WO2015074591A1 - 一种含碳物质反应系统及方法 - Google Patents

一种含碳物质反应系统及方法 Download PDF

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Publication number
WO2015074591A1
WO2015074591A1 PCT/CN2014/091839 CN2014091839W WO2015074591A1 WO 2015074591 A1 WO2015074591 A1 WO 2015074591A1 CN 2014091839 W CN2014091839 W CN 2014091839W WO 2015074591 A1 WO2015074591 A1 WO 2015074591A1
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Prior art keywords
cooling
temperature
syngas
carbonaceous material
reaction
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PCT/CN2014/091839
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English (en)
French (fr)
Inventor
信伟
李红海
高瑞恒
陈永进
李晓飞
刘品
李立志
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航天长征化学工程股份有限公司
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Priority to SG11201601465WA priority Critical patent/SG11201601465WA/en
Priority to PL14863389T priority patent/PL3075819T3/pl
Priority to JP2016554785A priority patent/JP2017500434A/ja
Priority to AP2016009233A priority patent/AP2016009233A0/en
Priority to KR1020167012376A priority patent/KR20160068932A/ko
Priority to EP14863389.4A priority patent/EP3075819B1/en
Priority to AU2014352357A priority patent/AU2014352357B2/en
Priority to BR112016009506-5A priority patent/BR112016009506B1/pt
Priority to US15/038,792 priority patent/US9926502B2/en
Priority to UAA201605120A priority patent/UA114683C2/uk
Publication of WO2015074591A1 publication Critical patent/WO2015074591A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • 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
    • C10J3/485—Entrained flow gasifiers
    • 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
    • C10J3/845—Quench rings
    • 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
    • C10J2300/16—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
    • C10J2300/1628—Ash post-treatment
    • C10J2300/1631—Ash recycling
    • 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
    • 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
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Definitions

  • the invention relates to a carbonaceous material gasification system and method, in particular to a large-scale system and method for producing synthesis gas by pressurized gasification of pulverized coal with a daily processing capacity of more than 2000 tons.
  • the development trend of modern petrochemical enterprises is large-scale and large-scale.
  • the large-scale high-pressure gasification unit is also the direction of the development of clean coal gasification technology, but existing gasification units have certain problems.
  • the single-nozzle gasifier is subject to certain restrictions in the direction of large-scale production due to restrictions on coal transportation.
  • the gasifier using a plurality of nozzles in the upstream process of the syngas can be further enlarged, but since the flow direction of the liquid slag is opposite to the flow direction of the syngas, a certain amount of water having a lower temperature is generated when the liquid slag falls into the slag pool.
  • the vapor enters the furnace through the slag outlet in the opposite direction to the flow direction of the liquid slag, which reduces the temperature of the liquid slag.
  • the liquid slag falls unbalanced, it is easy to cause the liquid slag to solidify without falling into the slag pool. Since there is not enough heat to melt the solid residue, the solid residue tends to accumulate thicker and eventually cause the problem of slag plugging, causing the device to stop.
  • the multi-nozzle gasifier using the syngas down process can be further enlarged, but in order to make full use of the furnace space, the nozzle is often placed in the upper part of the furnace near the top of the furnace, and the high temperature gas and liquid residue in the reaction process will continuously erode.
  • the top of the furnace is easy to cause the phenomenon of overheating at the top of the furnace, which becomes a hidden danger of safe production.
  • the present invention provides a carbonaceous material dry powder gasification system characterized by comprising a carbonaceous material reaction device and for boosting crude syngas from a portion of the reaction device, cooled and initially purified. The gas returning device is then blended with the high temperature crude syngas from the reaction device.
  • the descending crude syngas is mainly to prevent slag blocking, and at the same time, the cooled low-temperature water syngas is pressurized and sent to the preliminary cooler to serve as a cooling medium to reduce the temperature of the ascending raw syngas.
  • the cooling substance may also be water, water mist, water + inert gas (CO2, N2), water + syngas, syngas.
  • cooling is mainly achieved by heat exchange with a cooling substance. Purification is mainly achieved by the separation of gas and particles under the action of gravity and inertial force.
