JP2013213090A - System for gasifying biomass fuel and system for synthesizing chemical product by using gasified gas - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a system for gasifying a biomass fuel by which the efficiency of the system can be improved by efficiently using steam, and to provide a system for synthesizing a chemical product by using the gasified gas.SOLUTION: A system for gasifying a biomass fuel includes a biomass-gasifying furnace 12 for gasifying, for example, biomass 11 of an organic fuel, a gas cooler 14 for cooling a formed gas 13A from the biomass-gasifying furnace 12, a gas-refining apparatus 15 for removing smut in a formed gas 13B after cooling, a second booster 30 for pressurizing a formed gas 13C after the removal of the smut, a chemical product-synthesizing apparatus 32 for synthesizing a chemical product by using a pressurized gas 31, a steam-feeding line Lfor feeding steam 21 (e.g. at 150-170°C) to the gas cooler 14 from the exterior, and a steam-introducing line Lfor introducing high-temperature steam (e.g. at 500°C) obtained by cooling the formed gas 13 by heat exchange at the gas cooler 14 into the biomass-gasifying furnace 12 as a gasifying agent 22A.

Description

  The present invention relates to a biomass fuel gasification system and a chemical synthesis system using gasification gas.

  Biomass generally refers to organisms that can be used as energy sources or industrial raw materials (for example, agricultural products or by-products, wood, plants, etc.), and are produced by the action of solar energy, air, water, soil, etc. So it can be played indefinitely.

By using the biomass as a gasification fuel, it becomes possible to produce clean energy sources such as fuel gas and methanol. Further, since biomass as waste can be treated, it is useful for environmental purification, and newly produced biomass is also grown by fixing CO ₂ by photosynthesis. Since it does not increase CO ₂ in the atmosphere, it leads to suppression of CO ₂ , which is a preferable technique.

  Here, as the biomass to be supplied, it is preferable to supply pulverized and dried biomass produced or discarded. In the present invention, the biomass means a biological resource (for example, agricultural product or by-product, wood, plant, etc.) that can be used as an energy source or an industrial raw material. (Patent Document 1 and Patent Document 2).

Moreover, it proposed previously about the system which gasifies and manufactures a liquid fuel using biomass (patent document 3).
The proposal of Patent Document 3 is a system that synthesizes various chemical products such as liquid fuel by gasifying biomass with steam and oxygen to generate a gas containing a large amount of hydrogen.
As a liquid fuel, for example, FT oil _{(C n H 2n + 2)} , when synthesizing such as methanol (CH ₃ OH) is biomass _{(C 1.1~1.3, H 2 O 0.8~0.9} ) product gas was used as a raw material In terms of its composition, hydrogen required for the chemical product is less than that of carbon.
Therefore, in order to efficiently synthesize chemical products, it is necessary to increase the H ₂ component in the obtained gasification gas (mainly H ₂ , CO, CO ₂ ).
For this reason, the H ₂ component in the gas is increased by a reformer (for example, a CO shift reaction catalyst or the like) of the produced gas.

JP 2001-240877 A JP 2001-240878 A JP 2008-208276 A

By the way, when biomass is burned in a biomass gasification furnace, when recovering and using the heat of the high-temperature gasification gas obtained from the gasification furnace, steam is produced from water and the gasification agent of the gasification furnace is used. It can be used as steam.
At this time, when the gasified gas of about 1,000 ° C. is cooled to, for example, 300 ° C. using 20 ° C. water, a steam of 500 ° C. is obtained. There is a problem that steam can be obtained only in an amount less than ₂ O / C (molar ratio) = 1.

  For this reason, conventionally, in order to produce steam necessary as a gasifying agent to be supplied to the biomass gasification furnace, heat generated by liquid fuel synthesis or heat generated by burning off-gas generated at the time of liquid fuel synthesis is separately produced. In addition, if this does not provide sufficient heat, it is necessary to produce hot steam from water using another heat source.

  In addition, in order to use the gasification gas from the biomass gasification furnace as a synthesis gas for the production of chemical products, it is necessary to install a reformer when increasing the hydrogen in the gasification gas, It is necessary to reheat the gas temperature, which has been lowered to about 40 ° C. in the gas purification step, to about 300 ° C., which is the operating temperature of the reformer, and a new heat source is required at this time.

