JP6201555B2 - Oxidation reformer - Google Patents

Description

  The present invention relates to an oxidation reformer that oxidizes and reforms tar contained in synthesis gas generated by gasifying a gasification raw material.

  In recent years, a technology has been developed that gasifies raw materials such as coal, biomass, and tire chips to generate synthesis gas instead of petroleum. Synthetic gas generated in this way is used for power generation systems, hydrogen production, synthetic fuel (synthetic petroleum) production, chemical fertilizer (urea) and other chemical products. Among the gasification raw materials used as the raw material for synthesis gas, coal, in particular, has a recoverable period of about 150 years, more than three times the recoverable period of oil, and reserves are unevenly distributed compared to oil. Therefore, it is expected as a natural resource that can be stably supplied over a long period of time.

  Conventionally, the gasification process of coal has been performed by partial oxidation using oxygen or air. However, since it is necessary to perform partial oxidation at a high temperature of 2000 ° C., there is a disadvantage that the cost of the gasification furnace increases. Had.

  In order to solve this problem, a technique (steam gasification) that uses steam to gasify coal at about 700 ° C. to 900 ° C. has been developed. In this technology, it is possible to reduce the cost by setting the temperature low, but the generated synthesis gas contains tar as compared with the synthesis gas generated by partial oxidation at a high temperature of 2000 ° C. Often included. When the temperature of the synthesis gas decreases in a process that uses the synthesis gas generated by steam gasification, the tar contained in the synthesis gas condenses, causing blockage of piping, failure of equipment used in the process, catalyst poisoning, etc. Problems arise.

  Therefore, an oxidation reformer that removes tar contained in the synthesis gas by adding oxygen and air to the generated synthesis gas, burning it, raising the temperature to 1100 ° C. to 1500 ° C. and performing oxidation reforming is used. Has been.

  In such an oxidation reforming apparatus, a first flow path formed so as to extend vertically upward from a first passage port provided on the bottom surface of the main body toward the inside of the main body, and provided from the inside of the main body to the bottom surface of the main body. A second flow path formed so as to extend vertically downward toward the second passage port, and an intermediate flow path communicating between both flow paths, the first flow path, the second flow path, In each of the above, there is disclosed a technique of providing a heat storage body having a honeycomb structure, supplying an oxidizing agent in an intermediate flow channel located above the heat storage body, and performing oxidation reforming by raising the temperature of the synthesis gas (for example, Patent Documents). 1).

  In the technique of Patent Document 1, the flow direction of the synthesis gas is introduced from the first passage port and discharged from the second passage port, and the flow direction is introduced from the second passage port and discharged from the first passage port. The heat storage body arranged in the first flow path and the heat storage body arranged in the second flow path are alternately heated by the heat of the synthesis gas after the oxidation reforming, and the heat storage The body is preheated by passing synthesis gas before oxidation reforming.

  In addition, the first passage port, the second passage port, the first passage, the second passage, and the intermediate passage described in Patent Document 1 are provided, and the first passage and the second passage are rotatable. A technique in which a heat storage body having a honeycomb structure is provided is also disclosed (for example, Patent Document 2). In the technique of Patent Document 2, when a portion of the heat storage body arranged in the second flow path is heated to a predetermined temperature, the heat storage body is rotated to position the heated portion in the first flow path. Therefore, the synthesis gas before the oxidation reforming is preheated.

JP-A-11-51358 Japanese Patent No. 3984535

  However, depending on the gasification raw material, ash may be included in the synthesis gas. In this case, if the synthesis gas is heated to 1100 ° C. or higher by the oxidizing agent in the oxidation reformer, it is included in the synthesis gas. Ashes melt and become molten slag.

  Then, in the techniques of Patent Documents 1 and 2, the molten slag falls on the heat storage body provided below the intermediate flow path where the oxidation reforming is performed, and the heat storage body is blocked by the molten slag.

  Therefore, in view of such a problem, the present invention devised the position of the heat storage body and the position of the oxidant supply unit with respect to the synthesis gas flow path to oxidize and reform tar from the synthesis gas. In addition, an object of the present invention is to provide an oxidation reforming apparatus that can remove ash and avoid a situation in which a heat storage body is blocked by molten slag.

