WO2015026023A1

WO2015026023A1 - Gasification reactor using biomass

Info

Publication number: WO2015026023A1
Application number: PCT/KR2014/001057
Authority: WO
Inventors: 김종표; 홍선일; 손진국; 이재구; 홍성구; 김명준; 김의용
Original assignee: 삼양에코너지 주식회사
Priority date: 2013-08-23
Filing date: 2014-02-07
Publication date: 2015-02-26
Also published as: CN104640959B; CN104640959A; KR101452327B1

Abstract

The present invention relates to a gasification reactor using biomass, capable of being selectively operated according to the characteristics and type of an injected biomass, increasing the synthetic gas production, and further improving the efficiency of the energy which can be applied to a gasification step again by collecting the sensible heat of the discharged synthetic gas and raising the temperature of the air supplied as an oxidizing agent.

Description

Gasification Reactor Using Biomass

The present invention relates to a gasification reaction apparatus using biomass, and more particularly, to produce biomass in a solid state as a synthesis gas such as hydrogen, carbon monoxide, and methane in a gaseous state by thermal and chemical energy conversion. The present invention relates to a gasification reaction apparatus using biomass to generate electric power by using a synthesis gas as a heat source of a boiler or a fuel of an internal combustion engine.

In general, gasification is the production of solid materials in the form of syngas, which is a gaseous material by thermal and chemical energy conversion methods, and is mainly applied to coal, waste, woody biomass (rice husk, Corn stalks, sawdust, wood chips).

Here, the gasification method is largely classified into a fixed bed method and a fluidized bed method, and the fixed bed method is subdivided into a bottom-up gasification method, a top-down gasification method, and a countercurrent gasification method, and the fluidized bed method is a circulating fluidized bed gasification method or a bubble bed fluidized bed gasification method. Can be divided.

Among them, the bottom-up gasification method is a method in which a solid raw material is input from the upper side and a gasification oxidant is supplied in a direction opposite to the solid raw material.

That is, the solid material may be divided into a drying zone, a pyrolysis zone, a reduction zone, and an oxidation zone from a top side into which the solid raw material is introduced.

In the bottom-up gasification method, the air as an oxidant is mainly supplied from the lower side to the upper side into which the raw material is input, so that the heat transfer efficiency is good for the solid raw material to be introduced, and the outlet temperature is relatively low, such as 250 to 300 degrees Celsius. Due to its high tar content, it is mainly used as a heat source replacement technology for boilers.

Next, the top-down gasification method is a system in which the input direction of the solid raw material and the input direction of air are parallel.

That is, it is divided into drying zone, pyrolysis zone, pyrolysis zone, combustion zone and reduction zone from the top of which solid raw material is input. It is the same direction as the input direction of the raw material.

In the top-down gasification method, due to insufficient heat transfer between solid fuels from the lower oxidation zone during the drying zone and pyrolysis zone where the synthesis gas is generated, the thermal efficiency is relatively low and only heat transfer by radiant heat results in the discharge of the synthesis gas. The temperature is relatively high at 700 ~ 750 degrees Celsius.

However, since the top-down gasification method has a relatively small amount of tar in the syngas (about 95 to 99% reduction in tar), the syngas generated by the top-down gasification method can be directly injected into a generator of an internal combustion engine and used as fuel. It is enough, and it is a technology that allows cogeneration with heat and electricity.

On the other hand, the countercurrent gasification method can be said to be a mixture of a bottom-up gasification method and a top-down gasification method, and the oxidizing agent is introduced from the side, and the tar decomposition rate in the syngas is lowered, and a low-density solid such as chaff and sawdust is mainly used. It is suitable for gasifying raw materials.

Therefore, in recent years, the development of a gasifier using a top-down gasification method with a relatively small tar content has been made.

However, the gasifier using the top-down gasification method has the same direction of injecting the solid raw material and the air as the oxidizing agent, and as a result, the heat transfer efficiency between the solid raw material and the air decreases, so that the sensible heat temperature of the syngas discharged is relatively high. Same as one.

Therefore, the development of a gasifier that can be widely applied to biomass solid raw materials having various types and properties, as well as using the sensible heat of the relatively high temperature synthesis gas is urgently needed.

