JP2008163873A - Solid fuel gasified gas using plant - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a solid fuel gasified gas using plant for improving plant efficiency in synthesis of liquid fuel by gasified gas and power generation by gas turbine driving, by reducing a heat loss of the gasified gas caused by such a temperature change, by reducing temperature variation in a temperature change between respective elements for conducting the gasified gas, in the plant used for both the synthesis of the liquid fuel by the gasified gas and the power generation by the gas turbine driving. <P>SOLUTION: This solid fuel gasified gas using plant is constituted so as to gasify solid fuel by using oxygen in a gasification furnace, and to drive a gas turbine by off-gas from a liquid fuel synthesizing means, and is characterized by being constituted so as to supply hydrogen generated by a water electrolyzing device to a gasified gas passage on the upstream side of the liquid fuel synthesizing means, and to supply the oxygen generated by the water electrolyzing device to the gasification furnace by setting operation pressure of the water electrolyzing device larger than pressure in the gasification furnace, by arranging the water electrolyzing device for generating the hydrogen and the oxygen by electrolyzing water. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention is applied to a coal gasification complex plant, a biomass feedstock gasification complex plant, etc., supplying solid fuel such as coal and biomass feedstock to a gasification furnace, and oxygen supplied from an oxygen supply means in the gasification furnace A solid fuel gasification gas utilization plant configured to gasify the solid fuel using a gas and drive a gas turbine with the gasification gas, or to synthesize and produce the liquid fuel with the liquid fuel synthesizing means. About.

FIG. 5 is a system diagram showing a conventional example of a gasification gas utilization plant for solid fuel such as coal and biomass raw material.
In FIG. 5, solid fuel such as pulverized coal and biomass material is supplied to the gasifier 2 by the solid fuel supply means 1. In the gasification furnace 2, the solid fuel is gasified by ejecting oxygen separated from nitrogen by an air separation device into the furnace. The gasification gas having an outlet temperature of about 400 ° C. of the gasification furnace 2 is introduced into a gas purification apparatus 3 that performs gas purification to remove sulfur, halogen, and the like in the gasification gas at a low temperature.
In the gas purifier 3, the operating temperature is lowered to about 40 to -15 ° C., and sulfur, halogen, etc. in the gasification gas are removed by wet low-temperature gas purification technology (chemical absorption method, physical absorption method, etc.). To do. The gasified gas from which such harmful substances have been removed is introduced into the CO shift reactor 41.

In the CO shift reactor 41, in order to compensate for the shortage of hydrogen in the gasification gas, a CO shift catalyst is used, and after conversion to H ₂ (hydrogen) to a CO concentration of about 5% by a high temperature reaction of about 500 ° C., 250 It is converted to a CO concentration of about 1% by the following low-temperature reaction at about ° C.
CO + H ₂ O⇔H ₂ + CO ₂
In the CO shift reaction in the CO shift reactor 41, water equivalent to CO is required for the reaction as shown in the above equation, and in the actual reaction, an excessive amount of water is required. A large amount of water vapor is supplied to the reactor 41, or water obtained by condensing and recovering excess water by cooling the gasification gas at the outlet of the CO shift reactor 41 with a cooler 43 is circulated and supplied.

In the CO shift reactor 41, the gasified gas that has undergone CO H ₂ shift is introduced into the liquid fuel synthesis reactor 6, where it is converted into a liquid fuel such as methanol, and the liquid fuel is taken out. Retrieved by means 7. About 300 ° C. off-gas from the liquid fuel synthesis reactor 6 is supplied to the gas turbine 8 to drive the gas turbine 8.
The exhaust gas discharged from the gas turbine 8 generates steam by heating the feed water with the exhaust heat recovery boiler 9, and then is discharged into the atmosphere through the exhaust gas discharging means 12 such as an exhaust gas purification device. Steam generated in the exhaust heat recovery boiler 9 is introduced into the steam turbine 10 to drive the steam turbine 10. Condensate from the steam turbine 10 is returned to the exhaust heat recovery boiler 9.

