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WO2017196111A2 - Dispositif de gazéification - Google Patents

Dispositif de gazéification Download PDF

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Publication number
WO2017196111A2
WO2017196111A2 PCT/KR2017/004900 KR2017004900W WO2017196111A2 WO 2017196111 A2 WO2017196111 A2 WO 2017196111A2 KR 2017004900 W KR2017004900 W KR 2017004900W WO 2017196111 A2 WO2017196111 A2 WO 2017196111A2
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WO
WIPO (PCT)
Prior art keywords
reactor
region
nozzle
gas
fuel
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/KR2017/004900
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English (en)
Korean (ko)
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WO2017196111A3 (fr
Inventor
조희강
조민규
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ecotrigen Renewable Power
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Ecotrigen Renewable Power
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from KR1020160058031A external-priority patent/KR101704768B1/ko
Priority claimed from KR1020160058030A external-priority patent/KR101704767B1/ko
Priority claimed from KR1020160058027A external-priority patent/KR101704766B1/ko
Application filed by Ecotrigen Renewable Power filed Critical Ecotrigen Renewable Power
Publication of WO2017196111A2 publication Critical patent/WO2017196111A2/fr
Publication of WO2017196111A3 publication Critical patent/WO2017196111A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • 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
    • C10J3/78—High-pressure apparatus

Definitions

  • the present invention relates to a gasification apparatus for producing a synthesis gas of renewable energy by thermally reacting waste and the like, and more particularly, to a gasification apparatus that more efficiently improves the production process to facilitate the production of syngas.
  • Gasification technology is a technology that treats wastes containing carbon materials through chemical reactions and obtains flammable products (syngas / syngas). Gasification technology uses waste as fuel to thermally react. Gasification process that maintains specific reaction conditions prevents complete combustion of fuel and induces additional chemical reactions. Through this, it is possible to obtain a syngas which is a useful energy source.
  • the waste gas can be treated through a gasification process to obtain useful renewable energy.
  • it is necessary to control and maintain the temperature inside the reactor at a constant temperature. Therefore, there is a problem that it is not easy to control and maintain the conventional reaction temperature.
  • it is necessary to properly supply specific reactants, but there is a problem that the supply of such reactants is not made efficiently and the productivity of the synthesis gas is reduced or the purity is lowered.
  • impurities such as tar generated by thermal reaction are mixed in the synthesis gas, and thus, it is difficult to maintain the purity of the product at an appropriate level.
  • Patent Document 1 Republic of Korea Patent Publication No. 10-2012-0126172, (2012.11.21)
  • the technical problem to be achieved by the present invention is to solve such a problem, to provide a gasification apparatus that improves the production process more efficiently to facilitate the synthesis gas production.
  • a gasifier according to the present invention comprises a reactor for thermally reacting a fuel containing a carbon material to produce a synthesis gas containing hydrogen and carbon monoxide; A fuel input unit formed on the reaction furnace; A fuel waste discharge portion formed in the lower portion of the reactor; A gas discharge pipe discharging the syngas to the outside of the reactor; And a first nozzle disposed inside the reactor to supply pyrolysis gas containing water to the reactor.
  • the reactor includes a first region in which the injected fuel is dried, a second region in which the dried fuel is carbonized, and a carbon component of the fuel and a supplied reactant are oxidized and reduced by thermal reaction to include hydrogen and carbon monoxide.
  • a third region for generating gas may be included therein, and the first nozzle may be disposed in the third region.
  • the apparatus may further include a circulation pipe connecting the first nozzle and the first region or the second region to provide the pyrolysis gas of the first region or the second region to the first nozzle.
  • the first nozzle is a main flow passage penetrating from the end of the circulation pipe toward the inside of the reactor, the induction passage for injecting a high-pressure gas into the main flow passage opening to the inner peripheral surface of the main flow passage, and the induction passage and the circulation It may include an induction curved surface that is formed at the end of the main flow path between the pipe and is curved toward the circulation pipe.
  • the high pressure gas may compress the pyrolysis gas generated in the first region or the second region at a high pressure.
  • the apparatus may further include a catalyst unit disposed on a flow path of the synthesis gas between the reactor and the gas discharge pipe and including a pyroelectric material generating a pyroelectric effect.
  • the catalyst unit may include a heat exchange passage in contact with the reaction furnace in a form surrounding the lower portion of the reaction furnace and in direct contact with the reaction furnace to exchange heat, and the pyroelectric material may be accommodated inside the heat exchange passage.
  • the catalyst unit may generate a pyroelectric effect by heat provided from the reactor.
  • the reactor includes a first zone in which the injected fuel is dried, a second zone in which the dried fuel is carbonized, and a reaction material and a carbon component of the fuel are oxidized and reduced by heat to reduce the synthesis gas.
