CN105419879A - Device and method for catalytically decomposing coal substances and separating coal substances at high temperatures - Google Patents
Device and method for catalytically decomposing coal substances and separating coal substances at high temperatures Download PDFInfo
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- CN105419879A CN105419879A CN201510751755.XA CN201510751755A CN105419879A CN 105419879 A CN105419879 A CN 105419879A CN 201510751755 A CN201510751755 A CN 201510751755A CN 105419879 A CN105419879 A CN 105419879A
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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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
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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
- 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
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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
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/86—Other features combined with waste-heat boilers
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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
- C10J2300/0936—Coal fines for producing producer 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
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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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
- C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis gas
Abstract
The invention discloses a device and a method for catalytically decomposing coal substances and separating the coal substances at high temperatures. The method includes mixing dried and ground pulverized coal and powder catalysts, and then conveying the pulverized coal and the powder catalysts into a sectional converter in a pressurized manner by the aid of gas; feeding the coal and catalyst powder into an upper section of the sectional converter and feeding coke powder, oxygen and steam into a lower section of the sectional converter; enabling the coal, the catalyst powder, the coke powder, the oxygen and the steam to respectively carry out conversion reaction in the sectional converter to ultimately generate semi-coke, coal gas and oil products; discharging three-phase high-temperature products from the upper portion of the sectional converter and sequentially removing the coke powder and tar in the three-phase high-temperature products by means of cyclone separation, fine filtration and solvent oil chilling step by step; returning the separated coke powder into the sectional converter to be used as a gasification reaction material; absorbing solvent oil in the oil products in the coal gas, separating the solvent oil by the aid of an oil separation tower and then recycling the solvent oil. The dried and ground pulverized coal is a raw material. The device and the method have the advantages that solid and liquid two-phase products in the crude coal gas are subjected to catalytic decomposition reaction and high-temperature separation, technologies are advanced, the yield of the products is high, and the device and the method conform to concepts of the modern coal chemical industry and accordingly have extremely broad application prospects.
Description
Technical field
The present invention relates to the separating at high temperature field of the thermolysis of coal material and gas-solid-liquid three-phase medium, specifically the device and method of a kind of coal substance catalyses decomposition and separating at high temperature.
Background technology
Coal is the main energy sources of China, accounts for about 70% of primary energy source total quantity consumed for a long time, and within the period quite grown future, will occupy an leading position in the energy structure of China.It is predicted, coal resources in China reserves are more than 5,000,000,000,000 tons, and proven reserve reach 1,145 hundred million tons.Wherein low-rank coal reserves account for the whole nation and have verified more than 55% of coal reserves, and reach 5,662 hundred million tons, wherein brown coal account for 12.7%, lower-grade metamorphic bituminously account for 42.5%.Low-rank coal is mainly distributed in NORTHWEST CHINA, North, Northeast China area, comprises the major areas such as Ordos, inner Mongolia, Yulin and Xinjiang.
In recent years, China coal industry achieves significant progress, and coal production increases fast, but the problem such as single extensive of coal utilization mode does not obtain basic change, and coal utilization efficiency is still on the low side.The low-rank coal being particularly rich in volatile matter in a large number utilizes just directly burning or gasification without sub-prime, causes the hydrocarbon resources of wherein a large amount of high added value to waste, also creates a series of ecosystem environment pollution problem simultaneously.Data presentation according to statistics, 2012, it was 56% that coal in China uses the contribution estimated value of the average annual concentration of environment PM2.5.Wherein the PM2.5 of about 60% directly to be burnt generation by coal, and the PM2.5 of about 40% is the key industry discharge that uses with coal.PM2.5, SO2 and NOX quantity discharged produced because of consumption of coal accounts for 62%, 93% and 70% of Chinese gross contamination emission respectively.Along with consumption of coal increases, China CO2 isothermal chamber gas purging amount also significantly increases.
National energy science and technology " 12 " planning lists low-rank coal upgrading modification technology in important technical research field, require active development have independent intellectual property right, the low-rank coal upgrading modification technology of wide adaptability and technique.In May, 2015, the notice that National Energy Board prints and distributes " Coal Clean efficiency utilization action plan (2015-2020) ", explicitly call for and " move forward steadily the demonstration of the processing of coal high quality, sub-prime classification cascade utilization, Coal Solid Wastes recycling etc. in China, build a collection of Coal Clean efficiency utilization demonstration projects." and propose the action plan timetable of Coal Clean efficiency utilization: 2017, low-rank coal classification upgrading gordian technique made a breakthrough; The year two thousand twenty, builds up a collection of megaton classification upgrading pilot project.
Therefore, the sub-prime staged conversion clean and effective actively developing coal utilizes, under coal will be the realistic background of China's main body energy for a long time, because of coal utilization extensive cause the severe situation of the waste of hydrocarbon resources in Heavy environmental pollution and low-rank coal under, ensure the energy safety of supply and promote Energy restructuring in the urgent need to and realistic choice.
At present, defined a variety of coal material low temperature thermal decomposition producing and manufacturing technique both at home and abroad, roughly can be divided into following several types:
(1) fixed bed coal thermal decomposition process: comprise the technology such as internal thermal upright stove, external-heat upright furnace, interior-outer formula upright furnace; Its advantage is technology maturation, and flow process is simple, and gas phase dust is few, tar quality better, and shortcoming is that feed coal needs certain particle size, and tar yield is low, and single covering device scale is less, and environmental pollution is larger.