The present invention has been invented to improve the above problems, and provides a gasification reaction apparatus using a biomass that can be selectively operated according to the nature and type of the biomass to be introduced and to increase the production of syngas. It is to.

In addition, the present invention is to provide a gasification reaction apparatus using a biomass to increase the energy efficiency by recovering the sensible heat of the syngas discharged to increase the temperature of the air supplied to the oxidant and put it back into the gasification process.

The present invention as a technical idea for solving the above object is to produce a synthesis gas (syngas) from the biomass by introducing a biomass (biomass) and air as an oxidant from the upper side, A reactor in which a drying zone, a pyrolysis zone, a combustion zone, and a reduction zone are sequentially formed from above; A plurality of first air supply assemblies disposed to be spaced apart along the outer surface of the reactor so as to penetrate downward from the upper side of the reactor and extend to the oxidation zone, and supply air for combustion of the biomass to the oxidation zone; Spaced apart along the outer surface of the reactor so as to penetrate downwardly from the top of the reactor to extend to the oxidation zone, and is disposed between the first air supply assembly and a neighboring first air supply assembly, and the combustion of the biomass A plurality of second air supply assemblies for supplying more air to the oxidation zone than the first air supply assembly, and a gas outlet formed at a lower side of the reactor, and the syngas discharged from the reduction zone; And a heat exchange unit for exchanging heat by mutually flowing air supplied from the outside.

According to the present invention having the above configuration, the following effects can be achieved.

First, the present invention has a first and second air supply assembly that can selectively adjust the air supply amount to the oxidation region according to the nature and type of the biomass to be injected, thereby applying a wide range of biomass of various types to high efficiency and high quality Syngas can be produced.

In addition, the present invention has a heat exchange unit that can reuse the high sensible heat of the syngas produced and discharged due to the structural characteristics of the top-down gasification method again to heat the air required for the gasification process, thereby minimizing unnecessary waste of energy and It is possible to improve the production efficiency.

1 is a cross-sectional conceptual view showing the overall configuration of a gasification reaction apparatus using biomass according to an embodiment of the present invention.

Figure 2 is a plan view of the gasification reaction apparatus using a biomass according to an embodiment of the present invention.

3 is a cross-sectional conceptual view showing the overall configuration of a second air supply assembly which is a main part of a gasification reaction apparatus using biomass according to an embodiment of the present invention.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings.

1 is a cross-sectional conceptual view showing the overall configuration of a gasification reaction apparatus using a biomass according to an embodiment of the present invention, Figure 2 is a plan view conceptual diagram of a gasification reaction apparatus using a biomass according to an embodiment of the present invention, 3 is a cross-sectional conceptual view showing the overall configuration of a second air supply assembly which is a main part of a gasification reaction apparatus using biomass according to an embodiment of the present invention.

For reference, a transparent arrow in FIG. 1 indicates a moving direction of the syngas 105 discharged from the reduction region 104, and an arrow indicated by a dashed-dotted line indicates a direction in which ash of the biomass 108 is discharged. Arrows indicated by the dashed-dotted line indicate the moving direction of the coolant flowing into and exiting the cooling jacket 680.

In addition, arrows indicated by solid lines in FIG. 3 indicate movement directions of air introduced by heat exchange from the heat exchange unit 400, and arrows indicated by dashed lines indicate movement directions of air introduced from the outside without heat exchange.

In addition, reference numeral 107 denotes air introduced from the outside without heat exchange, and reference numeral 700 denotes a support frame for supporting the reactor 100.

As shown in the present invention, it can be understood that the first and second

air supply assemblies

200 and 300 and the heat exchange unit 400 are provided in the reactor 100.

The reactor 100 generates biogas 108 and syngas from biomass 108 by injecting biomass 108 and air as an oxidant from the upper side, and the upper side of the inner space in which the biomass 108 is filled. The drying zone 101, the pyrolysis zone 102, the oxidation zone 103, the combustion zone, and the reduction zone 104 are sequentially formed.

The first air supply assembly 200 is spaced apart along the outer surface of the reactor 100 so as to penetrate downward from the upper side of the reactor 100 to extend to the oxidation region 103, and for combustion of the biomass 108. A plurality of things supply air to the oxidation region 103.

