JP6020951B1 - Gasification system and gasification method in gasification system - Google Patents

Abstract

An object of the present invention is to efficiently gasify biomass. The present invention introduces a low-temperature flow path 36 through which a slurry body prepared from biomass as a gasification raw material flows, and a supercritical high-temperature fluid, and the introduced high-temperature fluid is heated with the slurry body in the low-temperature flow path 36 and heat. A heat exchanger 31 having a high-temperature flow path 37 that flows while being exchanged, and a gas that is heated by the heat exchanger 31 to further heat the slurry body to a temperature at which it can be gasified in a supercritical state A gasification system 10 comprising a gasification reactor 33 and an introduction path 35 for introducing a slurry body in a supercritical state into a high-temperature flow path 37 as a high-temperature fluid, which is provided in the middle of the introduction path 35 and is in a supercritical state And a pressurizing device 38 that pressurizes the slurry body and introduces it into the high-temperature channel 37.

Description

  The present invention relates to a gasification system and a gasification method in which a slurry body prepared by using biomass as a raw material is decomposed in a supercritical state to generate fuel gas.

  There is known a gasifier that obtains fuel gas by decomposing biomass in a supercritical state. For example, Patent Document 1 discloses that a biomass slurry containing a nonmetallic catalyst is hydrothermally treated under conditions of a temperature of 374 ° C. or higher and a pressure of 22.1 MPa or higher, and the generated gas is used to generate a power generator. A biomass gasification power generation system that generates power and heats a slurry body using exhaust heat from a power generation device is described.

JP 2008-246343 A

  FIG. 7 is a diagram illustrating a general biomass gasification power generation system. As shown in the figure, the gasification system 2 includes a heat exchanger 3, a heater 4, and a gasification reactor 5. Among these units, the heat exchanger 3 is a device for heating the slurry body. This slurry body is prepared by, for example, adding water and activated carbon (catalyst) to biomass such as shochu residue, egg-collecting chicken manure, and sludge and mixing them. The heater 4 is a device that raises the temperature of the slurry heated by the heat exchanger 3 to a gasification reaction temperature (temperature at which the slurry is gasified (gasification is possible)). The gasification reactor 5 is an apparatus that keeps the slurry body constant at the gasification reaction temperature. The fluid that has undergone the gasification reaction is then gas-liquid separated, and the gas component is used as fuel gas.

  Here, as the heat exchanger 3, for example, a double-pipe heat exchanger is used. FIG. 8 is a diagram illustrating the configuration of the double pipe 6 provided in the double pipe heat exchanger. As shown in the figure, in the double pipe 6, a low-temperature flow path 8 is defined inside the inner pipe 7, and a high-temperature flow path 11 is defined between the outer pipe 9 and the inner pipe 7. A slurry body 13 is circulated through the low temperature flow path 8. On the other hand, a high-temperature fluid 14 that exchanges heat with the slurry body 13 flows through the high-temperature channel 11 in the opposite direction to the slurry body 13. Then, the slurry body 13 introduced from the inlet 12 of the low-temperature channel 8 is heated while exchanging heat with the high-temperature fluid 14 and discharged from the outlet 15.

  FIG. 9 is a diagram illustrating an example of a change in the temperature of the slurry body 13 and a change in the temperature of the high-temperature fluid 14 in the heat exchanger 3 including the double pipe 6. In this figure, the vertical axis indicates the temperature of the fluid, and the horizontal axis indicates the distance of the double pipe 6. Supplementing the distance of the double pipe 6, the distance of the double pipe 6 is from the inlet 12 when the position of the inlet 12 in the inner pipe 7 is 0 and the position of the outlet 15 is 100. Is the distance.

  As shown in FIG. 9, the temperature of the slurry 13 introduced into the inlet 12 at room temperature is raised, but the intermediate portion 16 of the heat exchanger 3 (the temperature of the slurry 13 is about 380 ° C. It can be seen that the temperature increase rate of the slurry body 13 is extremely slow at a portion of about 30 to about 70). Similarly, with respect to the high temperature fluid 14, almost no temperature change is observed in the intermediate portion 16, and the temperature is about 380 ° C. which is substantially the same as that of the slurry body 13.

  Thus, the reason why the temperature change of the low temperature fluid 13 and the high temperature fluid 14 in the intermediate portion 16 is smaller than that in the other portions is that the constant pressure specific heat of the slurry body 13 and the high temperature fluid 14 in the intermediate portion 16 is high. It is thought that it is because.

  That is, the internal pressure of the heat exchanger 3 is a high pressure (for example, 25 MPa), but under such a high pressure, the constant pressure specific heat of the slurry body 13 and the high temperature fluid 14 is a specifically high peak near the critical temperature (about 380 ° C.). It is known to take a value. Actually, the constant pressure specific heat of the high temperature fluid 14 peaks at a temperature slightly lower than the constant pressure specific heat of the slurry body 13 due to pressure loss in the double pipe 6. For this reason, in the intermediate part 16, the temperature difference between the slurry body 13 and the high-temperature fluid 14 is reduced, and the amount of exchange heat per unit area is also reduced, so that the temperature of the slurry body 13 is hardly increased. That is, when heat is exchanged from a low-pressure high-temperature fluid to a high-pressure low-temperature fluid, the pseudo-critical point of the high-pressure low-temperature fluid from the temperature range near the pseudo-critical point of the low-pressure high-temperature fluid as shown in the intermediate portion 16 of FIG. In the vicinity of the temperature range, the temperature difference between the low-pressure high-temperature fluid and the high-pressure low-temperature fluid becomes small, and the amount of exchange heat per unit heat transfer area decreases.

