Entitled: catalysis method using a continuous fixed bed catalytic reactor and this Technical field [0001] 　The present invention relates to a technique of continuous fixed-bed catalytic reactor and a catalytic reaction method using the same for carrying out a chemical reaction of the fluid with a bulk catalyst. 　The present application, to January 20, 2012, Japanese Patent Application No. 2012-010460, filed in Japan, on January 20, 2012, Japanese Patent Application No. 2012-010464, filed in Japan, and January 20, 2012 to, claims priority based on Japanese Patent application No. 2012-010479, filed in Japan, which is incorporated herein by reference. Background technique [0002] 　In a chemical reaction of the fluid using a fixed bed catalyst reactor filled with the catalyst, when generating precipitates of a solid such as by catalytic reaction often is the solid deposits in the space between the catalyst in the catalyst layer deposition to. As a result, the catalyst layer is obstruction, a problem that can not be venting occurs. [0003] 　For example, in Patent Document 1, hydrogen, carbon dioxide, water vapor, tar-containing gas, fixed at the bed catalytic reactor, a technique of contacting the catalyst comprising nickel cerium-aluminum performs modification of Tarugasu is disclosed there. In this technique, solid carbon is deposited on the catalyst surface during the reforming, it is necessary reproduction process of contacting the steam or air to the carbon in order to remove it. [0004] 　Patent Document 1, the use of catalytic reactor moving bed type and fluidized bed type is also illustrated. In these schemes can remove the carbon deposited on the catalyst surface during the reaction process. However, such a reaction vessel, the apparatus is complicated as compared with the fixed bed catalytic reaction vessel, also tends to be unstable even operation in the case of a fluidized bed manner. Thus, in particular, not common as a reaction vessel for processing the high temperature and high pressure and highly corrosive fluids. [0005] 　On the other hand, the moving bed type and fluidized bed type catalytic reactor vessel there is no problem as described above in a fixed bed reactor, typically, a space provided on both sides of the catalyst layer, by flowing a fluid from one space to another react on. In order to form a space on both sides of the catalyst layer, the catalyst of the holding mechanism is required. Representative examples of the catalyst holding mechanism is described in Patent Document 2, than the catalyst diameter using a punching metal plate or mesh having a smaller pore diameter has secured retention and ventilation of the catalyst. Although examples of which are illustrated in FIG. 6, and catalyst 2 is housed in the catalytic reaction vessel 1, the catalyst of the holding is conducted by punching metal plate 3 and nets. 6, the material gas 4 flows from the inlet 5, flows out from the outlet 6 as a reformed gas 7. [0006] 　As it means for preventing the clogging of the catalyst layer by the deposition of solid precipitates in the reaction, for example, Patent Document 2, between the two catalyst layers in free space where the gas is vented, and flows out from the first catalyst layer gas technique for preventing clogging in the second catalytic layer by supplementing the dust in is described. In this case, however, generated inside the catalyst layer can not be prevented clogging of the catalyst layer due to dust adhering to and accumulates on the catalyst at a space between the catalysts. [0007] 　Patent Document 3, by irradiating ultrasonic waves to the catalytic layer in the cell for a fuel cell, a technique of flowing out and removing the water produced on the catalyst. However, ultrasound is greater attenuation in free space in or granule layer, the powder layer can not act only on the illumination source near. Therefore, it is effective for a relatively small as in the catalyst layer in the fuel cell, the catalyst layer of the large to handle large quantities of fluid, is difficult to vibrate the entire catalyst layer by ultrasonic it is. [0008] 　Patent Document 4, a technique for suppressing coking by implementing steam reforming of hydrocarbons at low temperatures is described. However, the catalytic reaction there is the perspective optimum reaction temperature from the catalyst durability and reaction rate, clogging of the catalyst layer due to coking is generated in the optimum condition. Therefore, when thus lowering the catalytic reaction temperature, since not the optimum conditions for the reaction, there is a problem that the catalytic performance is lowered. [0009] 　Patent Document 5, the prior art, it is described that the removal of partial obstruction of the catalyst layer by depositing dust in the moving bed catalyst reaction container by Tsuchida device and a vibrator. In this case, by hammering or vibration, the fill rate of the catalyst is increased narrowing the space between the catalyst, there is a problem that fluidity of the catalyst is rather deteriorated. [0010] 　Non-Patent Document 1, as a special fixed bed catalyst reactor, parallel flow type, a monolith type, tube wall type and the like are described. Both of these, and a catalyst layer in the catalytic reaction vessel, by providing an air flow path dedicated surrounded by a catalyst layer, thereby reducing the airflow resistance of the catalytic reaction vessel. Briefly, in the parallel flow type, arranged plurality in parallel a conventional catalyst layer was held at both ends with such a net, the space of the catalytic layers and a dedicated air flow path. The monolith type, the catalyst supported on the surface of the structure of a honeycomb structure or the like, the pores of the honeycomb structure a dedicated air flow path. In the pipe-wall, the pipe line to a dedicated air flow path, carrying the catalyst on the inner surface of the tube. [0011] 　When a dedicated air flow path of, the solid product by the catalytic reaction occurs, narrowing the flow path width of the dedicated air flow path solid product is deposited on the catalyst surface which constitutes a dedicated air flow path, it may result in obstruction is there. Alternatively, even if not causing clogging of the airflow path, the exchange of fluid in the dedicated air flow path and the catalyst layers is hampered by the solid products deposited on the catalyst surface which constitutes a dedicated air flow path, the raw material gas was retained activity catalyst results in a "blow-by" phenomenon of catalytic reaction efficiency and outflow without contact is remarkably decreased. Alternatively, a dedicated air flow path into the reaction vessel as a monolith type there are multiple, isolated each dedicated air flow path from each other (i.e., a state in which the suppression of mass transfer and heat exchange associated therewith between the adjacent air passage) and which, in a reaction vessel provided with an airflow path can not be performed the heat supply from the outside with dedicated air flow path at the deep portion of the reaction vessel, in the case of the catalytic reaction is a strong endothermic reaction, downstream by reaction of