JP6635594B2 - Biojet fuel manufacturing method and manufacturing equipment - Google Patents

Description

  The present invention relates to a biojet fuel production method and a production facility.

In recent years, with the aim of countermeasures against soaring fuel prices, reducing the burden on the global environment, and facilitating the securing of fuel, the development of technologies for manufacturing bio-jet fuel for aircraft using biomass resources such as wood and algae has been promoted. Demand for bio jet fuel is expected to increase.
For example, Patent Literatures 1 and 2 describe a technology for producing a liquid fuel from biomass. In order to produce a liquid fuel from biomass, for example, as described in Patent Literature 1, a step of gasifying biomass and a step of synthesizing the gasified substance to obtain a liquid fuel are performed.

  Patent Literature 3 describes a technique for producing a liquid fuel from natural gas. In this technology, in order to produce a liquid fuel from natural gas, unnecessary components are removed from the natural gas by a preparation process, which is processed in a Fischer-Tropsch synthesis process to synthesize a liquid hydrocarbon, and then isomerized. It is supposed that liquid hydrocarbons are isomerized into long-chain hydrocarbons by a hydrolyzing step (hydrocracking / hydroisomerization step), and further, an intermediate fraction is obtained by a distillation step, and liquid fuel is taken out from the intermediate fraction.

JP 2010-535282 A JP-T-2010-529274 JP-T-2015-504934 Gazette

  By the way, when manufacturing a bio-jet fuel, how to reduce the manufacturing cost is an important issue. To this end, when producing fuel from biomass resources, among the components other than the fuel obtained in the manufacturing process, those that can be used effectively can be used as much as possible to reduce waste and recover biojet fuel. It is effective to improve the rate. In this regard, the above-described conventional technology has room for improvement.

From this point of view, in the process of devising the present invention, one proposal for a biojet fuel production method and production facility as shown in FIG. 4 has been created.
As shown in FIG. 4, the production equipment includes a gasification processing section 11, a compression processing section 12, an FT synthesis processing section 13, an isomerization processing section 14, a first atmospheric distillation processing section 15, and a second atmospheric distillation processing section. 16 and a dehydrogenation processing unit 17. In the production method, the gasification step P11, the compression step P12, the FT synthesis step P13, the isomerization step P14, the first atmospheric distillation step P15, and the second atmospheric distillation step P16 are performed by these processing units 11 to 16. Perform in order.

More specifically, when the biomass resource is supplied to the gasification step P11, the biomass resource is gasified by so-called steaming. Next, the gas thus obtained is sent to the compression step P12 and compressed.
Further, the generated gas is sent to an FT synthesis step P13, where a liquid hydrocarbon is synthesized from the carbon monoxide and hydrogen in the gas using a catalytic reaction by a Fischer-Tropsch (FT) reaction as a liquid fuel synthesis step. . The synthesized liquid hydrocarbon is sent to the isomerization step P14, where isomerization is performed in which the atomic arrangement is changed and converted into another molecule.

This isomerized liquid hydrocarbon is sent to the first atmospheric distillation step P15 where it is distilled at normal pressure (atmospheric pressure or a slightly higher pressure), and the off-gas of the distilled gas component and the distillation gas are distilled off. Light oil is removed from the liquid content.
The distilled liquid hydrocarbon is sent to the second atmospheric distillation step P16, where it is distilled at normal pressure (atmospheric pressure or slightly higher pressure), separated into jet fuel and wax component, and jet fuel is separated. can get.

  The remaining components separated in the first atmospheric distillation step P15 are sent to a dehydrogenation step P17 to remove hydrogen and olefins, sent to an upstream FT synthesis step P13 and an isomerization step P14, Used for FT synthesis and isomerization.

  In this way, it is conceivable to improve the recovery rate of the bio-jet fuel by effectively utilizing the hydrogen and olefins generated in the production process by returning them upstream and recirculating them.

The individual processing steps shown in FIG. 4 are existing processing steps. If individual processing equipment is arranged in such a manner that all gas amounts are processed according to the processing order and processing proceeds in order to the next step, the size and capacity increase. This leads to an increase in installation space and cost associated with the manufacturing equipment. Therefore, with this technique, the recovery rate of the biojet fuel can be improved, but on the other hand, the equipment cost increases, which is a hindrance in suppressing the production cost.
Therefore, the bio-jet fuel manufacturing method and manufacturing equipment have been further improved, and the recovery rate of bio-jet fuel has been improved while suppressing the increase in installation space and cost related to the manufacturing equipment. There is a need to keep jet fuel manufacturing costs down.

  The present invention, when producing bio-jet fuel from biomass resources, it is possible to improve the recovery rate of bio-jet fuel while reducing the installation space related to the production equipment and reducing the installation cost, An object of the present invention is to provide a method and a facility for manufacturing jet fuel.

