KR101704768B1 - Gasifier using pyroelectric effect - Google Patents

Abstract

Provided is a gasification device using a pyroelectric effect. The gasification device using a pyroelectric effect comprises: a reaction furnace producing synthetic gas containing hydrogen and carbon monoxide by carrying out a thermal reaction using carbonic material-containing fuel; a fuel insertion part formed on an upper portion of the reaction furnace; a fuel residue release part formed on a lower portion of the reaction furnace; a gas release pipe releasing the synthetic gas to the outside of the reaction furnace; and a catalyst part disposed on a synthetic gas flowing path between the reaction furnace and the gas release pipe, and including a pyroelectric material capable of creating a pyroelectric effect.

Description

[0001] Gasifier using pyroelectric effect [0002]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gasification apparatus for producing syngas which is a renewable energy by thermally reacting waste or the like and more particularly to a gasification apparatus using a pyroelectric effect, .

Energy recycling technology is also evolving as environmental problems are emerging. A technique of recovering energy by heat exchange from a high temperature waste gas generated in an engine is applied, and a technique of charging electric energy from mechanical movement is also being commercialized. Techniques have been developed and applied to obtain additional energy for industrial wastes, which have been burned as before.

Gasification technology is a technology that treats waste containing carbon materials through chemical reaction and obtains flammable products (syngas / syngas). Gasification technology is a technique of heat-reacting by using waste materials as fuel, and it prevents gasification of fuel completely and induces additional chemical reaction through gasification process which maintains specific reaction conditions. This gives us a useful syngas for energy.

That is, the waste can be treated through the gasification process to obtain a useful renewable energy. However, in the general gasification process, impurities such as tar generated by the thermal reaction are mixed with the syngas, which makes it difficult to maintain the purity of the product at an appropriate level. Further, in order to proceed the gasification process smoothly, it is necessary to adjust and maintain the temperature inside the reaction apparatus at a constant temperature, which makes it difficult to control and maintain the conventional reaction temperature. Further, it is necessary to supply a specific reaction material appropriately in order to maintain the reaction conditions inside the apparatus, but the supply of such reaction materials can not be efficiently provided, and the productivity of the synthesis gas is decreased.

Korean Patent Laid-Open Publication No. 10-2012-0126172, (2012.11.21)

Disclosure of Invention Technical Problem [8] Accordingly, the present invention has been made to solve the above-mentioned problems occurring in the prior art, and it is an object of the present invention to provide a gasification apparatus using a pyroelectric effect that improves process efficiency by treating impurities and the like using a pyroelectric effect.

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

The gasification apparatus using the pyroelectric effect according to the present invention comprises a reaction furnace for producing a synthesis gas containing hydrogen and carbon monoxide by thermally reacting a fuel containing a carbon material; A fuel injector formed on the reactor; A fuel residue discharging portion formed at a lower portion of the reactor; A gas discharge pipe for discharging the syngas to the outside of the reactor; And a catalyst part disposed on the flow path of the syngas between the reaction furnace and the gas discharge pipe and including a pyroelectric effect to generate a pyroelectric effect.

The catalytic unit may generate a pyroelectric effect by heat provided from the reactor.

At least a part of the catalyst part may be in contact with the reaction furnace to receive heat.

The reaction furnace is characterized in that the first region where the injected fuel is dried, the second region where the dried fuel is carbonized, and the carbon material of the reaction material and the fuel supplied to the reactor are oxidized and reduced by heat, And the catalytic portion is communicated with the third region of the reaction furnace on the one side and the gas discharge pipe on the other side with the third region to be generated, Wherein the pyroelectric material is in contact with the heat exchange passage and surrounds the third region.

A first nozzle disposed in the third region inside the reaction furnace to supply an oxyhydrogen gas, which is a mixed gas of hydrogen and oxygen, to the reaction furnace; a second nozzle disposed below the first nozzle in the third region, And a third nozzle disposed below the second nozzle of the third region for supplying pyrolysis gas containing moisture generated in the first region or the second region, .

The pyroelectric material may comprise tourmaline mineral.

The pyroelectric material is crushed and accommodated in the catalyst part, and a plurality of pores may be formed between the pyroelectric materials.

