CN113025365A - System and method for treating direct coal liquefaction residues - Google Patents

System and method for treating direct coal liquefaction residues Download PDF

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CN113025365A
CN113025365A CN201911350784.XA CN201911350784A CN113025365A CN 113025365 A CN113025365 A CN 113025365A CN 201911350784 A CN201911350784 A CN 201911350784A CN 113025365 A CN113025365 A CN 113025365A
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coal
unit
pyrolysis
hot air
raw coal
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彭宝仔
刘臻
冯子洋
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China Energy Investment Corp Ltd
National Institute of Clean and Low Carbon Energy
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China Energy Investment Corp Ltd
National Institute of Clean and Low Carbon Energy
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers

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Abstract

The invention relates to a coal direct liquefaction residue treatment process, in particular to a system and a method for treating coal direct liquefaction residue. The system comprises a co-pyrolysis unit, a solid-liquid separation unit and a solid-liquid separation unit, wherein the co-pyrolysis unit is used for pyrolyzing a mixture of coal direct liquefaction residues and raw coal to obtain a co-pyrolysis solid product; the grinding unit is used for drying and grinding the co-pyrolysis solid product and the raw coal to obtain a first powdery mixture; the gasification unit is used for gasifying the first powdery mixture; wherein, the outlet of the co-pyrolysis solid product of the co-pyrolysis unit is communicated with the inlet of the milling unit. The system and the method can obtain more oil products and synthesis gas products with high added values, fully utilize the direct coal liquefaction residues, and have simple process and convenient operation.

Description

System and method for treating direct coal liquefaction residues
Technical Field
The invention relates to a coal direct liquefaction residue treatment process, in particular to a system and a method for treating coal direct liquefaction residue.
Background
Coal is directly liquefied, one of the coal liquefaction methods is a process of converting coal into liquid fuel through hydrocracking under the action of hydrogen and a catalyst. Besides obtaining the required liquefied product in the direct coal liquefaction process, some hydrocarbon molecules and CO can be generatedxGas, process water and liquefaction residues (also called coal direct liquefaction residues) generated in the solid-liquid separation process.
The direct coal liquefaction residue is solid hazardous waste and mainly contains inorganic substances and organic substances, wherein the organic substances comprise liquefied heavy oil, asphalt substances and unconverted coal, and the inorganic substances comprise mineral substances in the coal and an additional catalyst.
How to reasonably and efficiently utilize the direct coal liquefaction residues is a difficult problem which needs to be solved urgently by a coal liquefaction process. There are many methods for treating coal direct liquefaction residues as reported in the following prior art.
CN106318422A discloses a treatment device and a treatment method for coal direct liquefaction residues. The processing device includes: a raw material supply unit for supplying a melt of the coal direct liquefaction residue or a slurry containing the coal direct liquefaction residue; the pyrolysis reaction unit is provided with a raw material inlet and a gas phase product outlet, and the raw material inlet is connected with the raw material supply unit through a raw material conveying pipeline; and the oil gas recovery unit is connected with the gas-phase product outlet through a gas-phase product conveying pipeline. The treatment device is favorable for improving the decomposition efficiency of the direct coal liquefaction residues, and further is favorable for improving the yield of tar, and the obtained coke can be directly used as fuel. In conclusion, the treatment device for the direct coal liquefaction residues is beneficial to the decomposition of hazardous waste properties of the direct coal liquefaction residues, and the utilization rate and the economic benefit of the direct coal liquefaction residues are greatly improved. Although the method can improve the yield of tar, the solid substances after pyrolysis still contain some hazardous substances and are not fully utilized.