  Furthermore, the reformer needs to supply steam to the reforming reaction, and a new heat source for producing this steam is required separately.

  Therefore, when gasifying biomass with a biomass gasification furnace and producing the synthesis gas for synthesis | combination of a chemical product, improvement of system efficiency is eagerly desired using steam efficiently.

  In view of the above problems, an object of the present invention is to provide a biomass fuel gasification system and a chemical product synthesis system using gasification gas that can efficiently improve the system efficiency by using steam.

  The first invention of the present invention for solving the above-described problems includes a biomass gasification furnace that gasifies biomass, a gas cooler that cools a product gas from the biomass gasification furnace, and a product gas after cooling. A gas refining device that removes soot and dust, a steam supply line that supplies steam to the gas cooler, and high-temperature steam obtained by heat exchange by cooling the generated gas with the gas cooler, A biomass fuel gasification system comprising: a steam introduction line for introducing a gasification agent into a gasification furnace.

  According to a second invention, in the first invention, the first booster that pressurizes the dust-generated product gas, a heat exchanger that heat-exchanges the boosted product gas, and the product that has passed through the heat exchanger. A reformer for reforming gas to obtain a reformed gas, and the remaining high-temperature steam used as a gasifying agent for a biomass gasification furnace among the high-temperature steam, either the heat exchanger or the reformer A biomass fuel gasification system having a steam supply line for supplying to one or both.

  According to a third invention, in the first or second invention, a gas component detector that detects a gas component of the reformed gas, and a reformed gas that bypasses the reformer and passes through the heat exchanger. And a control device for adjusting the opening of the first control valve according to the gas composition detected by the gas component detector. And a biomass fuel gasification system.

A fourth invention is the biomass according to the third invention, wherein a CO ₂ removal device for removing CO ₂ in the reformed gas is provided between the reformer and the gas component detector. In the fuel gasification system.

According to a fifth invention, in the fourth invention, a second bypass line comprising a second adjustment valve that bypasses the CO ₂ removal device and causes the reformed gas to flow to the downstream side of the CO ₂ removal device. It is in the biomass fuel gasification system characterized by providing.

  A sixth invention includes a biomass fuel gasification system according to any one of the first to fifth aspects, a second booster that boosts a mixed gas of the reformed gas and the product gas, and a second booster. There is provided a chemical product synthesis system using a gasified gas from biomass fuel, comprising a chemical product synthesis device that synthesizes a chemical product using a pressurized gas under pressure.

According to the present invention, high-temperature steam obtained by gas cooling can be supplied as a gasification agent to a biomass gasification furnace, and surplus high-temperature steam is returned as high-temperature steam useful for a chemical plant or the like that supplies low-temperature steam. System efficiency can be improved.
Moreover, when installing the reformer which reforms gasification gas, an excess high temperature steam can be introduce | transduced into the heat exchanger which reheats the product gas introduced into this reformer, and can be heat-exchanged. Furthermore, in the reformer, it can be used as steam for steam reforming, the surplus steam generated in the system can be used effectively, and the thermal efficiency of the system can be further improved.

FIG. 1 is a schematic diagram of a biomass fuel gasification system according to a first embodiment. FIG. 2 is a schematic diagram of a biomass fuel gasification system according to the second embodiment. FIG. 3 is a schematic diagram of a biomass fuel gasification system according to a third embodiment. FIG. 4 is a schematic diagram of a biomass fuel gasification system according to a fourth embodiment.

  Hereinafter, the present invention will be described in detail with reference to the drawings. Note that the present invention is not limited to the embodiments. In addition, constituent elements in the following embodiments include those that can be easily assumed by those skilled in the art or those that are substantially the same.

A biomass fuel gasification system according to an embodiment of the present invention will be described with reference to the drawings. FIG. 1 is a schematic diagram of a biomass fuel gasification system according to a first embodiment.
As shown in FIG. 1, a biomass fuel gasification system 10A according to the present embodiment cools, for example, a biomass gasification furnace 12 that gasifies biomass 11 that is an organic fuel, and a product gas 13A from the biomass gasification furnace 12. The gas cooler 14 that performs the cooling, the gas purifier 15 that removes the dust in the product gas 13B after cooling, the second booster 30 that boosts the product gas 13C after the dust removal for chemical synthesis, and the pressure booster. A chemical composition synthesizer 32 that synthesizes a chemical product using the pressurized gas 31, a steam supply line L ₁₁ that supplies steam (for example, 150 to 170 ° C.) 21 from the outside to the gas cooler 14, and gas cooling Steam introduction line for introducing high-temperature (for example, 500 ° C.) steam obtained by cooling the produced gas 13A in the vessel 14 and heat exchange into the biomass gasification furnace 12 as a gasifying agent 22A _12, those having a.

