WO2017196111A2 - Gasification device - Google Patents

Abstract

Provided is a gasification device having a production process improved more efficiently such that a synthetic gas can be produced more easily. The gasification device comprises: a reaction furnace for causing fuel, which comprises a carbon material, to undergo a thermal reaction, thereby generating a synthetic gas comprising hydrogen and carbon monoxide; a fuel injection portion formed on the upper portion of the reaction furnace; a fuel remnant discharge portion formed on the lower portion of the reaction furnace; a gas discharge tube for discharging the synthetic gas to the outside of the reaction furnace; and a first nozzle arranged inside the reaction furnace so as to supply a pyrolysis gas, which comprises moisture, to the reaction furnace.

Description

Gasifier

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.

As environmental issues arise, energy recycling technologies are also developing. The technology of recovering energy by heat-exchanging secondary and tertiary from high-temperature waste gas generated in an engine has been applied, and the technology of charging electrical energy from mechanical movement is also commercialized. A technology for additionally obtaining energy has also been developed and applied to industrial wastes that have been incinerated conventionally.

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.

In other words, the waste gas can be treated through a gasification process to obtain useful renewable energy. However, in order to smoothly proceed with the gasification process, 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. In addition, in order to maintain the reaction conditions inside the apparatus, 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. In addition, in the general gasification process, 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.

(Prior art document)

(Patent literature)

(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.

The technical problem of the present invention is not limited to the above-mentioned problem, and other technical problems not mentioned will be clearly understood by those skilled in the art from the following description.

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.

Is disposed above the first nozzle of the third region, and further comprising a second nozzle for supplying air to the reactor, wherein the high pressure gas may be provided by branching the air supplied to the second nozzle. .

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. A third region to be generated therein, the heat exchange passage, one side of which is in communication with the third region of the reactor, the other side of which is in communication with the gas discharge pipe, between one side and the other side of the third region; 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.

According to the present invention, a reactant for maintaining the reaction conditions can be more efficiently supplied into the apparatus. In particular, it is possible to efficiently supply the reactants in the apparatus by using the circulation structure of the pyrolysis gas. In addition, 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. In addition, 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.

1 is a conceptual diagram of a gasifier according to an embodiment of the present invention.

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.

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.

6 is a perspective view illustrating an example of a third nozzle installed in the reactor of FIG. 2.

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.

Advantages and features of the present invention and methods for achieving them will be apparent with reference to the embodiments described below in detail in conjunction with the accompanying drawings. However, the present invention is not limited to the embodiments disclosed below, but may be implemented in various forms, and only the present embodiments make the disclosure of the present invention complete and the general knowledge in the technical field to which the present invention belongs. It is provided to fully convey the scope of the invention to those skilled in the art, and the invention is only defined by the claims. Like reference numerals refer to like elements throughout.

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.

Hereinafter, a gasifier according to an embodiment of the present invention will be described in detail with reference to FIGS. 1 to 10.

1 is a conceptual diagram of a gasifier according to an embodiment of the present invention.

Referring to FIG. 1, a gasifier 1 according to an embodiment of the present invention 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. In addition, 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).

 In particular, the gasifier 1 according to the embodiment of the present invention 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. . By using this, 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. In addition, 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. In addition, 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.

Hereinafter, the gasification apparatus 1 of this invention which has such a characteristic is demonstrated in detail with reference to each figure. Other features of the present invention that are not mentioned through the following description will be more clearly understood.

As shown in FIG. 1, 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. First, 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. For example, 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.

However, 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. . Hereinafter, with reference to FIGS. 2 to 7 will be described in more detail with respect to the specific structure and reaction process of the reactor for producing synthesis gas.

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, and 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.

Referring to Figure 2, 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. Below, 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.

As shown in FIG. 3, 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. As a reaction for generating the synthesis gas (E) in the reactor 10, the following reaction formula may be considered.

(Scheme 1) C + H ₂ O-> CO + H ₂ , (Scheme 2) C + 2H _2- > CH ₄

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.

Therefore, a substance containing water (water) or oxygen (air) is required as a reaction substance for reacting with the carbon component. 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. In addition, 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.

In addition, 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. As described above, 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. In addition, 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.

As shown in FIG. 2, 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. In particular, a first nozzle 110 for supplying pyrolysis gas containing water to the third region 103 where the gasification process is performed, a second nozzle 120 for supplying air C, and a mixture of hydrogen and oxygen A third nozzle 130 for injecting oxyhydrogen gas, which is a gas, is formed. As described above, 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. 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. Although not shown, 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.

As shown in FIG. 2, 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. Accordingly, 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.

Since 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. In addition, since 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.

In particular, 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. As shown in FIG. 4, the first nozzle 110 is connected to the circulation pipe 140 and an air injection pipe 114 is connected to one side thereof. As shown in FIG. 5, 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. It is formed at the end of the induction path 112 opening the inner circumferential surface and injecting the high-pressure gas into the main flow path 111, and the main flow path 111 between the induction path 112 and the circulation pipe 140. It is formed in a shape including a guide curve 113 that is a curved surface extending toward.

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. In particular, as shown, 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. However, 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.

That is, 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. Through this, 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. By arranging in the third region 103 and connecting to the second region 102 through the circulation tube 140, the pyrolysis gas containing water is circulated effectively in the required place (i.e., the third region) in the reactor 10. It is possible to supply.