The second air supply assembly 300 is disposed to be spaced apart along the outer surface of the reactor 100 so as to penetrate downward from the upper side of the reactor 100 to extend to the oxidation region 103, and the first air supply assembly 200 It is disposed between the adjacent first air supply assembly 200, the plurality of air supply for the combustion of the biomass 108 to the oxidation region 103 more than the first air supply assembly 200.

The arrangement of the first and second

air supply assemblies

200 and 300 can be clearly seen in FIG. 2. Of course, the first and second

air supply assemblies

200 and 300 may be alternately arranged at equal intervals as shown, as well as various modifications and application designs such as asymmetrically disposed on one side. Of course.

The heat exchange unit 400 is provided at the gas outlet 106 formed at the lower side of the reactor 100, and exchanges heat by synthesizing the syngas 105 discharged from the reduction zone 104 and air supplied from the outside. It is to let. Accordingly, the present invention can selectively adjust the air supply amount to the oxidation region 103 according to the nature and type of the biomass 108 introduced by the first and second

air supply assemblies

200 and 300, It can be applied to a wide range of biomass.

In addition, the present invention reuses the high sensible heat of the syngas 105 produced and discharged due to the structural characteristics of the top-down gasification method to heat the air necessary for the gasification process by the heat exchange unit 400 again, thereby minimizing unnecessary waste of energy. It is possible to improve the production efficiency of the syngas 105.

The present invention can be applied to the embodiments as described above, it is also possible to apply the various embodiments as follows.

The reactor 100 is for producing the syngas 105 from the biomass 108 introduced as described above, the reactor upper body 110 and the outer case 120 are largely interconnected, and the inner case 130 is It can be seen that the structure is built in the outer case 120. Prior to the description of each component of the reactor 100, a brief description will be given of the drying zone 101, the pyrolysis zone 102, the oxidation zone 103 and the reduction zone 104 which are sequentially formed from the upper side in the reactor 100. see.

First, in the drying region 101, the moisture content in the biomass 108 introduced into the reactor 100 is controlled by combustion heat transfer. In the pyrolysis zone 102, gaseous conversion materials such as char or tar are extracted from the inside of the biomass 108 introduced into the reactor 100 by combustion heat transfer. In addition, although not specifically illustrated in the oxidation region 103, partial combustion by an ignition burner connected to the reactor 100 occurs.

Air is introduced through the first and second

air supply units

200 and 300, which will be described later, according to types or properties of the biomass 108 introduced to promote partial combustion of the oxidation region 103. In addition, in the reduction region 104, mainly composed of char (char), pyrolysis gas is converted into hydrogen and carbon monoxide while passing through this region.

On the other hand, the reactor upper body 110 is formed in a shape that gradually widens from the upper side, the drying region 101 and the pyrolysis region 102 is formed therein, forming a residence space 511 to temporarily receive the heat-exchanged air The distribution unit 500 is formed in a band shape to surround the outside of the drying area 101 along the upper outer surface. And, the outer case 120 is connected from the lower edge of the reactor upper body 110, the gas outlet 106 is formed on one side. In addition, the inner case 130 is accommodated in the outer case 120, and communicates with the inside of the reactor upper body 110 to form the oxidation region 103 and the reducing region 104 therein. Here, the first air supply assembly 200 and the second air supply assembly 300, which will be described later, are inclined along the upper inner circumferential surface of the inner case 130, respectively.

At this time, between the outer surface of the inner case 130 and the inner surface of the outer case 120 through the bottom surface of the inner case 130, the syngas 105 is discharged from the reduction zone 104 is raised to the gas outlet 106 Guided through, it is preferable that the discharge space 125 is discharged from the reduction zone 104 through the bottom of the inner case 130 is formed. In addition, the discharge space 125 is also connected to the ash discharge unit 600 to be described later. In this case, the reactor upper body 110, the outer case 120 and the inner case 130 is preferably made of a refractory material excellent in heat insulation.

Looking at the reactor upper body 110 in more detail it can be seen that the structure including the first fire-resistant wall layer 111 and the fire wall slope 112.

The first fireproof wall layer 111 is formed to have a constant thickness from the lower portion of the drying region 101 along the inner circumferential surface of the reactor upper body 110.

