Patent Publication Number: US-2011065815-A1

Title: Method and apparatus for production of hydrocarbon from biomass

Description:
TECHNICAL FIELD 
     The present invention relates to a method and an apparatus for carrying out synthesis of a hydrocarbon series liquid or a gas as a product using hydrogen and carbon monoxide, which are generated by use of a biomass such as grass or a tree as a raw material, as a reactant and especially relates to a producing method and an apparatus of hydrocarbon utilizing Fischer-Tropsch method (hereinafter referred to as FT method) as a synthesis method of the hydrocarbon. 
     BACKGROUND ART 
     Conventionally, synthesis of a petroleum alternative synthetic fuel by the FT method for synthesizing liquidized hydrocarbon has been carried out by catalytic reaction between hydrogen and carbon monoxide, which are obtained by partially burning a natural gas or resolving water vapor by coal under a high temperature and high pressure condition. According to this FT method, in a case where petroleum resources are drained or price of the petroleum is elevated, petroleum alternative fuel can be temporarily synthesized from a natural gas or coal by the FT method. Therefore, various studies, improvement, and modification of the method have been conducted. 
     However, there are problems that a synthesis method and a synthesis apparatus of a hydrocarbon fuel by the conventional FT method require very high pressure and size of the apparatus becomes large due to the demand for the high pressure. 
     Meanwhile, along with the strong demand for usage of recyclable resources these days, necessity of usage of a biomass energy has been strongly recognized. This is because there is high expectation to utilization of the biomass energy from a viewpoint of possibility of recycling or possibility of mass production while there is still a big problem in direct utilization of the natural gas or coal or synthetic fuel from the natural gas or coal by the above-mentioned FT method as a petroleum alternative fuel from a viewpoint of global warming caused by emission of carbon dioxide or recyclability, although certain usefulness thereof is recognized. 
     To respond to such expectation, the inventors of the present invention have proceeded development of a biomass gasification unit or an apparatus for generation of high-temperature combustion gas to generate hydrogen and carbon monoxide using a biomass as a raw material or a fuel as disclosed in the Patent Document 1 and the Patent Document 2. 
     However, because it is difficult to obtain hydrogen and carbon monoxide both quantitatively and qualitatively from the conventional biomass gasification unit in the Patent Document 1 or the like, there has been no method and apparatus to synthesize liquid or gas hydrocarbon fuel by use of the FT method while using hydrogen and carbon monoxide, which is obtained by using biomass as a raw material, as a reactant. 
     Patent Document 1: Japanese Unexamined Patent Application Publication No. 2005-105285 
     Patent Document 2: Japanese Unexamined Patent Application Publication No. 2006-300501 
     The present invention has been made in consideration of the above-mentioned condition and a first purpose thereof is to provide a method for producing hydrocarbon from a biomass which uses hydrogen and carbon monoxide, which is generated by use of a biomass such as grass or a tree, as a reactant and enables to synthesize liquid or gas hydrocarbon fuel as a product with a high yield while being small-sized and low pressured. A second purpose of the present invention is to provide an apparatus for producing hydrocarbon from a biomass. 
     SUMMARY OF INVENTION 
     Technical Problem 
     To achieve the above-mentioned first purpose, a method for producing hydrocarbon from a biomass of the present invention is characterized by generating a mixed gas including hydrogen and carbon monoxide as main components thereof by heating powder or chipped raw material biomass to 800° C. or more and at the same time bringing the biomass into contact with water vapor of 800° C. or more and causing the mixed gas to be in contact with a predetermined catalyst under a predetermined temperature and a predetermined pressure to convert the mixed gas into hydrocarbon. 
     It is preferable that the pressure under which the mixed gas is brought into contact with the catalyst is lower than 3 MPa. 
     It is preferable that the catalyst to be in contact with the mixed gas has a single body or a compound of one selected from iron and copper or both of them as a basic catalyst and at the same time a single body or a compound of one or more substances selected from magnesium, calcium, cobalt, nickel, potassium, and sodium which is added as a backup catalyst or assistant catalyst, while one or more substances selected from zeolite, alumina, and silica are supported. 
     Catalytic reaction is a chemical reaction expressed by the following chemical equation formula. 
       CO+2H 2   →n   −1 (CH 2 ) n +H 2 O 
     It becomes possible to repeatedly carry out predetermined catalytic reaction to the mixed gas and to reduce the amount of the unreacted mixed gas while gradually converting the unreacted mixed gas into hydrocarbon if a route of bringing the mixed gas into contact with the catalyst to convert the gas into hydrocarbon by the predetermined catalytic reaction and bringing unreacted mixed gas remained in a previous step into contact with a catalyst equivalent to the aforementioned catalyst so that the gas is converted into hydrocarbon by the catalytic reaction is set to include predetermined number of steps. 
     Hydrogen obtained by electrolysis of water by the power of a recyclable energy other than a biomass is added to the mixed gas including hydrogen and carbon monoxide as its main components which are generated by heating the raw material biomass to 800° C. or more and at the same time bringing the biomass into contact with water vapor of 800° C. or more enables to improve yield of hydrocarbon per raw material biomass. 