  Further, it is known that tar derived from biomass components is easily generated in the intermediate portion 16. The generated tar adheres to the inner wall of the inner pipe 7 and covers the inner surface of the pipe, thereby preventing the passage of heat and further reducing the amount of exchange heat.

  This invention is made | formed in view of such the present condition, The objective is to provide the gasification method for performing gasification of biomass efficiently, and the gasification method in a gasification system.

  In order to achieve the above-mentioned object, the present invention introduces a low-temperature flow path through which a slurry body prepared from biomass as a gasification raw material flows, a high-temperature fluid in a supercritical state, and the introduced high-temperature fluid is A heat exchanger having a high-temperature flow path flowing while being heat-exchanged with a slurry body in a low-temperature flow path, and further heating the slurry body heated by the heat exchanger to make the slurry body in a supercritical state and gas A gasification system comprising a gasification reactor that can be converted to a temperature capable of being gasified, and an introduction path for introducing the slurry body in the supercritical state into the high-temperature flow path as the high-temperature fluid, And a pressurizing device that pressurizes and introduces the slurry body in the supercritical state into the high-temperature flow path.

  According to the gasification system of the present invention, since the high-temperature fluid is pressurized by the pressurizing device, the temperature at the pseudocritical point where the constant-pressure specific heat of the high-temperature fluid flowing through the heat exchanger peaks can be raised. Accordingly, the amount of heat exchanged per unit heat transfer area can be increased in heat exchange with the slurry body. As a result, the time during which the temperature of the low-temperature fluid stagnates at a temperature at which tar is easily generated can be shortened. For this reason, generation | occurrence | production of tar at the time of heating a slurry body can be suppressed, and gasification of biomass can be performed efficiently. Further, according to the present system, the amount of exchange heat per unit heat transfer area can be increased, so that the heat exchanger can be reduced in size if the same amount of exchange heat is used.

  In the gasification system described above, the high temperature flow path is divided into a first high temperature flow path on the inlet side where the high temperature fluid is introduced and a second high temperature flow path on the discharge port side where the high temperature fluid is discharged. A high-temperature fluid acquisition channel that communicates with the downstream end of the first high-temperature channel and takes out the high-temperature fluid in a subcritical state from the heat exchanger; and the high-temperature fluid that is sent through the high-temperature fluid acquisition channel A gas-liquid separator that separates fuel gas from a fluid; a turbine that includes a turbine and that rotates the turbine by the pressure of the fuel gas separated by the gas-liquid separator; and an upstream end of the second high-temperature channel And a high-temperature fluid return flow path for returning the high-temperature fluid after the fuel gas is separated by the gas-liquid separator to the heat exchanger.

  In this gasification system, gas (fuel gas) is separated from the subcritical high-temperature fluid taken from the middle of the double-tube heat exchanger (downstream end of the first high-temperature flow path). Then, the turbine of the power unit is rotated by the pressure of the separated fuel gas. Further, the high-temperature fluid after the fuel gas is separated is returned to the middle of the heat exchanger (upstream end of the second high-temperature flow path). Thus, the pressure of the fuel gas separated from the high-temperature fluid can be used as power for the power unit. Further, since the high-temperature fluid after the fuel gas is separated is used for heat exchange, the ratio of the liquid component having a larger specific heat per unit volume than the fuel gas is high in the high-temperature fluid, and the high-temperature fluid liquid and the low-temperature fluid Since the heat transfer area for heat exchange can be increased, the amount of exchange heat per unit heat transfer area can be increased. As a result, the energy of the high temperature fluid can be used effectively.

  The present invention also provides a low-temperature channel through which a slurry body prepared from biomass as a gasification raw material flows, a supercritical high-temperature fluid, and the introduced high-temperature fluid is a slurry body in the low-temperature channel. A double-pipe heat exchanger having a high-temperature channel that flows while being heat-exchanged, and the slurry body heated by the heat exchanger is further heated to make the slurry body in a supercritical state and gasified A gasification system comprising a gasification reactor capable of achieving a possible temperature and an introduction path for introducing the slurry body in the supercritical state into the high-temperature flow path as the high-temperature fluid, the high-temperature flow path including the The first high-temperature channel on the inlet side into which the high-temperature fluid is introduced and the second high-temperature channel on the outlet side from which the high-temperature fluid is discharged are configured to be separated at the downstream end of the first high-temperature channel. Communicating and transferring the hot fluid to the heat exchanger A high-temperature fluid acquisition flow path to be taken out, a pressurization device for pressurizing the high-temperature fluid taken out by the high-temperature fluid acquisition flow path, and an upstream end of the second high-temperature flow path, and pressurized by the pressurization apparatus And a high-temperature fluid return path for returning the high-temperature fluid to the heat exchanger.

  According to the gasification system of the present invention, the high-temperature fluid taken out from the middle of the double-pipe heat exchanger (the downstream end of the first high-temperature channel) is pressurized by the pressurizer. Then, the pressurized high-temperature fluid is returned to the middle of the heat exchanger (upstream end of the second high-temperature channel). By the pressurization by the pressurizing device, the temperature of the pseudocritical point where the constant pressure specific heat of the high temperature fluid flowing through the second high temperature channel reaches a peak can be raised. Accordingly, in the heat exchange with the slurry body in the second high-temperature channel, the exchange heat amount per unit heat transfer area can be increased. As a result, the time during which the temperature of the low-temperature fluid stagnates at a temperature at which tar is easily generated can be shortened. As a result, tar generation when the slurry body is heated can be suppressed, and biomass gasification can be efficiently performed. In addition, according to the present system, the amount of exchange heat per unit heat transfer area can be increased, so that the heat exchanger can be downsized with the same amount of exchange heat.

