WO2018218915A1 - 一种煤热解工艺装置 - Google Patents

一种煤热解工艺装置 Download PDF

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Publication number
WO2018218915A1
WO2018218915A1 PCT/CN2017/114976 CN2017114976W WO2018218915A1 WO 2018218915 A1 WO2018218915 A1 WO 2018218915A1 CN 2017114976 W CN2017114976 W CN 2017114976W WO 2018218915 A1 WO2018218915 A1 WO 2018218915A1
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WIPO (PCT)
Prior art keywords
coal
primary
coal pyrolysis
gas outlet
pyrolysis device
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PCT/CN2017/114976
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English (en)
French (fr)
Inventor
朱书成
王希彬
曹国超
李明德
李金峰
李仿
吕艳吾
Original Assignee
河南龙成煤高效技术应用有限公司
河北龙成煤综合利用有限公司
陕西龙成煤清洁高效利用有限公司
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Application filed by 河南龙成煤高效技术应用有限公司, 河北龙成煤综合利用有限公司, 陕西龙成煤清洁高效利用有限公司 filed Critical 河南龙成煤高效技术应用有限公司
Priority to AU2017416200A priority Critical patent/AU2017416200B2/en
Priority to US16/478,222 priority patent/US20200032151A1/en
Priority to RU2019124330A priority patent/RU2734349C1/ru
Priority to JP2019540602A priority patent/JP6968183B2/ja
Priority to CA3047860A priority patent/CA3047860C/en
Priority to KR1020197021310A priority patent/KR20190099041A/ko
Priority to EP17911578.7A priority patent/EP3549998A4/en
Publication of WO2018218915A1 publication Critical patent/WO2018218915A1/zh
Priority to ZA2019/04691A priority patent/ZA201904691B/en

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/30—Other processes in rotary ovens or retorts
    • 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
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B27/00—Arrangements for withdrawal of the distillation gases
    • 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
    • C10B33/00—Discharging devices; Coke guides
    • 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
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • 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
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/02—Multi-step carbonising or coking processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/18—Modifying the properties of the distillation gases in the oven
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1269—Heating the gasifier by radiating device, e.g. radiant tubes
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment

Definitions

  • the invention relates to the field of heat exchange technology, in particular to a coal pyrolysis process device.
  • Coal pyrolysis equipment varies greatly depending on the requirements of the final product.
  • the pyrolysis equipment also has significant differences.
  • the coal tar yield is also significantly different, such as the coke oven used for coking and the blue carbon furnace used to produce blue carbon.
  • the coke oven produces coke volatiles are relatively low, coal tar yield is low, but the gas volume is large, the blue carbon furnace produces higher volatile carbon, the coal tar yield is relatively high, the gas volume is slightly lower,
  • CN101985558 a patent for decomposition equipment of coal materials, discloses a decomposition device for coal materials, comprising a closed kiln body with a feed port and a discharge port, and a flame gas pipe is arranged in the kiln body
  • the heating mechanism, the coal material heating mechanism formed between the flame gas pipe heating mechanism and the inner wall of the kiln advances a decomposition passage, and the coal kiln body is provided with a coal decomposition gas collecting pipe that communicates with the coal material propulsion decomposition passage.
  • the invention transfers a large amount of heat generated by the flame gas duct heating mechanism to the coal powder of the coal material propelling decomposition passage, the coal powder is fully absorbed, and the coal powder is heated and decomposed, and is decomposed into gas in the coal material propulsion separation passage.
  • Coal, gas and coke oil with high coke oil and gas and high calorific value are connected to the gas dedusting and liquefaction mechanism outside the rotary kiln through the coal gas decomposition gas collection pipe, and the gas, coke oil and gas decomposed into, dedusted, separated, pressurized and liquefied.
  • the object of the present invention is to provide a coal pyrolysis process device for the disadvantages of the prior art, which can achieve both high-efficiency gas production and coal-producing tar.
