JP4644831B2 - Liquid fuel production equipment from biomass - Google Patents

Description

  The present invention relates to an apparatus for producing liquid fuel by gasifying biomass. More specifically, biomass such as woody biomass such as unused trees, thinned wood, residual lumber, driftwood, pruned wood, building waste, sewage sludge, chicken manure, cow dung, waste biomass such as RDF, weeds, grass The present invention relates to an apparatus for producing liquid fuel from biomass for efficiently gasifying and liquefying herbaceous biomass such as sugarcane as a raw material.

  Liquid fuel target biomass generally refers to a living organism that can be used as an energy source, and is one of the renewable energies generated using solar energy. Biomass is the only renewable organic matter that can be converted to energy.

  Currently, more than 30% of the primary energy we use is oil, and more than 40% is liquid fuel for transportation. Therefore, it is very useful to produce liquid fuel from renewable biomass. Production of liquid fuel from biomass can be realized by a combination of several techniques and has been conventionally performed. Among them, biomass is gasified, CO and hydrogen are obtained, and liquid fuel is produced by a catalytic reaction, and this technique is attracting attention. Next, a conventional technique for producing a liquid fuel will be described.

Biomass comes in a wide variety of forms such as woody, waste and herbaceous. On the other hand, CO and hydrogen are required in the liquid fuel production process. Here, the process of producing liquid fuel from biomass via gasification may be simpler than other processes in that CO and hydrogen can be obtained regardless of the type of biomass.
When biomass is gasified, the gas yield and the amount of tar produced depend greatly on the gasifier type, gasifying agent, and reaction conditions.

  Gasifier types are broadly divided into fixed beds, fluidized beds, and spouted beds. The fixed floor has a simple structure, low equipment costs, and is suitable for small scale. Comparing the downdraft and the updraft, the downdraft produces less tar than the updraft. The fluidized bed is suitable for the medium scale, but in order to keep the bed in the gasification furnace fluidized, it is necessary to supply a process flow gas corresponding to at least three times the minimum fluidization speed, resulting in gasification. The gas contains nitrogen at a high concentration.

  In addition, the amount of tar produced is high. The spouted bed does not depend on the scale and has the advantage that the amount of tar generated is low, but it requires the power to pulverize the gasification raw material, and the process flow gas that floats the powder in the gasification furnace is necessary. Therefore, as with the fluidized bed, the gasification gas contains a high concentration of nitrogen.

  Typical gasifying agents include air, carbon dioxide, and water vapor. When air is used, there is an advantage that external heat is unnecessary, the gasification rate is high, and the gas yield is high, but nitrogen is mixed in the gasification gas. Also, when oxygen is used, there are similar advantages, but the cost of separating nitrogen from air is high.

  When carbon dioxide is used, nitrogen is not mixed in the gasification gas, and when the liquid fuel production process continues in the latter stage, there is an advantage that the gasification gas cooling process is unnecessary, but external heat is required, and the reaction rate Is slow. Furthermore, when the liquid fuel production process continues in the subsequent stage, the yield of liquid fuel is low because the hydrogen / CO ratio is low. In the case of using water vapor, a gas with a high hydrogen / CO ratio can be obtained with a low mixing of nitrogen as a process flow gas in the gasification gas. However, external heat is required, and the use of excess water vapor increases the water vapor fraction in the gasification gas, thus requiring a cooling step for removal as water.

  The gas purification process can be broadly divided into a wet method in which impurities are dissolved in a solvent, particularly water, and a dry method that does not use water. Generally, a wet method is used. However, the initial cost and the running cost of the entire process are increased from the viewpoint of the huge processing equipment and the cost of wastewater treatment.

  Regarding the dry method, a method of removing tar and particulate matter contained in the gasification gas at a pressure of atmospheric pressure and a temperature of 130 ° C. or less has been reported (for example, see Non-Patent Documents 1 and 2). This is a method of collecting dust using a cyclone or a method using an adsorbent such as sand or activated carbon. Since both the wet method and the dry method have a purification gas temperature of 130 ° C. or lower, a process for reheating is required when the subsequent process requires a reaction temperature higher than the purification gas temperature. It becomes.