CN103695057B discloses a method for preparing water coal by directly liquefying coal residuesA slurry process, a coal water slurry and a gasification process therefor. The method for preparing the coal water slurry by using the direct coal liquefaction residues comprises the following steps: s1, extracting the direct coal liquefaction residues, carrying out solid-liquid separation, and drying to obtain an extract residue; and S2, crushing and grinding the raffinate, adding water and an optional surfactant into the raffinate, and stirring to obtain the coal water slurry. After the coal direct liquefaction residue is extracted, heavy oil and asphalt substances in the coal direct liquefaction residue can be separated from unconverted coal and ash, and the unconverted coal and the ash are collectively called raffinate. The coal water slurry can be formed after crushing and grinding the raffinate and adding water and optional surfactant. The coal water slurry can be used as common fuel and can be used in gasification production. Therefore, the raffinate of the direct coal liquefaction residue is effectively utilized, and the utilization rate and the added value of the direct coal liquefaction residue are improved. The extracting agent such as tetrahydrofuran, coal direct liquefied oil, etc. is used at 0.1-1.0MPa, 80-280 deg.C and H2Or N2Heavy oil and asphaltene substances in the extracted coal direct liquefaction residue are possibly incompletely extracted under the environment, so that the subsequent raffinate has high cohesiveness; in addition, the content of sulfur and nitrogen in the liquefaction residue is also high.
However, the above methods have a problem that the direct coal liquefaction residue is not sufficiently utilized, and therefore, a method for efficiently treating the direct coal liquefaction residue is demanded.
Disclosure of Invention
The invention aims to solve the problems of low oil yield, insufficient comprehensive utilization and the like of the coal direct liquefaction residue in the prior art, and provides a system and a method for treating the coal direct liquefaction residue.
In order to achieve the above object, a first aspect of the present invention provides a system for treating a coal direct liquefaction residue, comprising:
the co-pyrolysis unit is used for directly liquefying the mixture of the residue and the raw coal by pyrolyzing the coal to obtain a co-pyrolysis solid product;
the grinding unit is used for drying and grinding the co-pyrolysis solid product and the raw coal to obtain a first powdery mixture;
the gasification unit is used for gasifying the first powdery mixture;
wherein, the outlet of the co-pyrolysis solid product of the co-pyrolysis unit is communicated with the inlet of the milling unit.
In a second aspect, the present invention provides a method for treating a coal direct liquefaction residue, the method comprising:
(1) co-pyrolyzing the mixture of the direct coal liquefaction residues and the raw coal to obtain a co-pyrolysis solid product;
(2) mixing the co-pyrolysis solid product and raw coal in proportion, drying and grinding to obtain a first powdery mixture;
(3) gasifying the first powdery mixture.
In a third aspect, the present invention provides a method for treating a coal direct liquefaction residue using the system of the first aspect of the present invention, the method comprising:
(I) co-pyrolyzing the mixture of the direct coal liquefaction residues and the raw coal in a co-pyrolysis unit to obtain a co-pyrolysis solid product;
(II) drying and grinding the co-pyrolysis solid product and raw coal in a grinding unit according to a ratio to obtain a first powdery mixture;
(III) gasifying the first powdered mixture in a gasification unit;
preferably, the first pulverized mixture is gasified in a dry pulverized coal entrained flow gasifier.
The system and the method can obtain more oil products and synthesis gas products with high added values, fully utilize the direct coal liquefaction residues, and have simple process and convenient operation. In addition, the system and method of the present invention increases oil and gas yield by coupling pyrolysis and gasification.
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FIG. 1 is a schematic view of an embodiment of a system for treating direct coal liquefaction residues according to the present invention.
Description of the reference numerals
Figure BDA0002334609130000031
Figure BDA0002334609130000041
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
The invention provides a system for processing direct coal liquefaction residues, which comprises:
the co-pyrolysis unit is used for directly liquefying the mixture of the residue and the raw coal by pyrolyzing the coal to obtain a co-pyrolysis solid product;
the grinding unit is used for drying and grinding the co-pyrolysis solid product and the raw coal to obtain a first powdery mixture;
the gasification unit is used for gasifying the first powdery mixture;
wherein, the outlet of the co-pyrolysis solid product of the co-pyrolysis unit is communicated with the inlet of the milling unit.
According to the present invention, a mixture of the pyrolysis coal direct liquefaction residue and the raw coal is co-pyrolyzed in a co-pyrolysis unit to produce tar, coal gas, and co-pyrolysis solid products.
