JP2003171675A - Liquid fuel synthesis system - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a liquid fuel synthesis system which enables the production of a liquid fuel with high efficiency by using a waste product, a solid fuel and the like as the raw material. <P>SOLUTION: The liquid fuel synthesis system has a gasification chamber 1 for gasifying a material to be treated with a high temperature fluid medium c1 to generate a product gas b having hydrogen and carbon monoxide as the major components, a char combustion chamber 2 for combusting a char to be generated with the gasification in the gasification chamber 1 to heat a fluid medium c2, and a synthesis apparatus 200 for synthesizing a liquid fuel with the use of the product gas b generated in the gasification chamber 1 and is constituted by separating the gasification chamber 1 from the char combustion chamber 2 so as not to allow a gas to flow in the upper part of a fluidized bed, forming a communicating opening at the lower part of a partition wall 15 to communicate the gasification chamber 1 to the char combustion chamber 2, and moving the heated fluid medium 2c from the side of the char combustion chamber 2 to the gasification chamber 1 through this opening. <P>COPYRIGHT: (C)2003,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a liquid fuel synthesizing system, and more particularly to a liquid fuel synthesizing system suitable for synthesizing liquid fuels such as methanol and dimethyl ether from various wastes and solid fuels as raw materials. It is a thing.

[0002]

2. Description of the Related Art In recent years, liquid fuel synthesis technology using organic waste as a raw material has been expected to be put into practical use due to environmental problems, resource depletion, and demand for fossil fuel reduction. Conventionally, for liquid fuel synthesis using waste as a raw material, a process of directly converting to oil and once gasifying the waste to obtain a produced gas (synthesis gas) mainly containing hydrogen, carbon monoxide, etc., There is a process of synthesizing liquid fuel using this as a raw material. Here, in the case of a process by gasification, the waste material as a raw material is partially combusted with air to cover the amount of heat required for gasification. In such a gasification process, a product gas is once passed through and then purified to obtain a liquid fuel, so that a high-purity, high-quality liquid fuel can be obtained.

[0003]

However, in the case of the conventional liquid fuel synthesis by gasification as described above, the combustion gas mainly composed of carbon dioxide is mixed in the produced gas, and the calorific value of the gas is lowered. Therefore, there is a problem that it is not necessarily suitable as a raw material for liquid fuel synthesis. Further, since air is used for partial combustion, there is a problem that the concentration of inert gas such as nitrogen and argon is increased and the yield of liquid fuel is decreased.

Therefore, an object of the present invention is to provide a liquid fuel synthesizing system which makes it possible to produce liquid fuel with high efficiency using waste, solid fuel or the like as a raw material.

[0005]

In order to achieve the above object, a liquid fuel synthesizing system according to a first aspect of the present invention has a high-temperature fluidized medium c as shown in FIGS. 1 and 2, for example.
1 is fluidized inside to form a gasification chamber fluidized bed having a first interface, and the product gas containing hydrogen and carbon monoxide as main components by gasifying the object a to be treated in the gasification chamber fluidized bed. a gasification chamber 1 for generating b; a high temperature fluidized medium c2 is internally fluidized to form a char combustion chamber fluidized bed having a second interface, and char h generated by gasification in the gasification chamber 1 A char combustion chamber 2 that heats the fluidized medium c2 by burning the gas in the fluidized bed of the char combustion chamber; and a synthesis device 200 that synthesizes liquid fuel using the generated gas b generated in the gasification chamber 1; gasification The chamber 1 and the char combustion chamber 2 are partitioned by a first partition wall 15 so that there is no gas flow in the vertical direction above the interface of the respective fluidized beds, and the lower part of the first partition wall 15 is A communication port 25 that connects the gasification chamber 1 and the char combustion chamber 2 Te, the height of the upper end of the continuous opening 25 is the first interface and the second interface or less is communicating port 2
5 is formed, and the fluidized medium c2 heated in the char combustion chamber 2 is moved from the char combustion chamber 2 side to the gasification chamber 1 side through the communication port 25.

Here, the object to be treated is, for example, waste or solid fuel. The liquid fuel to be synthesized is, for example, an oxygen-containing fuel such as methanol or dimethyl ether, or a hydrocarbon fuel such as gasoline, kerosene, or light oil.

According to this structure, since the gasification chamber for flowing the high-temperature fluid medium therein is provided, the object to be treated can be gasified to generate the produced gas b containing hydrogen and carbon monoxide as main components. It is possible to heat the fluidized medium because it has a char combustion chamber in which a high-temperature fluidized medium is made to flow and burns the char, and it is possible to synthesize liquid fuel because it is equipped with a synthesizer that uses generated gas that is generated. Since the first partition wall is provided, the gasification chamber and the char combustion chamber can be partitioned so that there is no gas flow vertically above the interface of the respective fluidized beds, and the lower part of the first partition wall is Since the communication port that connects the gasification chamber and the char combustion chamber is formed, the fluidized medium heated in the char combustion chamber can be moved from the char combustion chamber side to the gasification chamber side through the communication port. .

According to this structure, typically, the product gas generated in the gasification chamber and the combustion gas generated in the char combustion chamber due to the combustion of char generated by the gasification in the gasification chamber do not mix with each other. Therefore, a product gas suitable for high-calorie liquid fuel synthesis can be obtained.

Further, as described in claim 2, in the liquid fuel synthesizing system according to claim 1, the gasification chamber 1 is configured to supply a fluidizing gas g1 for fluidizing the fluidized bed, The fluidizing gas g1 is mainly composed of one gas selected from the group consisting of steam, hydrogen gas, hydrocarbon gas, carbon dioxide gas and product gas b, or a mixture of two or more gases selected from the group. You may do it.

With this structure, it is possible to prevent air from being used as the fluidizing gas, and the fluidizing gas can be a gas that does not substantially contain nitrogen gas and oxygen gas.

As described in claim 3, in the liquid fuel synthesizing system according to claim 2, steam is mainly used as the fluidizing gas g1, and the steam includes hydrogen gas, hydrocarbon gas, and carbon dioxide gas. One or more of the above gases may be mixed and used, and an adjusting device for adjusting the addition amount of the one or more gases to the water vapor may be provided.

Since the adjusting device is provided, the components of the fluidizing gas g1 in the gasification chamber 1 can be adjusted, that is, the components of the fluidizing gas g1 in the gasification chamber 1 can be adjusted by adjusting the amount of gas added. It can be adjusted and the molar ratio of hydrogen gas and carbon monoxide gas in the produced gas b can be maintained at a predetermined value.

Further, as described in claim 4, in the liquid fuel synthesizing system according to claim 3, the adjusting device has a molar ratio of hydrogen gas and carbon monoxide gas in the produced gas b of 2 to 2.
You may set so that it may be adjusted so that it may become 5.

According to this structure, the molar ratio of the hydrogen gas and the carbon monoxide gas is adjusted to be 2 to 5, so that it is suitable for synthesizing methanol as the liquid fuel.

Further, as described in claim 5, in the liquid fuel synthesizing system according to claim 3, the adjusting device has a molar ratio of hydrogen gas and carbon monoxide gas in the produced gas b of 0.
You may set so that it may adjust so that it may become 7-2.

According to this structure, the molar ratio of hydrogen gas to carbon monoxide gas is adjusted to be 0.7 to 2, so that it is suitable for synthesizing dimethyl ether as a liquid fuel.

Further, as described in claim 6, in the liquid fuel synthesis system according to any one of claims 2 to 5, at least one gas selected from hydrogen gas, hydrocarbon gas and carbon dioxide gas is used. The excess gas may be generated and used as the fluidizing gas g1 of the gasification chamber 1.

Further, as described in claim 7, in the liquid fuel synthesizing system according to any one of claims 1 to 6 (see, for example, FIG. 2), it is provided in contact with the char combustion chamber 2. A heat recovery chamber 3 is provided; between the char combustion chamber 2 and the heat recovery chamber 3, a second partition wall 12 for partitioning a fluidized bed portion of the char combustion chamber fluidized bed is provided, and a lower part of the second partition wall 12 is provided. An opening 22 is formed in the flow path, and the fluidized medium in the char combustion chamber 2 flows into the heat recovery chamber 3 from the upper part of the second partition wall 12 and forms a circulation flow that returns to the char combustion chamber 2 through the opening 22. It may be configured as follows.

Since the heat recovery chamber is provided, part of the heat generated by the combustion of char can be recovered as, for example, steam. Further, it is possible to balance the heat between the gasification chamber and the char combustion chamber.

Further, for example, as shown in FIG. 4, the above liquid fuel synthesis system has a waste heat boiler 111 for recovering heat from the combustion gas e generated in the char combustion chamber 2 of the integrated gasification furnace 101. A part of or all of the steam 322, 325 generated in the heat recovery chamber 3 of the waste heat boiler 111 and / or the integrated gasification furnace 101 is a liquid fuel using the generated gas b from the integrated gasification furnace 101 as a raw material. It may be configured to be used as a part or all of the heat source in the synthesis step 200.

