JP6822025B2 - Tar reformer - Google Patents

Description

The present disclosure relates to a tar reformer that reforms tar in syngas.

In recent years, instead of petroleum, a technology for producing synthetic gas by gasifying raw materials such as coal, biomass, and unused fuel such as tire chips has been developed. The synthetic gas produced in this way is used in power generation systems, hydrogen production, synthetic fuel (synthetic petroleum) production, chemical fertilizer (urea) and other chemical products. Of the raw materials for synthetic gas, coal has a recoverable life of about 100 years, which is more than double the recoverable age of petroleum, and the reserves are not unevenly distributed compared to petroleum, so it is a long-term source. It is expected as a natural resource that can be stably supplied over the years.

Conventionally, the gasification process of coal has been carried out by partial oxidation using oxygen or air. However, the conventional gasification process has a drawback that the cost of the gasification furnace is high because it is necessary to partially oxidize at a high temperature of 2000 ° C.

In order to solve this problem, a technique for gasifying coal at about 700 ° C. to 900 ° C. using steam (steam gasification) has been developed. In this steam gasification technology, it is possible to reduce the cost by setting the temperature low. However, the generated synthetic gas contains a large amount of tar as compared with the synthetic gas produced by partial oxidation at a high temperature of 2000 ° C. Therefore, when the temperature of the synthetic gas drops in the process of using the synthetic gas generated by steam gasification, the tar contained in the synthetic gas condenses, causing blockage of pipes, failure of equipment used in the process, and poisoning of the catalyst. Etc. will occur.

Therefore, a technique has been developed in which tar contained in the synthetic gas is removed by bringing the synthetic gas into contact with the catalyst and modifying the tar with the catalyst (for example, Patent Document 1). In the technique of Patent Document 1, in order to raise the synthetic gas to the active temperature of the catalyst, an oxidizing agent is supplied to the synthetic gas to burn a part of the synthetic gas.

Japanese Unexamined Patent Publication No. 2014-205582

In the technique of Patent Document 1 described above, diffusion combustion may occur when an oxidizing agent is supplied to the synthetic gas, and soot may be generated from hydrocarbons and tar in the synthetic gas. In this case, soot causes a problem in the operation of the device.

In view of such problems, the present disclosure aims to provide a tar reformer capable of reducing the amount of soot generated.

In order to solve the above problems, the tar reformer communicates with the large-diameter space into which the synthetic gas is introduced and the downstream end of the large-diameter space, and the cross-sectional area of the flow path gradually decreases from the upstream side to the downstream side. The squeezing space is communicated with the downstream end of the squeezing space, and is communicated with the small diameter space having a smaller diameter than the large diameter space and the downstream end of the small diameter space, and the flow path cross-sectional area gradually increases from the upstream side to the downstream side. has a larger space, the at least the duct of premixed gas containing synthesis gas and the oxidant passes through a baffle plate provided in said duct, the oxidizing agent downstream of the baffle plate in the duct an oxidant supply device for supplying said diaphragm to introduce an oxidizing agent into the space and a premixed gas generator generating the premixed gas in the small diameter space, the oxidizing oxidant supplier supplies The flow rate of the agent is smaller than the flow rate of the oxidant introduced by the premixture generation unit .

It is possible to reduce the amount of soot generated.

It is a figure for demonstrating the synthetic gas generator. It is a figure for demonstrating the tar reformer. It is a figure explaining the duct, the premixture generation part, and the soot generation suppression apparatus. It is a figure explaining the soot generation suppression apparatus. It is a figure explaining the obstacle board concerning the modification. It is a figure explaining the temperature change of the premixture between an Example and a comparative example.

The embodiment will be described in detail with reference to the accompanying drawings. The dimensions, materials, other specific numerical values, etc. shown in such an embodiment are merely examples for facilitating understanding, and do not limit the present disclosure unless otherwise specified. In the present specification and drawings, elements having substantially the same function and configuration are designated by the same reference numerals to omit duplicate description, and elements not directly related to the present disclosure are omitted from the illustration. To do.

