JP6518108B2 - Bubble column slurry bed reactor - Google Patents

Description

  The present invention relates to a bubble column slurry bed reactor, and more particularly, to a bubble column slurry bed reactor in which a gas is caused to flow through a slurry in which a particulate solid catalyst is suspended in a solvent to catalyze hydrocarbon synthesis. About.

  The Fischer-Tropsch synthesis reaction (hereinafter referred to as "FT synthesis reaction") is a series of reaction of synthesis gas consisting of hydrogen and carbon monoxide in the presence of a solid catalyst to synthesize liquid hydrocarbons. Say the process of

  When the FT synthesis reaction is performed using a bubble column slurry bed reactor, the specific gravity of the catalyst is sufficiently larger than the specific gravity of the hydrocarbon charged as a solvent at the beginning and the hydrocarbon which is the reaction product, so It tends to settle down in the reaction column and deposit at the bottom. In order to prevent the sedimentation of the catalyst, it is necessary to eject syngas so that the catalyst floats and flows mainly by the upward flow of the slurry.

  In Patent Document 1, a reactor main body for containing a slurry in which solid catalyst particles are suspended in liquid hydrocarbon, and a lower part of the reactor main body are mainly composed of hydrogen and carbon monoxide. A reaction gas supply unit for injecting synthesis gas downward and supplying the slurry to the slurry, and a bottom portion of the reactor main body are separately disposed in the injection direction of the synthesis gas injected from the reaction gas supply unit, the flow of the slurry And a liquid hydrocarbon outlet provided at the bottom of the reactor body and discharging only the liquid hydrocarbon, wherein the barrier member is a synthetic gas injected from the reaction gas supply unit. And a filter element installed parallel to a horizontal plane perpendicular to the height direction of the reactor body and limiting the flow of only the catalyst particles in the slurry. Do Foam column type hydrocarbon synthesis reactor is disclosed.

Patent Document 2 discloses a slurry zone arranged to accommodate a predetermined amount of slurry consisting of a liquid phase in which solid catalyst particles are suspended during use, a gas space above the slurry zone, and a gas. A slurry bubble column reactor comprising a gas supply arranged to supply the slurry to the slurry zone, a gas outlet from the gas space, and a liquid outlet, said gas supply comprising: Means and a set of gas nozzles, the gas supply / distribution means being arranged to deliver gas to the set of gas nozzles, the openings of the nozzles being open downwards, In use, gas is injected into the slurry zone of the reactor to form a gas jet extending down the length L into the slurry, the number and configuration of the nozzles being across the reactor surface In, 1 m ² per 75 amino are selected to provide a distribution of the nozzle corresponding to the minimum density of uniformly distributed nozzle, the opening of each nozzle, the reactor length from the bottom in the perpendicular direction of D A slurry bubble column reactor is disclosed, which is located at: D = 0.75 to 1.5 L.

Patent No. 4874660 Patent No. 5242157

  However, the bubble column type hydrocarbon synthesis reactor described in Patent Document 1 is equipped with a screen between the reaction gas supply unit and the bottom of the reactor body to restrict the flow of the slurry and allow only the liquid hydrocarbon and the bubbles to pass. It is necessary to provide a barrier member, and a part of the reaction gas injected downward passes through the screen, which restricts the rolling-up power of the catalyst particles and inhibits the flow of a good slurry, or a minute catalyst. The particles clogged the screen, requiring frequent maintenance.

  In addition, the gas supply device installed in the bubble column type hydrocarbon synthesis reactor disclosed in Patent Documents 1 and 2 is provided with a large number of gas nozzles that eject gas toward the barrier member or the bottom surface of the reactor body. Since the gas flow injected from each gas nozzle and deflected upward at the barrier member or the bottom surface causes the slurry to flow upward while interfering with each other, the upward flow and the downward flow of the slurry interfere with each other to cause the slurry inside the reactor body. Not only is the flow non-uniform, there is also a loss in energy for flowing the slurry, and there is also a problem that there is a possibility that the contact opportunity between the gas for FT synthesis and the catalyst may be limited.

