CN112275225A - Radial moving bed reaction system and flow-solid reaction method - Google Patents
Radial moving bed reaction system and flow-solid reaction method Download PDFInfo
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- CN112275225A CN112275225A CN201910678967.8A CN201910678967A CN112275225A CN 112275225 A CN112275225 A CN 112275225A CN 201910678967 A CN201910678967 A CN 201910678967A CN 112275225 A CN112275225 A CN 112275225A
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Abstract
The present disclosure relates to a radial moving bed reaction system and a method of flow-solid reaction. The radial moving bed reaction system is provided with the hopper which is integrally arranged with the reactor barrel, and the hopper is communicated with the catalyst filling area in the reactor barrel through the catalyst feeding pipe which is positioned in the reactor barrel, so that the catalyst can enter the filling area after being preheated in the reactor barrel and moves downwards along the axial direction of the reactor, the temperature distribution uniformity of the catalyst filling area is improved, and the catalytic reaction is facilitated; in addition, a conical blanking structure is adopted, so that the catalyst flows more smoothly. The reactor disclosed by the invention can uniformly distribute reaction raw materials, effectively avoids short circuit of the reaction raw materials, enables the fluid to flow nearly in a plug flow manner, and enables the solid to flow smoothly without dead zones; meanwhile, the method has the advantages of low processing and manufacturing difficulty, low operation and maintenance cost and the like.
Description
Technical Field
The present disclosure relates to the field of petrochemical industry, and in particular, to a radial moving bed reaction system and a method of flow-solid reaction.
Background
Moving beds are a reactor type commonly used in the field of petrochemical industry. Within the moving bed, solid particles move slowly and come into contact with a gas or liquid phase. Moving bed reactors include counter-flow, parallel-flow and cross-flow, depending on the direction of relative movement of the solids and fluid. Wherein, the radial moving bed is the better choice for realizing low pressure drop and high flux.
The existing radial moving bed is generally applied to the fields of continuous reforming, isomerization, low-carbon hydrocarbon conversion, water treatment and the like. The main problems of radial moving beds in industrial applications are uneven fluid distribution, poor catalyst flow, dead flow zones, etc.
Disclosure of Invention
It is an object of the present disclosure to provide a radial moving bed reaction system and method that enables uniform axial distribution of fluid within the reactor, eliminating dead zones of flow.
In order to achieve the above object, a first aspect of the present disclosure provides a radial moving bed reaction system, which includes a reactor cylinder and a hopper, wherein the hopper is integrally disposed at an upper portion of the reactor cylinder; a catalyst filling area is arranged in the reactor cylinder, the radial section of the catalyst filling area is annular, a shunting flow channel is formed between the outer side wall of the catalyst filling area and one part of the inner wall of the reactor cylinder, a collecting flow channel is formed between the inner side wall of the catalyst filling area and the other part of the inner wall of the reactor cylinder, and the shunting flow channel and the collecting flow channel are only communicated through the fluid of the catalyst filling area; the top of the catalyst filling area is sealed, the bottom of the catalyst filling area is communicated with a conical catalyst blanking area, a catalyst discharge hole is formed in the bottom of the catalyst blanking area, an opening in the bottom end of the hopper is communicated with the catalyst filling area only through a catalyst feed pipe, and the catalyst feed pipe is positioned in the reactor barrel; a reactant inlet and a product outlet are formed in the reactor cylinder; the reactant inlet is in fluid communication with the diverging flow channels, the product outlet is in fluid communication with the collecting flow channels, and the product outlet is located at an upper portion of the collecting flow channels.