  In the gasification system described above, a gas-liquid separator that is provided in the middle of the high-temperature fluid acquisition passage and separates fuel gas from the high-temperature fluid in a subcritical state, and a turbine, are separated by the gas-liquid separator. Preferably, the pressurizing device pressurizes the high-temperature fluid after the fuel gas is separated by the gas-liquid separator.

  In this gasification system, fuel gas is separated from a subcritical hot fluid. Then, the turbine of the power unit is rotated by the pressure of the separated fuel gas. Further, after the high-temperature fluid after the fuel gas is separated is pressurized by the pressurizing device, it is returned to the middle of the heat exchanger. By the pressurization by the pressurizing device, the temperature of the pseudocritical point where the constant pressure specific heat of the high temperature fluid flowing through the second high temperature channel reaches a peak can be raised. Accordingly, in the heat exchange with the slurry body in the second high-temperature channel, the exchange heat amount per unit heat transfer area can be increased. As a result, the time during which the temperature of the low-temperature fluid stagnates at a temperature at which tar is easily generated can be shortened. In addition, the ratio of the liquid component having a specific heat larger than that of the fuel gas is increased in the high-temperature fluid, and the heat transfer area in which the high-temperature fluid liquid and the low-temperature fluid exchange heat can be increased. The amount of exchange heat can be increased.

  In the gasification system described above, it is preferable that the power unit includes a combustion device that combusts fuel gas after rotating the turbine, and further rotates the turbine with the gas after combustion.

  In this gasification system, the fuel gas separated by the gas-liquid separator is combusted to further rotate the turbine, so that the energy of the high-temperature fluid can be used effectively.

  The present invention also provides a low-temperature channel through which a slurry body prepared from biomass as a gasification raw material flows and a supercritical high-temperature fluid, and the introduced high-temperature fluid is a slurry body in the low-temperature channel. A double-pipe heat exchanger having a high-temperature flow path that flows while being heat-exchanged, and the slurry body heated by the heat exchanger is further heated to gasify the slurry body in a supercritical state A gasification method in a gasification system, comprising: a gasification reactor that makes the temperature possible, and an introduction path that introduces the slurry body in the supercritical state into the high-temperature flow path as the high-temperature fluid, The slurry body in a critical state is pressurized in the middle of the introduction path, and the pressurized slurry body is introduced into the high-temperature channel.

  The present invention also provides a low-temperature channel through which a slurry body prepared from biomass as a gasification raw material flows, a supercritical high-temperature fluid, and the introduced high-temperature fluid is a slurry body in the low-temperature channel. A double-pipe heat exchanger having a high-temperature channel that flows while being heat-exchanged, and the slurry body heated by the heat exchanger is further heated to make the slurry body in a supercritical state and gasified A gasification method in a gasification system, comprising: a gasification reactor capable of achieving a possible temperature; and an introduction path for introducing the supercritical slurry into the high-temperature flow path as the high-temperature fluid, the high-temperature flow The path is divided into a first high-temperature channel on the inlet side into which the high-temperature fluid is introduced and a second high-temperature channel on the outlet side from which the high-temperature fluid is discharged. From the downstream end of the subcritical state The hot fluid extraction to the outside of the heat exchanger, after pressurizing said hot fluid taken out above, and returns from the upstream end of said second hot channel inside the heat exchanger.

  According to the present invention, biomass can be efficiently gasified in the gasification system and the gasification method of the gasification system.

It is a figure explaining the composition of the gasification system concerning a 1st embodiment. It is the figure which showed the relationship between temperature, a pressure, and a constant pressure specific heat. It is a graph which shows the constant pressure specific heat curve of a high temperature fluid. It is a figure explaining the gasification system which concerns on 2nd Embodiment. It is a figure explaining the gasification system which concerns on 3rd Embodiment. It is a figure explaining the gasification system which concerns on 4th Embodiment. It is a figure explaining a general supercritical gasification system. It is a figure explaining the structure of the double pipe in a double pipe type heat exchanger. It is the figure which illustrated the temperature change of the high temperature fluid and the slurry body in a double tube type heat exchanger.

  Embodiments of the present invention will be described below. First, the first embodiment will be described. FIG. 1 is a diagram illustrating a configuration of a gasification system 10 according to the first embodiment. In the gasification system 10, a slurry body is prepared from biomass that is a raw material such as shochu residue, egg-collecting chicken manure, sludge, etc., and combustion gas is generated by heating and pressurizing the prepared slurry body. As shown in the figure, the gasification system 10 includes a raw material preparation unit 20, a heat treatment unit 30, and a gas processing unit 40.

  The raw material preparation unit 20 is a part that prepares a slurry body from biomass. The raw material preparation unit 20 includes a preparation tank 21, a pulverizer 22, a supply pump 23, and a heat exchanger introduction pump 24.

  The preparation tank 21 is a container for mixing biomass, water, and activated carbon (a kind of nonmetallic catalyst). In the preparation tank 21, a mixture in which biomass, water, and activated carbon are mixed is prepared. For example, porous particles having an average particle diameter of 200 μm or less are used as the activated carbon. The mixing ratio of biomass, water, and activated carbon is appropriately adjusted according to the type, amount, moisture content, and the like of biomass.