(1) In order to achieve the above object, the first method for producing a biojet fuel of the present invention provides a gasification step of gasifying biomass resources, and FT synthesis of the gas generated in the gasification step. An FT synthesis step, and a hydrocarbon-based material synthesized by the FT synthesis step is distilled at a high pressure higher than normal pressure to obtain an off-gas containing a hydrocarbon-based material having at least 4 or less carbon atoms and / or an inert gas. And light oil of a hydrocarbon-based material having 5 to 8 carbon atoms, a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms, and a residual component that did not become the fuel material component . A first distillation step of separating each, and, from the residual components separated in the first distillation step, a solid content and a fuel material component of a hydrocarbon material having 8 to 32 carbon atoms in a normal pressure state. Separation A second distillation step that, and a isomerization step of isomerizing the iso- paraffins said fuel feedstock component separated in about the first distillation Engineering, to obtain a jet fuel through at least the isomerization step Features.

(2) The second method for producing a bio-jet fuel according to the present invention includes a gasification step of gasifying biomass resources, an FT synthesis step of performing FT synthesis on the gas generated in the gasification step, and the FT synthesis step. The hydrocarbon-based material synthesized by the method described above is distilled under normal pressure to obtain a hydrocarbon-based material having at least 4 or less carbon atoms and / or an off-gas containing an inert gas, and a hydrocarbon-based material having 5 to 8 carbon atoms. A first distillation step of separating light oil as a material and a residual component containing a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms, and the residual component separated in the first distillation step A second distillation step of separating a solid content and a fuel material component of a hydrocarbon material having 8 to 32 carbon atoms at normal pressure, and the fuel material component separated in the second distillation step Is - and a isomerization step of isomerizing a paraffin, is characterized by obtaining a jet fuel through at least the isomerization step.

(3) The third method for producing a biojet fuel according to the present invention includes a gasification step of gasifying biomass resources, an FT synthesis step of performing FT synthesis on the gas generated in the gasification step, and the FT synthesis step. The hydrocarbon-based material synthesized by the method described above is distilled under normal pressure to obtain a hydrocarbon-based material having at least 4 or less carbon atoms and / or an off-gas containing an inert gas, and a hydrocarbon-based material having 5 to 8 carbon atoms. A first distillation step of separating light oil as a material and a residual component containing a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms, and the residual component separated in the first distillation step , A second distillation step of separating a solid content and a fuel material component of a hydrocarbon material having 8 to 32 carbon atoms at normal pressure, the first distillation step and / or the second distillation step Separated by An isomerization step of isomerizing the fuel raw material component contained in the residual component into iso-paraffin, and a second distillation for separating a solid content from the residual component treated in the isomerization step under normal pressure. A jet fuel is obtained through at least the isomerization step and the second distillation step.

( 4 ) A dehydrogenation step of extracting hydrogen from the second fuel raw material component from which the solids have been separated by the second distillation step, wherein the hydrogen extracted in the dehydrogenation step is subjected to the FT synthesis step and the isomerization step. Is preferably refluxed to at least one of the above.

( 5 ) Preferably, after the second distillation step, an alcohol dehydration step of dehydrating alcohol from the second fuel raw material component separated in the second distillation step to olefinate is provided.

( 7 ) Preferably, after the gasification step and before the FT synthesis step, a decarbonation step of removing a carbonic acid component from the gas generated by the gasification step is provided.

( 7 ) Further, the first bio-jet fuel production facility of the present invention includes a gasification processing section for gasifying biomass resources, and an FT synthesis processing section for FT-synthesizing the gas generated by the gasification processing section. Distilling the liquid hydrocarbons synthesized by the FT synthesis processing section at a high pressure higher than normal pressure to form an off-gas containing at least 4 or less hydrocarbon-based material and / or an inert gas; A light oil of a hydrocarbon material having 5 to 8 or less, a fuel material component of a hydrocarbon material having 8 to 32 carbon atoms, and a residual component which has not become the fuel material component . A solid content and a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms are separated from the residual component separated by the first distillation treatment unit and the first distillation treatment unit at normal pressure. Second steam A processing unit, wherein the isomerization unit for isomerizing the separated said fuel ingredients into iso- paraffin first distillation unit, comprising a, through at least the isomerization unit, to obtain a jet fuel Features.

( 8 ) A second bio-jet fuel production facility according to the present invention includes: a gasification processing unit for gasifying biomass resources; an FT synthesis processing unit for performing FT synthesis on the gas generated by the gasification processing unit; The liquid hydrocarbon synthesized by the FT synthesis processing section is distilled under normal pressure, and an off-gas containing at least a hydrocarbon material having 4 or less carbon atoms and / or an inert gas, and 5 to 8 carbon atoms or less. A first distillation section for separating a light oil of a hydrocarbon material and a residual component containing a fuel raw material component of a hydrocarbon material having 8 to 32 carbon atoms, respectively, and a first distillation section for separation; A second distillation section for separating a solid component and a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms at normal pressure from the residual component thus obtained, and a second distillation section. The fuel isolated Comprising a isomerization unit for isomerizing a raw material component to iso- paraffins, and through at least the isomerization unit is characterized by obtaining a jet fuel.

