• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention relates to a process for producing process carbon (PC) in indirectly heated gasification, wherein carbon particles are fed to a gasification reactor (1), and that in the case of gasification-supplied process gas (P) it is thereby reduced to synthesis gas (S), the synthesis gas (S) being removed from the gasification reactor. (1). The invention also relates to a plant for producing process coal (PC) in indirectly heated gasification. Characteristic of the process according to the present invention is that at the same time as single gasification takes place, a coking of carbon takes place in an internal reactor (4) arranged inside the gasification reactor (1), that the internal reactor (4) is indirectly heated, and that during coking it is produced process coal (PC) in the internal reactor (4). (Fig. 1) Cortus AB Rolf Ljunggren 2008-06-11
    公开号:SE1001004A1
    申请号:SE1001004
    申请日:2010-10-11
    公开日:2012-04-12
    发明作者:Rolf Ljunggren
    申请人:Cortus Ab；
    IPC主号:
    专利说明:

    2 (4) Production of coal by indirect heat gasification With an indirect heat gasification reactor, the problems of purification of the synthesis gas and physically limiting phenomena as above can be handled.
    Simultaneous coking of coal during indirectly heated gasification means that heat for the coking can be obtained from the reactor of the gasification process. A heating reactor designed for the purpose with a separate flow is arranged in the gasification reactor. The carbon heating reactor is heated indirectly by radiation inside the gasification reactor. The coal is fed into the top of this internal heating reactor to be heat treated to a high temperature in the gasification reactor before the now coked coal is fed out to the bottom. During the heat treatment process, the carbon emits flammable gases. Through the reactor, the gases travel upwards and the coal downwards. This countercurrent movement evens out temperature and variations in the composition of the reactor. Heavier components such as aromatics can crack into smaller molecules due to the high temperature in the reactor. The combustible gases from the coking are returned and mixed with the combustion gases emitted by the pyrolysis of the biomass. The entire fuel gas volume can be used for the heating needs of drying, pyrolysis, coking and gasification. If a surplus arises, it can be used to advantage for external energy needs or equivalent.
    Cortus AB Rolf Ljunggren 2008-06-11 3 (4) Production of cow / in the case of indirect heat gasification Brief description A preferred embodiment according to the invention is described below, with reference to the accompanying drawing, in which: Fig. 1 shows a flow chart for a preferred process according to the present invention, said diagram also schematically showing units which form a plant for carrying out the method; Detailed description of a preferred embodiment according to the invention Fig. 1 schematically shows a number of units which form the plant for carrying out the method.
    The lines, pipes, etc. that connect the system's units are not described or shown in detail.
    The pipes, pipes, etc. are suitably designed to fulfill their function, ie. to transport gases and solids between the plant's units. Figure 1 shows an indirectly heated gasification reactor 1 which is normally a ceramic-lined reactor. In the reactor 1, an internal reactor 4 for coking the coal has been introduced. Solid carbon particles C are supplied partly to the internal reactor 4 and partly to the reactor 1 together with the process gas P through an injection nozzle 5. The carbon particles C come from a pyrolysis which preceded the gasification. The size of the carbon particles C is preferably sufficient to be able to be carried by incoming gas stream with process gas P into the reactor 1. The carbon particles are normally larger to the inner reactor 4 than to the outer one (1).
    The process gas P may be steam or recycled and purified exhaust gas A from the combustion stage.
    The coking in the reactor 4 reduces the amount of carbon in this flow while combustible gases are formed.
    The temperature rise of 300 to 700 ° C on the carbon in reactor 4 is expected to reduce the solid carbon content by 10 to 35%.
    If the process gas P is recycled exhaust gas A, it can contain both water vapor (H 2 O) and carbon dioxide (CO 2). The process gas P is preheated by heat extracted from the outgoing synthesis gas S in the heat exchanger 2.
    The reaction that takes place in gasification reactor 1 is when the carbon C injected through the injection nozzle 5 reduces the content of the process gas P (H 2 O and CO 2) to synthesis gas S (H 2 and CO) which consumes the heat supplied to the process by burners Br 1 to Br n.
    Gasification reactor 1 is heated indirectly by burner Br 1 to Br n (where n denotes the number of burners required for the gasification reactor 1). The internal reactor is similarly heated indirectly by Br 1 to Br n. Heat is supplied to the gasification reaction by radiation from Br 1 to Br n where the combustion takes place inside radiation tubes, i.e. separated from the gasification stream. No direct gas exchange takes place in the gasification reactor 1 between Br 1 to Br n and process gas P or its reaction products.
    Burners Br 1 to Br n are supplied with fuel F from preferably a previous pyrolysis step of the carbonaceous material. Oxidizing agent 0 in the form of air, oxygen-enriched air or pure oxygen is added to the combustion. heat exchanger 3 extracts the heat from outgoing exhaust gases A and preheats incoming oxidant O.
    The exhaust gases A go to the flue gas purification where emission requirements for the process are met with cyclones, catalytic purification, filters (electric or textile) and scrub as needed based on the carbonaceous material contained.
    Carbon C comes from an earlier pyrolysis step and contains residues of ash. By controlling the temperature in gasification reactor 1 to either below (or above) the melting temperature of the ash, Cortus AB Rolf Ljunggren 2008-06-11 4 (4) Production of coal by indirect heat gasification it can preferably be removed by a subsequent high temperature cyclone (or in liquid form as slag).
    Outgoing synthesis gas S can be used as energy gas for combustion purposes or as a basis for further processing into liquid fuels (Fischer Tropsch for typical vehicle fuels, methanol production or the like).