(Syngas generator 100)
FIG. 1 is a diagram for explaining the syngas generator 100. As shown in FIG. 1, the syngas generator 100 includes a combustion furnace 112, a medium separation device (cyclone) 114, a gasification furnace 116, a tar reformer 200, and a purification device 300. To. In FIG. 1, the flow of raw materials is indicated by dashed arrows, the flow of gas is indicated by solid arrows, and the flow of fluidized medium (sand) is indicated by dashed arrows.

In the syngas generator 100, a fluid medium composed of sand such as quartz sand (silica sand) having a particle size of about 300 μm is circulated as a heat medium as a whole. Specifically, first, the flow medium is heated to about 900 ° C. to 1000 ° C. in the combustion furnace 112. The fluid medium heated in the combustion furnace 112 is introduced into the medium separator 114 together with the combustion exhaust gas containing carbon dioxide (CO ₂ ). In the medium separating device 114, the high-temperature fluid medium and the combustion exhaust gas are separated. The separated hot fluid medium is introduced into the gasifier 116. Then, the fluidized medium introduced into the gasification furnace 116 is fluidized by the gasifying agent (water vapor) introduced from the bottom surface of the gasification furnace 116, and then finally returned to the combustion furnace 112. Further, the combustion exhaust gas separated by the medium separating device 114 is heat-recovered by a boiler or the like.

The gasification furnace 116 is, for example, a bubble fluidized bed gasification furnace which is a kind of a circulating fluidized bed system. The gasification furnace 116 gasifies the raw material at 700 ° C. to 900 ° C. to generate a synthetic gas. The raw materials are, for example, coal such as lignite, solid raw materials such as petroleum coke (petro coke), biomass and tire chips, and liquid raw materials such as black liquor. In the present embodiment, by supplying steam to the gasification furnace 116, the raw material is gasified to generate a synthetic gas (steam gasification).

Here, the gasification furnace 116 will be described by taking the circulating fluidized bed method as an example. However, if the raw material can be gasified, the configuration of the gasification furnace 116 is not limited. For example, the gasification furnace 116 may be a simple bubble fluidized bed system or a mobile bed system in which sand flows down vertically due to its own weight to form a moving bed.

The synthetic gas GG1 generated in the gasification furnace 116 contains tar, steam and the like. Therefore, the synthetic gas GG1 is introduced into the tar reformer 200 described later, and the tar is reformed by the tar reformer 200. The tar-modified synthetic gas GG2 in the tar reformer 200 is further refined in the purification device 300. Further, the char (raw material residue) generated in the gasification furnace 116 is introduced into the combustion furnace 112 together with the flow medium and burned in the combustion furnace 112.

The purification device 300 includes a heat exchanger, a spray tower, a mist separator, a pressurizer, a desulfurization device, a denitration device, a desalination device, and the like, and purifies the synthetic gas GG2. The heat exchanger cools the synthetic gas GG2 delivered from the tar reformer 200. The spray tower sprays water on the syngas cooled by the heat exchanger to remove residual tar and sludge. The mist separator sprays synthetic gas with atomized water to further remove residual tar and sludge. The booster boosts the synthetic gas from which residual tar and sludge have been removed. The desulfurization equipment removes sulfide from syngas. The denitration device removes nitrides from syngas. The desalting device removes chloride from the syngas.

(Tar reformer 200)
Subsequently, a specific configuration of the tar reformer 200 will be described. FIG. 2 is a diagram for explaining the tar reformer 200, and FIG. 3 is a diagram for explaining the duct 210, the premixture generation unit 220, and the soot generation suppression device 260. In the following figures including FIGS. 2 and 3 of the present embodiment, the vertically intersecting X-axis (horizontal direction), Y-axis (horizontal direction), and Z-axis (vertical direction) are defined as shown in the figure. Further, in FIG. 2, the synthetic gas GG1 generated in the gasifier 116 is indicated by a black filled arrow, the premixed gas KG of the synthetic gas GG1 and the oxidizing agent is indicated by a cross-hatching arrow, and the synthetic gas GG1 is modified. The quality of the synthetic gas GG2 is indicated by a white arrow. Further, in FIG. 3, the synthetic gas GG1 generated in the gasifier 116 is indicated by a black arrow, the premixed gas KG of the synthetic gas GG1 and the oxidant is indicated by a cross-hatching arrow, and the oxidant is outlined. It is indicated by an arrow.