  • the technical solution adopted by the present invention is: a coal pyrolysis process device, comprising a primary coal pyrolysis device and a secondary coal pyrolysis device, wherein the primary coal pyrolysis device is rotary kiln radiation a tube-heated coal decomposition device, the primary coal pyrolysis device comprising a first-stage feed port, a first-stage discharge port, a first-stage gas outlet, and a first-stage radiant tube heating mechanism;
  • the secondary coal pyrolysis device comprises a secondary feed port, a secondary discharge port, a secondary gas outlet, and a secondary heating mechanism;
  • the primary discharge port is in communication with the secondary feed port, and the coal is maximally extracted from the primary coal pyrolysis device, and then enters the secondary coal pyrolysis device, and the coal is in the secondary coal pyrolysis device.
  • the upper part continues to heat up and pyrolyze, so that after the first stage pyrolysis The volatile matter of the coal is further reduced in the secondary coal pyrolysis unit to produce more gas.
  • the secondary coal pyrolysis device is a rotary kiln radiant tube heating type coal decomposition device or a shaft kiln heat exchange type coal decomposition device.
  • the coal pyrolysis process device further includes a drying device for setting coal before the primary coal pyrolysis device, and the dried coal enters the primary coal pyrolysis device.
  • the coal pyrolysis process device further comprises a first-stage gas outlet setting dust collector, and the second-stage gas outlet is provided with a dust remover, wherein the dust remover is a high-temperature membrane filter of a cyclone dust collector or a gravity dust collector or a filter core surface film.
  • the primary gas outlet and the secondary gas outlet are brought together into a high temperature membrane filter.
  • the primary gas outlet and the secondary gas outlet are brought together through a cyclone or a gravity precipitator and then into the high temperature membrane filter.
  • the primary gas outlet enters the membrane filter one, and the secondary gas outlet enters the membrane filter 2.
  • the first-stage gas outlet first passes through a cyclone or a gravity dust collector, and enters the membrane filter.
  • the second-stage gas outlet first passes through a cyclone or a gravity dust collector 2, and then enters the membrane filter 2.
  • the invention has the advantages that: in the primary coal pyrolysis device, the tar yield reaches the maximum value, and the upgraded coal with higher volatile content in the first stage enters the secondary coal pyrolysis device under heat; Heating and pyrolysis, producing upgraded coal with lower volatile content, and increasing production of more gas.
  • the gas produced by secondary pyrolysis contains more CO and H2, and CO can be converted into H2 by gas conversion, which can be coal tar. Hydrogenation provides sufficient H2 source to effectively reduce the cost of coal tar hydrogenation.
  • the filter is added to filter the dust and tar-containing gas before the oil and gas are separated to ensure the cleanliness of the oil and gas. Subsequent processing lays a good foundation.
  • Embodiment 1 is a schematic structural view of Embodiment 1 of the present invention.
  • Embodiment 2 is a schematic structural view of Embodiment 2 of the present invention.
  • Embodiment 3 is a schematic structural view of Embodiment 3 of the present invention.
  • Embodiment 4 is a schematic structural view of Embodiment 4 of the present invention.
  • a coal pyrolysis process device comprises a primary coal pyrolysis device 1 and a secondary coal pyrolysis device 2, wherein the primary coal pyrolysis device 1 is a rotary kiln radiant tube heating Coal decomposition equipment, the first coal pyrolysis device 1 package Including a first feed port 11, a first discharge port 12, a first gas outlet 13, a first radiant tube heating mechanism 14;
  • the secondary coal pyrolysis device 2 comprises a secondary feed port 21, a secondary discharge port 22, a secondary gas outlet 23, and a secondary heating mechanism 24;
  • the primary discharge port 12 is in communication with the secondary feed port 21, and the coal is extracted in the primary coal pyrolysis device 1 to maximize the coal tar, and then enters the secondary coal pyrolysis device 2, and the coal is in the secondary
  • the upper part of the coal pyrolysis device 2 continues to be heated and pyrolyzed, so that the volatile coal of the upgraded coal after the primary pyrolysis is further reduced in the secondary coal pyrolysis device 2 to produce more gas.
  • the secondary coal pyrolysis device 2 is a rotary kiln radiant tube heating type coal decomposition device.
  • the coal pyrolysis process apparatus further includes a drying device 3 for arranging coal before the primary coal pyrolysis device 1, and the dried coal enters the primary coal pyrolysis device 1.
  • the primary gas outlet and the secondary gas outlet enter a high temperature membrane filter 5.