  • the pyroelectric material may contact the heat exchange passage and surround the third region.
  • the pyroelectric material may include tourmaline mineral.
  • a plurality of pores may be formed between the pyroelectric materials.
  • a second nozzle disposed above the first nozzle in the third zone and supplying air to the reactor, and disposed above the second nozzle in the third zone to mix hydrogen and oxygen in the reactor; It may further include a third nozzle for supplying an oxyhydrogen gas which is a gas.
  • the reactant may include water, and the water may be generated and supplied in the reactor by a thermal reaction of the oxyhydrogen gas.
  • the oxyhydrogen gas may have a 2: 1 mixing ratio of hydrogen: oxygen.
  • a reactant for maintaining the reaction conditions can be more efficiently supplied into the apparatus.
  • the internal temperature of the reactor can be maintained very conveniently and stably at the proper temperature required for the process, and the reaction in the device can be promoted in a simple manner, so that the gasification process proceeds very effectively.
  • the impurities generated during the reaction can be treated very conveniently and effectively to maintain the purity of the synthesis gas at a high level. Therefore, the productivity of the syngas can be increased by using the gasifier of the present invention, and it is possible to produce a higher purity syngas.
  • FIG. 1 is a conceptual diagram of a gasifier according to an embodiment of the present invention.
  • FIG. 2 is a view illustrating in detail the reactor of the gasifier of FIG.
  • FIG. 3 is a schematic diagram of a reaction process performed in the reactor of FIG. 2.
  • FIG. 4 is a perspective view illustrating an example of a first nozzle installed in the reactor of FIG. 2.
  • FIG. 5 is an operation diagram illustrating an internal structure of the first nozzle of FIG. 4 together with a circulation pipe.
  • FIG. 6 is a perspective view illustrating an example of a third nozzle installed in the reactor of FIG. 2.
  • FIG. 7 is an enlarged view of a catalyst unit of the gasifier of FIG. 1.
  • 8 to 10 are operation diagrams sequentially showing the reaction process of the gasifier according to an embodiment of the present invention.
  • the 'pyroelectric effect' in the present specification is an effect that the electric force is formed by spontaneous electrical polarization when the temperature is changed
  • the 'pyroelectric material' refers to a material capable of generating such a pyroelectric effect.
  • the pyroelectric material may include a crystalline material such as, for example, a specific ceramic.
  • FIG. 1 is a conceptual diagram of a gasifier according to an embodiment of the present invention.
  • a gasifier 1 includes a reactor 10 for generating a synthesis gas including hydrogen and carbon monoxide by thermally reacting a fuel including a carbon material, and a reactor ( 10) the fuel input unit 20 formed in the upper portion, the fuel residue discharge portion 30 formed in the lower portion of the reactor 10, the gas discharge pipe 40 for discharging the synthesis gas to the outside of the reactor 10 and the reactor (10)
  • the first nozzle 110 is disposed in the interior and supplies a pyrolysis gas containing water to the reactor 10.
  • the reactor 10 of the gasifier 1 includes a first region (see 101 in FIG. 2) in which the injected fuel (fuel containing carbon material) is dried, and a second region in which the dried fuel is carbonized (FIG. 2). 102) includes a third region (see 103 in FIG. 2) in which the carbon component of the fuel and the supplied reactant are oxidized and reduced by heat to generate a synthesis gas containing hydrogen and carbon monoxide.
  • the one nozzle 110 is disposed in the third region 103 inside the reactor 10.
  • the gasifier 1 connects the first nozzle 110 and the first region 101 or the second region 102 to remove the pyrolysis gas of the first region 101 or the second region 102. It is formed in a structure including a circulation pipe 140 provided to one nozzle (110).
  • the gasifier 1 includes a structure (a first nozzle and a circulation pipe) for circulating and supplying a fluid required for the reaction by connecting different regions inside the reactor 10. .
  • a substance capable of activating a thermal reaction (which may be a pyrolysis gas including water) may be easily provided inside the reactor 10 and the synthesis gas may be efficiently produced.
  • the gasifier 1 according to the present invention has a combustion characteristic including a structure injecting an oxygen gas, which is a mixed gas of hydrogen and oxygen (mixing ratio of hydrogen: oxygen, may be 2: 1) to the reactor 10. And to control the temperature of the reactor 10 can be maintained at an appropriate temperature.
  • the oxyhydrogen gas injected into the reactor 10 not only promotes fluid circulation in the reactor 10 but also generates water by thermal reaction, so that other reactants required for the gasification process may include water. (10) It can be provided very easily inside.
  • the gasifier 1 according to the present invention includes the structure of the catalyst unit 150 which is catalytically reacted with the synthesis gas by a pyroelectric effect, and the like, and uses the compound gas in combination to produce a productivity of the final synthesis gas. It is possible to efficiently produce a higher purity syngas.