In order to solve the above-described problems, an oxidation reforming apparatus of the present invention is an oxidation reforming apparatus that oxidizes and reforms a synthesis gas generated by gasifying a gasification raw material, the first heat storage body, A first oxidant supply unit that is disposed vertically below the one heat storage body and supplies an oxidant is provided, and a first flow path section through which the synthesis gas flows, a second heat storage body, and a vertical direction of the second heat storage body A second oxidant supply unit that is disposed below and supplies an oxidant, and is provided below the second flow path unit through which the synthesis gas flows, the first oxidant supply unit, and the second oxidant supply unit. a communication portion for communicating the first flow path portion and the second flow channel portion, and the slag reservoir disposed below the communicating portion, the flow direction of the synthesis gas, the second heat storage body side from the first thermal storage side obtain Bei a first direction towards the, and switching means for switching to a second direction from the second thermal storage side toward the first thermal storage side, the And wherein the door.

  Further, when the flow direction of the synthesis gas is the first direction, the temperature of the synthesis gas after the heat exchange with the second heat storage body is measured, and the flow direction of the synthesis gas is the second direction. In some cases, a temperature measuring unit that measures the temperature of the synthesis gas after heat exchange with the first heat storage body, and the switching means, when the flow direction of the synthesis gas is the first direction, When the temperature of the synthesis gas after the heat exchange with the second heat storage body measured by the temperature measurement unit is equal to or higher than a predetermined temperature, the flow direction of the synthesis gas is switched to the second direction, When the gas flow direction is the second direction, the temperature of the synthesis gas after heat exchange with the first heat storage body measured by the temperature measurement unit is equal to or higher than a predetermined temperature. The flow direction of the synthesis gas may be switched to the first direction.

  Further, the first flow path part and the second flow path part may extend in the vertical direction and be provided in parallel with each other.

  Moreover, a communicating part is good also as a taper shape which a horizontal cross-sectional area reduces gradually as it communicates with a slag storage part and goes vertically downward.

  Moreover, it is good also as an auxiliary | assistant burner provided in a communicating part and heating a molten slag.

  ADVANTAGE OF THE INVENTION According to this invention, while oxidizing and removing tar from synthesis gas, ash can be removed and the situation where a thermal storage body is obstruct | occluded with molten slag can be avoided.

It is a figure for demonstrating a synthesis gas production | generation system. It is a figure for demonstrating an oxidation reforming apparatus. It is a figure for demonstrating control of the valve | bulb by a control part, a 1st oxidizing agent supply part, and a 2nd oxidizing agent supply part. It is a figure for demonstrating control of the valve | bulb by a control part, a 1st oxidizing agent supply part, and a 2nd oxidizing agent supply part. It is a figure for demonstrating the oxidation reforming apparatus of a modification.

  Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. The dimensions, materials, and other specific numerical values shown in the embodiments are merely examples for facilitating the understanding of the invention, and do not limit the present invention unless otherwise specified. In the present specification and drawings, elements having substantially the same function and configuration are denoted by the same reference numerals, and redundant description is omitted, and elements not directly related to the present invention are not illustrated. To do.

(Syngas generation system 100)
FIG. 1 is a diagram for explaining a synthesis gas generation system 100. As shown in FIG. 1, the synthesis gas generation system 100 includes a synthesis gas generation device 110, an oxidation reforming device 150, and a purification device 160. In addition, in FIG. 1, the flow of gasification raw material, gas, water vapor | steam, and air is shown by the solid line arrow, and the flow of a fluid medium (sand) is shown by the dashed-dotted arrow.

(Syngas generator 110)
The synthesis gas generator 110 includes a combustion furnace 112, a medium separator (cyclone) 114, and a gasification furnace 116. The syngas generator 110 is a circulating fluidized bed gasification system, and as a whole, a fluid medium composed of sand such as silica sand (silica sand) having a particle size of about 300 μm is circulated as a heat medium. More specifically, the fluid medium is first heated to about 900 ° C. to 1000 ° C. in the combustion furnace 112 and introduced into the medium separator 114 together with the combustion exhaust gas EX. In the medium separation device 114, the high-temperature fluid medium and the combustion exhaust gas EX are separated, and the separated combustion exhaust gas EX is heat-recovered by a heat exchanger (for example, a boiler) or the like (not shown), and then sent to the outside. Discharged.