Optionally, the hopper, the catalyst loading zone and the reactor barrel are coaxially arranged; the top end of the catalyst filling area is provided with an annular cover plate; the bottom end of the catalyst feeding pipe is opened to penetrate through the annular cover plate to be communicated with the catalyst filling area; the inner side wall of the catalyst filling area is formed into a perforated pipe, the top end of the perforated pipe is open, and the bottom end of the perforated pipe is closed; the outer side of the perforated pipe is provided with an outer screen or a fan-shaped cylinder module to form the outer side wall of the catalyst filling area; the fan-shaped cylinder module comprises 10-100 fan-shaped cylinders, the fan-shaped cylinders are vertically communicated, the radial sections of the fan-shaped cylinders are fan-shaped, the inner arc-shaped walls of the fan-shaped cylinders are provided with openings, and the fan-shaped cylinders are symmetrically distributed around the axial center of the reactor.
Optionally, the reactor barrel sequentially comprises a conical barrel section, a cylindrical barrel section and an inverted conical barrel section from top to bottom, and the bottom end of the hopper is hermetically connected with the top end of the conical barrel section; the product outlet is positioned in the conical barrel section, and the reactant inlet is positioned at the upper part or the lower part of the cylindrical barrel section; the catalyst discharge port is arranged at the bottom of the inverted cone-shaped cylinder section;
the bottom of the perforated pipe is provided with a catalyst guide assembly, and the catalyst guide assembly comprises a guide cylinder; the guide cylinder is coaxially arranged with the perforated pipe, the guide cylinder is in an inverted cone shape, and the cone bottom of the inverted cone shape is aligned with the catalyst discharge port;
and a gap between the inverted conical cylinder section and the guide cylinder is formed into the catalyst blanking area.
Optionally, the conical bottom of the guide shell is closed, and the catalyst discharge port is provided with a sealing gas inlet so as to spray sealing gas into the catalyst discharge port from bottom to top; alternatively, the first and second electrodes may be,
the conical bottom of draft tube has the opening, the inside sealed gas entry that is equipped with of draft tube to from top to bottom to catalyst discharge gate sprays sealed gas.
Optionally, one of the upper end and the lower end of the outer side wall of the catalyst loading zone is fixed, and the other end is a free end; one of the upper end and the lower end of the inner side wall of the catalyst filling area is fixed, and the other end of the inner side wall of the catalyst filling area is a free end; the outer side wall and the inner side wall are not provided with expansion joints;
preferably, the top end of the outer screen is fixedly connected with the reactor cylinder, and the bottom end of the outer screen is a free end, or the bottom end of the fan-shaped cylinder module is fixedly connected with the reactor cylinder, and the top end of the fan-shaped cylinder module is a free end; the bottom end of the perforated pipe is connected to the inverted cone-shaped section of the reactor barrel, and the top end of the perforated pipe is a free end.
Optionally, a supporting cylinder is arranged at the bottom end of the porous pipe; the supporting cylinder is coaxially arranged between the perforated pipe and the guide cylinder, a plurality of reinforcing ribs extending axially are arranged on the outer side of the supporting cylinder, and the supporting cylinder is clamped and fixed with the inner wall of the inverted cone-shaped cylinder section through the reinforcing ribs.
Optionally, the radial width B of the catalyst loading area is 100-1500 mm; the opening rate of the outer side wall of the catalyst filling area is 15% -35%, and the opening rate of the inner side wall of the catalyst filling area is 0.5% -10%; the upper parts of the inner side wall and the outer side wall of the catalyst filling area respectively comprise a non-porous area, and the axial length of the non-porous area is 0.3B-5B.
Optionally, a feed distributor is further included, the feed distributor being located within the split flow channel, the feed distributor facing the reactant inlet; the feed distributor is a baffle distributor, a blade distributor or a tangential circulation distributor, or a combination of two or three of them.
A second aspect of the present disclosure provides a method of performing a flow-solids reaction using the system of the first aspect of the present disclosure, the method comprising: continuously feeding the solid material in the hopper into the catalyst loading zone; and enabling the reaction material to enter the catalyst filling area through the reactant inlet to perform contact reaction with the solid material.