A waste heat boiler 11 for recovering heat from the combustion gas e from the char combustion chamber 2 of the integrated gasification furnace 101.
1 and uses a part or all of the steam generated in the waste heat boiler 111 and / or the heat recovery chamber 3 of the integrated gasification furnace 101 to generate electricity by the steam turbine 113 and integrate the obtained electric power. The generated gas b from the type gasification furnace 101 may be used as a part or all of the electric power required for the liquid fuel synthesizing apparatus 200 using the raw material.

A waste heat boiler 11 for recovering heat from the combustion gas e from the char combustion chamber 2 of the integrated gasification furnace 101.
1, and the steam 322 generated in the heat recovery chamber 3 of the waste heat boiler 111 and / or the integrated gasification furnace 101,
Electric power is generated by the steam turbine 113 using part or all of 325, and the obtained electric power is used as the integrated gasification furnace 101.
Liquid fuel synthesizing apparatus 200 using gas b generated from
The extracted steam 327 from the steam turbine 113 may be used as a part or all of the electric power required for the liquid fuel synthesizing apparatus 200.

Further, as described in claim 8, in the liquid fuel synthesizing system according to any one of claims 3 to 7 (see, for example, FIG. 5), the gasification chamber 1 and the synthesizing device 40 are provided.
A gas cleaning device 103 for cleaning the generated gas b between 0 and 0.
May be provided.

With this structure, the gas cleaning device 10
3 is provided, the generated gas b that has left the gasification chamber 1 is cleaned by the gas cleaning device 103, and the generated gas b is harmful to the liquid fuel synthesis reaction (for example, acidic gas such as hydrogen chloride or hydrogen sulfide) and dust. The minute f and the like can be removed.

According to a ninth aspect of the present invention, there is provided a liquid fuel synthesizing system according to the eighth aspect (see, for example, FIG. 5).
The adjusting device 115 introduces the high temperature cleaning liquid 116 after cleaning the generated gas b from the cleaning device 103, and the high temperature cleaning liquid 11
The liquid fuel synthesis system may be configured to humidify the at least one gas by using 6 as a heat source.

According to this structure, since the adjusting device 115 is provided, the high temperature cleaning liquid 11 after cleaning the generated gas b is prepared.
6 can be introduced from the cleaning device 103, and the high temperature cleaning liquid 116 can be used as a heat source to humidify at least one gas selected from hydrogen, hydrocarbon and carbon dioxide. Therefore, one or more humidified gases can be added to steam and the steam can be supplied to the gasification chamber 1 as the fluidizing gas g1, and the sensible heat of the gasification raw material can be used without waste. it can. For example, the purge gas 507a containing hydrogen gas, hydrocarbon gas, and carbon dioxide gas from the synthesis device 400 is introduced into the adjustment device 115, and the cleaning device 103 is introduced.
The purge gas 507a may be humidified by bringing it into contact with the high temperature cleaning liquid 116 from FIG. It is possible to mix the humidified purge gas 507a with steam and supply the steam to the gasification chamber 1 as the fluidizing gas g1. By using the cleaning liquid 116 that has been heated to a high temperature by cleaning the high-temperature generated gas b as a humidification source of the purge gas 507a,
The sensible heat of the gasification raw material can be used without wasting it. Purge gas 507a introduced into adjusting device 115
The amount by adjusting the hydrogen gas added to the water vapor, hydrocarbon gas, it is possible to adjust the amount of carbon dioxide gas, the product gas b near the H _{2 /} CO molar ratio which is suitable for synthesizing device 400 It is possible to make the fluidizing gas g1 suitable for obtaining.

[0027]

BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the present invention will be described below with reference to the drawings. In each drawing, the same or corresponding members are designated by the same reference numerals, and duplicate description will be omitted. FIG. 1 is a flow chart of a methanol synthesis system as a liquid fuel synthesis system according to a first embodiment of the present invention. This is a basic embodiment of the present invention, which is a fluidized bed type integrated gasification furnace 101 for gasifying waste or solid fuel, and a synthesis apparatus utilizing the generated gas b generated in the gasification furnace 101. The system is configured to include the methanol synthesis apparatus 200 as described above. Although a methanol synthesis system will be described here as an example of the liquid fuel synthesis system, a similar system can be used for the synthesis of other liquid fuels such as gasoline and dimethyl ether described later.

The methanol synthesis system according to the present embodiment comprises an integrated gasification furnace 101 for generating a product gas (hereinafter also referred to as "synthesis gas" as appropriate), a gas cleaning device 103 for cleaning the product gas, and a cleaned gas. The CO converter 104 for CO conversion, the desulfurizer 105 for removing sulfur from the CO converted gas, and the decarbonator 106 for separating carbon dioxide gas from the desulfurized gas are provided along the flow path of the produced gas b. It is installed in this order. Further decarbonator 1
On the downstream side of 06, a gas compressor 107 that compresses the decarbonated gas 301a and a methanol synthesis device 200 that synthesizes methanol using the compressed gas 301b are installed. As described below, the gas cleaning device 10
3, the desulfurization device 105, and the CO conversion device 104 may be installed in this order.

A centrifugal compressor is used as the gas compressor 107 and is driven by an electric motor 108. However, when the gas flow rate handled is relatively small, a reciprocating compressor may be used instead of the centrifugal compressor. As the drive device of the compressor 107, other types of drive devices, in particular, steam turbines may be used instead of the electric motor.

The integrated gasification furnace 101 is provided with a classification device 102 for classifying the fluidized medium c3 and the incombustible substance d extracted from the gasification chamber 1. After the classification, the fluidized medium c3 is returned to the gasification chamber 1, and the incombustible material d is taken out to the outside. The integrated gasification furnace 101 will be described in detail later with reference to FIG. 2 and the methanol synthesizer with reference to FIG.

Continuing to refer to FIG. 1, the operation of this device will be explained.
Reveal Methanol synthesis is based on fossil fuels such as natural gas and coal.
Hydrogen gas obtained by steam reforming or partial combustion reforming
Su H _TwoAnd a synthesis gas containing carbon monoxide gas CO as a main component
Is generally used as a raw material. Therefore,
Even if waste is used as a raw material, if fossil fuel is used as a raw material,
If it is possible to obtain syngas with properties similar to those of
Methanol synthesis can be carried out.

In the figure, the combustible product gas (synthesis gas) generated in the integrated gasification furnace 101 usually contains a dust component f in addition to the gas component b. This gas is first cleaned in the gas cleaning device 103 to remove chlorine content and dust content f. Unlike the case where natural gas is used as a raw material, this device is required particularly when a waste material is used as it contains chlorine and dust.

Next, in the CO conversion device 104, a CO shift reaction represented by the following formula is performed using a catalyst to adjust the H ₂ / CO ratio in the synthesis gas. In the case of CO + H ₂ O ← → H ₂ + CO ₂ methanol synthesis, it is desirable that the H ₂ / CO ratio (molar ratio (the same applies below)) is stoichiometrically 2 or more. Therefore, this step is not necessary if the H2 / CO ratio is above ₂ in the initial syngas stage.

Further, in the next desulfurization apparatus 105, H ₂
The S gas is removed. Here, the sulfur content is removed to 0.1 ppm or less. Next, excess CO ₂ gas 302 is removed in the carbon dioxide removal device 106. Integrated gasifier 10
When the H ₂ / CO ratio of the first syngas generated from 1 is 2 or less, the H ₂ / CO ratio obtained by the CO conversion step in the CO converter is
_When adjusting the ₂ / CO ratio, CO ₂ is generated by the reaction, and it is necessary to remove this in the decarbonation process in the decarbonation device 106. CO removed
_{The 2} gas 302 may be released to the atmosphere, but may be fixed in the form of liquefied carbon dioxide or dry ice and reused.

The synthesis gas 301a from which the excess components have been removed in the above steps is compressed to a pressure required for methanol synthesis in the compression step by the gas compressor 107, and is supplied to the methanol synthesis system 200 as the compressed gas 301b. It The compression process by the gas compressor 107 is
It may be performed before the CO conversion step in the CO conversion apparatus 104, the desulfurization step in the desulfurization apparatus 105, and the decarbonation step in the decarbonation apparatus 106. This gives C
The O conversion step, the desulfurization step and the decarbonation step can be performed under pressure, and the reactivity can be improved.

The integrated gasification furnace 101 will now be described with reference to the conceptual sectional view of FIG. This integrated gasification furnace 101 has three types of thermal decomposition, that is, gasification, char combustion, and heat recovery.
The furnace is provided with a gasification chamber 1, a char combustion chamber 2, and a heat recovery chamber 3, which are respectively in charge of one of the two functions, and is housed, for example, in a furnace body having a cylindrical or rectangular shape as a whole. The gasification chamber 1, the char combustion chamber 2, and the heat recovery chamber 3 are divided into partition walls 11, 12, 13, 14,
It is divided by 15, and a fluidized bed which is a dense layer containing a fluidized medium is formed at the bottom of each. In order to fluidize the fluidized bed of each chamber, that is, the gasification chamber fluidized bed, the char combustion chamber fluidized bed, and the heat recovery chamber fluidized bed, the furnace bottom, which is the bottom of each chamber 1, 2, and 3, is fluidized. An air diffuser for injecting fluidizing gas into the medium is provided. The air diffuser is configured to include, for example, a perforated plate laid on the bottom of the furnace, and the perforated plate is divided into a plurality of chambers in the width direction to change the superficial velocity of each part in each chamber. In addition, the flow velocity of the fluidizing gas blown out from each room of the air diffuser through the perforated plate is changed. Since the superficial velocity is relatively different in each part of the chamber, the fluidized medium in each chamber also has a different flow state in each part of the chamber, so that an internal swirl flow is formed. The internal swirl flow circulates in each chamber in the furnace because the flow state is different in each part of the chamber. In the figure, the size of the hatched arrow shown in the air diffuser indicates the flow velocity of the fluidizing gas blown out. For example, the thick arrow at the location indicated by 2b has a higher flow velocity than the thin arrow at the location indicated by 2a.