The fire wall slope 112 is formed to be inclined downward toward the inner case 130 side at the upper end portion of the first fire wall layer 111, and the fire wall slope 112 is introduced into the biomass 108 smoothly to the lower side. It is designed to descend.

In addition, when the inner case 130 is looked at in more detail, it can be seen that the structure includes the shaft diameter portion 132 and the enlarged diameter portion 134.

The shaft diameter portion 132 includes a combustion slope 131 that is formed to be gradually narrowed from the upper side, and the enlarged diameter portion 134 extends from an edge of the lower end of the combustion slope 131 to be gradually widened. Here, the oxidation region 103 is formed above the shaft diameter portion 132 and the enlarged diameter portion 134, and the reduction region 104 is formed below the enlarged diameter portion 134.

The structure of the reactor upper body 110 and the inner case 130 will be described in more detail.

First, reference numerals shown in the lower right of FIG. 1 will be described.

Reference numeral w1 denotes the width or diameter of the lower edge of the fire wall slope 112 at the first width, and reference numeral w2 denotes the width or diameter of the lower edge of the reactor upper body 110 at the second width.

Reference numeral w3 denotes the width or diameter of the lower edge of the combustion slope 131 at the third width, and reference numeral w4 denotes the lower edge of the enlarged diameter portion 134 at the fourth width, that is, the lower edge of the reduction area 104. Represents the width or diameter to be made.

Here, the second width (w2) is preferably formed larger than the first width (w1), which is a structure for the biomass 108 introduced from the reactor upper body 110 to be smoothly introduced without a bridge (bridge) phenomenon Because it is.

In this case, the fourth width w4 is preferably larger than the third width w3 because the ash of the biomass 108 is smoothly discharged from the reduction region 104.

The outer diameter of the shaft diameter portion 132 and the enlarged diameter portion 134 includes a second fireproof wall layer 133.

In addition, the reactor 100 is connected to the upper end of the reactor upper body 110 and at least one or more mounted to each of the hopper 140 and the upper end and the lower end of the hopper 140, which is injected into the biomass 108 is input while rotating Embodiments of the structure further including a torque sensor 150 for detecting a supply amount of the biomass 108 may be applied.

When the torque sensor 150 detects the input of the biomass 108 through the hopper 140, the torque sensor 150 rotates to quantitatively control the input amount of the biomass 108 in real time.

On the other hand, the air is an oxidant introduced to promote partial combustion of the biomass 108 in the oxidation region 103 and through one or all of the first air supply assembly 200 and the second air supply assembly 300. It is injected into the oxidation region 103. In other words, when the injected biomass 108 is a wood-based material, such as rice hulls, corn stalks, sawdust, wood chips, etc., about 20% to 35% of the air supply for the complete combustion of the biomass 108 (0.7) ~ 0.8 Nm 3 / kg) may be injected, so the first air supply assembly 200 to be described later may be used.

In addition, when the injected biomass 108 is carbon intensive such as coal and waste and a high molecular material such as petroleum compound, it may be injected about 30 to 50% more than the air supply amount condition of the biomass 108 which is wood-based. 2 may be used as the air supply assembly 300.

Therefore, the first and second

air supply assemblies

200 and 300 may be applied to various operating methods such as individually or fully operating in view of the above conditions.

Looking at the first air supply assembly 200 in detail, it can be seen that the structure includes a first main pipe 210, the first valve 220 and the air supply pipe 230.

The first main pipe 210 is disposed on an upper outer surface of the reactor 100, ie, the upper part of the reactor 110, and divides the first main pipe 210 to form a retention space 511 in which air heat-exchanged from the heat exchange unit 400 is temporarily received. It is branched from the unit 500 toward the lower side of the reactor 100.

In addition, the first valve 220 opens and closes the flow path in the first main pipe 210, and the air supply pipe 230 extends inclined with respect to the first main pipe 210 to be heat-exchanged in the oxidation region 103. The flow path for injecting air is formed.

In detail, the second air supply assembly 300 may be understood to have a structure including a second main pipe 310, a second valve 320, and first and

second cylinder parts

330 and 340.