  Moreover, in patent document 1 (Unexamined-Japanese-Patent No. 2002-193858) which concerns the application of this applicant, biomass raw material is supplied to a gasification furnace, and oxygen supplied from an oxygen supply means in this gasification furnace is used. A plant for purifying methanol from a biomass raw material configured to gasify the biomass raw material and liquefy the gasified gas by methanol synthesis means to purify methanol, and electrolyze water to produce hydrogen and oxygen. A water electrolysis device to be generated is provided, and hydrogen generated by the water electrolysis device is supplied to the methanol synthesis means, and oxygen generated by the water electrolysis device is supplied to the gasifier A methanol refining plant from the finished biomass feedstock is disclosed.

JP 2002-193858 A

In the gasification gas utilization plant of solid fuel such as coal and biomass raw material shown in FIG. 5, when the solid fuel is coal, in order to synthesize the liquid fuel in the liquid fuel synthesis reactor 6, The molar ratio of CO (carbon monoxide) to H ₂ (hydrogen) is preferably 1: 2, but in the case of coal gasification gas, the molar ratio is 1: 1 to 3: 1, and H ₂ ( Hydrogen) is insufficient.
Therefore, in the conventional gasification gas utilization plant shown in FIG. 5, a CO shift reactor 41 using a CO shift catalyst is provided upstream of the liquid fuel synthesis reactor 6, and steam is supplied to the CO shift reactor 41. By supplying a large amount of water vapor containing surplus water by means 42 or cooling the gasification gas at the outlet of the CO shift reactor 41 with a cooler 43 and circulatingly supplying water obtained by condensing and recovering surplus water, about 500 ° C. after conversion to CO concentration of about 5% to H _{2 (hydrogen)} at a high temperature reaction, it is supplemented with the H _{2 (hydrogen)} by converting to about CO concentration of 1 percent below the low temperature reaction of about 250 ° C..

Therefore, in the conventional gasification gas utilization plant shown in FIG. 5, after the gasification gas at the outlet of the gasification furnace 2 is lowered to the maximum operating temperature of about 40 ° C. in the gas purification apparatus 3, the CO shift reactor is used. In 41, the temperature is raised to a reaction temperature of about 500 ° C., and then H ₂ (hydrogen) is converted to a CO concentration of about 1% by a low-temperature reaction of about 250 ° C., and the temperature of each element through which the gasification gas flows. It is necessary to change the operation with a large temperature amplitude such as about 400 ° C. (gasification furnace 2) → 40 to −15 ° C. (gas purification device 3) → 500 ° C. → 250 ° C. (CO shift reactor 41).

  Therefore, in such a conventional gasification gas utilization plant, since there is a temperature change with a large temperature amplitude between the elements through which the gasification gas flows, the heat loss of the gasification gas becomes large. Thus, there is a problem to be solved that the plant efficiency related to the synthesis of liquid fuel by gasification gas and the power generation by gas turbine drive is lowered.

  In the technique of Patent Document 1 (Japanese Patent Application Laid-Open No. 2002-193858), hydrogen generated by a water electrolysis apparatus that electrolyzes water to generate hydrogen and oxygen is supplied to the methanol synthesis means. Since oxygen generated in the water electrolysis apparatus is supplied to the gasifier, hydrogen can be replenished in the liquid fuel synthesizing means (methanol synthesizing means), and the conventional gas shown in FIG. Although it is possible to obtain the required hydrogen without using the CO shift reactor 41 such as a conversion gas utilization plant, the technique of Patent Document 1 uses liquid fuel synthesizing means (methanol synthesizing means) from biomass raw material. This is a technology for producing fuel (methanol). Patent Document 1 discloses the use of gasified gas that uses gasified gas for both synthesis of liquid fuel and power generation by driving a gas turbine. In Holland, to the point of solving the above problems are not mentioned.

  In view of such a problem of the prior art, the present invention is a plant that uses gasified gas for both synthesis of liquid fuel and power generation by driving a gas turbine, and the temperature of temperature change between each element through which the gasified gas flows. A solid fuel gasification gas utilization plant that reduces the heat loss of gasification gas due to such temperature changes by reducing the amplitude, and improves the plant efficiency related to synthesis of liquid fuel by gasification gas and power generation by gas turbine drive The purpose is to provide.