  • the gasifier 1 of the present invention includes a structure in which fuel is introduced around the reactor 10, a structure in which fuel is discharged, and a synthesis gas produced in the reactor 10. (10) Includes a structure for discharging to the outside.
  • the overall configuration of the gasifier 1 will be described with reference to FIG. 1, and then the specific structure and reaction process of the reactor 10 will be described in more detail with reference to each drawing.
  • the fuel input unit 20 is formed on the reactor 10.
  • the fuel introduced into the reactor 10 includes a carbonaceous material.
  • the carbon component of the fuel is maintained under appropriate reaction conditions in the reactor 10 and is thermally reacted with the injected reactant (which may include water) to generate flammable syngas.
  • the fuel may utilize various wastes containing carbon materials, and other materials including carbon components may be used as fuel even if the wastes are not wastes.
  • the fuel input unit 20 is formed in various structures in which fuel can be easily introduced into the reactor 10.
  • the fuel input unit 20 may be, for example, an input structure such as a pipe line connected to the reactor 10, a chute, a hopper, etc., and a transfer device (conveyor, etc.) to transfer fuel materials to the input structure. It can be made of). If necessary, the fuel input unit 20 may be configured in various forms.
  • the reactor 10 is connected to the fuel input unit 20 and includes a reaction space capable of conducting a thermal reaction therein. As described above, the reaction space inside the reactor 10 is divided into first, second, and third regions (see 101, 102, and 103 of FIG. 2), and different processes are performed in each region. Inside the reactor 10, a first nozzle 110 for supplying pyrolysis gas containing water to the reactor 10, a second nozzle 120 for supplying air to the reactor 10, and a reactor ( 10) a third nozzle 130 for injecting oxyhydrogen gas, which is a mixed gas of hydrogen and oxygen, is formed. In particular, the first nozzle 110 is connected to the circulation pipe 140 to communicate with another region (first region or second region) of the reactor 10 in which the first nozzle 110 is not disposed. The catalyst unit 150 is formed at one side of the reactor 10 so that the synthesis gas generated in the reactor 10 passes through and reacts with the catalyst. The structure and reaction process of the reactor 10 will be described later in more detail.
  • the fuel residue discharge portion 30 is formed at the bottom of the reactor 10.
  • the reactor 10 is formed in a form in which the width of the bottom portion gradually decreases as shown, and is formed to easily discharge the residue left after the reaction.
  • the fuel dreg discharge part 30 is located at the bottom of the reactor 10 to recover the discharged fuel dregs and discharge them to the outside.
  • the fuel dregs discharge part 30 is formed in various structures that can easily discharge the fuel dregs to the outside.
  • the fuel residue discharge part using various structures such as a conveyor device including a belt or a chain, a screw conveyor including a screw rotating inside the pipeline, or an elevator device or a discharge pipe that can move vertically ( 30) can be configured.
  • Gas discharge pipe 40 is formed on one side of the reactor (10).
  • the gas discharge pipe 40 discharges the synthesis gas generated in the reactor 10 to the outside of the reactor 10.
  • the gas discharge pipe 40 may be directly connected to the reactor 10, but may be connected to the reactor 10 via the catalyst structure that forms a catalyst reaction with the synthesis gas as in the present embodiment. That is, as shown, the catalyst unit 150 is disposed in the syngas flow path between the reactor 10 and the gas discharge pipe 40 so that the syngas is discharged to the gas discharge pipe 40 through the catalyst unit 150. Can be configured.
  • the present invention does not need to be limited in this manner, and the synthesis gas generated in the reactor 10 may be changed depending on the structure of the gasifier 1, the location of the reactor 10, the location of the gasifier 1, and the like. 10) it is possible to form a gas discharge pipe 40 that can be easily discharged to the outside.
  • the rear end of the gas discharge pipe 40 may be further connected to the device for processing or storing the produced syngas. That is, fuel such as a waste containing carbon material may be introduced into the reactor 10, and a thermal reaction may be performed in the reactor 10 to produce a combustible synthetic gas, which is a renewable energy source, to be discharged and stored in the gas discharge pipe 40.
  • fuel such as a waste containing carbon material
  • a thermal reaction may be performed in the reactor 10 to produce a combustible synthetic gas, which is a renewable energy source, to be discharged and stored in the gas discharge pipe 40.
  • FIG. 2 is a view illustrating in detail the reactor of the gasifier of FIG. 1
  • FIG. 3 is a schematic view of a reaction process performed in the reactor of FIG. 2
  • FIG. 4 is a first nozzle installed in the reactor of FIG. 2. It is a perspective view showing an example. 5 is an operation view showing an internal structure of the first nozzle of FIG. 4 together with a circulation pipe
  • FIG. 6 is a perspective view illustrating an example of a third nozzle installed in the reactor of FIG. 1 is an enlarged view of the catalyst unit of the gasifier of FIG. 1.