upstream fluid temperature is lowered significantly becomes the following reaction possible temperature, the reaction efficiency is extremely reduced. In the case of the catalytic reaction is strongly exothermic reaction, on the other hand, since the amount of heat generated in the deep portion of the reaction vessel can not be discharged to the outside through the reaction vessel, or deactivate the catalyst fluid temperature is excessively elevated in downstream, catalyst it may burn out the reaction vessel. [0012] 　Further, if the monoliths type, a whole generally becomes large and complicated shape monolith carrier for carrying the catalyst or, due to the need to molded as a single structure of the catalyst itself, catalyst preparation art, applied catalyst design that can be (structure) is relatively simple (for example, equal to uniformly applied to the surface of the carrier a single chemical component species of catalyst) there is a problem that is limited to. Thus, for example, as a tar reforming catalyst, the surface is complicated, such as finely divided by each species component compartment of a plurality of different chemical species component exerts a catalytic effect in cooperation with each other design (structure catalyst applying the monolith expression of) is a very difficult, also become extremely expensive as it is possible. CITATION Patent literature [0013] Patent Document 1: Japanese Unexamined Patent Publication No. 2010-77219 Patent Document 2: Japanese Unexamined Patent Publication No. 2011-6289 Patent Document 3: Japanese Unexamined Patent Publication No. 2009-48797 Patent Document 4: Japanese Unexamined Patent 2008-120604 No. Publication Patent Document 5: Japanese Unexamined Patent Publication No. 8-24622 Non-Patent Document [0014] Non-Patent Document 1: catalyst Gakkai: catalyst Lecture Volume 6 (engineering ed 2) catalytic reactor and its design, Kodansha (Tokyo), 1985, pp. 100-169 Summary of the invention Problems that the Invention is to Solve [0015] 　Thus, there is no means to effectively remove solid product formed and accumulates in a large fixed bed catalyst layer in the prior art. Accordingly, the present invention comprises a continuous fixed bed catalytic reactor having an effective means for removal of the solid product formed, deposited on large fixed-bed catalyst layer, a raw material gas using the same, particularly tar-containing material the gas, and the first object of the present invention to provide a catalytic reaction process for modifying a high efficiency. [0016] 　Further, in the prior art has the following problems. (A) In the punching metal or mesh, constraints on the intensity of the holding mechanism, the aperture ratio can not be set large (1- [opening total area] / [an apparent cross-sectional area of the flow path) (70% maximum) , prone to high air resistance and obstruction. 　Thus, for example, when the holding mechanism using a mesh, since the upper limit of the mesh mesh opening is present, no choice but to reduce the wire diameter of the wire rod constituting the network in order to increase the aperture ratio. However, the relatively high temperature operating conditions required in catalytic reactions, extremely thin wire is because it is impossible to employ because thus easily broken by contact with a reactive gas that can be included in the material gas. Since (B) openings isolated in that each hole (entire circumference of the small openings is surrounded by a solid), e.g., the case of the reforming reaction or the like with the catalyst of the source gas including tar, with the reforming reaction on gradually grow toward the aperture center to adhere to the outer periphery of each aperture of the solids fall-scattered over holding mechanism holding mechanism such as carbon generated in the catalyst surface, eventually to close the opening, It can not be ventilation. 　In particular, in order to retain the high temperature or highly corrosive fluids, Ni containing alloys (stainless steel, Inconel, Hastelloy, etc.) it is of strength and corrosion resistance over the use of, but preferably, the metal Ni are often hydrocarbons exhibits the action of the reforming catalyst to precipitate a solid such as carbon in the catalyst surface of the cage, this effect promotes the closure of the opening. 　Accordingly, the present invention is to realize a prevention of clogging and high aperture ratio in the catalyst retainer, also that thereby reforming the tar-containing gas at a high efficiency and the second object. Means for Solving the Problems [0017] 　In order to solve the above problems, the present invention adopts the following configuration. (1) a first aspect of the present invention, the outflow path of the inflow passage and the reformed gas of the source gas for catalytic reactions, is connected to the inflow passage and said outflow passage, a catalytic reaction container holding the bulk catalyst , a catalyst retainer that holds the bulk catalyst which has a gas-permeable, comprising a, a drive mechanism for raising and lowering the bulk catalyst by elevating the catalyst retainer, a continuous fixed-bed catalytic reactor. (2) above in a continuous fixed bed catalytic reactor according to (1), below the catalyst layer is a population of the bulk catalyst, for storing the contaminant solid or liquid generated in the catalyst layer it may be provided with a space. (3) in a continuous fixed bed catalytic reactor according to the above (1) or (2), at least a portion of the catalyst constituting the outer peripheral side surface of the catalyst layer may be in contact with the inner wall of the catalytic reaction vessel . (4) above (2) or in a continuous fixed bed catalytic reactor according to (3), the height of the catalyst layer is not more than 2 times the catalyst reaction vessel in thickness, and of the bulk catalyst it may be three times the maximum value of the representative length of the outer surface. (5) above (1) in a continuous fixed bed catalytic reactor according to any one of (4), the average speed at the time of descent of the drive mechanism may be faster than the average speed during ascent. (6) above (1) in a continuous fixed bed catalytic reactor according to any one of (5), the catalyst retainer, they are arranged parallel to each other, and, the bulk catalyst directly at the tip it may comprise a plurality of pins to hold the. (7) in a continuous fixed bed catalytic reactor according to the above (6), among the plurality of pins, the center distance of adjacent pins, [center distance of the pins - [outer diameter dimension of pin] clearance of the catalyst between the space] has a state of 　　　'the size of the individual deposition Carbon] <[the gap] of the catalyst between the space unless the, it can not be mass removal of carbon from the catalyst layer, backwashing of the catalyst layer by the blow from the catalyst layer outside are not effective for this. [0029] 　Accordingly then, as a second countermeasure, the reaction vessel exterior surface and Tsuchida, destruction of the deposited carbon layer, or attempted to expand the catalyst between space. [0030] 　As a result, a result Tsuchida after the first occlusion