  • Cooling means that the mass of the injected coolant is reduced so that the mixed gas is reduced to a specified temperature (for example, to 900 ° C). Cooling means that an excessive amount of cooling material is injected to make it sufficiently heat exchange, and the cooling temperature is greater.
  • Purification involves the removal of ash and entrained droplets from the syngas, which does not include water removal.
  • the carbonaceous material reaction apparatus includes a gasification reaction section, an upper gas outlet, and a lower gas outlet.
  • part or all of the crude syngas flowing out from the lower gas outlet is subjected to temperature reduction and preliminary purification, and then is pressurized by the gas flowing through the pipeline, and the upward crude syngas flowing out from the gasification reaction section mixing.
  • the carbonaceous material reaction apparatus further comprises a lower cooling purification section for cooling, preliminary purifying the descending high temperature crude syngas flowing out of the gasification reaction section; and a lower cooling purification section inlet and gasification The lower outlet of the reaction section is connected, and the syngas outlet is at the upper middle portion of the lower cooling section.
  • the syngas outlet of the lower cooling purification section and the lower outlet of the system may be one port.
  • the lower cooling purification section further comprises a quenching device, a slag pool, and a coarse slag outlet.
  • the gas returning device comprises a coarse slag removing device and a pneumatic press
  • the inlet of the coarse slag removing device is connected to the lower cooling and purifying section syngas outlet through a pipe, and the air press is used for improving the cooling and cooling.
  • the crude syngas pressure can be injected partially or completely by a preliminary cooling and cooling device at a pressure higher than 0.1 MPa to 6 MPa of the ascending gas, or partially or completely by an ascending quenching device.
  • the pressurized raw syngas is at a lower temperature and the entrained water actually acts as a cooling medium, which can reduce energy consumption and reduce water consumption.
  • the number of air presses is from 1 to 10, preferably from 2 to 5.
  • the carbonaceous material reaction apparatus further comprises a temperature-lowering reaction section disposed in the upper middle portion of the apparatus, the inlet being connected to the upper outlet of the gasification reaction section.
  • the inlet of the temperature-lowering reaction section and the upper outlet of the gasification reaction section are provided with a preliminary cooling device for the low-temperature water-slurry synthesis gas injection through the pressure machine.
  • High-temperature crude syngas blending with ash Mixing on the one hand, cooling and cooling, the fly ash temperature entrained in the ascending high-temperature crude syngas is reduced below t2 (softening temperature of ash) to make it lose viscosity, and on the other hand, the reactants are supplemented, and the carbon in the fly ash is further completed in the cooling reaction section.
  • the gasification reaction increases the hydrogen to carbon ratio of the syngas, and the ash here is fly ash.
  • the crude syngas cooled and purified by the lower cooling section usually still entrains some of the larger ash slag.
  • the crude syngas with entrained water and fine ash is sent to the preliminary cooling device by the air press to serve as cooling. a substance used to cool the raw syngas entering the cooling reaction zone and participate in the cooling reaction.
  • the carbonaceous material reaction apparatus further comprises an upper cooling purification section, wherein when the apparatus has a cooling reaction section, the inlet is connected to the upper outlet of the cooling reaction section; when the apparatus does not have a cooling reaction In the section, the inlet is connected to the upper outlet of the gasification reaction section and is connected to the outlet of the gas return means.
  • the upper cooling purification section comprises a quenching device, a ash pool and a syngas outlet, wherein the syngas outlet is arranged at an upper middle portion of the upper cooling section, and one or more may be arranged, It is preferably 1 to 3.
  • the syngas is passed through the quenching in the upper cooling and purifying device, and after one or more cooling and purification, it is sent to the subsequent process through the syngas outlet.
  • the nozzles may be arranged in 1 layer or in a plurality of layers, preferably 1 to 3 layers.