  Biomass in the present invention refers to biological resources that can be used as an energy source or industrial raw material (for example, agricultural products or by-products, wood, plants, etc.), and examples include sweet sorghum, napiergrass, spirulina, and the like. it can. It also includes agricultural and forestry waste such as firewood, wood scrap, and thinned wood.

  Conventionally, water was supplied as a refrigerant in the gas cooler 14 to cool the gas. However, in this embodiment, a low-temperature steam of 150 to 170 ° C., for example, is supplied and a high temperature (for example, 800 to Gas cooling is performed using the generated gas 13A of 1,100 ° C.).

  In the present embodiment, the steam 21 used as a heat medium in the gas cooler 14 uses exhaust steam generated in an adjacent chemical plant (chemical synthesis plant such as methanol or paper mill). Therefore, it is not necessary to produce steam from conventional water, and a new heat source necessary for producing steam is not necessary.

Here, when the high-temperature product gas 13A is cooled to about 300 ° C. by the gas cooler 14, the high-temperature steam (H ₂ O) is H ₂ O / C = 5 with respect to the amount of carbon (C) in the input biomass. About (molar ratio) will be manufactured.
In the biomass gasification furnace 12, H ₂ O / C = 2 (molar ratio) is required as a gasifying agent. Therefore, steam necessary for gasification of the biomass 11 is converted to H ₂ O / C = 2 (molar ratio). However, the remaining high-temperature steam 22B corresponding to H ₂ / C = 3 becomes surplus.
For example, when the throughput of biomass 11 is 20 t / d, 5t of low-temperature steam 21 is required to cool the high-temperature product gas 13A of about 1000 ° C. to 300 ° C., but the steam required for gasification is 2t. Therefore, 3t becomes a surplus.
Therefore, excess hot steam 22B, by returning via the steam supply line L ₁₃ in the chemical plant or the like adjacent a source of cryogen vapor 21, for example, 0.99 ° C. The low-temperature steam 21 high 500 ° C. utility value of Can be reused as high temperature steam.

  As a result, a new heat source for generating steam from conventional water becomes unnecessary, and high-temperature steam obtained by gas cooling can be supplied to the biomass gasification furnace 12 as the gasifying agent 22A, and surplus The high-temperature steam 22B can be returned as high-temperature steam useful for the chemical plant or the like that supplies the low-temperature steam 21, and the system efficiency can be improved.

A biomass fuel gasification system according to an embodiment of the present invention will be described with reference to the drawings. FIG. 2 is a schematic diagram of a biomass fuel gasification system according to the second embodiment. In addition, about the same structural member as Example 1, the same code | symbol is attached | subjected and the description is abbreviate | omitted.
As shown in FIG. 2, the biomass fuel gasification system 10B according to the present embodiment is the same as the biomass fuel gasification system 10A according to the first embodiment, after the first booster 16 that boosts the generated gas 13C after the dust removal. On the flow side, a heat exchanger 17 that exchanges heat of the pressurized product gas 13D, a sulfur removal device 18 that removes sulfur in the product gas 13E after heat exchange, and a product gas 13F from which sulfur has been removed are provided. A reformer 20 for reforming to obtain a reformed gas 19 is provided.

The biomass 11 is combusted and gasified in a biomass gasification furnace 12 together with a gasifying agent (steam) (not shown), and is mainly composed of hydrogen (H ₂ ) and carbon monoxide (CO) at high temperatures (for example, 800 to 1,100 ° C.). A product gas 13A is obtained. Since this generated gas 13A is high in temperature, it is cooled to 300 ° C. by steam 21 in the gas cooler 14. Thereafter, dust and tar content in the gas are removed from the cooled product gas 13B by a gas purifier 15 such as a scrubber. The purified product gas 13C becomes a low temperature (40 ° C.), and this low temperature product gas 13C is boosted to a predetermined pressure by the first booster 16, and then reheated to about 300 ° C. by the heat exchanger 17. Yes.