As shown in FIG. 2, the tar reformer 200 includes a duct 210, a premixture generation unit 220, a reformer 230, a flow path cross-sectional area changing unit 240, a catalyst holding unit 250, and soot generation suppression. It is configured to include the device 260.

The duct 210 is a pipe that connects the gasification furnace 116 and the reforming furnace 230, which will be described later. The duct 210 is a pipe whose YZ cross section is bent in an L shape in FIG. 2, and includes an upstream pipe 212 and a downstream pipe 214. The upstream pipe 212 is a pipe extending in the vertical direction (Z-axis direction in FIG. 2), one end of which is connected to the gasifier 116 and the other end of which is connected to the downstream pipe 214. Further, the flow path cross-sectional area of the upstream pipe 212 (XY cross-sectional area in FIG. 2, inner diameter) is substantially the same in the vertical direction.

The downstream pipe 214 is a pipe extending in the horizontal direction (Y-axis direction in FIG. 2), one end of which is connected to the upstream pipe 212 and the other end of which is connected to the introduction port 232 of the reforming furnace 230. As shown in FIG. 3, the downstream pipe 214 has a large diameter space 214a and a drawing space 214b from the upstream side (upstream pipe 212 side) to the downstream side (reformer 230 side) in the flow direction of the synthetic gas GG1. A small diameter space 214c, an enlarged space 214d, and a medium diameter space 214e are formed inside.

One end (upstream end) of the large-diameter space 214a communicates with the internal space of the upstream pipe 212, and the other end (downstream end) communicates with the throttle space 214b. The flow path cross-sectional area (XZ cross-sectional area, diameter in FIG. 2) of the large-diameter space 214a is substantially the same over the horizontal direction. One end (upstream end) of the aperture space 214b communicates with the downstream end of the large diameter space 214a, and the other end (downstream end) communicates with the small diameter space 214c. The throttle space 214b is configured such that the flow path cross-sectional area (XZ cross-sectional area, diameter in FIG. 2) gradually decreases from one end to the other end. In the small diameter space 214c, one end (upstream end) is communicated with the downstream end of the aperture space 214b, and the other end (downstream end) is communicated with the enlarged space 214d. The flow path cross-sectional area of the small diameter space 214c (XZ cross-sectional area, diameter in FIG. 2) is substantially equal to the flow path cross-sectional area of the other end of the throttle space 214b, and is substantially the same in the horizontal direction.

One end (upstream end) of the expanded space 214d communicates with the downstream end of the small diameter space 214c, and the other end (downstream end) communicates with the medium diameter space 214e. The enlarged space 214d is configured such that the flow path cross-sectional area (XZ cross-sectional area, diameter in FIG. 2) gradually increases from one end to the other end. The flow path cross-sectional area at one end of the enlarged space 214d is substantially equal to the flow path cross-sectional area of the small diameter space 214c. One end (upstream end) of the medium-diameter space 214e is communicated with the downstream end of the expanded space 214d, and the other end (downstream end) is communicated with the introduction port 232 of the reformer 230. The flow path cross-sectional area of the medium-diameter space 214e (XZ cross-sectional area, diameter in FIG. 2) is substantially equal to the flow path cross-sectional area of the other end of the enlarged space 214d, and is substantially the same in the horizontal direction.