Optionally, the flow-solid reaction comprises at least one of a dehydrogenation reaction of lower hydrocarbons, a reforming reaction, and a gas desulfurization reaction; the solid material comprises a solid catalyst and/or a solid adsorbent.
The radial moving bed reaction system is provided with the hopper which is integrally arranged with the reactor barrel, and the hopper is communicated with the catalyst filling area in the reactor barrel through the catalyst feeding pipe which is positioned in the reactor barrel, so that the catalyst can enter the filling area after being preheated in the reactor barrel, and the temperature distribution uniformity of the catalyst filling area is improved; a conical blanking structure is adopted, so that solid in the reactor flows smoothly without dead zones, and the catalytic reaction is facilitated; the reactor can prevent the catalyst feeding pipe from passing through the outlet pipeline of the material flow, and reduce the leakage risk of the outlet material flow. In addition, the reactor disclosed by the invention can enable reaction raw materials to be uniformly distributed, and the fluid flow is nearly plug flow, so that the short circuit of the reaction raw materials is effectively avoided; meanwhile, the method has the advantages of low processing and manufacturing difficulty, low operation and maintenance cost and the like.
Additional features and advantages of the disclosure will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure without limiting the disclosure. In the drawings:
FIG. 1 is a schematic diagram of the structure of one embodiment of the radial moving bed reaction system of the present disclosure.
FIG. 2 is a schematic diagram of another embodiment of a radial moving bed reaction system of the present disclosure.
Description of the reference numerals
1-reactor 2-hopper
3-reactant inlet 4-product outlet
5-catalyst inlet 6-catalyst outlet
7-feeding distributor 8-split flow channel
9-collector channel 10-catalyst loading zone
11-catalyst blanking zone 12-reactor cylinder
13-outer screen 14-perforated pipe
15-catalyst feeding pipe 16-guide cylinder
17-inverted cone section 18-solid material (catalyst)
Detailed Description
The following detailed description of specific embodiments of the present disclosure is provided in connection with the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.
In the present disclosure, unless otherwise stated, the use of directional words such as "up" and "down" generally refers to the up and down of the device in normal use, and specifically refers to the orientation of the drawing in fig. 1. The "inner and outer" are with respect to the outline of the device itself. The material flowing in the catalyst loading zone is not limited to solid catalyst, but may be selected from solid adsorbent, solid absorbent, and the like, which react with and/or contact the fluid material in the reactor, and the "catalyst" or "solid catalyst" described below may refer to the solid material.
The first aspect of the present disclosure provides a radial moving bed reaction system, which includes a reactor cylinder 12 and a hopper 2, wherein the hopper 2 is integrally arranged on the upper part of the reactor cylinder 12; a catalyst filling area 10 is arranged in the reactor cylinder, the radial section of the catalyst filling area is annular, a shunt flow channel 8 is formed between the outer side wall of the catalyst filling area and the inner wall of one part of the reactor cylinder, a collecting flow channel 9 is formed between the inner side wall of the catalyst filling area and the inner wall of the other part of the reactor cylinder, and the shunt flow channel 8 is in fluid communication with the collecting flow channel 9 only through the catalyst filling area; the top of the catalyst filling area is sealed, the bottom of the catalyst filling area is communicated with a conical catalyst blanking area 11, a catalyst discharge port 6 is arranged at the bottom of the catalyst blanking area 11, an opening at the bottom end of the hopper is communicated with the catalyst filling area only through a catalyst feed pipe 15, and the catalyst feed pipe 15 is positioned in the reactor barrel; a reactant inlet 3 and a product outlet 4 are arranged on the reactor cylinder; reactant inlet 3 is in fluid communication with a split flow channel 8, product outlet 4 is in fluid communication with a collector flow channel 9, and product outlet 4 is located in the upper portion of collector flow channel 9.
