CN111100658A - Coal chemical hydrogenation pyrolysis process - Google Patents
Coal chemical hydrogenation pyrolysis process Download PDFInfo
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- CN111100658A CN111100658A CN201811252678.3A CN201811252678A CN111100658A CN 111100658 A CN111100658 A CN 111100658A CN 201811252678 A CN201811252678 A CN 201811252678A CN 111100658 A CN111100658 A CN 111100658A
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- 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
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/005—After-treatment of coke, e.g. calcination desulfurization
-
- 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
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- 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
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
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- 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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0966—Hydrogen
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a coal chemical industry hydropyrolysis process, which comprises the following steps: performing coal hydropyrolysis reaction on pulverized coal and synthesis gas, then feeding the pulverized coal and the synthesis gas into a cyclone separator and a fly ash filter for gas-solid separation, sending the obtained oil product to a flash tower, and cooling heavy component oil gas discharged from the bottom of the flash tower through an external heavy oil pipeline to be sent out as a heavy oil product; the light component oil gas enters a rectifying tower to obtain triphenyl and hydrogen; and (3) feeding the semicoke into a coke hydrogenation gasification furnace to obtain a semicoke raw material and raw material ash. The invention discloses a coal chemical industry hydropyrolysis process, which can greatly improve the hydropyrolysis efficiency of the coal chemical industry, and can fully utilize solid, liquid and gaseous states obtained by pyrolysis to form various coal chemical products, thereby greatly improving the output efficiency of the coal chemical products; simple process, low energy consumption, high coal conversion rate, high oil product yield and less equipment investment.
Description
Technical Field
The invention belongs to the technical field of coal chemical industry, relates to a coal chemical industry process, and particularly relates to a coal chemical industry hydropyrolysis process.
Background
The hydropyrolysis of coal is a coal conversion technology newly developed on the basis of coal pyrolysis, and is mainly characterized in that: the coal heating rate is very fast, coal chemical pyrolysis is a key step for coal conversion, and coal gasification, liquefaction, coking and combustion all pass through or generate pyrolysis processes. In different processes, the heating rate and the ambient atmosphere of coal pyrolysis are different; the coal fast hydrogenation pyrolysis technology can obtain liquid aromatic hydrocarbons such as benzene, toluene, xylene, phenol, cresol, xylenol and the like, light oil and the like from coal to the maximum extent, and simultaneously obtain methane-rich high-calorific-value coal gas, and the total carbon conversion rate can reach about 50%; the oil-water separation adopts a sedimentation tank operated intermittently, the flow is complex, the equipment is various, and the device is not favorable for stable operation; reaction tail gas or coal gas is used as fuel gas and is not reasonably utilized; the consumption of hydrogen is large, generally 6-10%, and a large amount of new hydrogen is needed to be supplemented in the process, and circulating oil is also needed to be used as a hydrogen supply solvent, so that the production capacity of the device is reduced.
Disclosure of Invention
In view of the technical problems of coal hydropyrolysis, the invention discloses a coal chemical hydropyrolysis process, which can greatly improve the coal chemical hydropyrolysis efficiency, and can fully utilize the solid, liquid and gaseous states of pyrolysis to form various coal chemical products, thereby greatly improving the output efficiency of the coal chemical products; simple process, low energy consumption, high coal conversion rate, high oil product yield and less equipment investment.
The technical scheme adopted by the invention is as follows:
a coal chemical industry hydropyrolysis process is characterized in that: the coal chemical industry hydropyrolysis process comprises the following steps:
(1) feeding the pulverized coal and the synthesis gas into a hydrocracking reactor for coal hydropyrolysis reaction, wherein the reaction temperature in the hydrocracking reactor is 800-900 ℃, the pressure is 3-5 MPa, the mass flow ratio of the pulverized coal to the synthesis gas is 2: 1-2: 1.5, and the reaction residence time is 2-5 s;
(2) discharging the obtained product from the outlet at the bottom of the coal hydrogenation reactor, cooling to 500-600 ℃, then introducing into a cyclone separator for gas-solid separation, separating out 98% of semicoke, and then conveying to a fly ash filter, wherein the working pressure is 3.0-5.0 MPa, the temperature is 500 ℃, and the dust content is less than 10mg/m3So as to obtain an oil product with dust content less than 0.1 percent;
(3) feeding the pyrolysis semicoke generated by the pyrolysis furnace in the step (2) into a coke hydrogenation gasification furnace, carrying out hydrogenation gasification under the conditions of pressure of 2.0-4.0MPa and temperature of 450-; sending the dust-removing gasified gas subjected to dust removal and purification by the gas-solid separator into a precooler, sending the obtained liquid product into an oil-water separator for oil-water separation, and sending the separated tar into a tar purifier for purification to obtain purified tar;
(4) sending the purified tar obtained in the step (3) into a purified tar separation unit, separating light components of phenols, aromatic hydrocarbons and heavy components of asphaltenes, sending the coal tar with the light and heavy components separated into the coal tar hydrofining unit, obtaining a mixed oil product after passing through the coal tar hydrofining unit, sending the mixed oil product into an oil product separation unit, and obtaining naphtha and fuel oil after treatment;
(6) sending the oil product obtained in the step (2) to a flash tower, separating light component oil gas and heavy component oil gas in the flash tower, and cooling the heavy component oil gas discharged from the bottom of the flash tower through an external heavy oil pipeline to be delivered as a heavy oil product;
(7) the light component oil gas obtained in the step (6) enters a rectifying tower for rectification operation, the rectified light oil flows out from an external light oil pipeline at the bottom of the rectifying tower to form a light oil product, and the rectified high-added-value products such as triphenyl and the like flow out from an external additional product pipeline at the side of the rectifying tower to form high-added-value products such as triphenyl and the like; the rectified gas enters a purifying device through a pipeline, after being purified by the purifying device, a part of gas is discharged from a gas outlet to be used as city gas, the pressure of the purified high-purity hydrogen is 0.2-0.6MPa, the temperature is lower than 60 ℃, and the high-purity hydrogen returns to the hydrogenation gasification furnace after being pressurized by a compressor.