  The pulverizer 22 is an apparatus for crushing the solid content of the mixture prepared in the preparation tank 21 to obtain a uniform size (preferably an average particle size of 500 μm or less, more preferably an average particle size of 300 μm or less). is there. By being processed by the pulverizer 22, the mixture becomes a slurry-like slurry body.

  The supply pump 23 supplies the slurry body discharged from the pulverizer 22 to the heat exchanger introduction pump 24. The heat exchanger introduction pump 24 pressurizes the slurry body sent from the supply pump and supplies it to the heat treatment unit 30. The slurry body is pressurized to about 0.1 to 4 MPa by the heat exchanger introduction pump 24.

  The heat treatment unit 30 is a part that heats and gasifies the slurry body prepared by the raw material preparation unit 20. The heat treatment section 30 includes a heat exchanger 31, a heater 32, a gasification reactor 33, and a high-temperature fluid pressurizing device 34.

  The heat exchanger 31 exchanges heat between the slurry body sent from the raw material preparation unit 20 and the high-temperature fluid sent from the gasification reactor 33 (hereinafter also referred to as a post-treatment fluid, which will be described later). Device. The heat exchanger 31 is a double tube heat exchanger and includes a low temperature channel 36 and a high temperature channel 37. For convenience of illustration, the double pipe is simplified in FIG. And the slurry body sent from the raw material preparation part 20 distribute | circulates to the low temperature flow path 36, and the high temperature fluid sent from the gasification reactor 33 distribute | circulates to the high temperature flow path 37.

  The temperature of the slurry body flowing through the low temperature flow path 36 is increased by absorbing heat released from the processed fluid flowing through the high temperature flow path 37. On the contrary, the temperature of the processed fluid flowing through the high temperature flow path 37 is lowered by heat radiation. In this embodiment, the introduction temperature of the slurry body to the heat exchanger 31 is normal temperature, and the discharge temperature from the heat exchanger 31 is about 450 ° C. On the other hand, the temperature at which the treated fluid is introduced into the heat exchanger 31 is about 600 ° C., and the discharge temperature from the heat exchanger 31 is about 120 ° C.

  The heater 32 is a device that heats the slurry body sent from the heat exchanger 31. The heater 32 includes a combustion device 32a. The combustion device 32a introduces and burns the fuel gas sent from the gas processing unit 40 into liquefied petroleum gas such as propane gas or air, and heats the slurry body. Thereby, the temperature of the slurry introduced into the heater 32 is raised to, for example, about 600 ° C. The heated slurry body is sent to the gasification reactor 33.

  The gasification reactor 33 keeps the slurry body sent from the heater 32 constant at a gasification reaction temperature (temperature at which the slurry body is gasified (gasification is possible)) in a supercritical state, This is an apparatus for hydrothermally treating an organic substance contained in a slurry body. The gasification reactor 33 includes a combustion device 33a. The combustion device 33a introduces the fuel gas sent from the gas processing unit 40 into liquefied petroleum gas or air and burns it, and hydrothermally heats the slurry body. In this hydrothermal treatment, the slurry body is hydrothermally treated for 1 to 2 minutes under conditions of, for example, 600 ° C. and 25 MPa.

  The slurry body that has undergone hydrothermal treatment and has completed the gasification reaction becomes a high-temperature fluid in a supercritical state (processed fluid), and is introduced into the high-temperature flow path 37 of the heat exchanger 31 through the introduction path 35. In this embodiment, a high-temperature fluid pressurizing device 34 is provided in the middle of the introduction path 35. The high-pressure fluid pressurizing device 34 is a device that further pressurizes the treated fluid sent from the gasification reactor 32 and introduces it into the heat exchanger 31 (the high-temperature channel 37). The high temperature fluid pressurizer 34 will be described later.

  The gas processing unit 40 is a part that extracts fuel gas from the processed fluid sent from the heat exchanger 31. The gas processing unit 40 includes a decompression mechanism 41, a cooling mechanism 42, a gas-liquid separator 43, and a gas tank 44.

  The decompression mechanism 41 is a device that decompresses the processed fluid sent from the heat exchanger 31. The cooling mechanism 42 is a device that cools the processed fluid sent from the decompression mechanism 41. The gas-liquid separator 43 is a device that separates the processed fluid cooled by the cooling mechanism 42 into a liquid (a liquid containing activated carbon or ash) and a gas (a fuel gas such as hydrogen or methane). Among these, the liquid is treated as drainage, and the gas is sent to the gas tank 44.

  The gas tank 44 is a container that stores the gas separated by the gas-liquid separator 43. A part of the gas stored in the gas tank 44 is supplied to the heater 32 and the gasification reactor 33 and consumed as fuel gas. In addition, this fuel gas can also be used as power generation or a power source.

  Next, the high-pressure fluid pressurizer 34 (hereinafter simply referred to as the pressurizer 34) will be described. The pressurization device 34 is provided to further pressurize the supercritical high-temperature fluid (processed fluid) sent from the gasification reactor 33 and introduce it into the heat exchanger 31. For example, It consists of a pressurizing device such as a plunger type, centrifugal type or axial flow type.