( 9 ) A third bio-jet fuel production facility according to the present invention includes a gasification processing unit for gasifying biomass resources, an FT synthesis processing unit for performing FT synthesis on the gas generated by the gasification processing unit, The liquid hydrocarbon synthesized by the FT synthesis processing section is distilled under normal pressure, and an off-gas containing at least a hydrocarbon material having 4 or less carbon atoms and / or an inert gas, and 5 to 8 carbon atoms. A first distillation section for separating light oil of a hydrocarbon-based material and a residual component containing a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms, and a first distillation section. An isomerization treatment section for isomerizing the fuel raw material component contained in the obtained residual component into iso-paraffin, and a solid component separated from the residual component treated in the isomerization step under normal pressure. A distillation unit, comprising a, through at least the isomerization unit and the second distillation section, is characterized by obtaining a jet fuel.

( 10 ) A dehydrogenation processing unit for extracting hydrogen from the second fuel raw material component from which the solid content has been separated by the second distillation processing unit, wherein the hydrogen extracted by the dehydrogenation processing unit is subjected to the FT synthesis processing unit and It is preferable to reflux to at least one of the isomerization treatment sections.

( 11 ) It is preferable that an alcohol dehydration unit for dehydrating alcohol from the second fuel raw material component separated by the second distillation unit is provided after the second distillation unit.

( 12 ) It is preferable that a decarboxylation unit for removing a carbonic acid component from the gas generated by the gasification unit is provided between the gasification unit and the FT synthesis unit .

According to the present invention, after the fuel material component is separated by the first distillation step or the second distillation step, isomerization is performed in the isomerization step, so that unnecessary components are removed in advance during isomerization, It can promote the isomerization reaction. Thereby, the recovery rate of the bio-jet fuel can be improved.
In addition, since only the fuel raw material component is supplied to the isomerization step, space saving of the isomerization apparatus can be achieved. As a result, it is possible to save space in the biojet fuel production facility.

Also, removed hydrogen by dehydrogenation step from the residual components other than the fuel feedstock component separated by the second distillation step, lever use in at least recirculated to one of the FT synthesis process or isomerization step, bio jet The fuel recovery rate can be improved.
Furthermore, if high-pressure distillation is performed in the first distillation step, the size of the apparatus can be reduced, and it also contributes to the promotion of isomerization.
Also, if the residual component separated in the second distillation step is alcohol-dehydrated and sent to the dehydrogenation step, oil and water can be separated and dehydrogenation can be promoted, and the recovery rate of biojet fuel can be improved. be able to.
Furthermore, if the carbon dioxide component is removed from the gas generated in the gasification step and then sent to the FT synthesis step, in the steps after the FT synthesis step, unnecessary components that hinder the treatment will not be sent. In addition, processing efficiency can be improved.

It is a block diagram showing a manufacturing method and manufacturing equipment of a bio jet fuel concerning a 1st embodiment. It is a block diagram showing the manufacturing method and manufacturing equipment of the bio jet fuel concerning a 2nd embodiment. It is a block diagram showing a manufacturing method and manufacturing equipment of a bio jet fuel concerning a third embodiment. 1 is a block diagram illustrating a method and a facility for producing a bio-jet fuel created in the process of devising the present invention.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings. Note that the embodiments described below are merely examples, and there is no intention to exclude various modifications and application of technology not explicitly described in the following embodiments. Each configuration of the following embodiments can be variously modified and implemented without departing from the spirit thereof, and can be selectively used as needed, or can be appropriately combined.

[First Embodiment]
The first embodiment will be described with reference to FIG.
FIG. 1 is a block diagram illustrating a method and a facility for manufacturing a biojet fuel according to the present embodiment. Each block in FIG. 1 indicates each processing unit of the manufacturing facility and each step of the manufacturing method. .

  As shown in FIG. 1, the biojet fuel production equipment according to the present embodiment includes a gasification processing section 1, a compression processing section 9, a decarboxylation processing section 2, an FT synthesis processing section 3, a first distillation processing section 4, It has an isomerization treatment section 5, a second distillation treatment section 6, an alcohol dehydration treatment section 7, and a dehydrogenation treatment section 8. In the method for producing a biojet fuel according to the present embodiment, the gasification step P1, the compression step P9, the decarboxylation step P2, the FT synthesis step P3, the first distillation step are performed by the processing units 1 to 5 and 9 among these. P4 and isomerization step P5 are performed in this order to produce a biojet fuel.

  The second distillation step P6, the alcohol dehydration step P7, and the dehydrogenation step P8 are performed using the second distillation processing section 6, the alcohol dehydration processing section 7, and the dehydrogenation processing section 8 in this order. Hydrogen is refluxed to both or one of the FT synthesis step P3 and the isomerization step P5.