According to the present invention, the purity of the synthesis gas can be maintained at a high level by treating the impurities produced during the reaction very conveniently and effectively. In addition, the internal temperature of the reaction apparatus can be kept very conveniently and stably at an appropriate temperature required for the process, and the reaction material for maintaining the reaction conditions can be supplied to the inside of the apparatus more efficiently, and the gasification process proceeds very effectively. Therefore, the productivity of the synthesis gas can be increased and the synthesis gas of higher purity can be produced by using the gasification apparatus utilizing the pyroelectric effect of the present invention.

1 is a conceptual diagram of a gasification apparatus using a pyroelectric effect according to an embodiment of the present invention.
Fig. 2 is a view showing the reactor furnace of the gasification apparatus using the pyroelectric effect of Fig. 1 in more detail.
FIG. 3 is a schematic diagram of a reaction process proceeding inside the reactor of FIG. 2. FIG.
Fig. 4 is an enlarged view of the catalyst part of the gasification apparatus using the pyroelectric effect of Fig. 1; Fig.
FIG. 5 is a perspective view and a cross-sectional view showing an example of a third nozzle provided in the reactor shown in FIG. 2;
6 to 8 are operation diagrams sequentially showing a reaction process of a gasification apparatus using a pyroelectric effect according to an embodiment of the present invention.

BRIEF DESCRIPTION OF THE DRAWINGS The advantages and features of the present invention and methods for achieving them will become apparent with reference to the embodiments described in detail below with reference to the accompanying drawings. The present invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art. Is provided to fully convey the scope of the invention to those skilled in the art, and the present invention is only defined by the claims. Like reference numerals refer to like elements throughout the specification.

The 'pyroelectric effect' in the present specification means an electric force is generated by spontaneous electropolishing when a temperature is changed, and a 'pyroelectric material' means a material capable of generating such a pyroelectric effect. The pyroelectric material may comprise a crystalline material, such as, for example, certain ceramics.

Hereinafter, a gasification apparatus using a pyroelectric effect according to an embodiment of the present invention will be described in detail with reference to FIGS. 1 to 8. FIG.

1 is a conceptual diagram of a gasification apparatus using a pyroelectric effect according to an embodiment of the present invention.

1, a gasification apparatus 1 using a pyroelectric effect according to an embodiment of the present invention includes a reactor 10 for generating a synthesis gas containing hydrogen and carbon monoxide by thermally reacting a fuel containing carbon material, A fuel injection unit 20 formed on the upper part of the reaction furnace 10, a fuel residue exhaust unit 30 formed on the lower part of the reaction furnace 10, a gas discharge pipe 40 for discharging the syngas to the outside of the reaction furnace 10, And a catalyst part 150 disposed on the flow path of the syngas between the reaction furnace 10 and the gas discharge pipe 40 and containing a pyroelectric material to generate a pyroelectric effect. The gasification apparatus (1) using the pyroelectric effect according to the present invention can remove the impurities mixed with the syngas by the catalytic action by the pyroelectric effect and simultaneously increase the effective components (hydrogen, carbon monoxide, etc.). This makes it possible to increase the productivity of syngas and to produce syngas with higher purity.

Further, the gasification apparatus 1 using the pyroelectric effect according to the embodiment of the present invention may further include a step of supplying an oxygen-scavenging gas, which is a mixed gas of hydrogen and oxygen (the ratio of hydrogen: oxygen may be 2: 1) The internal combustion characteristics can be controlled and the temperature of the reactor 10 can be maintained at an appropriate temperature. Further, the reaction efficiency can be greatly increased by connecting the different regions in the reaction furnace 10 to circulate and supply the pyrolysis gas necessary for the reaction. The oxyhydrogen gas injected into the reactor 10 promotes fluid circulation in the reactor 10 and generates water by a thermal reaction so that the reactants (including water) necessary for the gasification process are also introduced into the reactor 10 It can be very easily provided. By using such a structure, it is possible to improve the productivity of the final calculated synthesis gas and to efficiently produce synthesis gas of higher purity.

Hereinafter, the gasification apparatus 1 using the pyroelectric effect of the present invention having these characteristics will be described in more detail with reference to the respective drawings. Other features of the invention that are not mentioned in the following description may be more clearly understood.