  On the other hand, the high-temperature fluid medium separated by the medium separator 114 is introduced into the gasification furnace 116. Then, the fluidized medium introduced into the gasification furnace 116 is fluidized by a gasifying agent (water vapor) introduced from the bottom surface of the gasification furnace 116, and finally returned to the combustion furnace 112.

  The gasification furnace 116 is, for example, a bubble fluidized bed (bubbling fluidized bed) gasification furnace, and a gasification raw material such as a solid raw material such as coal such as lignite, petroleum coke, biomass, tire chips, or a liquid raw material such as black liquor. Is gasified at 700 ° C. to 900 ° C. to generate synthesis gas. In this embodiment, by supplying water vapor to the gasification furnace 116, the gasification raw material is gasified to generate synthesis gas (water vapor gasification).

  Here, the gasification furnace 116 has been described by taking a circulating fluidized bed system as an example. However, if the gasification raw material can be gasified, the gasification furnace 116 may be a simple fluidized bed system or a sand having its own weight. The moving bed method may be used in which the moving bed is formed by flowing down vertically.

  Since the synthesis gas X1 generated in the gasification furnace 116 contains tar, water vapor, ash (combustion ash, fluid medium), etc., it is sent to the subsequent oxidation reformer 150 and the refiner 160 for purification. Is done.

  As will be described in detail later, the oxidation reformer 150 supplies an oxidizing agent to the synthesis gas X1, removes the tar contained in the synthesis gas X1 by oxidation reforming, and melts and removes ash as molten slag. .

  The purifier 160 further purifies by removing tar from the synthesis gas X2 from which tar and ash have been removed, or removing nitrogen compounds such as sulfur, sulfur compounds, ammonia, chlorine and chlorine compounds contained in the synthesis gas X2. Generate synthesis gas.

  Hereinafter, the characteristic oxidation reformer 150 in the present embodiment will be described.

(Oxidation reformer 150)
FIG. 2 is a diagram for explaining the oxidation reformer 150 according to the present embodiment. In FIG. 2 of the present embodiment, an X axis (horizontal direction), a Y axis (horizontal direction), and a Z axis (vertical direction) that intersect perpendicularly are defined as illustrated. In FIG. 2, the gas flow is indicated by solid arrows, and the signal flow is indicated by broken arrows.

  As shown in FIG. 2, the oxidation reformer 150 includes a main body 210, a first heat storage body 230a, a second heat storage body 230b, an oxidant supply unit 240, a slag storage unit 250, an auxiliary burner 260, A temperature detection unit 270, a temperature measurement unit 280, and a control unit 290 are included.

  The main body 210 is a hollow container extending in the vertical direction (Z-axis direction in FIG. 2), and a flow path through which the synthesis gas X1, X2 flows is formed. Specifically, the main body 210 is provided with a partition wall 212 that divides the internal space into two in the horizontal direction (X-axis direction in FIG. 2). A second flow path portion B is formed. Therefore, the first flow path part A and the second flow path part B extend in the vertical direction, and are provided in the main body 210 in parallel with each other with the partition wall 212 interposed therebetween. Further, the main body 210 is formed with a communication portion C that communicates the first flow path portion A and the second flow path portion B. That is, the flow path formed in the main body 210 includes the first flow path part A, the communication part C, and the second flow path part B.

  Further, on the top surface of the main body 210, synthesis gas inlets 220a and 220b to which an introduction pipe 214 through which the synthesis gas X1 sent from the gasification furnace 116 flows are connected. The synthesis gas inlet 220a communicates with the first flow path portion A, and the synthesis gas inlet 220b communicates with the second flow path portion B.