  The present invention achieves the above-mentioned object. A solid fuel containing coal is supplied to a gasification furnace, and the solid fuel is gasified using oxygen supplied from an oxygen supply means in the gasification furnace. In the solid fuel gasification gas utilization plant configured to liquefy the gasified gas by the liquid fuel synthesizing means to purify the liquid fuel and to drive the gas turbine by the off-gas from the liquid fuel synthesizing means, water is electrolyzed. A hydrogen electrolyzer for generating hydrogen and oxygen is supplied to the gasified gas passage on the upstream side of the liquid fuel synthesizing means, and the water electrolyzer The operation pressure is set larger than the pressure in the gasification furnace, and oxygen generated by the water electrolysis apparatus is supplied to the gasification furnace.

In addition, the present invention further includes start-up air supply means for starting up the gasification furnace using one or both of air extracted from the gas turbine and air generated by the energy of the gasification gas. It is characterized by.
In the present invention, preferably, the air generated by the energy of the gasified gas is generated by a compressor driven by the energy of steam from an exhaust heat recovery boiler attached to the gas turbine.

The present invention, the exhaust gas cooling after the gas turbine driven, water compressed to produce a CO ₂ rich gas and water, the CO ₂ recovery unit provided, the water electrolysis of water from the aqueous, the CO ₂ recovery unit with use in the electrolysis of water is supplied to the apparatus, water, characterized in that the CO ₂ rich gas from the CO ₂ recovery unit is arranged to supply to said gasification furnace.

  In the present invention, an oxygen expansion turbine driven by the oxygen is provided in an oxygen passage for supplying oxygen generated by the water electrolyzer to the gasifier, and hydrogen generated by the water electrolyzer is A hydrogen expansion turbine driven by the hydrogen is provided in a hydrogen passage supplied to the liquid fuel synthesizing means.

As described above, according to the present invention, hydrogen produced by the water electrolysis apparatus is introduced into the liquid fuel synthesizing means and used for producing liquid fuel from the gasification gas. A CO shift reactor for converting (carbon oxide) to H ₂ (hydrogen) becomes unnecessary.
For this reason, it is sufficient to raise the temperature of the gasification gas leaving the gas purification apparatus (operation temperature 40 to −15 ° C.) to about 300 ° C., which is the reaction temperature of the liquid fuel synthesis, as in the prior art. It is not necessary to raise the reaction temperature of the CO shift reactor to about 500 ° C. Therefore, the temperature of each element through which the gasification gas flows is about 400 ° C. (gasification furnace) → 40 to −15 ° C. (Gas purification device) → 300 ° C. (liquid fuel synthesizing means), and the temperature change amount becomes smaller than that of the conventional technique.
Thereby, compared with the said prior art, the heat loss of gasification gas can be reduced and the plant efficiency concerning the synthesis | combination of the liquid fuel by gasification gas and the electric power generation by a gas turbine drive improves.

  Further, as described above, the CO shift reactor, the steam supply means to the CO shift reactor and the cooler in the prior art are unnecessary, the pressure loss of the system is reduced, the plant efficiency is improved, and the apparatus Can be simplified and the economy can be improved (cost reduction).

  Further, according to the present invention, oxygen generated in the water electrolysis apparatus is jetted into the gasification furnace and used for gasification of solid fuel together with oxygen from the air separation apparatus. The amount of oxygen supplied from the apparatus to the gasification furnace can be reduced, and the driving power of the air separation apparatus can be reduced.

  In addition, a starting air supply means for starting the gasification furnace using either one or both of air extracted from the gas turbine and air generated by the energy of the gasification gas is provided. If the air generated by the energy of the gasification gas is generated by a compressor driven by the energy of the steam from the exhaust heat recovery boiler attached to the gas turbine, the oxygen of the gasification agent of the gasification furnace As the air separation device uses air generated by the energy of gasified gas such as compressed air extracted from the gas turbine and compressed air from the start-up auxiliary compressor driven by the steam extracted from the steam turbine. The capacity of the system can be reduced to the capacity of the utility required for the plant, and the equipment cost can be reduced.