The premixture generation unit 220 blows the oxidizing agent into the throttle space 214b in the downstream pipe 214 at a high speed (for example, about 139 m / s). Specifically, the premixture generation unit 220 is configured to include the nozzle 222, and is provided so that the tip of the nozzle 222 is located in the throttle space 214b. Here, the oxidizing agent is, for example, oxygen or air.

When the premixture generation unit 220 blows the oxidizing agent into the downstream pipe 214, the small diameter space 214c becomes low pressure due to the ejector effect. Then, the synthetic gas GG1 (for example, about 800 ° C.) is mixed from the gasifier 116 into the downstream pipe 214 (for example, about 4.8 m / s), and the synthetic gas GG1 and the oxidizing agent are predicted in the downstream pipe 214. The air-fuel mixture KG will be generated.

In the internal space of the downstream pipe 214 (large diameter space 214a, throttle space 214b, small diameter space 214c, enlarged space 214d, medium diameter space 214e), the synthetic gas GG1 in the premixed gas KG and the oxidizing agent are rapidly burned. The premixture KG is designed to flow at a flow velocity higher than the propagation velocity of the flame generated by the reaction. As a result, it is possible to prevent the generation of flame (avoid a sudden temperature rise) and prevent the generation of soot, while preventing flashback (a phenomenon in which the flame propagates to the upstream side).

The premixture KG thus generated is modified after the flow velocity becomes high in the throttle space 214b (for example, about 17 m / s) and the flow velocity becomes low in the expansion space 214d (for example, about 8.8 m / s). It will be introduced into the furnace 230.

Returning to FIG. 2, the reforming furnace 230 includes a cylindrical outer wall portion 230a, an upper wall portion 230b forming the upper surface of the outer wall portion 230a, and a lower wall portion 230c forming the lower surface of the outer wall portion 230a. Consists of including. The reforming furnace 230 is provided so that the axis of the outer wall portion 230a is in the vertical direction (Z-axis direction in FIG. 2). The outer wall portion 230a is provided with an introduction port 232 through which the premixed gas KG of the synthetic gas GG1 and the oxidizing agent is guided, and a synthetic gas GG2 provided below the introduction port 232 and reformed in the reforming furnace 230. The outlet 234 is provided. Therefore, a flow passage 236 through which the premixed gas KG and the synthetic gas GG2 flow is formed between the introduction port 232 and the delivery port 234 in the reforming furnace 230. The premixed air KG will flow through the flow passage 236 from the introduction port 232 toward the delivery port 234.

Since the flow path cross-sectional area of the flow passage 236 (XY cross-sectional area in FIG. 2) is larger than the flow path cross-sectional area of the medium-diameter space 214e, the premixed air KG introduced into the reforming furnace 230 from the introduction port 232. The flow velocity is low (for example, about 1.9 m / s). Then, the combustion reaction between the synthetic gas GG1 in the premixed gas KG and the oxidizing agent is rapidly promoted to generate a flame, and the temperature of the premixed gas KG rises to about the active temperature of the catalyst holding portion 250 described later. It becomes.

The flow path cross-sectional area changing portion 240 is a ring-shaped member provided between the introduction port 232 and the delivery port 234 on the inner peripheral surface of the outer wall portion 230a. The flow path cross-sectional area changing portion 240 flows from the upper wall portion 230b toward the lower wall portion 230c toward the narrowing portion 242a that gradually reduces the flow path cross-sectional area of the flow passage 236, and from the narrowing portion 242a toward the lower wall portion 230c. It is composed of a top portion 242b in which the road cross-sectional area is substantially constant, and an enlarged portion 242c in which the flow path cross-sectional area is gradually increased from the top portion 242b toward the lower wall portion 230c.

With the configuration including the flow path cross-sectional area changing portion 240, the premixed air KG can be recirculated below the expanding portion 242c. Therefore, it is possible to promote the combustion reaction between the synthetic gas GG1 and the oxidizing agent. Therefore, it is possible to avoid a situation in which the oxidizing agent in the premixture KG flows into the catalyst holding unit 250 without reacting, soot generation is reduced, and the temperature of the premixture KG is raised (synthesis). (Promotes the combustion reaction between the gas GG1 and the oxidizing agent).