As shown in Fig. 1, the gasification apparatus 1 using the pyroelectric effect according to the present invention comprises a structure for injecting fuel around a reactor 10, a structure for discharging fuel debris, a synthesis And a structure for discharging the gas to the outside of the reaction furnace 10. First, the overall structure of the gasification apparatus 1 using the pyroelectric effect will be described with reference to FIG. 1, and then the detailed structure and reaction process of the reactor 10 will be described in detail with reference to the drawings.

A fuel inlet 20 is formed in the upper part of the reactor 10. The fuel injected into the reactor 10 includes a carbonaceous material. The carbon component of the fuel is maintained within the reaction furnace 10 under suitable reaction conditions and is thermally reacted with the reacted reactants (including water) introduced to produce flammable syngas. The fuel can utilize various wastes containing carbon materials, and other materials, including carbon, can be used as fuel even if it is not waste. The fuel injecting section 20 is formed in various structures that can easily inject fuel into the reaction furnace 10. The fuel injecting section 20 may be, for example, a feed structure such as a conduit connected to the reactor 10, a chute, a hopper, etc., and a conveying device ). The fuel injecting unit 20 can be configured in various forms as needed.

The reaction furnace 10 includes a reaction space connected to the fuel inlet 20 and capable of undergoing a thermal reaction therein. The reaction space inside the reaction furnace 10 is divided into a first region where the injected fuel is dried (see 101 in FIG. 2), a second region where the dried fuel is carbonized (see 102 in FIG. 2) And a third region (see 103 in FIG. 2) in which the supplied reactant and the carbon component of the fuel are oxidized and reduced by heat to generate a synthesis gas. In the first, second, and third regions, a different process is performed. A first nozzle 110 injects a mixed gas of hydrogen and oxygen into the reaction furnace 10, and air is supplied to the reaction furnace 10 A third nozzle 130 for supplying a pyrolysis gas containing moisture to the second nozzle 120 and the reaction furnace 10 is formed. The third nozzle 130 is connected to the circulation pipe 140 and communicates with another region where the third nozzle 130 of the reaction furnace 10 is not disposed. The structure and reaction process of the reaction furnace 10 will be described later in more detail.

A fuel waste discharging portion 30 is formed below the reactor 10. As shown in the drawing, the reaction furnace 10 is formed in such a shape that the width of the bottom portion gradually decreases, and the remaining residue after the reaction is easily discharged downward. The fuel residue discharging portion 30 is located below the reactor 10 to recover the discharged fuel residue and discharge it to the outside. The fuel residue discharging portion 30 is formed in various structures that can easily discharge the fuel residue to the outside. For example, various types of structures such as a conveyor apparatus including a belt, a chain, etc., a screw conveyor including a screw rotating in the duct, etc., or an elevator apparatus or a discharge pipe capable of vertical movement, 30).

A gas discharge pipe 40 is formed on one side of the reaction furnace 10. The gas discharge pipe 40 discharges the syngas produced in the reactor 10 to the outside of the reactor 10. The gas discharge pipe 40 is connected to the reactor 10 via a catalyst structure catalyzing a syngas. That is, as shown in the drawing, the catalyst portion 150 may be disposed on the syngas flow path between the reaction furnace 10 and the gas discharge pipe 40 so that the syngas can be discharged through the catalyst portion to the gas discharge pipe 40 have.

The shape of the gas discharge pipe 40 is not limited to the shape shown in the drawings. The synthesis gas produced in the reactor 10 is introduced into the reactor 10 in accordance with the structure of the gasification apparatus 1 utilizing the pyroelectric effect, the position of the reactor 10, the installation place of the gasification apparatus 1 using the pyroelectric effect, It is possible to form the gas discharge pipe 40 which can be easily discharged to the outside. A device for post-treating or storing the produced syngas may further be connected to the downstream end of the gas discharge pipe 40. That is, fuel such as waste containing carbonaceous material is charged into the reaction furnace 10 and is subjected to a thermal reaction in the reactor 10 to produce combustible syngas, which is a renewable energy, to be discharged and stored in the gas discharge pipe 40 . Hereinafter, the specific structure and reaction process of the reactor for producing syngas will be described in more detail with reference to FIGS. 2 to 5. FIG.