     To achieve the second purpose, means taken in an apparatus for producing hydrocarbon from a biomass of the present invention is characterized by including a biomass gasification unit for generating a mixed gas including hydrogen and carbon monoxide as main components thereof using a biomass as a raw material and fuel, a pressurization means for pressurizing the mixed gas generated by the biomass gasification unit, a temperature adjustment means for adjusting the mixed gas to have an appropriate temperature, a catalyst for obtaining hydrocarbon as a product by causing a predetermined catalytic reaction using the mixed gas which is pressurized by the pressurization means while maintained in the appropriate temperature by the temperature adjustment means as a reactant, a reaction chamber in which the catalyst is provided and the mixed gas which is appropriately pressurized and has appropriate temperature is brought into contact with the catalyst to cause a predetermined catalytic reaction, a liquidization means for liquidizing the hydrocarbon generated by the catalytic reaction, and a collection means for collecting the liquidized hydrocarbon liquidized by the liquidization means. 
     It is preferable that the reaction chamber includes an inlet for supplying the mixed gas and an exhaust for discharging the hydrocarbon generated by the catalytic reaction in the reaction chamber and the unreacted mixed gas wherein the catalyst is provided on a route from the inlet to the exhaust. 
     The reaction chamber has the inlet for supplying the mixed gas in an upper part thereof, has the exhaust for discharging the hydrocarbon generated by the catalytic reaction of the mixed gas in the reaction chamber and the unreacted mixed gas in an lower part of the chamber, and the catalyst is provided on a route from the inlet to the exhaust. A plurality of the reaction chambers are provided, the inlet of the reaction chamber positioned at the uppermost stream connected the biomass gasification unit so that the mixed gas generated by the biomass gasification unit can be introduced, the exhaust of the reaction chamber positioned at the uppermost stream connected to the inlet of the reaction chamber positioned on immediate downstream, and hereinafter an exhaust of the reaction chamber positioned on immediate upper stream is connected to the inlet of the reaction chamber positioned on immediate downstream. 
     It is preferable that the liquidization means includes a liquidization chamber having the inlet on the upper stream side and an exhaust for discharging the unreacted mixed gas on the down stream side and an extraction port for extracting liquidized hydrocarbon on the down stream side and a cooling means for cooling down the liquidization chamber, wherein the inlet is connected to the exhaust of the reaction chamber positioned on the upper stream side of the liquidization chamber and the exhaust is connected to the inlet of the reaction chamber positioned on the down stream side of the liquidization chamber. 
     The collection means for collecting the liquidized hydrocarbon includes a pipeline connecting with each extraction ports of the plurality of liquidization chambers wherein the pipeline can be freely opened or closed by a valve provided on a route thereof. 
     The temperature adjustment means for adjusting temperature of the mixed gas to be the predetermined temperature before introduction of the mixed gas into the reaction chamber may intervene on the upper stream side of the inlet for supplying the mixed gas into the reaction chamber. 
     The reaction chamber may include an air inlet for supplying air controlled to have a predetermined temperature by a constant room temperature adjustment means and an air exhaust for emitting air and may be provided in a constant temperature room which is partitioned and surrounded by an heat insulating material. 
     It is preferable that the catalyst has a single body or a compound of one selected from iron and copper or both of them as a basic catalyst and at the same time a single body or a compound of one or more substances selected from magnesium, calcium, cobalt, nickel, potassium, and sodium is added as a backup catalyst or assistant catalyst thereto, while one or more substances selected from zeolite, alumina, and silica are supported. 
     The biomass gasification unit used for the present invention includes an heat insulating room which is partitioned and surrounded by an heat insulating wall material, a gasification reaction chamber having a raw material biomass introduction means partitioned and surrounded by a thermally conductive wall material in the heat insulating room for supplying the raw material biomass roughly crushed to have a diameter of approximately 2 cm or less inside and an overheated water vapor introduction means for supplying overheated water vapor inside, and a combustion high temperature gas generation unit for supplying a combustion high temperature gas in a space between the heat insulating room and the gasification reaction chamber, wherein the raw material biomass and the overheated water vapor introduced into the gasification reaction chamber are heated by the combustion high temperature gas supplied from the combustion high temperature gas generation unit to the space between the heat insulating room and the gasification reaction chamber via the thermally conductive wall material of the gasification reaction chamber to cause the raw material biomass and the overheated water vapor to react endothermically so that the mixed gas including hydrogen and carbon monoxide as main components thereof is generated. 
     The combustion high temperature gas generation unit generates a combustion high temperature gas of 800° C. or more by perfectly combusting a fuel biomass and supplies the generated combustion high temperature gas to the space between the heat insulating room and the gasification reaction chamber. 
    
    
     
       BRIEF DESCRIPTION OF DRAWINGS 
         FIG. 1  is a schematic view showing configuration of the whole of an apparatus for producing hydrocarbon from a biomass. 
         FIG. 2  is a schematic view showing configuration of the whole of a biomass gasification unit. 
         FIG. 3  is a view showing a main part of the gasification unit of a biomass and also showing configuration of a unit for generating a mixed gas. 
         FIG. 4  is a view showing configuration of a combustion high temperature gas generation unit. 
         FIG. 5  is a view showing configuration of a hydrocarbon synthesis unit, a liquidization means, and a collection means. 