The catalyst holding unit 250 holds a catalyst that promotes the modification of tar in the flow passage 236. Here, the catalyst is composed of at least Ni (nickel). The catalyst can reform the tar in the premixture KG by contacting with the premixture KG in an environment (atmosphere) of an active temperature.

In this way, the synthetic gas GG2 whose tar has been modified (removed) by the catalyst holding unit 250 is supplied to the purification apparatus 300 through the delivery port 234.

As described above, when the premixed gas KG is introduced into the reforming furnace 230 from the introduction port 232, a rapid temperature rise (flame) occurs in the reforming furnace 230 due to the decrease in the flow velocity. Then, hydrocarbons and tar in the synthetic gas GG1 may become soot. In this case, the soot may cause problems such as blockage of the flow path and piping between the catalysts and failure of the equipment constituting the purification apparatus 300.

Therefore, the tar reformer 200 of the present embodiment includes a soot generation suppressing device 260. The soot generation suppressing device 260 is configured to include a supply pipe (oxidizing agent supply device) 262 and a baffle plate 264.

FIG. 4 is a diagram illustrating a soot generation suppressing device 260. 4 (a) is a sectional view taken along line IVa-IVa in FIG. 3, FIG. 4 (b) is an enlarged view of the soot generation suppressing device 260, and FIG. 4 (c) is a perspective view of the soot generation suppressing device 260. Is. In FIG. 4A, the premixture KG is indicated by a solid arrow, and the oxidizing agent is indicated by a broken line arrow. Further, in FIG. 4A, the premixture generation unit 220 is omitted for ease of understanding.

As shown in FIG. 4A, the supply pipe 262 is arranged so that the tip is located in the small diameter space 214c. Further, as shown in FIGS. 4 (b) and 4 (c), an opening 262a is formed in the vicinity of the tip of the supply pipe 262 so that the opening 262a faces the downstream side (introduction port 232 side). Will be installed. The supply pipe 262 supplies the oxidant into the downstream pipe 214 through the opening 262a. The flow rate of the oxidant supplied by the supply pipe 262 (introduction amount per unit time) is smaller than the flow rate of the oxidant introduced by the premixture generation unit 220, for example, about 1/10. That is, the supply pipe 262 supplies a smaller amount of the oxidant to the premixed KG than the oxidant in the premixed KG.

The baffle plate 264 is a plate having a V-shaped horizontal cross section (XY cross section in FIG. 4), and is installed in the small diameter space 214c so that the top portion 264a is arranged on the upstream side (large diameter space 214a side). In the present embodiment, the baffle plate 264 is fixed by being welded to the supply pipe 262. Specifically, the top 264a of the baffle plate 264 is fixed to the supply pipe 262 so as to be arranged on the upstream side of the opening 262a of the supply pipe 262. That is, the oxidizing agent is supplied from the downstream side of the baffle plate 264. The size of the baffle plate 264 is not limited, but is, for example, a size that occupies 1/2 of the flow path cross-sectional area of the small diameter space 214c.

With the configuration including the baffle plate 264, the premixed air KG flowing on the upstream side of the baffle plate 264 collides with the baffle plate 264, and the premixed air KG can be recirculated on the downstream side of the baffle plate 264. That is, a vortex in the direction opposite to the main flow of the premixed air KG is formed on the downstream side of the baffle plate 264, and it is possible to reduce the flow velocity of a part of the premixed air KG. As a result, the combustion reaction of the synthetic gas GG1 in the premixed gas KG and the oxidizing agent on the downstream side of the baffle plate 264 in the downstream pipe 214 can proceed to the extent that no flame is generated. Therefore, it is possible to raise the temperature of the premixed gas KG in the downstream pipe 214 while avoiding a rapid temperature rise (without generating a flame).

