CN106497606A - Coal direct hydrogenation method for pyrolysis - Google Patents

Coal direct hydrogenation method for pyrolysis Download PDF

Info

Publication number
CN106497606A
CN106497606A CN201610858298.9A CN201610858298A CN106497606A CN 106497606 A CN106497606 A CN 106497606A CN 201610858298 A CN201610858298 A CN 201610858298A CN 106497606 A CN106497606 A CN 106497606A
Authority
CN
China
Prior art keywords
coal
gas
pyrolysis
gasification
nozzle
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN201610858298.9A
Other languages
Chinese (zh)
Other versions
CN106497606B (en
Inventor
郭强
赵国忠
李克海
杨松峰
王鲁杰
李峰
吴德民
曹孟常
吴妙奇
陈文哲
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sinopec Engineering Group Co Ltd
Sinopec Ningbo Engineering Co Ltd
Sinopec Ningbo Technology Research Institute
Original Assignee
Sinopec Engineering Group Co Ltd
Sinopec Ningbo Engineering Co Ltd
Sinopec Ningbo Technology Research Institute
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sinopec Engineering Group Co Ltd, Sinopec Ningbo Engineering Co Ltd, Sinopec Ningbo Technology Research Institute filed Critical Sinopec Engineering Group Co Ltd
Priority to CN201610858298.9A priority Critical patent/CN106497606B/en
Publication of CN106497606A publication Critical patent/CN106497606A/en
Application granted granted Critical
Publication of CN106497606B publication Critical patent/CN106497606B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • 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
    • 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
    • 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
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The present invention relates to a kind of coal direct hydrogenation method for pyrolysis, coal dust from coal-grinding apparatus delivers to the gasification nozzle and fine coal nozzle of gasification furnace by pulverized coal conveying device, the steam produced by drum and the oxygen come from battery limit (BL) enter vaporizer reaction via gasification nozzle together with coal dust, produce high temperature hydrogen-rich synthetic gas and cinder；Cinder is entered in Quench room along down-comer, and synthesis gas enters pyrolysis chamber via each spray orifice, is reacted with the coal dust from fine coal burner, and the oil gas of generation and coal tar enter cyclone separator and isolate coal tar and oil gas；Gas and oil separating plant is entered after oil gas and boiler water heat exchange, oil product and fuel gas is isolated；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, and steam water interface enters drum, separate vapour and water, and steam sends to gasification nozzle.