  • the reactor 10 is formed in a vessel-shaped structure provided with a reaction space therein. At least three regions in which different reaction processes are performed are formed in the reaction space of the reactor 10.
  • the first region 101 in which the fuel containing the carbon material (fuel injected through the fuel input unit) is dried is formed on the uppermost layer, and the second region 102 in which the dried fuel is carbonized is formed thereon.
  • a third region 103 is formed in which the carbon component of the fuel and the supplied reactant are oxidized and reduced by heat to generate a synthesis gas.
  • Syngas is a combustible gas containing hydrogen and carbon monoxide and is discharged through the gas discharge pipe 40 and then used as an energy source in various applications. A closer look at the reaction process follows.
  • the fuel A including the carbon material is first injected and then dried. In the drying process, volatile substances and the like may evaporate and the fuel A may solidify.
  • This fuel A is again carbonized through thermal reaction. That is, the carbide (A) can be oxidized under appropriate reaction conditions (proper temperature composition and supply of reactants) to produce carbide (char).
  • the carbon component of the carbonized fuel (A) is oxidized and reduced with other reactants through a thermal reaction, whereby a flammable syngas (E) containing hydrogen and carbon monoxide can be produced (gasification process).
  • the remaining fuel dregs F are discharged and disposed of.
  • Syngas (E) is produced in large quantities through the thermal reaction of carbon components and moisture, thermal reaction of carbon components and oxygen, and secondary reactions of materials produced primarily by thermal reactions.
  • the following reaction formula may be considered.
  • the carbon component (C) in the above reaction formula is obtained from the above-mentioned carbides (char), and combustible synthesis gas (E) containing hydrogen and carbon monoxide as a main component can be obtained by reacting the carbon component with water vapor or the like in a reducing atmosphere. Since the gasification process is an endothermic reaction that requires heat of reaction, if the reaction temperature is appropriately increased, the reaction rate may be increased, and the conversion rate of converting carbon into reactants such as syngas may be increased. In addition, the gasification process may be accelerated by heat generation due to partial combustion of carbide (char). The carbon component may react with other reactants provided in the reactor 10 to generate a synthesis gas (E), and may contain another combustible material such as methane through a secondary reaction.
  • E combustible synthesis gas
  • the present invention supplies a pyrolysis gas (D) containing a hydrogen gas (B), air (C), and water, a mixed gas of hydrogen and oxygen for this purpose during the reaction process.
  • Oxygen gas (B) of the present invention is a material having a 2: 1 mixture ratio of hydrogen: oxygen, and it is known that oxyhydrogen gas (B) mixed in such a ratio generates a stable flame during combustion and effectively maintains the reaction temperature. . Therefore, it is possible to easily adjust the combustion characteristics in the reactor (see 10 of FIG. 2) with the oxyhydrogen gas (B) and to easily maintain a proper temperature at which the reaction is easy.
  • the oxyhydrogen gas (B) which is a mixed gas of hydrogen and oxygen, easily generates water (moisture) in the combustion process, so that a reactant for generating syngas (E) is easily generated in the reactor 10. And supply is possible.
  • the pyrolysis gas (D) containing water supplied with the air (C) is very easily used to promote the first or second reaction of the above-described gasification process.
  • Pyrolysis gas (D) containing water is recycled to the region (third region) where the gasification process proceeds and reused in another region (first region or second region) in the reactor 10 to improve the reaction efficiency. It can be maximized. That is, it is possible to maximize the production efficiency of the synthesis gas by providing a pyrolysis gas containing water generated in the carbonization zone to the region where the synthesis gas is generated through the circulation path.
  • the present invention provides a pyrolysis gas (D) including oxygen and hydrogen gas (B), air (C), and water, which are a mixture of hydrogen and oxygen, in an organic manner to the reaction process, thereby providing more efficient and effective synthesis gas ( E) can be produced.
  • the synthesis gas (E) may be catalytically reacted while passing through the above-described catalyst unit 150 to increase purity, and at the same time, impurities such as tar may be removed.
  • a first region 101, a second region 102, and a third region 103 are formed in the reactor 10 where such a reaction process proceeds.
  • the catalyst unit 150 is disposed in the syngas flow path between the reactor 10 and the gas discharge pipe 40.
  • a third nozzle 130 for injecting oxyhydrogen gas, which is a gas, is formed.
  • the first nozzle 110 connects the first nozzle 110 and the second region 102 to provide the first nozzle 110 with pyrolysis gas containing water in the second region 102.