     
    
    
     REFERENCE NUMERALS 
     
         
           1 : An apparatus for producing hydrocarbon from a biomass; 
           101 : Biomass gasification unit; 
           110  Heat insulating room; 
           111 : Combustion high temperature gas inlet; 
           112 : Combustion high temperature gas exhaust; 
           120 : Gasification reaction chamber; 
           121 : Porous body; 
           122 : Ash discharging means; 
           123 : Mixed gas exhaust means; 
           124 : Gasification space; 
           125 : Raw material biomass inlet; 
           126 : Overheated water vapor inlet; 
           127 : Mixed gas exhaust; 
           128 : Ash exhaust; 
           130 : Raw material biomass introduction means; 
           131 : Screw feeder; 
           132 : Hopper; 
           140 : Overheated water vapor introduction means; 
           141 : Boiler; 
           142 : Fan motor; 
           143 : Chimney; 
           150 : Combustion high temperature gas generation unit; 
           151 : Fire lattice; 
           152 : Combustion furnace; 
           153 : Air preheating device; 
           154 : Upper combustion room; 
           155 : Bottom combustion room; 
           156 : Fuel biomass inlet; 
           157 : First air inlet; 
           158 : Second air inlet; 
           159 : Third air inlet; 
           160 : Combustion high temperature gas exit; 
           161 : Ash pit; 
           201 : Cleaning up means; 
           202 : Heat exchanger; 
           203 : Cyclone; 
           204 : Water injector; 
           301 : Gas tank; 
           302 : Purified mixed gas inlet; 
           303 : Mixed gas exit; 
           304 : Inlet for reintroduction of mixed gas; 
           401 : Pressurization pump; 
           501 : Hydrocarbon synthesis unit; 
           510 : Pressurized mixed gas inlet; 
           520 : Temperature adjustment means; 
           521 : Constant temperature room; 
           522 : Constant temperature room temperature adjustment unit; 
           523 : Temperature-controlled air inlet; 
           524 : Temperature-controlled air exhaust; 
           525 : High temperature gas introduction line; 
           526 : Air introduction line; 
           527 : Temperature-controlled air feeding line; 
           30   a : First reaction chamber; 
           530   b : Second reaction chamber; 
           530   c : Third reaction chamber; 
           530   d : Fourth reaction chamber; 
           530   e : Fifth reaction chamber; 
           531 : Catalyst; 
           532   a : First mixed gas introduction line; 
           532   b : Second mixed gas introduction line; 
           532   c : Third mixed gas introduction line; 
           532   d : Fourth mixed gas introduction line; 
           532   e : Fifth mixed gas introduction line; 
           533   a ,  533   b ,  533   c ,  533   d ,  533   e : Mixed gas inlets; 
           534   a ,  534   b ,  534   c ,  534   d ,  534   e : Exhaust lines; 
           535   a ,  535   b ,  535   c ,  535   d ,  535   e : Temperature adjustment units; 
           540 : Liquidization means; 
           541   a : First liquidization chamber; 
           541   b : Second liquidization chamber; 
           541   c : Third liquidization chamber; 
           541   d : Fourth liquidization chamber; 
           541   e : Fifth liquidization chamber; 
           542 : Cooling water introduction line; 
           543 : Cooling water discharging line; 
           544 : Cooling bath; 
           545   a ,  545   b ,  545   c ,  545   d ,  545   e : Introduction lines; 
           546   a ,  546   b ,  546   c ,  546   d ,  546   e : Liquidized hydrocarbon exhausts; 
           547   a ,  547   b ,  547   c ,  547   d : Cooled mixed gas exhausts; 
           547   e : Final unreacted mixed gas exhaust; 
           548 : Circulation line; 
           550 : Collection means; 
           551   a : First collection pipe; 
           551   b : Second collection pipe; 
           551   c : Third collection pipe; 
           551   d : Fourth collection pipe; 
           551   e : Fifth collection pipe; 
           552 : Liquidized hydrocarbon extraction pipe; 
           553 : Valve; 
         A, A 1 , A 2 , A 3 : Air; 
         B: Combustion high temperature gas; 
         FB: Fuel biomass; 
         G: Mixed gas; 
         MB: Raw material biomass; 
         S: Overheated water vapor; 
         TA: Temperature-controlled air; and 
         W: Cooling water 
       
    
     BEST MODES FOR CARRYING OUT THE INVENTION 
     Hereinafter, a preferable embodiment of the present invention will be explained in detail with reference to  FIGS. 1 to 5 . 
     A method and an apparatus for producing hydrocarbon from a biomass of the present embodiment use a powder or chipped biomass as a raw material. The raw material biomass is heated to 800° C. or more and brought into contact with water vapor of 800° C. or more to generate a mixed gas including hydrogen and carbon monoxide as its main components. The mixed gas generated from biomass is used as a reactant. The reactant is converted into hydrocarbon by the FT method and liquidized to obtain a liquid hydrocarbon of synthetic fuel. 
     The method of the present embodiment for synthesizing liquid hydrocarbon from the mixed gas generated from biomass including hydrogen and carbon monoxide as its main components is to set the mixed gas to be between 150° C. and 300° C. and at the same time to pressurize the gas with less than 3 MPa of pressure to bring the gas into contact with a predetermined catalyst to cause a predetermined catalytic reaction as expressed by the above-mentioned chemical equation formula so that hydrogen and carbon monoxide are converted into gas phase hydrocarbon and heat exchange is carried out between refrigerant substances such as water or air to cool down the gas phase hydrocarbon to obtain liquid hydrocarbon. 
     The catalyst has a single body or a compound of one selected from iron and copper or both of them as a basic catalyst and at the same time a single body or a compound of one or more substances selected from magnesium, calcium, cobalt, nickel, potassium, and sodium is added as a backup catalyst or assistant catalyst thereto, while one or more substances selected from zeolite, alumina, and silica are supported. 
     As the catalyst, for example, a catalyst configured by combining a heretofore known FT catalyst and a solid acid catalyst such as zeolite may be used and in this case as the catalytic reaction, a mixed gas including hydrogen and carbon monoxide is reacted first on the FT catalyst to generate heavy hydrocarbon. 