  Further pressurization of the high-temperature fluid is performed in order to improve the heat exchange efficiency in the heat exchanger 31. Therefore, the reason why the heat exchange efficiency is improved by this pressurization will be described. FIG. 2 is a graph showing the relationship between temperature, pressure, and constant pressure specific heat in water. From this graph, it can be seen that water under a very high pressure has a specific high specific pressure at a specific temperature range. For example, if the pressure is 24 MPa, the constant pressure specific heat is rapidly increased at 380 ° C. It can also be seen that by further increasing the pressure from 24 MPa, the peak value of the constant pressure specific heat decreases and the temperature corresponding to the peak shifts to the high temperature side.

  A high-temperature fluid containing water as a main component also has similar characteristics. Here, FIG. 3 is a graph showing a constant pressure specific heat curve of a high-temperature fluid, where the horizontal axis is temperature and the vertical axis is constant pressure specific heat. A constant pressure specific heat curve 61 at a certain pressure P1 and a constant pressure specific heat curve 62 at a pressure P2 higher than the pressure P1 are drawn.

  The high-temperature fluid having the pressure P1 will be described. In this high-temperature fluid, as shown in the constant-pressure specific heat curve 61, there is no significant change in the constant-pressure specific heat from 600 ° C. (introduction temperature T0) to the temperature T5. Thereafter, until the temperature T3, the value of the constant pressure specific heat gradually increases as the temperature decreases. Furthermore, during the period up to the critical temperature T1, the value of the constant pressure specific heat increases rapidly as the temperature decreases. The constant-pressure specific heat at the critical temperature T1 indicates Cp1, which is a peak value. When the critical temperature T1 is exceeded, the constant pressure specific heat rapidly decreases and finally shows a value comparable to the constant pressure specific heat at the introduction temperature T0.

  Next, the high-temperature fluid having the pressure P2 will be described. In this high-temperature fluid, as shown in the constant-pressure specific heat curve 62, there is no significant change in the constant-pressure specific heat from 600 ° C. to the temperature T6. Thereafter, until the temperature T4, the value of the constant pressure specific heat gradually increases as the temperature decreases. Furthermore, during the period up to the critical temperature T2, the value of the constant pressure specific heat increases rapidly as the temperature decreases. The constant-pressure specific heat at the critical temperature T2 indicates the peak value Cp2. When the critical temperature T2 is exceeded, the constant pressure specific heat rapidly decreases, and finally shows a value similar to the constant pressure specific heat at the introduction temperature T0.

  Here, the temperature T6, the temperature T4, and the temperature T2 are slightly higher than the temperature T5, the temperature T3, and the temperature T1, respectively. Further, the constant pressure specific heat Cp2 is lower than the constant pressure specific heat Cp1. It can be seen that by increasing the pressure of the high-temperature fluid from P1 to P2, the pseudocritical temperature at which the constant pressure specific heat reaches a peak can be increased from T1 to T2. In addition, it can be seen that the constant pressure specific heat of the fluid having a high pressure indicated by the constant pressure specific heat curve 62 is always higher than the constant pressure specific heat of the fluid having a low pressure indicated by the constant pressure specific heat curve 61 in the temperature range of T2 or higher. These show that high pressure fluids have more heat at the same temperature than low pressure fluids. Accordingly, the temperature of the high-pressure high-temperature fluid after releasing a predetermined amount of heat to the low-pressure fluid can be kept higher than that of the low-pressure fluid.

  As a result, in the heat exchange in the heat exchanger 31, the time during which the temperature of the high-temperature fluid (processed fluid) stagnates at a temperature at which tar is easily generated (around 380 ° C.) can be shortened. In connection with this, since it becomes difficult to stagnate in this temperature range also about a slurry body, generation | occurrence | production of tar can be suppressed. As a result, biomass gasification can be performed efficiently. Moreover, since a slurry body is heated rapidly, the length of the double tube which comprises the heat exchanger 31 can be made shorter than the conventional apparatus. That is, it is possible to reduce the size by reducing the heat transfer area.

  Referring to the graph of FIG. 2, it can be understood that by increasing the pressure of the high-temperature fluid from 25 MPa to 26 MPa by the pressurizing device 34, the temperature of the pseudocritical point where the constant pressure specific heat reaches a peak can be increased.

  Next, a second embodiment will be described with reference to FIG. As shown in the figure, also in the second embodiment, the gasification system 10 includes a raw material preparation unit 20, a heat treatment unit 30, and a gas processing unit 40. Among these, since the raw material preparation part 20 is the same as that of 1st Embodiment, description is abbreviate | omitted.

  The heat treatment unit 30 of the present embodiment includes a heat exchanger 31, a heater 32, a gasification reactor 33, a gas-liquid separator 38, a subcritical high temperature fluid pressurizing device 58, a decompression mechanism 51, and a cooling mechanism 52. . Among these, the heater 32 and the gasification reactor 33 are configured in the same manner as in the first embodiment, and thus description thereof is omitted.

  The heat exchanger 31 is a double-pipe heat exchanger having a double pipe, and is introduced from the low-temperature flow path 36 through which the slurry sent from the raw material preparation unit 20 flows and the gasification reactor 33. And a high-temperature flow path 37 through which the high-temperature fluid (processed fluid) generated in the gasification reactor 33 flows. The high temperature channel 37 is divided into a first high temperature channel 37a on the inlet side into which the high temperature fluid is introduced and a second high temperature channel 37b on the outlet side from which the high temperature fluid is discharged. .