  In addition, since conventional gas purification methods are performed near atmospheric pressure, it is necessary to input power to compress the gas when the subsequent process is operated under pressurized conditions such as liquid fuel production and membrane separation. Become. Accordingly, a compressor is required, resulting in an increase in the initial cost of the process. In addition, some have a heat exchanger that recovers the heat of the gasified gas and the purified gas, but the initial cost for installing the heat exchanger increases.

  In the process for producing liquid fuel from biomass via gasification, an apparatus for producing methanol after gasifying organic waste and purifying the gas has also been proposed. When liquid fuel is produced from CO and hydrogen, the equilibrium yield is preferably under pressurized conditions of about several megapascals. However, the pressure conditions of the conventional technology are not limited, and it is difficult to obtain high methanol under normal pressure conditions. In addition, some have a heat exchanger that recovers the heat of the gasified gas and the gas after purification, but the initial cost for installing the heat exchanger increases. Furthermore, the power to pressurize the purified gas results in an increase in energy input to the process. Therefore, the initial cost also increases due to the booster device installation.

  Next, a specific conventional example related to the present invention will be described. In technologies for burning and gasifying biomass, for example, a partial combustion gas having oxygen gas reacts with biomass, and after the biomass is partially burned, it is reacted with a gasification gas having water vapor to gasify the biomass. The technique to make is known (for example, refer patent document 1).

  In addition, a technique is also disclosed in which, when burning biomass, a combustion exothermic reaction of biomass and an endothermic reaction of biomass are separately performed in a combustion space and a gasification space (for example, patents). Reference 2).

  As a technique for compressing and purifying, for example, there is a technique that is applied to a pressure swing adsorption purifying apparatus, and purifies a part of the gas by purifying the remainder of the pressurized gas and the membrane separation and purifying apparatus and then introducing the gas pressurized by the compressor. It is known (see, for example, Patent Document 3).

  In the technology for producing methanol, the gas obtained by gasifying biomass is cooled to synthesize methanol, and heat is exchanged with water supplied from the outside by heat exchange means to generate high-temperature steam, which is purified. A technique for producing methanol fuel is known (see, for example, Patent Document 4).

  In addition, when biomass is gasified, water is electrolyzed with water electrolysis equipment using the power generated by the solar power generation facility or wind power generation facility, and the amount of hydrogen in the generated gas is reduced by 2 to the amount of carbon monoxide. A technique for producing methanol by supplying hydrogen gas so as to be twice or more is known (see, for example, Patent Document 5).

  Furthermore, the gas containing hydrogen and carbon monoxide obtained by biomass gasification is stored in a gas tank, pressurized to 0.5-5.0 MPa with a pressure pump, and then produced in a methanol synthesis unit filled with a catalyst. There is also known a technique of cooling methanol gas to obtain methanol (see, for example, Patent Document 6).

  As a technology configured to move a series of devices that gasify biomass, for example, a mobile vehicle equipped with components for the process of temporarily storing pulverized biomass, and a process associated with the production of purified gas that gasifies biomass What was comprised as a mobile vehicle carrying a component apparatus is known (for example, refer patent document 7).

  Further, as a technology for burning char, clay is used as a catalyst for gasification. However, a technology is disclosed in which char is burned to supplementally heat biomass to promote gasification, and carbon monoxide and A technique is also disclosed in which methanol is produced by performing a methanol synthesis reaction after components of a biomass gas containing hydrogen are adjusted by a shift reactor as necessary to remove carbon dioxide (see, for example, Patent Document 8).