  • the circulation pipe (140) It is connected to the circulation pipe (140). That is, the first nozzle 110, the second nozzle 120, and the third nozzle 130 are organically disposed in the third region 103 such that pyrolysis gas, air, and oxyhydrogen gas containing moisture react with each other. ) Is supplied in the optimal path.
  • at least one heating source such as a torch may be installed in at least one of the first region 101, the second region 102, and the third region 103 in the reactor 10.
  • the first nozzle 110 is located below the second nozzle 120, and the third nozzle 130 is located above the second nozzle 120. That is, the second nozzle 120 is disposed above the first nozzle 110 of the third region 103 to supply air to the reactor 10, and the third nozzle 130 is the third region 103. It is disposed above the second nozzle 120 to supply an oxyhydrogen gas, which is a mixed gas of hydrogen and oxygen, to the reactor 10.
  • the first nozzle 110, the second nozzle 120, and the third nozzle 130 are all located in the third region 103, and are sequentially disposed from the bottom of the third region 103 to the top thereof.
  • oxyhydrogen gas which is a mixed gas of hydrogen and oxygen, is injected from the third nozzle 130 to the top of the third region 103, and air is supplied from the second nozzle 120 to the center of the third region 103.
  • the pyrolysis gas containing water is injected from the first nozzle 110 to the lower portion of the third region 103. Since the oxyhydrogen gas can flow from the top of the third region 103 to the second region 102, the second region 102 and the upper portion positioned upward through stable flame composition during combustion by a heating source (torch, etc. described above). The temperature can be effectively maintained up to one region 101.
  • the oxyhydrogen gas injected to the top of the third region 103 generates water (moisture) during combustion, the generated hydrogen is naturally supplied and supplied to the entire third region 103 where gasification proceeds. Accordingly, the reactant (which may include water) is easily filled in the entire third region 103, and the oxidation and reduction reaction (gasification process) between the carbon component and the reactant is performed very effectively.
  • the second nozzle 120 and the first nozzle 110 provide a reactant to the third region 103 by injecting pyrolysis gas containing air and moisture, respectively, the first and second processes of the above-described gasification process. The reaction is accelerated and syngas is easily produced.
  • the third nozzle 130 for supplying the oxyhydrogen gas, the second nozzle 120 for supplying the air, and the first nozzle 110 for supplying the pyrolysis gas containing water are thus disposed in the third region 103. It can be arranged organically to produce syngas very efficiently.
  • the first nozzle 110 is formed in a shape as shown in FIGS. 4 and 5, so that the pyrolysis gas containing water in the second region (see 102 in FIG. 2) is included in the third region (see 103 in FIG. 2). Can be supplied very effectively.
  • the first nozzle 110 is connected to the circulation pipe 140 and an air injection pipe 114 is connected to one side thereof.
  • the first nozzle 110 has a main flow passage 111 penetrating from the end of the circulation pipe 140 toward the inside of the reaction furnace (see 10 in FIG. 2) and the main flow passage 111.
  • the circulation pipe 140 connects the first nozzle 110 and the first region 101 or the second region 102 to produce a pyrolysis gas containing moisture in the first region 101 or the second region 102.
  • the first nozzle 110 is provided.
  • an end portion of the circulation pipe 140 may be connected to the first region 101, through which the pyrolysis is formed in the second region 102 and moves upward to stay in the first region 101. It can be configured to easily inhale the gas.
  • the present invention is not necessarily limited thereto, and the circulation pipe 140 is connected to the first region 101 or the second region 102 as necessary to provide pyrolysis gas of the first region 101 or the second region 102. It may be formed in various forms that can be provided to the first nozzle (110).
  • the guide curve 113 of the first nozzle 110 more effectively induces a fluid flow from the circulation pipe 140 toward the main flow path 111. That is, as shown, when the high pressure gas is injected from the induction path 112, a primary fluid flow is induced along the high pressure gas, and a part of the pyrolysis gas containing water from the circulation pipe 140 toward the main flow path 111 is formed. Is inhaled. At this time, the pyrolysis gas containing the sucked water flows along the guide curve 113 at the end of the main flow path 111 by viscosity, and flows in a state in which it is in close contact with the inner circumferential surface of the main flow path 111. Create (Coanda effect). As a result, the suction force of the main flow passage 111 is increased to allow more pyrolysis gas to flow into the main flow passage 111 from the circulation pipe 140.
  • the first nozzle 110 provides an increased suction force inside the circulation tube 140 by using a nozzle structure including the guide curve 113 and sucks a larger amount of pyrolysis gas through the circulation tube 140. can do.
  • the gasification of the pyrolysis gas containing water generated in the first region (see 101 of FIG. 2) where drying proceeds or the second region (see 102 of FIG. 2) where carbonization proceeds is performed through the circulation pipe 140.
  • It can be supplied very efficiently by circulating to the third region (see 103 in FIG. 2) which is advanced.