The gasification chamber 1 and the char combustion chamber 2 are partitioned by a partition wall 11 and a partition wall 15, and the char combustion chamber 2 and the heat recovery chamber 3 are partitioned by a partition wall 12 so that the gasification chamber 1 and The space between the heat recovery chambers 3 is partitioned by a partition wall 13 (this drawing shows the furnace in a plan view, so the partition wall 1
1 is shown as if it is not between the gasification chamber 1 and the char combustion chamber 2 and the partition wall 13 is not as between the gasification chamber 1 and the heat recovery chamber 3). That is, in the integrated gasification furnace 101, each chamber is not configured as a separate furnace but is integrally configured as one furnace. Further, a settling char combustion chamber 4 is provided near the surface of the char combustion chamber 2 in contact with the gasification chamber 1 so that the fluidized medium descends. That is, the char combustion chamber 2 is divided into a settling char combustion chamber 4 and a char combustion chamber main body other than the settling char combustion chamber 4. Therefore, a partition wall 14 is provided for partitioning the settled char combustion chamber 4 from the other part of the char combustion chamber 2 (char combustion chamber main body). The settling char combustion chamber 4 and the gasification chamber 1 are separated by the partition wall 1.
It is divided by 5.

Here, the fluidized bed and the interface will be described.
The fluidized bed consists of a concentrated layer in the vertically lower part, which contains a fluidized medium (for example, silica sand) in a fluidized state by the fluidizing gas, and a fluidized medium in the vertically upper part of the concentrated layer. It consists of a splash zone where a large amount of gas coexists and the fluid medium is vigorously splashing. Above the fluidized bed, that is, above the splash zone, there is a freeboard section containing almost no fluidized medium and mainly gas.
The interface refers to the splash zone having a certain thickness, but may also be regarded as a virtual surface intermediate between the upper surface and the lower surface of the splash zone (the upper surface of the rich layer).

Further, "partitioned by a partition wall so that gas does not flow above the interface of the fluidized bed in the vertical direction."
In that case, it is preferable that the gas does not flow above the upper surface of the dense layer below the interface.

The partition wall 11 between the gasification chamber 1 and the char combustion chamber 2 is almost entirely partitioned from the furnace ceiling 19 to the furnace bottom (perforated plate of the air diffuser), but the lower end is the furnace. There is a second opening 21 near the bottom of the furnace without contacting the bottom.
However, the upper end of the opening 21 does not reach above the interface between the fluidized bed interface of the gasification chamber and the fluidized bed interface of the char combustion chamber. More preferably, the upper end of the opening 21 does not reach above the upper surface of the rich layer of the gasification chamber fluidized bed or the upper surface of the rich layer of the char combustion chamber fluidized bed. In other words, it is preferable that the opening 21 is always formed so as to be submerged in the dense layer. That is, the gasification chamber 1 and the char combustion chamber 2 are separated from each other by a partition wall so that there is no gas flow at least in the freeboard portion, that is, above the interface, and more preferably above the upper surface of the rich layer. It will be partitioned.

The partition wall 12 between the char combustion chamber 2 and the heat recovery chamber 3 has its upper end near the interface, that is, above the upper surface of the rich layer, but below the upper surface of the splash zone. The lower end of the partition wall 12 is up to the vicinity of the furnace bottom, and like the partition wall 11, the lower end does not contact the furnace bottom, and there is an opening 22 near the furnace bottom that does not reach above the upper surface of the rich layer. In other words, only the fluidized bed portion between the char combustion chamber 2 and the heat recovery chamber 3 is partitioned by the partition wall 12, and the partition wall 12 has an opening 22 near the hearth surface. The fluidized medium of No. 2 flows into the heat recovery chamber 2 from the upper portion of the partition wall 12 and is returned to the char combustion chamber 2 again through the opening 22 near the hearth surface of the partition wall 12.

Partition wall 13 between gasification chamber 1 and heat recovery chamber 3
Is completely partitioned from the furnace bottom to the furnace ceiling. The partition wall 14 for partitioning the inside of the char combustion chamber 2 to provide the sedimentation char combustion chamber 4 has an upper end near the interface of the fluidized bed and a lower end in contact with the furnace bottom. The relationship between the upper end of the partition wall 14 and the fluidized bed is
This is the same as the relationship between the partition wall 12 and the fluidized bed. The partition wall 15 for partitioning the settling char combustion chamber 4 and the gasification chamber 1 is the partition wall 1
Similar to No. 1, it is partitioned almost entirely from the furnace ceiling to the furnace bottom, the lower end does not contact the furnace bottom, there is a first opening 25 near the furnace bottom, and the upper end of this opening Is below the top surface of the dense layer. That is, the relationship between the first opening 25 and the fluidized bed is the same as the relationship between the opening 21 and the fluidized bed.

The waste or solid fuel a put into the gasification chamber 1 receives heat from the fluidized medium c1 and is thermally decomposed and gasified. Typically, the waste or fuel a does not burn in the gasification chamber 1 and is so-called carbonization. Remaining dry char h
Is the opening 2 at the bottom of the partition wall 11 together with the fluid medium c1.
From 1 to the char combustion chamber 2. In this way, the char h introduced from the gasification chamber 1 burns in the char combustion chamber 2 to heat the fluidized medium c2. The fluidized medium c2 heated by the combustion heat of the char h in the char combustion chamber 2 is the partition wall 1
2 passes over the upper end of 2 and flows into the heat recovery chamber 3, and is arranged in the heat recovery chamber 3 so as to be below the interface in the layer heat transfer tube 41.
After the heat is collected by and is cooled, it again flows into the char combustion chamber 2 through the lower opening 22 of the partition wall 12.

Here, the heat recovery chamber 3 is not essential in the gas supply device according to the embodiment of the present invention. That is, if the amount of char h mainly consisting of carbon remaining after gasification of the volatile components in the gasification chamber 1 and the amount of char required to heat the fluidized medium c2 in the char combustion chamber 2 are substantially equal to each other. The heat recovery chamber 3 that removes heat from the fluid medium is unnecessary. If the difference in the amount of the char is small, for example, the gasification temperature in the gasification chamber 1 becomes high, and the amount of CO gas generated due to the gasification of carbon in the char in the gasification chamber 1 is increased. The heat balance is automatically maintained by increasing the number.

However, as shown in FIG. 2, the heat recovery chamber 3
When equipped with, it is possible to deal with a wide variety of wastes or fuels, from coal that generates a large amount of char to municipal waste that hardly generates char. That is,
Regardless of what kind of waste or fuel, by adjusting the heat recovery amount in the heat recovery chamber 3, the char combustion chamber 2
The temperature of the fluidized medium can be maintained appropriately by appropriately adjusting the combustion temperature of the.

On the other hand, the fluidized medium c2 heated in the char combustion chamber 2 flows into the settling char combustion chamber 4 over the upper end of the partition wall 14, and then into the gasification chamber 1 through the opening 25 at the bottom of the partition wall 15. Inflow.

Here, the flow state and movement of the flowing medium between the chambers will be described. In the vicinity of the surface in contact with the partition wall 15 between the sedimentation char combustion chamber 4 and the inside of the gasification chamber 1, a strong fluidization region 1b in which a stronger fluidization state is maintained as compared with the fluidization of the sedimentation char combustion chamber 4. It has become. As a whole, it is preferable to change the superficial velocity of the fluidizing gas depending on the location so that the mixed diffusion of the injected fuel and the fluidized medium is promoted. As an example, as shown in FIG. In addition to this, a weak fluidization region 1a is provided so that a swirling flow is formed.

The char combustion chamber 2 has a weak fluidization region 2 at the center.
a, it has a strong fluidization region 2b in the peripheral portion, and the fluidizing medium and the char form an internal swirling flow. It is preferable that the fluidization rate in the strong fluidization zone in the gasification chamber 1 and the char combustion chamber 2 is 5 Umf or more and the fluidization rate in the weak fluidization zone is 5 Umf or less, but the weak fluidization zone and the strong fluidization If there is a clear relative difference in the chemical range, there is no problem in exceeding this range. Heat recovery chamber 3 in char combustion chamber 2 and settling char combustion chamber 4
It is preferable to dispose the strong fluidization region 2b in the portion in contact with. If necessary, it is preferable to provide a gradient on the bottom of the furnace so that it goes down from the weak fluidization zone side to the strong fluidization zone side (not shown). Here, Umf is a unit in which the minimum fluidization speed (speed at which fluidization is started) is 1 Umf. That is, 5 Umf is 5 times the minimum fluidization rate.