     Subsequently, the heavy hydrocarbon is decomposed on the adjacent solid acid catalyst to be a lighter branch hydrocarbon. According to the catalyst having such a configuration, there are advantages such as it becomes possible to synthesize hydrocarbon from the mixed gas including hydrogen and carbon monoxide and moreover to automatically decompose and remove wax, which is accumulated on the FT catalyst to cause a problem before, so that slowing down of expansion of the mixed gas due to deactivation of the catalyst or to the wax can be suppressed. 
     Specifically, as the FT catalyst, a cobalt FT catalyst with required loading of cobalt can be obtained by impregnating cobalt nitrate into silica gel which was previously dried for two hours in the air at 200° C. by incipient wetness method, subsequently drying for 12 hours at 120° C. and then burning at 400° C. for two hours for preparation. Moreover, it is also possible to prepare an iron FT catalyst by solving predetermined amount of iron nitrate, copper nitrate, magnesium nitrate, and calcium nitrate in 500 mL of water and simultaneously mixing. The solution and sodium carbonate solution which was adjusted to 20 g/500 mL are dropped into 500 mL of water adjusted 60° C. and pH of 8 to generate precipitate, and then, after all the solutions are dropped, the solutions are further mixed for one hour, the precipitate is filtered, washed by distilled water, dried, and burnt at 400° C. for preparation. 
     Further, a composite catalyst configured by combining the above-mentioned zeolite and the FT catalyst can be prepared by preparing a sol precursor solution by use of tetraethyl orthosilicate, aluminum nitrate, tetrapropyl ammonium hydroxide, water, and ethanol while mixing previously prepared cobalt FT catalyst and zeolite and then putting the prepared solution into an autoclave for hydrothermal synthesis at 180° C. Moreover, it is possible to prepare the composite catalyst by mixing the previously prepared iron FT catalyst and zeolite and then pressurizing the mixture for 20 minutes by a uniaxial pressing machine with 600 kgf/cm 2  of pressure. Then, a cobalt series composite catalyst obtained by combining the cobalt FT catalyst and the zeolite catalyst, and an iron series composite catalyst obtained by combining the iron FT catalyst and the zeolite catalyst may be mixed in a composite manner to be used as a catalyst. 
     Moreover, the method of converting the mixed gas into hydrocarbon to be in contact with the catalyst may be carried out in one stage. However, more preferably, the mixed gas including hydrogen and carbon monoxide generated from biomass as main components thereof is caused to be in contact with the catalyst to convert the gas a into hydrocarbon by the predetermined reaction as a first step, after this step is over, unreacted mixed gas remained in the first step is caused to be in contact with a catalyst equivalent to the aforementioned catalyst to convert the gas a into hydrocarbon by the catalytic reaction as a second step, and further, subsequently, similar steps are carried out as a third step and a fourth step to follow previously determined number of steps to repeatedly carry out predetermined catalytic reaction so that unreacted mixed gas is converted into hydrocarbon and the amount of the mixed gas is reduced in a stepwise manner. 
     Further, hydrogen obtained by electrolysis of water by the power of recyclable energy other than a biomass may be added to the mixed gas generated from biomass and in this case it becomes possible to significantly improve yield of hydrocarbon per raw material biomass. 
     An apparatus  1  for producing hydrocarbon from a biomass according to the present embodiment for specifically carrying out the method for producing hydrocarbon from a biomass as explained above includes a biomass gasification unit  101  for generating a mixed gas G including hydrogen and carbon monoxide as main components thereof by supplying a raw material biomass MB, overheated water vapor S for gasification of the raw material biomass MB, fuel biomass FB, and air A for combustion of the fuel biomass FB, a cleaning up means  201  for purifying the mixed gas G generated by the biomass gasification unit  101 , a gas tank  301  for temporarily storing the cleaned-up mixed gas G, a pressurization pump  401  for pressurizing the mixed gas G, and a hydrocarbon synthesis unit  501  for converting the pressurized mixed gas G into hydrocarbon, as shown in  FIG. 1 . 
     The biomass gasification unit  101  includes an heat insulating room  110  for blocking heat from inside and outside of the room, a gasification reaction chamber  120  provided in the heat insulating room  110 , a raw material biomass introduction means  130  for supplying the raw material biomass MB roughly crushed to have a diameter of approximately 2 cm or less into the gasification reaction chamber  120 , an overheated water vapor introduction means  140  for supplying the overheated water vapor S into the gasification reaction chamber  120 , and a combustion high temperature gas generation unit  150  for supplying a combustion high temperature gas B to a space between the heat insulating room  110  and the gasification reaction chamber  120 . 
     At an appropriate height position in the gasification reaction chamber  120 , a porous body  121  having a plurality of through-holes which communicate vertically for partitioning the gasification reaction chamber  120  between upper and lower parts is provided. Moreover, the gasification reaction chamber  120  includes an ash discharging means  122  for discharging ash generated in the gasification reaction chamber  120  outside and a mixed gas exhaust means  123  for emitting the mixed gas G having hydrogen and carbon monoxide as its main components which are generated in the gasification reaction chamber  120  to outside. 
     The heat insulating room  110  is for blocking heat to and from the room and especially is configured to be enabled to heat inside the heat insulating room  110  and to maintain required temperature, preferably 800° C. or more. The heat insulating room  110  may be configured by a heretofore known heat insulating material and as long as the gasification reaction chamber  120  provided in the heat insulating room  110  can be surrounded, shape or size are appropriately designed. However, a space is provided between an inner surface of the heat insulating room  110  and an external surface of the gasification reaction chamber  120  and the combustion high temperature gas B generated by the combustion high temperature gas generation unit  150  is introduced thereto so that the gasification reaction chamber  120  can be heated from outside of the wall. 