In addition, CO ₂ rich gas and water for generating CO ₂ rich gas and water by cooling and compressing the exhaust gas after driving the gas turbine, and CO ₂ recovery means are provided, and water from the CO ₂ recovery means is supplied to the water electrolyzer If the gas is used for electrolysis water and CO ₂ rich gas from the water and CO ₂ recovery means is supplied to the gasification furnace, the exhaust gas is cooled and compressed on the outlet side of the exhaust gas, and the CO ₂ rich gas and water to produce water, the water comprising a CO ₂ recovery facility and CO ₂ compression storage facility, provided with a CO ₂ recovery unit, since the recovery of CO ₂ in the exhaust gas, reduce the emission of CO ₂ from the plant it can.

The water, the CO ₂ from the CO ₂ recovery unit, so can be used as a gasifying agent in the gasification furnace, air separation unit for supplying gasifying agent (oxygen) to the gasification furnace is not required.
Furthermore, by using the water and the recovered water from the CO ₂ recovery means as the electrolyzed water of the water electrolysis apparatus, the amount of hydrogen produced in the water electrolysis apparatus can be increased, and the production amount of liquid fuel can be increased.

  Hereinafter, the present invention will be described in detail with reference to the embodiments shown in the drawings. However, the dimensions, materials, shapes, relative arrangements, and the like of the component parts described in this example are not intended to limit the scope of the present invention only to specific examples unless otherwise specified. Only.

  FIG. 1 is a system diagram showing an overall configuration of a solid fuel gasification gas utilization plant according to a first embodiment of the present invention. In this embodiment, a case where pulverized coal is used as the solid fuel will be described. It is.

In FIG. 1, a solid fuel composed of pulverized coal is supplied to a gasification furnace 2 by a solid fuel supply means 1. In the gasification furnace 2, the solid fuel is gasified by jetting oxygen (O ₂ ) separated from nitrogen by the air separation device 4 and oxygen from a water electrolysis device 5 described later into the furnace. A gasification gas composed of CO + H ₂ is generated.
A gasification gas having an outlet temperature of about 400 ° C. of the gasification furnace 2 is introduced into a gas purification apparatus 3 that performs gas purification to remove sulfur, chlorine, and the like in the gasification gas at a low temperature.
In the gas purification apparatus 3, the gasified gas is cooled to an operating temperature of about 40 to −15 ° C., and sulfur in the gasified gas is obtained by wet low-temperature gas purification technology (chemical absorption method, physical absorption method, etc.). Remove halogen, etc. The gasified gas from which such harmful substances have been removed is supplied with hydrogen (H ₂ ) generated by a water electrolysis apparatus 5 to be described later and then introduced into a liquid fuel synthesis reactor 6 constituting liquid fuel synthesizing means. The

The water electrolysis apparatus 5 is a known apparatus for decomposing water into hydrogen (H ₂ ) and oxygen (O ₂ ), and the hydrogen produced in the water electrolysis apparatus 5 (operation temperature about 100 ° C.) is the liquid. The gas is supplied to the gasification gas passage 3 a upstream of the fuel synthesis reactor 6 and introduced into the liquid fuel synthesis reactor 6.
The oxygen generated by the water electrolysis device 5 is jetted into the gasification furnace 2 and used for gasification of solid fuel together with oxygen from the air separation device 4.
In this case, the operation pressure of the water electrolysis apparatus 5 is set to be larger than the pressure in the gasification furnace 2, and oxygen generated by the water electrolysis apparatus 5 is supplied to the gasification furnace 2. By setting such a pressure level, the oxygen generated by the water electrolysis apparatus 5 can be smoothly supplied to the gasification furnace 2 without blowing back from the gasification furnace 2.

Hydrogen produced by the water electrolysis apparatus 5 and supplied to the gasification gas passage 3 a is introduced into the liquid fuel synthesis reactor 6. In the liquid fuel synthesis reactor 6, the gasification gas is synthesized into a liquid fuel such as methanol at an operating temperature of about 300 ° C., and the liquid fuel is synthesized and manufactured. This liquid fuel is taken out by the liquid fuel take-out means 7 and used as fuel for various engines.
On the other hand, about 300 ° C. off-gas from the liquid fuel synthesis reactor 6 is supplied to the gas turbine 8 to drive the gas turbine 8.
The exhaust gas discharged from the gas turbine 8 generates steam by heating the feed water with the exhaust heat recovery boiler 9, and then is discharged into the atmosphere through the exhaust gas discharging means 12 such as an exhaust gas purification device. The steam generated in the exhaust heat recovery boiler 9 is introduced into the steam turbine 10 to drive the steam turbine 10. Condensate from the steam turbine 10 is returned to the exhaust heat recovery boiler 9.