The second main pipe 310 is disposed on the upper outer surface of the reactor 100, the reactor from the distribution unit 500 to form a residence space 511 to temporarily receive the air heat exchanged from the heat exchange unit 400 therein ( It is branched toward the lower side of 100). The second valve 320 opens and closes the flow path in the second main pipe 310.

The first cylinder portion 330 communicates with the second main pipe 310 to form a communication space 335 through which the heat-exchanged air passes.

The second cylinder portion 340 is disposed through both ends of the first cylinder portion 330, and the external air supplied from one end portion joins the heat exchanged air passing through the communication space 335 to form a high speed from the other end portion. To be sprayed.

That is, the first and

second cylinders

330 and 340 naturally use the suction pressure formed in the reactor 100 in the gasification process of the biomass 108 to naturally introduce air introduced from the outside into the reactor 100. When sucked in, a pressure difference is generated due to the wall adhesion phenomenon of the fluid, i.e., the flow of flow, and the main classification is attached to the lower pressure side. Air can be injected into the air.

Looking at the first cylinder portion 330 in more detail it can be seen that the structure includes a first cylinder body 331 and the guide 332.

The first cylinder body 331 is a cylindrical member that accommodates one side of the second cylinder portion 340, the guide 332 extends from the end edge of the first cylinder body 331, the second cylinder portion 340. It wraps around the outer circumferential surface, and is a truncated cone-shaped member inclined at an angle with respect to the outer circumferential surface of the second cylinder portion 340.

Therefore, the air heat-exchanged through the heat exchange unit 400 to be described later is guided along the inclined surface inside the guide 332 to the outside from the other end of the second cylinder portion 340 through the inner circumferential surface of the second cylinder portion 340. It is sprayed by joining air.

Looking at the second cylinder portion 340 in more detail it can be seen that the structure includes a second cylinder body 342, a coanda orifice (343) and a venturi nozzle (344).

The second cylinder body 342 is accommodated in the first cylinder portion 330, one end is a cylindrical member exposed to the outside.

The coanda orifice 343 is inclined with respect to the inclined surface of the guide 332 having a truncated conical shape formed at the end edge of the first cylinder portion 330, a plurality of members penetrated along the outer peripheral surface of the other end of the second cylinder body 342 to be.

The venturi nozzle 344 extends gradually larger than the second cylinder body 342 so as to be exposed to the outside of the first cylinder part 330 from the other end of the second cylinder body 342.

The coanda orifice 343 is preferably disposed proximate to the end edge of the guide 332 to promote wall attachment of the fluid to enhance the coanda effect.

On the other hand, the heat exchange unit 400 as described above for the cross-flow flow of the syngas 105 and the air supplied from the outside to exchange heat, the gas conduit 410, the exchange jacket 420 and the air baffle (430, It can be seen that the structure including the air baffle).

The gas conduit 410 is connected to the gas outlet 106 and forms a flow path through which the syngas 105 is discharged.

The exchange jacket 420 is provided with an air inlet port 421 through which air is introduced from the outside at one side, and the heat exchange toward the residence space 511 of the distribution unit 500 disposed at the upper outer surface of the reactor 100 at the other side. An air discharge port 422 is provided to supply the heat exchanged air from the unit 400, and surrounds the entire outer circumferential surface of the gas conduit 410 and forms an exchange space 415 therein.

The air baffle 430 is formed in a spiral shape along the formation direction of the exchange space 415 between the inner circumferential surface of the exchange jacket 420 and the outer circumferential surface of the gas conduit 410. Accordingly, the air introduced through the air inlet port 421 undergoes a sufficient heat exchange with the syngas 105 discharged at a high temperature while causing a retardation flow along the formation direction of the air baffle 430, and then the first air supply assembly ( 100) and the second air supply assembly 200 are supplied to the side.

That is, the heat exchange unit 400 has a gas conduit 410 and the exchange jacket 420 has an exchange space 415 in the form of a double pipe to exchange heat with the synthesis gas 105 in which air introduced from the outside is discharged to a high temperature. It can be said that it is prepared in terms of the use of waste heat recovery through.

In some cases, it is also possible to arrange the application of the water pipe to the heat exchange unit 400 together with the water supply and the modified design to be supplied to the hot water or heating water.