     To the heat insulating room  110 , connecting holes which connect the raw material biomass introduction means  130 , the overheated water vapor introduction means  140 , the mixed gas exhaust means  123 , or ash discharging means  122  to outside of the heat insulating room  110  to communicate inside and outside of the room are formed in a closely connected manner respectively to the raw material biomass introduction means  130 , the overheated water vapor introduction means  140 , the mixed gas exhaust means  123 , ash discharging means  122 , or the like to prevent heat from leaking. 
     Moreover, a combustion high temperature gas inlet  111  and a combustion high temperature gas exhaust  112  are formed to the heat insulating room  110  so that combustion high temperature gas B can be supplied from the combustion high temperature gas generation unit  150  into the heat insulating room  110  or can be emitted from the room. 
     The gasification reaction chamber  120  is partitioned and surrounded by a thermal conductive wall material, has a gasification space  124  having a predetermined capacity and area inside thereof, and the external surface of the wall material of the gasification reaction chamber  120  is further surrounded by a wall surface of the heat insulating room  110 . In the gasification reaction chamber  120 , a raw material biomass inlet  125  for supplying the raw material biomass MB from outside into the gasification reaction chamber  120  and an overheated water vapor inlet  126  for supplying the overheated water vapor S from outside into the gasification reaction chamber  120  are formed, which are respectively connected to the raw material biomass introduction means  130  and the overheated water vapor introduction means  140  so that the raw material biomass MB and the overheated water vapor S can be introduced into the gasification reaction chamber  120 . 
     The raw material biomass inlet  125  is formed on an upper part of the gasification reaction chamber  120  and the raw material biomass MB to be introduced from outside into the gasification reaction chamber  120  through the raw material biomass inlet  125 , and the raw material biomass is dropped inside the gasification reaction chamber  120  and in the process of dropping, gasification can be carried out. 
     The overheated water vapor inlet  126  is formed in a lower part of the gasification reaction chamber  120  and the overheated water vapor S to be introduced from outside into the gasification reaction chamber  120  through the overheated water vapor inlet  126  can be introduced as an upward flow in the gasification reaction chamber  120 . 
     Moreover, the gasification reaction chamber  120  has a mixed gas exhaust  127  for emitting the mixed gas G generated inside the chamber from the gasification reaction chamber  120  and an ash exhaust  128  for discharging ash which is, though very little, generated during gasification by the raw material biomass MB and the overheated water vapor S in the gasification reaction chamber  120 , each of which is respectively connected to a mixed gas exhaust means  123  and an ash discharging means  122  so that the mixed gas G or the ash generated in the gasification reaction chamber  120  can be emitted outside. 
     The mixed gas exhaust  127  is formed in an appropriate height position on a side surface of the gasification reaction chamber  120 , preferably in a position higher than the height position where the porous body  121  is provided. On the other hand, the ash exhaust  128  is formed on the bottom of the gasification reaction chamber  120  which is lower than the porous body  121  so that in a case where the ash is accumulated, the ash falls by its own weight and is taken outside. 
     The wall material of the gasification reaction chamber  120  includes a material having thermal conductivity, heat resistance, and thermal shock properties which allows heat to be easily transferred from outside to inside of the gasification reaction chamber  120  and also endures required temperature and change in temperature. Capacity and shape of the gasification space  124  in the gasification reaction chamber  120  may be appropriately designed depending on the required gasification processing throughput. However, the gasification space  124  is designed to have the size and shape which allows the raw material biomass MB which is a target of gasification to exist by an appropriate amount. Surface area inside the gasification reaction chamber  120  may be appropriately designed depending on the required gasification processing throughput. 
     Inside of the gasification reaction chamber  120  is partitioned in upper and lower parts by the porous body  121  having appropriate thickness which is provided at an appropriate height position in vertical directions. The porous body  121  includes a metal or ceramics which can endure required high temperature, is approximately plate-shaped as a whole, and has a plurality of through-holes which communicate vertically. It is preferable that the size of the through-holes is designed to have a diameter which allows water vapor to pass through without difficulty but does not allow the raw material biomass MB which has not been gasified to pass through. Moreover, the porous body  121  may be provided in a condition slightly inclined than level. 
     The raw material biomass introduction means  130  connects with the raw material biomass inlet  125  formed to the gasification reaction chamber  120  and includes a pipe of a heat resistant material having a predetermined inner diameter and length which is extended approximately vertically to outside of the heat insulating room  110  through the connecting hole formed to the heat insulating room  110 , a screw feeder  131  having an exit connected to the upper edge of the pipe and a screw extended approximately horizontally provided inside the screw feeder  131 , and a hopper  132  for supplying the raw material biomass MB to the screw feeder  131 . 
     The screw feeder  131  includes a cylindrical body extended for a predetermined length in approximately horizontal direction, a screw provided inside the cylindrical body in a rotatable manner having approximately same length as the cylindrical body, and an actuator for driving the screw provided on one edge of the screw. In the vicinity of an edge opposite to the side where the actuator is provided, an exit for discharging the raw material biomass MB supplied by the rotation of the screw is formed in the cylindrical body and on an upper part in the vicinity of the actuator in the cylindrical body, an inlet for taking the raw material biomass MB from the hopper  132  into the screw feeder  131  is formed. Of course, the hopper  132  is continued to this inlet. 