According to the first embodiment, the hydrogen produced in the water electrolysis apparatus 5 is introduced into the liquid fuel synthesis reactor 6 to be used for producing liquid fuel from the gasification gas. The CO shift reactor 41 for converting (carbon monoxide) to H ₂ (hydrogen) is not necessary.
For this reason, it is sufficient to raise the temperature of the gasification gas leaving the gas purification apparatus 3 (operation temperature 40 to -15 ° C.) to about 300 ° C., which is the reaction temperature of the liquid fuel synthesis reactor 6, It is not necessary to raise to about 500 ° C., which is the reaction temperature of the CO shift reactor 41 as in the technology, and therefore the temperature of each element through which the gasification gas flows is about 400 ° C. (gasification furnace 2). → 40 to -15 ° C. (gas purification device 3) → 300 ° C. (liquid fuel synthesis reactor 6), and the temperature amplitude of the temperature change is smaller than that in the conventional technique.
Thereby, compared with the said prior art, the heat loss of gasification gas can be reduced and the plant efficiency concerning the synthesis | combination of the liquid fuel by gasification gas and the electric power generation by a gas turbine drive improves.

  Further, as described above, the CO shift reactor 41 and the steam supply means 42 and the cooler 43 to the CO shift reactor 41 in the prior art are unnecessary, and the pressure loss of the system is reduced and the paper plant efficiency is improved. In addition to simplifying the device, it is possible to improve economy (lower costs).

  Further, according to the first embodiment, oxygen generated by the water electrolysis apparatus 5 is jetted into the gasification furnace 2 to gasify the solid fuel together with oxygen from the air separation apparatus 4. Therefore, the amount of oxygen supplied from the air separation device 4 to the gasification furnace 2 can be reduced, and the driving power of the air separation device 4 can be reduced.

FIG. 2 is a system diagram showing an overall configuration of a solid fuel gasification gas utilization plant according to a second embodiment of the present invention.
In the second embodiment, a hydrogen power recovery turbine 14 driven by hydrogen generated by the water electrolyzer 5 and an oxygen power recovery driven by oxygen generated by the water electrolyzer 5. A turbine 13 is provided. Then, the hydrogen power recovery turbine 14 is driven by the expansion work of the hydrogen generated by the water electrolysis apparatus 5 to supply sufficiently expanded hydrogen to the liquid fuel synthesis reactor 6, and the water electricity The oxygen power recovery turbine 1 is driven by the expansion work of oxygen generated by the decomposition apparatus 5, thereby supplying sufficiently expanded oxygen to the gasifier 2.
In this case, the electrolysis pressure of water in the water electrolysis apparatus 5 exceeds the pressure of the gasifier 2 and is maintained in the subcritical range of water.
Other configurations are the same as those of the first embodiment, and the same members are denoted by the same reference numerals.

  According to the second embodiment, the hydrogen power recovery turbine 14 is driven by the hydrogen generated by the increase in the electrolysis pressure due to the compression of water in the water electrolyzer 5, and the water electrolyzer 5 generates the water. By driving the oxygen power recovery turbine 13 with oxygen, the energy of the water electrolyzer 5 can be recovered by the hydrogen power recovery turbine 14 and the oxygen power recovery turbine 13. Plant efficiency related to power generation by turbine drive can be improved.