Then, the premixed gas KG is introduced into the reforming furnace 230 after a part of the oxidizing agent is consumed in the downstream pipe 214. Therefore, the amounts of the synthetic gas GG1 (unreacted) and the oxidizing agent (unreacted) in the premixed gas KG introduced into the reforming furnace 230 are smaller than those without the baffle plate 264. As a result, even if the flow velocity of the premixed gas KG in the reforming furnace 230 decreases, the rapid combustion reaction can be suppressed, and the generation of flame can be suppressed. Therefore, the amount of soot generated can be reduced.

Further, if the combustion reaction does not proceed only by installing the baffle plate 264, the supply pipe 262 supplies a small amount of the oxidizing agent, so that the combustion reaction can proceed in the downstream pipe 214.

As described above, according to the tar reformer 200 according to the present embodiment, the temperature of the premixed air KG is higher than that of the configuration provided with the soot generation suppressing device 260 due to the configuration provided with the soot generation suppressing device 260. The rise (combustion reaction) can be made in multiple stages, and a rapid temperature rise (generation of flame) can be suppressed. Therefore, the tar reformer 200 according to the present embodiment can raise the temperature of the synthetic gas GG1 (premixed gas KG) while reducing the amount of soot generated.

(Modification example)
In the above embodiment, an example in which the baffle plate 264 is formed of a plate having a V-shaped horizontal cross section (XY cross section in FIG. 4) has been described. However, the baffle plate 264 is not limited in configuration as long as it can reduce the flow velocity of a part of the premixed air KG (form a recirculation region).

FIG. 5 is a diagram illustrating a baffle plate according to a modified example. FIG. 5A shows a horizontal sectional view of the baffle plate 264 according to the first modification, and FIG. 5B shows a perspective view of the baffle plate 264 according to the first modification. FIG. 5C shows a horizontal sectional view of the baffle plate 264 according to the second modification, and FIG. 5D shows a perspective view of the baffle plate 264 according to the second modification.

For example, as shown in FIGS. 5A and 5B, the baffle plate 264 may be formed of a plate having a semicircular horizontal cross section (XY cross section in FIG. 5). Further, as shown in FIGS. 5C and 5D, the baffle plate 264 may be formed of a triangular pyramid. Further, the baffle plate 264 may be formed of a simple flat plate.

(About temperature change of downstream pipe 214, flow passage 236, catalyst holding part 250)
Temperature change of premixture KG when the above tar reformer 200 is used (Example) and temperature change of premixture KG when a tar reformer without soot generation suppression device 260 is used (comparison). A simulation was performed for (example) and.

FIG. 6 is a diagram illustrating a temperature change of the premixed gas KG between the example and the comparative example. In FIG. 6, an embodiment is shown by a solid line, and a comparative example is shown by a broken line. Further, since the temperature change up to the baffle plate 264 and the temperature change after the flow path cross-sectional area changing portion 240 in the examples are the same as those in the comparative example, the description is omitted in FIG.

As shown in FIG. 6, in the comparative example, the temperature of the premixed air KG hardly rises in the duct 210. However, when introduced into the reformer 230, the temperature of the premixture KG rises to the temperature at which soot is produced by a rapid combustion reaction (soot generation temperature). Then, after the temperature of the premixture KG drops once and then reaches the flow path cross-sectional area changing portion 240, the temperature of the premixture KG rises again. After that, although the temperature of the premixed gas KG decreases, it is maintained above the active temperature in the catalyst holding portion 250.

On the other hand, in the embodiment, the temperature of the premixed air KG rises on the downstream side of the baffle plate 264 in the duct 210. However, unlike the comparative example, the temperature of the premixed gas KG does not reach the soot formation temperature. Then, once the temperature of the premixture KG is lowered and then introduced into the reforming furnace 230, the temperature of the premixture KG rises. However, even if it is introduced into the reforming furnace 230, unlike the comparative example, the temperature of the premixed gas KG does not reach the soot formation temperature because some oxygen has already been consumed. Then, after the temperature of the premixture KG drops once and then reaches the flow path cross-sectional area changing portion 240, the temperature of the premixture KG rises again. After that, although the temperature of the premixed gas KG decreases, it is maintained above the active temperature in the catalyst holding portion 250.