     The overheated water vapor introduction means  140  is connected to the overheated water vapor inlet  126  formed to the gasification reaction chamber  120  and includes a pipe having a heat resistant and water vapor resistant material and having a predetermined inner diameter and length which is extended to outside of the heat insulating room  110  through the communicating hole formed to the heat insulating room  110 . It is preferable that a boiler  141  for obtaining overheated water vapor S generated by heating water with the combustion high temperature gas B discharged from the heat insulating room  110  as a heat source is connected on the downstream of the pipe and the overheated water vapor S is previously heated before introduction into the gasification reaction chamber  120  to be the overheated water vapor S. The combustion high temperature gas B which passed out through the boiler  141  is discharged from the chimney  143  via the fan motor  142 . 
     The mixed gas exhaust means  123  is connected to the mixed gas exhaust  127  formed to the gasification reaction chamber  120  and includes a pipe of a heat resistant or corrosion resistant material having a predetermined inner diameter and length which is extended to outside of the heat insulating room  110  through the communication hole formed to the heat insulating room  110 . The cleaning up means  201  for purifying the generated mixed gas is connected on the downstream of the pipe. 
     The ash discharging means  122  is connected to the ash exhaust  128  formed to the gasification reaction chamber  120  and includes a pipe of a heat resistant material having a predetermined inner diameter and length which is extended to outside of the heat insulating room  110  through the communication hole formed to the heat insulating room  110 . It is preferable that a valve which can freely open or close the pipe for opening or closing communication between inner and external side of the gasification reaction chamber  120  by the pipe is provided on the downstream of the pipe. 
     The combustion high temperature gas generation unit  150  includes a combustion furnace  152  formed to have a vertical shape with a fire lattice  151  provided inside at approximate center in height direction thereof and an air preheating device  153  for previously heating an air A to be introduced into the combustion furnace  152 , as shown in  FIG. 4 . 
     The combustion furnace  152  has an upper combustion room  154  positioned on an upper part of the fire lattice  151  and a bottom combustion room  155  positioned on a lower part of the fire lattice  151 . The combustion furnace  152  includes a fuel biomass inlet  156  for supplying a fuel biomass FB roughly crashed on the upper part inside thereof and a first air inlet  157  for supplying an air A 1  so that the air for combusting the fuel biomass FB introduced into the upper combustion room  154  is blown into the room. At the approximate center in height direction of the combustion furnace  152 , a second air inlet  158  for blowing an air A 2  from the fire lattice  151  while introducing the air A 2  into the fire lattice  151  provided inside the furnace is formed for more efficiently combusting the fuel biomass FB which falls while burning. In the vicinity of the bottom of the combustion furnace  152 , a third air inlet  159  for introducing an air A 3  into the bottom combustion room  155  for more completely combusting the combustion high temperature gas B flown down into the bottom combustion room  155  through the fire lattice  151  is formed so that the introduced air A 3  is blown in approximately horizontal direction in the combustion furnace  152 . A combustion high temperature gas exit  160  for discharging the approximately completely combusted combustion high temperature gas B is formed in a position opposite to the third air inlet  159  on a side wall of the bottom combustion room  155 . An ash pit  161  for accumulating ash which is cinder after combustion of the fuel biomass FB is formed on the bottom part of the combustion furnace  152 . 
     The fire lattice  151  is metallic and has a lattice shape having a through path inside thereof through which the air A 2  introduced from the second air inlet  158  flows and on both top and bottom surfaces of the lattice-shaped fire lattice  151 , a plurality of air nozzles are formed so that the air A 2  introduced from the second air inlet  158  is blown out therefrom up-and-down directions. 
     The air preheating device  153  heat the air A to be introduced into the combustion furnace  152  from the first air inlet  157 , the second air inlet  158 , or the third air inlet  159  up to 450° C. in advance by use of part of the combustion high temperature gas B generated by the combustion high temperature gas generation unit  150 . 
     The cleaning up means  201  includes a heat exchanger  202 , a cyclone  203 , and a water injector  203  as shown in  FIG. 2  and they are connected in series to allow the mixed gas G to pass through the heat exchanger  202 , the cyclone  203 , and the water injector  204  so that ash, soot, tar, or water which is very little but mixed in the mixed gas G which passed through this is removed for purification by the cyclone  203  and the water injector  204  while excess heat is removed by heat exchange in the heat exchanger  202 . At the downmost stream of the series of the heat exchanger  202 , the cyclone  203 , and the water injector  204 , a gas tank  301  for temporarily accumulating the purified mixed gas G is connected. 
     The gas tank  301  is configured to store temporarily the mixed gas G including hydrogen and carbon monoxide as its main components which were purified by passing through the cleaning up means  201  as shown in  FIG. 2  and includes a purified mixed gas inlet  302  for supplying the purified mixed gas G into inside, a mixed gas exit  303  for transferring the mixed gas G to a pressurization pump  401  connected on the downstream of the gas tank  301 , and an inlet for reintroduction of mixed gas  304  for supplying unreacted mixed gas G which finally remained unreacted in a hydrocarbon synthesis unit  501  into the gas tank  301  again. 
     The pressurization pump  401  is connected to the mixed gas exit  303  of the gas tank  301  arranged just upstream and is configured to pressurize the mixed gas G up to required pressure while allowing the mixed gas G which was temporarily stored to flow down from the gas tank  301  and feeds the mixed gas G pressurized to the required pressure to the hydrocarbon synthesis unit  501  connected on just downstream of the pressurization pump  401 , as shown in  FIG. 2 . 