  • the structure of the first nozzle 110 is a structure capable of suctioning the entire main flow path 111 even with a relatively low fluid pressure by using the fluid flow of the guide curve 113.
  • the high pressure gas injected through the induction furnace 112 may compress the pyrolysis gas generated in the first region 101 or the second region 102 to a high pressure.
  • the air supplied to the second nozzle 120 disposed above the first nozzle 110 to supply air to the reactor 10 may be provided by branching. That is, various types of gas generated or supplied in the reactor 10 may be utilized as a high pressure gas that is initially supplied to provide suction power to the main flow passage 111.
  • the high-pressure gas may be formed in various ways and injected into the induction furnace 112.
  • the pyrolysis gas containing water may be more efficiently supplied into the reactor 10 as shown in FIG. 2, and the thermal reaction may be activated.
  • the second nozzle 120 and the third nozzle 130 may be formed in the form of a general nozzle capable of fluid injection, but may be applied to the structure of the illustrated first nozzle 110 as necessary.
  • Each of the first nozzle 110, the second nozzle 120, and the third nozzle 130 has a suitable shape for circulating and supplying pyrolysis gas containing water, for easily injecting air, or for injecting oxyhydrogen gas. It can be formed as.
  • the third nozzle 130 may be formed, for example, as shown in FIG. 6.
  • the third nozzle 130 in a form including a main pipe 131, at least three distribution pipes 132 branched from the main pipe 131, and at least three injection holes 133 formed in each distribution pipe 132. Can be formed.
  • the injection port 133 can be maintained upward and the oxyhydrogen gas can be easily injected into the uppermost portion of the third region (see 103 in FIG. 2).
  • the main pipe 131 may be partitioned and oxygen and hydrogen may be divided and injected into each injection hole 133 to implement a nozzle structure in which the ratio of oxyhydrogen gas injected through the injection hole 133 is maintained at 2: 1. It is also possible. However, since this is only one example, it is not necessary to limit the formation method of the third nozzle 130 in this manner.
  • the catalyst unit 150 is formed at one side of the reactor 10 as shown in FIGS. 2 and 7.
  • the catalyst unit 150 has a pyroelectric effect caused by heat (see G in FIG. 7) provided from the reactor 10, and is formed such that at least a portion thereof is in contact with the reactor 10 to receive heat.
  • the catalyst unit 150 includes a heat exchange passage 151 contacting the reactor 10 in a form surrounding the lower portion of the reactor 10 and directly contacting the reactor 10 to exchange heat.
  • the pyroelectric material may be accommodated inside.
  • one side of the catalyst unit 150 communicates with the third region 103 of the reactor 10, the other side communicates with the gas discharge pipe 40, and a third side between the one side and the other side.
  • the heat exchange passage 151 is in contact with and surrounds the region 103, and the pyroelectric material is formed to contact the heat exchange passage 151 and surround the third region 103.
  • the pyroelectric material is crushed and accommodated inside the catalyst unit 150 (that is, the inside of the heat exchange passage), and a plurality of pores are formed between the pyroelectric materials so that the syngas can easily flow.
  • the pores may be due to irregular gaps between the crushed pyroelectric materials or may be formed on the pyroelectric materials themselves.
  • the pyroelectric material may include tourmaline mineral 152 and the tourmaline mineral 152 may be accommodated in the heat exchange passage 151 to generate a pyroelectric effect.
  • the tourmaline mineral 152 will be described as representing the pyroelectric material.
  • the pyroelectric material may include a material other than tourmaline mineral 152.
  • the pyroelectric material may be disposed in contact with the heat exchange passage 151 to surround the third region 103 to increase the thermal efficiency and to more efficiently catalyze the reaction.
  • the catalyst unit 150 is disposed in the syngas flow path between the reactor 10 and the gas discharge pipe 40 to catalytically react with the syngas by a pyroelectric effect.
  • Pyroelectric effect refers to the effect that a specific material provides electric power by spontaneous electric polarization caused by temperature change.
  • the catalyst unit 150 is, for example, one side is in communication with the third region 103 of the reactor 10, the other side is in communication with the gas discharge pipe 40 and at least a portion between one side and the other side ( 10) may include a heat exchange passage 151 in contact with the circumference to exchange heat, and a tourmaline mineral 152 accommodated in the heat exchange passage 151.
  • the heat exchange passage 151 is formed in a shape surrounding the lower portion of the reactor 10 as shown, it can be easily heat exchanged with the reactor (10).
  • the heat exchange passage 151 may be formed in a shape surrounding the lower portion of the reactor 10 as shown in order to be in contact with the reactor 10 and facilitate the heat (G) of the reactor 10 through the contact surface. Can be provided. Accordingly, when the temperature inside the heat exchange passage 151 rises, an electric force is provided by the pyroelectric effect of the tourmaline mineral 152, and the synthesis gas E is electrically catalyzed.