FIG. 2 is a view showing the reaction furnace of the gasification apparatus using the pyroelectric effect of FIG. 1 in more detail, FIG. 3 is a schematic diagram of a reaction process proceeding inside the reactor of FIG. 2, Fig. 1 is an enlarged view of a catalyst part of a gasification apparatus to be used; FIG. 5 is a perspective view and a cross-sectional view showing an example of a third nozzle provided in the reactor shown in FIG. 2;

Referring to FIG. 2, the reactor 10 is formed in a container-like structure having a reaction space therein. In the reaction space of the reaction furnace 10, at least three regions where different reaction processes proceed are formed. A first region 101 in which a fuel containing carbon material is dried is formed on the uppermost layer, a second region 102 in which the dried fuel is carbonized is formed, A third region 103 is formed in which the reacted material is oxidized and reduced by heat to generate a synthesis gas. The syngas is discharged through the gas discharge pipe 40 as a combustible gas containing hydrogen and carbon monoxide, and is used as an energy source in various uses. The reaction process is as follows.

As shown in FIG. 3, the fuel (A) containing the carbon material is first subjected to a drying process after being charged. Volatile materials and the like may be evaporated during the drying process and the fuel (A) may be solidified. This fuel (A) is carbonized again through a thermal reaction. That is, it is possible to oxidize the fuel (A) with appropriate reaction conditions (proper temperature composition and supply of reactants) to produce carbide (char). The carbon component of the carbonized fuel A undergoes oxidation and reduction reactions with other reactants through a thermal reaction, through which a combustible syngas (E) containing hydrogen and carbon monoxide can be produced (gasification process). The remaining fuel debris (F) is discharged and processed. Synthesis gas (E) is produced in large quantities through processes such as thermal reaction of carbon component and water, thermal reaction of carbon component and oxygen, and secondary reaction of the primary product by thermal reaction. The following reaction formula can be considered as the reaction for producing the syngas (E) in the reactor (10).

(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 carbide (char), and a combustible synthesis gas (E) containing hydrogen and carbon monoxide as main components can be obtained by reacting the carbon component with steam or the like in a reducing atmosphere. Since the gasification process is an endothermic reaction requiring a heat of reaction, it is possible to increase the reaction rate by appropriately raising the reaction temperature and increase the conversion rate of carbon to the reaction product such as synthesis gas. In addition, the gasification process can be promoted by the heat generated by the partial combustion of the char. The carbon component may react with other reactants provided in the reactor 10 to produce syngas (E), and may contain another combustible material such as methane through a secondary reaction or the like.

Therefore, a substance (air) containing water (moisture) or oxygen is required as a reactant for reacting with the carbon component. To this end, the present invention supplies an oxygen scavenger gas (B), a gas mixture of hydrogen and oxygen, air (C), and a pyrolysis gas (D) containing water during the course of the reaction. It is known that the oxyhydrogen gas (B) of the present invention is a material having a hydrogen: oxygen mixing ratio of 2: 1, and the oxyhydrogen gas (B) mixed at such a ratio produces a stable flame in the combustion process and effectively maintains the reaction temperature . Therefore, it is possible to control the combustion characteristics in the reaction furnace (refer to 10 in FIG. 2) with the hydrogen gas (B) and easily maintain an appropriate temperature at which the reaction is easy. In addition, since the oxyhydrogen gas (B), which is a mixed gas of hydrogen and oxygen, easily generates water (moisture) in the combustion process, a reaction material for generating the synthesis gas (E) And the like.

Further, the pyrolysis gas (D) containing water supplied together with the air (C) can be easily used to promote the primary or secondary reaction of the above-described gasification process. The pyrolysis gas (D) containing water is circulated to another region (the first region or the second region) in the reaction furnace 10 to the region where the gasification process proceeds (the third region) Can be maximized. As described above, the present invention provides the organic gas (B), the air (C), and the pyrolysis gas (D) containing water as a mixed gas of hydrogen and oxygen in an organic manner in a reaction process, E). Also, the syngas (E) is catalytically reacted while passing through the catalyst part (150) to increase the purity and at the same time remove impurities such as tar.