As described above, from the simulation results, it was confirmed that the temperature of the premixed gas KG did not rise to the soot formation temperature in the examples.

As described above, according to the tar reformer 200 according to the present embodiment, the temperature of the synthetic gas GG1 can be reduced while reducing the amount of soot generated by a simple configuration such as installing the soot generation suppressing device 260. It is possible to raise the temperature of the catalyst holding unit 250 to the active temperature. Therefore, the tar contained in the synthetic gas GG1 is reformed and removed while avoiding the situation where the flow path formed between the catalysts, the piping, the equipment constituting the purification apparatus 300, etc. are blocked by soot. Can be done.

Further, as described above, since the gasification furnace 116 performs steam gasification, the synthetic gas GG1 generated in the gasification furnace 116 contains a large amount of steam (for example, about 50%). Therefore, by bringing the catalyst into contact with the synthetic gas GG1, the tar in the mixed gas can be reacted with water vapor, and the tar can be reformed into hydrogen (H ₂ ), carbon monoxide (CO), or the like. It will be possible.

Although the embodiments have been described above with reference to the accompanying drawings, it goes without saying that the present disclosure is not limited to such embodiments. It is clear that a person skilled in the art can come up with various modifications or modifications within the scope of the claims, and it is understood that they also naturally belong to the technical scope.

For example, in the above embodiment, the configuration in which the soot generation suppressing device 260 includes an oxidizing agent supply device (supply pipe 262) has been described as an example. However, the soot generation suppressing device 260 may include at least a baffle plate 264.

Further, in the above embodiment, the configuration in which the tip of the supply pipe 262 is located in the small diameter space 214c has been described as an example. However, the supply pipe 262 may be located in the expanded space 214d or the medium diameter space 214e.

Further, in the above embodiment, the configuration including the flow path cross-sectional area changing section 240 has been described as an example, but the flow path cross-sectional area changing section 240 is not an essential configuration. Further, the configuration may include a plurality of flow path cross-sectional area changing portions 240.

Further, in the above-described embodiment, a catalyst containing at least Ni as a catalyst has been described as an example. However, the material of the catalyst is not limited as long as the tar in the mixed gas can be reformed to remove the tar. For example, oxides or carbonates of one or more elements selected from the group Ca (calcium), Mg (magnesium), Fe (iron), and Si (silicon), such as limonite, olivine, and the like. Natural ores such as limonite and olivine may be used as catalysts. That is, a catalyst containing one or more selected from the group of Ca, Mg, Fe, and Si may be adopted.

The present disclosure can be used in a tar reformer that reforms tar in syngas.

200 Tar reformer 210 Duct 214a Large diameter space 214b Squeezing space 214c Small diameter space 214d Expanded space 220 Premixed air generator 262 Supply pipe (oxidizer supply device)
264 obstacle board

Claims (1)

It is communicated with the large-diameter space into which the syngas is introduced, the throttle space that is communicated with the downstream end of the large-diameter space, and the flow path cross-sectional area gradually decreases from the upstream side to the downstream side, and the downstream end of the throttle space. the a small diameter of the small diameter space from among a large径空, communicates with the downstream end of the small diameter space, has a larger space in which a flow path cross-sectional area from the upstream side to the downstream side gradually increases, and at least the syngas and A duct through which the premixture containing the oxidant passes, and
The baffle plate provided in the duct and
An oxidant supply device that supplies an oxidant to the downstream side of the baffle plate in the duct,
A premixture generator that introduces an oxidizing agent into the throttle space to generate the premixture in the small diameter space,
Equipped with a,
A tar reformer in which the flow rate of the oxidant supplied by the oxidant supply device is smaller than the flow rate of the oxidant introduced by the premixture generator.

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