JP7057050B2 - Processing gas reaction tower - Google Patents

Description

The present invention relates to a processing gas reaction tower for circulating a processing gas to a processing agent, and more particularly to a processing gas reaction tower applied to an impurity removing device in a dry gas refining facility provided in an integrated coal gasification combined cycle facility.

Integrated coal gasification combined cycle (IGCC) is known as one method of thermal power generation using coal as fuel. In integrated coal gasification combined cycle, a gas turbine is driven by using coal gasification gas as fuel to obtain electric power, and the exhaust heat of the gas turbine is recovered to generate steam, and the generated steam drives the steam turbine to generate electric power. Is getting.

Since the coal gasification gas generated in the coal gasification furnace contains impurities such as halogen compounds, ammonia, and sulfur compounds (sulfides), impurities that affect subsequent equipment, and trace components, gas purification equipment The impurities of the coal gasification gas are removed to make the fuel gas.

The gas refining facility is provided with a reaction tower for removing impurities from coal gasification gas, and the inside of the reaction tower is filled with a processing member for removing impurities to form a packed bed (a packed bed is formed). For example, a packed layer having a honeycomb lattice structure). It is preferable that the coal gasification gas sent to the reaction tower reduces the pressure loss as much as possible so that the coal gasification gas flows evenly throughout the packed bed.

In particular, in a reaction tower provided with a packed bed having a honeycomb lattice structure, the coal gasified gas is uniformly flowed, so that even a small packed bed can be supported by a catalyst with extremely little pressure loss. Good contact with the absorbent is maintained and an efficient reaction is possible.

As a technique for preventing the uneven flow of gas flowing through the pressure vessel, in the case of using a granular adsorbent, the adsorbent is pressed against the elastic body on the wall surface of the vessel by a pressurizing means to eliminate the voids between the particles and adsorb the gas. A technique for adsorbing to an agent has been conventionally known (Patent Document 1).

In the technique of Patent Document 1, it is possible to suppress a decrease in the adsorption efficiency of impurities due to gas flowing through the gaps between the granular adsorbents. However, in the case of a granular adsorbent, the gas naturally diffuses. Therefore, in the technique of Patent Document 1, it is not considered to equalize the gas over the entire pressure vessel, and the gas is brought into contact with the surface. The fact is that it cannot be applied as a technique for suppressing drift in a treatment agent such as a catalyst for adsorbing gas. In other words, since it is not a technique for equalizing the inflowing gas, there is a limit to the applicable treatment agents.

Japanese Unexamined Patent Publication No. 2009-29977

The present invention has been made in view of the above circumstances, and an object of the present invention is to provide a treated gas reaction tower capable of evenly distributing the treated gas flowing into the container.

The processing gas reaction tower of the present invention according to claim 1 for achieving the above object has a hemispherical inlet portion and a tubular portion continuous with the inlet portion, and the tubular portion is filled with a processing agent. The container body is provided at the top of the inlet and the container body, which introduces the treatment gas from the inlet and circulates the treatment gas to the treatment agent, and the tip is arranged so as to face the inside of the inlet. Control to control the flow direction of the processing gas by interfering with the inflow pipe that introduces the processing gas into the inside of the container body and the processing gas that is attached to the tip of the inflow pipe and is sent from the inflow pipe. The control plate has a plate surface having a diameter larger than the diameter of the inflow pipe and orthogonal to the axial direction of the inflow pipe, and the processing gas is applied to the hemispherical inner surface of the inlet portion. It is characterized in that a spiral flow is formed by contacting the gas and the flow direction of the processing gas is controlled.

In the present invention according to claim 1, the processing gas introduced from the inflow pipe interferes with the control plate and the flow direction is controlled so as to come into contact with the hemispherical inner surface of the inlet portion. By bringing the processing gas into contact with the inner surface of the hemispherical inlet, the processing gas is evenly dispersed in the radial direction of the cylinder along the inner surface of the hemisphere, and the distribution of the flow condition of the processing gas flowing through the cylinder (flow velocity). Distribution) is suppressed.

As a result, the processing gas flowing into the container can be evenly distributed, and the processing gas can be evenly contacted regardless of the mode of the processing agent. In particular, by applying it to a packed layer having a honeycomb lattice structure, it is possible to make the flow of the inflowing processing gas uniform, reduce the flow velocity distribution, and evenly distribute the processing gas throughout the packed layer having a honeycomb lattice structure. The value of the diameter of the inflow pipe with respect to the value of the diameter of the cylinder portion of the container body is set in the range of 5% to 30%.

Various techniques for suppressing the drift of the processing gas by using a jam plate have been proposed (for example, JP-A-2000-179830 and JP-A-2013-199979). However, these techniques are techniques for rectifying the processing gas in the flow direction, and are different from the techniques for equalizing the flow of the processing gas in the pressure vessel provided with the hemispherical inlet portion. For this reason, a technique different from the mechanism of suppressing and equalizing the distribution of the flow of the processing gas (distribution of the flow velocity) by abutting the processing gas on the inner surface of the hemisphere to form a spiral flow. It is the content.

The treated gas reaction tower of the present invention according to claim 2 is the treated gas reaction tower according to claim 1, wherein the control plate has an inclined portion inclined toward the top of the inlet portion around the control plate. It is characterized by being formed.

In the present invention according to claim 2, the processing gas introduced from the inflow pipe interferes with the control plate and flows, and is directed to a position closer to the top side of the inner peripheral surface of the inlet portion along the inclined portion. As a result, the processing gas abuts on the arcuate inner peripheral surface of the inlet portion, and mainly flows downward in an arcuate shape, so that a vortex-like flow can be formed.

The treated gas reaction tower according to claim 3 is the treated gas reaction tower according to claim 2, wherein the inclined portion of the control plate is between 30 degrees and 70 degrees toward the top of the inlet portion. It is characterized in that it is formed at the angle of.

