CN106497606B - Coal direct hydrogenation method for pyrolysis - Google Patents
Coal direct hydrogenation method for pyrolysis Download PDFInfo
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- CN106497606B CN106497606B CN201610858298.9A CN201610858298A CN106497606B CN 106497606 B CN106497606 B CN 106497606B CN 201610858298 A CN201610858298 A CN 201610858298A CN 106497606 B CN106497606 B CN 106497606B
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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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
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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
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
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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
- 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
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
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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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
-
- 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
- C10J3/50—Fuel charging devices
-
- 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
- C10J3/62—Processes with separate withdrawal 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
- C10J3/58—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
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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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
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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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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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
- 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
- C10J2300/0959—Oxygen
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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
- 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
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The present invention relates to a kind of coal direct hydrogenation method for pyrolysis, coal dust from coal-grinding apparatus is sent by pulverized coal conveying device to the gasification nozzle of gasification furnace and fine coal nozzle, the steam generated by drum and the oxygen come from battery limit (BL) enter vaporizer reaction, generation high temperature hydrogen-rich synthetic gas and cinder via gasification nozzle together with coal dust；Cinder enters in shock chamber along down-comer, and synthesis gas enters pyrolysis chamber via each spray orifice, reacts with the coal dust from fine coal burner, and the oil gas and coal tar of generation enter cyclone separator and isolates coal tar and oil gas；Enter gas and oil separating plant after oil gas and boiler water heat exchange, isolates oil product and fuel gas；Fuel gas enters gas cleaning plant, isolates synthesis gas and fuel gas, and fuel gas sends to coal-grinding unit；Boiler water after heat exchange enters the cold wall of gasification furnace, generates steam water interface after absorbing heat, steam water interface enters drum, separate vapour and water, and steam sends to gasification nozzle.
Description
Technical field
The present invention relates to coal chemical industries, refer specifically to a kind of coal direct hydrogenation method for pyrolysis.
Background technique
Coal direct hydrogenation technical process mainly include the broken and drying of coal, coal slurry preparation, hydrogenation liquefaction, separation of solid and liquid,
Gas purification, liquid product fractionation and the parts such as purification and hydrogen manufacturing.Main flow are as follows: at high temperature under high pressure, high concentration coal slurry
In coal be pyrolyzed, carry out under the action of catalyst plus hydrogen and decomposition, eventually become stable fluid molecule.Liquefaction process
In, by coal slurry made of coal, catalyst and recycle oil, is mixed with hydrogen obtained and be sent into reactor.In liquefying reactor, coal
Pyrolytic reaction occurs first, generates free radical " fragment ", unstable free radical " fragment " is again with hydrogen in catalyst existence condition
Lower combination forms the molecular weight primary hydrogenation products more much lower than coal.The product of reactor is constituted sufficiently complex out, including gas,
Liquid, solid three-phase.The main component of gas phase is hydrogen, and reactor is recycled back into after separation and participates in reaction again；Solid phase is unreacted
Coal, minerals and catalyst；Liquid phase is then the fractions such as light oil (raw gasoline), middle oil oil and heavy oil.Liquid phase fraction oil is through upgrading
Processing (such as hydrofinishing is hydrocracked and reforms) obtains the products such as qualified gasoline, diesel oil and aviation kerosine.The liquid of heavy
Gu slurry is prepared as circulation solvent for coal slurry through further isolated heavy oil and residue, heavy oil.
In existing direct coal liquefaction technology, reactor reaction pressure is up to 17MPa-30Mpa, and hydrogen consumption is up to 6%-
10%, process is complicated, and cost of investment is high.A large amount of new hydrogen are not only supplemented in technical process, it is also necessary to recycle oil makees hydrogen supply dissolvent,
Plant capacity reduces, out the product complicated composition of liquefying reactor, and solid-liquid two-phase laminated flow is difficult, and oil productivity is low.
Summary of the invention
The technical problem to be solved by the present invention is to the statuses for the prior art to provide a kind of collection coal hydrogen manufacturing and coal hydrogenation
Integration, without mating coal device for producing hydrogen and reaction condition is mild, hydrogen consumption is small, oil productivity is high coal direct hydrogenation method.