     The hydrocarbon synthesis unit  501  includes, as shown in  FIG. 5 , a pressurized mixed gas inlet  510  for supplying the mixed gas G pressurized up to the required pressure by the pressurization pump  401 , a temperature adjustment means  520  for adjusting the introduced mixed gas G to appropriate temperature, and a catalyst  531  for obtaining hydrocarbon as a product by the predetermined catalytic reaction as explained above by use of the mixed gas G maintained to the appropriate temperature by the temperature adjustment means  520  while being pressurized by the pressurization pump  401 , as a reactant and has a reaction chamber  530  for the predetermined catalytic reaction of contacting the mixed gas G with the catalyst  531  under appropriate temperature and pressure, a liquidization means  540  for liquidizing the hydrocarbon generated by the catalytic reaction, and a collection means  550  for collecting the liquidized hydrocarbon liquidized by the liquidization means  540 . 
     The temperature adjustment means  520  includes constant temperature room  521  and a constant temperature room temperature adjustment unit  522  for adjusting temperature in the constant temperature room  521 . The constant temperature room  521  is partitioned and surrounded by an heat insulating material to have a predetermined volume capacity and has a pressurized mixed gas inlet  510  for supplying the mixed gas G inside thereof pressurized by the pressurization pump  401 , a temperature-controlled air inlet  523  for supplying a temperature-controlled air TA which is controlled to have a required temperature by the constant temperature room temperature adjustment unit  522 , and a temperature-controlled air exhaust  524  for discharging the temperature-controlled air TA which was introduced into the constant temperature room  521  and flew down in the constant temperature room  521 . In the constant temperature room  521 , a plurality of reaction chambers  530  are provided. That is, in the present example, first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e , which are equivalent to each other, are provided and these first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e  can be maintained in the required temperature holistically. 
     The constant temperature room temperature adjustment unit  522  includes a high temperature gas introduction line  525  for supplying a high temperature gas, an air introduction line  526 , and a temperature-controlled air feeding line  527 . The temperature-controlled air feeding line  527  generates the temperature-controlled air TA by bringing an air introduced from the air introduction line  526  into direct or indirect contact with the high temperature gas introduced from the high temperature gas introduction line  525  to control the air to have required temperature and feeds the temperature-controlled air TA into the constant temperature room  521 . Inside temperature of the constant temperature room  521  is maintained to be the required temperature by feeding an appropriate amount of the temperature-controlled air TA with appropriate temperature generated by the constant temperature room temperature adjustment unit  522  into the constant temperature room  521  and at the same time by discharging the temperature-controlled air TA from the constant temperature room  521  to flow. Thus, the mixed gas G to be introduced into the constant temperature room  521  or temperature of the first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e  can be maintained to the required temperature. Here, the combustion high temperature gas B discharged from the biomass gasification unit or the like may be used as the high temperature gas. 
     The first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e  respectively has first to fifth mixed gas inlets  533   a ,  533   b ,  533   c ,  533   d , and  533   e  respectively connected to first to fifth mixed gas introduction lines  532   a ,  532   b ,  532   c ,  532   d , and  532   e  for setting the mixed gas G pressurized to the predetermined pressure to have the predetermined temperature and for supplying the mixed gas G into first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e ; the catalysts  531  provided in the first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e  for causing the mixed gas G introduced into the first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e  to carry out catalytic reaction; and discharge lines  534   a ,  534   b ,  534   c ,  534   d , and  534   e  for discharging outside the unreacted mixed gas G which flew down the first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e  or hydrocarbon generated by the catalytic reaction. Here, the FT catalyst or the above-mentioned composite catalyst may be used as the catalyst  531 . 
     The first to fifth mixed gas introduction lines  532   a ,  532   b ,  532   c ,  532   d , and  532   e  have first to fifth temperature adjustment units  535   a ,  535   b ,  535   c ,  535   d , and  535   e  for adjusting the mixed gas G to have the required temperature by bringing the mixed gas G into indirect contact with the temperature-controlled air TA introduced into the constant temperature room  521  before the mixed gas G is introduced into the reaction chamber  530  so that the mixed gas G can be adjusted to the required temperature before the gas is respectively introduced into the first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e.    
     The first to fifth reaction chambers  530  are connected in series to gradually convert the unreacted mixed gas G which flows from upstream side to the downstream side into hydrocarbon and at the same time to reduce the amount of the unreacted mixed gas G. 
     In the hydrocarbon synthesis unit  501  of the present embodiment, the pressurized mixed gas inlet  510  is connected to the first reaction chamber  530   a  through the first mixed gas introduction line  532   a  and the first reaction chamber  530   a  is connected to the second reaction chamber  530   b  through the first liquidization chamber  541   a  connected in the downstream of the first reaction chamber  530   a  and the second mixed gas introduction line  532   b  connected in the further downstream thereof. Then, the second reaction chamber  530   b  is connected to the third reaction chamber  530   c  through the second liquidization chamber  541   b  connected in the downstream of the second reaction chamber  530   b  and the third mixed gas introduction line  532   c  connected in the further downstream thereof. Similarly, the third reaction chamber  530   c  is connected to the fourth reaction chamber  530   d  through the third liquidization chamber  541   c  connected in the downstream of the third reaction chamber  530   c  and the fourth mixed gas introduction line  532   d  connected in the further downstream thereof, and the fourth reaction chamber  530   d  is connected to the fifth reaction chamber  530   e  through the fourth liquidization chamber  541   d  connected in the downstream of the fourth reaction chamber  530   d  and the fifth mixed gas introduction line  532   e  connected in the further downstream thereof. Thus, the five-staged first to fifth reaction chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e  are set. Here, although the number of stages of the reaction chambers is set to five, it is needless to say that the stage is not limited to five and the number of stages may be designed appropriately. 