  • the present invention provides a method for gasification of a large carbonaceous material dry powder, comprising the steps of:
  • the carbonaceous material and the gasifying agent are reacted in the gasification reaction device to form a crude synthesis gas whose main components are CO and H2 and a ash residue whose main component is inorganic matter; wherein some of the high-temperature crude synthesis gas and the fly ash and the liquid residue are descended. , part of the high temperature crude syngas gas and fly ash up;
  • the descending liquid slag is quenched and discharged out of the furnace;
  • the cooled and synthesized crude syngas continues to rise upwards through the ascending quenching device and then enters the upper cooling section to cool down and remove the ash to obtain the crude syngas that meets the requirements of the subsequent process.
  • the method comprises the following steps:
  • the carbonaceous material and the gasifying agent are sprayed into the gasification reaction section through a plurality of nozzles, and rapidly reacted under high temperature (1200 ° C to 2000 ° C) high pressure (0.1 MPa to 11 MPa) to form a crude synthesis of CO and H 2 as main components.
  • Gas and ash which is mainly composed of inorganic substances;
  • the slag discharge device wherein the majority mostly represents, for example, more than 50%, preferably more than 55%, preferably more than 60%, preferably more than 65%, preferably more than 70%, preferably more than 75%, preferably more than 80%, preferably more than 85%, etc.;
  • the crude syngas and fly ash after the reaction continue to ascend, and after quenching, enter the upper cooling and purifying section. After cooling and purifying, the fly ash in the crude syngas is removed, and the relatively clean low-temperature crude syngas is sent to the subsequent process.
  • the so-called rapid reaction means completion in less than 10 seconds and 90% in 5 seconds.
  • the process of the invention can be carried out in any suitable system, preferably in the system of the invention.
  • the thermal efficiency is effectively improved, the energy consumption of the device is reduced, the amount of water is reduced, the ash of the syngas is reduced, and the pressure of the subsequent process is reduced.
  • the invention adopts the method of venting the gas at the same time as the crude syngas, and on the one hand, effectively avoids the slag slag problem of the upstream gas outlet mode, and on the other hand avoids the top overheating problem of the down gas outlet mode;
  • the invention adopts a multi-nozzle arrangement, which is beneficial to the full reaction and is advantageous for the enlargement of the device;
  • Figure 1 is a schematic illustration of the gasification process of the present invention.
  • Figure 2 is a schematic illustration of a system of the present invention.
  • a method for gasification of a large carbonaceous material dry powder is characterized in that it comprises the following steps:
  • the pulverized coal and oxygen are injected into the gasification reaction section 2 through the nozzle 21, and rapidly reacted at a high temperature (1200 ° C to 2000 ° C) high pressure (4.5 MPa) to form a crude synthesis gas whose main components are CO and H 2 and whose main components are Inorganic ash.
  • the quenched ash is discharged through the tapping port discharge device, and the cooled and purified raw syngas with water and ash is removed, and the ash residue of the large particles is removed by the coarse slag removing device 51, and is sent to the preliminary cooling device by the air press 52.
  • 31 acts as a cooling substance and a gasifying agent.
  • Part of the high-temperature crude syngas and the high-temperature fly ash are mixed with the cooling substance injected from the preliminary cooling device 31 to cool down, and then enter the cooling reaction section 3, and the carbon which is not completely reacted in the cooling reaction section 3 reacts with the supplemented H2O to further increase the carbon.
  • the conversion rate and temperature are lowered to increase the hydrogen to carbon ratio of the syngas.
  • the crude syngas and fly ash after the reaction continue to ascend, and after quenching, enter the upper cooling and purifying section 4, after cooling and purifying, the fly ash in the crude syngas is removed, and the relatively clean low-temperature crude syngas is sent to the subsequent process.
  • a large-scale carbonaceous material dry powder gasification system is characterized by comprising a carbonaceous material reaction device and a gas return device.
  • the carbonaceous material reaction device comprises a lower cooling purification section 1, a gasification reaction section 2, a temperature reduction reaction section 3, an upper cooling purification section 4, and a casing 6.
  • the lower cooling purification section 1 is disposed at a lower portion of the apparatus, and the inlet is connected to a lower outlet of the gasification reaction section 2, and includes a downflow quenching device 11, a downcomer 12, a lower syngas outlet 13, a riser 14, and a slag pool 15, Crude slag outlet 16 and so on.