The radial moving bed reaction system is provided with the hopper which is integrally arranged with the reactor barrel, and the hopper is communicated with the catalyst filling area in the reactor barrel through the catalyst feeding pipe which is positioned in the reactor barrel, so that the catalyst can enter the filling area after being preheated in the reactor barrel and moves downwards along the axial direction of the reactor, the temperature distribution uniformity of the catalyst filling area is improved, and the catalytic reaction is facilitated; in addition, the reactor disclosed by the invention can be used for uniformly distributing reaction raw materials, effectively avoiding short circuit of the reaction raw materials, enabling the fluid to flow nearly horizontally and smoothly and enabling the solid to flow smoothly without dead zones, and being beneficial to reaction.
In order to uniformly distribute the reaction raw material in the radial direction, in one embodiment, as shown in fig. 1, the hopper, the catalyst loading zone and the reactor cylinder may be coaxially disposed; furthermore, the top end of the catalyst loading area can be provided with an annular cover plate, and the top ends of the inner side wall and the outer side wall of the catalyst loading area can be respectively connected with the annular cover plate in a sealing way so as to seal the top end of the catalyst loading area; a sealing plate can be arranged between the outer edge of the annular cover plate and the inner wall of the reactor cylinder body so as to seal the top end of an outer flow passage positioned outside the catalyst filling area; the bottom end opening of the catalyst feeding pipe can penetrate through the annular cover plate to be communicated with the catalyst filling area; further, in order to make the reaction material flow through the catalyst loading region radially in the cylinder of the reactor to form cross flow, the inner side wall and the outer side wall of the catalyst loading region may respectively have openings, for example, the inner side wall of the catalyst loading region may be formed as a porous tube 14, the top end of the porous tube 14 is open, and the bottom end thereof is closed, for example, the bottom end of the porous tube may be provided with a sealing plate; in one embodiment, the outside of the perforated tube 14 may be sleeved with an outer screen 13 to form the outside wall of the catalyst loading zone; in another embodiment, the outside of the perforated tubes 14 may be provided with a segment cylinder module to form the outside wall of the catalyst loading zone; the sector cylinder module can be of a conventional type in the field, preferably, the sector cylinder module can comprise 10-100, preferably 10-40 sector cylinders, the sector cylinders can be vertically communicated, the radial cross sections of the sector cylinders are in a sector shape, so that the shunt flow channels 8 are formed in the sector cylinders, in this embodiment, in order to enable reaction materials to radially flow in the reactor cylinder, the inner arc-shaped walls of the sector cylinders can be provided with openings, the sector cylinders can be symmetrically distributed around the axial center of the reactor, and further, the sector cylinders can be tightly arranged around the outer side wall of the catalyst loading area, so that an annular gap between the outer side wall of the catalyst loading area and the inner wall of the reactor cylinder is filled with the sector cylinder module.
In a specific embodiment, the reactor barrel may sequentially comprise a conical barrel section, a cylindrical barrel section and an inverted conical barrel section from top to bottom, and the bottom end of the hopper 2 may be hermetically connected with the top end of the conical barrel section, and in this embodiment, preferably, the top end of the catalyst loading area is approximately the same as the top end of the cylindrical barrel section in height, that is, the catalyst loading area is distributed in the whole axial length direction of the cylindrical barrel section; the product outlet 4 can be located in the conical barrel section, in one embodiment, the reactant inlet 3 can be located in the upper part of the cylindrical barrel section, so that the reactant enters the reactor to form an upward-outward centripetal pi-shaped flow mode, in this embodiment, after entering the reactor barrel, the reactant enters the flow dividing flow channel between the outer wall of the annular catalyst filling area and the inner wall of the reactor barrel, after being uniformly distributed in the axial direction, the reactant enters the catalyst filling area along the radial direction, moves from the periphery to the center in the filling area, is in cross-flow contact with the catalyst, flows out from the inner side wall of the catalyst filling area, enters the flow collecting flow channel inside the annular catalyst filling area, and flows out from the product outlet in the upper part after the flow collecting flow channel is distributed; in another embodiment, the reactant inlet 3 may be located at the lower part of the cylindrical barrel section, so that the reactant enters the reactor to form a downward-in-upward-out centripetal Z-shaped flow pattern, in this embodiment, the reactant enters the reactor barrel from the lower part, enters the flow dividing channel between the outside of the annular catalyst filling region and the inner wall of the reactor barrel, axially and uniformly distributed, enters the catalyst filling region in the radial direction, moves from the periphery to the center in the filling region, contacts with the catalyst in a cross flow manner, flows out through the inner side wall of the catalyst filling region, enters the flow collecting channel inside the annular catalyst filling region, and flows out through the product outlet at the upper part after the flow collecting channel is distributed.