     On the downstream of the exhaust line  534   e  of the fifth reaction chamber  530   e  which discharges hydrocarbon and the unreacted mixed gas G generated in the fifth reaction chamber  530   e , the fifth liquidization chamber  541   e  is connected. 
     The liquidization means  540  includes a cooling water introduction line  542  for supplying a cooling water W and a cooling water discharging line  543  for discharging the cooling water W and has a cooling bath  544  which stores the cooling water W introduced inside. In the cooling bath  544 , the first liquidization chamber  541   a , the second liquidization chamber  541   b , the third liquidization chamber  541   c , the fourth liquidization chamber  541   d , and the fifth liquidization chamber  541   e  are provided and these first to fifth liquidization chambers  541   a ,  541   b ,  541   c ,  541   d , and  541   e  are holistically cooled down by the cooling water W which flows down in the cooling bath  544 . 
     The first to fourth liquidization chambers  541   a ,  541   b ,  541   c , and  541   d  are configured to be equivalent to each other and each of them respectively has introduction lines  545   a ,  545   b ,  545   c , and  545   d  for supplying the unreacted mixed gas G and generated hydrocarbon flown down from the first to fourth reaction chambers  530   a ,  530   b ,  530   c , and  530   d  connected to just above the stream; liquidized hydrocarbon exhausts  546   a ,  546   b ,  546   c , and  546   d  for discharging the hydrocarbon cooled and liquidized in the first to fourth liquidization chambers  541   a ,  541   b ,  541   c , and  541   d ; and cooled mixed gas exhausts  547   a ,  547   b ,  547   c , and  547   d  for discharging the mixed gas G which is gasified though being cooled to the mixed gas introduction lines  532   b ,  532   c ,  532   d , and  532   e  connected to just down the stream. 
     The fifth liquidization chamber  541   e  includes the introduction line  545   e  for supplying the unreacted mixed gas G and generated hydrocarbon flown down from the fifth reaction chamber  530   e  connected to just above the upstream; the liquidized hydrocarbon exhaust  546   e  for discharging the hydrocarbon cooled down and liquidized in the fifth liquidization chamber  541   e ; and the final unreacted mixed gas exhaust  547   e  for discharging the gasified mixed gas G which finally remained unreacted though being cooled. The final unreacted mixed gas exhaust  547   e  is connected to the mixed gas reintroduction inlet  304  of the gas tank  301  via a circulation line  548  to collect the finally unreacted mixed gas G into the gas tank  301  again and to circulate the gas. 
     The liquidized hydrocarbon liquidized by the liquidization means  540  is collected by a collection means  550  configured to have a collecting pipe shape. The collection means  550  includes a first collection pipe  551   a , a second collection pipe  551   b , a third collection pipe  551   c , a fourth collection pipe  551   d , and a fifth collection pipe  551   e  respectively connected to the liquidized hydrocarbon exhausts  546   a ,  546   b ,  546   c ,  546   d , and  546   e  of the first to fifth liquidization chambers  530   a ,  530   b ,  530   c ,  530   d , and  530   e ; a liquidized hydrocarbon extraction pipe  552  to which these first to fifth collection pipes  551   a ,  551   b ,  551   c ,  551   d , and  551   e  are connected; and a valve  553  provided in downmost stream of the liquidized hydrocarbon extraction pipe  552 , is configured to have a collecting pipe shape as a whole, and the liquidized hydrocarbon can be appropriately taken out by opening and closing control of the valve  553 . 
     As described above, since the apparatus for producing hydrocarbon from a biomass of the present invention is configured to cause catalytic reaction of unreacted mixed gas gradually by connecting a plurality of reaction chambers in series, hydrocarbon can be obtained with high yield even though it is relatively low pressured. 
     Moreover, since the present invention is configured to maintain temperature in the reaction chamber by providing the reaction chamber in the constant temperature room which temperature can be controlled easily, it becomes possible to easily maintain temperature by a simple configuration without getting the apparatus complexed. Moreover, maintenance of the apparatus is easy, the apparatus is suitable for practical use, and operational reliability as a whole of the apparatus for producing hydrocarbon from a biomass is improved. 
     Further, in the present invention, The biomass gasification unit using reaction between a raw material biomass and overheated water vapor by supplying heat from outside through a wall enables to gasify the biomass with high yield and to obtain stable production of a mixed gas including hydrogen and carbon monoxide as its main components. 
     Further, since hydrogen obtained by electrolysis of water by a recyclable energy is added to the mixed gas including hydrogen and carbon monoxide as its main components which are obtained from the biomass gasification unit, yield of hydrocarbon from the raw material biomass can be significantly increased. 
     The method and the apparatus  1  for producing hydrocarbon from a biomass of the present invention is configured as explained above. However, scope of the present invention is not restricted within the embodiments in this Description. 
     INDUSTRIAL APPLICABILITY 
     As described above, the method of the present invention provides a method for producing hydrocarbon from a biomass using hydrogen and carbon monoxide generated by use of a biomass such as grass or a tree as a raw material as a reactant and enables to synthesize liquid or gas hydrocarbon fuel as a product with a high yield while being small-sized and low pressured, and provides an apparatus thereof.