As shown in FIG. 2, a first region 101, a second region 102, and a third region 103 are formed in the reaction furnace 10. The catalyst portion 150 is disposed in the syngas flow path between the reaction furnace 10 and the gas discharge pipe 40. Particularly, a first nozzle 110 for injecting an oxyhydrogen gas, which is a mixed gas of hydrogen and oxygen, a second nozzle 120 for supplying air (C), and a second nozzle And a third nozzle 130 for supplying a pyrolysis gas containing the pyrolysis gas. The third nozzle 130 is connected to the circulation pipe 140 connecting the third nozzle 130 and the second region 102 to contain moisture generated in the first region 101 or the second region 102 To the third region (103). That is, the first nozzle 110, the second nozzle 120, and the third nozzle 130 are disposed in the third region 103 in an organic manner so that the thermal decomposition gas containing the above-described oxyhydrogen gas, air, (10). 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 reaction furnace 10.

The first nozzle 110 is positioned above the second nozzle 120 and the third nozzle 130 is positioned below the second nozzle 120 as shown in FIG. That is, the first nozzle 110, the second nozzle 120, and the third nozzle 130 are all located in the third region 103, and are arranged in order from the upper portion to the lower portion of the third region 103. As a result, the oxyhydrogen gas is injected to the uppermost end of the third region 103, air is injected to the central portion of the third region 103, and pyrolysis gas containing water is injected into the lower portion of the third region 103 . Since the oxyhydrogen gas can flow from the uppermost end of the third region 103 to the second region 102, the second region 102 and the second region 102 positioned above the stable region through the stable flame composition upon combustion by the heating source 1 region 101. The temperature of the first region 101 can be effectively maintained.

As described above, since the oxyhydrogen gas injected to the uppermost end of the third region 103 generates water (moisture) during combustion as described above, the generated moisture naturally falls and is supplied to the entire third region 103 where gasification proceeds. Thus, the reaction material (including water) is easily filled in the entire third region 103, and the oxidation reaction and the reduction reaction (gasification process) between the carbon component and the reaction material are very effective. The second nozzle 120 and the third nozzle 130 spray the pyrolysis gas containing air and moisture to provide the reactive material to the third region 103, so that the first and second The reaction is promoted and the synthesis gas is easily produced. A first nozzle 110 for supplying an oxygen scavenger gas, a second nozzle 120 for supplying air, and a pyrolysis gas containing water generated in the first region 101 or the second region 102 The third nozzle 130 can be arranged in the third region 103 in this manner to produce the synthesis gas very efficiently.

The catalyst part 150 is formed such that a pyroelectric effect is generated by the heat G provided from the reaction furnace 10 and at least a part of the catalyst part 150 is in contact with the reaction furnace 10 to receive heat. 4, one side communicates with the third region 103 of the reaction furnace 10, the other side communicates with the gas discharge pipe 40, and the third region 103 between the one side and the other side is surrounded and surrounded by the third region 103 The superconducting material is formed so as to surround the third region 103 while being in contact with the heat exchange passage 151. [ The pyroelectric material may be crushed to be accommodated in the inside of the catalyst section 150 (that is, inside the heat exchange passage), and a plurality of pores may be formed between the pyroelectric materials, so that the syngas can easily flow. The pores may be irregularly spaced between the fractured superconducting materials, or they may be formed in the superconducting material itself.

As in one embodiment of the present invention, the pyroelectric material can include the tourmaline mineral 152 and the tourmaline mineral 152 can be accommodated in the heat exchange passage 151 to generate the pyroelectric effect. Hereinafter, in one embodiment of the present invention, a tourmaline mineral 152 will be described as a typical example of a pyroelectric material. However, in other embodiments, the pyroelectric material may comprise a material other than the tourmaline mineral 152. It is possible to arrange the pyroelectric material in the form of surrounding the third region 103 in contact with the heat exchange passage 151 to enhance the thermal efficiency and catalyze the reaction more efficiently.

The heat exchange passage 151 may be formed in a manner to surround the lower portion of the reaction furnace 10 so as to be in contact with the reaction furnace 10 and facilitate the heat G of the reaction furnace 10 through the contact face Can be provided. Accordingly, when the temperature inside the heat exchange passage 151 rises, electric power is supplied by the pyroelectric effect of the tourmaline mineral 152, and the syngas E is electrically catalytically reacted. The heat exchange passage 151 may be connected to the inlet 151a formed at the lower portion of the reaction furnace 10 and the other end connected to the outlet 151b facing the gas discharge pipe 40.