  • the gasification reaction section 2 is disposed in the middle and lower part of the apparatus, the gasification reaction section 2 is uniformly distributed with 8 nozzles 21 in the circumferential direction, the nozzle 21 is arranged in 1 layer, and the lower outlet of the gasification reaction section 2 is connected to the lower cooling purification section 1 to be gasified.
  • the upper outlet of the reaction section 2 is connected to the temperature-lowering reaction section 3.
  • the nozzle 21 is arranged such that a reciprocating effect is formed after the reactant discharge port (relative The nozzle centerline is tangent to the same circle).
  • the temperature-lowering reaction section is disposed at the upper middle portion of the device, and the inlet is connected to the upper outlet of the gasification reaction section, and a preliminary cooling device 31 is disposed at the joint, and an appropriate amount of low-temperature crude syngas is sprayed into the crude syngas.
  • cooling and cooling on the other hand, supplementing the reactants, further completing the gasification reaction of carbon in the fly ash in the cooling reaction section, and increasing the hydrogen-carbon ratio of the synthesis gas.
  • the crude syngas after the reaction continues to be sent up through the upper cooling and purifying device 4 to the subsequent process.
  • the upper cooling purification section 4 is disposed at an upper portion of the device, and the inlet is connected to an upper outlet of the temperature-lowering reaction section, and the upward high-temperature crude syngas passes through the ascending quenching device 41, the air guiding baffle 42, the ash pool 47, and the baffle
  • the device 43, the shower device 44, the separating device 45, the upper syngas outlet 46 and the like achieve the purpose of cooling, humidifying, purifying dust and water. .