In this way, the char combustion chamber 2 and the heat recovery chamber 3
By keeping the fluidized state on the side of the char combustion chamber near the partition wall 12 relatively stronger than the fluidized state on the side of the heat recovery chamber 3, the fluidized medium is the interface of the fluidized bed of the partition wall 12. The fluid medium flowing from the side of the char combustion chamber 2 to the side of the heat recovery chamber 3 over the upper end in the vicinity, and the inflowing fluid medium moves downward due to a relatively weak fluidized state in the heat recovery chamber 3, that is, a high-density state. It moves to the char combustion chamber 2 side from the heat recovery chamber 3 side through the lower end (opening 22) of the partition wall 12 near the furnace bottom.

Similarly, the fluidized state on the side of the char combustion chamber body near the partition wall 14 between the body of the char combustion chamber 2 and the settled char combustion chamber 4 is more relative to that on the side of the sedimented char combustion chamber 4 than the fluidized state. By maintaining an extremely strong fluidized state, the fluidized medium moves and flows from the side of the main body of the char combustion chamber 2 to the side of the settled char combustion chamber 4 over the upper end near the interface of the fluidized bed of the partition wall 14. The fluidized medium flowing into the settling char combustion chamber 4 moves downward (toward the furnace bottom) due to the relatively weak fluidized state in the settling char combustion chamber 4, that is, the high density state, and the furnace of the partition wall 15 is moved. It moves from the settling char combustion chamber 4 side to the gasification chamber 1 side through the lower end (opening 25) near the bottom. Here, the fluidized state on the gasification chamber 1 side near the partition wall 15 between the gasification chamber 1 and the sedimentation char combustion chamber 4 is relatively stronger than the fluidized state on the sedimentation char combustion chamber 4 side. Is kept at. This assists the movement of the fluidized medium from the settling char combustion chamber 4 to the gasification chamber 1 by an attractive action.

Similarly, the fluidized state on the char combustion chamber 2 side near the partition wall 11 between the gasification chamber 1 and the char combustion chamber 2 is relatively stronger than the fluidized state on the gasification chamber 1 side. It has been kept in an activated state. Therefore, the fluidized medium is the partition wall 11
Flowing into the char combustion chamber 2 side through an opening 21 (submerged in the rich layer) below the interface of the fluidized bed, preferably below the upper surface of the rich layer.

The heat recovery chamber 3 is fluidized uniformly as a whole, and is normally maintained so as to be weaker than the fluidized state of the char combustion chamber 2 in contact with the heat recovery chamber. Therefore, the superficial velocity of the fluidizing gas in the heat recovery chamber 3 is 0 to 3 Umf,
Alternatively, it is controlled within the range of 0 to 3 Umf, and the fluidized medium forms a sedimented fluidized bed while gently flowing. 0 here
Umf is the state in which the fluidizing gas has stopped. With such a state, heat recovery in the heat recovery chamber 3 can be minimized. That is, the heat recovery chamber 3 can arbitrarily adjust the amount of recovered heat in the maximum to minimum range by changing the fluidized state of the fluidized medium. Further, in the heat recovery chamber 3, the fluidization may be uniformly started or stopped or the strength may be adjusted in the entire chamber, but it is also possible to stop the fluidization in a part of the region and place the other in the fluidized state. However, the strength of the fluidized state in a part of the area may be adjusted.

The relatively large incombustibles contained in the waste or fuel are incombustibles discharge port 33 provided at the furnace bottom of gasification chamber 1.
Discharge from. Also, the furnace bottom of each room may be horizontal,
In order not to make a stagnant part of the flow of the fluid medium,
The furnace bottom may be inclined according to the flow of the fluidized medium near the furnace bottom. The incombustibles outlet 33 may be provided not only on the bottom of the gasification chamber 1 but also on the bottom of the char combustion chamber 2 or the heat recovery chamber 3.

The most preferable fluidized gas in the gasification chamber 1 is to pressurize the produced gas b for recycling. In this way, the gas emitted from the gasification chamber 1 is purely the gas generated from the fuel, and a very high quality gas can be obtained. Water vapor if that is not possible,
It is preferable to use a gas containing as little oxygen as possible (oxygen-free gas) such as carbon dioxide gas (CO ₂ ) or combustion exhaust gas obtained from the char combustion chamber 2. When the bed temperature of the fluidized medium decreases due to the endothermic reaction during gasification, if necessary, high-temperature combustion exhaust gas, for example, combustion exhaust gas having a temperature higher than the thermal decomposition temperature is supplied, or in addition to oxygen-free gas Alternatively, oxygen or a gas containing oxygen, for example, air may be supplied to burn a part of the produced gas to maintain the bed temperature. The fluidizing gas supplied to the char combustion chamber 2 supplies a gas containing oxygen necessary for char combustion, for example, air, a mixed gas of oxygen and water vapor. Calorific value of fuel a
When is low, it is preferable to increase the oxygen ratio in the mixed gas, and pure oxygen may be supplied as it is. As the fluidizing gas supplied to the heat recovery chamber 3, air, steam, combustion exhaust gas, or the like is used.

The upper portion of the fluidized bed of the gasification chamber 1 and the char combustion chamber 2 (the upper surface of the splash zone), that is, the freeboard portion, is completely partitioned by the partition walls 11 and 15. Furthermore, since the portion above the upper surface of the dense bed of the fluidized bed, that is, the splash zone and the freeboard portion is completely partitioned by the partition wall, the char combustion chamber 2
Even if the balance of the pressures of the freeboard portions of the gasification chamber 1 and
Alternatively, the turbulence can be absorbed only by a slight difference in the position difference of the upper surface of the dense layer, that is, the layer height difference. That is, since the gasification chamber 1 and the char combustion chamber 2 are partitioned by the partition walls 11 and 15, even if the pressure in each chamber fluctuates, this pressure difference can be absorbed by the bed height difference. Layer 2 is opening 2
It can be absorbed until it descends to the upper ends of 1, 25. Therefore, the upper limit of the pressure difference between the freeboards of the char combustion chamber 2 and the gasification chamber 1 that can be absorbed by the bed height difference is the gasification from the upper ends of the openings 21 and 25 in the lower portions of the partition walls 11 and 15 that partition each other. It is almost equal to the head difference between the head of the chamber fluidized bed and the head of the char combustion chamber fluidized bed.

In the integrated gasification furnace 101 described above,
Inside a single fluidized bed furnace, three gasification chambers, a char combustion chamber, and a heat recovery chamber are installed through partition walls, and the char combustion chamber and gasification chamber, and the char combustion chamber and heat recovery chamber are respectively separated. Adjacent to each other. This integrated gasifier 101
Since a large amount of fluidized medium can be circulated between the char combustion chamber and the gasification chamber, a sufficient amount of heat for gasification can be supplied only by the sensible heat of the fluidized medium.

Further, in the above integrated gasification furnace, since the seal between the char combustion gas and the produced gas is perfected,
The pressure balance between the gasification chamber and the char combustion chamber is well controlled, the combustion gas and the produced gas are not mixed, and the property of the produced gas is not deteriorated.

The fluid medium c1 as the heat medium and the char h flow from the gasification chamber 1 side to the char combustion chamber 2 side, and the same amount of the fluid medium c2 is supplied from the char combustion chamber 2 side. Since it is configured to return to the gasification chamber 1 side, it is naturally mass-balanced and mechanically conveyed using a conveyor or the like to return the fluidized medium from the char combustion chamber 2 side to the gasification chamber 1 side. There is also no problem that handling of high-temperature particles is difficult and sensible heat loss is large.

A specific operation when the integrated gasification furnace 101 described above is used in the methanol synthesis system according to the first embodiment of the present invention will be described. The waste or fuel a supplied to the gasification chamber 1 of the integrated gasification furnace 101 is decomposed into combustible gas b, char h, and ash f by thermal decomposition. Here, examples of the waste or fuel a include waste plastic, waste tire, car shredder dust, wood waste, general waste RDF, coal, heavy oil, tar, and other organic materials having a high calorific value. It is desirable that it is a solid waste or fuel.

Among the chars h produced by thermal decomposition in the gasification chamber 1, those having a large particle size and not entrained in the combustible gas are transferred to the char combustion chamber 2 together with the fluidized medium c1. In the char combustion chamber 2, the char h is completely burned by using air, oxygen-enriched air, or an oxygen-containing gas such as oxygen as the fluidizing gas g2. Part of the amount of heat generated by the combustion of the char h is supplied to the gasification chamber 1 as sensible heat of the fluidized medium c2 that is circulated back to the gasification chamber 1 and is used as the amount of heat required for thermal decomposition in the gasification chamber 1. Used.

According to this method, the combustible gas b generated by the thermal decomposition of the waste or solid fuel a in the gasification chamber 1
That is, since the generated gas and the combustion gas e generated by the combustion of the char h in the char combustion chamber 2 do not mix, a high calorie generated gas suitable for liquid fuel synthesis can be obtained.

In particular, the fluidized gas g1 in the gasification chamber 1 contains no air or oxygen gas, and the total amount of heat required for thermal decomposition is determined by the amount of heat generated by the combustion of the char h in the char combustion chamber 2. Is supplied via the sensible heat of the fluidized medium, so that the combustion gas concentration of CO ₂ , H ₂ O, etc. is extremely low and the calorie content is high, without causing partial combustion in the gasification chamber 1. Product gas can be obtained.