  • the heat exchange passage 151 may have one side connected to the inlet 151a formed under the reactor 10 and the other side connected to the outlet 151b facing the gas discharge pipe 40.
  • the heat exchange passage 151 is configured to be in direct contact with the reactor 10 as shown, it is possible for a very efficient heat exchange. Since a fireproof material or the like is attached to the circumference of the reaction furnace 10, it is possible to hinder the propagation of heat.
  • the heat transfer blocker such as the fireproof material is removed between the heat exchange passage 151 and the reaction furnace 10 of the present invention. Therefore, the heat exchange passage 151 may be in direct contact with the reactor 10 so that heat exchange is possible, and the heat exchange passage 151 easily absorbs heat from the reactor 10 and heats very efficiently. Through this structure, the pyroelectric effect can be easily induced and the syngas can be catalyzed.
  • the catalyst unit in a form that can easily pass the synthesis gas (E) between the reactor (10) and the gas discharge pipe (40) in contact with the reactor (10) to easily propagate heat (G) into the interior.
  • 150 is configured.
  • the pyroelectric effect of the tourmaline mineral 152 may be induced, and the synthesis gas may be electrically catalyzed to remove impurities mixed in the synthesis gas and increase the concentration of the active ingredient.
  • the catalytic reaction proceeds by electric force without a separate chemical reaction, and it is possible to raise the purity of the synthesis gas (E) very efficiently without generating additional impurities.
  • a detailed manufacturing process of the synthesis gas including the catalytic action of the catalyst unit 150 will be described in more detail later.
  • the tourmaline mineral 152 is accommodated in the heat exchange passage 151 as described above.
  • the heat exchange passage 151 is formed to surround the reactor 10, one side of which is connected to the inlet 151a formed at the bottom of the reactor 10, and the other side of the heat exchange passage 151 faces the gas discharge pipe 40. It can be connected to form a flow path of syngas.
  • the tourmaline mineral 152 contained in the heat exchange passage 151 is heated by the heat energy absorbed from the reactor 10 to provide electric power by the pyroelectric effect.
  • the synthesis gas passing through the heat exchange passage 151 may be partially decomposed or the tar component may be decomposed in the inside by the electrocatalytic action of the tourmaline mineral 152 by the electric force. Accordingly, the amount of hydrogen may be increased or the amount of carbon monoxide may be increased to increase the purity of hydrogen, and the synthesis gas including carbon monoxide.
  • the nozzle structure is disposed inside the reactor 10 and organically supplies the pyrolysis gas, air, and oxyhydrogen gas containing moisture to the reactor 10, between the reactor 10 and the gas discharge pipe 40.
  • a characteristic configuration such as the catalyst unit 150 is disposed in the synthesis gas flow path of the electric catalytic action, it is possible to more effectively proceed the thermal reaction process of the fuel including gasification process and to easily produce the synthesis gas.
  • a reaction process of producing a synthesis gas will be described in more detail with reference to FIGS. 8 to 10.
  • 8 to 10 are operation diagrams sequentially showing the reaction process of the gasifier according to an embodiment of the present invention.
  • fuel A is introduced into the reactor 10.
  • the fuel A may be automatically introduced into the reactor 10 through the fuel input unit 20 formed on the reactor 10.
  • the fuel (A) may utilize various wastes including carbon materials, and other materials including carbon components may be used as fuel (A) even if the wastes are not wastes.
  • Oxygen hydrogen gas B which is a mixed gas of hydrogen and oxygen, is provided through the third nozzle 130 and air C is provided through the second nozzle 120 to be burned by a heating source. do.
  • the temperature inside the reactor 10 rises and a flame is generated to maintain the temperature of the reactor 10 at an appropriate temperature.
  • the fuel A injected into the reactor 10 is dried while passing through the first region 101 and carbonized while passing through the second region 102. That is, as described above, in the drying process, volatiles and the like evaporate, the fuel A solidifies, and oxidizes again through thermal reaction to generate carbides.
  • the stable flame composition of the oxyhydrogen gas B supplied from the third nozzle 130 to the second region 102 and the first region 101 located above the third nozzle 130 effectively. Temperature can be maintained.
  • the carbonized fuel passes through the third region 103 and is oxidized and reduced with other reactants by heat. That is, the carbon component of the carbonized fuel reacts with other reactants including water, oxygen, and the like to produce flammable synthesis gas (E) containing hydrogen and carbon monoxide. Syngas (E) is produced in large quantities through the thermal reaction of carbon components and moisture, thermal reaction of carbon components and oxygen, and secondary reactions of materials produced primarily by thermal reactions.