  • a coal pyrolysis process device comprises a primary coal pyrolysis device 1 and a secondary coal pyrolysis device 2, wherein the primary coal pyrolysis device 1 is a rotary kiln radiant tube heating a coal-calculating device, the primary coal pyrolysis device 1 comprises a first-stage feed port 11, a first-stage discharge port 12, a first-stage gas outlet 13, a first-stage radiant tube heating mechanism 14;
  • the secondary coal pyrolysis device 2 comprises a secondary feed port 21, a secondary discharge port 22, a secondary gas outlet 23, and a secondary heating mechanism 24;
  • the primary discharge port 12 is in communication with the secondary feed port 21, and the coal is extracted in the primary coal pyrolysis device 1 to maximize the coal tar, and then enters the secondary coal pyrolysis device 2, and the coal is in the secondary
  • the upper part of the coal pyrolysis device 2 continues to be heated and pyrolyzed, so that the volatile coal of the upgraded coal after the primary pyrolysis is further reduced in the secondary coal pyrolysis device 2 to produce more gas.
  • the secondary coal pyrolysis device 2 is a rotary kiln radiant tube heating type coal decomposition device.
  • the coal pyrolysis process apparatus further includes a drying device 3 for arranging coal before the primary coal pyrolysis device 1, and the dried coal enters the primary coal pyrolysis device 1.
  • the primary gas outlet 13 and the secondary gas outlet 23 are first passed through a cyclone or gravity precipitator 4 and then into the high temperature membrane filter 5.
  • a coal pyrolysis process device comprises a primary coal pyrolysis device 1 and a secondary coal pyrolysis device 2, wherein the primary coal pyrolysis device 1 is a rotary kiln radiant tube heating a coal-calculating device, the primary coal pyrolysis device 1 comprises a first-stage feed port 11, a first-stage discharge port 12, a first-stage gas outlet 13, a first-stage radiant tube heating mechanism 14;
  • the secondary coal pyrolysis device 2 comprises a secondary feed port 21, a secondary discharge port 22, a secondary gas outlet 23, and a secondary heating mechanism 24;
  • the primary discharge port 12 is in communication with the secondary feed port 21, and the coal is extracted in the primary coal pyrolysis device 1 to maximize the coal tar, and then enters the secondary coal pyrolysis device 2, and the coal is in the secondary
  • the upper part of the coal pyrolysis unit 2 continues to heat up and pyrolyze, so that the first stage heat
  • the volatile coal of the upgraded coal after the degreasing is further reduced in the secondary coal pyrolysis unit 2 to produce more gas.
  • the secondary coal pyrolysis device 2 is a shaft kiln heat exchange type coal decomposition device.
  • the coal pyrolysis process apparatus further includes a drying device 3 for arranging coal before the primary coal pyrolysis device 1, and the dried coal enters the primary coal pyrolysis device 1.
  • the primary gas outlet 13 enters the membrane filter 51, which enters the membrane filter 222.
  • a coal pyrolysis process device comprises a primary coal pyrolysis device 1 and a secondary coal pyrolysis device 2, wherein the primary coal pyrolysis device 1 is a rotary kiln radiant tube heating a coal-calculating device, the primary coal pyrolysis device 1 comprises a first-stage feed port 11, a first-stage discharge port 12, a first-stage gas outlet 13, a first-stage radiant tube heating mechanism 14;
  • the secondary coal pyrolysis device 2 comprises a secondary feed port 21, a secondary discharge port 22, a secondary gas outlet 23, and a secondary heating mechanism 24;
  • the primary discharge port 12 is in communication with the secondary feed port 21, and the coal is extracted in the primary coal pyrolysis device 1 to maximize the coal tar, and then enters the secondary coal pyrolysis device 2, and the coal is in the secondary
  • the upper part of the coal pyrolysis device 2 continues to be heated and pyrolyzed, so that the volatile coal of the upgraded coal after the primary pyrolysis is further reduced in the secondary coal pyrolysis device 2 to produce more gas.
  • the secondary coal pyrolysis device 2 is a shaft kiln heat exchange type coal decomposition device.
  • the coal pyrolysis process apparatus further includes a drying device 3 for arranging coal before the primary coal pyrolysis device 1, and the dried coal enters the primary coal pyrolysis device 1.
  • the primary gas outlet 13 enters the membrane filter 51, which enters the membrane filter 222.