JP 2002-235091 A JP 2002-88379 A JP-A-6-210120 JP 2001-240878 A JP 2002-193858 A Japanese Patent Laid-Open No. 2005-13239 JP-A-9-176664 JP 2003-41268 A Hasler, P., and Nussbaumer, T., Biomass & Bioenergy, 16, 385 (1999) Devi, L., Ptasinski, K. J., and Janssen, F. J. J. G., Biomass & Bioenergy, 24, 125 (2003)

Since the step of compressing the gasification gas and the purified gas leads to an increase in the initial cost of the process and the input energy, it is necessary to omit the compression process.
In order to obtain CO and hydrogen in the gasification step, water vapor is usually used as a gasifying agent, but it is necessary to limit the amount of water vapor input so that the cooling / water separation step, which causes an increase in initial cost, is unnecessary.

  When liquid fuel is produced from CO and hydrogen, as described above, the equilibrium yield is preferably under a pressurized condition of about several megapascals. However, for example, in the case of the aforementioned patent document, the pressure condition is not limited, and a high methanol yield cannot be obtained under the normal pressure condition. As described above, in the conventional technique, there are conditions that can be applied to each technique, but it is not necessarily performed efficiently in the entire process of gasifying biomass to produce liquid fuel.

  In a liquid fuel production process, since a high synthesis gas (CO + hydrogen) partial pressure is desirable, a process is required in which a purified gas having a low or no nitrogen, oxygen, carbon dioxide, or water vapor concentration is obtained. Furthermore, the process must be a process for efficiently producing liquid fuel by gasifying biomass with as little waste as possible. The present invention has been made in order to overcome the above-mentioned problems against the background of such a situation.

  That is, the object of the present invention is necessary for gasification, which is a factor that increases the input energy without using a gas compression device and a heat exchanger, which are factors that increase the initial cost of the liquid fuel production process via gasification. A device for producing liquid fuel from biomass in which the concentration of nitrogen, oxygen, water vapor, carbon dioxide, etc. is reduced in the liquid fuel synthesis process, which reduces the amount of heat and reduces the gas compression power and liquid fuel yield There is.

  Another object of the present invention is to circulate unreacted materials again in the same apparatus and efficiently reuse them without waste in order to streamline a series of steps for gasifying biomass and producing liquid fuel. The object is to provide an apparatus for producing liquid fuel from biomass.

  Thus, as a result of extensive research on the background of such problems, the present inventor does not include the pressurization step of gasification gas and purified gas, and does not require compression power and related equipment and heat exchanger. And found a simple process that can achieve high liquid fuel yield while reducing the initial cost and input energy of the plant using only a minimum amount of nitrogen, and completed the present invention based on this knowledge. It is. Next, specific means will be described.

The apparatus for producing liquid fuel from biomass according to the first aspect of the present invention includes a gasification unit that holds a certain amount of biomass and heats it with a heating body and gasifies it in a pressure range of 1 to 5 MPa, and monoxide generated by the gasification unit A gas purification unit for removing at least one substance selected from particulate matter, tar, sulfur compounds and nitrogen compounds from biomass gas, which is a mixed gas of carbon and hydrogen, and purifying the biomass gas; A liquid fuel production unit that produces a biomass liquid fuel stock solution that is a hydrocarbon by liquefying the purified biomass gas by a catalytic reaction , and a gas-liquid separation unit that separates the biomass liquid fuel stock solution into biomass liquid fuel, water, and light hydrocarbons And a decompression recovery unit that recovers the biomass liquid fuel separated by the gas-liquid separation unit by reducing the pressure, and is not gasified by the gasification unit The reaction was allowed to burn, and the combustion section for supplying generated heat to the gasification unit, composed, keeping from the gasification constant pressure until the liquified, thereby boosting the biomass gas or the biomass purified gas It is characterized by not having a pressurizing device.