In the system according to the present disclosure, the number of the catalyst feeding pipes is preferably multiple, for example, 2 to 10, and the upper ends of the multiple catalyst feeding pipes are respectively communicated with the outlet at the bottom of the hopper, and the lower ends are distributed at equal intervals around the circumferential direction at the top of the annular catalyst loading area; further, a portion of the catalyst feed may extend at an angle to the axial direction, e.g., the upper portion of the catalyst feed may be parallel to the conical section of the barrel and the lower portion may extend axially along the reactor.
In the system according to the present disclosure, the catalyst enters the catalyst feeding pipe from the outlet at the bottom end of the hopper, moves downwards, enters the catalyst filling area, continues to move downwards in the filling area, contacts with the reaction material passing through the catalyst filling area in the radial direction in a cross flow manner, then enters the conical annular catalyst blanking space, and flows out of the reactor through the catalyst discharging port; further, in order to smoothly move the catalyst downward, the bottom of the perforated pipe 14 may be provided with a catalyst guide assembly in one embodiment, and the catalyst guide assembly may include a guide cylinder 16 in one embodiment; the guide shell 16 may be disposed coaxially with the perforated pipe 14, and in a preferred embodiment, the guide shell may have a tapered diameter in a radial section, for example, the guide shell may have an inverted cone shape, and the bottom of the inverted cone shape may be aligned with the catalyst outlet 6. In this embodiment, the bottom end of the perforated pipe can be connected with the guide cylinder 16, the outer diameter of the upper end of the guide cylinder is preferably the same as the outer diameter of the bottom end of the perforated pipe, so as to facilitate the downward flow of the solid catalyst, the gap between the inverted cone-shaped cylinder section 17 and the guide cylinder 16 can be formed into a catalyst blanking zone 11, the cross section of the catalyst blanking zone is annular, the diameter of the catalyst blanking zone is gradually reduced from top to bottom, a space for a catalyst flowing area is formed below the catalyst loading zone, so as to facilitate the downward flow of the catalyst, reduce the dead zone of the catalyst to the utmost extent, and prevent the catalyst; the catalyst outlet 6 can be arranged at the bottom of the inverted cone-shaped cylinder section 17, preferably in the center of the bottom.
The draft tube 16 can occupy the space below the perforated tube 14 to avoid dead space formed by the accumulation of catalyst flowing downward; further, in an embodiment, the conical bottom of the guide cylinder 16 may be closed, and the catalyst discharge port 6 may be provided with a seal gas inlet, so that seal gas is injected into the catalyst discharge port 6 from bottom to top, and the seal gas may perform a stripping action on the catalyst flowing downward, thereby preventing a reaction material in the catalyst zone from flowing out of the catalyst discharge port 6 and losing; in another embodiment, as shown in fig. 1, the conical bottom of the guide cylinder 16 may have an opening, and the guide cylinder may be provided with a sealing gas inlet inside, so as to inject sealing gas into the catalyst outlet from top to bottom, so as to further promote the catalyst to flow downward at the outlet 6; in this embodiment, the seal gas inlet is preferably located on the centerline above the opening of the draft tube 16.