  In view of the above-mentioned problems, it is an object of the present invention to provide a bubble column type slurry bed reactor which can ensure good fluidity of the catalyst inside the reaction tower and sufficient contact opportunity between the synthesis gas and the catalyst. It is in.

In order to achieve the above-mentioned objects, the first feature of the bubble column slurry bed reactor according to the present invention is the catalyst particles solid in liquid hydrocarbon as described in claim 1 of the claimed document. , A synthesis gas supply unit disposed in the lower portion of the reaction tower for supplying synthesis gas, and gaseous hydrocarbons produced from the synthesis gas disposed in the upper portion of the reaction tower The bubble column slurry bed reactor comprises a gas outlet for discharging the gas and a plurality of cooling members disposed inside the reaction tower, wherein the synthesis gas supply unit guided inside the reaction tower, at 0 ° <θ <45 inclination angle between ° theta with respect to the vertical downward direction, a plurality of nozzles for ejecting the synthesis gas in one direction in the circumferential direction of the reaction column but it is formed in an annular region around the axis of the reactor It lies in the fact that.

  Slurry containing catalyst particles on the bottom surface by synthesis gas injected toward the same circumferential direction at an inclination angle θ between 0 ° <θ <45 ° with respect to the vertically downward direction from the nozzle provided in the synthesis gas supply unit Is rolled up along the circumferential direction, and further swirls in the circumferential direction inside the reaction tower and rises, so that the energy possessed by the synthesis gas is efficiently used to form the upward flow of the slurry. Further, even when the supply of the reaction gas is stopped, since the nozzle is formed in the synthesis gas supply unit so that the nozzle is inclined to the vertically downward direction, the slurry which settles thereafter flows from the nozzle into the inside of the synthesis gas supply unit There is no such thing as an obstruction.

According to the second feature, as described in claim 2, in addition to the above-mentioned first feature, the synthesis gas supply unit is between 5 ° ≦ θ ≦ 15 ° with respect to the vertically downward direction. At an inclination angle θ, a nozzle is formed to eject the synthesis gas in one circumferential direction of the reaction tower .

  When the nozzle is formed at an inclination angle θ between 5 ° ≦ θ ≦ 15 ° with respect to the vertically downward direction, particularly, good flow performance of the slurry can be obtained.

  According to the third aspect, as described in the second aspect, in addition to the above-mentioned first or second aspect, the reaction tower is provided with a rising region in which the slurry mainly rises, and a rising slurry Is mainly divided into a descending region where the nozzle falls, and the nozzle is formed in the synthesis gas supply unit so as to be located below the ascending region.

  By positioning the nozzle below the rising region where the slurry mainly rises in the reaction tower, a good flow of slurry containing catalyst particles is efficiently formed toward the rising region, and the resistance to the downward flow in the falling region As a result, it is possible to quickly lower to the bottom and to form a good circulation path in which the lowered slurry rapidly moves to the rising region side at the bottom.

  According to the fourth feature, as described in the fourth aspect, in addition to the first or second feature described above, the cooling member forms a tubular shape in a posture along the axis of the reaction tower. The synthetic gas supply unit is disposed below the cooling member.

  Since the FT synthesis reaction generated by the contact between the catalyst in the slurry flowing inside the reaction tower and the synthesis gas is an exothermic reaction, a cooling member is installed inside the reaction tower to continuously remove the heat of reaction. There is. Since the synthesis gas supply unit is disposed below the cooling member, a good slurry flow can be formed without impeding the flow of synthesis gas injected from the nozzle.

  According to a fifth feature of the present invention, in addition to the fourth feature described above, the nozzle has a cylindrical shape formed by at least the cooling member in the axial center direction of the reaction tower. Is located in the outer area of the

  When the nozzle is disposed in the cylindrical outer region formed by the cooling member in the axial direction of the reaction tower, the rising member of the slurry generated by the synthetic gas injected from the nozzle is blocked by the cooling member. There is no such thing as

  According to the sixth aspect, as described in the sixth aspect, in addition to the fifth aspect, the rising area and the falling area are divided by the cooling member, and the nozzle is the rising area. It is in the point formed in the above-mentioned synthetic gas supply part so that it may be located below.