The apparatus for producing liquid fuel from biomass according to the present invention 2 is an apparatus for producing liquid fuel from biomass according to the present invention 1, wherein the gasification unit is configured to supply water vapor containing moisture contained in biomass to a molar ratio of carbon in the biomass. Is gasified in the range of 0 to 1, and the liquid fuel production apparatus does not have a heat exchanger that recovers heat of the biomass gas or the biomass refined gas.

The apparatus for producing liquid fuel from biomass of the present invention 3 is an apparatus for producing liquid fuel from the biomass of the present invention 1 or 2, wherein the gasification unit is configured to heat the biomass at a temperature of 600 to 1000 ° C. by the heating element. Heating , the gas purification unit removes at least one substance selected from particulate matter, tar, sulfur compounds and nitrogen compounds from the biomass gas at a temperature of 200 to 900 ° C., and the liquid fuel production part Liquefy the purified biomass purified gas at a temperature of 100 to 400 ° C. by a catalytic reaction, and the liquid fuel production apparatus does not have a mechanism for reheating the biomass gas or the biomass purified gas. Features. In the present invention 3, the heating temperature of the biomass is preferably 700 to 800 ° C.

The apparatus for producing liquid fuel from biomass according to the present invention 4 is an apparatus for producing liquid fuel from biomass according to the present invention 3, wherein the gas-liquid separator performs gas-liquid separation at a temperature from room temperature to 100 ° C. And

The apparatus for producing liquid fuel from biomass of the present invention 5 is an apparatus for producing liquid fuel from biomass of the present invention 3 or 4, wherein the catalytic reaction is one catalyst selected from Fe, Co, and Ru- based catalysts. It is made to react by. In a liquid fuel production process using a general catalytic reaction, hydrocarbons such as methanol, dimethyl ether, gasoline, kerosene and light oil can be produced by changing the type of catalyst used. For example, methanol is synthesized by the following reaction formula using a Cu—Zn-based catalyst.
CO + 2H ₂ → CH ₃ O (1)

Since dimethyl ether has a structure in which two molecules of methanol are dehydrated, the addition of γ-alumina as a dehydration catalyst can be obtained by the following general reaction formula.
3CO + 3H ₂ → CH ₃ OCH ₃ + CO ₂ (2)

In addition, the production of hydrocarbons such as gasoline, kerosene, and light oil is represented by the following reaction formula using Fe, Co, and Ru-based catalysts.
nCO + 2nH ₂ → CnH ₂ n + nH ₂ O (3)

Liquid fuel production apparatus from biomass present invention 6 is a liquid fuel production apparatus 1 of the biomass is selected from the Inventions 1 to 5, a mounting table provided in a lower portion of the liquid fuel production apparatus, the installation The liquid fuel production apparatus can be transported through a table.

The apparatus for producing liquid fuel from biomass according to the seventh aspect of the present invention is the apparatus for producing liquid fuel from one biomass selected from the first to fifth aspects of the present invention, wherein a moving carriage is provided below the liquid fuel producing apparatus, and the movement The liquid fuel production apparatus can be moved via a carriage.

In the first to seventh aspects of the present invention, a tar decomposition catalyst may be provided at the bottom of the gasification unit. Biomass is processed in a semi-batch process in the gasification section. Semi-batch treatment means opening the gasification furnace, charging the raw material biomass, heating it, raising it to the specified pressure, and then allowing the minimum amount of nitrogen, carbon dioxide, or recycle gas to flow through to advance the gasification reaction Means that.

Further, the tar decomposition catalyst may be one catalyst selected from dolomite, CaO, Ni-based catalyst, and Rh-based catalyst . For example, dolomite is obtained by replacing a part of calcium with magnesium in seawater after corals and the like are deposited on the seabed to form limestone. Calcium and magnesium act on biomass to cause tar decomposition.

In the present invention 1 7 has a plurality of the gasification unit, be sequentially run multiple gasification unit by connecting a plurality of the gasification unit to the selected gas refining section the required gasification unit it can.