In accordance with the disclosed system, the inner and outer side walls of the catalyst loading zone may be fixed within the reactor, e.g., in one embodiment, one of the upper and lower ends of the inner side wall is fixed and the other end is a free end; one of the upper end and the lower end of the outer side wall is fixed, and the other end of the outer side wall is a free end; the outer side wall and the inner side wall are not provided with expansion joints; further, in one embodiment, the bottom end of the perforated pipe can be fixedly connected with the reactor cylinder, and the top end is a free end; in embodiments where the outer sidewall of the catalyst loading zone is formed as an outer screen, the top end of the outer screen may be fixedly connected to the cylindrical section of the reactor barrel, the bottom end being a free end; in the embodiment where the fan-shaped barrel module is disposed outside the perforated pipe, the bottom end of the fan-shaped barrel module may be fixedly connected to the inverted conical barrel section of the reactor barrel, and the top end is a free end. In the above embodiment, only one end of the upper and lower ends of the inner side wall and the outer side wall of the catalyst filling area is fixed, and the other end is a free end, so that the stable form of the catalyst filling area can be ensured, the expansion joint can be prevented from being installed, the difficulty of processing, installation and maintenance is reduced, and the equipment investment is saved.
In an embodiment in which the bottom end of the perforated pipe is fixedly connected with the reactor cylinder, further, in an embodiment, the system may further comprise a support cylinder, the support cylinder may be disposed at the bottom of the perforated pipe, for example, coaxially between the perforated pipe and the guide cylinder, and the outer diameter of the support cylinder is preferably the same as the outer diameter of the bottom end of the perforated pipe; further, the outside of supporting a section of thick bamboo can set up a plurality of axially extended strengthening ribs, and a plurality of strengthening ribs can be around section of thick bamboo wall circumference evenly distributed, and the shape of strengthening rib can be for example falling trapezoidal to it is fixed with the inner wall block of back taper section of thick bamboo to make supporting a section of thick bamboo pass through the strengthening rib. In this embodiment, the bottom end of the perforated pipe can be fixedly connected with the reactor cylinder through the support cylinder in a manner that does not affect the downward flow of the catalyst in the conical catalyst blanking zone 11 and does not easily form a catalyst dead zone.
In the system according to the present disclosure, the size of the catalyst loading zone may vary within a large range, preferably the radial width B of the catalyst loading zone may be 100-1500 mm, preferably 150-1000 mm; the opening rate of the outer side wall of the catalyst loading area can be 15-35%, and is preferably 15-25%; the opening rate of the inner side wall of the catalyst filling area can be 0.5-10%, and preferably 0.5-3%; within the preferred size range, the axial distribution of the feed fluid velocity can be ensured to be uniform, and the pressure drop of the bed layer is lower than 20 kPa. Further, in order to prevent short-circuiting of the streams, the upper portions of the inner and outer side walls of the catalyst loading zone may respectively include a non-porous region, and the axial length of the non-porous region may be 0.3B to 5B, preferably 0.3B to 2B.
In one embodiment, in order to make the reactant material uniformly distributed, the system of the present disclosure may further include a feed distributor in one embodiment, the feed distributor may be located in the divided flow channel, and the feed distributor may be directed toward the reactant inlet 3, for example, in one embodiment, the feed distributor is located near the reactant inlet and spaced from the reactant inlet, preferably, the projection of the feed distributor in the direction of the reactant inlet covers the reactant inlet; the type of feed distributor is not particularly limited, for example the feed distributor is a baffled distributor, a vaned distributor or a tangential ring distributor, or a combination of two or three of them.
A second aspect of the present disclosure provides a method for performing a flow-solid reaction using the above system, the method comprising: continuously feeding the solid material in the hopper into a catalyst filling area; the reaction material enters the catalyst filling area through a reactant inlet 3 and is in contact reaction with the solid material.