  The upstream end of the high temperature fluid acquisition passage 53 is communicated with the downstream end of the first high temperature passage 37a, and the downstream end of the high temperature fluid return passage 54 is communicated with the upstream end of the second high temperature passage 37b. . A gas-liquid separator 38 is provided between the downstream end of the high-temperature fluid acquisition passage 53 and the upstream end of the high-temperature fluid return passage 54. The gas-liquid separator 38 gas-liquid separates the high-temperature fluid that has flowed from the high-temperature fluid acquisition flow path 53 and sends the liquid component (the high-temperature fluid after the fuel gas is separated) to the high-temperature fluid return path 54. Further, the gas-liquid separator 38 sends a gas component (fuel gas) to the gas processing unit 40. Further, a subcritical high-temperature fluid pressurizing device 58 (hereinafter simply referred to as a pressurizing device 58) is provided in the middle of the high-temperature fluid return path.

  The decompression mechanism 51 is a device that decompresses the high-temperature fluid (processed fluid) discharged from the second high-temperature channel 37b, and communicates with the second high-temperature channel 37b through a pipe. The cooling mechanism 52 is a device that cools the processed fluid sent from the decompression mechanism 51 and communicates with the decompression mechanism 51 through a pipe. The cooling mechanism 52 is provided with a discharge pipe with a valve.

  The gas processing unit 40 includes a turbine device 46, a flow rate adjusting mechanism 45, and a gas tank 44.

  The turbine device 46 corresponds to a power unit, and rotates the turbine 46 a using the pressure of the gas (fuel gas) separated by the gas-liquid separator 38. The rotating shaft of the turbine 46 a is connected to the rotating shaft of the generator G. For this reason, the generator G generates electric power by the rotation of the turbine 46a.

  The flow rate adjusting mechanism 45 adjusts the flow rate of the fuel gas that has finished work in the turbine device 46 to the gas tank 44. The fuel gas whose flow rate is adjusted by the flow rate adjusting mechanism 45 is sent to the gas tank 44. The gas tank 44 stores the sent fuel gas. A part of the fuel gas stored in the gas tank 44 is consumed as fuel for the heater 32 and the gasification reactor 33.

  In the gasification system 10 of the present embodiment, the high-temperature fluid (processed fluid) that has become a subcritical state by heat exchange in the first high-temperature channel 37 a passes outside the heat exchanger 31 through the high-temperature fluid acquisition channel 53. It is taken out. The extracted high-temperature fluid flows into the gas-liquid separator 38, and the fuel gas is separated. The high-temperature fluid from which the fuel gas has been separated is sent to the high-temperature fluid return path 54. Thereafter, the high-temperature fluid is pressurized by the pressurizing device 58 and introduced into the second high-temperature channel 37b. That is, the fuel gas is separated and the pressurized high-temperature fluid is returned to the heat exchanger 31.

  In the second high-temperature channel 37b, the high-temperature fluid exchanges heat with the slurry flowing in the low-temperature channel 36. However, since the pressure of the high-temperature fluid is increased, the temperature at the pseudocritical point where the constant pressure specific heat reaches a peak is set. Can be raised. This makes it difficult for the temperature of the low-temperature fluid to stagnate at a temperature at which tar is easily generated. Furthermore, since the fuel gas is separated, the liquid ratio in the high-temperature fluid can be increased. From these, the slurry body can be rapidly heated, and generation of tar can be suppressed.

  The high-temperature fluid discharged from the heat exchanger 31 (second high-temperature channel 37 b) is introduced into the decompression mechanism 51 and the cooling mechanism 52. By these decompression mechanism 51 and cooling mechanism 52, the high-temperature fluid is decompressed and cooled to about room temperature and normal pressure. This cooled liquid (liquid containing activated carbon or ash) is treated as drainage.

  Thus, in the gasification system 10 of this embodiment, the high temperature fluid introduced into the first high temperature channel 37a of the heat exchanger 31 is transferred from the downstream end of the first high temperature channel 37a to the outside of the heat exchanger 31. I'm taking it out. Then, the high-temperature fluid after separating the fuel gas is pressurized and returned to the inside of the heat exchanger 31 from the upstream end of the second high-temperature channel 37b. Thereby, the pseudocritical point temperature at which the constant pressure specific heat of the high-temperature fluid in the heat exchanger 31 reaches a peak can be increased. As a result, the amount of exchange heat per unit heat transfer area in the heat exchanger 31 can be increased. Moreover, generation | occurrence | production of a tar can be suppressed in the case of heating of a slurry body. As a result, it is possible to suppress an increase in thermal resistance in the heat exchanger 31 due to tar adhesion and prevent a decrease in the heat passage rate.

  Moreover, in this gasification system 10, since the turbine 46a which the turbine apparatus 46 has is rotated using the pressure of the fuel gas isolate | separated from the high temperature fluid, and the generator G is performing electric power generation, fuel gas has The energy of pressure can be used effectively. Furthermore, since the fuel gas that has finished work in the turbine device 46 is stored in the gas tank 44 and used as fuel, energy can also be used effectively in this respect.

  Next, a third embodiment will be described with reference to FIG. As shown in the figure, also in the third embodiment, the gasification system 10 includes a raw material preparation unit 20, a heat treatment unit 30, and a gas processing unit 40.

  In the third embodiment, similarly to the second embodiment, the high-temperature channel 37 of the heat exchanger 31 is divided into a first high-temperature channel 37a and a second high-temperature channel 37b. A gas-liquid separator 38 is provided between the high-temperature fluid acquisition passage 53 and the high-temperature fluid return passage 54. In the third embodiment, a pressurizing device 34 is provided in the middle of the introduction path 35 as in the first embodiment. Accordingly, the pressurizing device 58 provided in the second embodiment is eliminated in the third embodiment.