  • the primary gas outlet 13 first passes through a cyclone or a gravity precipitator 41, and enters the membrane filter 51.
  • the secondary gas outlet 23 passes through a cyclone or a gravity precipitator 42 before entering the membrane. Filter two 52.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Industrial Gases (AREA)
  • Drying Of Solid Materials (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

一种煤热解工艺装置，包括一级煤热解装置(1)和二级煤热解装置(2)，一级煤热解装置(1)的出料口(12)与二级煤热解装置(2)的进料口(21)连通，煤在一级煤热解装置(1)将煤焦油最大化提取出来，然后进入二级煤热解装置(2)，煤在二级煤热解装置(2)上部继续升温热解，使经一级热解提质后的提质煤挥发份，在二级煤热解装置(2)中进一步降低，生产更多煤气。

Description

一种煤热解工艺装置 技术领域
本发明涉及热交换技术领域，具体涉及一种煤热解工艺装置。
背景技术
煤的热解设备根据对最终产物要求的不同，热解设备也有重大不同，煤焦油产率也有重大不同，比如用于制焦的焦炭炉和用于生产兰碳的兰碳炉在炉型上有重大差别，焦炉所产焦炭挥发份比较低，煤焦油产率低，但煤气量大，兰碳炉所产兰碳挥发份较高，煤焦油产率相对较高，煤气量稍低，随着石油战略的需求，近几年用于产油率高的低温煤焦油的回转窑成为新宠。申请号201010262786.6、公开号CN101985558、煤物质的分解设备的专利，公开了一种煤物质的分解设备，包括一个带有进料口和出料口的密闭窑体，所述窑体内设置焰气管道加热机构，所述焰气管道加热机构与窑体内壁之间形成的煤物质推进分解通道，所述窑体上设置与煤物质推进分解通道连通的煤分解气收集管。由于该发明将焰气管道加热机构产生的大量的热传导、辐射到煤物质推进分解通道的煤粉上，煤粉充分地吸收，煤粉升温分解，就在煤物质推进分离通道内分解成燃气、焦油气和热值较高的煤，燃气和焦油气通过所述煤分解气收集管与回转窑外的气体除尘液化机构连接，将分解到的燃气、焦油气，除尘、分离、加压液化。
上述专利在油产率方面确实比较高，是一个示范，但此专利仅考虑了最大限度产焦油率，没有考虑这种低温热解带来的提质后的煤挥发份仍然较大，以及焦油加氢对煤气量的需求。上述专利有其局限性，要么煤焦油产率高，而煤气量低，要么产气量高，而煤焦油产率低，二者无法兼顾。
发明内容
有鉴于此，本发明提供的目的是针对现有技术的不足，提供一种煤热解工艺装置，能够做到兼顾高效产气和产煤焦油。
为解决上述技术问题，本发明所采取的技术方案是：一种煤热解工艺装置，包括一级煤热解装置和二级煤热解装置，所述一级煤热解装置为回转窑辐射管加热式煤分解设备，所述一级煤热解装置包括一级进料口，一级出料口，一级煤气出口，一级辐射管加热机构；
所述二级煤热解装置包括二级进料口，二级出料口，二级煤气出口，二级加热机构；
所述一级出料口与所述二级进料口连通，煤在一级煤热解装置将煤焦油最大化提取出来，然后进入二级煤热解装置，煤在二级煤热解装置上部继续升温热解，使经一级热解提质后的提 质煤挥发份，在二级煤热解装置中进一步降低，生产更多煤气。
所述二级煤热解装置为回转窑辐射管加热式煤分解设备或竖窑热交换式煤分解设备。
所述煤热解工艺装置还包括在一级煤热解装置前设置煤的干燥装置，经干燥后的煤进入一级煤热解装置。