Description

Coal direct hydrogenation method for pyrolysis
Technical field
The present invention relates to Coal Chemical Industry, refers specifically to a kind of coal direct hydrogenation method for pyrolysis.
Background technology
Coal direct hydrogenation technical process mainly include the broken and drying of coal, coal slurry preparation, hydrogenation liquefaction, separation of solid and liquid, The parts such as gas purification, fluid product fractionation and refined and hydrogen manufacturing.Main flow is：At high temperature under high pressure, high concentration coal slurry In coal be pyrolyzed, be hydrogenated with catalyst action and decomposed, eventually become stable fluid molecule.Liquefaction process In, coal slurry that coal, catalyst and recycle oil are made mixes feeding reactor with obtained hydrogen.In liquefying reactor, coal There is pyrolytic reaction first, generate 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.Go out reactor product constitute sufficiently complex, including gas, Liquid, solid three-phase.The main component of gas phase is hydrogen, separates Posterior circle Returning reactor and participates in again reaction；Solid phase is unreacted Coal, mineral matter 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, be hydrocracked and reform) obtains the products such as qualified gasoline, diesel oil and aviation kerosine.The liquid of heavy Gu slurry is prepared for coal slurry as circulating solvent 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%, flow process is complicated, and cost of investment is high.A large amount of new hydrogen will be not only supplemented in technical process, in addition it is also necessary to which hydrogen supply dissolvent made by recycle oil, Plant capacity reduces, and the product composition for going out liquefying reactor is complicated, and solid-liquid two-phase laminated flow is difficult, and oil productivity is low.
Content of the invention
The technical problem to be solved is a kind of present situation offer collection coal hydrogen manufacturing and the coal hydrogenation for prior art Integration, without the need for supporting coal device for producing hydrogen and reaction condition be gentle, the coal direct hydrogenation method that hydrogen consumption is little, oil productivity is high.
The present invention solve the technical scheme that adopted of above-mentioned technical problem for：The coal direct hydrogenation method for pyrolysis, its feature It is to comprise the steps：
Coal dust from coal-grinding apparatus delivers to the gasification nozzle and fine coal nozzle of gasification furnace by pulverized coal conveying device, its In, fine coal conveying mixed phase flow velocity is 4～15m/s；Hybrid density is 200～550kg/m3；
The steam produced by drum and the oxygen come from battery limit (BL) enter vaporizer reaction via gasification nozzle together with coal dust, Produce high temperature hydrogen-rich synthetic gas and cinder；The ratio for controlling steam, oxygen and coal dust is 0.2～0.8Nm3Oxygen/kg coals, 0.1 ～0.5Nm3Steam/Nm3Oxygen；Vaporizer interior reaction temperature is controlled for 600～1500 DEG C, pressure is 1.0～6.0MPag；
Cinder and synthesis gas enter down-comer；Cinder is entered in Quench room in self gravitation effect, lower edge down-comer, cooling After discharge；
Synthesis gas is up, enters via each spray orifice that pyrolysis is indoor, reacts with the coal dust from fine coal burner, generate oil gas and Coal tar；The reaction temperature for controlling the pyrolysis interior is 600～1200 DEG C, pressure is 1.0～6.0MPag；
The oil gas and coal tar are discharged from discharging opening, are entered in cyclone separator and are isolated coal tar and oil gas；
Coal tar after separating is discharged from the outlet at bottom of the cyclone separator；The oil gas that isolates 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 main into The fuel gas for dividing；
The 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 the gasification furnace, generates steam water interface, steam-water mixing after absorbing heat Thing enters drum, separate vapour and water, and the steam sends to the gasification nozzle.
It is preferred that the particle diameter 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 separated for two stage cyclone.
Preferably, be provided with gasification nozzle at the top of gasification furnace in above-mentioned each scheme, the inner chamber of the gasification furnace is from upper And under be sequentially provided with vaporizer, pyrolysis chamber and shock chamber, the upper port of down-comer connects the outlet at bottom of the vaporizer, described The lower port of down-comer is inserted in the Quench room through the pyrolysis chamber；The bottom of the gasification furnace is provided with slag outlet；
The top entry of the down-comer connects the lateral wall of the vaporizer by guard seal；It is spaced on the baffle plate It is provided with multiple to pyrolysis chamber's spray orifice；
The side wall of the gasification furnace is provided with least one pair of fine coal nozzle to the pyrolysis chamber；The side of the gasification furnace The material outlet for connecting the pyrolysis chamber is additionally provided with wall.
The baffle plate is 15～60 ° with the axial angle of the gasification furnace.
The axial direction of the fine coal nozzle is 0～60 ° with the radial direction angle of the gasification furnace (1), so that coal dust and synthesis gas It is fully contacted, 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 on described The extreme lower position of pyrolysis chamber.
The fine coal nozzle has multiple, and the perisporium along the gasification furnace is evenly arranged.
Compared with prior art, provided by the present invention is coal direct hydrogenation method for pyrolysis, will be integrated to coal hydrogen manufacturing and pyrolysis of coal Coal hydrogen manufacturing and the integration of coal hydrogenation is achieved in a reactor, without the need for supporting coal device for producing hydrogen；And reaction condition is gentle, External hydrogen source is not needed, hydrogen consumption is little, only 2% or so, oil productivity is high, low equipment investment；And need catalyst, operation operation Expense is low；
Key reaction was completed in 1～3 second, and reactor for treatment ability is big；