  In the gasification system 10 of the present embodiment, after the high-temperature fluid (processed fluid) in the subcritical state is taken out of the heat exchanger 31 through the high-temperature fluid acquisition passage 53 and the fuel gas is separated by the gas-liquid separator 38. The high-temperature fluid is returned to the heat exchanger 31. Also in this gasification system 10, since the high-temperature fluid is pressurized by the pressurizing device 34, the pseudocritical point temperature at which the constant pressure specific heat reaches a peak can be raised. As a result, since the temperature difference between the high-temperature fluid and the slurry body is kept large and the exchange heat amount per unit heat transfer area is increased, the exchange heat amount per unit heat transfer area in the heat exchanger 31 can be increased. And generation | occurrence | production of a tar can be suppressed in the case of heating of a slurry body. As a result, it is possible to suppress an increase in thermal resistance in the heat exchanger 31 due to tar adhesion and prevent a decrease in the heat passage rate.

  Next, a fourth embodiment will be described with reference to FIG. As shown in the figure, also in the fourth embodiment, the gasification system 10 includes a raw material preparation unit 20, a heat treatment unit 30, and a gas processing unit 40.

  In the fourth embodiment, similarly to the second embodiment, the high-temperature channel 37 of the heat exchanger 31 is divided into a first high-temperature channel 37a and a second high-temperature channel 37b. A gas-liquid separator 38 is provided between the high-temperature fluid acquisition flow path 53 and the high-temperature fluid return path 54, and a pressurizing device 58 is provided in the middle of the high-temperature fluid return path 54. On the other hand, the fourth embodiment is different from the second embodiment in that a combustion device 47 is provided in addition to the turbine device 46 and that the gas tank 44 and the flow rate adjusting mechanism 45 are eliminated.

  The combustion device 47 burns the fuel gas that has finished work in the turbine device 46 together with air. The high-pressure exhaust gas generated by the combustion is introduced into the turbine device 46, and the turbine 46a is rotated. That is, a gas turbine is configured by the turbine device 46 and the combustion device 47. And the rotating shaft of the generator G is connected with the rotating shaft of the turbine 46a. For this reason, the generator G can generate electric power by the rotation of the turbine 46a.

  In the fourth embodiment, since the turbine 46a is rotated by the pressure of the fuel gas and the pressure of the exhaust gas, the energy of the fuel gas can be effectively used as electric power.

  The above description of the embodiment is for facilitating the understanding of the present invention, and does not limit the present invention. The present invention can be changed and improved without departing from the gist thereof, and the present invention includes equivalents thereof.

  For example, the raw material of biomass may be other than shochu residue, for example, egg-collecting chicken manure, sewage sludge and other water-containing biomass.

  In each of the above embodiments, water and a catalyst are mixed when the slurry body is generated, but these may not be mixed.

  For example, in the second embodiment of FIG. 4, the gas-liquid separator 38 is eliminated, and the high-temperature fluid (post-treatment fluid) that has flowed through the high-temperature fluid acquisition flow path 53 is pressurized by the pressurizer 58, and the pressurized high temperature The fluid may be returned through the hot fluid return path 54. In this case, the gas processing unit 40 is configured as in the first embodiment of FIG.

  In this configuration, by the pressurization by the pressurizing device 58, the pseudo critical point temperature at which the constant pressure specific heat of the high temperature fluid flowing through the second high temperature channel 37b peaks can be raised. Accordingly, in the heat exchange with the slurry body in the second high-temperature channel 37b, the temperature difference is kept large and the exchange heat amount per unit heat transfer area is increased, so that the temperature of the high-temperature fluid is set to a temperature at which tar is easily generated. The time for stagnation can be shortened. As a result, tar generation when the slurry body is heated can be suppressed, and biomass gasification can be efficiently performed.

  Moreover, the combustion apparatus 47 may be provided in the gasification system 10 of 3rd Embodiment of FIG. 5, and the turbine 46a of the turbine apparatus 46 may be rotated with the pressure of fuel gas, and the pressure of waste gas. In this case, the gas processing unit 40 is configured as in the fourth embodiment of FIG.

DESCRIPTION OF SYMBOLS 2 ... Gasification system, 3 ... Heat exchanger, 4 ... Heater, 5 ... Gasification reactor, 6 ... Double pipe, 7 ... Inner piping, 8 ... Low temperature flow path, 9 ... Outer piping, 10 ... Gasification system, 11 ... high temperature flow path, 12 ... inlet, 13 ... slurry body, 14 ... high temperature fluid, 15 ... discharge port, 16 ... intermediate part, 20 ... raw material preparation unit, 21 ... preparation tank, 22 ... pulverizer , 23 ... Supply pump, 24 ... Heat exchanger introduction pump, 30 ... Heat treatment section, 31 ... Heat exchanger, 32 ... Heater, 32a ... Combustion device, 33 ... Gasification reactor, 33a ... Combustion device, 34 ... High temperature Pressurizing device for fluid, 35 ... introducing channel, 36 ... low temperature channel, 37 ... high temperature channel, 37a ... first high temperature channel, 37b ... second high temperature channel, 38 ... gas-liquid separator, 39 ... discharge port , 40 ... gas processing unit, 41 ... pressure reducing mechanism, 42 ... cooling mechanism, 43 ... gas-liquid separator, 44 ... gas tank 45 ... Flow rate adjusting mechanism, 46 ... Turbine device, 46a ... Turbine, 47 ... Combustion device, 51 ... Decompression mechanism, 52 ... Cooling mechanism, 53 ... High temperature fluid acquisition passage, 54 ... High temperature fluid return passage, 58 ... Subcritical high temperature Pressurizing device for fluid, 61 ... first constant pressure specific heat curve, 62 ... second constant pressure specific heat curve