On the other hand, the present invention is disposed on the upper outer surface of the reactor 100, the first air supply assembly 200 and the second air supply assembly while using the air heat exchanged from the heat exchange unit 400 as a heat source of the drying area 101 Embodiments of a structure further including a distribution unit 500 for supplying to 300 may be applied.

The distribution unit 500 may reduce the combustion load of the biomass 108 in the oxidation region 103 by increasing the temperature of the drying region 101 and the pyrolysis region 102 in the reactor 100, and greatly. It can be seen that the structure includes a distribution jacket 510 and a connection pipe 520.

The distribution jacket 510 is formed in a band shape along the upper outer surface of the reactor 100 to form a residence space 511 for temporarily receiving heat-exchanged air.

The connection pipe 520 communicates the air discharge port 422 and the retention space 511 of the heat exchange unit 400 with each other.

Accordingly, the first air supply assembly 200 and the second air supply assembly 300 communicate with the residence space 511 to supply the heat-exchanged air to the oxidation region 103, respectively.

Since the dispensing unit 500 has a direction in which the biomass 108 is injected and a direction in which air is used as an oxidant is the same direction, a structure for increasing the temperature of the drying region 101 and the pyrolysis region 102 is required.

The structure of the distribution unit 500 also serves to accelerate the drying of moisture in the biomass 108 and to mitigate the increase in thermal entropy of the (gasification) process of thermally decomposing the biomass 108.

In addition, the distribution unit 500 is oxidized when the air heat-exchanged and heated through the heat exchange unit 400 is injected into the oxidation region 103 through the first air supply assembly 200 or the second air supply assembly 300. Local combustion of the biomass 108 in the region 103 can be promoted, and productivity of the syngas 105 can be improved.

Therefore, the distribution unit 500 is to play an important role in the gasification reaction apparatus to produce a synthesis gas 105 of 2 to 2.5 Nm 3 per kg of biomass 108 together with the heat exchange unit 400. .

On the other hand, the present invention is disposed on the lower side of the reactor 100, and further comprises a ash discharge unit 600 for discharging the remaining ash from the synthesis gas 105 from the reduction zone 104 to the outside of the reactor 100 It is preferable to include. The re-discharge unit 600 includes a drive motor 610, a thrust bearing 621, a drive shaft 620, a grate assembly, a reclosing tank 640, a discharge screw 650, and a discharge motor ( It can be seen that the structure including a 660 and the discharge induction pipe 670.

The drive motor 610 is disposed on the bottom of the reactor 100 to transfer the driving force to the drive shaft 620 connected to the drive motor 610, the drive shaft 620 is rotatably supported by the thrust bearing 621, It receives the driving force from the drive motor 610 to rotate.

The great assembly 630 is connected to the upper end of the drive shaft 620, is embedded in the lower portion of the reduction zone 104 and rotated at a constant speed while burning the ash of the biomass 108 burned from the reduction zone 104 by a predetermined amount. It is a truncated cone-shaped member in which the disks which formed the some step | paragraph 631 which fall are piled up. Although not particularly illustrated, the great assembly 630 forms a structure in which ash of the biomass 108 may be discharged in a grill or mesh form on the bottom thereof, and interlocks with the drive shaft 620 that rotates intermittently very slowly. Periodically, the ash of the biomass 108 is discharged from the reduction zone 104 by a predetermined amount.

The reclosing tank 640 is provided at the bottom of the reactor 100 to form a space for temporarily receiving the ashes of the biomass 108 that has fallen.

Discharge screw 650 is formed in a spiral shape along the outer circumferential surface of the discharge shaft 651 is formed to be inclined upward from the bottom of the re-receiving tank 640 to rotate in one direction.

The discharge motor 660 is connected to the end of the discharge shaft 651 to transmit a driving force to the discharge shaft 651.

The discharge guide pipe 670 extends from the receptacle tank 640 and includes a discharge screw 650, and has a ash discharge port 671 on which ash is discharged.

Therefore, the ashes of the biomass 108 dropped and accumulated in the reclosing tank 640 are conveyed in one direction by the discharging screw 650 as the discharging shaft 651 also rotates when the discharging motor 660 is operated. It is discharged to the outside through the port 671.