  • the gas returning device 5 includes a coarse slag removing device 51, a pneumatic press 52, and the like, and an inlet of the coarse slag removing device 51 is connected to the syngas outlet 13 of the lower cooling section 1 through a pipe.
  • the number of air presses 52 is one to many, preferably three.
  • the crude syngas after cooling and purifying in the lower cooling section 1 still entrains some ash with larger particles, and after removing the slag by the coarse slag removing device 51, the crude syngas with entrained water and fine ash is sent to the preliminary cooling device 31 by the air press 52. Acting as a cooling substance for cooling the raw syngas entering the cooling reaction zone and participating in the cooling reaction.

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Abstract

一种含碳物质干粉气化系统及气化方法。所述系统包括含碳物质反应装置和用于将反应装置部分下行经过冷却和初步净化的粗合成气升压后与反应装置上行高温粗合成气掺混降温的气体返回装置。所述方法包括将含碳物质与气化剂在气化反应装置内反应生成粗合成气及灰渣，其中部分高温粗合成气与飞灰、液渣下行，部分高温合成气与飞灰上行；下行的部分高温粗合成气经过冷却降温，初步净化、除渣后，经升压后带水的粗合成气注入系统，与上行的高温粗合成气掺混；其余部分高温合成气与飞灰上行，分别与初步冷却器注入的低温带水合成气掺混降温，选择性地进入降温反应段，降温的或将降温反应后的粗合成气继续上行经过上部冷却段再次降温除灰得到粗合成气。

Description

一种含碳物质反应系统及方法 所属技术领域
本发明涉及一种含碳物质气化系统及方法，尤其是用于单台日处理量在2000吨以上的粉煤加压气化生产合成气的大型系统及方法。
背景技术
现代石油化工企业的发展趋势是大型化，规模化。高压气化装置大型化也是洁净煤气化技术发展的方向，但是现有气化装置都存在一定的问题。
单喷嘴气化炉由于受到输煤的限制在大型化的方向受到一定的制约。
采用了合成气上行流程的多个喷嘴的气化炉，能够进一步大型化，但是由于液渣流动方向与合成气流动方向相反，液渣落入渣池时会产生一定量的温度较低的水蒸气，其与液渣流动方向反向通过出渣口进入炉膛，此过程会降低液渣的温度。当液渣下落不均衡时容易出现液渣还未落入渣池就凝固的现象。由于没有足够的热量融化固渣，固渣往往会越积越厚最终造成出渣口堵塞的问题，引起装置停车。
采用了合成气下行流程的多喷嘴气化炉也能够进一步大型化，但是为了充分利用炉膛空间，往往将喷嘴布置在炉膛上部接近炉顶的位置，反应过程的高温气和液渣会不断冲蚀炉膛顶部，容易引起炉膛顶部超温的现象，成为安全生产的隐患。
发明内容
本发明的一个目的是提供一种大型含碳物质干粉气化系统。本发明的另一个目的是提供一种大型含碳物质干粉气化方法。
一方面，本发明提供了一种含碳物质干粉气化系统，其特征在于，包括含碳物质反应装置和用于将从所述反应装置部分下行、经过冷却和初步净化的粗合成气升压后与从所述反应装置上行的高温粗合成气掺混降温的气体返回装置。
下行的粗合成气主要是防止堵渣，同时经过冷却后的低温带水合成气加压送入初步冷却器充当冷却介质，降低上行粗合成气温度。在本发明中，冷却物质还可以是水、水雾、水+惰性气体(CO2、N2)、水+合成气、合成气。在本发明中，冷却主要是通过与冷却物质换热实现降温。净化主要是通过在重力、惯性力作用下实现气体与颗粒的分离。
降温是指喷入定量冷却物质量使得混合后的气体降低到某一指定温度(比如到900℃)，冷却是指喷入过量的冷却物质，使其充分换热，冷却的降温幅度更大。