  Since the rising flow of the slurry is formed along the rising region partitioned by the cooling member, it is not necessary to provide a separate guiding member for dividing the rising region.

  According to a seventh aspect of the present invention, in addition to any of the fourth to sixth features described above, as described in the seventh aspect of the present invention, the rising area is formed in the cylindrical outer area formed by the cooling member. Is formed in the inner area, and the nozzle is formed in the synthesis gas supply unit such that the nozzle is located below the rising area.

  The swirling upflow of the slurry is formed in the cylindrical outer region according to the flow of the synthesis gas injected from the nozzle located below the cylindrical outer region formed by the cooling member, thereby promoting the FT reaction. The raised slurry descends in the cylindrical inner region, settles to the bottom of the reaction tower, and is circulated again to rise in the rising region.

  According to an eighth characterizing feature of the present invention, in addition to the seventh characterizing feature as described in claim 8, further, a guide nozzle for guiding the lowered slurry to the rising region is provided to the synthesis gas supply unit. The guide nozzle is provided below the descent region, and the guide nozzle is formed to eject the synthesis gas in the same circumferential direction as the nozzle and toward the ascending region.

  The slurry containing the catalyst particles which has fallen to the bottom of the reaction column by descending the descending region is pushed out to the ascending region by the flow of synthesis gas jetted from the guide nozzle and follows the flow of the gas flow of synthesis gas jetted from the nozzle Since the catalyst rises while swirling in the rising region, the catalyst flows stably while being well dispersed in the reaction tower.

  According to the ninth characteristic configuration, as described in the ninth aspect, in addition to any of the above-described first to eighth characteristic configurations, formation of a nozzle in which the lowered slurry is formed at least in the synthesis gas supply unit An inclined guide portion is formed on the bottom of the reaction tower so as to be guided to an area enveloping the position.

  The catalyst particles which may settle or settle at the bottom of the reaction column move along the inclined guide to the area enveloping the position where the nozzle is formed, so that the gas flows efficiently by the syngas gas jetted from the nozzle It will be.

  In addition to the above-described sixth to eighth features, as in the tenth aspect, in the tenth aspect, the reaction is performed so that the lowered slurry is guided to the rising region. It is in the point where the inclined guide part is formed in the bottom of the tower.

  The catalyst particles which may settle or settle at the bottom of the reaction tower are guided along the inclined guide portion to the ascending region, so that they flow efficiently by the gas flow of synthesis gas jetted from the nozzles.

  As described above, according to the present invention, it is possible to provide a bubble column type slurry bed reactor capable of ensuring good fluidity of the catalyst inside the reaction tower and sufficient contact opportunity between the synthesis gas and the catalyst. It became so.

Illustration of FT synthesizer (A) is a longitudinal cross-sectional explanatory view of a bubble column type slurry bed reactor according to the present invention, (b) is a cross-sectional explanatory view of the same device Cross section of the main part of bubble column type slurry bed reactor Explanatory view of the synthesis gas supply unit viewed from the bottom of the reaction tower (A), (b), and (c) show another embodiment, and are explanatory drawings of the synthesis gas supply part seen from the bottom of the reaction tower Explanatory drawing of the synthetic gas supply part which showed another embodiment and was seen from the bottom of the reaction tower. (A), (b) and (c) are principal part explanatory drawing of the reaction tower which shows another embodiment Principal part explanatory drawing of the reaction tower which shows another embodiment (A) to (e) illustrate the nozzle Experiment explanation

Hereinafter, an embodiment of a bubble column type slurry bed reactor according to the present invention will be described.
As shown in FIG. 1, the FT synthesis device 14 includes a compressor 15, a heater 16, a reactor 17, and a condenser 18.