In the present invention according to claim 3, the processing gas introduced from the inflow pipe is directed to an appropriate position on the inner peripheral surface of the inlet portion along the inclined portion formed at an angle between 30 degrees and 70 degrees. The gas is brought into contact with the arcuate inner peripheral surface of the inlet portion, and a spiral flow mainly flowing downward is formed, so that the processing gas can be evenly distributed in the radial direction of the tubular portion.

The treated gas reaction tower according to claim 4 is the treated gas reaction tower according to claim 3, wherein the inclined portion of the control plate is between 45 degrees and 55 degrees toward the top of the inlet portion. It is characterized by being formed at an angle.

In the present invention according to claim 4, the processing gas introduced from the inflow pipe is arcuate toward the inner peripheral surface of the inlet portion along the inclined portion formed at an angle between 45 degrees and 55 degrees. A large vortex-like flow that flows downward is formed, which abuts on the inner peripheral surface of the cylinder, suppresses the distribution of the flow state of the processing gas (distribution of flow velocity) in the radial direction of the cylinder, and evenly distributes the processing gas. Can be distributed to.

Further, the processing gas reaction tower according to claim 5 is the processing gas reaction tower according to claim 2, wherein the control plate is formed with a variable inclination angle of the inclined portion.

In the present invention according to claim 5, by changing the inclination angle of the inclined portion according to the position of the control plate with respect to the length direction of the radius r of the inlet portion, a large vortex-like flow flows regardless of the position of the control plate. Can be brought into contact with the optimum position on the inner peripheral surface of the inlet portion so that the processing gas can be formed.

Further, in the processing gas reaction tower according to claim 6, in the processing gas reaction tower according to any one of claims 1 to 5, the inflow pipe is freely fixed at an arbitrary position in the axial direction. It is characterized in that the tip portion is arranged at an arbitrary position.

In the present invention according to claim 6, by fixing the inflow pipe at an arbitrary position in the axial direction, the control plate can be positioned at an arbitrary position in the length direction of the radius r of the inlet portion.

Further, the treated gas reaction tower according to claim 7 is the treated gas reaction tower according to claim 1, wherein the control plate has a length from the top of the inlet portion to the length of the radius r of the hemispherical inlet portion. On the other hand, it is characterized in that it is arranged at a position from 0.40r to 0.70r.

In the present invention according to claim 7, the processing gas introduced from the inflow pipe abuts on the control plate arranged at the position from 0.40r to 0.70r with respect to the length of the radius r of the inlet portion. It is directed toward the inner surface of the hemispherical entrance and abuts on the inner surface of the hemisphere. The processing gas in contact with the hemispherical inner surface mainly flows downward in an arc shape and can form a vortex-shaped flow.

Further, the treated gas reaction tower according to claim 8 is the treated gas reaction tower according to claim 7, wherein the control plate has a length from the top of the inlet portion to the length of the radius r of the hemispherical inlet portion. On the other hand, it is characterized in that it is arranged at a position from 0.45r to 0.65r.

In the present invention according to claim 8, the processing gas introduced from the inflow pipe abuts on the control plate arranged at the position from 0.45r to 0.65r with respect to the length of the radius r of the inlet portion. It is directed toward the inner peripheral surface of the inlet and abuts on the arcuate inner peripheral surface, forming a large vortex-like flow that mainly flows downward, and the distribution of the processing gas flow state in the radial direction of the cylinder ( The distribution of the flow velocity) can be suppressed and the processed gas can be evenly distributed.

The treated gas reaction tower according to claim 9 is the treated gas reaction tower according to any one of claims 1 to 8, wherein the treatment agent filled in the cylinder portion of the container body is a honeycomb. It is formed of blocks having a lattice structure, and is characterized in that a large number of flow passages along the axial direction of the tubular portion are formed in the circumferential direction of the tubular portion.

In the present invention according to claim 9, the distribution of the flow state (flow velocity distribution) of the processing gas flowing into the packed layer of the honeycomb lattice structure is suppressed to reduce the flow velocity distribution, and the processing gas is applied to the entire packed layer of the honeycomb lattice structure. Can be distributed evenly.

In the processing gas reaction tower of the present invention, the processing gas flowing into the container can be evenly distributed, and the processing gas can be evenly contacted regardless of the mode of the processing agent.

FIG. 3 is an overall configuration diagram of an integrated coal gasification combined cycle power generation facility equipped with a dry gas refining facility having a processing gas reaction tower according to the first embodiment of the present invention. It is a schematic system diagram of the dry gas purification equipment which has the processing gas reaction tower which concerns on 1st Embodiment of this invention. It is a block diagram of the main part of the processing gas reaction tower which concerns on 1st Embodiment of this invention. It is an external view of the tip part of an inflow pipe. It is a concrete explanatory diagram of the main part of the processing gas reaction tower which concerns on 1st Embodiment of this invention. It is explanatory drawing of the flow state of the processing gas. It is an external view of the packed bed (desulfurizing agent block) of a honeycomb lattice structure. It is a graph of the flow velocity distribution. It is a concrete explanatory diagram of the main part of the processing gas reaction tower which concerns on 2nd Embodiment of this invention. It is explanatory drawing of the flow state of the processing gas. It is a graph of the flow velocity distribution. It is a concrete explanatory view of the main part of the processing gas reaction tower which concerns on 3rd Example of this invention. It is explanatory drawing of the flow state of the processing gas. It is a graph of the flow velocity distribution. It is a concrete explanatory diagram of the main part of the processing gas reaction tower which concerns on 4th Example, 5th Example, 6th Example of this invention. It is explanatory drawing of the flow state of the processing gas. It is an external view of the packed bed (desulfurizing agent block) of a honeycomb lattice structure. It is a graph of the flow velocity distribution. It is a graph of the flow velocity distribution. It is a graph of the flow velocity distribution.

FIG. 1 is a schematic system for explaining the overall configuration of an integrated coal gasification combined cycle facility equipped with a dry gas purification facility having a processing gas reaction tower according to an embodiment of the present invention, and FIG. 2 is an embodiment of the present invention. A schematic system illustrating a dry gas purification facility in FIG. 1 having a treated gas reaction tower according to an example is shown.