净化包括除去合成气中的灰和夹带的液滴，除灰不包括除水。
按照本发明系统的一个具体实施方案，其中含碳物质反应装置包括气化反应段、上出气口和下出气口。
按照本发明系统的一个具体实施方案，其中从下出气口流出的部分或全部粗合成气经过降温和初步净化后通过管道流经气体返回装置升压，与气化反应段流出的上行粗合成气混合。
按照本发明系统的另一个具体实施方案，其中含碳物质反应装置还包括下部冷却净化段，用于冷却、初步净化气化反应段流出的下行高温粗合成气；下部冷却净化段入口与气化反应段的下出口相连，其合成气出口在下部冷却段的中上部。
下部冷却净化段的合成气出口和系统的下出气口可以为一个口。
按照本发明系统的一个具体实施方案，其中下部冷却净化段还包括急冷装置，渣池，粗渣出口。
按照本发明系统的一个具体实施方案，其中气体返回装置包括除粗渣器和气压机，除粗渣器的入口通过管道与下部冷却净化段合成气出口相连，气压机用于提高经过冷却降温的粗合成气压力，使其能够以高于上行气体0.1MPa～6MPa的压力部分或者全部通过初步冷却降温装置注入，或者部分或者全部通过上行急冷装置注入。
此处加压的粗合成气温度较低且夹带一定的水实际上起到了冷却介质的作用，此种方法可以降低能耗，减少水耗。
按照本发明系统的一个具体实施方案，其中气压机数量为1个到10个，优选2～5个。
按照本发明系统的一个具体实施方案，其中含碳物质反应装置还包括降温反应段，其设置在装置的中上部，入口与气化反应段的上出口相连。
按照本发明系统的一个具体实施方案，其中所述降温反应段入口与气化反应段的上出口连接处设置一个初步降温装置，用于将经过气压机升过压的低温带水粗合成气喷入与上行带灰的高温粗合成气掺 混，一方面冷却降温使上行高温粗合成气夹带的飞灰温度降低到t2(灰的软化温度)以下使其失去粘性，另一方面补充反应物，在降温反应段进一步完成飞灰中的碳的气化反应，提高合成气的氢碳比，此处的灰即是飞灰。
下部冷却段冷却净化后的粗合成气通常仍夹带一些颗粒较大的灰渣，经过除粗渣器除渣后由气压机将夹带水和细灰的粗合成气输送至初步降温装置，充当冷却物质，用于冷却进入降温反应段的粗合成气并且参与降温反应。
按照本发明系统的一个具体实施方案，其中含碳物质反应装置还包括上部冷却净化段，当装置带有降温反应段时，其入口与降温反应段的上出口相连；当装置不带有降温反应段时，其入口与气化反应段的上出口相连，并与气体返回装置出口相连。
按照本发明系统的一个具体实施方案，其中所述的上部冷却净化段包括急冷装置，灰水池和合成气出口，其中合成气出口布置在上部冷却段的中上部，可以布置1个或者多个，优选1～3个。合成气在上部冷却净化装置先后通过急冷，一次或多次冷却净化后经过合成气出口送往后续流程。
按照本发明系统的一个具体实施方案，其中气化反应段周向布置(优选均布)多个喷嘴，喷嘴可以布置1层或上下多层，优选1～3层。
另一方面，本发明提供一种大型含碳物质干粉气化方法，其特征在于，包括以下步骤：
将含碳物质与气化剂在气化反应装置内反应，生成主要成分为CO和H2的粗合成气及主要成分为无机物的灰渣；其中部分高温粗合成气与飞灰、液渣下行，部分高温粗合成气气体与飞灰上行；
Ⅰ：下行的部分高温粗合成气与飞灰经过冷却降温，初步净化后送往粗除渣器，经过气压机升压后带水的粗合成气通过初步降温装置或者上行急冷装置注入系统，与上行高温粗合成气掺混；
下行的液渣经过淬冷后排出炉外；
Ⅱ：其余部分高温粗合成气与飞灰上行，分别与初步降温装置注入的低温带水合成气掺混降温到900℃～t2温度之间使飞灰失去粘性，同时确保进入降温反应段的H2O与残碳能够进一步反应，提高碳转化率并提高氢碳比。
降温且反应后的粗合成气继续上行经过上行急冷装置快速降温后进入上部冷却段再次降温除灰得到满足后续流程需要的粗合成气。
在一种具体的大型含碳物质干粉气化方法中，其特点是，包括以下步骤：
将含碳物质与气化剂通过多个喷嘴喷入装置气化反应段，在高温(1200℃～2000℃)高压(0.1MPa～11MPa)环境下快速反应生成主要成分为CO和H2的粗合成气及主要成分为无机物的灰渣；
部分高温粗合成气及大部分灰渣下行进入下部冷却净化段，经过冷却净化后粗合成气经过除渣器除去大颗粒的灰渣后用气压机送往降温反应段，经过淬冷的灰渣经出渣口排出装置，其中所述大部分例如表示超过50％，优选超过55％，优选超过60％，优选超过65％，优选超过 70％，优选超过75％，优选超过80％，优选超过85％等等；