所述煤热解工艺装置还包括一级煤气出口设置除尘器，二级煤气出口设置除尘器，所述除尘器为旋风除尘器或重力除尘器或滤芯表面覆膜的高温膜式过滤器。
所述一级煤气出口和所述二级煤气出口汇集一起进入高温膜式过滤器。
所述一级煤气出口和所述二级煤气出口汇集一起先经过旋风除尘器或重力除尘器，再进入所述高温膜式过滤器。
所述一级煤气出口进入膜式过滤器一，所述二级煤气出口进入膜式过滤器二。
所述一级煤气出口先经过旋风除尘器或重力除尘器一，进入膜式过滤器一，所述二级煤气出口先经过旋风除尘器或重力除尘器二，再进入膜式过滤器二。
本发明的优点：煤在一级煤热解装置中，焦油产率达到最大的值，将一级含挥发份仍较高的提质煤在热的状态下进入二级煤热解装置中继续升温热解，生产出挥发份更低的提质煤，同时增产更多的煤气，二次热解产生的煤气含CO、H2量更多，CO可通过煤气转化变成H2，可为煤焦油加氢提供足够的H2源，有效降低煤焦油加氢的成本。
增加干燥装置有利于减少煤热解的能耗；增设过滤器是为了将含粉尘、含焦油的煤气，在油、气分离前将粉尘过滤除去，保证油和气的洁净度，为油、气的后续处理奠定良好基础。
附图说明
图1为本发明实施例一的结构示意图；
图2为本发明实施例二的结构示意图；
图3为本发明实施例三的结构示意图；
图4为本发明实施例四的结构示意图。
具体实施方式
为使本发明实施例的目的、技术方案和优点更加清楚，下面将结合本发明实施例的附图1-4，对本发明实施例的技术方案进行清楚、完整地描述。显然，所描述的实施例是本发明的一部分实施例，而不是全部的实施例。基于所描述的本发明的实施例，本领域普通技术人员所获得的所有其他实施例，都属于本发明保护的范围。
实施例一:如图1所示，一种煤热解工艺装置，包括一级煤热解装置1和二级煤热解装置2，所述一级煤热解装置1为回转窑辐射管加热式煤分解设备，所述一级煤热解装置1包 括一级进料口11，一级出料口12，一级煤气出口13，一级辐射管加热机构14；
所述二级煤热解装置2包括二级进料口21，二级出料口22，二级煤气出口23，二级加热机构24；
所述一级出料口12与所述二级进料口21连通，煤在一级煤热解装置1将煤焦油最大化提取出来，然后进入二级煤热解装置2，煤在二级煤热解装置2上部继续升温热解，使经一级热解提质后的提质煤挥发份，在二级煤热解装置2中进一步降低，生产更多煤气。
所述二级煤热解装置2为回转窑辐射管加热式煤分解设备。
所述煤热解工艺装置还包括在一级煤热解装置1前设置煤的干燥装置3，经干燥后的煤进入一级煤热解装置1。
所述一级煤气出口和所述二级煤气出口进入一个高温膜式过滤器5。
实施例二：如图2所示，一种煤热解工艺装置，包括一级煤热解装置1和二级煤热解装置2，所述一级煤热解装置1为回转窑辐射管加热式煤分解设备，所述一级煤热解装置1包括一级进料口11，一级出料口12，一级煤气出口13，一级辐射管加热机构14；
所述二级煤热解装置2包括二级进料口21，二级出料口22，二级煤气出口23，二级加热机构24；
所述一级出料口12与所述二级进料口21连通，煤在一级煤热解装置1将煤焦油最大化提取出来，然后进入二级煤热解装置2，煤在二级煤热解装置2上部继续升温热解，使经一级热解提质后的提质煤挥发份，在二级煤热解装置2中进一步降低，生产更多煤气。
所述二级煤热解装置2为回转窑辐射管加热式煤分解设备。
所述煤热解工艺装置还包括在一级煤热解装置1前设置煤的干燥装置3，经干燥后的煤进入一级煤热解装置1。
所述一级煤气出口13和所述二级煤气出口23汇集先经过一个旋风除尘器或重力除尘器4，再进入所述高温膜式过滤器5。
实施例三：如图3所示，一种煤热解工艺装置，包括一级煤热解装置1和二级煤热解装置2，所述一级煤热解装置1为回转窑辐射管加热式煤分解设备，所述一级煤热解装置1包括一级进料口11，一级出料口12，一级煤气出口13，一级辐射管加热机构14；
所述二级煤热解装置2包括二级进料口21，二级出料口22，二级煤气出口23，二级加热机构24；