The pulverized coal has the coal quality of 5-90 microns in granularity and 2-3% of water.
The invention has the beneficial effects that:
the coal hydropyrolysis oil-making process provided by the invention recycles the coal hydropyrolysis oil-making byproduct wastewater, can simultaneously prepare products such as coal gas, hydrogen, triphenyl, light oil, heavy oil and the like, improves the effective utilization of resources and reduces the discharge of three wastes; compared with the traditional process, the method has no water participating in the reaction, and the water consumption is only circulating cooling water, so that the water consumption is less; the invention operates under higher pressure, is favorable for the device to enlarge and implement poly-generation; the invention has simple flow, reduces equipment investment, realizes reasonable utilization of resources, has good energy-saving and consumption-reducing effects, and is a novel energy-saving coal hydrogenation oil-making process technology.
Detailed Description
Specific implementations of the present invention will now be further described with reference to examples.
The invention provides a coal chemical industry hydropyrolysis process, which comprises the following steps:
grinding and drying the pulverized coal to obtain pulverized coal with the particle size of 5-90 microns, the water content of 2-3% and the temperature of 105 ℃; feeding the obtained pulverized coal and synthesis gas into a hydrocracking reactor according to the mass flow ratio of 2:1, carrying out a hydropyrolysis reaction at the temperature of 850 ℃ and the pressure of 3-5 MPa, and keeping the reaction time of the pulverized coal and the synthesis gas at 3 s;
discharging the product from the bottom outlet of the coal hydrogenation reactor after passing through the hydropyrolysis reactor, spraying and cooling the product to 550 ℃ by adopting purified wastewater, then introducing the product into a cyclone separator for gas-solid separation, separating 98% of semicoke, and then conveying the semicoke to a fly ash filter, wherein the working pressure is 4MPa, the temperature is 500 ℃, and the dust content is 9mg/m3Filtering the oil product by a filter to obtain an oil product with dust content of 0.08 percent;
sending the separated semicoke into a coke hydrogenation gasification furnace, carrying out hydrogenation gasification under the conditions of pressure of 3MPa and temperature of 480 ℃, sending part of the split hydropyrolysis semicoke into coke quenching passivation equipment, carrying out coke quenching and passivation treatment to obtain a semicoke raw material which can be directly utilized, sending part of the hydropyrolysis semicoke split by a semicoke splitter into the gasification furnace together with a gasification agent, carrying out semicoke gasification reaction at 1500 ℃, sending gasification gas discharged from the gasification furnace into ash and ash left after gasification of the gasification furnace, and taking the ash and ash as raw material for processing and utilization; sending the dust-removing gasified gas subjected to dust removal and purification by the gas-solid separator into a precooler, sending the obtained liquid product into an oil-water separator for oil-water separation, and sending the separated tar into a tar purifier for purification to obtain purified tar; sending the obtained purified tar into a purified tar separation unit, separating light components of phenols, aromatic hydrocarbons and heavy components of asphaltenes, sending the coal tar with the separated light and heavy components into a coal tar hydrofining unit, obtaining a mixed oil product after passing through the coal tar hydrofining unit, sending the mixed oil product into an oil product separation unit, and obtaining naphtha and fuel oil after treatment;
sending the obtained oil product with the dust content of 0.08% to a flash tower, separating light component oil gas and heavy component oil gas in the flash tower, and cooling the heavy component oil gas discharged from the bottom of the flash tower through an external heavy oil pipeline to be delivered as a heavy oil product; the obtained light component oil gas of the flash tower enters a rectifying tower for rectification operation, the rectified light oil flows out from an external light oil pipeline at the bottom of the rectifying tower to form a light oil product, and the rectified high-added-value products such as triphenyl and the like flow out from an external additional product pipeline at the side of the rectifying tower to form high-added-value products such as triphenyl and the like; and the rectified gas enters a purification device through a pipeline, after the gas is purified by the purification device, a part of the gas is discharged from a gas outlet to be used as urban gas, the pressure of the purified high-purity hydrogen is 0.3MPa, the temperature is 50 ℃, and the high-purity hydrogen is pressurized by a compressor and then returns to the hydrogenation gasification furnace.