As described above, in the liquid fuel synthesis, it is important to keep the concentration of the inert gas such as nitrogen and argon in the raw material gas low in order to improve the liquid fuel yield. Therefore, the fluidized gas g1 in the gasification chamber 1
In addition, the concentration of the inert gas such as the nitrogen gas and the argon gas in the produced gas b is included in the waste or the solid fuel a by configuring that the inert gas such as the nitrogen gas and the argon gas is not included at all. It is possible to reduce the concentration to nitrogen and argon.

In the case of a general partial-combustion gasification furnace, it was necessary to supply pure oxygen as an oxidant in order to prevent nitrogen from being mixed in the produced gas, but the integrated type used in the embodiment of the present invention is used. When the gasification furnace 101 is used, even if air is used as the oxidant in the char combustion chamber 2, the nitrogen in the air is not mixed with the side of the produced gas b, so that the oxygen production power is reduced and the nitrogen in the produced gas b is reduced. It is possible to achieve both reduction of gas concentration, which is particularly effective.

As described above, in the liquid fuel synthesis, there is an appropriate H ₂ / CO ratio in the produced gas depending on the type of the liquid fuel as the final product. Therefore, in the first embodiment, C / of the target waste or solid fuel is
In order to deal with the case where the H ratio is not suitable for the liquid fuel as a product, the CO conversion device 104 is provided in the subsequent stage.
Thereby, the H ₂ / CO ratio of the produced gas can be set to a predetermined value.

As a modification of the first embodiment, hydrogen gas or hydrocarbon gas such as methane, ethane, propane, etc. is used as all or part of the fluidizing gas g1 in the gasification chamber 1 of the integrated gasification furnace 101. Alternatively, if carbon dioxide gas is used, the H ₂ / CO ratio of the produced gas can be set to an optimum value for the synthesis of the target liquid fuel. This H ₂ / CO
It is desirable that the ratio value be 2 or more in the case of methanol synthesis and 1 or more in the case of dimethyl ether synthesis.

In this case, the hydrogen gas or the hydrocarbon gas such as methane, ethane or propane or the carbon dioxide gas is the surplus gas generated in the liquid fuel synthesizing step in the liquid fuel synthesizing apparatus 200 using the produced gas b as a raw material. It may be recycled for use.

The fluidizing gas g supplied to the gasification chamber 1
As a whole or a part of 1, the main component is one gas selected from the group consisting of steam, hydrogen gas, hydrocarbon gas, carbon dioxide gas and product gas b, or a mixture of two or more gases selected from the above group. By doing so, it becomes possible not to use air as the fluidizing gas, and the fluidizing gas can be a gas that does not substantially contain nitrogen gas and oxygen gas. In this case, the term “main component” means that oxygen is not substantially contained and air is not substantially contained, for example. In particular, it means that it does not substantially contain an inert gas such as nitrogen or argon. The term "substantially free of" means not including a level of impurities due to leakage or the like. The hydrocarbon gas is, for example, methane, ethane, propane or the like. When using these gases, the molar ratio of hydrogen gas to carbon monoxide gas in the produced gas can be maintained at a predetermined value.

In adjusting the molar ratio of the hydrogen gas and the carbon monoxide gas in the produced gas, the purified gas 3 in FIG.
The composition of 01a may be measured by a gas component measuring device (not shown), and the amount of hydrogen gas, hydrocarbon gas, carbon dioxide gas or the like added to the fluidizing gas g1 may be adjusted based on the result. In addition, the measurement point by the gas component measuring device is the gasification furnace 10
It may be anywhere from the latter stage of 1 to the former stage of the liquid fuel device 200.

In the embodiment shown in FIG. 1, the fluidizing gas g
As 1, the water vapor is mainly used.
A line from the adjusting device 109 is connected to the steam supply line so as to join. Lines of hydrogen gas, hydrocarbon gas, and carbon dioxide gas are connected to the adjusting device 109 that receives a signal from the gas component measuring device (not shown). The components of the fluidizing gas g1 can be adjusted by adjusting the amounts of hydrogen gas and carbon dioxide added. In addition, CO ₂ gas 302 from the decarbonator 106,
Alternatively, the purge gas 307a containing hydrogen, carbon monoxide, and hydrocarbon as a main component from the methanol synthesis tower apparatus may be supplied to the adjusting apparatus 109 and mixed with the steam to be used as the fluidizing gas in the gasification chamber 1. . By doing this,
Hydrogen, carbon monoxide, hydrocarbons and carbon dioxide gas generated from the raw materials can be used as the fluidizing gas and can be effectively used without waste. Purge gas 307a from the methanol synthesis tower device
May have hydrogen, carbon monoxide, hydrocarbon, or carbon dioxide as a main component.

Now referring to the flow chart of FIG.
An example of the methanol synthesizer 200 as a synthesizer will be described. This synthesizer is an adiabatic quench type reactor. The gas 301a whose pressure has been increased to the methanol synthesis reaction pressure by the gas compressor 107 is used as the methanol synthesis device 2
Sent to 00. The compressed gas 301b sent to the synthesizer 200 merges with the unreacted circulating gas 307b and is supplied to the suction side of the circulator 202. A centrifugal blower is used as the circulator 202.

In the adiabatic quench type reactor, after the synthesis gas is preheated by the heat recovery unit 203 to the temperature required for the reaction,
A gas 303 of 40 to 60% of the total raw material synthesis gas amount is supplied to the first catalyst layer in the methanol synthesis column 201. The remaining gas 304 is supplied as quench gas to each catalyst layer in order to control the temperature of the catalyst layers below the second catalyst layer to an appropriate temperature, and is uniformly mixed with the gas that has passed through the upper catalyst layer. . As a result, the temperature of the reaction gas increased by the adiabatic reaction in the catalyst layer is lowered, and the temperature of the next catalyst layer is properly controlled. A heat exchanger is used as the heat recovery unit 203.

Outlet gas 305 of methanol synthesis tower 201
In the heat recovery unit 203, the retained heat is recovered and cooled by preheating the raw material synthesis gases 303 and 304 supplied to the synthesis tower 201, generation of low-pressure steam used in the distillation step described later, and the like. The cooled gas 306 is passed through the high pressure separator 204 to the crude methanol 308 and the unreacted gas 30.
It is separated into 7. In order to keep the concentration of the inert components such as methane and nitrogen accumulated in the unreacted gas 307 at a certain level, a certain amount of gas is extracted as the purge gas 307a. The remaining gas 307b is compressed as a circulation gas together with the synthesis gas 301b sent from the compression step in the circulator 202, preheated in the heat recovery unit 203, and then supplied to the methanol synthesis tower 201. It The unreacted gas 307 is a gas containing hydrogen, carbon monoxide, and hydrocarbon as main components, which is supplied to the methanol synthesis tower 201.

The separated crude methanol 308 is used in the distillation column 2
At 05, the distillation process is performed. The crude methanol 308 is refined into a product methanol 309 through a distillation process. Although not shown, the distillation column 205 includes two columns, a first distillation column and a rectification column. The first distillation column is operated at almost normal pressure to distill off low boiling point components 310 such as methyl formate, dimethyl ether, acetone and paraffins from crude methanol. The rectification column is operated under almost normal pressure or a pressure of about 0.1 MPa to remove high boiling point components 311 such as water and higher alcohols,
The product methanol 309 is obtained.

In the methanol synthesis tower 201, a synthesis gas containing carbon monoxide and hydrogen as main components is supplied at a pressure of 5 to 10 MPa.
a, under the condition of a temperature of 200 to 300 ° C., the reaction is carried out on a catalyst containing copper and zinc as main components to synthesize methanol. This reaction is an exothermic reaction and a large amount of heat is generated. The heat of reaction is recovered and used in the heat recovery device 203 as described above, but efficient removal of this reaction heat is effective in increasing the reaction efficiency, and therefore is not shown for heat recovery. Boiler water may be supplied to the heat recovery device 203 through the supply pipe to heat the reaction heat as steam at a medium pressure of about 200 ° C. to recover the heat.

Since the methanol synthesis reaction is an equilibrium reaction, the yield is not so high even if it passes through the synthesis tower 201 once. Therefore, as described above, the circulation machine (circulation blower) is used.
Circulating the reaction gas using 202 is performed.
From this circulation system, it is necessary to constantly withdraw the produced methanol and inert components such as nitrogen and argon that do not participate in the reaction. The inert gas component is discharged as a purge gas out of the system, but since only the inert gas component cannot be removed from the reaction system, a certain amount of the circulating gas is extracted and the amount of the inert gas component contained therein is input. By making the amount equal to the above amount, the concentration of the inert gas component in the reaction system is kept constant.

Since the extracted purge gas 307a contains a large amount of combustible components, it can be used as a fuel. However, the larger the amount of the extracted purge gas, the more effective components originally used for methanol synthesis are extracted. Therefore, the yield of methanol decreases. Therefore, it is desirable that the initial synthesis gas contains as few inert gas components as possible.

Although the liquid fuel synthesis process from syngas has been described above by taking methanol as an example, other types of fuel such as gasoline, kerosene, light oil, and dimethyl ether described later have different catalyst species and reaction conditions. The basic structure of the process is similar, with only some differences.