The technical scheme of the invention to solve the technical problem is: the coal direct hydrogenation method for pyrolysis, feature
It is to include the following steps:
Coal dust from coal-grinding apparatus is sent by pulverized coal conveying device to the gasification nozzle of gasification furnace and fine coal nozzle,
In, it is 4~15m/s that fine coal, which conveys mixed phase flow velocity,；Hybrid density is 200~550kg/m3；
By drum generate steam and from battery limit (BL) come oxygen together with coal dust via gasification nozzle enter vaporizer react,
Generate high temperature hydrogen-rich synthetic gas and cinder；The ratio for controlling steam, oxygen and coal dust is 0.2~0.8Nm3Oxygen/kg coal, 0.1
~0.5Nm3Steam/Nm3Oxygen；Controlling vaporizer interior reaction temperature is 600~1500 DEG C, and pressure is 1.0~6.0MPag；
Cinder and synthesis gas enter down-comer；Cinder enters in shock chamber under self gravitation effect along down-comer, cooling
After be discharged；
Synthesis gas uplink enters in pyrolysis chamber via each spray orifice, reacts with the coal dust from fine coal burner, generate oil gas and
Coal tar；Control that the indoor reaction temperature of the pyrolysis is 600~1200 DEG C, pressure is 1.0~6.0MPag；
The oil gas and coal tar are discharged from discharge port, into cyclone separator in isolate coal tar and oil gas；
Coal tar after separation is discharged from the outlet at bottom of the cyclone separator；The oil gas isolated is then from cyclone separator
Top exit discharge, with boiler water heat exchange after enter gas and oil separating plant, isolate oil product and with CO, H2And CH4For mainly at
The fuel gas divided；
The fuel gas enters gas cleaning plant, isolates synthesis gas and fuel gas, and fuel gas sends to coal-grinding apparatus；
Boiler water after heat exchange enters the cold wall of the gasification furnace, generates steam water interface, steam-water mixing after absorbing heat
Object enters drum, separate vapour and water, and the steam sends to the gasification nozzle.
It is preferred that the partial size of the coal dust is less than or equal to 90 microns, water content is less than or equal to 2wt%, the temperature of coal dust is 80~
100℃。
The pulverized coal conveying device is Pneumatic conveyer.
It is preferred that the cyclonic separation is two stage cyclone separation.
Preferably, the top of the gasification furnace in above-mentioned each scheme is equipped with gasification nozzle, the inner cavity of the gasification furnace is from upper
Vaporizer, pyrolysis chamber and shock chamber are successively arranged under and, the upper port of down-comer connects the outlet at bottom of the vaporizer, described
The lower port of down-comer passes through the pyrolysis chamber and is inserted into the shock chamber；The bottom of the gasification furnace is exported equipped with slag；
The top entry of the down-comer connects the lateral wall of the vaporizer by guard seal；It is spaced on the baffle
Equipped with multiple opposite directions pyrolysis chamber's spray orifice；
The side wall of the gasification furnace is equipped with the fine coal nozzle of at least one opposite pyrolysis chamber；The side of the gasification furnace
The material outlet for being connected to the pyrolysis chamber is additionally provided on wall.
The axial angle of the baffle and the gasification furnace is 15~60 °.
The axial direction of the fine coal nozzle and the radial angle of the gasification furnace (1) are 0~60 °, so that coal dust and synthesis gas
It comes into full contact with, improves reaction efficiency.
The bottom surface of the pyrolysis chamber is arranged relative to the sidewall slope of the gasification furnace, and the material outlet is arranged described
The extreme lower position of pyrolysis chamber.
The fine coal nozzle has multiple, and the peripheral wall along the gasification furnace is evenly arranged.