The integrated coal gasification combined cycle facility 1 shown in the figure includes a coal gasification furnace 2, and in the coal gasification furnace 2, coal gasification gas g is generated by the reaction between coal and an oxidizing agent (oxygen, air). The coal gasified gas g is adjusted to a predetermined temperature and sent to the dry gas refining facility 4, and impurities are removed by the dry gas refining facility 4 to purify the coal gas f.

The fuel gas f is sent to the combustor 6 as a combustion means of the turbine equipment. That is, the turbine equipment includes a compressor 7 and an expansion turbine 8, and the compressed air and fuel gas f compressed by the compressor 7 are sent to the combustor 6. In the combustor 6, the fuel gas f is burned, and the combustion gas f is sent to the expansion turbine 8 to be expanded to obtain power. The exhaust gas of the expansion turbine 8 is heat-recovered by the exhaust heat recovery boiler 9, and after the nitrogen oxides are removed by the smoke exhaust treatment device 10, it is released to the atmosphere.

On the other hand, the steam turbine 11 is connected coaxially with the compressor 7 and the expansion turbine 8, and the generator 12 is connected to the steam turbine 11. The exhaust heat recovery boiler 9 is supplied with condensate condensate of the exhaust steam of the steam turbine 11 by a condenser (not shown), and the exhaust heat recovery boiler 9 generates steam by the exhaust gas of the expansion turbine 8. The steam generated in the exhaust heat recovery boiler 9 is sent to the steam turbine 11 to obtain power.

The generator 12 is driven by the power of the compressor 7 and the steam turbine 11 connected in series, and combined power generation is performed by the compressor 7 and the steam turbine 11.

In the integrated coal gasification combined cycle facility 1 having the above configuration, the coal gasification gas g is refined by the dry gas purification facility 4 to obtain the fuel gas f.

The dry gas refining equipment 4 will be described with reference to FIG.

The coal gasification gas g adjusted to a predetermined temperature is introduced into the halide removing device 21 from which solid impurities have been removed by the dust filter 20, and the halide is removed by the halide absorber 22. The coal gasification gas g from which the halide has been removed by the halide removing device 21 is sent to the desulfurization device 23.

The scrubber 23 has a treatment tower 24 as a treatment gas reaction tower, and the treatment tower 24 has four scrubber blocks 25 (along the flow direction of the coal gasification gas g) as treatment agents in the vertical direction in the figure. The catalyst of the honeycomb lattice structure) is filled. The desulfurization agent block 25 is a catalyst block in which zinc ferrite is formed into a honeycomb shape and a plurality of desulfurization catalysts having a honeycomb structure are assembled.

By circulating coal gasification gas g (treatment gas) from the upper part to the lower part of the treatment tower 24, the coal gasification gas g is sequentially contacted with the four desulfurizing agent blocks 25, and the iron of zinc ferrite (ZnFe ₂ O ₄ ) is contacted. And zinc synergistically remove hydrogen sulfide ₍ H 2S), carbonyl sulfide (COS), and the like. The desulfurization catalyst of the desulfurization agent block 25 is periodically subjected to catalyst regeneration treatment by releasing sulfide.

The gas from which the sulfur component has been removed by the desulfurization apparatus 23 is sent to the mercury removal tower 27, and in the mercury removal tower 27, mercury is absorbed by a copper-based absorber mainly composed of copper and absorbing mercury. The gas from which mercury has been removed by the mercury removal tower 27 is sent to the dust filter 28. The dust filter 28 physically filters impurities including solid precipitates, fine particles, and powder contained in the gas. The gas whose impurities are physically filtered by the dust filter 28 is heated to a predetermined temperature by a heat exchange device (not shown), is converted into a high-temperature fuel gas f, and is supplied to the combustor 6 (see FIG. 1).

In the processing tower 24 provided with the desulfurizing agent block 25 having the honeycomb lattice structure described above, the coal gasified gas g is evenly flowed so that even a small desulfurizing agent block 25 has an extremely small pressure loss. Good contact with the supported catalyst and absorber is maintained, and an efficient reaction is possible.

Therefore, the processing tower 24 is provided with a control plate for controlling the flow direction of the processing gas, and the flow of the inflowing coal gasification gas g is controlled by the control plate to control the flow of the coal gas in the width direction of the desulfurizing agent block 25. The distribution of the flow velocity of the gasified gas g is suppressed.

The configuration of the processing tower 24 will be specifically described with reference to FIGS. 3 and 4.

FIG. 3 shows a structural explanation of a portion (upper portion) into which coal gasified gas g flows into the processing tower 24 as a processing gas reaction tower according to an embodiment of the present invention, and FIG. 4 shows the tip of an inflow pipe. The appearance situation is shown.

As shown in FIG. 3, since the processing tower 24 (container body) is a pressure vessel, it is provided with a hemispherical inlet portion 31. The inlet portion 31 has a continuous tubular portion 32, and the tubular portion 32 is filled with a desulfurization agent block 25 (treatment agent) that is a catalyst for the honeycomb lattice structure. The coal gasification gas g is introduced from the inlet portion 31 of the treatment tower 24, and the coal gasification gas g is circulated through the desulfurizing agent block 25.

As shown in FIGS. 3 and 4, an inflow pipe 34 is provided at the top of the inlet portion 31. The inflow pipe 34 is arranged so that the tip end thereof faces downward and faces the inside of the inlet portion, and the coal gasification gas g is introduced toward the cylinder portion 32 (desulfurizing agent block 25) inside the treatment tower 24. To. A control plate 36 is attached to a portion (tip portion) of the tip of the inflow pipe 34 via a connecting rod 35.

The control plate 36 has a board surface 37 having a diameter larger than the diameter of the inflow pipe 34 and orthogonal to the axial direction of the inflow pipe 34, and the peripheral edge of the board surface 37 is inclined toward the top of the inlet portion 31. An inclined portion 38 is formed. The coal gasification gas g sent from the inflow pipe 34 interferes with the board surface 37 of the control plate 36 to control the flow direction (flow to the peripheral side), and is directed upward by the inclined portion 38 (on the inner peripheral surface). (Directed to a position closer to the top side), it abuts on the hemispherical inner surface of the inlet 31.