occurred (first round of hammering), can remove portions of the deposited carbon, the pressure loss is also reduced to about half, a certain effect was observed. Thereafter, again hammering after re-occlusion occurs (second round of hammering), the removal of the deposited carbon is very small, no change in the pressure loss, it was not possible to avoid clogging. That is, the hammering of the reaction vessel outer surface, the second and subsequent were found to be not effective in removing the deposition of carbon. The reason for this is that, it is considered the next thing. [0031] 　1) Usually, the causes simply fall from the upper portion when stacking the catalyst into the reaction vessel, the catalyst in the catalyst layer is not in closest packing state. Here, the addition of the first round of hammering, catalyzed by vibration to become the closest packing or state close thereto (for simplicity, will be referred to as a "close-packed prioritization" in the following). The relative position between the catalyst in the course of the closest packing of moves in the order of magnitude of 30% of the catalyst representative length in total. The movement of the relative position (ie, the catalyst between the relative movement) at the time, together with a portion of the deposited carbon to downsize been destroyed by the contact stress of the catalyst, since they produce a moment that the spacing between the catalyst is spread to temporary, 　　　[ individual size of the deposited carbon] <[clearance of the catalyst between the space] is the relationship to realize a fall the catalyst layer, has finally been removed from the catalyst layer. [0032] 　2) On the other hand, the catalyst layer after completion 1st of hammering are closest packing of the relative position between even if the hammering of the second subsequent catalyst hardly changes, destruction of the deposition of carbon It does not occur spread of spacing between and catalyst. Therefore, in the second and subsequent times of hammering effect of the removal of the deposited carbon was observed. [0033] 　These can be concluded that:. 　That is, in the obstruction effect of eliminating one-time, in many cases, can not satisfy the required processing duration in the catalytic reaction vessel, hammering of the reaction vessel surface is insufficient for continued removal of the deposited carbon . In order to continuously remove the deposited carbon from the catalyst layer, 　　　[size of each deposited carbon] <[interstices of the catalyst between the space] After the, need a way to eliminate the closest packing state of the catalytic layer it is. [0034] 　Based on the conclusions described above, as a third measure, attempted movement of the catalyst layer itself in the reaction vessel. More particularly, in a state where the catalyst is in contact with the reaction vessel inner wall in a stationary reactor (i.e., in a state where at least a portion of the catalyst constituting the outer circumferential side surface of the catalyst layer is in contact with the inner wall of the catalytic reaction vessel), I tried to raise and lower the overall catalyst layer by elevating the retainer provided on the bottom of the catalyst layer. As a result, after several lifting operations, the lifting movement of the catalyst layer reaches a steady state (after one cycle of the lifting operation, the catalyst layer is returned to the average of the state of the start point of the cycle). In this stable state, at the time of rise of the retainer towards the rise amount at the catalyst layer upper end it is generally smaller than the increase amount of the catalyst layer lower end, after descent of the cage returns to the position of the start point with the catalyst layer vertical edges. Therefore, in the cage in the elevating cycle, average and produce a variation in the fill factor of the catalyst layer (catalyst layer mean filling rate is increased when the cage increases, decreases at the time the cage descends), at least in the catalyst layer catalyst between the relative movement in the vertical direction is generated. Difference in the rise amount of the upper and lower ends of the catalyst layer at the time of the cage lift is increased as the catalyst layer height (distance between the catalyst layer top and bottom) is large, it is finally in a state that does not rise almost catalyst layer upper throughout. In the state where no movement of the catalyst layer upper end, the catalyst layer near the upper end of the catalyst is not moved by the originally retainer elevating the catalyst between the relative movement does not occur. Consequently, it can not be removed by the retainer elevating the deposition of carbon between the catalyst in this region. Therefore, in order to remove the deposited carbon between catalyzed by a cage elevating in the entire catalyst layer, the cage elevating, not only to vary the average filling factor of the catalyst layer, a sufficient lifting stroke in the catalyst layer upper It was found to be necessary to ensure. [0035] 　4, catalyst was packed to form a catalyst layer in the duct-like reaction vessel of constant rectangular cross-section of the cross-sectional area, by providing a cage below the catalyst layer in the device of mechanism for holding the catalyst layer, the holding by vessels to rise 27 mm, the catalyst layer of the stationary reactor in the stable state of the 5 times after lifting in a state in which the catalyst is in contact with the reaction vessel inner wall, the catalyst layer upper height, expressed as the displacement of the catalyst layer upper end height It is shown. The vertical axis is a catalyst layer the upper end height, 0 mm as a reference corresponds to the vertical position of the catalyst layer upper end of the front retainer increases. The catalyst layer height / reactor thick horizontal axis is an index, also referred to as "aspect ratio" of the catalyst layer in the following, the reaction vessel thickness, the shortest of the representative length of the reaction vessel in the horizontal plane in the longitudinal It corresponds to, for example, in the case a horizontal cross section of the reaction vessel is rectangular length of the shorter side, in the case of a circular equivalent to the diameter. [0036] 　From FIG. 4, of the catalyst layer aspect ratio (catalyst layer height / reaction vessel thickness)> time of 2, the amount of increase in the catalyst layer (5 times of the lifting operation after finally accepted the lift before the start of from a height increase amount) it is found to be much smaller than the cage lift amount (27 mm) and the catalyst dimensions (diameter) 15 mm. This is because when the retainer rise (ascent catalyst layer) becomes large catalyst loading rate, when the cage descends (the catalyst layer down) means that the filling rate decreases. Here, both when the cage up and down, the moving speed as the lower part of the catalyst is large, since the moving speed of each catalyst of the catalyst layer height direction it is different, resulting in the catalyst between the relative motion of at least the vertical direction. In the condition (aspect ratio> 2), the