As shown in the figure, the heat exchange passage 151 is in direct contact with the reaction furnace 10, and highly efficient heat exchange is possible. Since the refractory material or the like is normally attached to the periphery of the reaction furnace 10, heat propagation can be hindered. In the present invention, all of the heat transfer obstruction elements such as the refractory material are removed between the heat exchange passage 151 and the reactor 10. Therefore, the heat exchange passage 151 is in direct contact with the reaction furnace 10 to enable heat exchange, and the heat exchange passage 151 easily absorbs the heat of the reaction furnace 10 and is heated very efficiently. Through this structure, the pyroelectric effect can be easily induced and the syngas can be catalytically reacted.

That is, the synthesis gas E is easily passed between the reaction furnace 10 and the gas exhausting pipe 40, and the catalyst G can be easily transferred to the inside of the reactor 10 in contact with the reaction furnace 10, (150). Using this structure, the pyroelectric effect of the tourmaline mineral 152 can be induced, and the syngas can be electrically catalytically reacted to remove the impurities mixed with the syngas to increase the concentration of the effective ingredient. Particularly, this catalytic reaction proceeds by an electric force without a separate chemical reaction, and it is possible to raise the purity of the synthesis gas E very efficiently without generating any additional impurities. The specific production process of the synthesis gas including the catalytic action of the catalyst section 150 will be described in more detail below.

Meanwhile, the third nozzle 130 may be formed in a shape as shown in FIG. The third nozzle 130 is connected to the circulation pipe 140 as shown in FIG. 5 (a), and the air injection pipe 134 is connected to one side. 5 (b), the third nozzle 130 is connected to the main flow path 131, the main flow path 131, and the main flow path 131, which extend from the end of the circulation pipe 140 toward the inside of the reaction path An induction passage 132 which is open to the inner peripheral surface of the main passage 131 and injects high pressure air into the main passage 131 and a circulation pipe 132 which is formed at the end of the main passage 131 between the induction passage 132 and the circulation pipe 140 140, which is a curved surface that extends toward the curved surface 133. As shown in Fig.

The guide curved surface 133 of the third nozzle 130 more effectively guides the flow of the fluid from the circulation pipe 140 toward the main flow path 131. As shown in the drawing, when high-pressure air is injected in the induction furnace 132, a primary fluid flow is induced along the high-pressure air, and a part of pyrolysis gas containing moisture from the circulation pipe 140 toward the main flow path 131 Inhaled. At this time, the pyrolysis gas that is sucked proceeds along the guide curved surface 133 at the end of the main flow path 131 due to viscosity or the like, and generates a relatively fast fluid flow flowing in close contact with the inner circumferential surface of the main flow path 131 Coanda effect). As a result, the suction force of the main flow path 131 increases, and more pyrolysis gas can flow into the main flow path 131 from the circulation pipe 140.

That is, the third nozzle 130 provides an increased suction force inside the circulation pipe 140 using the nozzle structure including the guide curved surface 133, and more efficiently supplies the pyrolysis gas containing moisture through the circulation pipe 140 . The pyrolysis gas generated from the first region (see 101 in FIG. 1) where progress of drying is progressed or the second region (see 102 of FIG. 2) where carbonization proceeds proceeds through the circulation pipe 140 to the third region Area (see 103 in FIG. 2). That is, the circulation pipe 140 connects the third nozzle 130 with the first region 101 or the second region 102 to prevent thermal decomposition including moisture in the first region 101 or the second region 102 The gas can be supplied to the third nozzle 130. Particularly, as shown in the drawing, the end of the circulation pipe 140 can be connected to the first region 101, through which the pyrolysis formed in the second region 102 and moving upward to stay in the first region 101 The gas can be easily sucked and supplied to the third region 103. However, the method of forming the third nozzle 130 is not limited to this, and if it can be realized in a more efficient form, it is possible to modify it in a form corresponding thereto.

By constructing the third nozzle 130 in this way, pyrolysis gas containing moisture can be more efficiently supplied into the reactor 10 as shown in FIG. The first nozzle 110 and the second nozzle 120 may be formed in the form of a general nozzle capable of fluid injection, but the structure of the third nozzle 130 may be applied as necessary. Each of the first nozzle 110, the second nozzle 120 and the third nozzle 130 can be formed into various suitable forms capable of more efficiently supplying pyrolysis gas containing oxyhydrogen gas, air, and moisture have.