  The reheated product gas 13E is introduced into, for example, a sulfur removal device 18 filled with a sulfur removal catalyst, and the sulfur content is removed here. The product gas 13F from which the sulfur content has been removed is supplied to a reformer (for example, a CO shift reaction catalyst, a reforming catalyst for cracking hydrocarbons, etc .: reaction temperature of about 300 ° C.) 20, and the supplied steam 22C is used. The gas is reformed by the catalyst.

Here, in the present embodiment, the steam 21 is supplied from the outside to the gas cooler 14 to cool the product gas 13A, and the low-temperature steam 21 becomes high-temperature steam by this cooling. Then, a predetermined amount of the high-temperature steam 22A is introduced into the biomass gasification furnace 12 as a gasifying agent. Then, the remaining excess temperature steam 22B of high-temperature steam 22A, a first steam inlet line L ₁₄ to be introduced into the heat exchanger 17, the vapor 22C after the heat exchange in the heat exchanger 17, a reformer 20 A second steam introduction line L ₁₅ to be introduced into is provided.

Thereby, the remaining high-temperature steam 22B of the high-temperature steam 22A used as the gasifying agent for the biomass gasification furnace 12 is introduced into the heat exchanger 17 to reduce the generated gas 13D to a low temperature (40 ° C.), for example, at 300 ° C. Reheating to gas temperature.
The steam 22C that has been subjected to heat exchange in the heat exchanger 17 and has reached an intermediate temperature (300 ° C.) is introduced into the reformer 20 through the second steam introduction line L ₁₅ , where steam for steam reforming is introduced. Used as

Incidentally, steam 22C for introducing the second steam inlet line L ₁₅ is, if less than the amount of steam required in the reformer 20 will be charged, but the introducing hot steam to the reformer 20 Unlike the conventional case where all the steam is supplied separately, the amount introduced is small.

  The reformed gas 19 is boosted to a high pressure suitable for chemical synthesis by the second booster 30 and used as a synthesis gas for the chemical synthesis apparatus 32.

  In this embodiment, the surplus high-temperature steam 22B is first used for heat exchange by the heat exchanger 17 and then sequentially supplied to the reformer 20, but the present invention is not limited to this. The excess high-temperature steam 22B may be introduced into either one or both of the heat exchanger 17 and the reformer 20, respectively.

  As a result, in the biomass fuel gasification system 10B, the steam necessary for the reforming reaction used in the reformer 20 can be effectively used as surplus steam generated in the system, and the thermal efficiency of the system can be improved. it can.

A biomass fuel gasification system according to an embodiment of the present invention will be described with reference to the drawings. FIG. 3 is a schematic diagram of a biomass fuel gasification system according to a third embodiment. In addition, about the same structural member as Example 1 and 2, the same code | symbol is attached | subjected and the description is abbreviate | omitted.
As shown in FIG. 3, the biomass fuel gasification system 10C according to the present embodiment detects the gas component of the reformed gas 19 reformed by the reformer 20 in the biomass fuel gasification system 10B of the second embodiment. The gas component detector 41 and the reformer 20 are bypassed, and the product gas 13F from which the sulfur content has been removed flows to the downstream side of the reformer 20, and the first bypass provided with the first control valve 42 A line 43 and a control device 44 that adjusts the opening of the first control valve 42 in accordance with the gas composition detected by the gas component detector 41 are provided.

In the present embodiment, a first bypass line 43 that bypasses the reformer 20 is provided, and the product gas 13F from which a predetermined amount of sulfur has been removed is caused to flow to the downstream side of the reformer 20, thereby reforming the reformer 20. The reforming amount in the vessel 20 is adjusted.
The gas amount is adjusted by the first control valve 42 interposed in the first bypass line 43.

Prior to this adjustment, a gas component detector 41 is provided on the downstream side of the reformer 20 to detect the composition of the combined gas of the reformed gas 19 and the product gas 13F from which the sulfur content has been removed. Yes.
Then, the gas composition information S ₁ detected by the gas component detector 41 is sent to the control device 44, and the first control valve 42 is opened according to the composition of the predetermined hydrogen concentration required by the chemical synthesis device 32. and to perform the command S ₂ to adjust the degree. As a result, the flow rate of the product gas 13F introduced into the reformer 20 and removed from the sulfur component to be reformed is adjusted to adjust the gas composition.