  Further, on the top surface of the main body 210, synthesis gas outlets 222a and 222b to which a discharge pipe 216 for discharging the synthesis gas X2 oxidized and reformed in the main body 210 to the purifier 160 are connected. The synthesis gas outlet 222a communicates with the first flow path portion A, and the synthesis gas outlet 222b communicates with the second flow path portion B.

  Therefore, the synthesis gas X1 introduced into one of the first flow path part A and the second flow path part B passes through the communication part C, and the first flow path part A and the second flow path part B. It will be discharged | emitted from either one of these to the outside.

  Further, a valve 214a is provided for the introduction pipe 214 connected to the synthesis gas inlet 220a, a valve 214b is provided for the introduction pipe 214 connected to the synthesis gas inlet 220b, and a valve is provided for the discharge pipe 216 connected to the synthesis gas outlet 222a. A valve 216b is provided in the discharge pipe 216 where the 216a is connected to the synthesis gas outlet 222b. The valves 214a, 214b, 216a, 216b are controlled to be opened and closed by a control unit 290 described later. The opening / closing control of the valves 214a, 214b, 216a, 216b by the control unit 290 will be described in detail later.

  The first heat storage body 230a and the second heat storage body 230b are made of ceramics such as cordierite, alumina, mullite, and silica, for example, and store the heat of the synthesis gas X2 or radiate it to preheat the synthesis gas X1. It has a function to do. The first heat storage body 230a is provided below the synthesis gas inlet 220a and the synthesis gas outlet 222a in the first flow path section A and above the communication section C, and the second heat storage body 230b is connected to the second flow path. It is provided below the synthesis gas inlet 220b and the synthesis gas outlet 222b in the part B and above the communication part C.

  The oxidant supply unit 240 includes a first oxidant supply unit 240a and a second oxidant supply unit 240b, and circulates through the first flow path unit A in accordance with a control command from the control unit 290. The oxidizing gas is supplied to the synthesis gas X1 preheated by the first heat storage body 230a in the process or the synthesis gas X1 preheated by the second heat storage body 230b in the process of flowing through the second flow path part B.

  More specifically, the first oxidant supply unit 240a is disposed vertically below the first heat storage body 230a in the first flow path part A and above the communication part C, and the first flow path part A An oxidant is supplied vertically below the first heat storage body 230a. The second oxidant supply unit 240b is arranged vertically below the second heat storage body 230b in the second flow path part B and above the communication part C, and supplies the oxidant vertically below the second heat storage body 230b. To do.

  Here, the oxidizing agent is a gas (for example, oxygen, air) containing at least oxygen. In the present embodiment, the first oxidant supply unit 240a and the second oxidant supply unit 240b are driven and controlled by the control unit 290. The drive control of the oxidant supply unit 240 (first oxidant supply unit 240a, second oxidant supply unit 240b) by the control unit 290 will be described in detail later.

  When the oxidant supply unit 240 supplies the oxidant, hydrogen contained in the synthesis gas X1 burns, and the synthesis gas X1 can be heated to about 1100 ° C. to 1500 ° C. With the configuration in which the synthesis gas X1 is set to about 1100 ° C. to 1500 ° C., tar contained in the synthesis gas X1 can be removed by oxidation reforming. Moreover, the ash contained in the synthesis gas X1 can be melted and removed as molten slag by setting the synthesis gas X1 to about 1100 ° C. to 1500 ° C. The molten slag generated in this way falls to the slag storage part 250 communicated below the communication part C.

  As shown in FIG. 2, in the present embodiment, the communication portion C has a tapered shape in which the horizontal sectional area gradually decreases as it goes vertically downward. For this reason, the molten slag generated by supplying the oxidizing agent by the oxidant supply unit 240 can be aggregated in the communication part C, and the aggregated molten slag can be collected in the main body 210 constituting the communication part C. It is possible to flow down along the wall surface and drop into the slag reservoir 250. Accordingly, the molten slag can be smoothly dropped into the slag storage unit 250, and accumulation of the molten slag in the main body 210 can be suppressed.