大部分高温粗合成气及高温飞灰上行与冷却物质混合降温后进入降温反应段，此时主要是未完全反应的碳与补充H2O发生反应，进一步提高碳的转化率并降低温度，提高合成气的氢碳比；
反应后的粗合成气及飞灰继续上行，经过急冷后进入上部冷却净化段，经过冷却净化后，除去粗合成气中的飞灰，较为洁净的低温粗合成气送往后续流程。
在本发明中，所谓的快速反应是指在不超过10秒内完成，90％在5秒内完成。
本发明的方法可以在任何合适的系统中进行，优选在本发明的系统中进行。
本发明由于采用了以上的技术方案，其产生的技术效果是明显的：
1、由于增加了气体返回装置，有效提高了热效率，降低装置能耗，同时减少了水的用量，减少了合成气带水带灰，减轻了后续流程的压力。
2、本发明采用了粗合成气上下同时出气的方式，一方面有效避免了上行出气方式的渣口堵渣问题，另一方面也避免了下行出气方式的顶部超温问题；
3、本发明采用了多喷嘴布置，有利于反应充分进行，并有利于装置的大型化；
4、由于增加了降温反应段，有效提高了碳转化率，提高合成气的 氢碳比，同时也提高了气化反应的热效率。
附图说明
下面结合附图和实施例对本发明进一步说明。
图1是本发明的气化方法示意图。
图2是本发明的一种系统示意图。
图中标记含义如下：1.下部冷却净化段；11.下行急冷装置；12.下降管；13.下合成气出口；14.上升管；15.渣水池；16.粗渣出口；2.气化反应段；21.喷嘴；22.气化室；23.气化室水冷壁；3.降温反应段；31.初步降温装置；4.上部冷却净化段；41.上行急冷装置；42.导气折流管；43.折流装置；44.喷淋装置；45.分离装置；46.上合成气出口；47.灰水池；5.气体返回段；51.除粗渣器；52.气压机；6.壳体。
具体实施方式
为了更好地对本方案进行理解，下面通过具体的实施案例并结合附图进行详细地说明：
实施例1
参阅附图1，一种大型含碳物质干粉气化方法，其特点是，包括以下步骤：
将粉煤与氧气通过喷嘴21喷入装置气化反应段2，在高温(1200℃～2000℃)高压(4.5MPa)环境下快速反应生成主要成分为CO和H2的粗合成气及主要成分为无机物的灰渣。
部分高温粗合成气及大部分灰渣下行进入下部冷却净化段1，经 过淬冷的灰渣经出渣口排出装置，冷却净化后的带水带灰的粗合成气，经过除粗渣器51除去大颗粒的灰渣，通过气压机52增压送往初步降温装置31充当冷却物质及气化剂。
部分高温粗合成气及高温飞灰上行与初步降温装置31喷入的冷却物质混合降温后进入降温反应段3，在降温反应段3中未完全反应的碳与补充的H2O发生反应，进一步提高碳的转化率并降低温度，提高合成气的氢碳比。
反应后的粗合成气及飞灰继续上行，经过急冷后进入上部冷却净化段4，经过冷却净化后，除去粗合成气中的飞灰，较为洁净的低温粗合成气送往后续流程。
实施例2
参阅附图2，一种大型含碳物质干粉气化系统，其特点是，包括含碳物质反应装置，气体返回装置。
所述的含碳物质反应装置包括下部冷却净化段1，气化反应段2，降温反应段3，上部冷却净化段4，壳体6。
所述的下部冷却净化段1设置在装置的下部，入口与气化反应段2的下出口相连，包括下行急冷装置11，下降管12，下合成气出口13，上升管14，渣水池15，粗渣出口16等。
所述的气化反应段2设置在装置的中下部，气化反应段2周向均布8个喷嘴21，喷嘴21布置1层，气化反应段2的下出口连接下部冷却净化段1，气化反应段2的上出口连接降温反应段3。
所述的喷嘴21布置应使得反应物喷出口后形成旋切效果(相对 喷嘴中心线与同一个圆相切)。
所述的降温反应段设置3在装置的中上部，入口与气化反应段的上出口相连，在连接处设置一个初步降温装置31，向粗合成气内喷入适量的带水低温粗合成气，一方面冷却降温，另一方面补充反应物，在降温反应段进一步完成飞灰中的碳的气化反应，提高合成气的氢碳比。
反应后的粗合成气继续上行经过上部冷却净化装置4送往后续流程。
所述的上部冷却净化段4设置在装置的上部，入口与降温反应段的上出口相连，上行的高温粗合成气先后经过上行急冷装置41，导气折流管42，灰水池47，折流装置43，喷淋装置44，分离装置45，上合成气出口46等实现冷却、增湿、净化除尘除水的目的。。
所述的气体返回装置5包括除粗渣器51，气压机52等，粗除渣器51的入口通过管道与下部冷却段1的合成气出口13相连。气压机52数量为1个到多个，优选3个。下部冷却段1冷却净化后的粗合成气仍夹带一些颗粒较大的灰渣，经过除粗渣器51除渣后由气压机52将夹带水和细灰的粗合成气输送至初步降温装置31，充当冷却物质，用于冷却进入降温反应段的粗合成气并且参与降温反应。