The angle θ of the inclined portion 38 with respect to the board surface 37 (see FIG. 5) is formed at an angle between 30 degrees and 70 degrees, preferably between 45 degrees and 55 degrees toward the top of the inlet portion 31. .. The coal gasification gas g introduced from the inflow pipe 34 is the inner peripheral surface of the inlet portion 31 along the inclined portion 38 formed at an angle between 30 degrees and 70 degrees (between 45 degrees and 55 degrees). It is directed to an appropriate position and abuts on the arcuate inner peripheral surface of the inlet portion 31.

As a result, the coal gasification gas g becomes a spiral (large) flow that mainly flows downward, and the distribution of the flow state (flow velocity distribution) of the coal gasification gas g is suppressed in the radial direction of the cylinder portion 32. Therefore, the coal gasification gas g can be evenly distributed to the desulfurizing agent block 25.

It is also possible to variably configure the tilt angle of the tilted portion 38 with respect to the board surface 37 of the control plate 36. By changing the inclination angle of the inclined portion 38 with respect to the board surface 37 according to the position of the control plate 36 with respect to the length direction of the radius r of the inlet portion 31, a large vortex-shaped flow is formed regardless of the position of the control plate 36. As possible, the coal gasification gas g can be brought into contact with the optimum position on the inner peripheral surface of the inlet portion 31.

Further, the control plate 36 is located at a position of 0.40r to 0.70r, preferably 0.45r to 0.65r, from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31. It is placed in a position. The coal gasification gas g introduced from the inflow pipe 34 abuts on the control plate 36 arranged at the positions of 0.40r to 0.70r (0.45r to 0.65r), and abuts on the inner peripheral surface of the inlet portion 31. A large vortex-like flow that flows downward is formed mainly by abutting against the arcuate inner peripheral surface, and the distribution of the flow state of the coal gasification gas g with respect to the radial direction of the tubular portion 32 (flow velocity). Distribution) can be suppressed and coal gasification gas g can be evenly distributed.

The position of the control plate 36 with respect to the length of the radius r of the inlet portion 31 can be fixed at an arbitrary position. Further, depending on the position of the control plate 36, the coal gasification gas g is brought into contact with the arcuate inner peripheral surface of the inlet portion 31 substantially horizontally without providing the inclined portion 38, and the vortex shape mainly flows downward. It is also possible to form a large flow.

The treated gas reaction tower according to the first embodiment will be specifically described with reference to FIGS. 5 to 8.

FIG. 5 shows an explanation of the specific configuration of the inlet portion 31 and the control plate 36 of the treated gas reaction tower according to the first embodiment of the present invention, and FIG. 6 shows an explanation showing the flow state of the coal gasification gas g. It is shown. Further, FIG. 7 shows the appearance of the desulfurizing agent block 25 for explaining the verification position of the flow velocity. The desulfurizing agent block 25 shown in FIG. 7 has a shape in which the corners are omitted according to the cylindrical pressure vessel.

FIG. 8 shows the state of the flow velocity distribution of the coal gasified gas g, FIG. 8 (a) shows the state of the line aa in FIG. 7, and FIG. 8 (b) shows the state of the line bb in FIG. 8 (c) shows the situation of the cc line in FIG. 7, and FIG. 8 (d) shows the situation of the dd line in FIG. 7.

As shown in FIG. 5, the control plate 36 is arranged at a position of 0.65 r from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31. The angle θ of the inclined portion 38 with respect to the board surface 37 is formed at an angle of 55 degrees toward the top of the inlet portion 31.

As shown in FIG. 6, the coal gasification gas g introduced from the inflow pipe 34 in this state is directed diagonally upward to the left and right in the figure and hits a high position on the arcuate inner peripheral surface of the inlet portion 31. Contact. The coal gasification gas g in contact with the inner peripheral surface mainly forms a large vortex-like flow that flows downward. That is, the coal gasification gas g directed to the left in the figure forms a large counterclockwise vortex, and the coal gasification gas g directed to the right in the figure has a large vortex in the clockwise direction. Form a flow.

By forming a large spiral flow with respect to the coal gasification gas g, the distribution of the flow state (flow velocity distribution) of the coal gasification gas g in the radial direction of the cylinder portion 32 is suppressed, and the desulfurizing agent. It is evenly distributed to the block 25.

FIG. 8A is a state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line aa (Y-axis = a) in FIG. 7.

As shown in FIG. 8A, at the position where the Y axis in FIG. 7 is a, the flow velocity is higher at both ends of the desulfurizing agent block 25 than the average flow velocity f of the coal gasified gas g (for example, the average flow velocity). (About twice f), the flow velocity in the central part is close to the average flow velocity f. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

FIG. 8 (b) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line bb (Y-axis = b) in FIG. 7.

As shown in FIG. 8B, at the position where the Y axis in FIG. 7 is b, the flow velocities on both sides of the desulfurizing agent block 25 are close to the average flow velocity f with respect to the average flow velocity f of the coal gas gas g. The flow velocity in the central part is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

FIG. 8 (c) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the cc line (Y-axis = c) in FIG. 7.

As shown in FIG. 8 (c), at the position where the Y axis in FIG. 7 is c, the flow velocities on both sides of the desulfurizing agent block 25 are substantially equivalent to the average flow velocity f of the coal gasified gas g. The flow velocity in the central portion is high (for example, about twice the average flow velocity f), and the flow velocity in the portion between both sides and the central portion is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

FIG. 8 (d) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the d-d line (Y-axis = d) in FIG. 7.