  The slag storage part 250 is comprised by the water tank, for example, and is provided under the communicating part C in the main body 210. The slag storage unit 250 stores water in advance, and the molten slag that has dropped through the communication unit C is cooled with water, solidified, and stored. The molten slag stored in the slag storage unit 250 is discharged to the outside by a carry-out device (not shown).

  The auxiliary burner 260 is provided in the communication part C and heats the molten slag. The auxiliary burner 260 heats the molten slag when the temperature of the communication part C detected by the temperature detection part 270 becomes lower than a predetermined temperature according to the control command of the control part 290. Here, the predetermined temperature is a minimum temperature at which the fluidity of the molten slag can be sufficiently secured, and is 1200 ° C., for example.

  With the configuration including the auxiliary burner 260, the fluidity of the molten slag can be ensured, and the situation where the molten slag accumulates on the wall surface of the main body 210 constituting the communication portion C can be avoided.

  The temperature measurement unit 280 measures the temperature of the synthesis gas X2 discharged from the synthesis gas outlets 222a and 222b.

  The control unit 290 is composed of a semiconductor integrated circuit including a CPU (Central Processing Unit), reads programs and parameters for operating the CPU itself from the ROM, and cooperates with the RAM as a work area and other electronic circuits. Thus, the entire oxidation reformer 150 is managed and controlled. In the present embodiment, the control unit 290 drives and controls the auxiliary burner 260 based on the temperature of the communication unit C detected by the temperature detection unit 270 as described above.

  The control unit 290 functions as a switching unit that switches the flow path of the synthesis gas X1, and controls the opening and closing of the valves 214a, 214b, 216a, and 216b based on the temperature of the synthesis gas X2 measured by the temperature measurement unit 280. The first oxidant supply unit 240a and the second oxidant supply unit 240b are driven and controlled.

  3 and 4 are diagrams for explaining control of the valves 214a, 214b, 216a, and 216b, the first oxidant supply unit 240a, and the second oxidant supply unit 240b by the control unit 290. FIG. First, when starting the oxidation reformer 150, the valves 214a, 214b, 216a, 216b are opened, and a purging gas (for example, air) is circulated through the main body 210 instead of the synthesis gas X1. Then, a temperature raising burner (not shown) provided at substantially the same position as the first oxidant supply unit 240a and the second oxidant supply unit 240b is driven to raise the temperature in the main body 210. When the temperature in the main body 210 reaches about 1200 ° C., the oxidation reforming of the synthesis gas X1 is started.

  In the following, the flow direction of the synthesis gas X1 from the first heat storage body 230a side to the second heat storage body 230b side, that is, in order from the upstream side, the first flow path section A, the communication section C, the second flow The direction in which the passage B is circulated is referred to as a first direction, and the second flow path is sequentially arranged from the upstream side to the circulation direction of the synthesis gas X1 from the second heat storage body 230b side to the first heat storage body 230a side. The direction in which the part B, the communication part C, and the first flow path part A circulate is referred to as a second direction.

  When starting the oxidation reforming of the synthesis gas X1, for example, the control unit 290 first closes the valve 214b and the valve 216a (shown in black in FIG. 3) as shown in FIG. The introduction of the synthesis gas X1 is started from 214, and the first oxidant supply unit 240a is driven.

  Then, as shown by the solid line arrow in FIG. 3, the synthesis gas X1 flows through the main body 210 in the first direction. That is, the synthesis gas X1 includes the synthesis gas inlet 220a, the first heat storage body 230a (first flow path section A), the first oxidant supply section 240a, the communication section C, and the second heat storage body 230b (second flow path). Part B) and the synthesis gas outlet 222b in this order are discharged to the discharge pipe 216.

  Then, the synthesis gas X1 before the oxidation reforming can be preheated by the first heat storage body 230a heated to about 1200 ° C. at the time of startup. Therefore, it is possible to reduce the amount of oxidant that is supplied by the first oxidant supply unit 240a and that is required to raise the temperature to the temperature necessary for oxidative reforming (about 1100 ° C. to 1500 ° C.). Thereby, the cost which an oxidizing agent requires can be reduced.