以上所述的仅是本发明的一些实施方式。对于本领域的普通技术人员来说，在不脱离本发明创造构思的前提下，还可以做出若干变形和改进，这些都属于发明的保护范围。

Claims (13)

  1. 一种含碳物质干粉气化系统，其特征在于，包括含碳物质反应装置和用于将从所述反应装置部分下行、经过冷却和初步净化的粗合成气升压后与从所述反应装置上行的高温粗合成气掺混降温的气体返回装置。
  2. 按照权利要求1的含碳物质干粉气化系统，其中含碳物质反应装置包括气化反应段、上出气口和下出气口。
  3. 按照权利要求2的含碳物质干粉气化系统，其中从下出气口流出的部分或全部粗合成气经过降温和初步净化后通过管道流经气体返回装置升压，与气化反应段流出的上行粗合成气混合。
  4. 按照权利要求1的含碳物质干粉气化系统，其中含碳物质反应装置还包括下部冷却净化段，用于冷却、初步净化气化反应段流出的下行高温粗合成气；下部冷却净化段入口与气化反应段的下出口相连，其合成气出口在下部冷却段的中上部。
  5. 按照权利要求4的含碳物质干粉气化系统，其中下部冷却净化段还包括急冷装置，渣池，粗渣出口。
  6. 按照权利要求1的含碳物质干粉气化系统，其中气体返回装置包括除粗渣器和气压机，除粗渣器的入口通过管道与下部冷却净化段合成气出口相连，气压机用于提高经过冷却降温的粗合成气压力，使其能够以高于上行气体0.1MPa～6MPa的压力部分或者全部通过初步冷却降温装置注入，或者部分或者全部通过上行急冷装置注入。
  7. 按照权利要求6的含碳物质干粉气化系统，其中气压机数量为1 个到10个，优选2～5个。
  8. 按照权利要求1-7任一项的含碳物质干粉气化系统，其中含碳物质反应装置还包括降温反应段，其设置在装置的中上部，入口与气化反应段的上出口相连。
  9. 按照权利要求8的含碳物质干粉气化系统，其中所述降温反应段入口与气化反应段的上出口连接处设置一个初步降温装置，用于将经过气压机升过压的低温带水粗合成气喷入与上行带灰的高温粗合成气掺混，一方面冷却降温使上行高温粗合成气夹带的飞灰温度降低到900℃～t2(灰的软化温度)之间使其失去粘性，另一方面补充反应物，在降温反应段进一步完成飞灰中的碳的气化反应，提高合成气的氢碳比。
  10. 按照权利要求8的含碳物质干粉气化系统，其中含碳物质反应装置还包括上部冷却净化段，其入口可以与降温反应段的上出口相连。
  11. 按照权利要求10的含碳物质干粉气化系统，其中所述的上部冷却净化段包括急冷装置，灰水池和合成气出口，其中合成气出口布置在上部冷却段的中上部，可以布置1个或者多个，优选1～3个。
  12. 按照权利要求2或3的含碳物质干粉气化系统，其中气化反应段周向均布多个喷嘴，喷嘴可以布置1层或上下多层，优选1～3层。
  13. 一种含碳物质干粉气化方法，其特征在于，包括以下步骤：
    将含碳物质与气化剂在气化反应装置内反应，生成主要成分为CO和H2的粗合成气及主要成分为无机物的灰渣；其中部分高温粗合成气与飞灰、液渣下行，部分高温粗合成气气体与飞灰上行；
    Ⅰ：下行的部分高温粗合成气与飞灰经过冷却降温，初步净化后送往粗除渣器，经过气压机升压后带水的粗合成气通过初步冷却器或者上部急冷装置注入系统，与上行高温粗合成气掺混；
    下行的液渣经过淬冷后排出炉外；
    Ⅱ：其余部分高温粗合成气与飞灰上行，分别与初步冷却器注入的低温带水合成气掺混降温到600℃～t2温度以下使飞灰失去粘性，选择性地进入降温反应段；
    优选初步降温的粗合成气在降温反应段中完成部分未反应碳的继续反应，提高碳转化率并提高氢碳比。
    降温的或降温反应后的粗合成气继续上行经过上部冷却段再次降温除灰得到满足后续流程需要的粗合成气。
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EP3075819A1 (en) 2016-10-05
CN104650988A (zh) 2015-05-27
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US9926502B2 (en) 2018-03-27
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US20170037330A1 (en) 2017-02-09
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