As an example, when synthesizing a hydrocarbon oil by FT synthesis, H ₂ / CO = 2 is set to a predetermined value requested from the synthesis catalyst side of the chemical product synthesis apparatus 32.
On the other hand, by setting a bypass amount based on a gas composition predicted in advance and passing a predetermined amount through the reformer 20, by increasing H ₂ , it is possible to approach H ₂ / CO = 2 in advance. deep.

Then, the H _2, CO concentration measured by the gas component detector 41, if you keep the H ₂ / CO = ₂ is consistent with the request from the synthesis catalyst side of the chemical products synthesizer 32 Therefore, the current situation will be maintained.

Next, when the hydrogen concentration in the gas component detector 41 is equal to or higher than a predetermined value (H ₂ / CO> 2), the control device 44 performs an operation of opening the first control valve 42.

On the other hand, when the hydrogen concentration in the gas component detector 41 is equal to or lower than a predetermined value (H ₂ / CO <2), the control device 44 performs an operation of closing the first control valve 42.

  Factors for fluctuations in the reformed gas 19 at the outlet of the reformer 20 include, for example, fluctuations in the type of biomass, fluctuations in properties such as moisture, fluctuations in the blending ratio, fluctuations in the gasification conditions of the biomass gasifier 12, and the like Is assumed.

The biomass 11 is combusted and gasified in a biomass gasification furnace 12 together with a gasifying agent (steam) (not shown), and is mainly composed of hydrogen (H ₂ ) and carbon monoxide (CO) at a high temperature (for example, 800 to 1,100 ° C.). A product gas 13A is obtained. The generated gas 13 </ b> A removes dust and tar content in the gas with a gas purifier 15 such as a scrubber. The purified product gas 13B is boosted to a predetermined pressure by the first booster 16, and introduced into, for example, a sulfur removal device 18 filled with a sulfur removal catalyst, where the sulfur content is removed. The product gas 13F from which the sulfur content has been removed is supplied to a reformer (for example, a CO shift reaction catalyst, a reforming catalyst that decomposes hydrocarbons, etc.) 20, and gas is reformed by the catalyst using steam.

At this time, conventionally, since the gas flow rate of the product gas 13F introduced into the reformer 20 is constant, the H ₂ and CO ratio in the gas is reformed to an equilibrium composition. It was difficult to adjust the composition.

On the other hand, in the present invention, the first bypass line 43 that bypasses the reformer 20 is provided, and the first control valve 42 is interposed in the first bypass line 43. Therefore, the gas component detector The change in the gas composition after reforming detected at 41 is detected, and when it is within the set range (for example, H ₂ / CO = 2), the flow rate is maintained as it is.

When the hydrogen concentration in the gas component detector 41 becomes equal to or higher than a predetermined value (H ₂ / CO> 2), the control device 44 executes an operation of opening the first control valve 42, and When the hydrogen concentration in the gas component detector 41 is equal to or lower than a predetermined value (H ₂ / CO <2), the control device 44 performs an operation of closing the first control valve 42.
Thereby, the reformed gas 19 in an appropriate range can always be supplied to the chemical synthesis apparatus 32.

  As a result, the hydrocarbon oil can be stably produced by the chemical synthesis device 32 using the reformed gas 19 from the reformer 20.

A biomass fuel gasification system according to an embodiment of the present invention will be described with reference to the drawings. FIG. 4 is a schematic diagram of a biomass fuel gasification system according to a fourth embodiment. In addition, about the same structural member as Example 3, the same code | symbol is attached | subjected and the description is abbreviate | omitted.
As shown in FIG. 4, the biomass fuel gasification system 10D according to the present embodiment includes a reformed gas between the reformer 20 and the gas component detector 41 in the biomass fuel gasification system 10C of the third embodiment. It is provided CO ₂ removing device 51 for removing CO ₂ in 19.