amplitude of the rise of the catalyst layer upper portion is small, the relative movement is comparatively small between the catalyst in this portion, the discharge capacity of the deposition of carbon between the catalyst is low. [0037] 　In contrast, when the aspect ratio ≦ 2 catalyst layer (aspect ratio = 1.8), the amount of increase in the catalyst layer upper end whereas slightly smaller (cage lift of 27mm, compared to the cage increases the amount, 20 mm increase in ) it can be seen. That is, in this condition, also satisfy the lifting stroke of the cage and the same level in the catalyst layer top, and, cage elevator that also ensure changes in the catalyst layer filling rate due to the catalyst between the relative movement in the catalyst layer throughout the can be realized, there is a high discharge capacity of the deposited carbon between the catalyst. [0038] 　In addition to these vertical effect of the catalyst between the relative motion, by the catalytic layer moves up and down in a state where the catalyst is in contact with the reaction vessel inner wall, between the catalyst on the thickness and width directions of the catalyst layer relative motion It can be effective to generate. That, considering the variation of catalyst between the relative position when the filling rate changes due to the elevation of the catalyst layer, restrained state for movement of each catalyst of the catalyst layer thickness direction (the reaction vessel thickness direction to the same) differs. This is due to friction with the wall surface, the more the catalyst close to the wall surface, restraint is large and is due to that the initial rise and fall speed of a small. As a result, since the moving speed of each catalyst of the catalyst layer thickness direction it is different, resulting in relative movement between the catalyst. [0039] 　Thus, when the catalyst is brought into contact with the inner wall of the container to lift the catalyst layer itself in the reaction vessel, the change of the catalyst between the relative position when the filling rate changes due to the elevation of the catalyst layer is increased, for example, cage If the lifting stroke of 30mm, is about 30% of the catalyst representative length (eg 15mm) every time the lift. [0040] 　The catalyst moves the relative position between the individual catalyst by elevating the catalyst layer itself is brought into contact with the inner wall of the vessel to a reaction vessel as described above, and stirred the whole catalyst layer deposited between the catalyst in the catalyst layer throughout solid, and carbon is deposited during the reforming reaction of gases including, for example, tar, effectively dropped from between the catalyst was found to be removed from the catalyst layer. [0041] 　The elevation rate of the catalyst, it is preferable that the average speed during descent is faster than the average speed during ascent. In particular, the cage during descent faster than the free fall velocity of the lower catalyst layer, more preferably faster than the free fall velocity of the catalyst of the catalyst layer lower end and is lowered, the catalyst layer lower end separated from the cage, cage the catalyst on the cage stopped earlier in the lower end position one after another swing accumulate, even in a catalyst layer which has been most densely reduction, the rearrangement of the catalyst, it is possible to lower the filling of. At the same time, because it can result in the moment when the gap between the catalyst during falling of the catalyst is extremely large, solid deposited between the catalyst can efficiently removed. [0042] 　In contrast, when the reaction vessel and the holding vessel was elevating at the same speed, the entire catalyst layer to lift at cage-reaction vessel at the same speed, there is no relative movement between the catalyst. Therefore, the effect of removing such solid carbon catalyst surface is low (hammering effect equivalent to that from the reaction vessel outside). In addition, the same applies to the case where to put the entire catalyst in the car, etc. at the same time lowering the basket and the catalyst layer. [0043] 　From the above, in order to remove the solid deposits to generate and deposit on the catalyst in a fixed bed catalyst layer is a catalyst layer together with the holder, it was found that it is preferable to move relative to the reaction vessel. This is the fundamental principle of the present embodiment. And according to the present embodiment, agitation of the entire catalyst layer (moving the relative position between the individual catalyst), by applying a short time in the catalytic reaction solid products such as solid carbon is produced, the catalyst layer the solid product deposited between catalyst effectively dropped from between the catalyst there is a significant effect that can be removed from the catalyst layer over the entire area. The solid product was removed from the catalyst layer can be dropped through the opening of the cage, the solid product collected in the downwardly falling can be discharged from the system, for example, during replacement of the catalyst, such as . [0044] 　According to the present embodiment can be suitably applied for the removal of solid product produced and accumulates on the catalyst in a fixed bed catalyst layer. For example, nickel, magnesium, cerium, zirconium, a composite metal oxide catalyst according reforming tar-containing gas reactions including aluminum, the deposition amount of solid carbon on the catalyst surface as compared to other reaction often is removed it needs are higher. According to this embodiment, even in the case of using the catalyst for solid carbon deposition amount is large tar-containing gas reforming on the catalyst surface reaction compared to other reaction, solid product to generate and deposit on the catalyst to enable the efficient removal of things. [0045] 　Unlike the fixed catalyst bed is the subject of the present embodiment, the moving bed is continually moves the catalyst during the reaction principle (and stirring) causes. In contrast, in this embodiment, intermittent movement of the catalyst layer in the reaction vessel, it is only necessary to practice a short time, it is not necessary to perform a catalytic stirred during the reaction. Further, in the moving bed, and it supplies the same amount of catalyst from the outside of the system as well as discharged out of the system a certain amount of the catalyst during the reaction. In contrast, in this embodiment, replacement of the catalyst is not performed in the reaction (for the catalyst layer is fixed bed). [0046] 　Further, as a fourth measure, using a "catalyst communication" as defined as aligned in a line through the center rod individual catalyst using a plurality of catalysts having an internal through-hole, a plurality of catalyst communication from defined as those formed by arranging at intervals to "catalyst fence" was placed into a catalytic reaction vessel, the space between each catalyst communication with a dedicated air flow path, and starts the operation of the catalytic reaction volume device I tried to reciprocate a short