radiation waste boiler, and the outlet of the gasification chamber is the inlet of the radiation waste boiler. The gasification chamber is used for gasification of ultrafine particles of the carbonaceous material, and the radiation waste boiler can be used to recover the heat of the synthesis gas from the gasification chamber. At the same time, after the synthesis gas is cooled, the solid fly ash or liquid slag therein partially settles due to gravity.

[0014] In the present invention, the gasification chamber of the gasification unit may adopt conventional refractory lining in the art, such as refractory brick lining or water-cooled wall lining.

[0015] In the present invention, preferably, when the gasification system is solid slag discharge, the gasification chamber is lined with refractory bricks; when the gasification system is liquid slag discharge, the gasification chamber is lined with water-cooled walls.

[0016] In the present invention, the high-temperature synthesis gas from the gasifier is first separated from coarse particles by a cyclone dust collector, and then enters a particle bed to separate finer particles to obtain synthesis gas with low solid content, which is then cooled by a convection waste boiler and finally removed from dust by a water scrubber.

[0017] Although the cyclone separator, particle bed, convection waste boiler and water washing tower in the present invention are all conventional dust removal devices, the fly ash in the synthesis gas obtained after gasification of ultrafine particles is easily entrained by the synthesis gas due to its small size, making separation more difficult. Therefore, it is not possible to achieve the separation effect of fly ash in the synthesis gas obtained by the present invention by a simple combination of all dust removal devices.

[0018] The present invention provides a gasification process for ultrafine particles of carbon-containing matter, which utilizes the above-mentioned gasification system for ultrafine particles of carbon-containing matter and comprises the following steps:

[0019] Ultrafine particles of carbon-containing substances are transported to the gasification unit by the carrier gas of the raw material transport unit, and undergo a gasification reaction with the gasification agent of the gasification unit to obtain a crude synthesis gas;

[0020] The crude synthesis gas passes through the synthesis gas purification unit to obtain synthesis gas;

[0021] The ultrafine particles refer to particles with an average particle size of less than 10 μm and a maximum particle size of no more than 50 μm.

[0022] The pulse frequency of the pulse power controller may be 1-60 Hz, preferably 10-50 Hz, and more preferably 25 Hz.

[0023] In the present invention, the carbon-containing material can be conventional in the art, generally including coal, petroleum coke, semi-coke, biomass, preferably coal. Among them, the type of coal is conventional in the art, preferably bituminous coal.

[0024] In the present invention, the ultrafine particles generally refer to particles with an average particle size of less than 10 μm and a maximum particle size of no more than 50 μm.

[0025] In the present invention, the ultrafine particles can be ground by conventional methods in the art, such as mechanical grinding or air flow milling, preferably air flow milling.

[0026] In the present invention, the carrier gas may be conventional in the art, generally one or more of N2, CO2 or air, preferably N2.

[0027] In the present invention, the flow rate of the carrier gas corresponding to each kilogram of the ultrafine particles of the carbon-containing substance may be 0.0025 to 0.005 Nm 3 , preferably 0.0033Nm 3 .

[0028] In the present invention, the gasifying agent can be conventional in the art, preferably one or more of oxygen, air, CO2 and water vapor, more preferably oxygen and water vapor.

[0029] Wherein, when the gasifying agent is oxygen and water vapor, the volume ratio of the oxygen to the water vapor may be (5-1.5):1; preferably 3:1.

[0030] In the present invention, the flow rate of the gasifying agent corresponding to each ton of the ultrafine particles of the carbonaceous material can be 0.45-0.6 Nm 3 .

[0031] In the present invention, when the gasification process is solid slag discharge, the flow rate of the gasifying agent can be 0.45-0.52Nm 3 / kg coal; when the gasification process is liquid slag discharge, the flow rate of the gasifying agent can be 0.5-0.6Nm 3 / kg coal.

[0032] In the present invention, the temperature of the gasification reaction can be adjusted according to the slag discharge method, and can generally be 800-1700°C.

[0033] Wherein, when the gasification process adopts solid slag removal, the temperature of the gasification reaction is lower than the ash melting temperature of the carbon-containing material. Preferably, the temperature of the gasification reaction is 100-400°C lower than the ash melting temperature of the carbon-containing material, and more preferably, it is 200°C lower than the ash melting temperature of the carbon-containing material.

[0034] In certain preferred embodiments, the gasification process is solid slagging, and the temperature of the gasification reaction is 800-1000°C.

[0035] Wherein, when the gasification process adopts liquid slag discharge, the temperature of the gasification reaction is higher than the ash melting temperature of the carbon-containing material. Preferably, the temperature of the gasification reaction is 50-300°C higher than the ash melting temperature of the carbon-containing material, and more preferably, it is 150°C higher than the ash melting temperature of the carbon-containing material.

[0036] In the present invention, the residence time of the gasification reaction can be controlled according to the average particle size of the ultrafine particles.

[0037] Wherein, when the average particle size of the ultrafine particles is 10 um, the residence time of the gasification reaction can be 0.05 s to 5 s, preferably 1 s.

[0038] Wherein, when the average particle size of the ultrafine particles is 5 um, the residence time of the gasification reaction can be 0.03s to 2s, preferably 0.5s.

[0039] In the present invention, the gasification reaction residence time of the gasification unit generally refers to the residence time of the ultrafine particles.

[0040] In the present invention, the raw synthesis gas generally includes CO (40-60%), H2 (20-30%), CO2 (5-10%), carrier gas (2-5%), H2O (2-10%), and ungasified carbon-containing solid particles, solid fly ash and liquid slag flowing out with the gas.

[0041] On the basis of being in accordance with the common sense in the art, the above-mentioned preferred conditions can be arbitrarily combined to obtain the preferred embodiments of the present invention.

[0042] The reagents and raw materials used in the present invention are commercially available.

[0043] The positive and progressive effects of the present invention are:

[0044] (1) The gasification efficiency is further improved, and the unit volume processing capacity of the gasifier is greatly increased. With the same processing capacity, the volume of the gasifier is only about one-fourth of that of the existing technology;

[0045] (2) During solid slag discharge, the gasification temperature can be reduced from 1400°C to below 1000°C, and the coal consumption can be reduced by 5.9% compared with the existing technology, thereby improving the coal utilization rate. The oxygen consumption can be reduced by 15% compared with the existing technology, thereby saving operating costs. At the same time, it also greatly reduces the erosion of the gasifier lining and extends the service life of the lining.

[0046] (3) The present invention can achieve uniform and smooth feeding of ultrafine particles, and the particle flow rate fluctuation is less than 5%.

[0047] (4) The ash content in the synthesis gas obtained by the synthesis gas purification unit of the present invention can be reduced to 1 mg / Nm 3 Below, it reaches the same level as traditional 100-micron particle gasification. BRIEF DESCRIPTION OF THE DRAWINGS

[0048] Figure 1 This is a schematic diagram of the ultrafine particle gasification system of carbonaceous matter in Example 1;

[0049] Figure 2 This is a schematic diagram of the ring pipe branch structure of Example 1.

[0050] 11-carrier gas inlet; 12-solenoid valve; 121-pulse power controller; 13-gas distributor; 14-air inlet; 15-silo; 16-first coal powder inlet; 2-gasifier; 21-second coal powder inlet; 22-gasifying agent inlet; 23-radiation waste pot; 24-coarse slag outlet; 31-cyclone separator; 311-dusty synthesis gas inlet; 312-coarse ash outlet; 32-granular layer filter; 321-first fine ash outlet; 33-convection waste pot; 331-second fine ash outlet; 332-circulating compressor; 333-circulating synthesis gas inlet; 34-washing tower; 341-clean synthesis gas outlet; 342-circulating washing water pipeline; 343-external waste water outlet. DETAILED DESCRIPTION

[0051] The present invention is further described below by way of examples, but the present invention is not limited to the scope of the examples. The experimental methods in the following examples without specifying specific conditions are carried out according to conventional methods and conditions, or selected according to the product specifications.

[0052] Example 1

[0053] like Figure 1 and 2 As shown, 6 layers of annular pipe branches are arranged at the lower part of the silo 15, and the number of air inlets 14 of each layer of annular pipe branches is 12. The synthesis gas purification unit includes a cyclone separator 31, two particle layer filters 32, a convection waste boiler and a washing tower. The two particle layer filters 32 are connected in parallel, and part of the synthesis gas from the convection waste boiler is transported by the compressor to the cyclone separator through the return pipeline for secondary purification.

[0054] Refer to Figure 1 In the ultrafine particle gasification system of carbon-containing materials shown in the figure, the carrier gas is transported from the carrier gas inlet 11 to the gas distributor 13 controlled by the solenoid valve 12; the solenoid valve 12 is controlled by the pulse power controller 121, so that the carrier gas is distributed in a pulsed manner. The carrier gas is distributed into multiple air streams in the gas distributor 13 and enters the silo 15 from each air inlet 14 respectively. The silo 15 contains ultrafine coal powder entering from the first pulverized coal inlet 16. The ultrafine coal powder enters the gasifier 2 from the second coal powder inlet 21 under the pulse carrier gas transport, and the gasifying agent enters the gasifier 2 from the gasifying agent inlet 22. The ultrafine coal powder and the gasifying agent undergo a gasification reaction in the gasification chamber of the gasifier 2. The generated synthesis gas is cooled in the radiation waste pot 23, and the slag or large-particle ash therein settles due to gravity and is discharged from the coarse slag outlet 24. The synthesis gas after cooling enters the cyclone separator 31 from the dusty synthesis gas inlet 311, and the coarse ash therein is separated. The synthesis gas continues to enter the particle layer filter 32, and the fine ash is separated and discharged from the first fine ash outlet 321; the further purified synthesis gas enters the convection waste boiler 33, and the fine ash in the synthesis gas is further separated and discharged from the second fine ash outlet 331. Part of the synthesis gas is mixed with the dust-containing synthesis gas from the gasifier 2 from the circulating synthesis gas inlet 333 through the circulating compressor 332 and enters the cyclone separator 31, and the remaining synthesis gas enters the washing tower 34 for washing and purification, and the synthesis gas is discharged from the clean synthesis gas outlet 341. Part of the washing water discharged from the bottom of the tower enters the washing tower 34 through the circulating washing water pipeline 342 for recycling, and the rest is discharged through the external wastewater outlet 343.

[0055] Example 2

[0056] The gasification system of Example 1 was used, and the pressure of the gasifier was 4.0 MPa. The raw coal shown in Table 1 was gasified. The processing capacity of a single gasification system was about 2,000 tons (dry basis coal) / day. The raw coal was ground by conventional mechanical grinding and high-speed airflow grinding to produce particles with an average particle size of about 8 μm. The carrier gas was added by program control pulses, and the pulse frequency was about 50 Hz. The ultrafine particles were continuously transported to the pipeline, and the particle concentration was 350 kg / m 3 Under the action of carrier gas, coal powder, oxygen and steam are continuously fed into the gasifier. The gasification temperature is controlled at 1400℃, and liquid slag removal is adopted. The particles stay in the gasifier for 0.5s before flowing out and then enter the synthesis gas purification unit for separation. After 2-stage cyclone, 1-stage particle bed and 1-stage water washing, the dust content is less than 1mg / Nm 3 In this embodiment, the diameter of the metal shell of the reactor is 1.8 m, the effective space in the center is 1.0 m, the height of the reactor is 5 m, and the furnace has a plug flow rapid reaction flow field.

[0057] Example 3

[0058] The processing capacity of a single gasification system is about 1,500 tons (dry basis coal) / day. The raw coal is ground by traditional mechanical grinding and high-speed airflow grinding, with a pulse frequency of about 25Hz and an ultrafine particle concentration of 300kg / m 3 The gasification temperature is controlled at 1050°C-1100°C, and the solid slag removal method is adopted. The particles flow out after staying in the gasifier for 2 seconds. In this embodiment, the metal shell diameter of the reactor is 2.2m, the central effective space is 1.4m, and other conditions and operations are the same as those in Example 2.

[0059] Comparative Example 1

[0060] The coal shown in Table 1 is used as the gasification raw material, and a traditional fluidized bed pulverized coal gasifier is used. The pressure of the gasifier is 4.0 MPa, and the processing capacity of a single gasification system is about 1500 tons (dry basis coal) / day. The raw coal is ground into particles with an average particle size of about 70um by traditional mechanical grinding; N2 is used as a carrier gas in the conveying unit, and under the action of the carrier gas, the coal powder, oxygen and water vapor are continuously fed into the gasifier. The gasification temperature is controlled at 1400°C, and the particles stay in the gasifier for 8s before flowing out, and then enter the synthesis gas purification unit for separation. After dust removal through the first-stage cyclone separator and the first-stage water washing tower, the dust content is less than 1mg / Nm 3 In this case, the diameter of the metal shell of the reactor is 3.6m, the effective space in the center is 2.6m, the reactor height is 8m, and the furnace is a nearly fully mixed flow reactor.

[0061] Table 1 Properties of raw coal

[0062]

[0063]

[0064] Table 2 Gasification process indicators and outlet gas composition

[0065] parameter Comparative Example 1 Example 2 Example 3 Gasifier diameter / m 3.4 1.8 2.2 Furnace effective diameter / m 2.4 1.0 1.4 Superficial gas velocity / m / s 0.8 10 3.2 Height of straight section of gasification chamber / m 10 5 6 Vaporization temperature / ℃ 1400 1400 1050 Slag discharge method Liquid slag discharge Liquid slag discharge Solid slag removal Carbon conversion rate / % 99 99 99 <![CDATA[Specific coal consumption / (kg / kNm 3 (CO + H2 + 3.12CH4))]]> 540 540 508 <![CDATA[Specific oxygen consumption / (Nm 3 / kNm 3 (CO + H2 + 3.12CH4))]]> 305 305 262 Refrigeration gas efficiency / % 80.1 80.1 85.1 <![CDATA[Ash content / (mg / Nm 3 )]]> <1 <1 <1

[0066] The size, gasification process and effect data of the gasifier used in each embodiment and comparative example are shown in Table 2. Embodiment 2 and Embodiment 3 are both ultrafine particle pulverized coal gasification, and Comparative Example 1 uses pulverized coal with a particle size of 60-80μm for gasification. The gasification temperature of Embodiment 2 and Comparative Example 1 is 1400℃ and liquid slag discharge, while Embodiment 3 uses 1050℃ and solid slag discharge. Under the same processing capacity, the volume of the gasifier of the ultrafine particle gasification system of the present invention is only about one-fourth of the volume of the traditional pulverized coal gasification furnace. Under solid slag discharge, the gasification temperature can be reduced from 1400℃ to 1050℃ or even below 1000 degrees, which saves energy, reduces energy consumption, and reduces oxygen consumption by 15%. After the syngas is dedusted by the syngas purification unit of the present invention, the ash content can be reduced to 1mg / Nm 3 Below, it reaches the same level as traditional pulverized coal particle gasification.

Claims

1. A carbonaceous material ultrafine particle gasification system, characterized in that: It includes a raw material conveying unit, a gasification unit and a synthesis gas purification unit; the outlet of the raw material conveying unit is connected to the inlet of the gasification unit, and the outlet of the gasification unit is connected to the inlet of the synthesis gas purification unit; The raw material conveying unit includes a carrier gas control system and a silo, wherein the lower end of the silo is provided with 2 to 10 layers of annular pipe branches, and each layer of the annular pipe branches is evenly provided with 4 to 20 gas inlets; the carrier gas control system includes a solenoid valve, a pulse power supply controller and a gas distributor, wherein the pulse power supply controller is electrically connected to the solenoid valve, the outlet of the solenoid valve is connected to the inlet of the gas distributor, and the outlet of the gas distributor is connected to each of the gas inlets; The synthesis gas purification unit comprises a cyclone separator, a particle layer filter, a convection waste boiler and a washing tower in sequence, the inlet of the cyclone separator is the inlet of the synthesis gas purification unit, the outlet of the cyclone separator is connected to the inlet of the particle layer filter, the outlet of the particle layer filter is connected to the inlet of the convection waste boiler, and the outlet of the convection waste boiler is connected to the inlet of the washing tower; The synthesis gas purification unit also includes a reflux pipeline and a compressor. One end of the reflux pipeline is connected to the outlet of the convection waste boiler, and the other end is connected to the inlet of the cyclone separator. The compressor is arranged on the reflux pipeline to reintroduce part of the synthesis gas leaving the convection waste boiler into the synthesis gas purification unit for secondary purification.

2. The ultrafine particle gasification system of carbonaceous matter according to claim 1, characterized in that: The number of layers of the ring tube branches is 4-8; And / or, the number of air inlets of the annular pipe branches on each layer is 5-15.

3. The ultrafine particle gasification system of carbonaceous matter according to claim 2, characterized in that: The number of layers of the ring tube branches is 6-7; And / or, the number of air inlets of the annular pipe branches on each layer is 12.

4. The ultrafine particle gasification system of carbonaceous matter according to claim 1, characterized in that: The number of the cyclone separators is one or more. When the number of the cyclone separators is multiple, the cyclone separators are connected in series or in parallel; And / or, the number of the particle layer filters is one or more; when the number of the particle layer filters is multiple, the particle layer filters are connected in series or in parallel; And / or, the number of the convection waste pots is one or more; when the number of the convection waste pots is multiple, the convection waste pots are connected in series or in parallel; And / or, the number of the washing towers is one or more; when the number of the washing towers is multiple, the washing towers are connected in series or in parallel.

5. A process for gasifying ultrafine particles of carbonaceous matter, characterized in that: The method is carried out using the ultrafine particle gasification system of carbonaceous matter according to any one of claims 1 to 4, and comprises the following steps: Ultrafine particles of carbon-containing substances are transported to the gasification unit by the carrier gas of the raw material transport unit, and undergo a gasification reaction with the gasification agent of the gasification unit to obtain a crude synthesis gas; The crude synthesis gas passes through the synthesis gas purification unit to obtain synthesis gas; The ultrafine particles are particles with an average particle size of less than 10 μm and a maximum particle size of no more than 50 μm.

6. The gasification process according to claim 5, characterized in that: The pulse frequency of the pulse power controller is 1-60 Hz.

7. The gasification process according to claim 6, characterized in that: The pulse frequency of the pulse power controller is 10-50 Hz.

8. The gasification process according to claim 7, characterized in that: The pulse frequency of the pulse power controller is 25 Hz.

9. The gasification process according to claim 5, characterized in that: The carbon-containing material is one or more of coal, petroleum coke, semi-coke and biomass.

10. The gasification process according to claim 9, characterized in that The carbon-containing material is coal.

11. The gasification process according to claim 5, characterized in that: The carrier gas is one or more of N2, CO2 and air; And / or, the amount of the carrier gas corresponding to each kilogram of the ultrafine particles of the carbon-containing substance is 0.0025 to 0.005 Nm 3 ; and / or, the gasifying agent is one or more of oxygen, air, CO2 and water vapor; And / or, the amount of the gasifying agent corresponding to each kilogram of the ultrafine particles of the carbonaceous material is 0.45-0.6 Nm 3 ; And / or, when the gasification process is solid slag discharge, the amount of the gasifying agent corresponding to each kilogram of ultrafine particles of the carbon-containing material is 0.45-0.52 Nm 3 When the gasification process is liquid slag discharge, the amount of the gasifying agent corresponding to each kilogram of ultrafine particles of the carbon-containing material is 0.5-0.6Nm 3 .

12. The gasification process according to claim 11, characterized in that The carrier gas is N2; And / or, the amount of the carrier gas corresponding to each kilogram of the ultrafine particles of the carbon-containing substance is 0.0033 Nm 3 ; And / or, the gasifying agent is oxygen and water vapor.

13. The gasification process according to claim 5, characterized in that: When the gasification process is solid-state slagging, the temperature of the gasification reaction is lower than the ash melting temperature of the carbon-containing material; When the gasification process is liquid slag discharge, the temperature of the gasification reaction is higher than the ash melting temperature of the carbon-containing material.

14. The gasification process according to claim 13, characterized in that When the gasification process is solid slag discharge, the temperature of the gasification reaction is 100-400° C. lower than the ash melting temperature of the carbonaceous material.

15. The gasification process according to claim 14, characterized in that When the gasification process is solid slag discharge, the temperature of the gasification reaction is 200° C. lower than the ash melting temperature of the carbon-containing material.

16. The gasification process according to claim 13, characterized in that: When the gasification process is liquid slag discharge, the temperature of the gasification reaction is 50-300° C. higher than the ash melting temperature of the carbonaceous material.

17. The gasification process according to claim 16, characterized in that When the gasification process is liquid slag discharge, the temperature of the gasification reaction is 150° C. higher than the ash melting temperature of the carbon-containing material.

18. The gasification process according to claim 5, characterized in that: When the average particle size of the ultrafine particles is 8 to 10 μm, the residence time of the gasification reaction is 0.05 to 5 seconds; When the average particle size of the ultrafine particles is 4 to 6 um, the residence time of the gasification reaction is 0.03 s to 2 s.

19. The gasification process according to claim 14, characterized in that: When the average particle size of the ultrafine particles is 8-10 um, the residence time of the gasification reaction is 1 s.

20. The gasification process according to claim 14, characterized in that When the average particle size of the ultrafine particles is 4-6 um, the residence time of the gasification reaction is 0.5 s.

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