(2) rotary kiln coal thermal decomposition process: comprise U.S. Toscol, U.S. Encoal, Canadian ATP, Mei Ke institute MRF etc., its advantage is less to the granularity requirements of coal, directly can use broken coal, shortcoming there are large-scale rotatable parts, equipment is huge, and breakage is comparatively serious, system complex, atmospheric operation, after-treatment system difficulty is large;
(3) moving-bed coal thermal decomposition process: comprise the technology such as U.S. LFC, German Lurgi-Ruhr, USSR (Union of Soviet Socialist Republics) ETCH-175, Dalian University of Technology DG, Shanxi coalification institute of the Chinese Academy of Sciences; Its advantage is that pyrolysis reactor structure is simple, stable, and shortcoming is that thermal barrier and coal mixing are uneven, and in tar, heavy component is high, and dust is difficult to eliminate, and semicoke Product Activity is poor;
(4) fluidized bed coal thermal decomposition process: comprise the technology such as U.S. COED, Australian CSIR O, Zhejiang University, Engineering Thermophysics institute of the Chinese Academy of Sciences, process engineering institute of the Chinese Academy of Sciences; Its advantage is multiple stage fluidized-bed, and tar yield is high, quality better, and shortcoming needs a large amount of pyrolysis gas to return as fluidizing medium, and many containing coke breeze in tar, in single hop fluidized-bed tar, heavy component is high.
The coal material thermal decomposition process of above several types mostly is normal pressure, or low voltage operated, and equipment takes up an area large, and environmental benefit is poor.And comparatively large to the dependency of feed coal, in general requirement feed coal, there is higher volatile matter, otherwise be difficult to the economic benefit embodying thermal decomposition process.In actual moving process, produce a large amount of semicokes, how effectively to utilize, never effectively solved.
Summary of the invention
The object of this invention is to provide the device and method of the decomposition of a kind of coal substance catalyses and separating at high temperature, to solve the thermolysis of existing coal material and isolation technique Problems existing.
In order to achieve the above object, the technical solution adopted in the present invention is:
The device of a kind of coal substance catalyses decomposition and separating at high temperature, it is characterized in that: comprise coal dust preparation system, segmentation converter, cyclonic separator, accurate fly-ash separator, waste heat boiler, raw gas quenching column, separating of oil tower, coke powder tank, recycle gas compressor, dregs breaker, grey slag ladle, drum, process furnace, three groups of interchanger, surge tank, three groups of pumps, gas-liquid separators, wherein:
Described segmentation converter has upper and lower two-stage reaction cavity, be integrated by trunnion series connection between upper and lower two-stage reaction cavity in segmentation converter, the segmentation converter furnace wall that epimere reaction cavity is corresponding arranges multiple raw coal inlet, the segmentation converter furnace wall that hypomere reaction cavity is corresponding arranges multiple semicoke burner, segmentation converter top is provided with gas exit, is provided with slag-drip opening bottom segmentation converter;
Described raw gas quenching column, separating of oil tower are the unidirectional valve tray column structure of ejection-type, raw gas quenching column, separating of oil top of tower are respectively equipped with gaseous phase outlet, raw gas quenching column, separating of oil tower bottom are respectively equipped with liquid-phase outlet, are vertically provided with multilayer column plate respectively in raw gas quenching column, separating of oil tower;
The delivery port of described coal dust preparation system is communicated with multiple raw coal inlets of segmentation converter respectively, the gas exit of segmentation converter is communicated with the inlet mouth of cyclonic separator, segmentation converter bottom slag discharge is communicated with dregs breaker opening for feed, and dregs breaker discharge port is communicated with grey slag ladle inner top;
The slag-drip opening of described cyclonic separator is communicated with coke powder tank top, the air outlet of cyclonic separator is communicated with the inlet mouth of accurate fly-ash separator, the slag-drip opening of accurate fly-ash separator is also communicated with coke powder tank top, and the air outlet of accurate fly-ash separator is communicated with the inlet mouth of waste heat boiler; Described drum inlet mouth is communicated to waste heat boiler top, and drum air outlet is communicated with steam output pipe, and the air outlet of waste heat boiler is communicated with interior below orlop column plate in raw gas quenching column;
Described raw gas quenching column top gas phase outlet is communicated with recycle gas compressor inlet mouth, recycle gas compressor air outlet is communicated with coke powder pot bottom side, coke powder pot bottom opposite side is communicated with multiple semicoke burners of segmentation converter respectively, the outlet of raw gas quenching column top gas phase is also communicated with the inlet mouth of first group of interchanger, first group of interchanger air outlet is communicated with gas-liquid separator inlet mouth, the gaseous phase outlet of gas-liquid separator is connected with raw gas output tube, the liquid phase of gas-liquid separator exports and is connected with condensate drain, the outlet of raw gas quenching column bottom liquid phases is communicated with process furnace inlet mouth by first group of pump, process furnace air outlet is communicated with column plate position in separating of oil tower,
Described separating of oil top of tower gaseous phase outlet is communicated with the inlet mouth of second group of interchanger, the air outlet of second group of interchanger is communicated with surge tank top, surge tank bottom is communicated to raw gas quenching column, separating of oil tower inner top respectively by second group of pump, separating of oil tower bottom liquid-phase outlet is communicated with the inlet mouth of the 3rd group of interchanger by the 3rd group of pump, and the air outlet of the 3rd group of interchanger is connected with tar output tube.
Described a kind of coal substance catalyses decomposition and the device of separating at high temperature, it is characterized in that: described coal dust preparation system comprises shredder assembly, drying installation, milling apparatus, catalyst preparing device, fine coal gas phase add pressure output device, fine coal storehouse, coal material is successively through shredder assembly is broken, drying installation is dry, milling apparatus forms fine coal after grinding, fine coal enters the powdered catalyst prepared with catalyst preparing device in fine coal storehouse and is mixed to form mixture, and the mixture exported from fine coal storehouse is sent into segmentation converter epimere reaction cavity by raw coal inlet.
Described a kind of coal substance catalyses decomposition and the device of separating at high temperature, it is characterized in that: in described segmentation converter, the furnace wall of epimere reaction cavity adopts refractory liner, the furnace wall of hypomere reaction cavity adopts water wall, using epimere reaction cavity as fine coal thermolysis section, using hypomere reaction cavity as char Gasification conversion zone, be also connected with back cover bottom segmentation converter, back cover is made up of refractory liner.
Described a kind of coal substance catalyses decomposition and the device of separating at high temperature, is characterized in that: be also provided with the outer annular space around center cavity in described semicoke burner.