time after a predetermined time has elapsed. As a result, it was found the next thing. [0047] 　(A) in the period from the initial state of the reaction to the deposition on the catalyst surface of the reaction solid product proceeds predetermined amount, 　　　[size of each deposited carbon] <[of the catalyst between the spatial gap (width of a dedicated air flow path )] and can be realized. Therefore, it is possible to separate the deposits from the catalyst surface by solid product reciprocating the catalyst fence until depositing a predetermined amount on the catalyst. Furthermore, the solid product was detached, by dropping or pneumatic conveying through a dedicated air flow path can be discharged out of the catalytic reaction vessel. In this way, by removing the product of the catalyst surface, it is possible to return the product deposition state of the catalyst surface in the same state as the initial state of the reaction, deposition of the product with this reciprocation operation by repeating each time to proceed, it is possible to maintain the breathability of the reaction vessel always good. [0048] 　Here, according to the present embodiment, while maintaining the catalyst loading of the catalyst layer and the same level of conventional simple layered structure, the cross section of each dedicated air flow path those vast (for example, the catalyst container height in the main flow direction the level, and it can be the same level) and the catalyst cross-sectional area in the main flow vertically. Therefore, since never in a little of the product accumulation amount in the air flow path the air permeability of the reaction vessel is inhibited, the required frequency of the reciprocating movement, as possible can be reduced (e.g., once / time). This is accomplished by a catalytic layer of a conventional simple layered structure the gap between the catalyst was a large number of small spaces dispersed in each catalyst, it is consolidated into a few thick air flow path in the present embodiment, a high air permeability is because it both high catalyst loading rate. On the other hand, in the catalyst layer of the conventional simple layered structure, since a structure of individual catalyst to form and hold a support each other with the catalyst layer together, the air flow path formed between adjacent catalyst is subdivided for each catalyst prone to stenosis with are of. Such most in the narrowed portion of the air flow path in the catalyst layer, because only about 1/10 of the flow path cross-sectional area of ​​the catalyst cross-sectional area can be secured, even if the deposition of small quantities of product in the air flow path, a reaction vessel the thus ventilation resistance is rapidly increased (ventilation resistance of the air flow passage will generally depend upon the cross-sectional area at the constriction). Moreover, not limited to this method, once the air flow path in a conventional catalyst layer, when the product is deposited, since the means for removing this was not present, the likely reaction vessel resulting product by the reaction, an increase in ventilation resistance by restrictions imposed by, continuous operation can be time was very short. [0049] 　During the reciprocating motion of (b) catalyst fence, in each catalyst communication, since next to meet catalysts are not bonded to each other, resulting in easy relative movement between the catalyst (e.g., a catalyst in the pore walls, center rod in contact with this the frictional force between the surfaces varies depending on the catalyst, even when moving the center rod at a constant speed, resulting in variations in the speed of the particular catalyst being driven to the center rod). Therefore, since a collision between catalyst easily cause the product caused a strong surface vibration at each of the catalysts at the time of a collision it can be released from the catalyst surface. [0050] 　In contrast, for example, a conduit and a dedicated air flow path, to support the catalyst on the inner surface, in the case of the catalytic reaction vessel of the prior art tube-wall, because the catalyst carrier is a single structure, the reciprocating motion the entire carrier also as was not to cause a relative movement within a carrier in the only move. Therefore, the surface vibration of the catalyst becomes limited (e.g., leaves from the striking point giving partial blow vibration of the catalyst surface ends up rapidly damped. Further, an attempt to uniformly strikes the entire tube wall also, not preferable because the structure, excessively complicated mechanism), the effect of the product is released from the catalyst surface is small. The reaction vessel of the type providing other dedicated air flow path (e.g., a monolith type) But since the catalyst structure is composed of a single structure, for the same reason as the reaction vessel Kankabeshiki, efficient overall catalyst by vibrating to it is difficult. [0051] 　(C) Since the deposition of bulk product of the catalytic surface by which periodically reciprocates the catalyst fence is decreased, the raw material gas in the catalytic reaction vessel can always reach the catalyst surface. For this reason, reduction of the catalyst reaction efficiency is low. [0052] 　(D) because the only air flow path between the catalyst communication are linked to each other gas is diffused into the mainstream vertical direction of the fluid (substance exchange and heat exchange due to this) it is easy. Therefore, even for remote catalyst from the outer wall surface of the catalytic reaction vessel is a heating surface (if the catalytic reaction is endothermic reaction), can come to supply sufficient heat from the heating surface by the gas diffusion, blow less likely to occur. [0053] 　(E) In particular, the center rod of the catalyst communication and high thermal conductivity material, by heating the end portion of the center rod, to compensate for the heat absorption of the reaction by heating through a central axis distant catalyst from the wall since it is possible to avoid the reforming efficiency decrease due to catalyst low temperature and low temperature catalyst by, it can be difficult to further rise to a stairwell. [0054] 　Thus, using a plurality of catalyst communication with aligned in a row through the respective catalyst center rod, together with a dedicated air flow path the space between each catalyst communication, the catalytic reactor catalyst fence is an aggregate of the catalyst communication in by reciprocating, it is possible to obtain a remarkable effect of removing from the catalyst layer throughout the solid products deposited on the catalyst surface effectively dropped the catalyst layer in the (total catalyst fence) (catalyst fence). [0055] 　Accordingly, the present embodiment can be suitably applied for the removal of solid product produced and accumulates on the catalyst in a fixed bed catalyst layer. For example, nickel, magnesium, cerium, zirconium, a composite metal oxide catalyst according reforming tar-containing gas reactions including aluminum, the deposition amount of solid carbon on the catalyst surface as compared to other reaction often