  Then, when the temperature of the synthesis gas X2 measured by the temperature measurement unit 280 is equal to or higher than a predetermined temperature, the control unit 290 maintains the introduction of the synthesis gas X1 from the introduction pipe 214 as shown in FIG. The valve 214a and the valve 216b are closed (shown in black in FIG. 4), the valve 214b and the valve 216a are opened, and the second oxidant supply unit 240b is driven. Here, the predetermined temperature is a value that can be regarded as the lowest value of the temperature of the second heat storage body 230b that can sufficiently preheat the synthesis gas X1 after switching the flow path, and is, for example, about 600 ° C. to 900 ° C. .

  Then, as shown by the solid line arrow in FIG. 4, the synthesis gas X <b> 1 flows through the main body 210 in the second direction. That is, the synthesis gas X1 includes the synthesis gas inlet 220b, the second heat storage body 230b (second flow path section B), the second oxidant supply section 240b, the communication section C, and the first heat storage body 230a (first flow path). Part A) and the synthesis gas outlet 222a are discharged in this order to the discharge pipe 216.

  Then, the synthesis gas X1 before the oxidation reforming can be preheated by the second heat storage body 230b heated to about 1200 ° C. in the operation shown in FIG. Accordingly, it is possible to reduce the amount of oxidant that is supplied by the second oxidant supply unit 240b and that is required to raise the temperature to the temperature necessary for oxidation reforming (about 1100 ° C. to 1500 ° C.). Thereby, the cost which an oxidizing agent requires can be reduced.

  Then, when the temperature of the synthesis gas X2 measured by the temperature measurement unit 280 is equal to or higher than the predetermined temperature, the control unit 290 maintains the introduction of the synthesis gas X1 from the introduction pipe 214 as shown in FIG. The valves 214b and 216a are closed, the valves 214a and 216b are opened, and the first oxidant supply unit 240a is driven. Thereafter, the state shown in FIG. 3 according to the temperature of the synthesis gas X2 measured by the temperature measurement unit 280. Then, the state shown in FIG. 4 is repeated.

  In other words, the control unit 290 switches the flow direction of the synthesis gas X1 between the first direction (the direction shown in FIG. 3) and the second direction (the direction shown in FIG. 4).

  As described above, according to the oxidation reforming apparatus 150 according to the present embodiment, the first heat storage body 230a and the second heat storage body 230b are alternately heated by the configuration in which the flow path of the synthesis gas X1 is switched, The synthesis gas X1 before the oxidation reforming can always be preheated by the heated heat accumulator. As a result, it is possible to reduce the amount of oxidant supplied by the oxidant supply unit 240 (the first oxidant supply unit 240a and the second oxidant supply unit 240b).

  In addition, as described above, in the oxidation reformer 150 according to the present embodiment, the first heat storage body 230a, the first oxidant supply unit 240a, the slag storage unit 250, or the second heat storage body 230b in order from the vertically upper side. The second oxidant supply unit 240b and the slag storage unit 250 are disposed. That is, the first heat storage body 230a and the second heat storage body 230b are supplied from the first oxidant supply unit 240a and the second oxidant supply unit 240b (the supply point where the oxidant supply unit 240 supplies the oxidant). It is provided outside the fall trajectory range of the molten slag.

  With this configuration, the molten slag generated by the first oxidant supply unit 240a and the second oxidant supply unit 240b does not contact the first heat storage body 230a and the second heat storage body 230b, and the first heat storage body 230a, The situation where the 2nd thermal storage body 230b is obstruct | occluded with molten slag can be avoided.

(Modification)
In the above-described embodiment, the configuration in which the slag reservoir 250 is located directly below the communication part C, that is, directly below the partition wall 212 has been described. However, the first heat accumulator 230a and the second heat accumulator 230b are formed of the molten slag from the supply locations (the first oxidant supply unit 240a and the second oxidant supply unit 240b) where the oxidant supply unit 240 supplies the oxidant. There is no limitation on the position of the slag reservoir 250 as long as it is disposed outside the fall locus range. For example, as shown in FIG. 5, an oxidation reformer provided with a slag reservoir 250 whose position in the horizontal direction with respect to the main body 210 (X-axis direction in FIG. 5) is biased toward the second flow path B from the partition wall 212. Quality device 350 may be used. In this case, the number of auxiliary burners 260 may be one.