As shown in FIG. 8 (d), at the position where the Y axis in FIG. 7 is d, the flow velocities on both sides of the desulfurizing agent block 25 are substantially equivalent to the average flow velocity f of the coal gasified gas g. The flow velocity in the central portion is high (for example, about twice the average flow velocity f), and the flow velocity in the portion between both sides and the central portion is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Therefore, it is arranged at a position of 0.65 r from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31, and the angle θ of the inclined portion 38 with respect to the board surface 37 is formed at 55 degrees. By using the control plate 36, the distribution of the flow state (flow velocity distribution) in the radial direction of the cylinder portion 32 of the coal gasified gas g can be suppressed to a narrow range distribution centered on the average flow velocity f.

This makes it possible to evenly distribute the coal gasification gas g to the desulfurization agent block 25 and evenly contact the coal gasification gas g. Therefore, even in the honeycomb lattice-shaped desulfurization agent block 25 in which the gas does not diffuse naturally, it is possible to maintain high desulfurization performance by evenly contacting the coal gasification gas g.

Incidentally, even when only the diffusion member is used without using the control plate 36, the coal gasification gas g can be sufficiently equalized, but the flow velocity at the center of the desulfurization agent block 25 is high. At the end, it has been confirmed that the velocity is negative (some gas is flowing backward). That is, it has been confirmed that the distribution has a wide range centered on the average flow velocity f.

The treated gas reaction tower according to the second embodiment will be specifically described with reference to FIGS. 9 to 11.

FIG. 9 shows an explanation of the specific configuration of the inlet portion 31 and the control plate 36 of the treated gas reaction tower according to the second embodiment of the present invention, and FIG. 10 shows an explanation showing the flow state of the coal gasification gas g. It is shown. FIG. 11 shows the state of the flow velocity distribution of the coal gasified gas g, FIG. 11 (a) shows the state of the line aa in FIG. 7, and FIG. 11 (b) shows the state of the line bb in FIG. 11 (c) shows the situation of the cc line in FIG. 7, and FIG. 11 (d) shows the situation of the dd line in FIG. 7.

As shown in FIG. 9, the control plate 36 is arranged at a position of 0.65 r from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31. The angle θ of the inclined portion 38 with respect to the board surface 37 is formed at an angle of 45 degrees toward the top of the inlet portion 31.

As shown in FIG. 10, the coal gasification gas g introduced from the inflow pipe 34 in this state is directed diagonally to the left and right in the figure and abuts on the arcuate inner peripheral surface of the inlet portion 31. The coal gasification gas g in contact with the inner peripheral surface mainly forms a vortex-like flow flowing downward. That is, the coal gas gas g directed to the left in the figure forms a counterclockwise vortex flow, and the coal gas gas g directed to the right in the figure forms a vortex flow in the clockwise direction. Form.

By forming a spiral flow with respect to the coal gasification gas g, the distribution of the flow state (flow velocity distribution) of the coal gasification gas g in the radial direction of the cylinder portion 32 is suppressed, and the desulfurizing agent block. It is evenly distributed to 25.

FIG. 11A is a state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line aa (Y-axis = a) in FIG. 7.

As shown in FIG. 11A, at the position where the Y axis in FIG. 7 is a, the flow velocity is higher at both ends of the desulfurizing agent block 25 than the average flow velocity f of the coal gas gas g (for example, the average flow velocity). (A little less than twice f), the flow velocity in the central part is slightly low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

FIG. 11B is a state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line bb (Y-axis = b) in FIG. 7.

As shown in FIG. 11B, at the position where the Y axis in FIG. 7 is b, the flow velocities on both sides of the desulfurizing agent block 25 are substantially equivalent to the average flow velocity f of the coal gasification gas g. , The flow velocity in the central part is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

FIG. 11 (c) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the cc line (Y-axis = c) in FIG. 7.

As shown in FIG. 11 (c), at the position where the Y axis in FIG. 7 is c, the flow velocities on both sides of the desulfurizing agent block 25 are close to the average flow velocity f of the coal gasified gas g. Therefore, the flow velocity in the central portion is high (for example, about twice the average flow velocity f), and the flow velocity in the portion between both sides and the central portion is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

FIG. 11 (d) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the d-d line (Y-axis = d) in FIG. 7.

As shown in FIG. 11D, at the position where the Y axis in FIG. 7 is d, the flow velocities on both sides of the desulfurizing agent block 25 are slightly lower than the average flow velocity f of the coal gasified gas g. The flow velocity in the central portion is high (for example, about 3 times the average flow velocity f), and the flow velocity in the portion between both sides and the central portion is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Therefore, it is arranged at a position of 0.65 r from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31, and the angle θ of the inclined portion 38 with respect to the board surface 37 is formed at 45 degrees. By using the control plate 36, the distribution of the flow state (flow velocity distribution) of the coal gasified gas g in the radial direction of the cylinder portion 32 can be suppressed to a limited range distribution centered on the average flow velocity f. ..

As a result, the coal gasification gas g can be distributed substantially evenly to the desulfurization agent block 25, and the coal gasification gas g can be brought into contact with the desulfurization agent block 25 in a nearly uniform state. Therefore, even in the honeycomb lattice-shaped desulfurization agent block 25 in which the gas does not diffuse naturally, it is possible to maintain high desulfurization performance by evenly contacting the coal gasification gas g.

The treated gas reaction tower according to the third embodiment will be specifically described with reference to FIGS. 12 to 14.

FIG. 12 shows an explanation of the specific configuration of the inlet portion 31 and the control plate 36 of the treated gas reaction tower according to the third embodiment of the present invention, and FIG. 13 shows an explanation showing the flow state of the coal gasification gas g. It is shown. FIG. 14 shows the state of the flow velocity distribution of the coal gasified gas g, FIG. 14 (a) shows the state of the line aa in FIG. 7, and FIG. 14 (b) shows the state of the line bb in FIG. 14 (c) shows the situation of the cc line in FIG. 7, and FIG. 14 (d) shows the situation of the dd line in FIG. 7.

As shown in FIG. 12, the control plate 36 is arranged at a position of 0.55 r from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31. The angle θ of the inclined portion 38 with respect to the board surface 37 is formed at an angle of 45 degrees toward the top of the inlet portion 31. That is, the third embodiment is an example in which the control plate 36 is arranged at a higher position than the second embodiment.