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. Alternatively, 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. When using the pyrolysis gas generated in the reactor 10, it is possible to use a separate compressor, etc., and when using a fluid (air) provided to another nozzle may be shared with the compressor connected to the nozzle. will be. In addition, the high-pressure gas may be formed in various ways and injected into the induction furnace 112.

By constructing the first nozzle 110 as described above, 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. By forming the third nozzle 130 in this manner, 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). In addition, if necessary, 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.

Meanwhile, 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.

As shown in FIG. 7, 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.

As in an embodiment of the present invention, 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. Hereinafter, in an embodiment of the present invention, the tourmaline mineral 152 will be described as representing the pyroelectric material. However, in other embodiments, 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.

As described above, 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.

That is, 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. Using this structure, 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. In particular, 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. By using 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. Hereinafter, 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.

First, as shown in FIG. 8, 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. As described above, 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. As a result, the temperature inside the reactor 10 rises and a flame is generated to maintain the temperature of the reactor 10 at an appropriate temperature.

In this state, 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. At this time, as described above, through 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.

At this time, through the first nozzle 110, the second nozzle 120, and the third nozzle 130 disposed in the third region 103, pyrolysis gas (D), air (C), And oxyhydrogen gas (B) is continuously supplied. 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. As a result, reactants (which may include water) for generating the syngas E may be easily generated and supplied in the reactor 10.

In addition, 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. To facilitate the first or second reaction of the gasification process. That is, 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. . As described above, 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.

On the other hand, 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.

That is, 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. In particular, it is possible to decompose the tar component and increase the amount of carbon monoxide by the electrical catalysis as an impurity to increase the purity of the synthesis gas (E) containing hydrogen and carbon monoxide finally discharged through the gas discharge pipe (40), and more. It is possible to produce high quality syngas (E). In this way, the gasification process can be effectively performed using the gasifier 1 of the present invention, and high-quality, high-purity synthetic gas (E) can be easily produced.

Although embodiments of the present invention have been described above with reference to the accompanying drawings, those skilled in the art to which the present invention pertains may implement the present invention in other specific forms without changing the technical spirit or essential features thereof. I can understand that. Therefore, it should be understood that the embodiments described above are exemplary in all respects and not restrictive.

(Explanation of the sign)

1: gasifier 10: reactor

20: fuel input portion 30: fuel residue discharge portion

40: gas discharge pipe 101: first region

102: second region 103: third region

110: first nozzle 111: main euro

112: induction furnace 113: induction surface

114: air injection pipe 120: the second nozzle

130: third nozzle 131: main pipe

132: distribution pipe 133: nozzle

140: circulation tube

150: tourmaline catalyst 151: heat exchange passage

151a: inlet 151b: outlet

152: tourmaline mineral

A: Fuel B: Oxyhydrogen Gas

C: air D: pyrolysis gas containing water

E: Syngas F: Fuel Leftover

Claims (15)

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 And a first nozzle disposed inside the reactor to supply pyrolysis gas containing water to the reactor. The method of claim 1, The reactor, A first zone in which the injected fuel is dried, a second zone in which the dried fuel is carbonized, and a carbon component of the fuel and the supplied reactant are oxidized and reduced by heat to generate a synthesis gas including hydrogen and carbon monoxide. 3 area inside, And the first nozzle is disposed in the third region. The method of claim 2, And 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 method of claim 3, The first nozzle, A main flow passage penetrating from the end of the circulation pipe toward the inside of the reactor; An induction furnace which opens to the inner circumferential surface of the main channel and injects a high pressure gas into the main channel; And an induction curved surface formed at an end of the main flow passage between the induction passage and the circulation pipe and extending toward the circulation pipe. The method of claim 4, wherein The high pressure gas is a gasifier of the high pressure compressed the pyrolysis gas generated in the first region or the second region. The method of claim 4, wherein A second nozzle disposed above the first nozzle in the third region, for supplying air to the reactor; The high pressure gas is a gasifier that is provided by branching the air supplied to the second nozzle. The method of claim 1, And a catalyst unit including a pyroelectric material disposed on a flow path of the syngas between the reactor and the gas discharge pipe and generating a pyroelectric effect. The method of claim 7, wherein The catalyst unit includes 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 for heat exchange, wherein the pyroelectric material is accommodated inside the heat exchange passage. The method of claim 7, wherein The catalyst unit is a gasifier device is a pyroelectric effect is generated by the heat provided from the reactor. The method of claim 8, The reactor, A first region in which the injected fuel is dried, a second region in which the dried fuel is carbonized, and a third region in which the reactants supplied to the reactor and the carbon component of the fuel are oxidized and reduced by heat to generate the synthesis gas Inside, The heat exchange passage, One side is in communication with the third region of the reactor, the other side is in communication with the gas discharge pipe, between one side and the other side is in contact with the third region, surrounds, The pyroelectric material is, A gasifier in contact with said heat exchange passage and surrounding said third region. The method of claim 7, wherein  The pyroelectric material is a gasifier comprising tourmaline mineral. The method of claim 7, wherein Gasification apparatus is formed a plurality of pores between the pyroelectric material. The method of claim 2, A second nozzle disposed above the first nozzle in the third region, for supplying air to the reactor; and And a third nozzle disposed above the second nozzle in the third region and supplying an oxyhydrogen gas, which is a mixed gas of hydrogen and oxygen, to the reactor. The method of claim 13, The reactant includes water, wherein the water is generated and supplied in the reactor by the thermal reaction of the oxyhydrogen gas. The method of claim 13, The oxyhydrogen gas is a gasifier of the hydrogen: oxygen mixing ratio of 2: 1.

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