Described a kind of coal substance catalyses decomposition and the device of separating at high temperature, is characterized in that: described cyclonic separator is made up of the alloy material of Wear-resistant, high-temperature resistant and the mould material of thermal insulation, forms mazy vapor phase stream path in cyclonic separator.
Described a kind of coal substance catalyses decomposition and the device of separating at high temperature, is characterized in that: described accurate fly-ash separator inwall is made up of mould material, and accurate fly-ash separator outer wall is made up of carbon steel material, is provided with the filter core that metallic substance is made in accurate fly-ash separator.
Described a kind of coal substance catalyses decomposition and the device of separating at high temperature, it is characterized in that: in described raw gas quenching column, separating of oil tower, liquid mass transfer carries out above column plate liquid layer, rely on gas flow at high rates that column plate upper liquid is injected into a large amount of comminuted drops, gas-liquid two-phase is disperse phase respectively with liquid, gas completes gas-liquid mass transfer for external phase state.
A kind of coal substance catalyses decomposes and separating at high temperature method, it is characterized in that: first the fine coal of coal dust preparation system output and the mixture of powdered iron series catalysts are sent in segmentation converter epimere reaction cavity by raw coal inlet;
Segmentation converter is divided into two sections reaction cavity, be integrated by trunnion series connection between two sections, epimere reaction cavity is fine coal thermolysis section: first the mixture of fine coal and catalyzer enters segmentation converter fine coal thermolysis section, the high temperature rough gas produced by hypomere char Gasification conversion zone char Gasification herein heats, high temperature rough gas temperature is 1300 ~ 1450 DEG C, fine coal transforms rapidly and resolves into semicoke under the effect of catalyzer, coal gas and oil product, gas phase temperature drops to 600 ~ 700 DEG C fast, and simultaneously along with the pushing effect of hypomere char Gasification conversion zone air-flow, three-phase product is rapidly to flowing, and leave segmentation converter, enter in cyclonic separator and accurate fly-ash separator successively, the coke breeze of the different-grain diameter in substep removing high temperature gas phase,
The hypomere reaction cavity of segmentation converter is char Gasification conversion zone: the coke powder be separated through the dedusting of raw gas quenching column turns back to semicoke burner center by gas two-phase transportation, with be preheating in the outer annular space of semicoke burner 180 DEG C oxygen and in press through hot steam and mix the hypomere reaction cavity being injected to segmentation converter, generating portion oxidizing reaction herein, generate high temperature rough gas, temperature gasification and high raw gas is advanced into the thermolysis section of segmentation converter, for the heat required for pulverized coal pyrolysis; The high-temperature slag that gasification section char Gasification produces, the refractory liner shock chamber flowing downstream into segmentation converter bottom carries out Quench, and slag is after the broken bulk slag of dregs breaker, and periodic exhaustion is to ash discharge slag ladle, drain into outside slag bath by grey slag ladle again, with dragveyer, the slag of discharging is exported;
The high temperature rough gas discharging on 600 DEG C, segmentation converter top, first enters in cyclonic separator, and oarse-grained solid semicoke enters coke powder tank after separating from gas; Gas phase enters in accurate fly-ash separator again, and isolate wherein fine powder further by metal filtering core burnt, fine powder Jiao is regularly sent in coke powder tank by pressurization; After going out in the raw gas of accurate fly-ash separator the coke powder removing about 99%, enter in waste heat boiler, middle pressure steam is produced by drum recovery waste heat, the raw gas going out waste heat boiler enters raw gas quenching column, cooled by low-temperature solvent oil wash in raw gas quenching column, raw gas is cooled to rapidly 100 DEG C, and the gas phase oil product simultaneously in coal gas is dissolved into rapidly in cold cycle solvent oil phase;
The raw gas that raw gas quenching column exports is divided into two strands: one gaseous stream send recycle gas compressor entrance, as the two-phase transportation gas of coke breeze, fine coal after pressurization; After another strand of gaseous stream send first group of interchanger to be cooled to normal temperature, feeding gas-liquid separator separates goes out the phlegma in gas phase, then is delivered to extraneous process further; From raw gas quenching column mixing oil product out, 350 DEG C are heated to by sending into process furnace after first group of pump pressurization, enter on the column plate on separating of oil tower top again, in separating of oil tower, carry out mass-and heat-transfer separation, the gas phase discharging of separating of oil column overhead is cooled to solvent oil through second group of interchanger, by second group of interchanger cooling, second group of pump pressurization, a part is back to separating of oil column overhead, another part sends into raw gas quenching column, continues Quench raw gas, and absorbs oil product wherein; Heavy tar out at the bottom of separating of oil tower tower, exports tar products and stores to outside tank field after the 3rd group of pump pressurization, the 3rd group of interchanger cooling.
The present invention is configured by Optimization Technology, adopts and carries out catalytic decomposition and gas phase separating at high temperature method to coal material, both improve the productive rate of product, and effectively reduced production cost, and realized again the cascade utilization of energy, increase substantially economic benefit.
Decompose and gasifying process relative to traditional coal, the present invention has following advantage:
1) by arranging the hot segmentation conversion process of coal substance catalyses, effectively can improve the productive rate of oil product and coal gas, reducing the property depended on unduly to raw material coal;
2) by arranging raw gas two-stage high-temperature dust removal and gas phase Quench and separating of oil technique, effectively can reduce the dust content in oil product, significantly reclaiming the oil product in raw gas simultaneously;
3) by adopting the production technique of ejection-type unidirectional float valve quenching column and separating of oil tower, throughput and the efficiency of device can be increased substantially.
Accompanying drawing explanation
Fig. 1 is structure principle chart of the present invention.
Fig. 2 is segmentation converter structural representation.