Impurities-free synthesis gas (H ₂ , CO) is compressed by the compressor 15 to about 0.9 MPa, and the compressed synthesis gas (H ₂ , CO) is heated by the heater 16 to about 280 ° C. Thus, the synthesis gas (H ₂ , CO) in the high temperature and high pressure state is sent to the reactor 17, that is, the bubble column slurry bed reactor 17. The heating by the heater 16 is used at the time of start-up where no exothermic reaction occurs in the reactor 17, and the heater 16 is turned off when the FT synthesis starts.

In the bubble column type slurry bed reactor 17, the synthesis gas (H ₂ , CO) in a high temperature / high pressure state is injected into a slurry-like solvent in which catalyst particles such as iron and cobalt are dispersed and contacted with the catalyst. In the form of synthetic hydrocarbons.

The gaseous synthetic hydrocarbon produced in the bubble column slurry bed reactor 17 is sent to the condenser 18 to be indirectly cooled and condensed, and recovered as a liquid synthetic hydrocarbon. At the same time, unreacted synthesis gas (H ₂ , CO) and light gases such as methane and ethane are separated and recovered. In the present embodiment, liquid gas oil is synthesized and recovered using H ₂ and CO as synthesis gas.

  As shown in FIGS. 2 (a), (b) and FIG. 3, the bubble column type slurry bed reactor 17 is composed of a substantially cylindrical metal container and is a liquid hydrocarbon (for example, polyalpha) as a solvent. A reaction tower 21 containing a slurry in which solid catalyst particles are suspended in an olefin), a synthesis gas supply unit 22 disposed at a lower portion of the reaction tower 21 and supplying synthesis gas to the slurry, and a reaction gas And a plurality of cooling pipes 24 disposed inside the reaction tower 21. The gas discharge unit 23 discharges the gaseous synthetic hydrocarbon generated from the synthesis gas. Although not shown in FIG. 2, the reaction tower 21 is provided with a slurry inlet and outlet, and a plurality of temperature sensors and pressure sensors. The cooling pipe 24 functions as a cooling member of the present invention.

  The FT synthesis reaction generated by the contact between the catalyst in the slurry flowing inside the reaction tower 21 and the synthesis gas is an exothermic reaction, and the cooling pipe serving as the cooling member of the present invention to continuously remove the heat of reaction. 24 are installed. Specifically, four double-pipe cooling pipes 24 are disposed at predetermined intervals so as to form a cylindrical shape around the vertical axis of the cooling pipe 24 in a posture along the axial center of the reaction tower 21, The cooling medium flowing from the outer pipe 24a above the reaction tower 21 descends while exchanging heat in the reaction tower 21, and rises from the bottom opening of the inner pipe 24b and flows out to the outside. Here, cooling water, air or the like is used as a cooling medium.

  The number of cooling pipes 24 is not limited to four, and may be plural. Also, although an example in which a cylindrical or square cylinder is formed by four cooling pipes 24 is described, depending on the number of cooling pipes, any type of cylinder such as an octagonal cylinder besides a cylinder or a square cylinder It may be formed in a shape.

  An annular rising region R1 in which the slurry mainly rises is formed in a cylindrical outer region 31 formed of a plurality of cooling pipes 24, and a cylindrical falling region in which the slurry mainly falls in the cylindrical inner region 32. The regions are partitioned such that R2 is formed.

  The synthesis gas supply unit 22 is disposed below the lower end of the cooling pipe 24. The synthesis gas supply unit 22 guides the synthesis gas to the inside of the reaction tower 21. The synthesis gas supply unit 22 has one end connected to the gas supply main pipe 22A. And a gas supply branch pipe 22B.

  Each gas supply branch pipe 22B is formed to extend in a direction orthogonal to each other in plan view at a position separated from the bottom surface of the reaction tower 21 by a predetermined distance, and an inclination angle between 0 ° <θ <45 ° with respect to the vertically downward direction At θ, a nozzle 22N that ejects synthesis gas in the same circumferential direction is formed to be located below the rising region R1. As described later, since the boundary between the rising area R1 and the falling area R2 is not clear, the nozzle 22N located below the rising area R1 may be located near the lower side of the rising area R1.