In the case of synthesizing hydrocarbon fuels such as gasoline, kerosene, and light oil, iron-based catalysts or cobalt-based catalysts are used. In the case of iron-based catalysts, generally 250 to 350 ° C,
The reaction is carried out at 2.0 to 4.0 MPa. In the case of a cobalt-based medium, 220 to 250 ° C, 0.5 to 2.0M
The reaction is performed at Pa. This is called the Fischer-Tropsch reaction, and although the pressure is slightly lower than in methanol synthesis, the temperature conditions are almost the same. In this process, since various hydrocarbon fuels such as gasoline, kerosene, and light oil are mixed and obtained, it is possible to separately obtain gasoline, kerosene, light oil, etc. by using a multistage distillation apparatus.

In any of the above processes, the following is required from the characteristics in order to efficiently synthesize liquid fuel. First of all, it is necessary that the calorific value of the synthesis gas is high, that is, the concentrations of H ₂ and CO gas that are effective components are high. This is an excess gas component, especially C
This means not containing a large amount of combustion gas components such as O ₂ and H ₂ O, and in the case of partial combustion gasification, it is particularly important to reduce the partial combustion ratio as much as possible.

Secondly, it is desirable that the concentration of inert gas such as nitrogen or argon is as low as possible. Since it is difficult to remove these before the liquid fuel synthesis step, they are removed as purge gas by being entrained in the circulating gas of the reaction system. Therefore, if the amount of the inert gas is large, a component effective for the reaction (H ₂ ,
The amount of CO, etc.) to be extracted also increases, which causes a decrease in the final liquid fuel yield.

The above two points mean that "the excess gas component for the reaction should be as small as possible". This is important because the smaller the surplus gas component, the more the compression power of the produced gas can be reduced and the energy efficiency of the process can be increased.

Thirdly, the H ₂ / CO ratio of the synthesis gas needs to be an appropriate value. Stoichiometrically, H ₂ / CO = 2 for methanol synthesis and H _{2 for} dimethyl ether synthesis.
_{If 2} / CO = 1, the reaction efficiency is highest. H ₂
If the CO / CO ratio is lower than this, the CO conversion step causes H
_It is necessary to adjust the ₂ / CO ratio, but if it is higher than this, the CO conversion step is unnecessary, and the cost can be reduced.

Fourthly, it is desirable that impurity components such as chlorine, sulfur and dust in the synthesis gas are as low as possible. As a result, it is possible to reduce costs such as the cleaning process and the desulfurization process.

In addition to the above, in consideration of the fact that the liquid fuel synthesis reaction is usually an exothermic reaction and medium-pressure steam can be recovered, and that the distillation step of the final product requires low-pressure steam as a heat source, It is important to enhance the energy efficiency to configure the process so that the heat can be utilized to the maximum extent in the entire process including the gasification process.

With reference to the flowchart of FIG. 4, the purpose is to maximize the efficiency of heat utilization in the system,
A second embodiment of the methanol synthesis system of the present invention will be described. Overlapping description of the same parts as those in the first embodiment will be omitted.

The system of the present embodiment has a waste heat boiler 11 for recovering heat from the combustion gas e discharged from the combustion chamber 2.
1, a steam 322 generated in the waste heat boiler 111, and a high-pressure steam reservoir 112 that stores steam 325 generated in the heat recovery chamber 3. The temperature of this high-pressure steam is approximately 300 ° C.
Is about 500 ° C., preferably about 400 ° C., and the pressure is about 3 to 10 MPa, preferably about 4 MPa. The waste heat boiler 111 is supplied with boiler feed water 321 pressurized by a boiler feed pump (not shown). Further, the in-layer heat transfer pipe 41 of the heat recovery chamber 3 is supplied with boiler feed water 324 pressurized by a boiler feed pump (not shown).

The present system further includes a steam turbine 11 which uses high pressure steam 326 from the high pressure steam reservoir 112 as a drive source.
3. A generator 114 that is driven by the steam turbine 113 to generate electric power is provided. The steam turbine 113 is an extraction steam turbine, and extracts low-pressure steam 327 from an intermediate stage.

Electric power 331 generated by the generator 114 is sent to the electric motor 108 which drives the produced gas compressor 107. In this way, the electric power 331 covers the required power in the present process, mainly the power for the electric motor 108.

Of course, the output shaft of the steam turbine 113 is directly connected to the power shaft of the gas compressor 107, and the steam turbine 1
Gas compression may be performed by 13. However,
Although the input amount of waste and the liquid fuel synthesis amount may fluctuate, it is preferable to use the generator 114 and the electric motor 108 in order to cope with this. That is, with the power generation device 114,
It is possible to take a method such as transmitting surplus power to the outside,
It is easy to deal with the fluctuation of the required power in the system.

From the steam turbine 113, a low pressure of 150 ° C.
The steam before and after is extracted and used as a low-temperature heat source in the liquid fuel distillation process. When power is generated by the steam turbine 113, since a large amount of low-temperature waste heat is usually present in the condenser, even if a large amount of such low-pressure steam is used for extraction, the power generation efficiency does not decrease so much and the entire process is reduced. It has a direct effect on the improvement of thermal efficiency.

Further, the steam at about 200 ° C. can be recovered from the methanol synthesizer (in particular, the heat recovery unit 203 (see FIG. 3)). This is recovered as medium pressure steam of about 1.2 to 1.6 MPa, preferably around 1.5 MPa,
It is particularly suitable to use as the fluidizing gas g1 in the gasification chamber 1 of the integrated gasification furnace 101. Alternatively, by increasing the supply water pressure to about 3 to 10 MPa, preferably about 4 MPa, the amount of heat is recovered as compressed water at about 200 ° C.,
By introducing this into the heat recovery chamber 3 of the integrated gasification furnace 101 or a part of the waste heat boiler 111, further heating,
By recovering as high pressure steam of about 3 to 10 MPa, preferably about 4 MPa and supplying it to the steam turbine 113,
It can also be used for power generation.

As described above, according to this embodiment, as the electric power source or heat source required in the liquid fuel synthesizing step,
The steam 322 generated in the heat recovery chamber 3 provided in the integrated gasification furnace 101 and the waste heat boiler 111 that recovers heat from the combustion gas e from the char combustion chamber 2 is used.

As described above, since liquid fuel synthesis is carried out under high pressure, a large amount of power is often required to compress the produced gas b. On the other hand, in the final step of fuel synthesis, impurities are separated by distillation, but this distillation step requires a large amount of heat at a relatively low temperature, generally around 150 ° C. Since the liquid fuel synthesis reaction from the synthesis gas mainly containing H ₂ and CO is an exothermic reaction, it is possible to recover this reaction heat as vapor by devising a reaction device. For example, in the case of methanol synthesis, the reaction is about 2
Since it is performed at 00 to 300 ° C, medium pressure steam around 200 ° C can be recovered. It is not preferable to use this as a heat source in the above-mentioned distillation step in terms of energy cascade use. The second embodiment solves the above problems,
It is possible to maximize the efficiency of heat utilization in the system.

Although not shown in the second embodiment and FIG. 4, when the water content of the object to be treated is relatively high, a part of the low pressure steam or medium pressure steam is dried. It can also be used as a source. Particularly, from the viewpoint of energy cascade use, low-pressure steam of about 150 ° C. is preferable as the dry heat source. As mentioned above, the use of low-pressure steam has the effect of reducing low-temperature waste heat in the condenser, so the power generation efficiency does not decrease so much. With this configuration, the cold gas efficiency is improved by lowering the water content of the raw material, so that the recovery amount of the liquid fuel can be increased and the thermal efficiency of the entire process is improved.

FIG. 5 shows a flow chart of a dimethyl ether synthesis system as a liquid fuel synthesis system according to a third embodiment of the present invention. In the present embodiment, an integrated gasification furnace 101 for gasifying waste or solid fuel, and a product gas b generated in the gasification furnace 101
A gas cleaning device 103 for cleaning the gas, a DME (dimethyl ether) synthesizer 400 using the cleaned gas, and
The humidifying device 115 is a system that includes at least a part of the purge gas 507a as the surplus gas from the ME synthesizing device 400, and the humidifying device 115 as the adjusting device that humidifies the high temperature cleaning liquid 116 by bringing them into contact with each other. Purge gas 507a
The fluidizing gas g1 in this system containing hydrogen, carbon monoxide, hydrocarbons, and carbon dioxide as main components may be only steam supplied from the steam supply line 118 shown in FIG. 5, or the purge gas 507a. May be only. Further fluidized gas g1 in this system
The purge gas 507a may be added to the steam supplied from the steam supply line 118, or the steam supplied from the steam supply line 118 is humidified by the humidifier 115 as shown in FIG. The purge gas 507a containing water vapor may be added. In the integrated gasification furnace 101, a classification device 10 for classifying the fluidized medium c3 and the incombustible substance d extracted from the gasification chamber 1
2 are installed. A dimethyl ether synthesis system will be described here as an example of the liquid fuel synthesis system.
It can also be used for the synthesis of other liquid fuels. In addition, in the present embodiment, the integrated gasification furnace 101 and the classification device 102
Is the same as in the first embodiment described above.