According to the invention, the solid product of the co-pyrolysis, raw coal, is dried and milled in a milling unit to obtain a first pulverulent mixture.
Preferably, in the milling unit, an air blowing device is provided for blowing air to the milling system during milling.
Preferably, the system further comprises a conveying unit for conveying the first powdered mixture into the gasification unit. Preferably, the conveying unit is communicated with the outlet of the grinding unit and the inlet of the gasification unit.
Preferably, the system further comprises a raw coal crushing and drying unit for crushing and drying the raw coal. Preferably, the outlet of the raw coal crushing and drying unit is respectively communicated with the inlet of the co-pyrolysis unit and the inlet of the grinding unit.
Preferably, the gasification unit is a dry coal powder entrained flow gasifier.
Preferably, the lining of the dry coal powder entrained flow gasifier is a water wall, refractory bricks or a mixture of the two, preferably a water wall.
Preferably, the first powdery mixture contains particles having a particle diameter of 90 μm or more in a volume content of not more than 10%. In this context, the particle volume content is determined by a laser particle size analyzer sampling test.
According to the invention, in the gasification unit, the first pulverized mixture is gasified to produce synthesis gas and ash.
Preferably, the system further comprises a syngas purification unit for receiving the coal gas produced by the co-pyrolysis unit and/or the syngas produced by the gasification unit for processing.
Preferably, the system further comprises an ash handling unit for handling ash produced by the gasification unit.
Preferably, the system also comprises an oil deep processing unit for receiving the tar produced by the co-pyrolysis unit for deep processing treatment.
Preferably, the system further comprises a tar recovery unit to collect tar produced by the co-pyrolysis unit, and a gas recovery unit to collect gas produced by the co-pyrolysis unit.
In a second aspect, the present invention provides a method for treating a coal direct liquefaction residue, the method comprising:
(1) co-pyrolyzing the mixture of the direct coal liquefaction residues and the raw coal to obtain a co-pyrolysis solid product;
(2) mixing the co-pyrolysis solid product and raw coal in proportion, grinding and drying to obtain a first powdery mixture;
(3) gasifying the first powdery mixture.
According to the present invention, preferably, in the step (1), the mass ratio of the coal direct liquefaction residue to the raw coal is 1 (0.01-20), preferably 1: (1-10).
Preferably, the conditions of the co-pyrolysis include: the temperature is 200 ℃ to 600 ℃, preferably 450 ℃ to 550 ℃.
During the co-pyrolysis, tar, coal gas and co-pyrolysis solid products are produced. Preferably, the tar is subjected to an oil further processing treatment, for example, the tar is introduced into an oil further processing unit for oil further processing treatment. Preferably, the gas is subjected to a further purification treatment.
According to the present invention, preferably, in the step (2), the mass ratio of the co-pyrolysis solid product to the raw coal is 1 (0.1-100), preferably 1: (1-20).
In one embodiment, the milling is performed in a mill, preferably a speed disc mill.
In order to obtain a powder having a small particle size suitable for gasification of dry pulverized coal, it is preferable to blow hot air during the pulverization. More preferably, the hot air is nitrogen, flue gas, or a mixed gas of air and nitrogen, wherein the oxygen content is less than 8 vol%.
Preferably, the inlet temperature of the hot air is 140-300 ℃, and the outlet temperature of the hot air is 35-100 ℃; more preferably, the hot air inlet temperature is 150-200 ℃ and the hot air outlet temperature is 35-60 ℃.
Preferably, the amount of inlet hot air required per 1kg of throughput is 0.5-5Nm3Preferably 1-3Nm3. Here, the throughput is a mixture of the co-pyrolysis solid product and raw coal.
Preferably, the pressure difference between the hot air inlet and the hot air outlet is not more than 2000 Pa.
Preferably, the first powdered mixture has an overall water content of 1 to 6%, preferably 1 to 3%, by milling. Preferably, the first powdery mixture contains particles having a particle diameter of 90 μm or more in a volume content of not more than 10%.
Preferably, in step (3), the gasification is carried out in a dry coal powder entrained flow gasifier.