The catalytic part 150 is disposed in the syngas flow path between the reaction furnace 10 and the gas exhausting pipe 40 as described above and is catalytically reacted with the syngas by the pyroelectric effect. The tourmaline mineral 152 accommodated in the heat exchange passage 151 is heated by the heat absorbed from the reactor 10 (see G in FIG. 4) to provide an electric force by the pyroelectric effect. The syngas passing through the heat exchange passage 151 is contained in the interior by the electric catalytic action by the electric power of the tourmaline mineral 152 so that a part of the water molecules flowing together can be decomposed or the tar component can be decomposed. Accordingly, the amount of hydrogen may be increased or the amount of carbon monoxide may be increased, thereby increasing the purity of the synthesis gas containing hydrogen and carbon monoxide.

As described above, the nozzle structure (first, second and third nozzles) arranged in the reaction furnace 10 to organically supply pyrolysis gas containing oxygen gas, air and moisture to the reaction furnace 10, The catalytic unit 150 disposed in the syngas flow path between the furnace 10 and the gas discharge pipe 40 and performing the electrical catalytic action can be used to more effectively control the thermal reaction process of the fuel including the gasification process And the synthesis gas can be easily produced. Hereinafter, the reaction process for producing the syngas will be described in more detail with reference to FIGS. 6 to 8. FIG.

6 to 8 are operation diagrams sequentially showing a reaction process of a gasification apparatus using a pyroelectric effect according to an embodiment of the present invention.

First, as shown in FIG. 6, the fuel A is injected into the reaction furnace 10. The fuel A can be automatically injected into the reactor 10 through the fuel inlet 20 formed on the reactor 10. As described above, the fuel (A) can utilize various wastes containing a carbon material, and a material containing a carbon component can be used as the fuel (A) even if it is not waste. An oxygen gas (B), which is a mixed gas of hydrogen and oxygen, is provided through the first nozzle 110 in the reaction furnace 10 and air C is supplied through the second nozzle 120, do. As a result, the internal temperature of the reaction furnace 10 rises and a flame is generated to maintain the temperature of the reaction furnace 10 at an appropriate temperature.

In this state, the fuel A injected into the reaction furnace 10 is dried while passing through the first region 101, and is carbonized while passing through the second region 102. That is, as described above, volatile substances and the like are evaporated in the drying process, the fuel A is solidified, and the carbon is oxidized through the thermal reaction to generate char. At this time, the second region 102 and the first region 101 located above the first nozzle 110 are effectively supplied through the stable flame composition of the oxyhydrogen gas B supplied from the first nozzle 110 Temperature can be maintained.

The carbonized fuel passes through the third region 103 as shown in FIG. 7, 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 a combustible syngas (E) containing hydrogen and carbon monoxide. Synthesis gas (E) is produced in large quantities through processes such as thermal reaction of carbon component and water, thermal reaction of carbon component and oxygen, and secondary reaction of the primary product by thermal reaction. The upper portion of the third region 103 may be divided into an oxidation region where oxidation proceeds and a lower region where reduction is progressed. In some cases, the oxidation and reduction may proceed throughout the third region 103.

At this time, an oxygen gas (B), air (C), and moisture are contained in the third region 103 through the first nozzle 110, the second nozzle 120 and the third nozzle 130 (D) is supplied. As described above, it is known that the oxyhydrogen gas (B), which is a mixed gas of hydrogen and oxygen, generates a stable flame and effectively maintains the reaction temperature in the combustion process. In addition, since water (moisture) is easily produced in the combustion process, (Including water) for producing the reaction product (E) in the reaction furnace 10 can be easily produced and supplied.

The third nozzle 130 sucks pyrolysis gas containing moisture through the circulation pipe 140 from the first region 101 or the second region 102 and provides the pyrolysis gas to the third region 103, To promote the primary or secondary reaction. That is, the pyrolysis gas D containing moisture generated in the other region of the reactor 10 can be circulated to the third region 103 where the gasification process proceeds, thereby maximizing the reaction efficiency. As described above, the present invention provides the organic gas (B), the air (C), and the pyrolysis gas (D) containing water as a mixed gas of hydrogen and oxygen in an organic manner in a reaction process, E). The remaining fuel debris F is discharged by the fuel residue discharging portion 30 and is easily treated.