The dimethyl ether synthesis system according to the present embodiment has an integrated gasification furnace 101 for generating a product gas b.
A gas cleaning device 103 for cleaning the generated gas b, a desulfurization device 105 for removing sulfur from the cleaned gas, and a CO conversion device 104 for converting the desulfurized gas into CO are installed along the flow path of the generated gas b. Has been done. Furthermore, CO
A gas compressor 107 that compresses the converted gas 501a and a dimethyl ether synthesizer 400 that synthesizes dimethyl ether using the compressed gas 501b are installed.

The gas discharged from the dimethyl ether synthesizer 400 contains unreacted hydrogen, carbon monoxide, hydrocarbons, and carbon dioxide gas as a reaction product. A part of this exhaust gas is a circulating gas 50 in the synthesizer 400.
7b, while the rest is purge gas 507a
Is introduced to the humidifier 115 as. In the humidifier 115, the purge gas 507a comes into contact with the high temperature cleaning liquid 116 from the gas cleaning device 103, and the purge gas 507a is humidified. The humidified gas is supplied to the gasification chamber 1 of the integrated gasification furnace 101 as a gasifying agent. In the humidifier 115, the high temperature cleaning liquid 116 is deprived of sensible heat by the purge gas 507a and cooled to become the low temperature cleaning liquid 117, which is discharged. Humidifier 1
The low temperature cleaning liquid 117 discharged from 15 is the gas cleaning device 1
Returned to 03. Here, consider the heat balance in the gas cleaning device 103. The hot product gas b is used in the gas cleaning device 1
03, countercurrently contacts the low temperature cleaning liquid 117, heat exchange is performed, the generated gas b is cooled and loses sensible heat, and the low temperature cleaning liquid 117 is heated to obtain sensible heat. That is, the sensible heat of the generated gas b is transferred to the cleaning liquid. The sensible heat of the high-temperature cleaning liquid 116 is recovered by the humidifying device 115 in the purge gas 507a, and the high temperature purge gas 507a is the fluidizing gas g.
1 is sent to the gasification chamber 1. That is, the sensible heat lost by the generated gas b in the gas cleaning device 103 is caused by the cleaning liquid 116,
It is recovered in the gasification chamber 1 through 117 and the purge gas 507a, and the sensible heat of the gas is effectively used.

The raw material a supplied to the gasification chamber 1 of the integrated gasification furnace 101 is pyrolyzed and gasified in the gasification chamber 1,
Produces pyrolysis gasification gas and a chain. The generated gas b thus generated is guided to the gas cleaning device 103 and cleaned.

As shown in FIG. 6, the gas cleaning device 103
There is a wet cleaning tower 103A as an example. The wet cleaning tower 103A includes a gas outlet 123 and a mist separator 1
22, the packed bed 121, the liquid collector 124, and the settling section 11
And 8 are included. By adopting the wet cleaning, the generated gas b and the cleaning liquid 117 are brought into countercurrent contact with each other, and acidic gases such as hydrogen chloride and hydrogen sulfide in the generated gas b can be absorbed and removed. Therefore, the cleaning liquid 116 may be a mixture of alkali such as caustic soda.
It is also possible to reduce corrosion of equipment by preventing 16 from becoming acidic due to absorption of acidic gas.

In the wet cleaning tower 103A shown in the figure, the cleaning liquid 117 is supplied from the upper part of the tower, the generated gas b is supplied from the middle part of the tower, and the packed bed 121 in the central part is in alternating contact. The generated gas b that has passed through the packed bed 121 and has been washed with the washing liquid 117 has the mist accompanying it removed by the mist separator 122 provided at the top of the tower, and is discharged from the gas outlet 123 provided at the top of the tower. It is sent to the next process. When the generated gas b contains solids such as dust f, the generated gas b fills the packed bed 12 with solids such as dust f.
In the process of passing 1, the gas moves to the cleaning liquid 116 side, and the generated gas b becomes a clean gas.

Product gas b supplied from the gasification furnace 101
Is a high temperature, but its sensible heat is transferred to the cleaning liquid 117 by coming into contact with the low temperature cleaning liquid 117 in the wet cleaning tower 103A, and the low temperature low temperature cleaning liquid 117 becomes high temperature and becomes the high temperature cleaning liquid 116. The high temperature cleaning liquid 116, which has been heated to a high temperature, is sent from the collector 124 to the settling section 118 at the bottom of the tower,
At 8, the solid content contained in the liquid is precipitated and separated, and the separated solid content is concentrated and discharged from the lower part of the tower. In the sedimentation separation of the solid content, finer particles can be separated as the rising speed of the liquid is slower. Therefore, it is preferable that the diameter of the sedimentation section 118 in the lower part of the column is wide. The cleaning liquid from which the solid content has been separated is supplied to the humidifier 115 as the high-temperature cleaning liquid 116. Settling section 1
It is possible to avoid troubles such as blockage of the liquid sending system by installing a weir 119A at 18 and providing a liquid overflow section 119 and supplying only the overflowed clean cleaning liquid as the high temperature cleaning liquid 116 to the humidifier 115. .

As shown in FIG. 5, the produced gas b cleaned by the gas cleaning device 103 is sent to the desulfurization device 105,
The desulfurization device 105 removes the sulfur compounds that were not removed by the gas cleaning device 103, and sends the sulfur compounds to the CO conversion device 104.

In the case of dimethyl ether synthesis, H in the gas
_{The 2} / CO ratio is preferably 1 or more as described above, but CO conversion is performed in order to bring the H ₂ / CO ratio in the gas after desulfurization to this appropriate value. In the CO conversion device 104, H _{2 is} generated by the reaction between CO in the produced gas b and steam.
And converted to CO _2. The gas leaving the CO conversion device 104 is pressurized by the gas compressor 107 and supplied to the DME synthesis device 400.

The dimethyl ether synthesis process is roughly divided into two methods. One is a dehydration reaction of the synthesized methanol. In this method, a dehydration catalyst device is added to the same system as the above-mentioned methanol synthesis method. The reaction conditions are the same as the methanol synthesis process (temperature 250-300 ° C, pressure 5-10MP).
a). Another method is direct synthesis,
The conditions of 50 to 280 ° C. and 3 to 7 MPa are suitable, and particularly high selectivity is exhibited at 260 ° C. and 5 MPa.

FIG. 7 shows an example of the DME synthesizer 400 in the case of the direct synthesis method which is one of the dimethyl ether synthesis processes. The DME synthesis device 400 includes a DME synthesis tower device 401, a cooling device 402, a gas-liquid separator 403, a DME.
It is configured to include a distillation device 404 and a circulator 405 (for example, a centrifugal blower). This synthesizer 400 is a slurry bed reactor. The gas 501b whose pressure has been increased to the dimethyl ether synthesis pressure by the gas compressor 107 is sent to the bottom of the dimethyl ether synthesis tower device 401. The entire amount of the gas after the reaction in the dimethyl ether synthesis tower device 401 is sent to the cooling device 402 from the top of the dimethyl ether synthesis tower device 401 and cooled, and the product dimethyl ether and the by-product methanol are liquefied and cooled. It is sent from the device 402 to the uppermost part of the gas-liquid separation device 403. In the gas-liquid separator 403, the crude dimethyl ether 508 which is a liquid component is separated into a gas component, and the liquid component is sent from the bottom part of the gas-liquid separator 403 to the middle part of the dimethyl ether distillation device 404. In the dimethyl ether distillation apparatus 404, the product dimethyl ether 509 is separated from the by-products methanol 510 and water by distillation, and the dimethyl ether 509 is recovered from the top and the methanol 510 and water from the bottom.

On the other hand, a part of the gas component separated by the gas-liquid separator 403 is circulated by the circulator 405, and the gas 5 whose pressure is increased by the gas compressor 107 as the circulating gas 507b.
01b is supplied to the dimethyl ether synthesis tower device 401. The remaining gas is sent out of the dimethyl ether synthesizer 400 as a purge gas 507a.

As shown in FIG. 5, at least a part of the delivered purge gas 507a is guided to the humidifying device 115 and humidified by contact with the high temperature cleaning liquid 116. A part of the purge gas 507a may be guided to the humidifier 115. The purge gas 507a that is not guided to the humidifier 115 may be discharged outside the system. The humidified gas is a gasifying agent g1
Is supplied to the gasification chamber 1 of the integrated gasification furnace 101. That is, in the present embodiment, among the gases separated and collected as the unreacted gas from the liquid component in the dimethyl ether synthesizer 400, the gas necessary for gasifying the raw material in the integrated gasification furnace 101 is a humidifier. It is supplied after being humidified at 115. The dimethyl ether synthesis gas preferably has an H ₂ / CO ratio of 1 or more, but when the H ₂ / CO ratio of the produced gas b exceeds 1,
The unreacted gas containing CO ₂ generated in the dimethyl ether synthesis step is humidified and used as a gasifying agent in the gasification chamber 1, whereby the generated gas b becomes a CO-rich gas, and H ₂ / CO
It is possible to get the ratio close to 1. Optimal product gas b
The amount of the purge gas 507a supplied to the humidification device 115 can be adjusted so that the molar ratio of H2 and CO in the inside is adjusted. A gas component measuring device is provided at any position from the latter stage of the gasification furnace 101 to the former stage of the dimethyl ether synthesizer 400, and the supply amount of the purge gas 507a can be adjusted based on the measurement result of the gas component measuring device. . That is, the humidifier 115 uses H ₂ / CO of the produced gas.
Has a molar ratio adjusting function.