As shown in FIG. 13, the coal gasification gas g introduced from the inflow pipe 34 in this state is directed diagonally upward to the left and right in the figure and hits a high position on the arcuate inner peripheral surface of the inlet portion 31. Contact. The coal gasification gas g in contact with the inner peripheral surface mainly forms a large vortex-like flow that flows downward. That is, the coal gasification gas g directed to the left in the figure forms a large counterclockwise vortex, and the coal gasification gas g directed to the right in the figure has a large vortex in the clockwise direction. Form a flow.

Similar to the first embodiment, the coal gasification gas g is formed with a large vortex-like flow, so that the coal gasification gas g is distributed in a flow state (flow velocity) in the radial direction of the cylinder portion 32. Distribution) is suppressed and evenly distributed to the desulfurizing agent block 25.

FIG. 14A is a state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line aa (Y-axis = a) in FIG. 7.

As shown in FIG. 14A, at the position where the Y axis in FIG. 7 is a, the flow velocity is higher at both ends of the desulfurizing agent block 25 than the average flow velocity f of the coal gas gas g (for example, the average flow velocity). (About 1.8 times f), the flow velocity in the central part is almost the same. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

FIG. 14 (b) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line bb (Y-axis = b) in FIG. 7.

As shown in FIG. 14 (b), at the position where the Y axis in FIG. 7 is b, the flow velocities on both sides of the desulfurizing agent block 25 are substantially equal to or slightly lower than the average flow velocity f of the coal gasified gas g. The flow velocity in the central part is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

FIG. 14 (c) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the cc line (Y-axis = c) in FIG. 7.

As shown in FIG. 14 (c), at the position where the Y axis in FIG. 7 is c, the flow velocities on both sides of the desulfurizing agent block 25 are substantially equal to or slightly lower than the average flow velocity f of the coal gasified gas g. The flow velocity in the central portion is high (for example, about 1.8 times the average flow velocity f), and the flow velocity in the portion between both sides and the central portion is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

FIG. 14 (d) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the d-d line (Y-axis = d) in FIG. 7.

As shown in FIG. 14 (d), at the position where the Y axis in FIG. 7 is d, the flow velocities on both sides of the desulfurizing agent block 25 are slightly higher than the average flow velocity f of the coal gasified gas g. The flow velocity in the central portion is high (for example, about 2.5 times the average flow velocity f), and the flow velocity in the portion between both sides and the central portion is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Therefore, it is arranged at a position of 0.55 r from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31, and the angle θ of the inclined portion 38 with respect to the board surface 37 is formed at 45 degrees. By using the control plate 36, the distribution of the flow state (flow velocity distribution) of the coal gasified gas g in the radial direction of the cylinder portion 32 of the coal gasified gas g can be measured as the average flow velocity f without increasing the angle θ of the inclined portion 38 with respect to the board surface 37. It is possible to suppress the distribution to a limited range centered on.

As a result, as in the first embodiment, the coal gasification gas g can be evenly distributed to the desulfurization agent block 25, and the coal gasification gas g can be evenly contacted. Therefore, even in the honeycomb lattice-shaped desulfurization agent block 25 in which the gas does not diffuse naturally, it is possible to maintain high desulfurization performance by evenly contacting the coal gasification gas g.

When the angle θ of the inclined portion 38 with respect to the board surface 37 is 30 degrees or more and less than 45 degrees, and more than 55 degrees and 70 degrees or less, coal gasification gas g is practically used for the desulfurizing agent block 25. It has been confirmed that it can be distributed within a range of distribution (for example, within a range that does not result in a negative flow velocity).

The treated gas reaction towers according to the fourth embodiment, the fifth embodiment, and the sixth embodiment will be specifically described with reference to FIGS. 15 to 19.

FIG. 15 shows a description of the specific configuration of the inlet portion 31 of the processing gas reaction tower and the control plate according to the fourth embodiment, the fifth embodiment, and the sixth embodiment of the present invention, and FIG. 16 shows the fourth embodiment. The explanation which shows the state of the flow of the coal gasification gas g is shown. Further, FIG. 17 shows the appearance of the desulfurizing agent block 25A for explaining the verification position of the flow velocity. The desulfurizing agent block 25A shown in FIG. 17 has a square column shape having a square cross section without omitting the corners.

FIG. 18 shows the state of the flow velocity distribution of the coal gasified gas g of the fourth embodiment, FIG. 18 (a) is the state of the line aa in FIG. 17, and FIG. 18 (b) is b in FIG. The situation of line b, FIG. 18 (c) is the situation of line cc in FIG. 17, and FIG. 18 (d) is the situation of line dd in FIG.

Further, FIG. 19 shows the state of the flow velocity distribution of the coal gasified gas g of the fifth embodiment, FIG. 19 (a) is the state of the line aa in FIG. 17, and FIG. 19 (b) is FIG. 17 The situation of the middle bb line, FIG. 19 (c) is the situation of the middle line cc in FIG. 17, and FIG. 19 (d) is the situation of the middle line dd.

Further, FIG. 20 shows the state of the flow velocity distribution of the coal gasified gas g of the sixth embodiment, FIG. 20 (a) is the state of the line aa in FIG. 17, and FIG. 20 (b) is FIG. 17 The situation of the middle bb line, FIG. 20 (c) is the situation of the middle line cc in FIG. 17, and FIG. 20 (d) is the situation of the middle line dd.

As shown in FIG. 15, the control plate 41 has only a board surface on which an inclined portion is not formed. The figure shows the control plate 41A of the fourth embodiment, the control plate 41B of the fifth embodiment, and the control plate 41C of the sixth embodiment at the same time. One 41 is provided.

The control plate 41A of the fourth embodiment is arranged at a position of 0.45r from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31.