In the first to seventh aspects of the present invention, the gas purification unit has two gas purification units, and the flow path can be switched to the other gas purification unit before the adsorbent of one gas purification unit breaks through and can be used alternately. structure can be made to have a such.

In the first to seventh aspects of the present invention, the liquid fuel production unit can be configured so that the unreacted biomass gas that has not been liquefied can be liquefied again .

In the first to seventh aspects of the present invention , the gas-liquid separator can be configured to send unreacted biomass gas that could not be gas-liquid separated to the gasifier so that it can be gasified again .

In the first to seventh aspects of the present invention, the gas-liquid separation unit can be configured to send unreacted biomass gas that could not be gas-liquid separated to the liquid fuel production unit so that it can be liquefied again .

In the present invention 1 7, wherein if unreacted substances Ru char der, the combustion unit may be a device for combusting the char extracted from the gasification unit during the stop.

  The apparatus for producing liquid fuel from biomass according to the present invention does not use a gas compression device or a heat exchanger, reduces the amount of heat necessary for gasification, such as nitrogen, oxygen, water vapor, carbon dioxide, etc. in the liquid fuel synthesis process. Since the concentration was lowered, the structure was simple. In addition, since the unreacted material is reused by recirculating it in the same apparatus, a high yield of liquid fuel can be obtained. In addition, since a plurality of gasification furnaces are provided, a plurality of gasification furnaces can be used while being switched to operate continuously, resulting in an efficient apparatus.

  Hereinafter, the apparatus for producing liquid fuel from biomass according to the present invention will be described in detail with reference to the drawings.

[First embodiment]
FIG. 1 shows a first embodiment of an apparatus for producing liquid fuel from biomass according to the present invention. The configuration of the apparatus for producing liquid fuel from biomass is as described in the above section. Biomass A is thrown into the gasification unit 2 for biomass gasification. The gasification unit 2 has a plurality of gasification furnaces. Hereinafter, the gasification unit 2 will be described by using the first gasification furnace 2a as a representative. The form of biomass A is more effective for gasification because the surface area becomes larger when it is made finer.

  Biomass A is charged into the gasification furnace 2a in such a manner that a certain amount is maintained. In this charging, a means such as a hopper may be used, but the type is not limited. The reason why the amount of biomass A is constant is that a stable gasification process is performed in consideration of the fact that the reaction conditions after gasification become substantially constant. It is also for batch processing described later. The apparatus of this embodiment is configured to enable batch processing. Batch processing, as described above, refers to putting a certain amount of biomass into a gasifier and conducting a gasification reaction by circulating a small amount of nitrogen, carbon dioxide, etc. Gasification of the plurality of gasification furnaces thus made is carried out selectively and sequentially in stages.

  This gasification unit 2 is a downdraft type fixed bed gasification furnace type, in which gasification raw material biomass A is filled in the gasification furnace 2a, and a small amount of nitrogen or carbon dioxide is circulated as a process flow gas. Yes. The upper part is a gasification furnace 2a for charging and gasifying the biomass A, and the lower part is a catalyst storage part 3a for a catalyst for decomposing tar. For a gasification furnace 2b, which will be described later, a catalyst housing 3b is provided. The biomass gas obtained by gasifying the biomass A is discharged from the gasification furnace 2a through the catalyst storage unit 3a.

Here, if the molar ratio of water vapor to carbon in the biomass ([H ₂ O] / [C]) including water contained in the biomass A is up to 1, a heat exchanger is unnecessary. For this reason, it is also possible to distribute a small amount of water vapor. This gasification step is maintained at the same pressure including the subsequent steps. This pressure is in the range of 1 to 5 MPa, and there is no pressurizing device for raising the pressure in the middle.

  The gasification of the biomass A proceeds by heating the gasification furnace 2a from the outside with an electric furnace. After the gasification step, it is connected to the next gas purification unit 4. As the gasification temperature is higher, the gas yield is higher. However, if the gasification temperature is 1000 ° C. or higher, an expensive material or a special structure of the gasification furnace is required. Further, when the gasification temperature is high, 700 to 800 ° C. is desirable because ash in the biomass may melt and clog the gasification furnace.