  The two-dot chain line L1 and L2 shown in FIG. 3 indicate the boundary between the rising region R1 and the falling region R2, and the two-dot chain line L3 indicates the lower end position of the cooling pipe 24. The slurries in the rising region R1 and the falling region R2 do not move completely independently, nor do they have a mutual dependency. The slurry in the two regions will have a weak dependence which diffuses mutually through the gaps of the adjacent four cooling pipes 24. Therefore, L1 and L2 do not necessarily have clear lines.

  As shown in FIG. 4, the slurry containing the catalyst particles on the bottom of the reaction tower 21 is wound up along the circumferential direction by the synthetic gas injected from the nozzle 22N in the same circumferential direction inside the reaction tower 21, Furthermore, it rises as it swirls in the circumferential direction inside the reaction tower 21, and the energy possessed by the synthesis gas is efficiently used to form the upward flow of the slurry. The rising flow is not only swirling and rising flow, but also may be generated by the air lift effect of synthesis gas in the slurry.

  Further, the distance from the bottom of the reaction tower 21 to the gas supply branch pipes 22B depends on the jet velocity of the synthesis gas from the nozzles, but the closer the distance is, the stronger the winding force becomes.

  As a result, a good flow of the slurry including the catalyst toward the rising region R1 including the lower portion of the falling region R2 is efficiently formed, and the resistance to the downward flow is decreased in the falling region R2 so that it rapidly falls to the bottom surface. As a result, a good circulation path is formed in which the lowered slurry moves quickly to the rising region side at the bottom.

  Further, even when the supply of the reaction gas is stopped, the nozzle 22N is formed in the gas supply branch pipe 22B so that the nozzle 22N is inclined at an angle θ with respect to the vertically downward direction. It does not flow into the inside of the branch pipe 22B and cause blockage.

  Further, since the rising region R1 and the falling region R2 are divided by the cooling pipe 24, it is not necessary to separately install a dedicated guide plate or the like for dividing the region inside the reaction tower 21.

  Since the synthesis gas supply unit 22 is disposed below the cooling pipe 24, the slurry flows well without the flow of the synthesis gas injected from the nozzle 22N being blocked by the cooling pipe 24.

  As shown in FIG. 5A, the gas supply branch pipe 22B is provided with a guide nozzle GN for guiding the slurry lowered to the bottom of the reaction tower 21 to the rising region R1 so as to be located immediately below the falling region R2. Is preferred. Even if catalyst particles contained in the slurry precipitated along the falling area R2 are deposited or deposited on the bottom surface, they are transported to the rising area by the synthesis gas ejected from the guide nozzle GN, and are again raised by the nozzle 22N. Will be rolled up.

  As shown in FIG. 5B, it is preferable that the guide nozzle GN be formed so as to eject the synthesis gas to the rising region R1 in the same circumferential direction as the nozzle 22N. The slurry containing the catalyst particles which has fallen to the bottom of the reaction tower 21 by descending the descending region R2 is pushed out to the ascending region R1 side by the flow of synthesis gas injected from the guide nozzle GN, and the synthesis gas injected from the nozzle 22N As the gas flows upward while swirling in the rising region R1, the catalyst particles are stably dispersed while being well dispersed in the reaction tower.

  As shown in FIG. 5C, the gas supply branch for the guide nozzle GN may be separately provided. As described above, the catalyst particles can be pushed out to the rising region R1 side by injecting the synthesis gas from the guide nozzle GN to a place where settling is easier.

  The number of gas supply branch pipes 22B described above is not limited to four, and may be two or more, and the number of nozzles 22N and the number of guide nozzles are not particularly limited. Further, the gas supply branch pipe 22B and the cooling pipe 24 may be arranged to overlap in a plan view.