When alcohol or the like is produced with the chemical product synthesizer 32, it is necessary to adjust the ratio of CO ₂ .
Normally, CO ₂ in biomass gasification gas cannot be used for catalyst synthesis. However, in methanol synthesis catalyst, the reverse reaction of CO shift reaction (see the following formula (1)) occurs, so hydrogen (H _In addition to ₂ ) and CO, CO ₂ can also be used for synthesis.
H ₂ + CO ₂ → H ₂ O + CO (1)
Therefore, the ideal gas composition for methanol synthesis is H ₂ / (2CO + 3CO ₂ ) = 1 or more, and this index is generally known as a so-called “M value”.
As a result, in the methanol synthesis, this M value becomes a predetermined value requested from the synthesis catalyst side of the chemical product synthesis apparatus 32.

For this reason, in this embodiment, the CO ₂ removal device 51 is connected to the downstream side of the reformer 20. Then, in this embodiment, the reformer 20 and the CO ₂ removing device 51 of the first bypass line 43 is provided bypassing the predetermined amount can be a flow-through gas to the reformer 20 and the CO ₂ remover 51 I am doing so.

The gas component detector 41 is installed after the bypass merge of the first bypass line 43.
Then, the gas composition information S ₁ detected by the gas component detector 41 is sent to the control device 44, and the first control valve 42 is opened according to the composition of the predetermined hydrogen concentration required by the chemical synthesis device 32. and to perform the command S ₂ to adjust the degree. Thus, the flow rate of the generated gas 13F to the reformer 20 and the CO ₂ removal device 51 is adjusted by the first control valve 42 according to the gas composition detected by the gas component detector 41, and the gas composition can be adjusted. Yes.

For example, in methanol synthesis, M value (H ₂ / (2CO + 3CO ₂ )) = 1 is an ideal composition on the synthesis catalyst side.
On the other hand, by adjusting the opening degree of the first control valve 42 based on the gas composition predicted in advance to set the bypass amount, and allowing a predetermined amount to pass through the reformer 20 and the CO ₂ removal device 51, M The value is brought close to “1”.

Next, when the H ₂ , CO, and CO ₂ concentrations are measured by the gas component detector 41 and M = 1 is maintained, the requirement from the synthesis catalyst side of the chemical synthesis device 32 is met. Therefore, the current situation will be maintained.

Next, gasification is performed, and H ₂ , CO, and CO ₂ are measured by the gas component detector 41. If the M value <1, the first control valve 42 is closed, and the generated gas to the reformer 20 The control device 44 adjusts the flow rate to increase, the H ₂ component to increase, and the CO ₂ removal amount to approach the M value = 1.

Next, gasification is performed, and H ₂ , CO, and CO ₂ are measured by the gas component detector 41. If the M value> 1, the first control valve 42 is opened, and the generated gas to the reformer 20 The flow rate is reduced, the H ₂ component is reduced, and the CO ₂ removal amount is adjusted by the control device 44 so as to approach the M value = 1.

Thus, according to this embodiment, by adjusting the flow rate of the product gas 13F bypassing the reformer 20 and the CO ₂ remover 51, can be adjusted to the desired gas composition for chemical products synthesis.

Furthermore, biomass fuel gasification system 10D according to the present embodiment, CO ₂ is removed device 51 bypass, the second having a second control valve 53 to flow the reformed gas 19 to the downstream side of the CO ₂ remover 51 The bypass line 52 may be provided.

Then, the information S ₁ of the gas composition detected by the gas component detector 41 is sent to the control device 44, and the second control valve 53 is opened according to the composition of the predetermined hydrogen concentration required by the chemical synthesis device 32. and to perform the command S ₃ for adjusting the degree. Thus, by adjusting the second control valve 53 interposed in the second bypass line 52, the flow rate of the reformed gas 19 supplied to the CO ₂ removal device 51 is adjusted, and the CO ₂ removal amount is adjusted. can do.
Therefore, in addition to controlling the first control valve 42, the controller 44 individually adjusts the second control valve 53 to adjust the CO ₂ removal amount so that the M value = 1. I try to adjust it.

Thus, according to this embodiment, by respectively adjusting the flow rate of the product gas 13F bypassing the reformer 20 and the CO ₂ remover 51, it can be adjusted to the desired gas composition for chemicals synthesis .

Furthermore, in the biomass fuel gasification system 10D according to the present embodiment, the adjustment of the CO ₂ removal capability is changed with respect to the CO ₂ removal device 51 (for example, variation in operating conditions (temperature, pressure, etc.) of the CO ₂ removal device) ).