FIG. 3 is a system diagram showing an overall configuration of a solid fuel gasification gas utilization plant according to a third embodiment of the present invention.
In the third embodiment, when the gasification furnace 2 is started, a part of the compressed air is extracted from the gas turbine 8, and this air is supplied to the gasification furnace 2 through an air pipe 8 a provided with an opening / closing valve 17. Supply.
Further, in the third embodiment, when the gasification furnace 2 is started, the steam extracted from the steam turbine 10 is led to the compressor driving means 16 that converts it into compressor driving power, and the compressor driving means 16 starts the auxiliary auxiliary compressor. 15 is driven, and compressed air from the starting auxiliary compressor 15 is supplied to the gasifier 2 through an air pipe 10 a provided with an on-off valve 18.
The on-off valve 17 is opened when the compressed air from the gas turbine 8 is sent to the gasification furnace 2, and the on-off valve 18 is opened when the compressed air from the auxiliary start compressor 15 is sent to the gasification furnace 2.
In addition, about the air supply means (8a-17) from a gas turbine to a gasifier, and the air supply means (16-15-10a-18) by steam turbine extraction steam, both or any one means is comprised. It may be.
This embodiment can also be applied to a solid fuel gasification gas utilization plant in which the liquid fuel synthesis reactor 6 is not provided and the gasification gas is directly fed to the gas turbine 8.
Other configurations are the same as those of the first embodiment, and the same members are denoted by the same reference numerals.

  According to the third embodiment, the compressed air extracted from the gas turbine 8 and compressed air from the start-up auxiliary compressor 15 driven by the steam extracted from the steam turbine as oxygen of the gasifying agent of the gasifier 2. Therefore, the capacity of the air separation device 4 can be reduced to the capacity of the utility required for the plant, and the device cost can be reduced.

  In the third embodiment, as indicated by a chain line in FIG. 3, as in the second embodiment, a hydrogen power recovery turbine 14 driven by hydrogen generated by the water electrolyzer 5; And an oxygen power recovery turbine 13 driven by oxygen generated by the water electrolyzer 5, and the hydrogen power recovery turbine 14 is driven by the expansion work of hydrogen generated by the water electrolyzer 5. The fully expanded hydrogen is supplied to the liquid fuel synthesizing reactor 6 and the oxygen power recovery turbine 13 is driven by the expansion work of the oxygen generated in the water electrolysis apparatus 5 to sufficiently expand the oxygen gas. It is also possible to configure so as to supply to the chemical furnace.

FIG. 4 is a system diagram showing an overall configuration of a solid fuel gasification gas utilization plant according to a fourth embodiment of the present invention.
In the fourth embodiment, on the outlet side of exhaust gas, that is, on the downstream side of the exhaust gas discharge means 12, the exhaust gas after driving the gas turbine 8 is cooled and compressed to generate CO ₂ rich gas and water, CO ₂ recovery A facility 20 and a CO ₂ compression storage facility 21 are provided.
The water and water from the CO ₂ recovery means are supplied to the water electrolyzer 5 through the water pipe 20a and used for electrolysis water.
Further, the CO ₂ rich gas compressed and stored in the CO ₂ compression storage facility 21 is supplied to the gasification furnace 2 through the gas pipe 21a and used as a gasifying agent and also as a utility gas.

According to the above fourth embodiment, the exhaust gas is cooled and compressed on the outlet side of the exhaust gas to provide the CO ₂ rich gas and water, the CO ₂ recovery facility 20 and the CO ₂ compression storage facility 21, Since CO ₂ is recovered, CO ₂ emission from the plant can be reduced.
Further, the CO ₂ from the CO ₂ recovery facility 20 and CO ₂ compression storage facility 21 enables utilization as a gasifying agent for gasifying furnace 2, air for supplying gasifying agent (oxygen) to the gasifier 2 Separation device 4 becomes unnecessary.
Furthermore, by using the recovered water from the CO ₂ recovery facility 20 and the CO ₂ compression storage facility 21 as the electrolyzed water of the water electrolysis device 5, the amount of hydrogen produced in the water electrolysis device 5 can be increased, and the liquid fuel The production amount of can be increased.
Other configurations are the same as those of the first embodiment, and the same members are denoted by the same reference numerals.

  In the fourth embodiment, as indicated by a chain line in FIG. 4, as in the second embodiment, a hydrogen power recovery turbine 14 driven by hydrogen generated by the water electrolyzer 5; And an oxygen power recovery turbine 13 driven by oxygen generated by the water electrolyzer 5, and the hydrogen power recovery turbine 14 is driven by the expansion work of hydrogen generated by the water electrolyzer 5. The fully expanded hydrogen is supplied to the liquid fuel synthesizing reactor 6 and the oxygen power recovery turbine 13 is driven by the expansion work of the oxygen generated in the water electrolysis apparatus 5 to sufficiently expand the oxygen gas. It is also possible to configure so as to supply to the chemical furnace.

  According to the present invention, in a plant that uses gasified gas for both synthesis of liquid fuel and power generation by gas turbine drive, the temperature amplitude of the temperature change between each element through which the gasified gas flows is reduced and applied. It is possible to provide a solid fuel gasification gas utilization plant in which heat loss of gasification gas due to change is reduced and plant efficiency related to synthesis of liquid fuel by gasification gas and power generation by gas turbine drive is improved.

1 is a system diagram showing an overall configuration of a solid fuel gasification gas utilization plant according to a first embodiment of the present invention. FIG. FIG. 3 is a view corresponding to FIG. 1 showing a second embodiment of the present invention. FIG. 6 is a view corresponding to FIG. 1 showing a third embodiment of the present invention. FIG. 6 is a view corresponding to FIG. 1 showing a fourth embodiment of the present invention. It is a systematic diagram which shows an example of the conventional of the gasification gas utilization plant of solid fuel.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Solid fuel supply means 2 Gasification furnace 3 Gas purification apparatus 4 Air separation apparatus 5 Water electrolysis apparatus 6 Liquid fuel synthesis reactor 8 Gas turbine 8a Air pipe 9 Waste heat recovery boiler 10 Steam turbine 10a Air pipe 13 Power recovery for oxygen Turbine 14 Power recovery turbine for hydrogen 15 Start-up auxiliary compressor 16 Compressor drive means 20 Water, CO ₂ recovery facility 21 CO ₂ compression storage facility

Claims (6)

  A solid fuel containing coal is supplied to a gasification furnace, the solid fuel is gasified using oxygen supplied from an oxygen supply means in the gasification furnace, and the liquid fuel is synthesized by the liquid fuel synthesizing means. In a solid fuel gasification gas utilization plant that is manufactured and configured to drive a gas turbine by off-gas from the liquid fuel synthesizing means, a water electrolysis apparatus is provided that electrolyzes water to generate hydrogen and oxygen. Supplying hydrogen generated in the water electrolyzer to the gasified gas passage upstream of the liquid fuel synthesizing means, and setting the operation pressure of the water electrolyzer higher than the pressure in the gasifier Then, the solid fuel gasification gas utilization plant is configured to supply oxygen generated by the water electrolysis apparatus to the gasification furnace.   The apparatus further comprises start air supply means for starting the gasification furnace using one or both of air extracted from the gas turbine and air generated by the energy of the gasification gas. Item 6. The solid fuel gasification gas utilization plant according to Item 1.   A solid fuel containing coal is supplied to a gasification furnace, the solid fuel is gasified using oxygen supplied from an oxygen supply means in the gasification furnace, and a gas turbine is driven by the gasification gas. In the solid fuel gasification gas utilization plant, the start-up air supply for starting up the gasification furnace using one or both of the air extracted from the gas turbine and the air generated by the energy of the gasification gas A solid fuel gasification gas utilization plant characterized by comprising means.   The air generated by the energy of the gasified gas is configured to be generated by a compressor driven by the energy of steam from an exhaust heat recovery boiler attached to the gas turbine. Or the solid fuel gasification gas utilization plant of any one of claim | item 3. The exhaust gas after the gas turbine driving cooling water compressed to produce a CO _2-rich gas and water, the CO ₂ recovery unit provided, water, and supplies the water from the CO ₂ recovery unit to the water electrolyzer with use in the electrolysis of water, water, CO ₂ rich gas to the solid fuel gasification gas utilization according to claim 1, characterized in that it is arranged to supply to said gasification furnace from the CO ₂ recovery unit plant.   An oxygen expansion turbine that is driven by oxygen is provided in an oxygen passage that supplies oxygen generated by the water electrolyzer to the gasifier, and hydrogen generated by the water electrolyzer is supplied to the liquid fuel synthesizing means. 6. The solid fuel gasification gas utilization plant according to any one of claims 1, 2, and 5, wherein a hydrogen expansion turbine driven by the hydrogen is provided in a hydrogen passage to be supplied to the plant.

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