On the other hand, the outer side of the thrust bearing 621 and the drive shaft 620 is further provided with a cooling jacket 680 having a coolant inlet port 681 through which the coolant flows from the outside and a coolant discharge port 682 through which the coolant is discharged. Therefore, heat generation and overheating of the drive shaft 620 and the thrust bearing 621 may be reduced.

As described above, the present invention can selectively operate according to the nature and type of the biomass to be introduced and can increase the amount of syngas produced, as well as the temperature of the air supplied to the oxidant by recovering the sensible heat of the syngas discharged. It can be seen that the basic technical idea is to provide a gasification reaction apparatus using biomass that can increase energy efficiency by increasing the energy efficiency and increasing the energy efficiency.

In addition, within the scope of the basic technical idea of the present invention, a person having ordinary knowledge in the industry may also apply many other modifications and applications, such as being applicable to gasification of other materials such as industrial, household waste or coal.

Claims

The biomass (biomass) and oxidant air is introduced from the upper side

Syngas is produced from odorous mass, and drying zone, pyrolysis zone, combustion zone and reduction zone are formed from the upper side of the internal space filled with the biomass. Two sequentially formed reactors;

Penetrates downwardly from the top of the reactor and leads to the oxidation zone;

A plurality of first air supply assemblies disposed to be spaced apart along the outer surface of the reactor and supplying air for combustion of the biomass to the oxidation zone;

Spaced apart along the outer surface of the reactor so as to penetrate downwardly from the top of the reactor to extend to the oxidation zone, and is disposed between the first air supply assembly and a neighboring first air supply assembly, and the combustion of the biomass A plurality of second air supply assemblies for supplying more air for the oxidizing region than the first air supply assembly; And

A heat exchange unit provided at a gas discharge port formed at a lower side of the reactor, the heat exchange unit configured to cross-flow heat exchange with the syngas discharged from the reduction zone and air supplied from the outside; and using a biomass Gasification reactor.
The method according to claim 1,

Gasification reaction apparatus using the biomass,

And a distribution unit disposed on an upper outer surface of the reactor and supplying the air heat-exchanged from the heat exchange unit to the first air supply assembly and the second air supply assembly while using the heat source of the drying zone. Gasification reaction apparatus using a biomass.
The method according to claim 1,

Wherein the air is introduced into the oxidation zone through one or all of the first air supply assembly and the second air supply assembly.
The method according to claim 1,

The first air supply assembly,

A first main pipe disposed on an upper outer surface of the reactor and branched from a distribution unit to a lower side of the reactor from a distribution unit forming a residence space therein to temporarily receive air exchanged from the heat exchange unit;

A first valve for opening and closing the flow path in the first main pipe;

And an air supply pipe extending inclined with respect to the first main pipe and having a flow path for injecting the heat-exchanged air into the oxidation region.
The method according to claim 1,

The second air supply assembly,

A second main pipe disposed on an upper outer surface of the reactor and branched from a distribution unit to a lower side of the reactor from a distribution unit forming a residence space therein to temporarily receive air exchanged from the heat exchange unit;

A second valve for opening and closing the flow path in the second main pipe;

A first cylinder portion communicating with the second main pipe to form a communication space through which the heat exchanged air passes;

And a second cylinder part disposed through both ends of the first cylinder part, and external air supplied from one end part joins the heat exchanged air that has passed through the communication space and is injected at a high speed from the other end part. Gasification reaction apparatus using a biomass.
The method according to claim 1,

The heat exchange unit,

A gas conduit connected to the gas outlet and forming a flow path through which the syngas is discharged;

One side is provided with an air inlet port through which air is introduced from the outside, and the other side is provided with an air discharge port for supplying air heat exchanged from the heat exchange unit toward the residence space of the distribution unit disposed on the upper outer surface of the reactor, An exchange jacket covering the entire outer circumferential surface of the gas conduit and forming an exchange space therein;

And an air baffle formed in a spiral shape between the inner circumferential surface of the exchange jacket and the outer circumferential surface of the gas conduit in a spiraling direction of the exchange space.
The method according to claim 1,

The reactor,

It is formed in a shape gradually widening from the upper side, the drying zone and the pyrolysis zone is formed therein, a distribution unit for forming a residence space for temporarily receiving the heat-exchanged air surrounds the outside of the drying zone along the upper outer surface A reactor upper body formed in a band shape,