  The catalyst storage unit 3a at the bottom of the gasification furnace 2a can be filled with a catalyst such as dolomite, CaO, Ni-based catalyst, or Rh-based catalyst as a catalyst for decomposing tar. For example, dolomite contains calcium and magnesium as described above and is a substance suitable for tar decomposition. The tar content contained in the gasified biomass gas is decomposed on the dolomite in the catalyst storage unit 3a.

  In order to promote gasification, a combustion section 1 is provided adjacent to the gasification furnace 2a. Unreacted char, which has not been gasified in the gasification furnace 2a, is taken out from the combustion section 1 after the operation of the gasification furnace 2a is stopped, and is installed in the combustion section 1 as indicated by a dotted line B. Entered. Combustion heat from the combustion of char is supplied as an auxiliary heating source to the gasification furnace 2a to promote gasification.

  A plurality of gasification units 2 are provided. If the amount of gas generated in the first gasification furnace 2a in operation, for example, decreases, before the system begins to depressurize, for example, the second system of the second system. The operation for the gasification process can be continued by switching to the gasification furnace 2b. A switching unit C for this switching is provided, and switching control is appropriately performed according to the selection of the required gasifier. Therefore, a plurality of gasifiers can be selectively operated sequentially. With this configuration, a series of gasification processes can be performed continuously without stopping, and the processing efficiency is improved.

  The gas sent out from the gasification furnace 2a is sent into the gas purification unit 4 as biomass gas. The gas purification unit 4 is an apparatus that removes particulate matter, tar, sulfur compounds, and nitrogen compounds contained in the biomass gas generated in the gasification unit 2 and purifies the biomass gas. The gas purification unit 4 is filled with an adsorbent such as a dust removal filter, activated carbon for adsorbing tar, charcoal, and sand, and the gas purification temperature is controlled to 200 to 900 ° C.

  This gas purification unit 4 has two systems, and is configured such that the flow path can be switched before the internal adsorbent breaks through. For example, the flow path of the biomass gas from the gasification section 2 is connected to the first gas purification section 4a, but the flow path is switched to the second gas purification section 4b before the adsorbent breaks through. It is. The figure shows the configuration, and the flow path can be switched by the switching means 4c.

  With such a configuration, it is possible to take out the adsorbent immediately before the breakthrough of the first gas purification unit 4a stopped by the switching, and to fill and wait for a new adsorbent. If the adsorbent of the second gas purification unit 4b is just before breakthrough, the flow path is switched again to the first gas purification unit 4a. If this is repeated, the gas purification process can be continued without stopping.

  Next, the biomass refined gas purified by the gas purification unit 4 is sent to the liquid fuel production unit 5 in order to produce a liquefied liquid fuel. The liquid fuel production process is connected to the outlet side of the gas purification process and receives the purified biomass refined gas. In the liquid fuel production process, a catalyst for producing a desired liquid fuel is filled. If the liquid fuel is methanol, it is a Cu—Zn-based catalyst. Since dimethyl ether has a structure in which two molecules of methanol are dehydrated, it is necessary to add a γ-alumina catalyst as a dehydration catalyst. Further, if the liquid fuel is a hydrocarbon type such as gasoline, kerosene and light oil, an Fe, Co, Ru type catalyst is used.

  Thus, each target product can be obtained by changing a catalyst. In this liquid fuel production part 5, a liquid fuel is produced in a pressure range of 1 to 5 MPa at a temperature of 100 to 400 ° C. by a catalytic reaction. The manufactured liquid fuel is fed into the gas-liquid separator 6 as a liquid fuel stock solution. The liquid fuel stock solution manufactured by the liquid fuel manufacturing unit 5 contains water, light hydrocarbons, and the like. For this reason, it is separated into liquid fuel refined liquid, water, light hydrocarbons, unreacted gas and the like by this gas-liquid separation unit 6. The separated water is condensed in this step and discharged out of the gas-liquid separation unit 6.