As shown in FIG. 16, the coal gasification gas g introduced from the inflow pipe 34 in this state is directed in the left-right direction in the figure and hits a position above half of the arcuate inner peripheral surface of the inlet portion 31. Contact. The coal gasification gas g in contact with the inner peripheral surface mainly forms a large vortex-like flow that flows downward. That is, the coal gasification gas g directed to the left in the figure forms a large counterclockwise vortex, and the coal gasification gas g directed to the right in the figure has a large vortex in the clockwise direction. Form a flow.

A large vortex-like flow is formed even in the control plate 41A having only the board surface arranged at the position of 0.45r with respect to the length of the radius r of the inlet portion 31 with respect to the coal gasification gas g. As a result, the distribution of the flow state (distribution of the flow velocity) of the coal gasified gas g is suppressed in the radial direction of the tubular portion 32, and the coal gasified gas g is evenly distributed to the desulfurizing agent block 25A.

The control plate 41B of the fifth embodiment is arranged at a position of 0.55 r from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31. Further, the control plate 41C of the sixth embodiment is arranged at a position of 0.65 r from the top of the inlet portion 31 with respect to the length of the radius r of the hemispherical inlet portion 31.

Also in the fifth and sixth embodiments, the coal gasification gas g introduced from the inflow pipe 34 is directed in a direction laterally intersecting the flow, and the inner circumference of the inlet portion 31 is arcuate. It abuts on the upper side of the surface. The coal gasification gas g abutting on the inner peripheral surface mainly forms a vortex-like flow flowing downward, and the coal gasification gas g is distributed in a flow state (flow velocity) in the radial direction of the cylinder portion 32. Distribution) is suppressed and evenly distributed to the desulfurizing agent block 25A.

FIG. 18A of the fourth embodiment shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line aa (Y-axis = a) in FIG. ..

As shown in FIG. 18A, at the position where the Y axis in FIG. 17 is a, the flow velocities at both ends of the desulfurizing agent block 25A are substantially equal to or higher than the average flow velocity f of the coal gasified gas g, and are in the center. The flow velocity of the part is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Further, FIG. 18B shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line bb-b (Y-axis = b) in FIG.

As shown in FIG. 18 (b), at the position where the Y axis in FIG. 17 is b, the flow velocities on both sides of the desulfurizing agent block 25A are substantially equal to or slightly lower than the average flow velocity f of the coal gasified gas g. The flow velocity in the central part is almost the same. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Further, FIG. 18 (c) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the c-c line (Y-axis = c) in FIG.

As shown in FIG. 18 (c), at the position where the Y axis in FIG. 17 is c, the flow velocities on both sides of the desulfurizing agent block 25A are lower than the average flow velocity f of the coal gasification gas g, and the center. The flow velocities of the parts are almost the same. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Further, FIG. 18 (d) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the dd line (Y-axis = d) in FIG.

As shown in FIG. 18 (d), at the position where the Y axis in FIG. 17 is d, the flow velocities on both sides of the desulfurizing agent block 25A are lower than the average flow velocity f of the coal gasification gas g, and the center. The flow velocities of the parts are almost the same. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Therefore, by using the control plate 41A arranged at the position of 0.45r with respect to the length of the radius r of the hemispherical entrance portion 31 from the top of the entrance portion 31, that is, the entrance portion 31 of the control plate 41A. By defining the position of the coal gasified gas g in the radial direction of the radius, the distribution of the flow state (distribution of the flow velocity) in the radial direction of the cylinder portion 32 of the coal gasified gas g can be suppressed to a distribution in a range close to the average flow velocity f.

FIG. 19A of the fifth embodiment shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line aa (Y-axis = a) in FIG. ..

As shown in FIG. 19A, at the position where the Y axis in FIG. 17 is a, the flow velocities at both ends of the desulfurizing agent block 25A are substantially equivalent to the average flow velocity f of the coal gasified gas g. , The flow velocity in the central part is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Further, FIG. 19B shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line bb-b (Y-axis = b) in FIG.

As shown in FIG. 19B, at the position where the Y axis in FIG. 17 is b, the flow velocities on both sides of the desulfurizing agent block 25A are lower than the average flow velocity f of the coal gasification gas g, and the center. The flow velocities of the parts are almost the same. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Further, FIG. 19 (c) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the c-c line (Y-axis = c) in FIG.

As shown in FIG. 19 (c), at the position where the Y axis in FIG. 17 is c, the flow velocities on both sides of the desulfurizing agent block 25A are lower than the average flow velocity f of the coal gasification gas g, and the center. The flow velocities of the parts are almost the same. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Further, FIG. 19 (d) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the dd line (Y-axis = d) in FIG.

As shown in FIG. 19 (d), at the position where the Y axis in FIG. 17 is d, the flow velocities on both sides of the desulfurizing agent block 25A are lower than the average flow velocity f of the coal gasification gas g, and the center. The flow velocity of the part is about the same to slightly higher. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Therefore, by using the control plate 41B arranged at the position of 0.55r with respect to the length of the radius r of the hemispherical entrance portion 31 from the top of the entrance portion 31, that is, the entrance portion 31 of the control plate 41B. By defining the position of the coal gasified gas g in the radial direction of the radius, the distribution of the flow state (distribution of the flow velocity) in the radial direction of the cylinder portion 32 of the coal gasified gas g can be suppressed to a distribution in a range close to the average flow velocity f.

FIG. 20A of the sixth embodiment shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line aa (Y-axis = a) in FIG. ..

As shown in FIG. 20 (a), at the position where the Y axis in FIG. 17 is a, the flow velocity is higher at both ends of the desulfurizing agent block 25A with respect to the average flow velocity f of the coal gasification gas g, and the center. The flow velocity of the part is low. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Further, FIG. 20B shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the line bb-b (Y-axis = b) in FIG.

As shown in FIG. 20 (b), at the position where the Y axis in FIG. 17 is b, the flow velocities on both sides of the desulfurizing agent block 25A are lower than the average flow velocity f of the coal gasification gas g, and the center. The flow velocities of the parts are almost the same. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Further, FIG. 20 (c) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the c-c line (Y-axis = c) in FIG.