Embodiment
As shown in Figure 1 and Figure 2, the device of a kind of coal substance catalyses decomposition and separating at high temperature, comprise coal dust preparation system 1, segmentation converter 2, cyclonic separator 3, accurate fly-ash separator 4, waste heat boiler 5, raw gas quenching column 6, separating of oil tower 7, coke powder tank 8, recycle gas compressor 9, dregs breaker 10, grey slag ladle 11, drum 12, process furnace 13, three groups of interchanger 14-1,14-2,14-3, surge tank 15, three groups of pump 16-1,16-2,16-3, gas-liquid separator 17, wherein:
Segmentation converter 2 has upper and lower two-stage reaction cavity 2-1, in segmentation converter 2, upper and lower series connection by trunnion 2-3 between two-stage reaction cavity 2-1,2-2 is integrated, segmentation converter 2 furnace wall that epimere reaction cavity 2-1 is corresponding arranges multiple raw coal inlet 2-4, segmentation converter 2 furnace wall that hypomere reaction cavity 2-2 is corresponding arranges multiple semicoke burner 2-5, segmentation converter 2 top is provided with gas exit 2-6, is provided with slag-drip opening 2-7 bottom segmentation converter 2;
Raw gas quenching column 6, separating of oil tower 7 are the unidirectional valve tray column structure of ejection-type, raw gas quenching column 6, separating of oil tower 7 top are respectively equipped with gaseous phase outlet, be respectively equipped with liquid-phase outlet bottom raw gas quenching column 6, separating of oil tower 7, in raw gas quenching column 6, separating of oil tower 7, be vertically provided with multilayer column plate respectively;
The delivery port of coal dust preparation system 1 is communicated with multiple raw coal inlet 2-4 of segmentation converter 2 respectively, the gas exit 2-6 of segmentation converter 2 is communicated with the inlet mouth of cyclonic separator 3, segmentation converter 2 bottom slag discharge 2-7 is communicated with dregs breaker 10 opening for feed, and dregs breaker 10 discharge port is communicated with grey slag ladle 11 inner top;
The slag-drip opening of cyclonic separator 3 is communicated with coke powder tank 8 top, the air outlet of cyclonic separator 3 is communicated with the inlet mouth of accurate fly-ash separator 4, the slag-drip opening of accurate fly-ash separator 4 is also communicated with coke powder tank 8 top, and the air outlet of accurate fly-ash separator 4 is communicated with the inlet mouth of waste heat boiler 5; Drum 12 inlet mouth is communicated to waste heat boiler 5 top, and drum 12 air outlet is communicated with steam output pipe 18, and the air outlet of waste heat boiler 5 is communicated with interior below orlop column plate in raw gas quenching column 6;
The outlet of raw gas quenching column 6 top gas phase is communicated with recycle gas compressor 9 inlet mouth, recycle gas compressor 9 air outlet is communicated with side bottom coke powder tank 8, bottom coke powder tank 8, opposite side is communicated with multiple semicoke burner 2-5 of segmentation converter 2 respectively, the outlet of raw gas quenching column 6 top gas phase is also communicated with the inlet mouth of first group of interchanger 14-1, first group of interchanger 14-1 air outlet is communicated with gas-liquid separator 17 inlet mouth, the gaseous phase outlet of gas-liquid separator 17 is connected with raw gas output tube 19, the liquid phase of gas-liquid separator 17 exports and is connected with condensate drain 20, the outlet of raw gas quenching column 6 bottom liquid phases is communicated with process furnace 13 inlet mouth by first group of pump 16-1, process furnace 13 air outlet is communicated with column plate position in separating of oil tower 7,
Separating of oil tower 7 top gas phase outlet is communicated with the inlet mouth of second group of interchanger 14-2, the air outlet of second group of interchanger 14-2 is communicated with surge tank 15 top, surge tank 15 bottom is communicated to raw gas quenching column 6, separating of oil tower 7 inner top respectively by second group of pump 16-2, separating of oil tower 7 bottom liquid phases outlet is communicated with the inlet mouth of the 3rd group of interchanger 14-3 by the 3rd group of pump 16-3, and the air outlet of the 3rd group of interchanger 14-3 is connected with tar output tube 21.
Coal dust preparation system 1 comprises shredder assembly, drying installation, milling apparatus, catalyst preparing device, fine coal gas phase add pressure output device, fine coal storehouse, coal material is successively through shredder assembly is broken, drying installation is dry, milling apparatus forms fine coal after grinding, fine coal enters the powdered catalyst prepared with catalyst preparing device in fine coal storehouse and is mixed to form mixture, and the mixture exported from fine coal storehouse is sent into segmentation converter 2 epimere reaction cavity 2-1 by raw coal inlet.
In segmentation converter 2, the furnace wall of epimere reaction cavity 2-1 adopts refractory liner 2-8, the furnace wall of hypomere reaction cavity 2-2 adopts water wall 2-9, using epimere reaction cavity 2-1 as fine coal thermolysis section, using hypomere reaction cavity 2-2 as char Gasification conversion zone, also be connected with back cover bottom segmentation converter 2, back cover is made up of refractory liner 2-10.
The outer annular space around center cavity is also provided with in semicoke burner 2-5.
Cyclonic separator 3 is made up of the alloy material of Wear-resistant, high-temperature resistant and the mould material of thermal insulation, forms mazy vapor phase stream path in cyclonic separator 3.
Accurate fly-ash separator 4 inwall is made up of mould material, and accurate fly-ash separator 4 outer wall is made up of carbon steel material, is provided with the filter core that metallic substance is made in accurate fly-ash separator 4.
In raw gas quenching column 6, separating of oil tower 7, liquid mass transfer carries out above column plate liquid layer, rely on gas flow at high rates that column plate upper liquid is injected into a large amount of comminuted drops, gas-liquid two-phase is disperse phase respectively with liquid, gas completes gas-liquid mass transfer for external phase state.