所述一级出料口12与所述二级进料口21连通，煤在一级煤热解装置1将煤焦油最大化提取出来，然后进入二级煤热解装置2，煤在二级煤热解装置2上部继续升温热解，使经一级热 解提质后的提质煤挥发份，在二级煤热解装置2中进一步降低，生产更多煤气。
所述二级煤热解装置2为竖窑热交换式煤分解设备。
所述煤热解工艺装置还包括在一级煤热解装置1前设置煤的干燥装置3，经干燥后的煤进入一级煤热解装置1。
所述一级煤气出口13进入膜式过滤器一51，所述二级煤气出口23进入膜式过滤器二52。
实施例四：如图4所示，一种煤热解工艺装置，包括一级煤热解装置1和二级煤热解装置2，所述一级煤热解装置1为回转窑辐射管加热式煤分解设备，所述一级煤热解装置1包括一级进料口11，一级出料口12，一级煤气出口13，一级辐射管加热机构14；
所述二级煤热解装置2包括二级进料口21，二级出料口22，二级煤气出口23，二级加热机构24；
所述一级出料口12与所述二级进料口21连通，煤在一级煤热解装置1将煤焦油最大化提取出来，然后进入二级煤热解装置2，煤在二级煤热解装置2上部继续升温热解，使经一级热解提质后的提质煤挥发份，在二级煤热解装置2中进一步降低，生产更多煤气。
所述二级煤热解装置2为竖窑热交换式煤分解设备。
所述煤热解工艺装置还包括在一级煤热解装置1前设置煤的干燥装置3，经干燥后的煤进入一级煤热解装置1。
所述一级煤气出口13进入膜式过滤器一51，所述二级煤气出口23进入膜式过滤器二52。
所述一级煤气出口13先经过旋风除尘器或重力除尘器一41，进入膜式过滤器一51，所述二级煤气出口23先经过旋风除尘器或重力除尘器二42，再进入膜式过滤器二52。
以上所述是本发明的优选实施方式，应当指出，对于本技术领域的普通技术人员来说，在不脱离本发明所述原理的前提下，还可以作出若干改进和润饰，这些改进和润饰也应视为本发明的保护范围。

Claims (8)

  1. 一种煤热解工艺装置，包括一级煤热解装置和二级煤热解装置，其特征在于：所述一级煤热解装置为回转窑辐射管加热式煤分解设备；
    所述一级煤热解装置包括一级进料口，一级出料口，一级煤气出口，一级辐射管加热机构；所述二级煤热解装置包括二级进料口，二级出料口，二级煤气出口，二级加热机构；
    所述一级出料口与所述二级进料口连通，煤在一级煤热解装置将煤焦油最大化提取出来，然后进入二级煤热解装置，煤在二级煤热解装置上部继续升温热解，使经一级热解提质后的提质煤挥发份，在二级煤热解装置中进一步降低，生产更多煤气。
  2. 如权利要求1所述的煤热解工艺装置，其特征在于：所述二级煤热解装置为回转窑辐射管加热式煤分解设备或竖窑热交换式煤分解设备。
  3. 如权利要求1所述的煤热解工艺装置，其特征在于：所述煤热解工艺装置还包括在一级煤热解装置前设置煤的干燥装置，经干燥后的煤进入一级煤热解装置。
  4. 如权利要求1所述的煤热解工艺装置，其特征在于：所述煤热解工艺装置还包括一级煤气出口设置除尘器，二级煤气出口设置除尘器，所述除尘器为旋风除尘器或重力除尘器或滤芯表面覆膜的高温膜式过滤器。
  5. 如权利要求4所述的煤热解工艺装置，其特征在于：所述一级煤气出口和所述二级煤气出口汇集一起进入高温膜式过滤器。
  6. 如权利要求4所述的煤热解工艺装置，其特征在于：所述一级煤气出口和所述二级煤气出口汇集一起先经过旋风除尘器或重力除尘器，再进入所述高温膜式过滤器。
  7. 如权利要求4所述的煤热解工艺装置，其特征在于：所述一级煤气出口进入膜式过滤器一，所述二级煤气出口进入膜式过滤器二。
  8. 如权利要求4所述的煤热解工艺装置，其特征在于：所述一级煤气出口先经过旋风除尘器或重力除尘器一，进入膜式过滤器一，所述二级煤气出口先经过旋风除尘器或重力除尘器二，再进入膜式过滤器二。
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