As shown in FIG. 20 (c), at the position where the Y axis in FIG. 17 is c, the flow velocities on both sides of the desulfurizing agent block 25A are lower than the average flow velocity f of the coal gasification gas g, and the center. The flow velocity of the part is from almost the same to high. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Further, FIG. 20 (d) shows the state of the flow velocity (Z-axis) of the coal gasified gas g in the direction (X-axis direction) along the dd line (Y-axis = d) in FIG.

As shown in FIG. 20 (d), at the position where the Y axis in FIG. 17 is d, the flow velocities on both sides of the desulfurizing agent block 25A are lower than the average flow velocity f of the coal gasification gas g, and the center. The flow velocity of the part is high. It has been confirmed that the flow velocity of the coal gasified gas g has a positive value in the entire range.

Therefore, by using the control plate 41C arranged at the position of 0.65r with respect to the length of the radius r of the hemispherical entrance portion 31 from the top of the inlet portion 31, that is, the entrance portion 31 of the control plate 41C. By defining the position in the radius r direction of, the distribution of the flow state (distribution of the flow velocity) of the coal gasified gas g in the radial direction of the cylinder portion 32 can be suppressed to the distribution within the range not deviating from the average flow velocity f. ..

As described above, by arranging the control plate 41 at the positions of 0.45r, 0.55r, and 0.65r with respect to the length of the radius r of the hemispherical inlet portion 31, the desulfurizing agent block 25A can be used. It becomes possible to evenly distribute the coal gasification gas g and bring the coal gasification gas g into contact evenly. Therefore, even in the honeycomb lattice-shaped desulfurization agent block 25A in which the gas does not diffuse naturally, it is possible to maintain high desulfurization performance by evenly contacting the coal gasification gas g.

When the control plate 41 is placed at a position of 0.40r or more and less than 0.45r, or more than 0.65r and 0.70r or less with respect to the length of the radius r of the hemispherical inlet portion 31, gasification is performed. It has been confirmed that the coal gasified gas g can be circulated to the agent block 25A within a practical flow velocity distribution range (for example, within a range that does not result in a negative flow velocity distribution).

Therefore, the treatment tower 24 described with reference to the first to sixth embodiments can evenly distribute the coal gasification gas g and flows into the desulfurizing agent block 25 (25A) from the inflow pipe 34. It becomes possible to evenly contact the coal gasified gas g. That is, even in the honeycomb lattice-shaped desulfurizing agent block 25 (25A) in which the coal gasification gas g does not diffuse naturally, the coal gasification gas g can be evenly contacted.

INDUSTRIAL APPLICABILITY The present invention is an industrial field of a processing gas reaction tower for distributing a processing gas to a processing agent, particularly an industry of a processing gas reaction tower applied to an impurity removing device in a dry gas purification facility provided in an integrated coal gasification combined cycle facility. It can be used in the field.

1 Coal gasification combined cycle equipment 2 Coal gasification combined cycle 4 Dry gas purification equipment 6 Combustor 7 Compressor 8 Expansion turbine 9 Exhaust heat recovery boiler 10 Exhaust heat treatment equipment 11 Steam turbine 12 Generator 20, 28 Dust filter 21 Hazard Removal device 22 Halogen absorber 23 Desmelting device 24 Treatment tower 25 Desulfurizing agent block 27 Mercury removal tower 31 Inlet part 32 Cylinder part 34 Inflow pipe 35 Connection rod 36, 41 Control plate 37 Board surface 38 Inclined part

Claims (9)

It has a hemispherical inlet portion and a continuous tubular portion at the inlet portion, the tubular portion is filled with a treatment agent, a treatment gas is introduced from the inlet portion, and the treatment gas is distributed to the treatment agent. The main body of the container to be made to
An inflow pipe provided at the top of the inlet portion, the tip portion thereof is arranged facing the inside of the inlet portion, and the treated gas is introduced into the inside of the container body.
It is provided with a control plate attached to the tip end portion of the inflow pipe and controlling the flow direction of the processing gas by interfering with the processing gas sent from the inflow pipe.
The control plate is
It has a plate surface having a diameter larger than the diameter of the inflow pipe and orthogonal to the axial direction of the inflow pipe, and a spiral flow is formed by abutting the processing gas on the hemispherical inner surface of the inlet portion. A treated gas reaction tower characterized in that the flow direction of the treated gas is controlled. In the treated gas reaction tower according to claim 1.
The control plate has
A processing gas reaction tower characterized in that an inclined portion inclined toward the top of the inlet portion is formed around the inlet portion. In the processing gas reaction tower according to claim 2.
The inclined portion of the control plate
A treated gas reaction column characterized in that it is formed at an angle between 30 degrees and 70 degrees toward the top of the inlet. In the processing gas reaction tower according to claim 3.
The inclined portion of the control plate
A treated gas reaction column characterized in that it is formed at an angle between 45 degrees and 55 degrees toward the top of the inlet. In the processing gas reaction tower according to claim 2.
The control plate is
A processing gas reaction tower characterized in that the inclination angle of the inclined portion is variably formed. In the processing gas reaction tower according to any one of claims 1 to 5.
The inflow pipe is
A processing gas reaction tower characterized in that it can be fixed at an arbitrary position in the axial direction and the tip portion is arranged at an arbitrary position. In the treated gas reaction tower according to claim 1.
The control plate is
A processing gas reaction tower characterized in that it is arranged at a position from 0.40r to 0.70r with respect to the length of the radius r of the hemispherical entrance portion from the top portion of the inlet portion. In the processing gas reaction tower according to claim 7.
The control plate is
A processing gas reaction tower characterized in that it is arranged at a position from 0.45r to 0.65r with respect to the length of the radius r of the hemispherical inlet portion from the top portion of the inlet portion. In the processing gas reaction tower according to any one of claims 1 to 8.
The treatment agent filled in the cylinder portion of the container body is
A processing gas reaction tower formed of blocks having a honeycomb lattice structure, characterized in that a large number of flow passages along the axial direction of the cylinder portion are formed in the circumferential direction of the cylinder portion.

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