Hereinafter, each step will be further described.
In the gasification process P1, in a gasification furnace of the gasification processing unit 1, supplied biomass resources (hereinafter, also simply referred to as biomass) such as wood (firewood, charcoal, chips, pellets, etc.) are pulverized and so-called steamed. (Partial oxidation reaction, etc.) and gasify.
Note that gasification refers to the generation of a combustible mixed gas containing carbon monoxide (CO) and hydrogen (H ₂ ), a hydrocarbon-based gas (C _n H _m ), and the like from biomass by a device such as a gasification reactor. It is to make it.

  Next, in a compression step P9 before FT synthesis, the compression processing unit 9 pressurizes and compresses the gas obtained in the gasification step P1 before performing the decarbonation gas step P2. In the present embodiment, the compression in the compression step P9 is performed, for example, to about 1 MPa to promote the synthesis in the subsequent FT synthesis step P3.

  Next, in the decarbonation step P2, in the decarbonation processing section 2, carbon dioxide gas is removed from the gas compressed in the compression step P12 after the gasification step P1. Carbon dioxide gas is an inert gas that does not contribute to the chemical reaction in the FT synthesis step P3. By removing the carbon dioxide gas, the partial pressure of the gas required for the chemical reaction is improved, and the reaction efficiency in the FT synthesis step P3 can be improved. An amine method or the like can be used for the removal. The decarbonation step P2 is preferably performed, but may be omitted.

Next, in the FT synthesis step P3, a liquid hydrocarbon is synthesized from the carbon monoxide and the hydrogen in the gas from which the carbon dioxide gas has been removed in the decarbonation step P2 using a catalytic reaction by using the Fischer-Tropsch method. Growing (C ₈ H ₁₈ -C ₁₆ H ₃₄ ) from carbon monoxide (CO) and hydrogen (H ₂ ) in a combustible mixed gas as a raw material through chain growth of olefins (C _n H _2n ) to produce hydrogen ( the paraffin reaction takes in H _2), generates a n- paraffins _{(n-C n H 2n +} 2).

The first distillation processing unit 4 is a high-pressure distillation processing unit that performs distillation (high-pressure distillation) at a high pressure (about 3 MPa, which is about 1 MPa, which is about three times the conventional value). Therefore, in the first distillation step P4 performed in the first distillation processing section 4, the liquid hydrocarbon synthesized in the FT synthesis step P3 is fractionally distilled by high-pressure distillation to separate and remove off-gas and light oil.
The off-gas is a gas mainly composed of a hydrocarbon gas having a low boiling point such as methane, ethane, propane or butane, or an inert gas which does not contribute to the reaction such as carbon dioxide.

This high pressure distillation, pumps, etc., for example, 1 MPa → pressurized to 3 MPa, by fractional _{distillation,} separating off C 8 _{H m} following components lighter the _{(C 5 H m ~C 8 H} m) as a light oil. Light oil separated and removed is used as fuel for boilers and the like.
C ₈ H _m or more heavy fuel component of the fuel material component comprising a _{(C 8 H 18 ~C 16 H} 34) and intermediate fractionation to fit the jet fuel specifications supplied to the isomerization step P5 the following steps I do.
Further, the residual components that have not become the fuel raw material components are sent to the second distillation section 6, where solid components are separated.

Therefore, according to the high-pressure distillation, the size of the distillation section (distillation column) can be reduced as compared with the distillation section (distillation column) of the atmospheric distillation having the same fractional distillation processing capacity.
Further, since the number of processing stages provided for each distillation processing unit can be reduced by making the distillation processing unit (distillation tower) smaller by setting the pressure to be higher, the number of processing stages can be set larger than that of the distillation processing unit at normal pressure. For this reason, it is possible to perform finer fractional distillation, and it is possible to further separate and extract only a fuel raw material component usable for jet fuel as an intermediate fraction by this distillation.
Therefore, the components supplied to the next isomerization step P5 are limited to increase the efficiency of the jet fuel production step and to reduce the capacity and size of the reactor of the isomerization treatment section 5 in the isomerization step P5. be able to.

In the isomerization step P5, the fuel material component taken out by the high-pressure distillation in the first distillation step P4 is isomerized into a light oil component to be a jet fuel. That is, the n-paraffin generated by the FT reaction in the FT synthesis step P3 is iso-paraffinized so as to meet the jet fuel standard (see the following formula).
・ Iso-paraffinization of n-paraffin n-C ₂ H ₆ → iso-C ₂ H _{6
n-C 3 H 6 → iso} -C 3 H 8
Incidentally, light oil component as a jet fuel are roughly classified into kerosene-based and wide-cut system, kerosene _{(C 10 H m ~C 15 H} m) and naphtha _{(C 6 H m ~C 9 H} m) is mainly Component.