  Next, the liquid fuel purified liquid separated by the gas-liquid separation unit 6 is sent to the reduced pressure recovery unit 7. In this reduced pressure recovery section 7, the separated liquid fuel purified liquid is cooled and decompressed. The decompression recovery unit 7 is provided with a decompression valve 7 a and is connected to a delivery port of the gas-liquid separation unit 7. Water and liquid fuel have different saturation vapor pressure curves and can be taken out of the system as a liquid from a substance having a high boiling point in the cooling process. The liquid fuel purified liquid taken out through the pressure reducing valve 7a is a liquid fuel 7b as a regular product that can be used, and is collected in a tank or the like.

[Second Embodiment]
FIG. 2 is a diagram showing a second embodiment of the apparatus for producing liquid fuel from biomass according to the present embodiment. In the liquid fuel production process, an embodiment is considered in which processing cannot be performed by a single process. A flow path 5 a is provided for returning unreacted gas that has not been liquefied by the liquid fuel production unit 5 to the receiving port of the liquid fuel production unit 5. By providing this flow path 5a, the biomass-refined gas is caused to flow through the liquid fuel production section 5 many times, whereby the unreacted gas is liquefied in a reused form. Therefore, the biomass purified gas can be liquefied efficiently.

[Third Embodiment]
FIG. 3 is a diagram showing a third embodiment of the apparatus for producing liquid fuel from biomass according to the present embodiment. After the biomass liquid fuel stock solution was separated from the liquid fuel and water in the cooling process of the gas-liquid separator 6, the unreacted gas was returned to the upstream of the gasification process via the flow path 6a. Thereby, the unreacted gas is gasified again, the liquefaction process is performed again, and the gas-liquid separation process is performed again. Thus, the present embodiment has a structure that can be efficiently converted into CO and hydrogen.

[Fourth Embodiment]
FIG. 4 is a diagram showing a fourth embodiment of the apparatus for producing liquid fuel from biomass according to the present embodiment. After the biomass liquid fuel stock solution was separated from the liquid fuel and water in the cooling process of the gas-liquid separator 6, the unreacted gas was returned to the upstream of the liquid fuel production process via the flow path 6b. Thereby, the unreacted gas is liquefied again, and the gas-liquid separation process is performed again.

  In any of the second to fourth embodiments, the unreacted material is circulated in the same apparatus and reused to effectively use the biomass without waste and to increase the yield of the liquid fuel. Next, other embodiments applicable to any of the embodiments will be described. That is, an installation base 8 is provided in the lower part of the liquid fuel production apparatus from biomass, and the liquid fuel production apparatus can be transported through the installation base 8, and the liquid fuel production apparatus from biomass is moved to the lower part. In this example, a carriage 9 is provided, and the liquid fuel production apparatus can be moved through the movable carriage 9.

  For example, the mounting base 8 at the lower part of the apparatus can be lifted with a crane or the like to transport the liquid fuel production apparatus to a predetermined position. Further, the liquid fuel production apparatus can be moved to a predetermined position by pulling the movable carriage 9 at the lower part of the apparatus manually or by power. Although the figure showing the embodiment is a figure in which a movable carriage 9 is provided, it may be a mounting base 8.

  While various embodiments have been described above, it goes without saying that the present invention is not limited to these embodiments.

  The present invention relates to an apparatus for producing liquid fuel from biomass, that is, a highly efficient plant for producing liquid fuel from renewable biomass with high efficiency, but as long as the principle can be utilized, other fields such as It is applicable to the field of low-quality coal use, and the field of use is wide-ranging.