is removed it needs are higher. According to this embodiment, even in the case of using the catalyst for solid carbon deposition amount is large tar-containing gas reforming on the catalyst surface reaction compared to other reaction, solid product to generate and deposit on the catalyst to enable the efficient removal of things. [0056] 　Unlike the fixed catalyst bed, moving bed is, constantly moving the catalyst in the reaction as a general rule (and stirring) make. In contrast, according to this embodiment, intermittent movement of the catalyst layer in the reaction vessel, it is only necessary to practice a short time, it is not necessary to perform a catalytic stirred during the reaction. Further, in the moving bed, and it supplies the same amount of catalyst from the outside of the system as well as discharged out of the system a certain amount of the catalyst during the reaction. In contrast, according to this embodiment, replacement of the catalyst is not performed in the reaction (for the catalyst layer is fixed bed). [0057] (First to third embodiments) 　with reference to the accompanying drawings, it will be described in detail for the first to third embodiments of the present invention. Note that in the, components having substantially the same function and structure the following description and drawings, without redundant description by referring to the figures. [0058] (First Embodiment) (Overall Structure) 　FIG. 1A, FIG. 1B, in FIG. 1C, shows a continuous fixed bed catalytic reactor 110 according to the first embodiment of the present invention. Figure 1A is a plan view, FIG. 1B is a front view, FIG. 1C is a side view. Continuous fixed-bed catalytic reactor 110 of the present embodiment includes a reaction vessel 111, in its inside, supported by a retainer 112 having an air permeability lower, catalyst layer 113 is a population of bulk catalyst containing is, the catalyst adjacent to the reaction vessel inner wall of the catalyst in the catalyst layer 113 (not shown) is in contact with the reaction vessel inner wall. In the present embodiment, since the catalyst is contacted in a reaction vessel inner wall elevating the catalyst layer, so as not to interfere with the movement of the catalyst during the lifting operation, it is preferable that the inner surface of the reaction vessel 111 is smooth. Under the retainer 112, a catalyst layer 113 and the driving mechanism 120 is positioned to move up and down by raising and lowering the cage, the drive mechanism 120 includes a lifting device 121, the elevating device 121 in the retainer 112 It is composed of a transmission shaft 122 to be connected. [0059] 　The reaction vessel 111, a raw material gas 114 is supplied to react with the catalyst layer 113 from below, the reformed gas 115 from catalyst bed 113 is discharged from the top of the reaction vessel 111. Examples of the raw material gas 114, the gas containing a hydrocarbon, optionally the like gas containing tar along with the hydrocarbons. Examples of the reformed gas 115 may in such a reformed gas obtained by reforming a gas containing a hydrocarbon. Examples of the catalyst may like bulk catalyst for hydrocarbon reforming, solid as a by-product of the catalytic reaction on the surface, for example, solid carbon is deposited. If catalysis is endothermic reaction, the temperature and the heat required for the reaction, by placing the catalytic reaction vessel 111 for example in a heating furnace (not shown), it may be given. If catalysis of exothermic reaction, heat of reaction may be removed by passing a coolant in the coolant passage provided outside the catalytic reactor (not shown). Optionally, the raw material gas into the reaction vessel 111, FIG. 1A, FIG. 1B, in contrast to FIG. 1C, can be supplied to flow from above the catalyst layer 113 downward. [0060] (Reaction shape of the container) 　the reaction vessel 111 has an opening 116a, the 117a at both ends, the catalyst may be any shape as long as the can be stored between these openings. Opening 116a is in communication with the supply pipe constituting the inflow path 116 of the fluid catalytic reaction (raw material gas), which corresponds to the inlet of the reaction vessel 111 of the raw material gas for the catalytic reaction. Opening 117a is in communication with the discharge tube constituting the outlet passage 117 of the reformed gas of the reaction vessel 111, it corresponds to the outlet from the reaction vessel 111 of the reformed gas. The reaction vessel 111 is, for example, cylindrical, may be any shape such as rectangular duct-like. The following is a description of the square-shaped duct-like reaction vessel as an example. [0061] 　In the following description, the "center axis of the container" is defined as had been centroid of the horizontal cross section of the container in the vertical direction. "Reaction vessel thickness" corresponds to a minimum length of the representative length of the reaction vessel in the horizontal section, "reaction vessel width", the maximum length of the representative length of the reaction vessel in the horizontal plane It corresponds to. If the container is of the cylinder, the "width" and "thickness" of the container may be replaced with the "diameter". [0062] (Reactor material) 　the material of the reaction vessel 111, the strength for holding the catalyst, heat resistance and corrosion resistance to the fluid involved in the catalytic reaction, as long as the material has a stain resistance of the reaction products, What But it can be used. For example, those processed carbon steels, stainless steels, nickel alloys, copper, copper alloy, aluminum, aluminum alloy, titanium, a metal material such as titanium alloys, silica, alumina, silicon nitride, the ceramic material (brick such as silicon carbide the included), soda glass can be a glass material such as fused silica. [0063] (The dimensions of the reaction vessel) 　the thickness of the reaction vessel, the representative dimensions of the lower limit of the bulk catalyst: must (eg diameter) or more (e.g., more than 10 mm). Generally in an exothermic or absorption in catalytic reactions, and for exchanging with the outside of these heat through the surface of the reaction vessel, in order to ensure heat transfer to the interior catalytic reaction vessel, the thickness there is an upper limit. The value of the upper limit, may be determined in engineering manner by reaction heat-flow, heat transfer characteristics, and the like (for example, 200mm). [0064] 　The width of the reaction vessel, functionally, there is no particular limitation. The catalyst layer volume should be maintained, the reaction vessel thickness based on, may be determined in engineering manner taking into account the constraints on structural and strength (e.g., 5000 mm). [0065] 　The height of the reaction vessel must be greater than the height of the catalyst layer. On the other hand, the upper limit of the reaction vessel height, rather than limitations on the functions may be determined in engineering manner taking into account the constraints on structural and strength (e.g., 5000 mm). [0066] (Holder of the catalyst layer) 　in the cage 112 to support the