In the first distillation step P4, the offgas, the light oil, and the fuel material component to be sent to the isomerization step P5 are separated by fractional distillation, but the remaining components other than these are separated from the first distillation processing section 4 by the second distillation section 4. It is sent to the processing unit 6.
The second distillation section 6 is an atmospheric distillation section that performs distillation (atmospheric distillation) under normal pressure (atmospheric pressure or slightly higher pressure). In the second distillation step P6 performed in the second distillation section 6, the residual component from the first distillation step P4 is subjected to atmospheric distillation to obtain a wax component (solid component) which is heavier than the fuel material component. Is separated and removed, and a second residual component that can be reused in the next step (alcohol dehydration step P7) is taken out.

In the alcohol dehydration step P7, the components remaining after the wax component (solid component) is separated and removed in the second distillation step P6 are subjected to alcohol dehydration to separate oil and water. That is, from the residual components obtained by the high-pressure distillation in the first distillation step P4, the fuel material components of C ₈ H _{10 to} C ₁₆ H ₃₄ and the wax component (solid component) are subjected to the atmospheric distillation in the second distillation process P6. In the dehydrogenation treatment of the removed second residual component, an alcohol dehydration treatment (pure alcohol is converted into an olefin with an acid catalyst) is performed, and impurities are processed into an olefin-containing oil. The recovery rate of hydrogen in the dehydrogenation treatment is improved. In this alcohol dehydration treatment, impurities (alcohol) are dehydrated with an acid catalyst, and olefination is performed as in the following formula.
C ₈ H ₁₈ O → H ₂ O + C ₈ H ₁₆
C ₉ H ₂₀ O → H ₂ O + C ₉ H ₁₈

Then, the water is separated, and only the oil is sent to the dehydrogenation step P8. When hydrogen is extracted from the oil, olefin is further extracted (see the following formula).
C ₈ H ₁₈ → H ₂ + C ₈ H ₁₆
C ₉ H ₂₀ → H ₂ + C ₉ H ₁₈
C ₁₆ H ₃₄ → H ₂ + C ₁₆ H ₃₂
Then, the extracted hydrogen is refluxed to both or one of the FT synthesis step P3 and the isomerization step P5.
Since the extracted olefin contributes to the improvement of the reaction efficiency of the FT synthesis, it is recycled to the FT synthesis step P3 to increase the jet fuel recovery rate.
In the dehydrogenation step P8, in the dehydrogenation treatment after the alcohol dehydration treatment, steam is added to supply energy for the endothermic reaction to dehydrogenate to obtain the necessary olefin. The oil component in the second residual component is defined as olefin. Since hydrogen is produced at this time, a larger amount of hydrogen is recovered than in the prior art, and the hydrogen is used as a raw material for the isomerization reaction, so that the recovery rate of the jet fuel can be improved.

Since the method and the equipment for manufacturing a biojet fuel according to the first embodiment are configured as described above, the following operations and effects can be obtained.
After the fuel necessary for the treatment step is separated and taken out in the isomerization step P5 in the first distillation step P4, the fuel is isomerized in the isomerization step P5. It has been removed and can promote the most important isomerization reaction in the biojet fuel production process. Thereby, the recovery rate of the biojet fuel can be improved, and the capacity and size of the isomerization processing section 5 can be reduced.
In the first distillation step P4, the high-pressure distillation process is performed about three times as much as the conventional one, so that the space in the first distillation step can be saved. Further, only the liquid fuel component usable for the jet fuel is sent to the isomerization step P5, so that the space in the isomerization processing section can be saved.

  Since the first distillation step P4 is a high-pressure distillation step in which high-pressure distillation is performed, the materials (gas and liquid components) synthesized in the FT synthesis step P3 can be compressed and processed in a reduced volume, so that the apparatus can be used. Compactness can be achieved. In addition, since high-pressure distillation enables finer fractional distillation, and a fuel raw material component usable for jet fuel can be taken out as an intermediate fraction, this fuel raw material component is directly sent to the isomerization step P5 to be subjected to the isomerization treatment. Can be performed. Since high-pressure distillation enables more appropriate fractional distillation, it also contributes to the promotion of isomerization.

  Further, solid components (wax components) are removed from the residual components separated and extracted in the second distillation step P6, impurities (alcohols) as liquid components are olefinated by a dehydration reaction, and then hydrogen is taken out in a dehydrogenation step. Since it is used by refluxing in the FT synthesis step P3 and the isomerization step P5, the recovery rate of the biojet fuel can be improved.

  Further, the residual component separated in the second distillation step P6 is alcohol-dehydrated in the alcohol dehydration step P7 and sent to the dehydrogenation step P8 to remove water, and oil / water is separated and extracted to promote dehydrogenation to produce olefin. , The FT synthesis step P3, and the recovery rate of the biojet fuel can be improved.

  Further, since the decarbonation step P2 is provided between the gasification step P1 and the FT synthesis step P3, the carbon dioxide component is removed from the gas generated in the gasification step P1 and then sent to the FT synthesis step P3. By doing so, in the steps after the FT synthesis step P3, unnecessary components not contributing to the processing are prevented from being sent, and the processing efficiency can be improved by increasing the partial pressure of the reaction components.