Compared with prior art, provided by the present invention is coal direct hydrogenation method for pyrolysis, and coal hydrogen manufacturing and pyrolysis of coal are integrated
Coal hydrogen manufacturing and the integration of coal hydrogenation are realized in a reactor, is not necessarily to mating coal device for producing hydrogen；And reaction condition is mild,
External hydrogen source is not needed, hydrogen consumption is small, and only 2% or so, oil productivity is high, low equipment investment；And catalyst is needed, operation operation
Expense is low；
Key reaction is completed in 1~3 second, and reactor for treatment ability is big；
Vaporizer and pyrolysis chamber are water wall structure, the most of heat reacted by recycling gasification reaction with hydrogenation
Amount generates a large amount of steam and reduces energy consumption；Synthesis gas partial heat is recycled by useless pot, improves heat utilization rate；It is energy-saving
Effect is good；
Gas and oil separating plant and gas cleaning plant are isolated fuel gas and are used for coal-grinding apparatus, and the circulation of material is realized
It utilizes, improves the efficiency of package unit.
Detailed description of the invention
Fig. 1 is flow diagram of the embodiment of the present invention；
Fig. 2 is the enlarged drawing of gasification furnace in the embodiment of the present invention；
Fig. 3 is the schematic cross-sectional view of gasification nozzle in the embodiment of the present invention；
Fig. 4 is the schematic cross-sectional view of fine coal nozzle in the embodiment of the present invention；
Fig. 5 is fine coal of embodiment of the present invention arrangement of nozzles schematic diagram.
Specific embodiment
The present invention will be described in further detail below with reference to the embodiments of the drawings.
As shown in Figures 1 to 5, main reactor used in the present embodiment is gasification furnace 1, and the top of gasification furnace 1 is equipped with
Gasification nozzle 2, the bottom of gasification furnace are equipped with slag outlet 14；The inner cavity of gasification furnace is divided into vaporizer 11, pyrolysis from top to bottom
Room 15 and shock chamber 13.
Wherein, the bottom surface of pyrolysis chamber 15 is arranged relative to the sidewall slope of gasification furnace 1；The side wall of gasification furnace 1, which is equipped with, to be connected
The lowest position of pyrolysis chamber 15 is arranged in the material outlet 17 of logical pyrolysis chamber 15, material outlet 17, to facilitate discharging.
The bottom of vaporizer 11 is pyramidal structure, and outlet at bottom 16 is the up-small and down-big horn mouth extended out, and bottom goes out
Mouth connection down-comer 12 is simultaneously accommodated in baffle 4.
Down-comer 12 connects vaporizer 11 and shock chamber 13, is the decline passway of slag charge；Its lower port passes through pyrolysis chamber 15
Bottom surface is inserted into the liquid level of shock chamber；The top entry of down-comer 12 is tightly connected the lateral wall of vaporizer 11 by baffle 4.
In the present embodiment, the axial angle of baffle 4 and gasification furnace 1 is that multiple opposite pyrolysis chambers are equipped at intervals on 45 ° of baffles 4
15 spray orifice 41.
Shock chamber 13 goes out gasification furnace for carrying out cooling heel row to slag charge caused by reaction, and down-comer 12 is connected with sharp
Device for cooling (not shown) is used for cooling protection down-comer, while providing cooling water to shock chamber；On the side wall of shock chamber also
Equipped with Quench aquaporin 18, it is used for the moisturizing into shock chamber, keeps liquid level in shock chamber.
Chilling device in the present embodiment can select as needed it is in the prior art any one.
Gasification nozzle 2 can be selected in the prior art any one as needed for the spray feed reaction mass into vaporizer
Kind.Gasification nozzle 2 in the present embodiment includes the first noumenon, is successively arranged fuel channel 22, oxygen from inside to outside on the first noumenon
Gas channel 23, steam channel 24 and the first cooling duct 25；Interlayer 26 between fuel channel 22 and the oxygen channel 23 is adopted
It is prepared with wear-resistant material.
Fine coal nozzle 3 has eight, is evenly arranged in the circumferential side wall of gasification furnace, exports opposite pyrolysis chamber 15, is used for heat
It solves and sprays coal dust in room 15；Including the second ontology 31, the second ontology 31 is equipped with fine coal channel 32, and fine coal channel 32 is externally provided with the
Two cooling ducts 33.Second ontology 31 is prepared using wear-resistant material.