Claims (7)

A low-temperature flow path through which a slurry body prepared from biomass as a gasification raw material flows and a supercritical high-temperature fluid are introduced, and the introduced high-temperature fluid flows while being heat-exchanged with the slurry body in the low-temperature flow path A heat exchanger comprising a high-temperature flow path;
A gasification reactor further heating the slurry body heated by the heat exchanger to bring the slurry body into a supercritical state and capable of gasification;
A gasification system comprising an introduction path for introducing the supercritical slurry body into the high temperature flow path as the high temperature fluid,
A gasification system comprising a pressurization device provided in the middle of the introduction path and pressurizing and introducing the slurry body in the supercritical state into the high temperature flow path. The high-temperature channel is divided into a first high-temperature channel on the inlet side into which the high-temperature fluid is introduced and a second high-temperature channel on the outlet side from which the high-temperature fluid is discharged.
A high-temperature fluid acquisition flow path that communicates with a downstream end of the first high-temperature flow path, and that takes out the high-temperature fluid in a subcritical state from the heat exchanger;
A gas-liquid separator that separates fuel gas from the high-temperature fluid sent through the high-temperature fluid acquisition flow path;
A power unit comprising a turbine and rotating the turbine by the pressure of the fuel gas separated by the gas-liquid separator;
A high-temperature fluid return channel that communicates with an upstream end of the second high-temperature channel and returns the high-temperature fluid after the fuel gas is separated by the gas-liquid separator to the heat exchanger. 2. The gasification system according to 1. A low-temperature flow path through which a slurry body prepared from biomass as a gasification raw material flows and a high-temperature fluid in a supercritical state are introduced, and the introduced high-temperature fluid flows through heat exchange with the slurry body in the low-temperature flow path A double-tube heat exchanger with a flow path;
A gasification reactor further heating the slurry body heated by the heat exchanger to bring the slurry body into a supercritical state and capable of gasification;
A gasification system comprising an introduction path for introducing the supercritical slurry body into the high temperature flow path as the high temperature fluid,
The high-temperature channel is divided into a first high-temperature channel on the inlet side into which the high-temperature fluid is introduced and a second high-temperature channel on the outlet side from which the high-temperature fluid is discharged.
A high-temperature fluid acquisition flow path that communicates with a downstream end of the first high-temperature flow path and extracts the high-temperature fluid from the heat exchanger;
A pressurizing device for pressurizing the high-temperature fluid taken out by the high-temperature fluid acquisition flow path;
A high-temperature fluid return path that communicates with the upstream end of the second high-temperature flow path and returns the high-temperature fluid pressurized by the pressurization device to the heat exchanger;
A gasification system comprising: A gas-liquid separator that is provided in the middle of the high-temperature fluid acquisition flow path and separates fuel gas from the high-temperature fluid in a subcritical state;
A turbine, and a power unit that rotates the turbine by the pressure of the fuel gas separated by the gas-liquid separator,
The gasification system according to claim 3, wherein the pressurizing device pressurizes the high-temperature fluid after the fuel gas is separated by the gas-liquid separator.   5. The gasification system according to claim 2, wherein the power unit includes a combustion device that combusts fuel gas after rotating the turbine, and further rotates the turbine with the gas after combustion. A low-temperature flow path through which a slurry body prepared from biomass as a gasification raw material flows and a supercritical high-temperature fluid are introduced, and the introduced high-temperature fluid flows while being heat-exchanged with the slurry body in the low-temperature flow path A double-tube heat exchanger with a high-temperature flow path;
A gasification reactor further heating the slurry body heated by the heat exchanger to bring the slurry body into a supercritical state and capable of gasification;
A gasification method in a gasification system comprising an introduction path for introducing the slurry body in the supercritical state into the high temperature flow path as the high temperature fluid,
Pressurizing the slurry body in the supercritical state in the middle of the introduction path,
A gasification method in which the pressurized slurry body is introduced into the high-temperature channel. A low-temperature flow path through which a slurry body prepared from biomass as a gasification raw material flows and a high-temperature fluid in a supercritical state are introduced, and the introduced high-temperature fluid flows through heat exchange with the slurry body in the low-temperature flow path A double-tube heat exchanger with a flow path;
A gasification reactor further heating the slurry body heated by the heat exchanger to bring the slurry body into a supercritical state and capable of gasification;
A gasification method in a gasification system comprising an introduction path for introducing the slurry body in the supercritical state into the high temperature flow path as the high temperature fluid,
The high temperature flow path is divided into a first high temperature flow path on the inlet side where the high temperature fluid is introduced and a second high temperature flow path on the discharge port side where the high temperature fluid is discharged,
From the downstream end of the first high-temperature channel, take out the high-temperature fluid in a subcritical state to the outside of the heat exchanger,
A gasification method in which after the pressurized high-temperature fluid is pressurized, it is returned to the inside of the heat exchanger from the upstream end of the second high-temperature flow path.