A kind of coal substance catalyses decomposes and separating at high temperature method, and first the fine coal of coal dust preparation system 1 output and the mixture of powdered iron series catalysts are sent in segmentation converter 2 epimere reaction cavity 2-1 by raw coal inlet;
Segmentation converter 2 is divided into two sections reaction cavity 2-1, 2-2, be integrated by trunnion 2-3 series connection between two sections, epimere reaction cavity 2-1 is fine coal thermolysis section: first the mixture of fine coal and catalyzer enters segmentation converter 2 fine coal thermolysis section, the high temperature rough gas produced by hypomere char Gasification conversion zone char Gasification herein heats, high temperature rough gas temperature is 1300 ~ 1450 DEG C, fine coal transforms rapidly and resolves into semicoke under the effect of catalyzer, coal gas and oil product, gas phase temperature drops to 600 ~ 700 DEG C fast, and simultaneously along with the pushing effect of hypomere char Gasification conversion zone air-flow, three-phase product is rapidly to flowing, and leave segmentation converter 2, enter in cyclonic separator 3 and accurate fly-ash separator 4 successively, the coke breeze of the different-grain diameter in substep removing high temperature gas phase,
The hypomere reaction cavity 2-2 of segmentation converter 2 is char Gasification conversion zone: the coke powder be separated through raw gas quenching column 6 dedusting turns back to semicoke burner 2-5 center by gas two-phase transportation, with be preheating in the outer annular space of semicoke burner 2-5 180 DEG C oxygen and in press through hot steam and mix the hypomere reaction chamber 2-2 body being injected to segmentation converter 2, generating portion oxidizing reaction herein, generate high temperature rough gas, temperature gasification and high raw gas is advanced into the thermolysis section of segmentation converter 2, for the heat required for pulverized coal pyrolysis; The high-temperature slag that gasification section char Gasification produces, what flow downstream into segmentation converter bottom carries out Quench through refractory liner shock chamber, slag is after the broken bulk slag of dregs breaker 10, periodic exhaustion is to ash discharge slag ladle 11, drain into outside slag bath 22 by grey slag ladle 11 again, export with the slag 22 of dragveyer by discharge;
The high temperature rough gas discharging on 600 DEG C, segmentation converter 2 top, first enters in cyclonic separator 3, and oarse-grained solid semicoke enters coke powder tank 8 after separating from gas; Gas phase enters in accurate fly-ash separator 4 again, and isolate wherein fine powder further by metal filtering core burnt, fine powder Jiao is regularly sent in coke powder tank 8 by pressurization; After going out in the raw gas of accurate fly-ash separator 4 coke powder removing about 99%, enter in waste heat boiler 5, middle pressure steam is produced by drum 12 recovery waste heat, the raw gas going out waste heat boiler 5 enters raw gas quenching column 6, cooled by low-temperature solvent oil wash in raw gas quenching column 6, raw gas is cooled to rapidly 100 DEG C, and the gas phase oil product simultaneously in coal gas is dissolved into rapidly in cold cycle solvent oil phase;
The raw gas that raw gas quenching column 6 exports is divided into two strands: one gaseous stream send recycle gas compressor 9 entrance, as the two-phase transportation gas of coke breeze, fine coal after pressurization; After another strand of gaseous stream send first group of interchanger 14-1 to be cooled to normal temperature, the phlegma in gas phase isolated by feeding gas-liquid separator 17, then is delivered to extraneous process further; From raw gas quenching column 6 mixing oil product out, send into process furnace 13 after being pressurizeed by first group of pump 16-1 and be heated to 350 DEG C, enter on the column plate on separating of oil tower 7 top again, mass-and heat-transfer separation is carried out in separating of oil tower 7, the gas phase discharging of separating of oil tower 7 tower top is cooled to solvent oil through second group of interchanger 14-2, pressurizeed by second group of interchanger 14-2 cooling, second group of pump 16-2, a part is back to separating of oil tower 7 tower top, another part sends into raw gas quenching column 6, continue Quench raw gas, and absorb oil product wherein; Heavy tar out at the bottom of separating of oil tower 7 tower, pressurizes through the 3rd group of pump 16-3, the 3rd group of interchanger 14-3 exports tar products after cooling and store to outside tank field.
Concrete implementation example:
The long-flame coal that this example adopts colliery, accurate thing Black Hills, Xinjiang to produce is raw material, implement scale: 1000kg/h.Coal analysis data are as shown in table 1:
Colliery, accurate thing Black Hills, table 1 Xinjiang ature of coal analytical data
By after feed coal fragmentation by Belt Conveying to coal dust preparation system, coal-grinding equipment adopt roller ring mill; Particle diameter feed coal being ground to more than 90% is 90 μm, feed coal is dried to about 5% in process of lapping simultaneously; Fine coal after drying is levigate is together sent in fine coal storehouse after fully mixing with powdered iron series catalysts FH, and catalyzer carries out proportioning according to 0.5% of feed coal; Coal dust out and catalyst mixture from fine coal storehouse, by carrying out cartalytic decomposition effect in high pressure (4.5MPaG) two-phase transportation to segmentation converter, gaseous conveying medium is the self-produced coal gas of device, and the situation that goes into operation adopts nitrogen conveying.
Segmentation converter is divided into two sections reaction cavity, be integrated by trunnion series connection between two sections, epimere joins 4 ~ 8 raw coal inlets: first fine coal and powder catalyzer two kinds of mixtures of materials enter segmentation converter epimere, utilize the gas phase thermal source of segmentation converter hypomere, carry out pyrolysis herein and generate semicoke, coal gas and oil product, and discharged from the top of segmentation converter by gas phase, gas phase temperature 600 DEG C, gaseous pressure 3.9MPaG, successively by high temperature cyclone separator and accurate fly-ash separator, the coke breeze of the different-grain diameter in substep removing high temperature gas phase.
From the coke powder of high temperature cyclone separator and accurate fly-ash separator, send outside as product after part cooling; Another part turns back to the burner center of segmentation converter hypomere by high pressure (4.5MPaG) gas two-phase transportation, with the oxygen (~ 180 DEG C) of preheating in the outer annular space of burner and in press through hot steam (3.82MPaG, 450 DEG C) mix the bottom being injected to segmentation converter, generating portion oxidizing reaction herein, generate high temperature (1400 DEG C) raw gas, high temperature rough gas fast uplink enters the thermolysis section of segmentation converter, for the heat required for pulverized coal pyrolysis through trunnion.