By performing the high-pressure distillation process P4 before the isomerization process P5 as the process step sequence, the efficiency of the isomerization process step P5 can be increased. According to the high-pressure distillation process P5, the efficiency of the jet fuel production process in the next foreign matter conversion process P5 can be improved, and the capacity and size of the isomerization treatment section 5 in the isomerization process P5 can be reduced.
Further, by increasing the pressure, the high-pressure distillation section 4 and the isomerization section 5 can be reduced in capacity and space can be saved, and the reaction efficiency of the FT synthesis step P3 can be improved to improve the biojet fuel recovery rate. Can be improved.

[Second embodiment]
A second embodiment will be described with reference to FIG.
FIG. 2 is a block diagram illustrating a method and a facility for manufacturing a biojet fuel according to the present embodiment. Each block in FIG. 2 indicates each processing unit of the manufacturing facility and each step of the manufacturing method. . In FIG. 2, the same reference numerals as those in FIG. 1 denote the same components, and thus the description thereof will be omitted or simplified.

  As shown in FIG. 1, the bio-jet fuel manufacturing facility according to the present embodiment includes a gasification processing section 1, a compression processing section 9, a decarboxylation processing section 2, an FT synthesis processing section 3, a first distillation processing section 4A, It has an isomerization treatment section 5, a second distillation treatment section 6, an alcohol dehydration treatment section 7, and a dehydrogenation treatment section 8. In the method for producing a biojet fuel according to the present embodiment, the gasification step P1, the compression step P9, the decarboxylation step P2, the FT synthesis step P3, the first distillation step are performed by the processing units 1 to 6, 9 among these. P4A, the second distillation step 6, and the isomerization step P5 are performed in this order to produce a biojet fuel.

  Further, similarly to the first embodiment, the second distillation step P6, the alcohol dehydration step P7, and the dehydrogenation step P8 are performed using the second distillation processing section 6, the alcohol dehydration processing section 7, and the dehydrogenation processing section 8. The hydrogen obtained in this order is refluxed to both or one of the FT synthesis step P3 and the isomerization step P5.

In the present embodiment, the first distillation processing unit 4A is a normal pressure distillation processing unit that performs distillation (normal pressure distillation) under normal pressure (atmospheric pressure or slightly higher pressure), and is performed by FT synthesis. Fractional distillation is performed from the synthesized liquid hydrocarbons to offgas, light oil, and other residual components including liquid fuel components usable for jet fuel. In addition, in order to avoid upsizing, in a normal-pressure distillation processing part, it cannot perform fine fractional distillation by increasing the number of processing stages like the high-pressure distillation processing part described in the first embodiment.
For this reason, after distillation in the first distillation processing section 4A, other remaining components are further distilled in the second distillation processing section 6, which performs distillation under normal pressure, to obtain only the fuel material components usable for jet fuel. Can be separated and taken out. The isomerization processing unit 5 is disposed downstream of the second distillation processing unit 6, and only the liquid fuel component usable for the extracted jet fuel is sent to the isomerization processing unit 5.

Therefore, in the present embodiment, in the first distillation step P4A, the liquid hydrocarbons synthesized in the FT synthesis step P3 are fractionally distilled to remove off-gas and light oil. Then, the residual component is fractionally distilled in the second distillation step P6 to separate and remove the wax component and the reusable component, and further take out a fuel raw material component usable for jet fuel as an intermediate fraction.
In the isomerization step P5, the fuel raw material component extracted by the distillation in the second distillation step P6 is isomerized into a light oil component to be a jet fuel. In addition, similarly to the first embodiment, the reusable components are processed in the order of the atmospheric distillation unit 6, the alcohol dehydration unit 7, and the dehydrogenation unit 8, and are recycled to the FT synthesis step P3.

  Since the biojet fuel manufacturing method and the manufacturing equipment according to the second embodiment are configured as described above, the space saving of the distillation process unit accompanying the high pressure when performing the high pressure distillation in the first distillation process P4 is achieved. Although no effect is obtained, the impurity (alcohol) is hardly generated again in the second distillation step P6. Therefore, in consideration of this point, the alcohol dehydration step P7 becomes unnecessary, and there is an effect that the steps and equipment can be simplified. . Otherwise, the same operation and effect as the first embodiment can be obtained.

[Third embodiment]
A third embodiment will be described with reference to FIG.
FIG. 3 is a block diagram showing a method and a facility for manufacturing a biojet fuel according to the present embodiment. Each block in FIG. 3 shows each processing unit of the manufacturing facility and each step of the manufacturing method. . Note that, in FIG. 3, the same reference numerals as those in FIGS. 1 and 2 denote the same components, and therefore, the description will be simplified.