Then, the gas composition information S ₁ detected by the gas component detector 41 is sent to the control device 44, and the removal capability of the CO ₂ removal device 51 according to the composition of the predetermined hydrogen concentration requested by the chemical synthesis device 32. and to perform the command S ₄ to regulate. Thereby, the CO ₂ removal amount of the reformed gas 19 supplied to the CO ₂ removal device 51 can be adjusted.
Therefore, the control device 44 individually adjusts the CO ₂ removal amount by changing the operating conditions of the CO ₂ removal device 51 and the like so that the M value = 1.

Thus, according to the present embodiment, the flow rate of the product gas 13F that bypasses the reformer 20 and the CO ₂ removal device 51 is adjusted, and the removal capability in the CO ₂ removal device is adjusted, thereby converting the chemical product. It can be adjusted to the desired gas composition for synthesis.

In this embodiment, the control of the first control valve 42 interposed in the first bypass line 43 that bypasses the reformer 20 and the CO ₂ removal device 51, and the _second that bypasses the CO ₂ removal device 51. The control of the second control valve 53 interposed in the bypass line 52 and the adjustment of the operating conditions of the CO ₂ removal device 51 to control the CO ₂ removal capacity may all be performed, and each priority order May be determined in advance and controlled based on the priority order to adjust to a desired gas composition for chemical synthesis.

  The biomass fuel gasification system and the chemical product synthesis system using the gasification gas of the present invention are not limited to the above-described embodiments, and can be appropriately changed within a range not departing from the gist thereof. For example, the sulfur removing device 18 may be provided on the upstream side of the first booster 16 in addition to being provided on the downstream side of the first booster 16. Moreover, it is good also as utilizing for a biomass fuel gasification system the sulfur content removal apparatus which removes sulfur content at normal temperature, such as a wet apparatus sulfur removal apparatus.

10A to 10D Biomass fuel gasification system 11 Biomass 12 Biomass gasification furnace 13A to 13F Product gas 14 Gas cooler 15 Gas purification device 16 First booster 17 Heat exchanger 18 Sulfur removal device 19 Reformed gas 20 Reformer 30 second booster 32 Chemicals synthesizer 41 gas component detector 42 first control valve 43 first bypass line 44 the control device 51 CO ₂ removing device 52 and the second bypass line 53 the second control valve

Claims (6)

A biomass gasification furnace for gasifying biomass;
A gas cooler for cooling the produced gas from the biomass gasification furnace;
A gas refining device that removes dust in the product gas after cooling;
A steam supply line for supplying steam to the gas cooler from the outside;
A biomass fuel gasification system comprising: a steam introduction line for introducing a high-temperature steam obtained by cooling the generated gas with the gas cooler and performing heat exchange into a biomass gasification furnace as a gasification agent . In claim 1,
A first booster for boosting the generated gas after dust removal;
A heat exchanger for exchanging heat of the product gas after the pressurization;
A reformer that reforms the product gas that has passed through the heat exchanger to obtain a reformed gas; and
A steam supply line that supplies the remaining high-temperature steam used as a gasification agent for a biomass gasification furnace to one or both of the heat exchanger and the reformer. A featured biomass fuel gasification system. In claim 1 or 2,
A gas component detector for detecting a gas component of the reformed gas;
A first bypass line including a first regulating valve that bypasses the reformer and causes the product gas that has passed through the heat exchanger to flow to the downstream side of the reformer;
A biomass fuel gasification system comprising: a control device that adjusts an opening degree of the first control valve according to a gas composition detected by the gas component detector. In claim 3,
A biomass fuel gasification system comprising a CO ₂ removal device for removing CO ₂ in the reformed gas between the reformer and the gas component detector. In claim 4,
The CO ₂ removal unit bypasses, the reformed biomass fuel gasification system and providing a second bypass line having a second control valve to flow to the downstream side of the gas CO ₂ removal device. A biomass fuel gasification system according to any one of claims 1 to 5;
A second booster that boosts the mixed gas of the reformed gas and the product gas;
A chemical product synthesizing system using gasified gas from biomass fuel, comprising: a chemical product synthesizing device that synthesizes a chemical product using the pressurized gas boosted by the second booster.

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