From segmentation converter top, high temperature rough gas temperature after substep dedusting is out 550 ~ 580 DEG C, then produces middle pressure steam by waste heat boiler recovery waste heat; The raw gas temperature 250 DEG C going out waste heat boiler enters raw gas quenching column, is cooled to rapidly 100 DEG C by cold cycle solvent oil Quench; In wash cooling process, the gas phase oil product drop in raw gas is dissolved in cold cycle solvent oil; Controlled the inlet amount of cold cycle solvent by raw gas temperature out, guarantee that the gaseous phase outlet temperature raw gas quenching column is in more than dew point, maintain the quality of recycled solvent oil.
The raw gas going out raw gas quenching column is divided into two bursts of logistics: one gaseous stream send recycle gas compressor entrance, as the two-phase transportation medium of coke breeze, fine coal after pressurization; After another strand of gaseous stream send interchanger to be cooled to normal temperature, feeding gas-liquid separator separates goes out the phlegma in gas phase, then is delivered to extraneous process further; From raw gas quenching column tower reactor mixing oil product out, 350 DEG C of separating of oil towers of feeding are heated to by sending into pyrolysis oven after pump pressurization, separating-purifying is carried out in separating of oil tower, the discharging of separating of oil column overhead gas phase is through being cooled to solvent oil, return raw gas quenching column and continue Quench raw gas, and absorb oil product wherein; Heavy tar out at the bottom of separating of oil tower tower, sends outside as product after interchanger cooling.
Detect each product production as follows: tar: 78kg/h, coal gas is (containing CH
4: ~ 5%): 1864Nm
3/ h; Semicoke 220kg/h.
Claims (8)
1. the device of a coal substance catalyses decomposition and separating at high temperature, it is characterized in that: comprise coal dust preparation system, segmentation converter, cyclonic separator, accurate fly-ash separator, waste heat boiler, raw gas quenching column, separating of oil tower, coke powder tank, recycle gas compressor, dregs breaker, grey slag ladle, drum, process furnace, three groups of interchanger, surge tank, three groups of pumps, gas-liquid separators, wherein:
Described segmentation converter has upper and lower two-stage reaction cavity, be integrated by trunnion series connection between upper and lower two-stage reaction cavity in segmentation converter, the segmentation converter furnace wall that epimere reaction cavity is corresponding arranges multiple raw coal inlet, the segmentation converter furnace wall that hypomere reaction cavity is corresponding arranges multiple semicoke burner, segmentation converter top is provided with gas exit, is provided with slag-drip opening bottom segmentation converter;
Described raw gas quenching column, separating of oil tower are the unidirectional valve tray column structure of ejection-type, raw gas quenching column, separating of oil top of tower are respectively equipped with gaseous phase outlet, raw gas quenching column, separating of oil tower bottom are respectively equipped with liquid-phase outlet, are vertically provided with multilayer column plate respectively in raw gas quenching column, separating of oil tower;
The delivery port of described coal dust preparation system is communicated with multiple raw coal inlets of segmentation converter respectively, the gas exit of segmentation converter is communicated with the inlet mouth of cyclonic separator, segmentation converter bottom slag discharge is communicated with dregs breaker opening for feed, and dregs breaker discharge port is communicated with grey slag ladle inner top;
The slag-drip opening of described cyclonic separator is communicated with coke powder tank top, the air outlet of cyclonic separator is communicated with the inlet mouth of accurate fly-ash separator, the slag-drip opening of accurate fly-ash separator is also communicated with coke powder tank top, and the air outlet of accurate fly-ash separator is communicated with the inlet mouth of waste heat boiler; Described drum inlet mouth is communicated to waste heat boiler top, and drum air outlet is communicated with steam output pipe, and the air outlet of waste heat boiler is communicated with interior below orlop column plate in raw gas quenching column;
Described raw gas quenching column top gas phase outlet is communicated with recycle gas compressor inlet mouth, recycle gas compressor air outlet is communicated with coke powder pot bottom side, coke powder pot bottom opposite side is communicated with multiple semicoke burners of segmentation converter respectively, the outlet of raw gas quenching column top gas phase is also communicated with the inlet mouth of first group of interchanger, first group of interchanger air outlet is communicated with gas-liquid separator inlet mouth, the gaseous phase outlet of gas-liquid separator is connected with raw gas output tube, the liquid phase of gas-liquid separator exports and is connected with condensate drain, the outlet of raw gas quenching column bottom liquid phases is communicated with process furnace inlet mouth by first group of pump, process furnace air outlet is communicated with column plate position in separating of oil tower,
Described separating of oil top of tower gaseous phase outlet is communicated with the inlet mouth of second group of interchanger, the air outlet of second group of interchanger is communicated with surge tank top, surge tank bottom is communicated to raw gas quenching column, separating of oil tower inner top respectively by second group of pump, separating of oil tower bottom liquid-phase outlet is communicated with the inlet mouth of the 3rd group of interchanger by the 3rd group of pump, and the air outlet of the 3rd group of interchanger is connected with tar output tube.
2. the device of a kind of coal substance catalyses decomposition according to claim 1 and separating at high temperature, it is characterized in that: described coal dust preparation system comprises shredder assembly, drying installation, milling apparatus, catalyst preparing device, fine coal gas phase adds pressure output device, fine coal storehouse, coal material is broken through shredder assembly successively, drying installation is dry, fine coal is formed after milling apparatus grinding, fine coal enters the powdered catalyst prepared with catalyst preparing device in fine coal storehouse and is mixed to form mixture, the mixture exported from fine coal storehouse is sent into segmentation converter epimere reaction cavity by raw coal inlet.
3. the device of a kind of coal substance catalyses decomposition according to claim 1 and separating at high temperature, it is characterized in that: in described segmentation converter, the furnace wall of epimere reaction cavity adopts refractory liner, the furnace wall of hypomere reaction cavity adopts water wall, using epimere reaction cavity as fine coal thermolysis section, using hypomere reaction cavity as char Gasification conversion zone, be also connected with back cover bottom segmentation converter, back cover is made up of refractory liner.