According to the invention, preferably, the conditions of the gasification comprise: the pressure is 0.1-10MPa, and the temperature is 1000-1600 ℃.
The gasification process produces syngas and ash. Preferably, the synthesis gas and the coal gas generated by the optional co-pyrolysis enter a downstream process after being subjected to synthesis gas purification treatment; preferably, the ash is subjected to ash treatment and then is used for building material processing.
According to the invention, preferably, the method further comprises drying and crushing the raw coal;
preferably, the drying conditions include: the temperature is 100-150 ℃.
Preferably, the raw coal is crushed to a particle size of 10mm or less.
Preferably, after crushing and drying, a part of raw coal and the direct coal liquefaction residue are mixed in proportion for co-pyrolysis, and the other part of raw coal and the co-pyrolysis solid product are mixed in proportion for grinding.
In a third aspect, the present invention provides a method for treating a coal direct liquefaction residue using the system of the first aspect of the present invention, the method comprising:
(I) co-pyrolyzing the mixture of the direct coal liquefaction residues and the raw coal in a co-pyrolysis unit to obtain a co-pyrolysis solid product;
(II) grinding and drying the co-pyrolysis solid product and raw coal in a grinding unit according to a certain proportion to obtain a first powdery mixture;
(III) gasifying the first powdered mixture in a gasification unit.
Preferably, the first pulverized mixture is gasified in a dry pulverized coal entrained flow gasifier.
Preferably, in step (II), the mass ratio of the co-pyrolysis solid product to the raw coal is 1 (0.1-100), preferably 1: (1-20).
Preferably, hot air is blown in during the milling process. Preferably, the hot air is a mixed gas of air and nitrogen, wherein the oxygen content is less than 8 vol%.
Preferably, the inlet temperature of the hot air is 140-300 ℃, and the outlet temperature of the hot air is 35-100 ℃; more preferably, the hot air inlet temperature is 150-200 ℃ and the hot air outlet temperature is 35-60 ℃.
Preferably, the amount of inlet hot air required per 1kg of throughput is 0.5-5Nm3Preferably 1-3Nm3。
Preferably, the pressure difference between the hot air inlet and the hot air outlet is not more than 2000 Pa.
Preferably, the first powdery mixture contains particles having a particle diameter of 90 μm or more in a volume content of not more than 10%.
The specific definitions of the steps of the process according to the second aspect of the invention apply equally to the process according to the third aspect of the invention, and are not to be considered superfluous here.
Fig. 1 shows a schematic diagram of an embodiment of the system according to the present invention, which comprises:
the system comprises a co-pyrolysis unit 1, a grinding unit 2, a gasification unit 3, a conveying unit 4, a raw coal crushing and drying unit 5, a synthetic gas purification unit 6, a tar recovery unit 8, an oil deep processing unit 9, a coal gas recovery unit 10 and an ash treatment unit 7. The method for treating the direct coal liquefaction residue by using the system comprises the following steps:
(a) introducing a mixture of the pyrolysis coal direct liquefaction residues and raw coal (processed by the raw coal crushing and drying unit 5) into a co-pyrolysis unit 1 for co-pyrolysis to generate co-pyrolysis solid products, tar and coal gas, wherein the generated tar is collected by a tar recovery unit 8 and further introduced into an oil deep processing unit 9 to be made into finished oil, and the generated coal gas is collected by a coal gas recovery unit 10 to be further introduced into a synthesis gas purification unit 6 for processing for a downstream process.
(b) Introducing the co-pyrolysis solid product and raw coal (treated by the raw coal crushing and drying unit 5, the mass ratio of the co-pyrolysis solid product to the raw coal is 1 (0.1-100)) into a grinding unit 2 for drying and grinding, wherein the drying and grinding conditions comprise: blowing hot air in the milling process, wherein the hot air is preferably nitrogen, flue gas or mixed gas of air and nitrogen, and the oxygen content is less than 8% by volume; preferably, the inlet temperature of the hot air is 140-300 ℃, and the outlet temperature of the hot air is 35-100 ℃; preferably, the amount of inlet hot air required per 1kg of throughput is 0.5-5Nm3(ii) a Preferably, the pressure difference between the hot air inlet and the hot air outlet is not more than 2000Pa, so as to obtain a first powdery mixture, wherein the first powdery mixture preferably has the total water content of 1-6% and the volume content of particles with the particle diameter of more than 90 mu m is not more than 10%.