  As shown in FIG. 6, the gas supply branch pipe 22B does not have to be a straight pipe, and is constituted by an annular pipe 22B, and in the annular pipe 22B, a plurality of nozzles 22N are directed in the same direction in the circumferential direction of the reaction tower 21. It may be configured to inject syngas. The number of such annular tubes does not have to be one, and a plurality of annular tubes may be provided concentrically.

  As shown in FIG. 7A, the slurry which has descended from the descending area R2 to the bottom surface is guided to at least the area enveloping the formation position of the nozzle 22N formed on each gas supply branch 22B, preferably an annular area. Preferably, the inclined guide portion GP is formed on the bottom of the reaction tower 21. In addition, although the inclination guide part GP may be formed by a plane, as shown in FIG.7 (b), it may be formed by a concave phase, and as shown in FIG.7 (c), it is a convex phase. It may be formed.

  The catalyst particles which have settled or are likely to settle at the bottom of the reaction tower 21 move along the inclined guide portion GP to an annular region enveloping the formation position of the nozzle 22N, so the gas flow of synthesis gas injected from the nozzle Will flow efficiently.

  Furthermore, as shown in FIG. 8, the inclined guide portion GP may be formed on the bottom surface of the reaction tower 21 so that the slurry dropped from the falling region R2 to the bottom surface is guided to the rising region R1.

  The nozzle 22N formed in each gas supply branch is configured to eject the synthesis gas in the same circumferential direction at an inclination angle θ between 5 ° ≦ θ ≦ 15 ° with respect to the vertically downward direction Is more preferable in that the flowability of the slurry is better.

  The inner region of the cylindrical cooling pipe 24 may be configured as the rising region R1 of the slurry, and the outer region may be configured as the falling region R2 of the slurry.

  A dedicated guide member may be provided which divides the rising region R1 in which the slurry mainly rises and the falling region R2 in which the rising slurry mainly drops. The guide member may be formed of a plate-like body connecting cooling pipes using a cooling pipe, a baffle pipe inserted between the cooling pipes, and the like.

Below, the result of having conducted experiment which confirmed the flow performance of the catalyst in a slurry using the bubble column type slurry bed reactor mentioned above is demonstrated.
The flow fraction ratio of the catalyst is obtained by sampling the slurry from each of the top, middle, bottom, and bottom along the height direction of the reaction tower during the test and measuring each existing ratio (wt%), except for the bottom It is the total value of the proportion of catalyst present. That is, it can be determined that the catalyst does not stay at the bottom and is distributed throughout the slurry as the flow fraction ratio increases. The direction of the nozzle of the gas injection unit is set vertically downward, and the cooling pipe is not disposed in the reaction tower.

  In FIG. 10, the number of nozzles 22N and the inclination angle θ with respect to the vertical lower side are made different from each other in the shape of the gas injection section (gas supply branch pipe 22B) as shown in FIG. The experimental conditions and experimental results of the fluid fraction ratio test of the case are shown.

  The details of the angles and numbers of the nozzles corresponding to the branch pipes a to e shown in FIG. 10 are shown in FIGS. 9 (a) to (e). The branch pipe a is a single nozzle directed vertically downward, the branch pipe b is a single nozzle with an inclination angle θ of 5 degrees with respect to the vertical downward, and the branch pipe c is a double with a nozzle respectively at a position inclined vertically downward and 90 degrees The nozzle and the branch pipe d are double nozzles inclined 45 degrees to the both sides from the vertical lower side, and the branch pipe e is a double nozzle with two nozzles inclined 5 degrees to the one side from the vertical lower side.

  It can be understood from this test that the flow ratio of the catalyst is good as compared with the branch pipe e. In addition, when the conditions were further changed and the test was advanced, a nozzle is formed which ejects synthesis gas in the same circumferential direction at an inclination angle θ between 0 ° <θ <45 ° with respect to the vertically downward direction. When this is done, a good flow fraction of catalyst can be obtained, and a nozzle is formed that ejects synthesis gas in the same circumferential direction at an inclination angle θ between 5 ° ≦ θ ≦ 15 ° with respect to the vertically downward direction. As it was, an even better catalyst flow rate was obtained.