4. a kind of coal substance catalyses decomposition according to claim 1 or 3 and the device of separating at high temperature, is characterized in that: be also provided with the outer annular space around center cavity in described semicoke burner.
5. the device of a kind of coal substance catalyses decomposition according to claim 1 and separating at high temperature, it is characterized in that: described cyclonic separator is made up of the alloy material of Wear-resistant, high-temperature resistant and the mould material of thermal insulation, forms mazy vapor phase stream path in cyclonic separator.
6. the device of a kind of coal substance catalyses decomposition according to claim 1 and separating at high temperature, it is characterized in that: described accurate fly-ash separator inwall is made up of mould material, accurate fly-ash separator outer wall is made up of carbon steel material, is provided with the filter core that metallic substance is made in accurate fly-ash separator.
7. the device of a kind of coal substance catalyses decomposition according to claim 1 and separating at high temperature, it is characterized in that: in described raw gas quenching column, separating of oil tower, liquid mass transfer carries out above column plate liquid layer, rely on gas flow at high rates that column plate upper liquid is injected into a large amount of comminuted drops, gas-liquid two-phase is disperse phase respectively with liquid, gas completes gas-liquid mass transfer for external phase state.
8. the coal substance catalyses based on device described in claim 1 decomposes and a separating at high temperature method, it is characterized in that: first the fine coal of coal dust preparation system output and the mixture of powdered iron series catalysts are sent in segmentation converter epimere reaction cavity by raw coal inlet;
Segmentation converter is divided into two sections reaction cavity, be integrated by trunnion series connection between two sections, epimere reaction cavity is fine coal thermolysis section: first the mixture of fine coal and catalyzer enters segmentation converter fine coal thermolysis section, the high temperature rough gas produced by hypomere char Gasification conversion zone char Gasification herein heats, high temperature rough gas temperature is 1300 ~ 1450 DEG C, fine coal transforms rapidly and resolves into semicoke under the effect of catalyzer, coal gas and oil product, gas phase temperature drops to 600 ~ 700 DEG C fast, and simultaneously along with the pushing effect of hypomere char Gasification conversion zone air-flow, three-phase product is rapidly to flowing, and leave segmentation converter, enter in cyclonic separator and accurate fly-ash separator successively, the coke breeze of the different-grain diameter in substep removing high temperature gas phase,
The hypomere reaction cavity of segmentation converter is char Gasification conversion zone: the coke powder be separated through the dedusting of raw gas quenching column turns back to semicoke burner center by gas two-phase transportation, with be preheating in the outer annular space of semicoke burner 180 DEG C oxygen and in press through hot steam and mix the hypomere reaction cavity being injected to segmentation converter, generating portion oxidizing reaction herein, generate high temperature rough gas, temperature gasification and high raw gas is advanced into the thermolysis section of segmentation converter, for the heat required for pulverized coal pyrolysis; The high-temperature slag that gasification section char Gasification produces, the refractory liner shock chamber flowing downstream into segmentation converter bottom carries out Quench, and slag is after the broken bulk slag of dregs breaker, and periodic exhaustion is to ash discharge slag ladle, drain into outside slag bath by grey slag ladle again, with dragveyer, the slag of discharging is exported;
The high temperature rough gas discharging on 600 DEG C, segmentation converter top, first enters in cyclonic separator, and oarse-grained solid semicoke enters coke powder tank after separating from gas; Gas phase enters in accurate fly-ash separator again, and isolate wherein fine powder further by metal filtering core burnt, fine powder Jiao is regularly sent in coke powder tank by pressurization; After going out in the raw gas of accurate fly-ash separator the coke powder removing about 99%, enter in waste heat boiler, middle pressure steam is produced by drum recovery waste heat, the raw gas going out waste heat boiler enters raw gas quenching column, cooled by low-temperature solvent oil wash in raw gas quenching column, raw gas is cooled to rapidly 100 DEG C, and the gas phase oil product simultaneously in coal gas is dissolved into rapidly in cold cycle solvent oil phase;
The raw gas that raw gas quenching column exports is divided into two strands: one gaseous stream send recycle gas compressor entrance, as the two-phase transportation gas of coke breeze, fine coal after pressurization; After another strand of gaseous stream send first group of interchanger to be cooled to normal temperature, feeding gas-liquid separator separates goes out the phlegma in gas phase, then is delivered to extraneous process further; From raw gas quenching column mixing oil product out, 350 DEG C are heated to by sending into process furnace after first group of pump pressurization, enter on the column plate on separating of oil tower top again, in separating of oil tower, carry out mass-and heat-transfer separation, the gas phase discharging of separating of oil column overhead is cooled to solvent oil through second group of interchanger, by second group of interchanger cooling, second group of pump pressurization, a part is back to separating of oil column overhead, another part sends into raw gas quenching column, continues Quench raw gas, and absorbs oil product wherein; Heavy tar out at the bottom of separating of oil tower tower, exports tar products and stores to outside tank field after the 3rd group of pump pressurization, the 3rd group of interchanger cooling.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105733688A (en) * | 2016-04-25 | 2016-07-06 | 中美新能源技术研发（山西）有限公司 | Coal liquefaction and coal gasification reactor |