As the humidifying device 115, a packed bed device similar to the cleaning device of FIG. 6 may be used, and the purge gas 507a and the high temperature cleaning liquid 116 from the cleaning device 103 are brought into countercurrent contact with each other to cause the gasification chamber 1 The purge gas 507a supplied as the fluidizing gas g1 can be humidified. The gas discharged from the humidifying device 115 in contact with the high temperature cleaning liquid 116 becomes a gas containing water vapor corresponding to the saturated vapor pressure at the discharge temperature. Therefore, the higher the temperature of the high-temperature cleaning liquid 116, the more the gas containing water vapor.

Similar to the second embodiment shown in FIG. 4,
Also in the present embodiment, the waste heat boiler 111 that recovers heat from the combustion gas e discharged from the char combustion chamber 2 of the integrated gasification furnace 101, and the high-pressure distillation sump 112 that stores the steam generated in the waste heat boiler 111 are provided. It may be provided. In this way, the heat can be efficiently used in the system.

As described above, according to the present embodiment, the generated gas b generated in the gasification chamber 1 and the combustion gas e generated in the char combustion chamber 2 are separated, so that high calorie generation suitable for dimethyl ether synthesis is generated. The gas b can be obtained, and the gas scrubber 103 and the desulfurizer 105 remove hydrogen chloride, sulfide compounds and the like of the produced gas b, and the CO converter 104 and the humidifier 115 generate H ₂ / CO molar ratios. The H ₂ / CO molar ratio in the gas b is set to an appropriate value, at least a part of the purge gas 507a humidified by the humidifier 115 is added to steam, and the steam added with the purge gas 507a is gasified as the fluidizing gas g1. The sensible heat lost to the generated gas b in the gas cleaning device 103 can be sent to the chamber 1 and the cleaning liquids 116 and 117 and the purge gas 507a.
Since it can be recovered in the gasification chamber 1 via the dimethyl ether, it is possible to provide a dimethyl ether synthesis system capable of efficiently producing dimethyl ether.

[0112]

As described above, according to the present invention, since the gasification chamber for flowing the high temperature fluid medium therein is provided, the gas to be treated is gasified and the produced gas containing hydrogen and carbon monoxide as the main components is produced. Since it is equipped with a char combustion chamber in which a high-temperature fluidizing medium is made to flow inside to burn the char,
The fluidized medium can be heated, the liquid fuel can be synthesized because it has the synthesizer that uses the generated gas, and the gasification chamber and the char combustion chamber have their respective fluidized beds because they have the first partition wall. It is possible to partition so that there is no gas flow above the interface in the vertical direction, and a communication port that connects the gasification chamber and the char combustion chamber is formed in the lower part of the first partition wall. Through, the fluidized medium heated in the char combustion chamber can be moved from the char combustion chamber side to the gasification chamber side.

According to this structure, since the generated gas generated in the gasification chamber and the combustion gas generated in the char combustion chamber are separated, a generated gas suitable for synthesizing a high-calorie liquid fuel can be obtained. Therefore, it becomes possible to provide a liquid fuel synthesis system capable of producing a liquid fuel with high efficiency.

[Brief description of drawings]

FIG. 1 is a flow chart of a methanol synthesis system according to a first embodiment of the present invention.

FIG. 2 is a conceptual cross-sectional view of an integrated gasification furnace used in the embodiment of the present invention.

FIG. 3 is a flow chart of an example of the methanol synthesis apparatus used in the embodiment of the present invention.

FIG. 4 is a flow chart of a methanol synthesis system according to a second embodiment of the present invention.

FIG. 5 is a flow diagram of a dimethyl ether synthesis system according to a third embodiment of the present invention.

6 is a block diagram showing a configuration of a gas cleaning device 103 used in the dimethyl ether synthesis system of FIG.

7 is a block diagram showing a configuration of a DME synthesizer used in the dimethyl ether synthesis system of FIG.

[Explanation of symbols]

1 gasification chamber 2 combustion chamber 3 heat recovery room 101 Integrated gasifier 103 gas cleaning device 104 CO converter 105 Desulfurization equipment 106 Decarbonator 107 gas compressor 108 electric motor 109 Adjustment device 111 Waste heat boiler 112 High-pressure steam reservoir 113 steam turbine 114 generator 115 Humidifier 116 (high temperature) cleaning liquid 117 (low temperature) cleaning liquid 118 Steam supply line 200 Methanol synthesizer 201 Methanol synthesis tower 203 heat recovery device 301b compressed gas 307a Purge gas 309 Methanol 400 dimethyl ether synthesizer 401 Dimethyl ether synthesis tower equipment 402 Cooling device 403 Gas-liquid separator 404 Dimethyl ether distillation equipment 405 circulator 501b compressed gas 507a Purge gas 509 dimethyl ether 510 methanol b Generated gas e Combustion gas g1 fluidized gas

─────────────────────────────────────────────────── ─── Continuation of front page (51) Int.Cl. ⁷ Identification code FI theme code (reference) C10J 3/54 C10J 3/54 K L M Z C10K 1/10 B09B 3/00 ZAB C10K 1/10 303L ( 72) Inventor Yuki Iwataki 11-11 Haneda-Asahi-cho, Ota-ku, Tokyo Inside EBARA CORPORATION (72) Inventor Kaori Sasaki 11-1 Haneda-Asahi-cho, Ota-ku, Tokyo F-term inside EBARA CORPORATION (reference) ) 4D004 AA07 AA11 AA12 AA28 AA46 AC05 BA03 CA27 CA28 CB05 CC02 CC03 4H013 BA02 4H060 AA01 BB02 BB03 BB23 CC03 CC04 DD11 DD24 EE01 EE03 GG08

Claims (9)

[Claims] 1. A high-temperature fluidizing medium is fluidized internally to
A gasification chamber which forms a fluidized bed of a gasification chamber having an interface of, and which gasifies the material to be treated in the fluidized bed of the gasification chamber to generate a product gas containing hydrogen and carbon monoxide as main components; The fluidized medium is fluidized inside to form a char combustion chamber fluidized bed having a second interface, and char generated by gasification in the gasification chamber is combusted in the char combustion chamber fluidized bed to produce the fluidized medium. A char combustion chamber that heats the gas; and a synthesizer that synthesizes liquid fuel using the generated gas generated in the gasification chamber; the gasification chamber and the char combustion chamber are the interfaces of the respective fluidized beds. It is partitioned by a first partition wall so that gas does not flow upward in the vertical direction, and a communication port that connects the gasification chamber and the char combustion chamber is formed in a lower portion of the first partition wall. , The height of the upper end of the communication port is the first interface And a communication port that is not more than the second interface is formed, and the fluidized medium heated in the char combustion chamber is moved from the char combustion chamber side to the gasification chamber side through the communication port. Liquid fuel synthesis system. 2. The gasification chamber is configured to supply a fluidizing gas that fluidizes the fluidized bed, and the fluidizing gas includes steam, hydrogen gas, hydrocarbon gas, carbon dioxide gas, and the generated gas. A gas selected from the group consisting of,
Alternatively, the liquid fuel synthesizing system according to claim 1, which comprises a mixture of two or more gases selected from the group as a main component. 3. As the fluidizing gas, water vapor is mainly used, and the water vapor is mixed with at least one gas selected from hydrogen gas, hydrocarbon gas, and carbon dioxide gas. The liquid fuel synthesizing system according to claim 2, further comprising an adjusting device that adjusts an addition amount of the one or more kinds of gas to the water vapor. 4. The liquid fuel synthesis according to claim 3, wherein the adjusting device is set so as to adjust the molar ratio of hydrogen gas and carbon monoxide gas in the produced gas to be 2 to 5. system. 5. The liquid according to claim 3, wherein the adjusting device is set so as to adjust the molar ratio of hydrogen gas and carbon monoxide gas in the produced gas to be 0.7 to 2. Fuel synthesis system. 6. The liquid fuel synthesizing system generates at least one of hydrogen gas, hydrocarbon gas, and carbon dioxide gas as a surplus gas, and uses the surplus gas as a fluidizing gas for the gasification chamber. The liquid fuel synthesizing system according to any one of claims 2 to 5, which is configured. 7. A heat recovery chamber provided in contact with the char combustion chamber; a second bed partitioning a fluidized bed portion of the char combustion chamber fluidized bed between the char combustion chamber and the heat recovery chamber. A partition wall is provided, an opening is formed in the lower part of the second partition wall, and the fluidized medium of the char combustion chamber flows into the heat recovery chamber from the upper part of the second partition wall, and through the opening part. The liquid fuel synthesizing system according to claim 1, wherein a circulation flow returning to the char combustion chamber is formed. 8. Between the gasification chamber and the synthesizer,
The liquid fuel synthesizing system according to any one of claims 3 to 7, further comprising a gas cleaning device that cleans the generated gas. 9. The adjusting device is configured to introduce a high temperature cleaning liquid after cleaning the generated gas from the cleaning device and humidify the at least one gas by using the high temperature cleaning liquid as a heat source. The liquid fuel synthesis system according to claim 8.