In the present embodiment, the axial direction of fine coal nozzle 3 and the radial angle of gasification furnace 1 are 60 °, the bottom conical surface with vaporizer
It is parallel.
It is 80~100 that partial size from coal-grinding apparatus 8, which is less than or equal to 2wt% // temperature less than or equal to 90 microns, water content,
DEG C coal dust sent to the gasification nozzle 2 of gasification furnace 1 and fine coal nozzle 3 by pulverized coal conveying device 9, wherein fine coal conveying mixing
Phase flow velocity is 10m/s；Hybrid density is 350kg/m3；The pulverized coal conveying device 9 is Pneumatic conveyer, and conveying gas is nitrogen
Gas, discharge pressure 4.0MPag.
The steam that is generated by drum 10 and from battery limit (BL) Lai oxygen enter vaporizer 11 via gasification nozzle 2 together with coal dust
Reaction is generated with CO+H2For the high temperature hydrogen-rich synthetic gas and cinder mainly formed；Control steam, oxygen and coal dust ratio be
0.50Nm3Oxygen/kg coal, quantity of steam can use 0.3Nm3/Nm3Oxygen；Controlling vaporizer interior reaction temperature is 600~1500 DEG C, pressure
Power is 1.0~6.0MPag；
Cinder and synthesis gas enter down-comer 12；Cinder enters shock chamber 13 along down-comer 12 under self gravitation effect
It is interior, it is discharged after cooling；The temperature of controlled chilling room is at 300 DEG C or less.
Synthesis gas uplink enters in pyrolysis chamber 15 via each spray orifice 41, reacts with the coal dust from fine coal burner 3, generates
Oil gas and coal tar；Control that the reaction temperature in the pyrolysis chamber 15 is 800~900 DEG C, pressure is 3.5 ± 0.2MPag；
The oil gas and coal tar are discharged from discharge port 17, sequentially enter in two stage cyclone separator 5 and isolate coal tar and oil
Gas；
Coal tar after separation is discharged from the outlet at bottom of the cyclone separator 5；The oil gas isolated is then from cyclonic separation
The top exit of device 5 is discharged, and enters gas and oil separating plant 6 after exchanging heat with boiler water, isolates oil product and with CO, H2And CH4Based on
Want the fuel gas of ingredient；
Fuel gas enters gas cleaning plant 7, isolates synthesis gas and fuel gas, and fuel gas sends to coal-grinding apparatus 8；
Boiler water after heat exchange enters the cold wall of the gasification furnace 1, generates steam water interface, steam-water mixing after absorbing heat
Object enters drum, separate vapour and water, and steam sends to the gasification nozzle 2.
Efficiency is up to 70~80% in the present invention, in the prior art the efficiency of Technology of direct coal liquefaction only about 50%；Coal
Consumption is 3.3~3.5 tons, is lower than existing Technology of direct coal liquefaction；Liquid-phase product yield is first intake up to 25~33% with existing
It is flat to maintain an equal level；CO20.05~0.5 ton/ton oil product of discharge amount obviously subtracts than existing 5~6 ton/ton oil product of Technology of direct coal liquefaction
Few, megaton Tou Zi not be the 50~60% of existing Technology of direct coal liquefaction.
Comprehensive technical indexes, environmental protection index and investing, the present invention all have apparent advantage compared with prior art.