Vaporizer is water wall structure with pyrolysis chamber, by reclaiming the major part heat of gasification reaction and hydrogenation reaction Amount, produces a large amount of steam and reduces energy consumption；Synthesis gas partial heat is reclaimed by useless pot, heat utilization rate is improve；Energy-saving Effect is good；
Gas and oil separating plant is isolated fuel gas with gas cleaning plant and is used for coal-grinding apparatus, it is achieved that the circulation of material Utilize, improve the efficiency of package unit.
Description of the drawings
Fig. 1 is embodiment of the present invention schematic flow sheet；
Fig. 2 is the enlarged drawing of gasification furnace in the embodiment of the present invention；
Fig. 3 is the cross-sectional schematic of gasification nozzle in the embodiment of the present invention；
Fig. 4 is the cross-sectional schematic of fine coal nozzle in the embodiment of the present invention；
Fig. 5 is embodiment of the present invention fine coal arrangement of nozzles schematic diagram.
Specific embodiment
The present invention is described in further detail below in conjunction with accompanying drawing embodiment.
As shown in Figures 1 to 5, the main reactor used in the present embodiment is gasification furnace 1, and the top of gasification furnace 1 is provided with Gasification nozzle 2, the bottom of gasification furnace are provided with slag outlet 14；The inner chamber 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 is provided with company The material outlet 17 of logical pyrolysis chamber 15, material outlet 17 are arranged on its lowest position of pyrolysis chamber 15, to facilitate discharging.
The bottom of vaporizer 11 is pyramidal structure, and its outlet at bottom 16 is the up-small and down-big horn mouth for extending out, and bottom goes out Mouth connection down-comer 12 is simultaneously contained in baffle plate 4.
Down-comer 12, connection vaporizer 11 and shock chamber 13, are the decline passway of slag charge；Its lower port passes through pyrolysis chamber 15 Bottom surface is inserted in the liquid level of shock chamber；The top entry of down-comer 12 is tightly connected the lateral wall of vaporizer 11 by baffle plate 4.
In the present embodiment, baffle plate 4 and the axial angle of gasification furnace 1 be interval with 45 ° of baffle plates 4 multiple to pyrolysis chamber 15 spray orifice 41.
Shock chamber 13, goes out gasification furnace for carrying out cooling heel row to the slag charge produced by reaction, and down-comer 12 is connected with sharp Device for cooling (not shown), for cooling protection down-comer, while provide cooling water to shock chamber；On the side wall of shock chamber also Quench aquaporin 18 is provided with, for moisturizing in Quench room, keeping liquid level in Quench room.
Chilling device in the present embodiment can as needed from of the prior art any one.
Gasification nozzle 2, for the indoor spray feed reaction mass of gasification, selecting as needed of the prior art any one Kind.Gasification nozzle 2 in the present embodiment includes the first noumenon, is sequentially provided with fuel channel 22, oxygen on the first noumenon from inside to outside Gas passage 23, steam channel 24 and the first cooling duct 25；Interlayer 26 between fuel channel 22 and the oxygen channel 23 is adopted Prepared with high-abrasive material.
Fine coal nozzle 3, has eight, is distributed in the circumferential side wall of gasification furnace, and which is exported to pyrolysis chamber 15, for heat Injection coal dust in solution room 15；Including the second body 31, the second body 31 is provided with fine coal passage 32, and fine coal passage 32 is externally provided with Two cooling ducts 33.Second body 31 is prepared using high-abrasive material.
In the present embodiment, the axial direction of fine coal nozzle 3 is 60 ° with the radial direction angle of gasification furnace 1, the bottom conical surface with vaporizer Parallel.
Particle diameter from coal-grinding apparatus 8 is 80～100 less than or equal to 90 microns, water content less than or equal to 2wt% // temperature DEG C coal dust the gasification nozzle 2 and fine coal nozzle 3 of gasification furnace 1 are delivered to 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 are 4.0MPag.
The steam produced by drum 10 and the oxygen come from battery limit (BL) enter vaporizer 11 via gasification nozzle 2 together with coal dust Reaction, generates with CO+H2For the high temperature hydrogen-rich synthetic gas that mainly constitute and cinder；The ratio for controlling steam, oxygen and coal dust is 0.50Nm3Oxygen/kg coals, quantity of steam can use 0.3Nm3/Nm3Oxygen；Vaporizer interior reaction temperature is controlled for 600～1500 DEG C, pressure Power is 1.0～6.0MPag；
Cinder and synthesis gas enter down-comer 12；Cinder enters shock chamber 13 in self gravitation effect, lower edge down-comer 12 Interior, discharge after cooling；The temperature of controlled chilling room is below 300 DEG C.
Synthesis gas is up, 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 reaction temperature in the pyrolysis chamber 15 be 800～900 DEG C, pressure be 3.5 ± 0.2MPag；
The oil gas and coal tar are discharged from discharging opening 17, are sequentially entered in two stage cyclone separator 5 and are isolated coal tar and oil Gas；
Coal tar after separating is discharged from the outlet at bottom of the cyclone separator 5；The oil gas that isolates is then from cyclonic separation The top exit of device 5 is discharged, and enters gas and oil separating plant 6, isolate oil product and with CO, H after exchanging heat with boiler water2And CH4Based on Want the fuel gas of composition；
Fuel gas enters gas cleaning plant 7, isolates synthesis gas and fuel gas, and fuel gas sends to coal-grinding unit 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 Thing enters drum, separate vapour and water, and steam sends to the gasification nozzle 2.
In the present invention, efficiency is up to 70～80%, the efficiency of Technology of direct coal liquefaction only about 50% in prior art；Coal Consume for 3.3～3.5 tons, less than existing Technology of direct coal liquefaction；Liquid-phase product yield is first intake with existing up to 25～33% Flat fair；CO20.05～0.5 ton/ton oil product of discharge capacity, substantially subtracts than 5～6 ton/ton oil product of existing Technology of direct coal liquefaction Few, megaton does not invest 50～60% for existing Technology of direct coal liquefaction.
Comprehensive technical indexes, environmental protection index and investing, the present invention are respectively provided with obvious advantage compared to existing technology.