Meanwhile, the syngas E thus generated is catalytically reacted while passing through the catalyst unit 150, thereby increasing the purity and simultaneously removing impurities such as tar. That is, the syngas E generated in the third region 103 is transferred to the heat exchange passage 151 through the inlet 151a formed in the lower portion of the reaction furnace 10, and the heated tourmaline mineral After being catalyzed by the pyroelectric effect of the catalyst 152, is discharged to the gas discharge pipe 40 through the discharge port 151b. As described above, the catalytic reaction is an electrical catalytic reaction by the electric force of the pyroelectric effect, thereby causing part of the water molecules flowing in the syngas (E) to be decomposed or the tar component to be decomposed.

That is, the amount of hydrogen increases or the amount of carbon monoxide increases due to the electric catalytic action by the pyroelectric effect while the synthesis gas E passes through the catalyst unit 150. Particularly, it is possible to decompose the tar component and increase the amount of carbon monoxide by the electric catalytic action, which is an impurity, thereby increasing the purity of the synthesized gas (E) containing hydrogen and carbon monoxide finally discharged through the gas discharge pipe 40 It is possible to produce a syngas (E) of good quality. In this way, the gasification process can be effectively carried out by using the gasification apparatus 1 using the pyroelectric effect of the present invention, and the synthesis gas E of high quality and high purity can be easily produced.

While the present invention has been described in connection with what is presently considered to be practical exemplary embodiments, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, You will understand. It is therefore to be understood that the above-described embodiments are illustrative in all aspects and not restrictive.

1: Gasification apparatus using pyroelectric effect 10:
20: fuel injecting section 30: fuel residue exhausting section
40: gas discharge pipe 101: first region
102: second area 103: third area
110: first nozzle 120: second nozzle
130: third nozzle 131: main flow path
132: induction furnace 133: induction curve
134: air inlet tube 140: circulation tube
150: catalyst part 151: heat exchange passage
151a: Inlet port 151b: Outlet port
152: Tourmaline Minerals
A: Fuel B: Hydrogen gas
C: air
D: Pyrolysis gas containing water E: Synthetic gas
F: fuel residue G: heat

Claims (7)

A reactor for thermally reacting a fuel containing a carbon material to produce a synthesis gas containing hydrogen and carbon monoxide;
A fuel injector formed on the reactor;
A fuel residue discharging portion formed at a lower portion of the reactor;
A gas discharge pipe for discharging the syngas to the outside of the reactor; And
And a catalyst part disposed on a flow path of the syngas between the reaction furnace and the gas discharge pipe and including a pyroelectric material to generate a pyroelectric effect,
Wherein the catalytic portion includes a heat exchange passage in contact with the reaction furnace in direct contact with the reaction furnace in such a manner as to surround the lower portion of the reaction furnace and performing heat exchange therewith and utilizing the pyroelectric effect in which the pyroelectric substance is accommodated in the heat exchange passage Gasification device. The method according to claim 1,
Wherein the catalytic portion utilizes a pyroelectric effect in which a pyroelectric effect is generated by heat provided from the reactor. 3. The method of claim 2,
Wherein the catalytic portion utilizes a pyroelectric effect in which at least a portion of the catalytic portion is in contact with the reaction furnace to receive heat. The method of claim 3,
In the reaction furnace,
A first region where the injected fuel is dried, a second region where the dried fuel is carbonized, and
A third region in which a reaction material supplied to the reaction furnace and a carbon component of the fuel are oxidized and reduced by heat to generate the synthesis gas,
The heat-
The first region communicates with the third region of the reaction furnace, the second region communicates with the gas discharge pipe, the one region communicates with the third region,
The above-
And a pyroelectric effect in contact with the heat exchange passage and surrounding the third region. 5. The method of claim 4,
A first nozzle disposed in the third region inside the reaction furnace to supply an oxyhydrogen gas, which is a mixed gas of hydrogen and oxygen, to the reaction furnace,
A second nozzle disposed below the first nozzle in the third region to supply air to the reaction furnace,
And a third nozzle disposed below the second nozzle of the third region for supplying a pyrolysis gas containing moisture generated in the first region or the second region. The method according to claim 1,
Wherein the pyroelectric material utilizes a pyroelectric effect including a tourmaline mineral. The method according to claim 1,
And a pyroelectric effect in which a plurality of pores are formed between the pyroelectric materials.

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