  In each of the above-described embodiments, the nozzle for ejecting the synthetic gas is formed by drilling a hole in the pipe, but any nozzle having a structure that can eject the synthetic gas, such as a commercially available fluid nozzle, may be used.

  The various embodiments described above only describe one specific example of the bubble column type slurry bed reactor according to the present invention, and the scope of the present invention is not limited by the description, and the specific configuration of each part is It is needless to say that appropriate design changes can be made as long as the effects of the present invention are exhibited.

14: FT synthesis apparatus 15: Compressor 16: Heater 17: Reactor (bubble column type slurry bed reactor)
18: Condenser 21: Reaction tower 22: Synthetic gas supply unit 22A: Gas supply main pipe 22B: Gas supply branch 22N: Nozzle 23: Gas discharge unit 24: Cooling pipe 31: Outer region 32: Inner region GN: Guide nozzle R1: Rising area R2: falling area

Claims (10)

A reaction tower containing a slurry of solid catalyst particles suspended in liquid hydrocarbon;
A synthesis gas supply unit disposed at a lower portion of the reaction tower to supply synthesis gas;
A gas discharge unit disposed at an upper portion of the reaction tower and discharging a gaseous hydrocarbon generated from synthesis gas;
A plurality of cooling members disposed inside the reaction tower;
A bubble column type slurry bed reactor comprising:
The synthesis gas supply unit guides the synthesis gas to the inside of the reaction tower, and in one direction in the circumferential direction of the reaction tower, at an inclination angle θ between 0 ° <θ <45 ° with respect to the vertically downward direction . A bubble column type slurry bed reactor, wherein a plurality of nozzles directed to jet the synthesis gas are formed in an annular region around the axis of the reaction tower . The synthesis gas supply unit is formed with a nozzle that ejects the synthesis gas toward one direction in the circumferential direction of the reaction tower at an inclination angle θ between 5 ° ≦ θ ≦ 15 ° with respect to the vertically downward direction. The bubble column type slurry bed reactor according to claim 1.   The reaction tower is divided into a rising region where the slurry mainly rises and a falling region where the raised slurry mainly falls, and the synthesis gas supply unit is positioned such that the nozzle is located below the rising region. The bubble column type slurry bed reactor according to claim 1 or 2, which is formed in   The cooling member is disposed at a predetermined interval so as to form a cylindrical shape in a posture along the axis of the reaction tower, and the synthesis gas supply unit is disposed below the cooling member. 2. The bubble column type slurry bed reactor according to 2.   The bubble column type slurry bed reaction apparatus according to claim 4, wherein the nozzle is disposed in a cylindrical outer region formed by at least the cooling member in the axial direction of the reaction column.   The bubble column slurry bed reactor according to claim 5, wherein the rising area and the falling area are sectioned by the cooling member, and the nozzle is formed in the synthesis gas supply unit so as to be located below the rising area. . The rising area is formed in a cylindrical outer area formed by the cooling member, and the falling area is formed in an inner area,
The bubble column type slurry bed reactor according to any one of claims 4 to 6, wherein the nozzle is formed in the synthesis gas supply unit so as to be located below the rising region.   Furthermore, the synthetic gas supply unit is provided with a guide nozzle for guiding the lowered slurry to the rising area so as to be located below the falling area, and the guide nozzle is in the same circumferential direction as the nozzle and to the rising area. 8. The bubble column slurry bed reactor according to claim 7, wherein the bubble column slurry bed reactor is formed to direct synthesis gas.   9. The inclined guide portion is formed on the bottom surface of the reaction tower so that the lowered slurry is guided to a region enveloping at least the formation position of the nozzle formed in the synthesis gas supply portion. The bubble column type slurry bed reactor according to claim 1. The bubble column type slurry bed reactor according to any one of claims 6 to 8, wherein an inclined guide portion is formed on a bottom surface of the reaction tower so that the lowered slurry is guided to the rising region.

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