  As shown in FIG. 3, the bio-jet fuel manufacturing facility according to the present embodiment includes a gasification processing unit 1, a compression processing unit 9, a decarboxylation processing unit 2, and an FT synthesis processing unit 3 as in the second embodiment. , A first distillation section 4A, an isomerization section 5, a second distillation section 6, an alcohol dehydration section 7, and a dehydrogenation section 8. In the method for producing a biojet fuel according to the present embodiment, the gasification step P1, the compression step P9, the decarboxylation step P2, the FT synthesis step P3, the first distillation step are performed by the processing units 1 to 6, 9 among these. P4A, isomerization step P5, and second distillation step P6 are performed in this order to produce a biojet fuel.

  Similarly to the first and second embodiments, the second distillation step P6, the alcohol dehydration step P7, and the dehydrogenation step are performed using the second distillation section 6, the alcohol dehydration section 7, and the dehydrogenation section 8. The hydrogen obtained by performing P8 in this order is refluxed to both or one of the FT synthesis step P3 and the isomerization step P5.

  This embodiment has the same processing units and steps as the second embodiment, but performs the processing in the order of the first distillation step P4A, the isomerization step P5, and the second distillation step P6. That is, in the first distillation step P4A, the residual component from which the off-gas and light oil have been removed is isomerized in the isomerization step P5 into a light oil component to be a jet fuel.

  Note that the residual components from the first distillation step P4A not only include fuel raw material components that can be used for jet fuel but also components that become wax components. Therefore, in the isomerization step P5, a part of the residual component is isomerized into a light oil component to be a jet fuel. Then, in the second distillation step P6, the wax component is separated and removed, and only the fuel material component usable for the jet fuel is separated and taken out.

  Since the method and the equipment for producing a biojet fuel according to the third embodiment are configured as described above, the effect of performing high-pressure distillation in the first distillation step P4 cannot be obtained, and the isomerization step P5 Although the efficiency of isomerization decreases, substantially the same operation and effect as in the first embodiment can be obtained except for these.

[Others]
As described above, the embodiments of the present invention have been described, but the present invention can be implemented by appropriately changing or combining the embodiments without departing from the spirit thereof.
For example, in each of the above-described embodiments, the decarboxylation step P2 and the decarboxylation processing section 2 are provided, and the effect of improving the processing efficiency is obtained, but this may be omitted. In each of the above embodiments, the alcohol dehydration step P7 and the alcohol dehydration processing unit 7 are provided, and the effect of improving the recovery rate of the biojet fuel is obtained. However, this may be omitted. Furthermore, in each of the above embodiments, the dehydrogenation step P8 and the dehydrogenation processing section 8 are provided to promote dehydrogenation, but this can be omitted.

1,11 Gasification processing section 2 Decarbonation processing section 3,13 FT synthesis processing section 4 First distillation processing section (high pressure distillation processing section)
4A, 15 1st distillation section (normal pressure distillation section)
5,14 Isomerization section 6,16 Second distillation section (Normal pressure distillation section)
7 Alcohol dehydration processing section 8, 17 Dehydrogenation processing section 9, 12 Compression processing section P1, P11 Gasification step P2 Decarbonation step P3, P13 FT synthesis step P4 First distillation step (high pressure distillation step)
P4A, P15 First distillation step (normal pressure distillation step)
P5, P14 Isomerization process P6, P16 Second distillation process (normal pressure distillation process)
P7 Alcohol dehydration process P8, P17 Dehydrogenation process P9, P12 Compression process

Claims (12)