    The pressure in the gasification reactor 1 can be controlled from atmospheric pressure to very high pressures (> 10O barg).
    The temperature in the gasification reactor 1 and the internal reactor 4 is controlled to achieve the best yields of synthesis gas S and process carbon PC. A typical value is in the range 750-1300 ° C.
    An alternative embodiment of the indirect heating of the process gas P and the carbon C can be arranged in a pipe system inside a reactor where the combustion takes place in such a reactor and the pipe system in this case becomes the gasification reactor 1 and the internal reactor 4. The embodiment is considered to be a boiler but at much higher temperatures.
    The geometry of the gasification reactor 1 is controlled based on the need for reaction time in the gasification process, which in turn is controlled by the selected temperature. The geometry of the internal reactor 4 is controlled based on the mass flow of carbon to coke and the need for heating and holding time of the carbon to coke at the temperature selected for reactor 1. The geometry can be rotationally symmetrical in tubular form where a very compact gasification process can be achieved to a more voluminous design. similar to a boiler and then without the requirement to be rotationally symmetrical. The size of the reactors can be designed from a small scale to a very large industrial scale.
    The synthesis gas S (H2 and CO) from the gasification reactor 1 will contain up to 60% hydrogen gas and the remainder carbon monoxide, carbon dioxide and methane depending on the composition of the process gas P.
    The thermal efficiency of an indirectly heated gasification reactor with an internal coke coke reactor will be very high and including previous pyrolysis steps and additional drying, up to 80% thermal efficiency can be achieved for such an integrated system.
    Cortus AB Rolf Ljunggren 2008-06-11
    权利要求:
    Claims (10)
    [1]
    A process for producing process coal (PC) in indirectly heated gasification, wherein carbon particles are fed to a gasification reactor (1), and that process gas (P) supplied during the gasification is thereby reduced to synthesis gas (S), the synthesis gas (S) being removed from the gasification reactor ( 1), characterized in that at the same time as a gasification takes place, a coking of carbon takes place in an internal reactor (4) arranged inside the gasification reactor (1), that the internal reactor (4) is indirectly heated, and that during the coking process coal (PC) is produced in the internal reactor (4).
    [2]
    Process according to Claim 1, characterized in that the process gas (P) is preheated, by heat exchange, by the synthesis gas (S).
    [3]
    Process according to Claim 1 or 2, characterized in that the internal reactor (4) is indirectly heated.
    [4]
    4. A method according to any one of the preceding claims, characterized in that during the coking the carbon emits combustible gases which are utilized.
    [5]
    Process according to one of the preceding claims, characterized in that the temperature in the gasification reactor (1) and the internal reactor (4) is in the range 7509 - 13009.
    [6]
    Method according to one of the preceding claims, characterized in that the pressure in the gasification reactor (1) can be controlled from atmospheric pressure to pressures above 100 bar.
    [7]
    A plant for producing process coal (PC) for indirectly heated gasification, the plant comprising a gasification reactor (1), a burner (Br 1-Br n) arranged in the gasification reactor (1) which generates radiant heat and an injection nozzle (5) for supplying carbon particles and process gas to the interior of the gasification reactor (1), characterized in that an inner reactor (4) is arranged in the gasification reactor (1), that the inner reactor (4) is designed so that carbon particles, during coking, pass the inner reactor (1). 4).
    [8]
    Plant according to claim 7, characterized in that the inner reactor (4) has a supply end for carbon particles located outside the gasification reactor (1), and that the inner reactor (4) has an outlet end for the coked coal located outside the gasification reactor (1). ).
    [9]
    Plant according to any one of claims 7 or 8, characterized in that it comprises a first heat exchanger (2) for heating process gas (P) and cooling synthesis gas (S).
    [10]
    Plant according to claim 9, characterized in that it comprises a second heat exchanger (3) which extracts heat from exhaust gases from the combustion in the burners (Br 1-Br n). Cortus AB Rolf Ljunggren 2008-06-11
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    同族专利:
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
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    WO2009060461A2|2007-11-10|2009-05-14|Genova Ltd|Method and apparatus for producing fuel gas from biomass|
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    SE532711C2|2008-06-11|2010-03-23|Cortus Ab|Process and plant for producing synthesis gas|CN104140848B|2014-07-01|2016-03-02|江苏金江生物能源科技有限公司|A kind of primary and secondary rubbish stalk gasifier|
    CN104232170A|2014-09-05|2014-12-24|黄熙瑜|Comprehensive utilization method of biomass energy|
    CN106635174B|2016-12-09|2022-02-18|中国科学院广州能源研究所|Heat accumulating type high-calorific-value synthesis gas gasification device and gasification production method based on same|
    CN109504442A|2018-10-30|2019-03-22|安徽科达洁能股份有限公司|A kind of high heating value combustion gas gas system and its producing gas method|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE1001004A|SE535222C2|2010-10-11|2010-10-11|Production of carbon in indirect heated gasification|SE1001004A| SE535222C2|2010-10-11|2010-10-11|Production of carbon in indirect heated gasification|
    CA2812916A| CA2812916C|2010-10-11|2011-10-10|Method and equipment for producing coke during indirectly heated gasification|
    PT11832826T| PT2627734T|2010-10-11|2011-10-10|Method and equipment for producing coke during indirectly heated gasification|
    EP11832826.9A| EP2627734B1|2010-10-11|2011-10-10|Method and equipment for producing coke during indirectly heated gasification|
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