  As mentioned above, although preferred embodiment of this invention was described referring an accompanying drawing, it cannot be overemphasized that this invention is not limited to this embodiment. It will be apparent to those skilled in the art that various changes and modifications can be made within the scope of the claims, and these are naturally within the technical scope of the present invention. Is done.

  For example, in the above-described embodiment, the configuration in which the first channel portion A and the second channel portion B extend in the vertical direction has been described. However, the first flow path portion A and the second flow path portion B do not necessarily extend in the vertical direction, and may extend in the horizontal direction, for example. As long as at least the first heat storage body 230a disposed in the first flow path section A and the second heat storage body 230b disposed in the second flow path section B are provided outside the fall trajectory range of the molten slag. Good.

  Moreover, in the said embodiment, the vertical position of the 1st heat storage body 230a and the 2nd heat storage body 230b was equal (or substantially equal), and the structure from which the position of a horizontal direction differs was demonstrated. However, in the second heat storage body 230b, the oxidizing agent supply unit 240 supplies the oxidizing agent on the flow path of the synthesis gas X1 and outside the range of the fall trajectory of the molten slag and in the flow direction of the synthesis gas X1. What is necessary is just to be provided in the opposite side to the 1st thermal storage body 230a on the boundary of a supply location. Therefore, the first heat storage body 230a and the second heat storage body 230b may have the same horizontal position (or substantially the same position) and different vertical positions.

  In the above-described embodiment, when the first flow path portion A and the second flow path portion B are provided in parallel via the partition wall 212 and the flow direction is the first direction, The heat of the synthesis gas X2 flowing through the second flow path portion B can be transferred to the synthesis gas X1 flowing through the first flow path portion A via the partition wall 212, and the flow direction is the second direction. In this case, the structure in which the heat of the synthesis gas X2 flowing through the first flow path part A can be transmitted to the synthesis gas X1 flowing through the second flow path part B via the partition wall 212, that is, the partition wall 212 Thus, the configuration in which heat exchange is possible between the synthesis gas flowing through the first flow path portion A and the synthesis gas flowing through the second flow path portion B has been described as an example. However, the first flow path part A and the second flow path part B may be separated as long as they are arranged in parallel. Moreover, the 1st flow path part A and the 2nd flow path part B do not need to be distribute | arranged in parallel. It is sufficient that at least the first heat storage body 230a and the second heat storage body 230b are provided outside the fall trajectory range of the molten slag.

  In the embodiment described above, the configuration in which the temperature measurement unit 280 measures the temperature of the synthesis gas X2 discharged from the synthesis gas outlets 222a and 222b has been described. However, when the flow direction of the synthesis gas X1 is the first direction, the temperature measurement unit 280 measures the temperature of the synthesis gas X2 after the heat exchange with the second heat storage body 230b, and the second If the temperature of the synthesis gas X2 after heat exchange with the first heat storage body 230a can be measured, the measurement position is not limited.

  Moreover, in the said embodiment, the control part 290 was the temperature of the synthesis gas X2 which the temperature measurement part 280 measured, and whether the heat storage body (the 1st heat storage body 230a or the 2nd heat storage body 230b) was fully heated indirectly. However, the temperature measurement unit 280 may directly measure the temperature of the heat storage body (the first heat storage body 230a or the second heat storage body 230b).

  In the above-described embodiment, the oxidation reformer 150 includes the synthesis gas inlets 220a and 220b and the synthesis gas outlets 222a and 222b, and the control unit 290 controls opening and closing of the valves 214a, 214b, 216a, and 216b. By driving and controlling the first oxidant supply unit 240a and the second oxidant supply unit 240b, the first direction and the second direction are switched. However, the top surface of the main body 210 is provided with two through holes, that is, a first passage port communicating with the first flow path portion A and a second passage port communicating with the second flow path portion B. In addition, the control unit 290 functions as a first direction by causing the first passage port to function as a synthesis gas inlet and the second passage port as a synthesis gas outlet, and to function as the second passage port as a synthesis gas inlet. And the second direction in which the first passage port functions as the synthesis gas outlet may be switched.