(c) Introducing the first powdery mixture into a gasification unit 3 through a conveying unit 4 for gasification, wherein the gasification conditions comprise: the pressure is 0.1-10MPa, the temperature is 1000-1600 ℃, the generated synthesis gas is introduced into a synthesis gas purification unit 6 for treatment for downstream processes, and the generated ash is introduced into an ash treatment unit 7 for treatment and then used for building material processing.
Compared with the prior art, the process provided by the invention has the following beneficial technical effects:
(i) the pyrolysis and gasification coupling process can improve the yield of oil gas and can also fully utilize the direct coal liquefaction residue;
(ii) the raw coal and the direct coal liquefaction residues are mixed according to a proportion, so that the process economy can be improved;
(iii) the method of the invention can obtain more oil products and synthesis gas products with high added values, fully utilize the direct coal liquefaction residue, and has simple process and convenient operation.
The present invention will be described in detail below by way of examples.
Example 1
Mixing the coal direct liquefaction residue (200kg/h) and crushed and dried raw coal (200kg/h, particle size of 10mm) into a co-pyrolysis unit 1, and co-pyrolyzing at 550 deg.C under normal pressure to produce tar (110kg/h) and coal gas (3000 Nm)3H, wherein CO and H are contained in the gas254% of the total gas) and the solid products of co-pyrolysis (242 kg/h).
Mixing the co-pyrolysis solid product with crushed and dried raw coal at a mass ratio of 1:3, feeding into a milling unit 2, wherein hot air (mixed gas of air and nitrogen, wherein oxygen content is 5 vol%) in the milling unit 2 has an inlet temperature of 180 deg.C and an outlet temperature of 50 deg.C, and the required inlet hot air amount per 1kg treatment amount is 3Nm3To obtain a first powdery mixture (containing 2.1% of total water and 90 μm or more of particles by volume)6%).
The obtained first powdery mixture is conveyed to a gasification unit 3 through a conveying unit 4 for gasification, and the gasification conditions comprise: the pressure was 4MPa and the temperature was 1350 ℃ producing synthesis gas and ash.
The obtained synthesis gas has an effective gas content of 86%, a carbon conversion rate of 99%, a cold gas efficiency of 83% and a specific oxygen consumption of 334kg/kNm3(CO+H2) The specific coal consumption is 556kg/kNm3(CO+H2)。
Example 2
Mixing the coal direct liquefaction residue (100kg/h) and crushed and dried raw coal (150kg/h, particle size of 10mm) into a co-pyrolysis unit 1, and co-pyrolyzing at 500 deg.C under normal pressure to produce tar (51kg/h) and coal gas (2400 Nm)3H, wherein CO and H are contained in the gas2Content 52% of total gas) and solid products of co-pyrolysis (154 kg/h).
Mixing the solid product of co-pyrolysis with crushed and dried raw coal at a mass ratio of 1:5, feeding into a milling unit 2, wherein hot air (mixed gas of air and nitrogen, wherein oxygen content is 5 vol%) in the milling unit 2 has an inlet temperature of 200 deg.C, an outlet temperature of 35 deg.C, and an inlet hot air amount of 3 Nm/1 kg treatment capacity3To obtain a first powdery mixture (total water content: 1.6%, volume content of particles having a particle diameter of 90 μm or more: 4%).
The obtained first powdery mixture is conveyed to a gasification unit 3 through a conveying unit 4 for gasification, and the gasification conditions comprise: the pressure was 4MPa and the temperature was 1400 ℃ producing synthesis gas and ash.