An outer case connected to an edge of a lower end of the reactor upper body, wherein the gas outlet is formed at one side;

It is accommodated in the outer case, and in communication with the inside of the reactor upper body includes an inner case in which the oxidation zone and the reduction zone is formed therein,

And the first air supply assembly and the second air supply assembly are inclined along the upper inner circumferential surface of the inner case, respectively.
The method according to claim 1,

Gasification reaction apparatus using the biomass,

And a ash discharging unit disposed on the lower side of the reactor and discharging the ash remaining after the synthesis gas is discharged from the reduction zone to the outside of the reactor.
The method according to claim 3,

The distribution unit,

A distribution jacket formed in a band shape along the upper outer surface of the reactor to form a residence space in which the heat exchanged air is temporarily received;

It includes a connecting pipe for communicating the heat exchange unit and the residence space with each other,

And the first air supply assembly and the second air supply assembly communicate with the residence space, respectively.
The method according to claim 5,

The first cylinder portion,

A cylindrical first cylinder body accommodating one side of the second cylinder portion,

And a truncated conical guide extending from an end edge of the first cylinder body to surround the outer circumferential surface of the second cylinder portion and inclined at an angle with respect to the outer circumferential surface of the second cylinder portion.

The heat-exchanged air is guided along the inclined surface inside the guide to join the external air from the other end of the second cylinder portion through the inner circumferential surface of the second cylinder portion and inject the gas to the biomass. .
The method according to claim 5,

The second cylinder portion,

A cylinder-shaped second cylinder body accommodated in the first cylinder portion and one end portion exposed to the outside;

A plurality of coanda orifices penetrating along the outer circumferential surface of the other end of the second cylinder body, inclined with respect to the inclined surface of the truncated guide formed on the end edge of the first cylinder portion,

Gasification reaction using a biomass, characterized in that it comprises a venturi (venturi) nozzle extending gradually larger than the second cylinder body to be exposed to the outside of the first cylinder portion from the other end of the second cylinder body Device.
The method according to claim 11,

The coanda orifice is a gasification reaction device using a biomass, characterized in that disposed close to the end edge of the guide.
The method according to claim 7,

The reactor upper body,

A first fireproof wall layer formed at a constant thickness from the lower portion of the drying region along the inner circumferential surface of the reactor body;

Gasification reaction apparatus using a biomass further comprises a refractory wall slope formed inclined downward toward the inner case side in the upper end portion of the first fireproof wall layer.
The method according to claim 7,

The inner case,

An axis diameter portion having a combustion slope formed gradually from the upper side,

It includes an enlarged diameter portion extending from the lower edge of the combustion slope gradually formed wider,

The oxidation region is formed on the shaft diameter portion and the enlarged diameter portion,

The reduction zone is a gasification reactor using a biomass, characterized in that formed in the lower portion of the enlarged diameter.
The method according to claim 7,

The reactor,

A hopper connected to an upper end of the reactor upper body and into which the biomass is injected;

Gasification reaction apparatus using a biomass further comprises a torque sensor for detecting the supply amount of the biomass that is inserted while rotating at least one mounted to the upper end and the lower end of the hopper, respectively.
The method according to claim 8,

The ash discharging unit,

A drive motor disposed on the bottom of the reactor;

It is rotationally supported by a thrust bearing and receives a driving force from the drive motor.

Oh with the driving shaft,

A great assembly having a truncated conical shape connected to an upper end of the drive shaft and formed in a lower portion of the reduction zone and rotating at a constant speed to form a plurality of steps for dropping the ash of the biomass combusted from the reduction zone by a predetermined amount; ,

A reclosing tank provided on a bottom surface of the reactor to form a space for temporarily receiving ashes of the biomass that have fallen;

A discharge screw formed in a spiral shape along an outer circumferential surface of the discharge shaft which is formed to be inclined upwardly from a lower portion of the reclosing tank and rotates in one direction;

A discharge motor connected to an end of the discharge shaft and transmitting a driving force to the discharge shaft;

Gasification reaction apparatus using a biomass, characterized in that it comprises a discharge induction pipe extending from the re containing tank and containing the discharge screw.