The coal chemical industry hydropyrolysis process provided by the embodiment can greatly improve the coal chemical industry hydropyrolysis efficiency, has high production efficiency and high product purity, can prepare products such as coal gas, hydrogen, triphenyl, light oil, heavy oil and the like, reduces the production cost, and brings huge economic benefits.
Claims (2)
1. A coal chemical industry hydropyrolysis process is characterized in that: the coal chemical industry hydropyrolysis process comprises the following steps:
(1) feeding the pulverized coal and the synthesis gas into a hydrocracking reactor for coal hydropyrolysis reaction, wherein the reaction temperature in the hydrocracking reactor is 800-900 ℃, the pressure is 3-5 MPa, the mass flow ratio of the pulverized coal to the synthesis gas is 2: 1-2: 1.5, and the reaction residence time is 2-5 s;
(2) discharging the obtained product from the bottom outlet of the coal hydrogenation reactor,cooling to 500-600 ℃, then entering a cyclone separator for gas-solid separation, separating 98% of semicoke, and then sending the semicoke to a fly ash filter, wherein the working pressure is 3.0-5.0 MPa, the temperature is 500 ℃, and the dust content is less than 10mg/m3So as to obtain an oil product with dust content less than 0.1 percent;
(3) feeding the pyrolysis semicoke generated by the pyrolysis furnace in the step (2) into a coke hydrogenation gasification furnace, carrying out hydrogenation gasification under the conditions of pressure of 2.0-4.0MPa and temperature of 450-; sending the dust-removing gasified gas subjected to dust removal and purification by the gas-solid separator into a precooler, sending the obtained liquid product into an oil-water separator for oil-water separation, and sending the separated tar into a tar purifier for purification to obtain purified tar;
(4) sending the purified tar obtained in the step (3) into a purified tar separation unit, separating light components of phenols, aromatic hydrocarbons and heavy components of asphaltenes, sending the coal tar with the light and heavy components separated into the coal tar hydrofining unit, obtaining a mixed oil product after passing through the coal tar hydrofining unit, sending the mixed oil product into an oil product separation unit, and obtaining naphtha and fuel oil after treatment;
(5) sending the oil product obtained in the step (2) to a flash tower, separating light component oil gas and heavy component oil gas in the flash tower, and cooling the heavy component oil gas discharged from the bottom of the flash tower through an external heavy oil pipeline to be delivered as a heavy oil product;
(6) the light component oil gas obtained in the step (6) enters a rectifying tower for rectification operation, the rectified light oil flows out from an external light oil pipeline at the bottom of the rectifying tower to form a light oil product, and the rectified high-added-value products such as triphenyl and the like flow out from an external additional product pipeline at the side of the rectifying tower to form high-added-value products such as triphenyl and the like; the rectified gas enters a purifying device through a pipeline, after being purified by the purifying device, a part of gas is discharged from a gas outlet to be used as city gas, the pressure of the purified high-purity hydrogen is 0.2-0.6MPa, the temperature is lower than 60 ℃, and the high-purity hydrogen returns to the hydrogenation gasification furnace after being pressurized by a compressor.
2. The coal chemical hydropyrolysis process of claim 1, wherein: the coal quality of the pulverized coal is 5-90 microns in granularity and 2-3% in water content.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811252678.3A CN111100658A (en) | 2018-10-25 | 2018-10-25 | Coal chemical hydrogenation pyrolysis process |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201811252678.3A CN111100658A (en) | 2018-10-25 | 2018-10-25 | Coal chemical hydrogenation pyrolysis process |
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| CN111100658A true CN111100658A (en) | 2020-05-05 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115466630A (en) * | 2022-09-09 | 2022-12-13 | 上海寰球工程有限公司 | Phenol tar hydrotreating method |
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2018
- 2018-10-25 CN CN201811252678.3A patent/CN111100658A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115466630A (en) * | 2022-09-09 | 2022-12-13 | 上海寰球工程有限公司 | Phenol tar hydrotreating method |
| CN115466630B (en) * | 2022-09-09 | 2024-04-30 | 上海寰球工程有限公司 | Phenol tar hydrotreating method |
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Application publication date: 20200505 |