Claims (8)
1. coal direct hydrogenation method for pyrolysis, it is characterised in that include the following steps:
Coal dust from coal-grinding apparatus (8) is sent by pulverized coal conveying device (9) to the gasification nozzle of gasification furnace (1) (2) and fine coal
Nozzle (3), wherein it is 4~15m/s that fine coal, which conveys mixed phase flow velocity,；Hybrid density is 200~550kg/m3；
The steam generated by drum (10) and the oxygen come from battery limit (BL) are together with coal dust via gasification nozzle (2) into vaporizer
(11) it reacts, generates high temperature hydrogen-rich synthetic gas and cinder；The ratio for controlling steam, oxygen and coal dust is 0.2~0.8Nm3Oxygen/
Kg coal, 0.1~0.5Nm3Steam/Nm3Oxygen；Vaporizer interior reaction temperature is 600~1500 DEG C, and pressure is 1.0~6.0MPag；
Cinder and synthesis gas enter down-comer (12)；Cinder enters shock chamber (13) along down-comer (12) under self gravitation effect
It is interior, it is discharged after cooling；
Synthesis gas uplink enters in pyrolysis chamber (15) via each spray orifice (41), reacts with the coal dust from fine coal nozzle (3), raw
Olefiant gas and coal tar；Control that the reaction temperature in the pyrolysis chamber (15) is 600~1200 DEG C, pressure is 1.0~6.0MPag；
The oil gas and coal tar are discharged from discharge port (17), isolate coal tar and oil gas into cyclone separator (5) is interior；
Coal tar after separation is discharged from the outlet at bottom of the cyclone separator (5)；The oil gas isolated is then from cyclone separator
(5) top exit discharge, enters gas and oil separating plant (6) after exchanging heat with boiler water, isolates oil product and with CO, H2And CH4For
The fuel gas of main component；
The fuel gas enters gas cleaning plant (7), isolates synthesis gas and fuel gas, and fuel gas sends to coal-grinding apparatus
(8)；
Boiler water after heat exchange enters the cold wall of the gasification furnace (1), generates steam water interface, steam water interface after absorbing heat
Into drum, separate vapour and water, the steam send to the gasification nozzle (2)；
The top of the gasification furnace (1) is equipped with gasification nozzle (2), and the inner cavity of the gasification furnace is successively arranged vaporizer from top to bottom
(11), pyrolysis chamber (15) and shock chamber (13), the upper port of down-comer (12) connect the outlet at bottom of the vaporizer (11), institute
The lower port for stating down-comer (12) passes through the pyrolysis chamber (15) and is inserted into the shock chamber (13)；The gasification furnace (1)
Bottom is equipped with slag outlet (14)；
The top entry of the down-comer (12) is tightly connected the lateral wall of the vaporizer (11) by baffle (4)；The gear
The multiple opposite direction pyrolysis chamber (15) spray orifices (41) are equipped at intervals on plate (4)；
The side wall of the gasification furnace (1) is equipped with the fine coal nozzle (3) of at least one opposite pyrolysis chamber (15)；The gasification
The material outlet (17) for being connected to the pyrolysis chamber (15) is additionally provided on the side wall of furnace (1).
2. coal direct hydrogenation method for pyrolysis according to claim 1, it is characterised in that the partial size of the coal dust is less than or equal to
90 microns, water content is less than or equal to 2wt%, and the temperature of coal dust is 80~100 DEG C.
3. coal direct hydrogenation method for pyrolysis according to claim 1 or 2, it is characterised in that the pulverized coal conveying device (9)
For Pneumatic conveyer.
4. coal direct hydrogenation method for pyrolysis according to claim 3, it is characterised in that the cyclonic separation is two stage cyclone
Separation.
5. coal direct hydrogenation method for pyrolysis according to claim 1, it is characterised in that the baffle (4) and the gasification furnace
(1) axial angle is 15~60 °.
6. coal direct hydrogenation method for pyrolysis according to claim 5, it is characterised in that the axial direction of the fine coal nozzle (3) with
The radial angle of the gasification furnace (1) is 0~60 °.
7. coal direct hydrogenation method for pyrolysis according to claim 6, it is characterised in that the bottom surface phase of the pyrolysis chamber (15)
Sidewall slope setting for the gasification furnace (1), lowest order of material outlet (17) setting in the pyrolysis chamber (15)
It sets.
8. coal direct hydrogenation method for pyrolysis according to claim 7, it is characterised in that the fine coal nozzle (3) have it is multiple,
Peripheral wall along the gasification furnace is evenly arranged.
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