Claims (9)

1. coal direct hydrogenation method for pyrolysis, it is characterised in that comprise the steps：
Coal dust from coal-grinding apparatus (8) delivers to the gasification nozzle (2) and fine coal of gasification furnace (1) by pulverized coal conveying device (9) Nozzle (3), wherein, fine coal conveying mixed phase flow velocity is 4～15m/s；Hybrid density is 200～550kg/m3；
The steam produced by drum (10) and the oxygen come from battery limit (BL) enter vaporizer via gasification nozzle (2) together with coal dust (11) react, produce high temperature hydrogen-rich synthetic gas and cinder；The ratio for controlling steam, oxygen and coal dust is 0.2～0.8Nm3Oxygen/ Kg coals, 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) in self gravitation effect, lower edge down-comer (12) Interior, discharge after cooling；
Synthesis gas is up, enters in pyrolysis chamber (15) via each spray orifice (41), reacts with the coal dust from fine coal burner (3), raw Olefiant gas and coal tar；Control reaction temperature in the pyrolysis chamber (15) be 600～1200 DEG C, pressure be 1.0～6.0MPag；
The oil gas and coal tar are discharged from discharging opening (17), are entered in cyclone separator (5) and are isolated coal tar and oil gas；
Coal tar after separating is discharged from the outlet at bottom of the cyclone separator (5)；The oil gas that isolates is then from cyclone separator (5) top exit is discharged, and enters gas and oil separating plant (6), isolate oil product and with CO, H after exchanging heat with boiler water2And 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 unit (8)；
Boiler water after heat exchange enters the cold wall of gasification furnace (1), generates steam water interface, steam water interface after absorbing heat Drum, separate vapour and water is entered, the steam sends to the gasification nozzle (2).
2. coal direct hydrogenation method for pyrolysis according to claim 1, it is characterised in that the particle diameter 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 and 2, it is characterised in that 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 Separate.
5. the coal direct hydrogenation method for pyrolysis according to Claims 1-4 any claim, it is characterised in that the gasification Gasification nozzle (2) is provided with the top of stove (1), and the inner chamber of the gasification furnace is sequentially provided with vaporizer (11), pyrolysis chamber from top to bottom (15) and shock chamber (13), the upper port of down-comer (12) connects the outlet at bottom of vaporizer (11), the down-comer (12) lower port is inserted in the shock chamber (13) through the pyrolysis chamber (15)；The bottom of gasification furnace (1) is provided with Slag exports (14)；
The top entry of down-comer (12) is tightly connected the lateral wall of the vaporizer (11) by baffle plate (4)；The gear It is interval with plate (4) multiple to the pyrolysis chamber (15) spray orifice (41)；
The side wall of gasification furnace (1) is provided with least one pair of fine coal nozzle (3) to the pyrolysis chamber (15)；The gasification The material outlet (17) for connecting pyrolysis chamber (15) is additionally provided with the side wall of stove (1).
6. coal direct hydrogenation method for pyrolysis according to claim 5, it is characterised in that baffle plate (4) and the gasification furnace (1) axial angle is 15～60 °.
7. coal direct hydrogenation method for pyrolysis according to claim 6, it is characterised in that the axial direction of fine coal nozzle (3) with The radial direction angle of gasification furnace (1) is 0～60 °.
8. coal direct hydrogenation method for pyrolysis according to claim 7, it is characterised in that the bottom surface phase of pyrolysis chamber (15) For the sidewall slope of the gasification furnace (1) is arranged, material outlet (17) are arranged on the lowest order of the pyrolysis chamber (15) Put.
9. coal direct hydrogenation method for pyrolysis according to claim 8, it is characterised in that fine coal nozzle (3) have multiple, Perisporium along the gasification furnace is evenly arranged.
CN201610858298.9A 2016-09-28 2016-09-28 Coal direct hydrogenation method for pyrolysis Active CN106497606B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610858298.9A CN106497606B (en) 2016-09-28 2016-09-28 Coal direct hydrogenation method for pyrolysis