catalyst layer 113, net, perforated metal, bar side-by-side each bar in the horizontal direction to produce the space between by using a plurality of rods rods parallel to each other and those at both ends have a fixed may be used. FIG. 1A, FIG. 1B, the cage 112 shown in FIG. 1C is an example of those prepared by fixing the opposite ends of the rods 118 in the fixture 119. [0067] 　When the aperture ratio of the retainer 112 is small, the passage of such as breathability and solid carbon worse. The high aperture ratio, in part to hold the catalyst in the cage is reduced, the strength of the cage is insufficient. The above cases of the forms of the retainer, the aperture ratio of the retainer 112 is preferably about 30-70%. [0068] 　The material of the cage 112 is preferably a metal material having heat resistance and corrosion resistance and strength. Examples of such metallic materials, stainless steel, Hastelloy (registered trademark) or Inconel (registered trademark) Ni alloy or the like, titanium, and titanium alloy. [0069] (The drive mechanism of the catalyst layer) 　In the present embodiment, elevating the catalyst layer 113 thereon in the reaction vessel 111 by raising and lowering the cage 112. For this purpose, the reaction vessel 111 of the present embodiment has a driving mechanism 120 for raising and lowering the catalytic retainer 112 is equipped. The drive mechanism 120 may be used air cylinders, such as the lifting device 121 utilizing a gear such as a rack-and-pinion, a common drive mechanism. Retainer 112 is coupled to the lifting device 121 using a transmission shaft 122. Operating the lifting device 121, moves the whole of the retainer 112 along the axis of the reaction vessel 111 is moved up and down again along the axis of the reaction vessel 111 the overall catalyst layer 113. [0070] 　At least a portion of the transmission shaft 122 retainer 112 side of the reaction vessel 111, or there is a need to be present on the inner side of the raw material gas flow path 116 and the reformed gas outflow channel 117 that may be present in the lower part of the reaction vessel 111. Lifting device 121 may be provided outside the reaction vessel 111. When placed in the reaction vessel 111 for example in a heating device such as a heating furnace (not shown) may also be provided with a lifting device 121 to the outside of the heating apparatus. In this case, while the use of a commercially available lifting device, it is preferable to seal the portion transmission shaft 122 penetrates the reactor 111 at a high temperature packing or the like. [0071] 　The entire drive mechanism 120, FIG. 1A, in the case where FIG. 1B, provided within the reaction vessel 111 as shown in FIG. 1C, the lifting device 121, for example, to protect from high temperatures or corrosive substances in the reaction vessel 111 it is preferable to that of the heat and corrosion resistance. This, as an example, the entire air cylinder drive mechanism 120 can be realized by a heat-resistant alloy such as Hastelloy (registered trademark). In this case, the supply to the air cylinder air pipe (not shown) is passing through the reaction vessel 111, because this portion is a non-moving part, may be Hakare sealing such as by circumferential welding pipes. [0072] 　When the cage increase, since a part of the cage 112 there is a case where bite into the catalyst layer 113 (in particular, then when using a pin type cage according to the second embodiment to be described), the retainer 112 is just at elevated it is preferable to also drive-time without falling. [0073] (Ascending and descending stroke of the cage) 　in order to perform sufficient relative motion between the catalyst, the ascending and descending stroke of the cage 112 is preferably greater. For example, a representative size of the catalyst outer surface: Since the effect of excitation even lifting stroke of about 0.1 times that of (for example, diameter) are present, the effect of removing sediment, such as solid carbon surface of the catalyst is approximately constant can get. Nevertheless, in order to include sufficient deposit removing effect is preferably ascending and descending stroke of the cage 112 is at least 0.5 times the catalyst outer surface representative dimension, more preferably 1 times or more. [0074] 　On the other hand, when the lifting stroke is extremely large, the reaction vessel 111 and the driving mechanism 120 is not efficient since large. Also, a small stroke (although more than one time) By repeating the lifting of the same effect as a larger lifting stroke is obtained. Therefore, the lifting stroke is preferably not more than 10 times the representative dimension of the catalyst outer surface. [0075] (Elevating speed) 　required lifting force required to raise the catalyst layer 113 along with the retainer 112 is smaller as the rising speed is smaller. Our results of the survey, the required lifting power when raising the catalyst layer together with the cage at 10 mm / s was found to be preferable to more than double when raising at 1mm / s. Further, the large increase rate, the catalyst is easily destroyed. Therefore, it is preferable rate of rise is small. However, since the difference between the required lifting power when raising the case and 0.5 mm / s to increase at 1 mm / s small, it is not always necessary to be slower than 1mm / s. Moreover, even rising speed of 10 mm / s, if the catalyst does not destroy, may be applied. [0076] 　As described above, the average speed during descent of the cage is preferably greater than the average speed during ascent. In particular, free-fall speed greater rate than the catalyst in the lowest end (example: 100mm / s) if down the cage, the catalyst is reduced restraint between the catalyst was removed from the cage, between the catalyst relative It preferred because the movement can be made large. However, there is no difference in the effect is also obtained by lowering the cage extremely at a rate greater than the free fall velocity of the catalyst. [0077] (Catalyst size) 　generally catalyst formed by supporting a material on a carrier of a porous having a catalytic action, it is necessary to remain in the catalyst layer 113 overlying the retainer 112. Therefore, the catalyst should be large enough not to pass through the opening of the retainer 112. [0078] (The shape of the catalyst) 　as described above, when holding the catalyst in a particular cage, there is a lower limit to the smallest of the representative dimension of the same catalyst outer surface. If the volume of the catalyst layer 113 is constant, generally as the number of the catalyst is large, the total surface area of the catalyst is increased, thereby improving the reaction speed of the reaction vessel 111. Thus, the catalyst of the shape close to a sphere and a sphere is preferred because easy to increase the number of catalyst in a fixed volume. Also the volume enclosed are the same at the outer circumference of the catalyst, it is greater than the shape of the surface area, for example, be preferably a cylindrical or ring-like shape. On the other hand, the rod-like or disk-like shape, so difficult to hold, not preferred. [0079] 　The ascent