It is a block diagram of the liquid fuel manufacturing apparatus from biomass concerning a 1st embodiment. It is a block diagram of the liquid fuel manufacturing apparatus from biomass concerning a 2nd embodiment. It is a block diagram of the liquid fuel manufacturing apparatus from biomass concerning a 3rd embodiment. It is a block diagram of the liquid fuel manufacturing apparatus from biomass concerning a 4th embodiment.

Explanation of symbols

1. 1. Combustion furnace Gasification part 3a, 3b. 3. Catalyst storage part 4. Gas purification unit Liquid fuel production section 5a. Flow path 6. Gas-liquid separator 6a, 6b. Flow path 7. Vacuum recovery unit 7a. Pressure reducing valve 7b. Liquid fuel8. Mounting base9. Moving trolley

Claims (7)

Biomass was heated at a constant amount held by the heating body, and a gasification section for the gas at a pressure range of 1 to 5 MPa,
At least one or more substances selected from particulate matter, tar, sulfur compounds and nitrogen compounds are removed from biomass gas which is a mixed gas of carbon monoxide and hydrogen generated by the gasification unit, and the biomass gas is purified A gas purification unit to
A liquid fuel production section for producing a biomass liquid fuel stock solution that is a hydrocarbon by liquefying the purified biomass refined gas by catalytic reaction ;
A gas-liquid separator that separates the biomass liquid fuel stock solution into biomass liquid fuel, water, and light hydrocarbons;
A reduced pressure recovery unit that recovers the biomass liquid fuel separated by the gas-liquid separation unit by reducing the pressure;
Combusting unreacted material that is not gasified in the gasification unit, and supplying the generated heat to the gasification unit ,
An apparatus for producing liquid fuel from biomass, characterized by not having a pressurizing device for maintaining a constant pressure from the gasification to the liquefaction and increasing the pressure of the biomass gas or the purified biomass gas. An apparatus for producing liquid fuel from biomass according to claim 1,
The gasification unit gasifies the molar ratio of supply water vapor containing moisture contained in biomass and carbon in biomass in the range of 0 to 1,
The said liquid fuel manufacturing apparatus does not have the heat exchanger which collect | recovers the heat | fever of the said biomass gas or the said biomass refinement | purification gas, The liquid fuel manufacturing apparatus from biomass characterized by the above-mentioned. An apparatus for producing liquid fuel from biomass according to claim 1 or 2,
The gasification section heats the biomass with the heating body at a temperature of 600 to 1000 ° C. ,
The gas purification unit, the biogas from particulate matter, tar, at least one or more substances selected from sulfur compounds and nitrogen compounds are removed at a temperature of 200 to 900 ° C.,
The liquid fuel production unit liquefies the purified biomass purification gas at a temperature of 100 to 400 ° C. by catalytic reaction ,
The said liquid fuel manufacturing apparatus does not have a mechanism for reheating the said biomass gas or the said biomass refined gas, The liquid fuel manufacturing apparatus from the biomass characterized by the above-mentioned. An apparatus for producing liquid fuel from biomass according to claim 3,
The apparatus for producing liquid fuel from biomass, wherein the gas-liquid separation unit performs gas-liquid separation at a temperature from room temperature to 100 ° C. An apparatus for producing liquid fuel from biomass according to claim 3 or 4,
The said catalytic reaction is made to react with one catalyst selected from a Fe, Co, and Ru type | system | group catalyst, The liquid fuel manufacturing apparatus from the biomass characterized by the above-mentioned. An apparatus for producing liquid fuel from biomass according to claim 1 selected from claims 1 to 5,
An apparatus for producing liquid fuel from biomass, wherein a mounting base is provided at a lower portion of the liquid fuel manufacturing apparatus, and the liquid fuel manufacturing apparatus can be transported through the mounting base. An apparatus for producing liquid fuel from biomass according to claim 1 selected from claims 1 to 5,
An apparatus for producing liquid fuel from biomass, wherein a moving carriage is provided at a lower portion of the apparatus for producing liquid fuel, and the apparatus for producing liquid fuel can be moved via the carriage.

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