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610858298.9A CN106497606B (en) 2016-09-28 2016-09-28 Coal direct hydrogenation method for pyrolysis

Publications (2)

Publication Number Publication Date
CN106497606A true CN106497606A (en) 2017-03-15
CN106497606B CN106497606B (en) 2019-05-17

Family

ID=58290895

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610858298.9A Active CN106497606B (en) 2016-09-28 2016-09-28 Coal direct hydrogenation method for pyrolysis

Country Status (1)

Country Link
CN (1) CN106497606B (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109595541A (en) * 2017-12-14 2019-04-09 湘潭锅炉有限责任公司 A kind of lignite circulating fluidized bed boiler
CN110184083A (en) * 2019-05-29 2019-08-30 中国成达工程有限公司 A kind of coal oil residue treatment technique and processing unit

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105713674A (en) * 2016-04-25 2016-06-29 中美新能源技术研发（山西）有限公司 Reactor for preparing oil and natural gas through pulverized coal pyrolysis

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105713674A (en) * 2016-04-25 2016-06-29 中美新能源技术研发（山西）有限公司 Reactor for preparing oil and natural gas through pulverized coal pyrolysis

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
国家机械工业委员会统编: "《发生炉煤气生产原理》", 31 October 1988, 机械工业出版社 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109595541A (en) * 2017-12-14 2019-04-09 湘潭锅炉有限责任公司 A kind of lignite circulating fluidized bed boiler
CN110184083A (en) * 2019-05-29 2019-08-30 中国成达工程有限公司 A kind of coal oil residue treatment technique and processing unit

Also Published As

Publication number Publication date
CN106497606B (en) 2019-05-17

Similar Documents

Publication Publication Date Title
US10787620B2 (en) Method of biomass grading pyrolysis gasification in a circulating fluidized bed
MXPA05008871A (en) Apparatus and method for coal gasification.
CN104877700B (en) A kind of pulverized coal pyrolysis hydrogenation reactor and hydrogenation reaction method
EP3894516A1 (en) Plastic-to-oil plant, according cracking reactor, and related methods for converting plastic waste into petrochemical products
CN106281398B (en) A kind of coal heat decomposition stove and pyrolysis of coal method
CN110923015B (en) Pyrolysis-gasification integrated treatment device and method
US2311140A (en) Manufacture of producer gas
CN104531222B (en) Pyrolysis of coal system and method using spouted bed reactor
CN106497606B (en) Coal direct hydrogenation method for pyrolysis
CN106479547A (en) The system and method that a kind of coal is classified dual treatment
US11230674B2 (en) Integrated method and apparatus for catalytic cracking of heavy oil and production of syngas
CN206266493U (en) The system that a kind of coal is classified dual treatment
CN110283609B (en) Pyrolysis-coking combined process and system for preparing coal tar by pyrolyzing pulverized coal
CN106833753A (en) A kind of up flow type pyrolysis and downstriker gasification coupling prepare the device and method of coal tar oil and gas
CN106147811A (en) A kind of pyrolysis oven and gas-based shaft kiln combined system and the method for process coal
CN206428193U (en) A kind of system of coal hydrogenation pyrolysis
US11230671B2 (en) Coupling reaction apparatus for heavy oil pyrolysis-gasification
US11230677B2 (en) Method and device for heavy oil lightening and synthesis gas production
CN112680249B (en) Organic solid waste pressure gasification system and method
CN106497594A (en) A kind of system and method for coal hydrogenation pyrolysis
CN210826069U (en) Upper and lower double-heat high-resolution suspension bed reaction device
CN210736666U (en) Coal oil slurry cracking gasification reaction device
CN106281399B (en) A kind of pyrolysis of coal liquefaction device and method
CN106433734A (en) Coal grading utilization method
CN208266125U (en) A kind of coal fast pyrogenation and the integral system of gasification

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant