JP2021170961A - Organic substance manufacturing method and organic substance manufacturing equipment - Google Patents

Abstract

To appropriately prevent a heat exchanger from being corroded by corrosive gas contained in synthetic gas.SOLUTION: A method for manufacturing an organic substance comprises the steps of: gasifying waste in a gasifier 11 to generate synthetic gas G1; cooling the synthetic gas G1 discharged from the gasifier 11 by passing it through a heat exchanger 14; producing an organic substance by bringing at least the synthetic gas G1 that has passed through the heat exchanger 14 into contact with a catalyst; and heating the heat exchanger 14 before passing the synthetic gas G1 through the heat exchanger 14.SELECTED DRAWING: Figure 1

Description

The present invention relates to a method for producing an organic substance using synthetic gas as a raw material, and an organic substance manufacturing apparatus for producing an organic substance using synthetic gas as a raw material.

Various types of waste such as industrial waste and general waste are generally completely burned. The exhaust gas discharged by complete combustion has a high temperature and is heat-recovered by a heat exchanger such as a boiler, and the recovered heat energy is used for power generation and the like. Waste contains a lot of miscellaneous components, and exhaust gas contains a lot of dust with a small particle size including chlorine, sulfur, heavy metals, etc., and the dust adheres to heat exchangers such as boilers. May cause performance degradation. Therefore, for example, as disclosed in Patent Documents 1 and 2, it is known that a dust removing device for removing dust adhering to a boiler is provided.

Further, a technique is widely known in which a gas is generated by thermal decomposition of waste in a gasification furnace and then reformed to obtain a synthetic gas by reforming the gas generated in the reforming furnace. The obtained synthetic gas is often used for power generation and the like. Further, in recent years, attempts have been made to use synthetic gas as a raw material for chemical synthesis, and for example, it has been attempted to convert it into an organic substance such as ethanol by a catalyst such as a microbial catalyst or a metal catalyst (for example, a patent). Reference 3).

When an organic substance such as ethanol is obtained from a synthetic gas using a catalyst, the synthetic gas needs to be cooled to a temperature of, for example, 200 ° C. or lower. Therefore, it is necessary to recover the heat of the synthetic gas by a heat exchanger such as a boiler as in the case of the complete combustion gas.
When synthetic gas is generated, complete combustion is not performed, and therefore, a large amount of corrosive gas such as _{SO 2} and SO _{3 is present in the gas.} Corrosive gases, when cooled by the heat exchanger, is liquefied below the dew point, the cause of corrosion of the heat exchanger becomes like H ₂ SO ₄ (e.g., see Non-Patent Document 1).

In order to avoid corrosion of the heat exchanger, it is conceivable to use resin or ceramic as a carrier of the heat exchanger, but the resin cannot be used for heat recovery at high temperature, and the ceramic has heat recovery efficiency and impact resistance. It has low properties, and it is difficult to use any of them practically for cooling synthetic gas.

JP-A-2019-158166 Japanese Patent No. 6603759 International Publication No. 2015/037710

Anticorrosion Technology, Vol. 26, pp. 731-740, 1977, "Sulfuric Acid Dew Point Corrosion", Hiroo Nagano

Therefore, according to the present invention, in a method for producing an organic substance from a synthetic gas generated from waste and an organic substance manufacturing apparatus, corrosion of a heat exchanger by a corrosive gas contained in the synthetic gas is appropriately applied. The challenge is to prevent it.

As a result of diligent studies, the present inventors have found that corrosion of the heat exchanger by the corrosive gas contained in the synthetic gas occurs remarkably at the start of continuous operation when the temperature of the heat exchanger is low. Then, as a result of further studies based on the findings, it was found that the above problem can be solved by preheating the heat exchanger to a predetermined temperature or higher before passing the synthetic gas through the heat exchanger. Was completed.
That is, the present invention provides the following [1] to [16].
[1] A process of gasifying waste to generate syngas in a gasifier,
A step of cooling the synthetic gas discharged from the gasifier by passing it through a heat exchanger.
At least the step of bringing the synthetic gas that has passed through the heat exchanger into contact with the catalyst to generate an organic substance, and
A method for producing an organic substance, which comprises a step of heating the heat exchanger before passing the synthetic gas through the heat exchanger.
[2] Further provided with a process of completely burning waste to generate complete combustion gas.
The method for producing an organic substance according to the above [1], wherein the heat exchanger is heated by the heat energy of the complete combustion gas before the synthetic gas is passed through the heat exchanger.
[3] The heat exchanger includes a gas flow path through which the synthetic gas is passed and a cooling medium flow path through which a cooling medium for cooling the synthetic gas is passed.
The method for producing an organic substance according to the above [2], wherein the heat exchanger is heated by passing the complete combustion gas through either the gas flow path or the cooling medium flow path.
[4] The heat exchanger includes a gas flow path through which a synthetic gas is passed and a cooling medium flow path through which a cooling medium for cooling the synthetic gas is passed.
In the heat exchanger for heating, the heat medium is heated by the heat energy of the complete combustion gas, and the heat medium is heated.
The method for producing an organic substance according to the above [2], wherein the heat exchanger is heated by passing the heated heat medium through either the gas flow path or the cooling medium flow path.
[5] The method for producing an organic substance according to any one of the above [2] to [4], wherein the waste is completely burned by a combustion device to generate the complete combustion gas.
[6] The method for producing an organic substance according to any one of [1] to [5] above, wherein the heat exchanger is heated to 200 ° C. or higher before the synthetic gas is passed through the heat exchanger.
[7] The method for producing an organic substance according to any one of the above [1] to [6], wherein the catalyst is a microbial catalyst.
[8] The method for producing an organic substance according to any one of the above [1] to [7], wherein the organic substance contains ethanol.
[9] A gasifier that gasifies waste to generate synthetic gas,
A heat exchanger that allows synthetic gas discharged from the gasifier to pass through and cools it.
It is provided with an organic substance generating unit that produces an organic substance by contacting a synthetic gas that has passed at least the heat exchanger with a catalyst.
An organic substance manufacturing apparatus capable of heating the heat exchanger before passing the syngas through the heat exchanger.
[10] The organic substance manufacturing apparatus according to the above [9], wherein the heat exchanger can be heated by the heat energy of the complete combustion gas obtained by completely burning the waste.
[11] The heat exchanger includes a gas flow path through which a synthetic gas is passed and a cooling medium flow path through which a cooling medium for cooling the synthetic gas is passed.
The organic substance manufacturing apparatus according to the above [10], wherein the heat exchanger is heated by passing the complete combustion gas obtained by completely burning the waste through either the gas flow path or the cooling medium flow path. ..
[12] The heat exchanger includes a gas flow path through which a synthetic gas is passed and a cooling medium flow path through which a cooling medium for cooling the synthetic gas is passed.
The organic substance manufacturing apparatus further includes a heat exchanger for heating that heats a heat medium with the thermal energy of the complete combustion gas.
The organic substance manufacturing apparatus according to the above [10], wherein the heat exchanger is heated by passing the heated heat medium through either the gas flow path or the cooling medium flow path.
[13] The organic substance manufacturing apparatus according to any one of [10] to [12] above, further comprising a combustion apparatus that completely burns the waste to generate the complete combustion gas.
[14] The organic substance manufacturing apparatus according to any one of [9] to [13] above, wherein the heat exchanger can be heated to 200 ° C. or higher before the synthetic gas is passed through the heat exchanger. ..
[15] The organic substance manufacturing apparatus according to any one of the above [9] to [14], wherein the catalyst is a microbial catalyst.
[16] The organic substance manufacturing apparatus according to any one of the above [9] to [15], wherein the organic substance contains ethanol.

According to the present invention, in a method for producing an organic substance by producing an organic substance from a synthetic gas generated from waste and an organic substance manufacturing apparatus, corrosion of a heat exchanger by a corrosive gas contained in the synthetic gas is appropriately performed. Can be prevented.

It is a schematic diagram which shows the whole structure of the organic substance manufacturing apparatus which concerns on 1st Embodiment of this invention. It is a schematic diagram which shows the whole structure of the organic substance manufacturing apparatus which concerns on 2nd Embodiment of this invention. It is a schematic diagram which shows the whole structure of the organic substance manufacturing apparatus which concerns on 3rd Embodiment of this invention.

Next, the present invention will be described with reference to the drawings.
<First Embodiment>
FIG. 1 shows an organic substance manufacturing apparatus according to a first embodiment of the present invention. Hereinafter, the organic substance manufacturing apparatus and the method for producing an organic substance according to the embodiment of the present invention will be described in detail with reference to the first embodiment.

In the first embodiment, the organic substance manufacturing apparatus 10 includes a gasification apparatus 11, a heat exchanger 14, a combustion apparatus 15, a heat exchanger 16 for complete combustion gas, and an organic substance generating unit 17.

(Gasifier)
The gasifier 11 gasifies the waste to generate the synthetic gas G1. The waste may be industrial waste such as industrial solid waste, general waste such as urban solid waste (MSW), plastic waste, garbage, waste tires, biomass waste, food waste. , Building materials, wood, wood chips, fibers, papers and other flammable substances. Of these, municipal solid waste (MSW) is preferred.

The gasifier 11 includes a gasifier 12 and a reformer 13. The gasification furnace 12 is not particularly limited, and examples thereof include a kiln gasification furnace, a fixed bed gasification furnace, a fluidized bed gasification furnace, a shaft type furnace, a plasma gasification furnace, and a carbonization furnace. In addition to waste, oxygen or air and, if necessary, steam are introduced into the gasification furnace 12. The gasification furnace 12 thermally decomposes the waste by heating it at, for example, 500 to 700 ° C., and appropriately partially oxidizes the waste to gasify it. The pyrolysis gas includes not only carbon monoxide and hydrogen, but also gaseous tar, powdered char and the like. The pyrolysis gas is supplied to the reforming furnace 13. Solids and the like generated as incombustibles in the gasification furnace 12 are appropriately recovered.

In the reforming furnace 13, the pyrolysis gas obtained by the gasifier 11 is reformed to obtain the synthetic gas G1. In the reforming furnace 13, the content of at least one of hydrogen and carbon monoxide in the pyrolysis gas increases, and the gas is discharged as the synthetic gas G1. In the reforming furnace 13, for example, tar, char, etc. contained in the pyrolysis gas are reformed into hydrogen, carbon monoxide, and the like.
The temperature of the synthetic gas G1 in the reforming furnace 13 is not particularly limited, but is, for example, 900 ° C. or higher, preferably 900 ° C. or higher and 1300 ° C., and more preferably 1000 ° C. or higher and 1200 ° C. or lower. By setting the temperature in the reforming furnace 13 within the above range, it becomes easy to obtain a synthetic gas G1 having a high content of carbon monoxide and hydrogen.

The temperature of the synthetic gas G1 discharged from the reformer 13 (that is, the gasifier 11) is the same as the temperature of the synthetic gas G1, for example, 900 ° C. or higher, preferably 900 ° C. or higher and 1300 ° C., more preferably. It is 1000 ° C. or higher and 1200 ° C. or lower.
The synthetic gas G1 discharged from the reformer 13 (that is, the gasifier 11) contains carbon monoxide and hydrogen. Further, the synthetic gas G1 contains, for example, carbon monoxide in an amount of 0.1% by volume or more and 80% by volume or less, and hydrogen in an amount of 0.1% by volume or more and 80% by volume or less.
The carbon monoxide concentration in the synthetic gas G1 is preferably 10% by volume or more and 70% by volume or less, and more preferably 20% by volume or more and 55% by volume or less. The hydrogen concentration in the synthetic gas G1 is preferably 10% by volume or more and 70% by volume or less, and more preferably 20% by volume or more and 55% by volume or less.

Syngas G1 may contain carbon dioxide, nitrogen, oxygen and the like in addition to hydrogen and carbon monoxide. The carbon dioxide concentration in the synthetic gas G1 is not particularly limited, but is preferably 0.1% by volume or more and 40% by volume or less, and more preferably 0.3% by volume or more and 30% by volume or less. The carbon dioxide concentration is particularly preferably lowered when ethanol is produced by using a microbial catalyst, and from such a viewpoint, it is more preferably 0.5% by volume or more and 25% by volume or less.
The nitrogen concentration in the synthetic gas G1 is usually 50% by volume or less, preferably 1% by volume or more and 20% by volume or less.
The oxygen concentration in the synthetic gas G1 is usually 5% by volume or less, preferably 1% by volume or less. Further, the oxygen concentration should be as low as possible, and may be 0% by volume or more. However, in general, oxygen is inevitably contained in many cases, and the oxygen concentration is practically 0.01% by volume or more.

The concentrations of carbon monoxide, carbon dioxide, hydrogen, nitrogen and oxygen in the synthetic gas G1 are the type of waste, the temperature of the gasifier 12 and the reformer 13, and the oxygen concentration of the supply gas supplied to the gasifier 11. By appropriately changing the combustion conditions such as, the predetermined range can be obtained. For example, if you want to change the concentration of carbon monoxide or hydrogen, change to waste with a high ratio of hydrocarbons (carbon and hydrogen) such as waste plastic, and if you want to reduce the nitrogen concentration, change the oxygen concentration in the gasifier 12. There is a method of supplying high gas.
Further, the concentration of each component of carbon monoxide, carbon dioxide, hydrogen and nitrogen may be appropriately adjusted in the synthetic gas G1. The concentration may be adjusted by adding at least one of these components to the synthetic gas G1.
The volume% of each substance in the above-mentioned synthetic gas G1 means the volume% of each substance in the synthetic gas G1 discharged from the gasifier 11.

In the above, the mode in which the gasification device 11 includes the gasification furnace 12 and the reforming furnace 13 has been described, but the configuration of the gasification device 11 is not limited to these, and the gasification furnace and the reforming furnace are included. It may be an integrated device, or any type of gasification device as long as it can generate the synthetic gas G1.
Further, in the present embodiment, the supply of the synthetic gas G1 from the gasifier 11 is started after the heat exchanger 14 is heated by the complete combustion gas G2 generated by the combustion device 15, as will be described later. Therefore, the operation of the gasification device 11 may be started after the start of operation of the combustion device 15 described later.

(Heat exchanger)
The synthetic gas G1 discharged from the gasifier 11 passes through the heat exchanger 14. The heat exchanger 14 is a device that cools the syngas G1 using a medium. The heat exchanger 14 cools the synthetic gas G1 by transferring the heat energy of the synthetic gas G1 to a medium (hereinafter, also referred to as “cooling medium M1”). The heat exchanger 14 is provided with, for example, a partition wall system, and includes a gas flow path 14A through which the synthetic gas G1 is passed and a cooling medium flow path 14B through which the cooling medium M1 for cooling the synthetic gas G1 is passed. The inner surface of the gas flow path 14A may be formed of metal. As the metal, steel materials such as stainless steel and other alloys can be used. Examples of stainless steel include austenitic stainless steel, ferritic stainless steel, and martensitic stainless steel. In addition, Hastelloy and the like can also be used. Further, the inner surface of the gas flow path may be appropriately coated with a protective film.
The cooling medium M1 may be either a gas or a liquid, or may be accompanied by a phase change between the gas and the liquid. Further, the cooling medium flow path 14B may have any shape such as a tubular shape or a plate shape. In the cooling medium M1, the thermal energy from the synthetic gas G1 passing through the gas flow path 14A is transferred in a state of being passed through the cooling medium flow path 14B.

A boiler is preferably used as the heat exchanger 14. The boiler is a device in which water as a cooling medium M1 is circulated inside the cooling medium flow path 14B, and the circulated water is heated by the heat energy of the synthetic gas G1 to be steamed. When the boiler is used as the heat exchanger 14, the steam generated in the boiler makes it possible to easily heat other devices, and the heat energy of the synthetic gas G1 can be easily reused.

As described above, the heat exchanger 14 cools the synthetic gas G1 supplied at a high temperature of, for example, 900 ° C. or higher, preferably at a temperature of 200 ° C. or higher. The synthetic gas G1 _{contains corrosive gases such as SO 2} and SO ₃ , but the temperature of the heat exchanger 14 is also maintained at 200 ° C. or higher by setting the cooling temperature to 200 ° C. or higher. Therefore, it is possible to prevent the heat exchanger 14 from being corroded by the corrosive gas without the corrosive gas falling below the dew point. Further, by setting the temperature to 200 ° C. or higher, even when the organic substance is synthesized by the metal catalyst in the organic substance generation unit 17, it is possible to prevent unnecessary heating in the subsequent processing apparatus.

In the heat exchanger 14, the synthetic gas G1 is more preferably cooled to a temperature of 240 ° C. or higher. By cooling the synthetic gas G1 to a temperature of 240 ° C. or higher, the temperature of the heat exchanger 14 is also maintained at 240 ° C. or higher, and the precipitation of tar content in the heat exchanger 14 can be effectively prevented. When the waste is gasified, the synthetic gas G1 contains a large amount of tar, but by preventing the precipitation of tar, clogging due to tar can be prevented in the heat exchanger 14.

Further, in the heat exchanger 14, it is preferable that the synthetic gas G1 is cooled to a temperature of 400 ° C. or lower. When the temperature is 400 ° C. or lower, even if the synthetic gas G1 is supplied to the organic substance generation unit 17 without being cooled more than necessary in the subsequent processing apparatus (post-stage processing apparatus 18), the organic substance generation unit 17 is appropriate. Can produce organic matter. Further, it is possible to prevent the heat exchanger 14 from being corroded by chlorine or the like contained in the synthetic gas G1. Further, from the viewpoint of further simplifying the cooling process in the subsequent processing apparatus (post-stage processing apparatus 18), the heat exchanger 14 cools the synthetic gas G1 to a temperature of more preferably 300 ° C. or lower, still more preferably 280 ° C. or lower. do.

The synthetic gas G1 that has passed through the heat exchanger 14 is sent to the organic substance generation unit 17. As shown in FIG. 1, the synthetic gas G1 is usually sent to the organic substance generation unit 17 after being appropriately treated in the post-stage treatment device 18.
In the present embodiment, the organic substance generating unit 17 is continuously operated. That is, in the gasifier 11, the waste is continuously burned, and the synthetic gas G1 is continuously passed through the heat exchanger 14, while the synthetic gas G1 is kept within the above temperature range by the heat exchanger 14. It is cooled to be maintained and discharged from the heat exchanger 14. Then, the synthetic gas G1 discharged from the heat exchanger 14 is continuously supplied to the organic substance generating section 17, and the organic substance is continuously generated in the organic substance generating section 17.

(Combustion device)
The combustion device 15 is a device that completely burns waste to generate a complete combustion gas, and includes, for example, a gasification furnace 19 and a combustion furnace 20.
The gasification furnace 19 is not particularly limited, and examples thereof include a kiln gasification furnace, a fixed bed gasification furnace, and a fluidized bed gasification furnace. In addition to waste, oxygen or air and, if necessary, steam are introduced into the gasification furnace 19. The gasification furnace 19 thermally decomposes the waste by heating it at, for example, 400 to 2000 ° C., and appropriately partially oxidizes the waste to gasify it. The pyrolysis gas includes, but is not limited to, flammable organic gases such as carbon dioxide, carbon monoxide, hydrogen, methane, and ethane, and also includes gaseous tar, powdered char, and the like. The pyrolysis gas is supplied to the combustion furnace 20. Solids and the like generated as incombustibles in the gasification furnace 19 are appropriately recovered.

The combustion furnace 20 is not limited as long as it is an apparatus capable of completely burning the pyrolysis gas supplied from the gasification furnace 19, but a known incinerator may be used. Oxygen or air is supplied to the combustion furnace 20 to completely burn the pyrolysis gas.
The combustion furnace 20 is not particularly limited as long as it can completely burn the pyrolysis gas obtained from the waste, but it is preferable to burn the pyrolysis gas at a temperature of, for example, 300 to 2000 ° C, preferably 600 to 1300 ° C. The gas discharged from the combustion furnace 20 may be mainly composed of carbon dioxide, oxygen, steam and the like.
In addition, in this specification, complete combustion includes not only combustion in which carbon monoxide is not generated at all but also combustion in which only a small amount of carbon monoxide is generated. In the exhaust gas exhausted from the combustion device 15 (hereinafter, also referred to as “complete combustion gas G2”), the content of carbon monoxide is less than that in the synthetic gas G1 exhausted to the gasifier 11, for example. It may be 15% by volume or less, preferably 10% by volume or less, more preferably 5% by volume or less, still more preferably 3% by volume or less, and most preferably 0% by volume.

(Heat exchanger for heating)
The complete combustion gas G2 exhausted from the combustion device 15 is supplied to the heating heat exchanger 16. The heating heat exchanger 16 is a device that heats the heat medium M2 by transferring the heat energy of the complete combustion gas G2 to a medium (hereinafter, also referred to as “heat medium M2”).
The heating heat exchanger 16 uses, for example, a partition wall system, and includes a complete combustion gas flow path 16A through which the complete combustion gas G2 passes, and a heat medium flow path 16B through which the heat medium M2 passes. The heat medium M2 may be either a gas or a liquid, or may be accompanied by a phase change between the gas and the liquid.

The heat medium flow path 16B may have any shape such as a tubular shape or a plate shape. The heat medium M2 is heated by transferring the heat energy from the complete combustion gas G2 passing through the complete combustion gas flow path 16A in a state of being passed through the heat medium flow path 16B.
The complete combustion gas G2 is a gas derived from waste, but since it is completely burned, the content of corrosive gas is low. Therefore, even if the complete combustion gas G2 passes through the heating heat exchanger 16, the heating heat exchanger 16 is not easily corroded by the corrosive gas.

In the heating heat exchanger 16, the heated heat medium M2 can be supplied to the heat exchanger 14. Specifically, a heat medium supply flow path 21 for connecting the heating heat exchanger 16 and the heat exchanger 14 is provided, and the heat medium M2 is the heating heat exchanger 16 via the heat medium supply flow path 21. Is supplied to the heat exchanger 14.
In this embodiment, the heat medium M2 supplied to the heat exchanger 14 passes through the gas flow path 14A inside the heat exchanger 14. Thereby, the inner surface of the gas flow path 14A of the heat exchanger 14 can be easily heated. Further, as will be described later, when switching from the supply of the heat medium M2 to the supply of the synthetic gas G1 to the heat exchanger 14, the heat exchanger 14 once heated is not cooled by the atmosphere or the like, and the heat medium M2 is not cooled. Subsequently, the synthetic gas G1 can continuously maintain the temperature of the heat exchanger 14 above a certain level.
The temperature of the heat medium M2 supplied to the heat exchanger 14 is preferably 200 ° C. or higher, more preferably 240 ° C. or higher, and preferably 400 ° C. or lower, more preferably 300 ° C. or lower, still more preferably 280 ° C. or higher. It is as follows.

The heat medium M2 may be either a gas or a liquid, but is preferably a gas. Among them, the heat exchanger 16 for heating is preferably a boiler and the heat medium M2 is preferably steam. By using gas, especially steam, as the heat medium M2, the heat exchanger 14 can be efficiently and easily not retained not only in the heat medium flow path 16B but also in the gas flow path 14A of the heat exchanger 14. Can be heated.

The gasifier 11 is continuously operated, and the synthetic gas G1 is continuously passed through the heat exchanger 14 by the continuous operation. In the present embodiment, before the synthetic gas G1 is passed through the heat exchanger 14, the heat medium M2 heated in the heating heat exchanger 16 is supplied to the heat exchanger 14, and the heat exchanger 14 is subjected to the heat exchanger 14. Let it pass.
The heat exchanger 14 is heated to a certain temperature or higher by passing through the heated heat medium M2. Specifically, the heat exchanger 14 is heated to preferably 200 ° C. or higher, more preferably 240 ° C. or higher. Then, after being heated to a certain temperature or higher, the supply of the synthetic gas G1 to the heat exchanger 14 is started, the synthetic gas G1 is passed through the heat exchanger 14, and the continuous operation of the organic substance generating unit 17 is started. ..
That is, at the time when the passage of the synthetic gas G1 is started during continuous operation, the temperature of the heat exchanger 14 has already been heated to a certain temperature or higher (preferably 200 ° C. or higher, more preferably 240 ° C. or higher).
The heat exchanger 14 is heated to a temperature of preferably 400 ° C. or lower, more preferably 300 ° C. or lower, still more preferably 280 ° C. or lower by passing through the heated heat medium M2. By setting the temperature of the heat exchanger 14 to 400 ° C. or lower, it is possible to prevent the heat exchanger 14 from being heated more than necessary by the heat medium M2.
Here, the temperature of the heat exchanger 14 means the temperature of the heat exchanger 14 at the position where the synthetic gas G1 comes into contact, and when the heat exchanger 14 has the gas flow path 14A as described above, the gas flow path 14A The temperature of the inner surface of.

Before passing through the synthetic gas G1 and the heat medium M2, the temperature of the heat exchanger 14 is generally around room temperature (for example, about 0 to 40 ° C.). When the synthetic gas G1 supplied from the gasifier 11 is passed through such a heat exchanger 14 near room temperature, a _{large amount of corrosive gas such as SO 2} and SO ₃ is a liquid substance (for example, H ₂ SO). ₄ ) to corrode the heat exchanger 14. However, in the present embodiment, by heating the heat exchanger 14 in advance, it is suppressed that the corrosive gas becomes a liquid substance even at the time when the passage of the synthetic gas G1 is started, thereby heat exchange. It is possible to appropriately prevent the vessel 14 from being corroded by the corrosive gas.

As described above, the combustion device 15 and the heat exchanger 16 for heating supply the heat medium M2 to the heat exchanger 14 before the synthetic gas G1 is supplied to the heat exchanger 14 during the continuous operation of the organic substance generating unit 17. It is used to do so. Therefore, when the continuous operation of the organic substance generating unit 17 is started, the operation of the combustion device 15 may or may not be stopped. Even if the operation is not stopped, the complete combustion gas G2 generated by the combustion device 15 heats the heat medium M2 in the heat exchanger 16 for heating, and the heated heat medium M2 is used as a device other than the heat exchanger 14. It is good to supply to and use it for other purposes such as power generation.

Further, in the above description, the mode in which the combustion device 15 includes the gasifier 19 and the combustion furnace 20 has been described, but the configuration of the combustion device 15 is not limited to these, and the gasifier and the combustion furnace are integrated. It may be a complete combustion device, or any type of combustion device as long as it can generate the complete combustion gas G2. For example, the combustion device 15 is an integrated type including a first combustion chamber that burns waste to generate gas and a second combustion chamber that secondarily burns the generated gas to generate complete combustion gas. A combustion device may be used.
The cooling medium M1 is supplied to the cooling medium flow path 14B when the heat exchanger 14 is heated by the heat energy of the complete combustion gas G2 (that is, when the heat medium M2 is supplied to the heat exchanger 14). It is preferable that the synthetic gas G1 is started at the same time as the heat exchanger 14 is supplied.

(Organic substance generator)
The synthetic gas G1 that has passed through the heat exchanger 14 is supplied to the organic substance generation unit 17. The organic substance generation unit 17 produces an organic substance by bringing the supplied synthetic gas G1 into contact with a catalyst such as a microbial catalyst or a metal catalyst. As the catalyst, a microbial catalyst is preferable. By using a microbial catalyst, it becomes possible to obtain an organic substance in a high yield at a low temperature. Further, as the microbial catalyst, gas-utilizing microorganisms are preferably used. The gas-utilizing microorganism is preferably a microorganism capable of producing ethanol.
The organic substance generation unit 17 includes a fermenter (reactor) filled with a culture solution containing water and a microbial catalyst. Syngas G1 is supplied to the inside of the fermenter, and the syngas G1 is converted into an organic substance inside the fermenter. The organic substance preferably contains ethanol.

The fermenter is preferably a continuous fermentation apparatus, and may be any of a stirring type, an air lift type, a bubble tower type, a loop type, an open bond type, and a photobio type.
The synthetic gas G1 and the culture solution may be continuously supplied to the fermenter, but it is not necessary to supply the synthetic gas G1 and the culture solution at the same time, and the synthetic gas G1 is supplied to the fermenter to which the culture solution has been supplied in advance. May be supplied. Syngas G1 is generally blown into a fermenter via a sparger or the like.
The medium used for culturing the microbial catalyst is not particularly limited as long as it has an appropriate composition according to the bacterium, but is limited to water as the main component and nutrients dissolved or dispersed in the water (for example, vitamins, phosphoric acid, etc.). It is a liquid containing and.
When a microbial catalyst is used, the organic substance generating unit 17 produces an organic substance by microbial fermentation of the microbial catalyst to obtain an organic substance-containing liquid.

The temperature of the fermenter is preferably controlled to 40 ° C. or lower. By controlling the temperature to 40 ° C. or lower, the microbial catalyst in the fermenter does not die, and the synthetic gas comes into contact with the microbial catalyst to efficiently generate an organic substance such as ethanol.
The temperature of the fermenter is more preferably 38 ° C. or lower, and in order to enhance the catalytic activity, it is preferably 10 ° C. or higher, more preferably 20 ° C. or higher, still more preferably 30 ° C. or higher.

Examples of the metal catalyst include a hydroactive metal or an aggregate of a hydroactive metal and a coactive metal. The hydride active metal may be, for example, a metal known as a metal capable of synthesizing ethanol from a mixed gas. For example, alkali metals such as lithium and sodium, manganese, renium and the like are included in Group 7 of the periodic table. Examples thereof include elements belonging to Group 8 of the periodic table such as ruthenium, elements belonging to Group 9 of the periodic table such as cobalt and rhodium, and elements belonging to Group 10 of the periodic table such as nickel and palladium.
One of these hydrogenated active metals may be used alone, or two or more thereof may be used in combination. Examples of the hydrogenated active metal include rhodium or ruthenium, such as a combination of rhodium, manganese and lithium, and a combination of ruthenium, renium and sodium, from the viewpoint of further improving the CO conversion rate and improving the selectivity of ethanol. A combination of an alkali metal and another hydroactive metal is preferable.

Examples of the coactive metal include titanium, magnesium, vanadium and the like. Since the coactive metal is supported in addition to the hydrogenated active metal, the CO conversion rate, the ethanol selectivity, and the like can be further increased.
As the metal catalyst, a rhodium-based catalyst is preferable. As the rhodium-based catalyst, a metal catalyst other than the rhodium-based catalyst may be used in combination. Examples of other metal catalysts include copper alone or a catalyst in which copper and a transition metal other than copper are supported on a carrier.
Even when a metal catalyst is used, it is preferable that the organic substance generating unit 17 is provided with a reactor, and the organic substance is generated by bringing the synthetic gas G1 into contact with the metal catalyst inside the reactor. The temperature inside the reactor is preferably maintained at, for example, 100 to 400 ° C, preferably 100 to 300 ° C.

(Refining equipment)
The organic substance production apparatus 10 may have a purification apparatus (not shown) for purifying the organic substance produced by the organic substance generation unit 17.
For example, when ethanol or the like is produced as a target product using a metal catalyst, a product containing an organic substance other than ethanol such as acetaldehyde and acetic acid in addition to ethanol is usually obtained. Therefore, a known purification device such as a distillation device may be used to purify the target organic substance (for example, ethanol) to obtain the target product.

When a microbial catalyst is used, an organic substance-containing liquid can be obtained as described above, but a separation device (not shown) that separates at least water from the organic substance-containing liquid may be provided. Examples of the separation device include a solid-liquid separation device, a distillation device, a separation membrane, and the like, and it is preferable to use the solid-liquid separation device and the distillation device in combination. Hereinafter, the separation step performed by combining the solid-liquid separation device and the distillation device will be specifically described.
However, the separation device may be omitted when it is not necessary to purify the organic substance produced by the organic substance generation unit 17 or when it is not necessary to separate water from the organic substance-containing liquid.

The organic substance-containing liquid obtained in the organic substance generating unit 17 may be separated into a solid component mainly composed of microorganisms and a liquid component containing an organic substance in a solid-liquid separator. The organic substance-containing liquid obtained in the organic substance generation unit 17 contains the target organic substance, as well as microorganisms and their carcasses contained in the fermenter as solid components, and thus removes them. Therefore, solid-liquid separation is recommended. Examples of the solid-liquid separator include a filter, a centrifuge, and an apparatus using a solution precipitation method. Further, the solid-liquid separation device may be a device (for example, a heating / drying device) that evaporates a liquid component containing an organic substance from an organic substance-containing liquid and separates the liquid component from the solid component. At this time, all of the liquid components including the target organic substance may be evaporated, or the liquid components may be partially evaporated so that the target organic substance evaporates preferentially.

The liquid component separated by solid-liquid separation may be further distilled in a distillation apparatus to further separate the target organic substance. By separation by distillation, a large amount of organic substances can be purified with high purity by a simple operation.
When distilling, a known distillation apparatus such as a distillation column may be used. In distillation, for example, the distillate contains the target organic substance (for example, ethanol) with high purity, while the canned liquid (that is, the distillation residue) contains water as the main component (for example, 70 mass by mass). % Or more, preferably 90% by mass or more). By operating in this way, the organic substance, which is the target substance, and water can be roughly separated.

The temperature inside the still during distillation of an organic substance (for example, ethanol) is not particularly limited, but is preferably 100 ° C. or lower, and more preferably about 70 to 95 ° C. By setting the temperature in the distillation apparatus to the above range, it is possible to surely separate the necessary organic substance from other components such as water.
The pressure in the distillation apparatus during distillation of the organic substance may be normal pressure, but is preferably less than atmospheric pressure, more preferably about 60 to 150 kPa (gauge pressure). By setting the pressure in the distillation apparatus within the above range, the separation efficiency of the organic substance can be improved and the yield of the organic substance can be improved.
The water separated in the separation device is preferably reused. For example, it is preferable that the water is supplied to the gas cooling tower of the post-stage treatment device 18 described later and used for water spraying in the gas cooling tower.

(Post-stage processing device)
In the post-stage processing apparatus 18, impurities contained in the synthetic gas G1 are removed, the temperature of the synthetic gas G1 is adjusted, and the like are appropriately performed. When a microbial catalyst is used as a catalyst in the organic substance generating section 17 described later, the synthetic gas G1 may be cooled to 40 ° C. or lower, preferably 38 ° C. or lower, and supplied to the organic substance generating section 17. Further, when a metal catalyst is used as a catalyst in the organic substance generating section 17 described later, the synthetic gas G1 is preferably temperature-adjusted to a temperature at which the metal catalyst can be activated and supplied to the organic substance generating section 17. For example, the temperature may be adjusted to 100 to 400 ° C., preferably about 100 to 300 ° C., and supplied to the organic substance generation unit 17.

The post-stage treatment device 18 includes a water separation device including a gas cooling tower, a filtration type dust collector, a water scrubber, a gas chiller, etc., a low temperature separation method (deep cooling method) separation device, and a fine particle separation device composed of various filters. Desulfurization device (sulfide separator), membrane separation type separator, deoxidizer, pressure swing adsorption type separator (PSA), temperature swing adsorption type separator (TSA), pressure temperature swing adsorption type separator (PTSA), a separation device using activated carbon, a deoxidizing catalyst, specifically, a processing device such as a separation device using a copper catalyst or a palladium catalyst can be mentioned. These processing devices may be used alone or in combination of two or more.

When a microbial catalyst is used as the catalyst, the post-stage treatment apparatus 18 preferably includes at least a gas cooling tower, a filtration type dust collector, and a water scrubber in this order from the front stage side.
In addition, in this specification, the "pre-stage" means the pre-stage along the supply flow of the synthetic gas G1. Further, the “second stage” means a rear stage along the supply flow of the synthetic gas G1. The supply flow of the synthetic gas G1 means a series of flows of the synthetic gas G1 until the synthetic gas G1 is generated by the gasifier 11 and the synthetic gas G1 is introduced into the organic substance generation unit 17.

The synthetic gas G1 discharged from the heat exchanger 14 may be further passed through the gas cooling tower, and the synthetic gas G1 is further cooled by passing through the gas cooling tower.
The gas cooling tower is, for example, a water spray port provided on the inner peripheral surface of the cooling tower while the synthetic gas G1 introduced from the upper side thereof and passed through the inside so as to become a downdraft passes through the inside. Cooled by more sprayed water. The synthetic gas G1 cooled by the gas cooling tower may be discharged from the lower side of the gas cooling tower.

The temperature of the synthetic gas G1 introduced into the gas cooling tower is sufficiently higher than 100 ° C., while the temperature of the water sprayed from the water spray port is lower than 100 ° C. Therefore, the synthetic gas G1 is cooled by the temperature difference thereof, and is also cooled by the heat of vaporization when the water sprayed from the water spray port is vaporized. It is preferable that a part of vaporized water is mixed as water vapor in the synthetic gas G1. The water sprayed from the water spray port may be partially or wholly vaporized at the time of spraying.

In the gas cooling tower, the synthetic gas G1 is preferably cooled in the gas cooling tower to a temperature of 100 ° C. or higher and 200 ° C. or lower, more preferably 120 ° C. or higher and 180 ° C. or lower, and further preferably 130 ° C. or higher and 170 ° C. or lower. It is preferable that the gas is cooled to a temperature and discharged to the outside of the gas cooling tower.
By cooling the synthetic gas to 200 ° C. or lower, the synthetic gas can be purified by the filtration type dust collector without damaging the filtration type dust collector described later or deteriorating the dust collection performance. Further, when the temperature is set to 100 ° C. or higher, most of the sprayed water is vaporized and mixed in the synthetic gas. Therefore, in the gas cooling tower, a large amount of sprayed water is not drained, so that it is not necessary to install a large-scale drainage facility in the gas cooling tower.

A so-called bag filter can be used as the filtration type dust collector, and solid impurities such as tar and char are removed by passing synthetic gas cooled by a gas cooling tower. By removing the solid impurities, it is possible to prevent the solid impurities from being clogged in each device in the subsequent stage of the filtration type dust collector.
In the present specification, "removal" means removing at least a part of the target substance to be removed from the synthetic gas to reduce the concentration of the target substance in the gas, and completely removes the target substance to be removed. Not limited to removal.

The synthetic gas that has passed through the filtration type dust collector should be further passed through the water scrubber. The water scrubber removes impurities contained in the synthetic gas by bringing the synthetic gas passing through the inside of the scrubber into contact with water. In the water scrubber, acid gases such as hydrogen sulfide, hydrogen chloride and blue acid, basic gases such as ammonia, and water-soluble impurities such as oxides such as NOx and SOx are removed. Further, oil impurities such as BTEX (benzene, toluene, ethylbenzene, xylene), naphthalene, 1-naphthol, 2-naphthol and the like may be appropriately removed.

The water scrubber is not particularly limited as long as it has a configuration in which the synthetic gas G1 and water are brought into contact with each other. It is preferable to have a configuration in which the inside is brought into contact with the synthetic gas G1 passing from the lower part to the upper part.
Further, the water scrubber may cool the synthetic gas G1 by bringing the synthetic gas G1 into contact with the washing water. As described above, the synthetic gas G1 is cooled by the gas cooling tower and introduced into the water scrubber in a state of being cooled to a predetermined temperature, while the temperature of the washing water in contact with the synthetic gas in the water scrubber is 100. It is less than ° C., preferably 0 ° C. or higher and 40 ° C. or lower, and more preferably 5 ° C. or higher and 30 ° C. or lower.
The synthetic gas G1 is cooled in the water scrubber to, for example, less than 100 ° C., preferably 40 ° C. or lower, and more preferably 38 ° C. or lower by contacting with water at the above temperature in the water scrubber. Further, the synthetic gas G1 is preferably cooled to a temperature of, for example, 0 ° C. or higher, preferably to a temperature of 5 ° C. or higher, by coming into contact with the washing water in the water scrubber. When the temperature of the synthetic gas G1 is 40 ° C. or lower, even if the synthetic gas G1 is supplied to the organic substance generating unit 17 at that temperature, the microbial catalyst is not killed.
Further, by passing the synthetic gas G1 through the water scrubber, the synthetic gas G1 can be washed and cooled in the water scrubber, and the water mixed in the synthetic gas G1 can be removed in the gas cooling tower.

The syngas discharged from the filter-type dust collector or water scrubber is further passed through one or more of the above-mentioned treatment devices other than the gas cooling tower, the filter-type dust collector, and the water scrubber. , Syngas may be appropriately purified and cooled.
In the above description, the configuration in which all of the gas cooling tower, the filtration type dust collector, and the water scrubber are provided in the subsequent stage of the heat exchanger 14, but some or all of them are omitted. You may. For example, even if the water scrubber is omitted, another cooling device may be provided in the subsequent stage to cool the synthetic gas G1 and supply it to the organic substance generation unit 17 at, for example, 40 ° C. or lower. Further, at least one or more of the gas cooling tower and the filtration type dust collector may be omitted, and the synthetic gas is purified and cooled only by the treatment equipment other than the gas cooling tower, the filtration type dust collector and the water scrubber. You may.

<Second embodiment>
Next, the second embodiment of the present invention will be described with reference to FIG. In the following description, the same components as those in the first embodiment are designated by the same reference numerals, and the description thereof will be omitted.
In the above first embodiment, the complete combustion gas G2 is supplied to the heating heat exchanger 16, and the heat medium heated by the complete combustion gas G2 in the heating heat exchanger 16 is supplied to the heat exchanger 14. The heat exchanger 14 was heated by the heat medium. On the other hand, in the organic substance manufacturing apparatus 25 of the second embodiment, as shown in FIG. 2, the heating heat exchanger 16 is omitted so that the complete combustion gas G2 itself can be supplied to the heat exchanger 14. good. Specifically, it is preferable to provide a complete combustion gas flow path 26 for supplying the complete combustion gas G2 to the heat exchanger 14. Then, the heat exchanger 14 is heated to a certain temperature or higher by the complete combustion gas G2 supplied to the heat exchanger 14 as in the first embodiment.

In the present embodiment, the complete combustion gas G2 passes through the gas flow path 14A inside the heat exchanger 14, thereby heating the inner surface of the gas flow path 14A of the heat exchanger 14. Then, after the heat exchanger 14 is heated to a certain temperature or higher by the complete combustion gas G2, the gas supplied to the heat exchanger 14 is transferred from the complete combustion gas G2 generated by the combustion apparatus 15 to the gasifier 11. It is preferable to switch to the generated synthetic gas G1 and allow the synthetic gas G1 to pass through the heat exchanger 14. The synthetic gas G1 that has passed through the heat exchanger 14 is supplied to the organic substance generation unit 17 as in the first embodiment.
On the other hand, the complete combustion gas G2 that has passed through the heat exchanger 14 may be appropriately treated, disposed of, or the like by the post-stage treatment device 18, and may not be supplied to the organic substance generation unit 17.

Since the complete combustion gas G2 has a low content of corrosive gas, even if the synthetic gas G1 passes through the heat exchanger 14 which is not sufficiently heated before passing through the heat exchanger 14, the heat exchanger 14 can be used. Hard to be corroded by corrosive gas. On the other hand, the synthetic gas G1 has a high content of corrosive gas, but since the synthetic gas G1 passes through the heat exchanger 14 after heating, the corrosive gas is less likely to be liquefied in the heat exchanger 14. Therefore, also in this embodiment, the corrosive gas contained in the synthetic gas G1 can appropriately prevent the heat exchanger 14 from being corroded.

In the above description of the second embodiment, the mode in which the heating heat exchanger 16 is omitted has been described, but the heating heat exchanger 16 may not be omitted. If the heating heat exchanger 16 is not omitted, even after the heat exchanger 14 is heated to a certain temperature or higher by the complete combustion gas G2, the combustion apparatus 15 is continuously operated and the complete combustion generated by the combustion apparatus 15 is performed. The gas G2 may be supplied to the heating heat exchanger 16. In the heat exchanger 16 for heating, the heat medium may be heated by the complete combustion gas G2, and the heated heat medium may be supplied to another device to be used for power generation or the like.

Further, in the first and second embodiments described above, the heat medium M2 or the complete combustion gas G2 supplied to the heat exchanger 14 is passed through the gas flow path 14A of the heat exchanger 14 to pass through the heat exchanger 14. 14 may be heated, but any configuration may be adopted as long as the heat exchanger 14 is heated by the heat energy of the complete combustion gas G2 before the synthetic gas is passed through the heat exchanger 14. For example, the heat exchanger 14 may be heated by passing the heat medium M2 or the complete combustion gas G2 through the cooling medium flow path 14B of the heat exchanger 14. Further, the heating before passing the synthetic gas through the heat exchanger 14 may be performed by a method other than the heat energy of the complete combustion gas G2.

Further, in the organic substance production devices 10 and 25 of the first and second embodiments described above, the gasification device 11 and the combustion device 15 show an embodiment having the gasification furnaces 12 and 19, respectively. It is not necessary to have a gasification furnace, and the gasification furnace of the gasification device 11 and the combustion device 15 may be shared.
That is, before passing the synthetic gas G1 through the heat exchanger 14, first, the thermal decomposition gas generated in the gasification furnace is supplied to the combustion furnace 20, and the complete combustion gas G2 is generated in the combustion furnace 20, and the complete combustion gas G2 is generated. The combustion gas G2 may be supplied to the heating heat exchanger 16 or the heat exchanger 14. Then, after the heat exchanger 14 is heated to a certain temperature or higher by the heat energy of the complete combustion gas G2, the thermal decomposition gas generated in the gasification furnace is supplied to the reforming furnace 13 and synthesized in the reforming furnace 13. It is preferable to generate the gas G1 and supply the synthetic gas G1 to the heat exchanger 14.

<Third embodiment>
Next, a third embodiment of the present invention will be described with reference to FIG. In the above first and second embodiments, the gasification device 11 and the combustion device 15 are provided, but in the third embodiment, the combustion device 15 is omitted. Further, the heat exchanger 16 for heating is also omitted. Hereinafter, the differences between the present embodiment and the first embodiment will be described.

In the present embodiment, both the complete combustion gas G2 for heating the heat exchanger 14 and the synthetic gas G1 for being supplied to the organic substance generation unit 17 are generated by the gasifier 11.
That is, in the present embodiment, first, pyrolysis gas is generated from the waste in the gasification furnace 12, the pyrolysis gas is supplied to the reforming furnace 13, and the complete combustion gas G2 is generated in the reforming furnace 13. NS. Here, in the reforming furnace 13, the supplied pyrolysis gas may be completely burned by a known method. Specifically, it is preferable to completely burn the gas by increasing the amount of oxygen supplied per unit time as compared with the time when the synthetic gas G1 described later is generated. Then, the obtained complete combustion gas G2 may be supplied to the heat exchanger 14, and the heat exchanger 14 may be heated by the complete combustion gas G2. The complete combustion gas G2 may pass through the gas flow path 14A inside the heat exchanger 14 to heat the heat exchanger 14. The complete combustion gas G2 that has passed through the heat exchanger 14 may be appropriately treated, disposed of, or the like by the post-stage treatment device 18.

When the temperature of the heat exchanger 14 becomes a certain temperature or higher due to the heating by the complete combustion gas G2 described above, the synthetic gas G1 is then generated from the thermal decomposition gas in the reforming furnace 13. Then, the generated synthetic gas G1 is continuously supplied to the heat exchanger 14. In the heat exchanger 14, the synthetic gas G1 is cooled by the cooling medium M1 supplied to the heat exchanger 14, and then supplied to the organic substance generation unit 17 to generate an organic substance.

As described above, also in the present embodiment, by heating the heat exchanger 14 in advance before passing through the synthetic gas G1, the corrosive gas becomes a liquid substance even when the passage of the synthetic gas G1 is started. This is suppressed so that the heat exchanger 14 can be adequately prevented from being corroded by the corrosive gas.
Further, in the present embodiment, since the combustion device 15 is omitted and both the synthetic gas G1 and the complete combustion gas G2 are generated in the gasification device 11, the configuration of the organic substance production device 30 can be simplified. Further, since both the synthetic gas G1 and the complete combustion gas G2 pass through the gas flow path 14A of the heat exchanger 14, it is not necessary to switch the flow path for supplying the gas to the heat exchanger 14. This also simplifies the configuration of the organic substance manufacturing apparatus 30.

However, also in the third embodiment, the complete combustion gas G2 may heat the heat exchanger 14 by passing through the cooling medium flow path 14B instead of passing through the gas flow path 14A of the heat exchanger 14. ..
Further, also in the third embodiment, as shown in the first embodiment, the heating heat exchanger 16 is provided, and the complete combustion gas G2 is passed through the heating heat exchanger 16 to heat the heat medium M2. , The heat exchanger 14 may be heated by the heat medium M2. The heat medium M2 may pass through the gas flow path 14A to heat the heat exchanger 14, or may pass through the cooling medium flow path 14B to heat the heat exchanger 14.

10, 25, 30 Organic material production equipment 11 Gasifier 12 Gasifier 13 Reformer 14 Heat exchanger 14A Gas flow path 14B Cooling medium flow path 15 Combustion device 16 Heating heat exchanger 16A Complete combustion gas flow path 16B Heat medium flow path 17 Organic substance generator 18 Post-stage processing device 19 Gasification furnace 20 Combustion furnace 21 Heat medium supply flow path 26 Complete combustion gas flow path G1 Synthetic gas G2 Complete combustion gas M1 Cooling medium M2 Heat medium

Claims (16)

The process of gasifying waste to generate syngas in a gasifier,
A step of cooling the synthetic gas discharged from the gasifier by passing it through a heat exchanger.
At least the step of bringing the synthetic gas that has passed through the heat exchanger into contact with the catalyst to generate an organic substance, and
A method for producing an organic substance, which comprises a step of heating the heat exchanger before passing the synthetic gas through the heat exchanger. Further equipped with a process to completely burn waste and generate complete combustion gas,
The method for producing an organic substance according to claim 1, wherein the heat exchanger is heated by the heat energy of the complete combustion gas before the synthetic gas is passed through the heat exchanger. The heat exchanger includes a gas flow path through which the synthetic gas is passed and a cooling medium flow path through which a cooling medium for cooling the synthetic gas is passed.
The method for producing an organic substance according to claim 2, wherein the heat exchanger is heated by passing the complete combustion gas through either the gas flow path or the cooling medium flow path. The heat exchanger includes a gas flow path through which a synthetic gas is passed and a cooling medium flow path through which a cooling medium for cooling the synthetic gas is passed.
In the heat exchanger for heating, the heat medium is heated by the heat energy of the complete combustion gas, and the heat medium is heated.
The method for producing an organic substance according to claim 2, wherein the heat exchanger is heated by passing the heated heat medium through either the gas flow path or the cooling medium flow path. The method for producing an organic substance according to any one of claims 2 to 4, wherein the waste is completely burned by a combustion device to generate the complete combustion gas. The method for producing an organic substance according to any one of claims 1 to 5, wherein the heat exchanger is heated to 200 ° C. or higher before the synthetic gas is passed through the heat exchanger. The method for producing an organic substance according to any one of claims 1 to 6, wherein the catalyst is a microbial catalyst. The method for producing an organic substance according to any one of claims 1 to 7, wherein the organic substance contains ethanol. A gasifier that gasifies waste to generate syngas,
A heat exchanger that allows synthetic gas discharged from the gasifier to pass through and cools it.
It is provided with an organic substance generating unit that produces an organic substance by contacting a synthetic gas that has passed at least the heat exchanger with a catalyst.
An organic substance manufacturing apparatus capable of heating the heat exchanger before passing the syngas through the heat exchanger. The organic substance manufacturing apparatus according to claim 9, wherein the heat exchanger can be heated by the thermal energy of the complete combustion gas obtained by completely burning the waste. The heat exchanger includes a gas flow path through which a synthetic gas is passed and a cooling medium flow path through which a cooling medium for cooling the synthetic gas is passed.
The organic substance manufacturing apparatus according to claim 10, wherein the heat exchanger is heated by passing the complete combustion gas obtained by completely burning the waste through either the gas flow path or the cooling medium flow path. The heat exchanger includes a gas flow path through which a synthetic gas is passed and a cooling medium flow path through which a cooling medium for cooling the synthetic gas is passed.
The organic substance manufacturing apparatus further includes a heat exchanger for heating that heats a heat medium with the thermal energy of the complete combustion gas.
The organic substance manufacturing apparatus according to claim 10, wherein the heat exchanger is heated by passing the heated heat medium through either the gas flow path or the cooling medium flow path. The organic substance manufacturing apparatus according to any one of claims 10 to 12, further comprising a combustion apparatus that completely burns the waste to generate the complete combustion gas. The organic substance production apparatus according to any one of claims 9 to 13, wherein the heat exchanger can be heated to 200 ° C. or higher before the synthetic gas is passed through the heat exchanger. The organic substance manufacturing apparatus according to any one of claims 9 to 14, wherein the catalyst is a microbial catalyst. The organic substance manufacturing apparatus according to any one of claims 9 to 15, wherein the organic substance contains ethanol.

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