  In the above-described embodiment, the first heat storage body 230a and the second heat storage body 230b are configured separately, and are fixedly installed on the main body 210, and the control unit 290 includes the valves 214a, 214b, 216a, By controlling the opening and closing of 216b, the flow paths of the synthesis gas X1 and X2 are switched, and the first heat storage body 230a and the second heat storage body 230b are alternately heated, and before the oxidation reforming by the heated heat storage body The configuration for always preheating the synthesis gas X1 has been described. However, you may comprise a 1st heat storage body and a 2nd heat storage body integrally. In this case, the flow direction of the synthesis gas X1 and X2 is fixed (for example, the first direction), and the one part of the heat storage body and the other part are alternated by rotating the heat storage body configured integrally. The synthesis gas X1 before oxidation reforming may be always preheated by the heated portion of the heat storage body.

  In the above-described embodiment, the case of oxidizing and reforming tar in the synthesis gas X1 generated in the gasification furnace 116 using steam as a gasifying agent has been described as an example. However, the embodiment is limited to the gasifying agent. For example, nitrogen may be used.

  INDUSTRIAL APPLICABILITY The present invention can be used for an oxidation reformer that oxidizes and reforms tar contained in synthesis gas generated by gasifying a gasification raw material.

A 1st flow path part B 2nd flow path part C Communication part 150, 350 Oxidation reformer 210 Main body 230a 1st heat storage body 230b 2nd heat storage body 240 Oxidant supply part 240a 1st oxidant supply part 240b 1st Dioxidant supply unit 250 Slag storage unit 260 Auxiliary burner 280 Temperature measurement unit 290 Control unit (switching means)

Claims (5)

An oxidation reforming apparatus that oxidizes and reforms synthesis gas generated by gasifying a gasification raw material,
A first heat storage body, and a first flow path section through which the synthesis gas flows, the first heat storage body and a first oxidizer supply section that is disposed vertically below the first heat storage body and supplies an oxidizer,
A second heat storage body, and a second flow path section through which the synthesis gas flows, the second heat storage body being provided vertically below the second heat storage body and supplying a second oxidizing agent supply section.
A communication part that communicates the first flow path part and the second flow path part below the first oxidant supply part and the second oxidant supply part;
And the slag reservoir portion that is disposed below the previous Symbol communicating portion,
Switching for switching the flow direction of the synthesis gas between a first direction from the first heat storage body side to the second heat storage body side and a second direction from the second heat storage body side to the first heat storage body side. Means,
Oxidation reformer, wherein the obtaining Bei a. When the flow direction of the synthesis gas is the first direction, the temperature of the synthesis gas after heat exchange with the second heat storage body is measured, and the flow direction of the synthesis gas is the second direction. A temperature measuring unit for measuring the temperature of the synthesis gas after heat exchange with the first heat storage body,
The switching means is
When the flow direction of the synthesis gas is the first direction, the temperature of the synthesis gas after the heat exchange with the second heat storage body measured by the temperature measurement unit is a predetermined temperature. If it is above, the flow direction of the synthesis gas is switched to the second direction,
When the flow direction of the synthesis gas is the second direction, the temperature of the synthesis gas after the heat exchange with the first heat storage body measured by the temperature measurement unit is determined in advance. When a temperature above the oxidation reforming apparatus according to claim 1, characterized in that switching the flow direction of the synthesis gas to the first direction. 3. The oxidation reformer according to claim 1, wherein the first flow path portion and the second flow path portion extend in a vertical direction and are provided in parallel with each other. Quality equipment. The communication part communicates with the slag storage part,
The oxidation reforming apparatus according to claim 3 , wherein the oxidation reforming apparatus has a tapered shape in which a horizontal cross-sectional area gradually decreases as it goes vertically downward. The oxidation reforming apparatus according to claim 4 , further comprising an auxiliary burner provided in the communication portion and heating the molten slag.

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