| CN106281474A (en) * | 2016-08-30 | 2017-01-04 | 河北美邦工程科技股份有限公司 | A kind of pressurization moving bed coal gasifier high-temperature gas duster and waste-heat recovery device and method thereof |
| CN107557039A (en) * | 2017-08-08 | 2018-01-09 | 山东大学 | A kind of hierarchical segmented formula coke breeze preparation system and technique |
| CN107723031A (en) * | 2017-11-23 | 2018-02-23 | 航天长征化学工程股份有限公司 | High-pressure gasification and pyrolysis integrated device for pulverized coal |
| CN110591745A (en) * | 2019-10-14 | 2019-12-20 | 西北大学 | Pyrolysis-gasification integrated device and process |
Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS606787A (en) * | 1983-06-24 | 1985-01-14 | Babcock Hitachi Kk | Coal gasifying equipment |
| CN2257496Y (en) * | 1996-05-29 | 1997-07-09 | 中国科学院化工冶金研究所 | Spray pyrolytic device for preparing hollow tiny powder material |
| CN1721511A (en) * | 2005-07-01 | 2006-01-18 | 煤炭科学研究总院北京煤化工研究分院 | Process for pressurized gasification of dry coal fines |
| US20080016769A1 (en) * | 2006-07-24 | 2008-01-24 | Clean Energy, L.L.C. | Conversion of carbonaceous materials to synthetic natural gas by pyrolysis, reforming, and methanation |
| CN101942344A (en) * | 2010-09-20 | 2011-01-12 | 中国科学院山西煤炭化学研究所 | Method and device for gasifying multi-segment staged converted fluidized bed |
| US20110107945A1 (en) * | 2008-07-11 | 2011-05-12 | Ihi Corporation | Method and device for controlling retention time of fluid medium in fluidized-bed gasification furnace in gasification facility |
| CN102533345A (en) * | 2011-12-14 | 2012-07-04 | 中国科学院山西煤炭化学研究所 | Method and device for coal gasification in combined type fluidized bed |
| CN103387839A (en) * | 2013-07-19 | 2013-11-13 | 陕西延长石油（集团）有限责任公司碳氢高效利用技术研究中心 | Carbonic material coal tar extraction and synthetic gas manufacture integrated method and device |
| CN103409156A (en) * | 2013-08-02 | 2013-11-27 | 天华化工机械及自动化研究设计院有限公司 | Heat carrier destructive distillation system for coal and method thereof |
| CN103980948A (en) * | 2014-06-11 | 2014-08-13 | 华东理工大学 | Coal powder pyrolysis and gasification method |
| CN104017594A (en) * | 2014-06-20 | 2014-09-03 | 中煤能源黑龙江煤化工有限公司 | Low-temperature dry distillation method of coal |
| CN104449872A (en) * | 2014-12-11 | 2015-03-25 | 余传林 | Gasification process system for fine particle biomass or solid fossil fuel |
| CN204356293U (en) * | 2014-12-11 | 2015-05-27 | 余传林 | The gasifying process system of a kind of fine particle biomass or solid fossil fuel |
-
2015
- 2015-11-05 CN CN201510751755.XA patent/CN105419879B/en active Active
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS606787A (en) * | 1983-06-24 | 1985-01-14 | Babcock Hitachi Kk | Coal gasifying equipment |
| CN2257496Y (en) * | 1996-05-29 | 1997-07-09 | 中国科学院化工冶金研究所 | Spray pyrolytic device for preparing hollow tiny powder material |
| CN1721511A (en) * | 2005-07-01 | 2006-01-18 | 煤炭科学研究总院北京煤化工研究分院 | Process for pressurized gasification of dry coal fines |
| US20080016769A1 (en) * | 2006-07-24 | 2008-01-24 | Clean Energy, L.L.C. | Conversion of carbonaceous materials to synthetic natural gas by pyrolysis, reforming, and methanation |
| US20110107945A1 (en) * | 2008-07-11 | 2011-05-12 | Ihi Corporation | Method and device for controlling retention time of fluid medium in fluidized-bed gasification furnace in gasification facility |
| CN101942344A (en) * | 2010-09-20 | 2011-01-12 | 中国科学院山西煤炭化学研究所 | Method and device for gasifying multi-segment staged converted fluidized bed |
| CN102533345A (en) * | 2011-12-14 | 2012-07-04 | 中国科学院山西煤炭化学研究所 | Method and device for coal gasification in combined type fluidized bed |
| CN103387839A (en) * | 2013-07-19 | 2013-11-13 | 陕西延长石油（集团）有限责任公司碳氢高效利用技术研究中心 | Carbonic material coal tar extraction and synthetic gas manufacture integrated method and device |
| CN103409156A (en) * | 2013-08-02 | 2013-11-27 | 天华化工机械及自动化研究设计院有限公司 | Heat carrier destructive distillation system for coal and method thereof |
| CN103980948A (en) * | 2014-06-11 | 2014-08-13 | 华东理工大学 | Coal powder pyrolysis and gasification method |
| CN104017594A (en) * | 2014-06-20 | 2014-09-03 | 中煤能源黑龙江煤化工有限公司 | Low-temperature dry distillation method of coal |
| CN104449872A (en) * | 2014-12-11 | 2015-03-25 | 余传林 | Gasification process system for fine particle biomass or solid fossil fuel |
| CN204356293U (en) * | 2014-12-11 | 2015-05-27 | 余传林 | The gasifying process system of a kind of fine particle biomass or solid fossil fuel |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105733688A (en) * | 2016-04-25 | 2016-07-06 | 中美新能源技术研发（山西）有限公司 | Coal liquefaction and coal gasification reactor |
| CN105733688B (en) * | 2016-04-25 | 2018-07-06 | 中美新能源技术研发（山西）有限公司 | A kind of coal liquifaction solid/liquid/gas reactions device |
| CN106281474A (en) * | 2016-08-30 | 2017-01-04 | 河北美邦工程科技股份有限公司 | A kind of pressurization moving bed coal gasifier high-temperature gas duster and waste-heat recovery device and method thereof |
| CN106281474B (en) * | 2016-08-30 | 2019-08-20 | 河北美邦工程科技股份有限公司 | A kind of pressurization moving bed coal gasifier high-temperature gas duster and waste-heat recovery device and its method |
| CN107557039A (en) * | 2017-08-08 | 2018-01-09 | 山东大学 | A kind of hierarchical segmented formula coke breeze preparation system and technique |
| CN107723031A (en) * | 2017-11-23 | 2018-02-23 | 航天长征化学工程股份有限公司 | High-pressure gasification and pyrolysis integrated device for pulverized coal |
| CN110591745A (en) * | 2019-10-14 | 2019-12-20 | 西北大学 | Pyrolysis-gasification integrated device and process |
| CN110591745B (en) * | 2019-10-14 | 2024-04-26 | 西北大学 | Pyrolysis-gasification integrated device and process |
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