The obtained synthesis gas has an effective gas content of 86%, a carbon conversion rate of 99%, a cold gas efficiency of 84% and a specific oxygen consumption of 312kg/kNm3(CO+H2) Specific coal consumption of 536kg/kNm3(CO+H2)。
Example 3
Mixing the coal direct liquefaction residue (50kg/h) and crushed and dried raw coal (200kg/h, particle size of 10mm) into a co-pyrolysis unit 1, and co-pyrolyzing at 600 deg.C under normal pressure to produce tar (56kg/h) and coal gas (3000 Nm)3H, wherein CO and H are contained in the gas256% of the total gas) and the solid product of co-pyrolysis (144 kg/h).
Mixing the co-pyrolysis solid product with crushed and dried raw coal at a mass ratio of 1:5, feeding into a milling unit 2, wherein hot air (mixed gas of air and nitrogen, wherein oxygen content is 5 vol%) in the milling unit 2 has an inlet temperature of 240 ℃, an outlet temperature of 60 ℃, and an inlet hot air amount of 3 Nm/1 kg of treatment capacity3To obtain a first powdery mixture (total water content: 1.8%, volume content of particles having a particle diameter of 90 μm or more: 5.4%).
The obtained first powdery mixture is conveyed to a gasification unit 3 through a conveying unit 4 for gasification, and the gasification conditions comprise: the pressure was 4MPa and the temperature was 1400 ℃ producing synthesis gas and ash.
The obtained synthesis gas has an effective gas content of 85%, a carbon conversion rate of 99%, a cold gas efficiency of 82% and a specific oxygen consumption of 332kg/kNm3(CO+H2) Specific coal consumption of 566kg/kNm3(CO+H2)。
Example 4
Treating the coal direct liquefaction residue as described in example 1, except that the inlet temperature of hot air of the pulverizing unit was set to 90 ℃ and the outlet temperature was set to 35 ℃; the rest is the same as in example 1. The first powdery mixture finally obtained contained 30% by volume of particles having a particle diameter of 90 μm or more.
The content of the effective gas of the finally obtained synthetic gas is 74 percent, the carbon conversion rate is 96 percent, the cold coal gas efficiency is 72 percent, and the specific oxygen consumption is 376kg/kNm3(CO+H2) Specific coal consumption of 612kg/kNm3(CO+H2)。
Example 5
The direct coal liquefaction residue was treated in the same manner as in example 1, except that hot air was not blown during the pulverization in the pulverizing unit. The first powdery mixture finally obtained contained 100% by volume of particles having a particle diameter of 90 μm or more. Is not suitable for dry coal powder gasification.
Comparative example 1
The direct coal liquefaction residue was treated in the same manner as in example 1, except that the direct coal liquefaction residue (200kg/h) was separately pyrolyzed.
The final tar yield was 63kg/h, gas (800 Nm)3H, wherein CO and H are contained in the gas2The content of the synthetic gas accounts for 34 percent of the total amount of the coal gas) and a co-pyrolysis solid product (112kg/h), the effective gas content of the gasified synthetic gas is 81 percent, the carbon conversion rate is 98 percent, the cold coal gas efficiency is 78 percent, and the specific oxygen consumption is 366kg/kNm3(CO+H2) Specific coal consumption is 594kg/kNm3(CO+H2)。
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.

Claims (10)

1. A system for processing coal direct liquefaction residues, comprising:
the co-pyrolysis unit is used for directly liquefying the mixture of the residue and the raw coal by pyrolyzing the coal to obtain a co-pyrolysis solid product;
the grinding unit is used for drying and grinding the co-pyrolysis solid product and the raw coal to obtain a first powdery mixture;
the gasification unit is used for gasifying the first powdery mixture;
wherein, the outlet of the co-pyrolysis solid product of the co-pyrolysis unit is communicated with the inlet of the milling unit.
2. The system of claim 1, further comprising a raw coal crushing and drying unit for crushing and drying raw coal, more preferably, an outlet of the raw coal crushing and drying unit is respectively communicated with an inlet of the co-pyrolysis unit and an inlet of the pulverizing unit;
preferably, the system further comprises a conveying unit for conveying the first powdered mixture into the gasification unit, more preferably, the conveying unit is in communication with the outlet of the milling unit and the inlet of the gasification unit.
3. System according to claim 1 or 2, wherein in the milling unit, an air blowing device is provided for blowing air to the milling system during milling.
4. The system of claim 1 or 2, wherein the gasification unit is a dry coal powder entrained flow gasifier;
preferably, the first powdery mixture contains particles having a particle diameter of 90 μm or more in a volume content of not more than 10%.
5. A method of processing coal direct liquefaction residue, the method comprising:
(1) co-pyrolyzing the mixture of the direct coal liquefaction residues and the raw coal to obtain a co-pyrolysis solid product;
(2) mixing the co-pyrolysis solid product and raw coal in proportion, grinding and drying to obtain a first powdery mixture;
(3) gasifying the first powdery mixture.
6. The method according to claim 5, wherein in the step (1), the mass ratio of the coal direct liquefaction residue to the raw coal is 1 (0.01-20), preferably 1: (1-10);
preferably, the conditions of the co-pyrolysis include: the temperature is 200-600 ℃, preferably 450-550 ℃;
preferably, the tar produced by the co-pyrolysis is subjected to oil further processing.
7. The method according to claim 5, wherein in the step (2), the mass ratio of the co-pyrolysis solid product to the raw coal is 1 (0.1-100), preferably 1: (1-20);
preferably, hot air is blown in during the milling process;
preferably, the hot air is nitrogen, flue gas or mixed gas of air and nitrogen, wherein the oxygen content is less than 8% by volume;
preferably, the hot air is a mixed gas of air and nitrogen, wherein the oxygen content is less than 8% by volume;
preferably, the inlet temperature of the hot air is 140-300 ℃, and the outlet temperature of the hot air is 35-100 ℃;
preferably, the amount of inlet hot air required per 1kg of throughput is 0.5-5Nm3Preferably 1-3Nm3；
Preferably, the pressure difference of the hot air inlet and the hot air outlet is not more than 2000 Pa;
preferably, the first powdery mixture contains particles having a particle diameter of 90 μm or more in a volume content of not more than 10%.
8. The method of claim 5, wherein the gasification is carried out in a dry coal fines entrained flow gasifier;
preferably, the conditions of the gasification include: the pressure is 0.1-10MPa, and the temperature is 1000-1600 ℃;
preferably, the method also comprises the steps of drying and crushing the raw coal,
preferably, the drying conditions include: the temperature is 100-150 ℃,
preferably, the raw coal is crushed to a particle size of 20mm or less, preferably 10mm or less.
9. A method of processing coal direct liquefaction residue using the system of any of claims 1-4, the method comprising:
(I) co-pyrolyzing the mixture of the direct coal liquefaction residues and the raw coal in a co-pyrolysis unit to obtain a co-pyrolysis solid product;
(II) drying and grinding the co-pyrolysis solid product and raw coal in a grinding unit according to a ratio to obtain a first powdery mixture;
(III) gasifying the first powdered mixture in a gasification unit;
preferably, the first pulverized mixture is gasified in a dry pulverized coal entrained flow gasifier.
10. The process according to claim 9, wherein in step (II), the mass ratio of the co-pyrolysis solid product to the raw coal is 1 (0.1-100), preferably 1: (1-20);
preferably, hot air is blown in during the milling process;
preferably, the hot air is a mixed gas of air and nitrogen, wherein the oxygen content is less than 8% by volume;
preferably, the inlet temperature of the hot air is 140-300 ℃, and the outlet temperature of the hot air is 35-100 ℃;
preferably, the amount of inlet hot air required per 1kg of throughput is 0.5-5Nm3Preferably 1-3Nm3；
Preferably, the pressure difference of the hot air inlet and the hot air outlet is not more than 2000 Pa;
preferably, the first powdery mixture contains particles having a particle diameter of 90 μm or more in a volume content of not more than 10%.
CN201911350784.XA 2019-12-24 2019-12-24 System and method for treating direct coal liquefaction residues Pending CN113025365A (en)

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Application publication date: 20210625