A gasification process for gasifying biomass resources;
An FT synthesis step of FT synthesizing the gas generated by the gasification step;
The hydrocarbon-based material synthesized in the FT synthesis step is distilled at a high pressure higher than normal pressure, and an off-gas containing at least a hydrocarbon-based material having 4 or less carbon atoms and / or an inert gas; A first oil for separating light oil of a hydrocarbon material having 5 or more and 8 or less, a fuel raw material component of a hydrocarbon material having 8 or more and 32 or less carbon atoms, and a residual component which has not become the fuel raw material component . A distillation step;
A second distillation step of separating a solid content and a fuel material component of a hydrocarbon material having 8 to 32 carbon atoms from the residual components separated in the first distillation step under normal pressure;
And a isomerization step of isomerizing the separated said fuel feedstock components iso- paraffins in about the first distillation Engineering,
A method for producing a bio-jet fuel, wherein a jet fuel is obtained through at least the isomerization step. A gasification process for gasifying biomass resources;
An FT synthesis step of FT synthesizing the gas generated by the gasification step;
The hydrocarbon-based material synthesized by the FT synthesis step is distilled under normal pressure, and the hydrocarbon-based material having at least 4 or less carbon atoms and / or the off-gas containing an inert gas, and the carbon atom having 5 to 8 carbon atoms are included. A first distillation step of separating light oil of a hydrocarbon-based material and residual components including a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms, respectively;
A second distillation step of separating a solid content and a fuel material component of a hydrocarbon material having 8 to 32 carbon atoms from the residual components separated in the first distillation step under normal pressure;
And a isomerization step of isomerizing the separated the fuel ingredients into iso- paraffin before Symbol second distillation step,
A method for producing a bio-jet fuel, wherein a jet fuel is obtained through at least the isomerization step. A gasification process for gasifying biomass resources;
An FT synthesis step of FT synthesizing the gas generated by the gasification step;
The hydrocarbon-based material synthesized in the FT synthesis step is distilled under normal pressure, and the hydrocarbon-based material having at least 4 or less carbon atoms and / or an off-gas containing an inert gas; A first distillation step of separating light oil of a hydrocarbon-based material and residual components including a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms, respectively;
An isomerization step of isomerizing the fuel raw material component contained in the residual component separated in the first distillation step into iso-paraffin;
A second distillation step of separating solids from the residual components treated in the isomerization step under normal pressure .
A method for producing a bio-jet fuel, wherein a jet fuel is obtained through at least the isomerization step and the second distillation step . A dehydrogenation step of extracting hydrogen from the second fuel raw material component from which the solid content has been separated by the second distillation step,
The hydrogen extracted in the dehydrogenation step is refluxed to at least one of the FT synthesis step and the isomerization step, the biojet fuel according to any one of claims 1 to 3 , Production method. 5. The method according to claim 1, further comprising, after the second distillation step, an alcohol dehydration step of dehydrating an alcohol from the second fuel raw material component separated in the second distillation step to olefinate the alcohol. 6 . A method for producing a biojet fuel according to any one of the preceding claims. And before the FT synthesis step after the gasification step, characterized in that it comprises a decarboxylation process for removing carbon dioxide component from the generated gas by the gasification process of claim 1-5 A method for producing a biojet fuel according to any one of the preceding claims. A gasification processing unit for gasifying biomass resources,
An FT synthesis processing unit that performs FT synthesis on the gas generated by the gasification processing unit;
The liquid hydrocarbon synthesized by the FT synthesis processing section is distilled at a high pressure higher than normal pressure, and an off gas containing at least a hydrocarbon material having 4 or less carbon atoms and / or an inert gas; A first oil for separating light oil of a hydrocarbon material having 5 or more and 8 or less, a fuel raw material component of a hydrocarbon material having 8 or more and 32 or less carbon atoms, and a residual component which has not become the fuel raw material component . A distillation section,
A second distillation section for separating a solid component and a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms from the residual components separated by the first distillation section at normal pressure; ,
An isomerization treatment unit that isomerizes the fuel raw material component separated in the first distillation treatment unit into iso-paraffin ,
A bio-jet fuel production facility, wherein a jet fuel is obtained through at least the isomerization treatment section. A gasification processing unit for gasifying biomass resources,
An FT synthesis processing unit that performs FT synthesis on the gas generated by the gasification processing unit;
The liquid hydrocarbon synthesized by the FT synthesis processing section is distilled at normal pressure to obtain an off-gas containing at least a hydrocarbon-based material having 4 or less carbon atoms and / or an inert gas, and 5 to 8 carbon atoms. A first distillation section for separating a light oil of a hydrocarbon-based material and a residual component containing a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms,
A second distillation section for separating a solid component and a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms from the residual components separated by the first distillation section at normal pressure; ,
And a isomerization unit for isomerizing the iso- paraffins separated the fuel feedstock components before Symbol second distillation unit,
A bio-jet fuel production facility, wherein a jet fuel is obtained through at least the isomerization treatment section. A gasification processing unit for gasifying biomass resources,
An FT synthesis processing unit that performs FT synthesis on the gas generated by the gasification processing unit;
The liquid hydrocarbon synthesized by the FT synthesis processing section is distilled at normal pressure to obtain an off-gas containing at least a hydrocarbon-based material having 4 or less carbon atoms and / or an inert gas, and 5 to 8 carbon atoms. A first distillation section for separating a light oil of a hydrocarbon-based material and a residual component including a fuel material component of a hydrocarbon-based material having 8 to 32 carbon atoms,
An isomerization treatment unit that isomerizes the fuel raw material component contained in the residual component separated in the first distillation treatment unit into iso-paraffin;
A second distillation section for separating solids from the residual components treated in the isomerization step under normal pressure ;
A facility for producing a bio-jet fuel, wherein a jet fuel is obtained through at least the isomerization treatment section and the second distillation treatment section . A dehydrogenation unit for extracting hydrogen from the second fuel raw material component from which the solids have been separated by the second distillation unit;
The biomass according to any one of claims 7 to 9 , wherein the hydrogen extracted by the dehydrogenation unit is refluxed to at least one of the FT synthesis unit and the isomerization unit. Jet fuel production equipment. The method according to any one of claims 7 to 10 , further comprising, after the second distillation section, an alcohol dehydration section for dehydrating alcohol from the second fuel raw material component separated by the second distillation section. 2. A facility for producing a biojet fuel according to claim 1. Between the said gas treatment unit FT synthesis processing unit, characterized in that it comprises a decarboxylation process unit for removing carbon dioxide component from a gas produced by the gasification unit, according to claim 7 12. The facility for producing a bio-jet fuel according to any one of items 11 to 11 .

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