  • the upper portion of the third region 103 may be divided into an oxidation region in which oxidation proceeds, and the lower portion may be divided into a reduction region in which reduction proceeds. However, in some cases, the oxidation and reduction may proceed in the entire third region 103.
  • Oxyhydrogen gas (B) which is a mixed gas of hydrogen and oxygen injected from the third nozzle 130, is known to generate a stable flame in the combustion process and effectively maintain the reaction temperature, and also easily removes water (moisture) during the combustion process.
  • reactants which may include water
  • for generating the syngas E may be easily generated and supplied in the reactor 10.
  • the first nozzle 110 sucks the pyrolysis gas containing water from the first region 101 or the second region 102 through the circulation pipe 140 and moves to the third region 103.
  • the reaction efficiency can be maximized by circulating and reusing the pyrolysis gas D including water generated in the second region 102 in the reactor 10 to the third region 103 where the gasification process is performed.
  • the present invention provides a pyrolysis gas (D) including oxygen and hydrogen gas (B), air (C), and water, which are a mixture of hydrogen and oxygen, in an organic manner to the reaction process, thereby providing more efficient and effective synthesis gas ( E) can be produced.
  • the remaining fuel dregs F are discharged by the fuel dregs discharge unit 30 and are easily processed.
  • the synthesis gas (E) thus produced is catalytically reacted while passing through the catalyst unit 150 again as shown in FIG. 10, thereby increasing purity and removing impurities such as tar. That is, the syngas E generated in the third region 103 moves to the heat exchange passage 151 through the inlet 151a formed under the reactor 10 and is heated tourmaline mineral inside the heat exchange passage 151. After the catalytic reaction by the pyroelectric effect of 152, it is discharged to the gas discharge pipe 40 through the outlet 151b. As described above, the catalytic reaction is an electrocatalytic reaction by electric force, which causes a part of the water molecules contained in the syngas (E) to flow or decomposes a tar component.
  • the synthesis gas (E) increases the amount of hydrogen or the amount of carbon monoxide by the electrocatalytic effect of the pyroelectric effect while passing through the catalyst unit 150.
  • Fuel B Oxyhydrogen Gas

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Industrial Gases (AREA)

Abstract

La présente invention concerne un dispositif de gazéification qui possède un procédé de production amélioré de manière plus efficace de telle sorte qu'un gaz de synthèse puisse être produit plus facilement. Le dispositif de gazéification comprend : un four de réaction conçu pour faire en sorte qu'un combustible, qui comprend du carbone, subisse une réaction thermique, pour ainsi générer un gaz de synthèse qui comprend de l'hydrogène et du monoxyde de carbone ; une partie d'injection de combustible formée sur la partie supérieure du four de réaction ; une partie d'évacuation de résidu de combustible formée sur la partie inférieure du four de réaction ; un tube d'évacuation de gaz pour évacuer le gaz de synthèse vers l'extérieur du four de réaction ; et une première buse agencée à l'intérieur du four de réaction afin de fournir un gaz de pyrolyse, qui comprend de l'humidité, au four de réaction.
PCT/KR2017/004900 2016-05-12 2017-05-11 Dispositif de gazéification Ceased WO2017196111A2 (fr)

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
KR10-2016-0058031 2016-05-12
KR1020160058031A KR101704768B1 (ko) 2016-05-12 2016-05-12 초전효과를 이용하는 가스화장치
KR1020160058030A KR101704767B1 (ko) 2016-05-12 2016-05-12 열분해가스 순환구조를 갖는 가스화장치
KR10-2016-0058027 2016-05-12
KR1020160058027A KR101704766B1 (ko) 2016-05-12 2016-05-12 가스화 장치
KR10-2016-0058030 2016-05-12

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WO2017196111A2 true WO2017196111A2 (fr) 2017-11-16
WO2017196111A3 WO2017196111A3 (fr) 2018-08-09

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JP2004155879A (ja) * 2002-11-06 2004-06-03 Mitsubishi Heavy Ind Ltd 発電装置を備えたガス化溶融システム
JP2004188397A (ja) * 2002-12-13 2004-07-08 Izumi Tile Carpet Kk 複合超微粒子触媒と、それを含有する組成物と、それらを加えた材料
JP2006002746A (ja) * 2004-06-18 2006-01-05 Obara Yaichi バイオマスの乾留ガス化燃焼熱変換発電装置
KR101103594B1 (ko) * 2009-08-07 2012-01-10 한국에너지기술연구원 가스화 합성가스를 이용하는 다단 유동층 수성가스 반응장치 및 이를 이용한 수소생산방법
KR101479906B1 (ko) * 2014-07-07 2015-01-08 삼양에코너지 주식회사 바이오매스를 이용한 반탄화 연료생산장치 및 이를 이용하여 반탄화 연료를 생산하는 방법

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