of the catalyst layer 113, the force acting between the catalyst toward the top in the catalyst layer is equal Kataka, vertical force comparable to the force for pushing up the catalyst layer 113 is generated in a direction other than this, frictional force proportional to the force occurs between the catalyst. The downward component of the friction force acts as a resistance force of the catalyst layer push-up. Reaction force and a catalyst between the lower side as the catalyst of the catalyst layer at the time of pushing up the catalyst layer 113 from the lower end - a large force acting between the reaction vessel inner wall. Vertical force at the catalyst layer of the rise, so it shall not be less than the sum of the vertical components of the upper resistance than that position, toward the lower side of the catalyst layer, necessary for the push-up force rapidly increased to. The maximum push force at the lower end of the catalyst layer, this force if excessive, can lead to destruction of the catalyst or the reaction vessel. [0080] 　From this viewpoint, the height of the catalyst layer, the better low. Crush strength 100 N, an angle of repose 35 ° typical catalyst (cylindrical) were directly held by the lifting tested then with pin type cage according to the second embodiment will be described. The results are shown in FIG. The horizontal axis in this figure is a catalyst layer height / the reaction vessel thickness ratio (aspect ratio of the catalyst layer), the catalyst layer pushed normalized as ordinate relative to the push-up peak load at the time of pushing up the catalyst layer in a specific condition which is the peak load. From this figure, it can be seen that the aspect ratio of the catalyst layer (catalyst layer height / the reaction vessel thickness ratio) of the load pushes exceeds 2 rapidly increased. Then, the aspect ratio of the catalyst layer (catalyst layer height / the reaction vessel thickness ratio) is equal to 2 or less, the catalyst was found that hardly destroyed. Further, as mentioned above, it is preferable that an aspect ratio in order to relative movement of the catalyst in the entire catalyst layer is 2 or less. [0081] 　On the other hand, when the catalyst layer height is too low, the relative motion between the catalyst due to the relative movement between the reaction vessel inner wall and the catalyst, is limited to near-wall reactor in the reaction vessel thickness direction, the reaction vessel thickness direction undesirable relative movement between the catalyst does not occur at the center portion. In particular, when the catalyst level is below average, the two layers of catalyst height (maximum height catalyst was stacked two in the vertical direction), the restraint of the upper layer of the catalyst is small, the catalyst is easily outermost and packing of, resulting in a further thwart the effect of relative motion so can not be low-filling of. Accordingly, the catalyst layer height 3 layer worth more than the height of the catalyst (the maximum height of the catalyst was stacked three in the vertical direction), i.e., is preferably at least three times the maximum value of the catalyst outer surface characteristic length . [0082] (Flowability of the catalyst) 　of the catalyst was increased along with the retainer 112 in the reaction vessel 111, hanging shelves in a reaction vessel (After raising the catalyst layer 113 in the retainer 112, the catalyst also lowers the cage 112 catalyst caused the self-locking of each other may cause the phenomenon) that do not fall. From the viewpoint of the shelf hanging prevention of the catalyst in the reaction vessel 111, the fluidity of the catalyst as granules group in the catalyst layer 113 is lower, it is preferable, it is preferable that an angle of repose of less than 50 °. [0083] 　On the other hand, in order to anisotropy in the catalyst layer of the force applied from the retainer during ascent of the cage 112 in the catalyst layer 113 (upward force dominant) holds up to a higher position of the catalyst layer 113, catalyst it is preferable that the liquidity is not extremely low, angle of repose is preferably at least 10 °. The wider non-isotropic regions of high force in the catalyst layer, it is possible to raise the retainer 112 with a smaller thrust, because the catalyst is not easily broken. [0084] (Material and action of the catalyst) 　materials and catalytic action of the catalyst can be applied a continuous fixed-bed catalytic reactor of the present embodiment, the fluid, especially if the catalyst used in the catalytic reaction of a gas as a raw material, any restriction Absent. Fluid is a gas, the catalyst product by catalytic reaction is a gas and solid or liquid reaction, among others, a gas fluid catalytic reaction contains a hydrocarbon, gas product by catalytic reaction and a solid or liquid catalytic reaction is, in particular, a gas fluid catalytic reaction contains tar, can be suitably used for catalyst product by catalysis is used in catalytic reactions involving carbon hydrocarbons or solid solid. [0085] 　In general, it can be widely used for oxide catalyst used in the catalytic reaction as described above, in particular a gas fluid catalytic reaction contains tar, product by catalytic reaction of the solid hydrocarbon or a solid carbon It can be suitably applied to the oxide catalyst used in catalytic reactions involving. [0086] 　Specific examples of catalysts which can be suitably used for a continuous fixed-bed catalytic reactor of the present embodiment, for example, nickel, magnesium, cerium, an oxide containing aluminum, at least one composite oxide wherein, alumina can be mentioned tar-containing gas reforming catalyst not containing a single compound (WO2010 / 134326). Suitable examples of the composite oxide, NiMgO, MgAl 2 O 4 , CeO 2 consists of crystalline phase, and further, among the crystal phases, the NiMgO crystalline phase determined by X-ray diffraction measurement (200) plane of the crystallite size is 50 nm ~ 1 nm, MgAl 2 O 4 size of 1 nm ~ 50 nm of the crystalline phase (311) plane of the crystallite, CeO 2 the crystallite size of (111) plane of the crystalline phase 1 nm ~ it is 50nm. This catalyst comprises a large amount of hydrogen sulfide which generates a carbonaceous feedstock upon thermal decomposition, even tar-containing gas easily condensed polycyclic aromatic mainly caused carbon deposition, tar, etc. accompanying heavy hydrocarbons the reformed with high efficiency, hydrogen, carbon monoxide, it is converted methane into light hydrocarbons mainly, also, when the catalyst performance is deteriorated, at least either of water vapor or air to the catalyst at a high temperature by contacting characterized in that operation that long-term stability to restore catalyst performance to remove precipitated carbon and adsorbed sulfur on the catalyst is possible. [0087] 　Further, mention may be made ​​of nickel, magnesium, cerium, zirconium, reforming catalyst of tar-containing gas, characterized by comprising a composite oxide containing aluminum (Japanese Patent 2011-212574 JP). Suitable examples of the composite oxide, NiMgO, MgAl 2 O 4 , Ce x Zr 1-x O 2 comprises a (0