The flow-solid reaction refers to a reaction in which a reaction raw material in which a solid material such as a solid catalyst and/or a solid adsorbent participates is a fluid, wherein the solid material can flow from top to bottom in a catalyst loading area of the system. Further, the flow-solid reaction may include at least one of a dehydrogenation reaction of a lower hydrocarbon, a reforming reaction, and a flue gas desulfurization reaction. The carbon number of the low-carbon hydrocarbon as the reaction raw material in the dehydrogenation reaction of the low-carbon hydrocarbon is, for example, 2 to 7, and the low-carbon hydrocarbon may be at least one of ethane, propane, butane, pentane, hexane, and heptane. The reaction raw material of the reforming reaction can be at least one of straight-run naphtha, hydrocracking heavy naphtha and ethylene cracking raffinate; the flue gas in the flue gas desulfurization reaction can be at least one of catalytic flue gas, heating furnace flue gas and incinerator flue gas.
In accordance with the present disclosure, the raw materials and conditions for performing the flow-solid reaction are not particularly limited and may be conventional in the art, preferred reaction raw materials may be gas or liquid, and preferred catalysts may be at least one of spherical, rod-shaped, porous cylindrical and butterfly-shaped.
The flow-solid reaction conditions may include: the operation pressure is 0.02-1.5 MPa, preferably 0.05-1.0 MPa, the reaction temperature is 400-650 ℃, and preferably 500-630 ℃; the reaction material can be gas, and the flow rate can be 20-250 m3Preferably 50 to 200 m/s3S; the loading of the catalyst can be 10-200 m3Preferably 40 to 100m3(ii) a The circulating amount of the catalyst may be 0.5 to 3kg/h, preferably 0.7 to 2.5 kg/h.
In the above-described embodiments in which the reaction system includes a seal gas inlet, the seal gas may be selected from at least one of hydrogen, nitrogen, and argon, and injected into the flow of seal gasThe amount of the water-soluble polymer can be 20 to 500m3H; further, in the embodiment of injecting the sealing gas into the catalyst discharge port 6 from bottom to top, the gas velocity of the sealing gas may be 40-70 m3S; in the embodiment of injecting the sealing gas toward the catalyst discharge port 6 from the top to the bottom, the gas velocity of the sealing gas may be 30 to 50m3/s。
Example 1
This example illustrates the radial moving bed reaction system of the present disclosure and a method for performing a flow-solid reaction using the same.
As shown in fig. 1, the radial moving bed reaction system comprises a reactant inlet 3, a feed distributor 7, a diversion flow channel 8, a catalyst filling area 10, a flow collecting flow channel 9, a product outlet 4, a catalyst inlet 5, a hopper 2, a catalyst feeding pipe 15, a catalyst discharging port 6 and a catalyst blanking area 11. Wherein, the reactant inlet 3 is positioned on the reaction cylinder body and has the same height with the upper part of the catalyst filling area; the product outlet 4 is positioned on the cylinder body of the reactor and is at the same height with the catalyst feeding pipe; the reactor barrel sequentially comprises a conical barrel section, a cylindrical barrel section and an inverted conical barrel section from top to bottom, the conical barrel section, the cylindrical barrel section and the inverted conical barrel section are sequentially connected to form a sealed barrel, and a perforated pipe and an outer screen sleeved outside the perforated pipe are arranged in the barrel; the hopper is positioned above the reactor, and the bottom of the hopper cylinder is connected with the top end of the reactor conical cylinder; the catalyst feeding pipe is completely positioned in the reactor; the flow dividing flow channel, the catalyst filling area and the flow collecting flow channel are coaxially arranged from outside to inside; the catalyst blanking area is positioned at the lower part of the reactor; the reactant inlet, the flow dividing channel, the catalyst filling area, the flow collecting channel and the product outlet are communicated in sequence.
The feeding structure at the bottom of the reactor adopts a conical guide cylinder, the guide cylinder is connected to the bottom end of the perforated pipe, and the bottom end of the guide cylinder is opened; the catalyst blanking area is positioned between the conical guide cylinder and the inverted conical cylinder section; the catalyst discharge port is positioned on the conical bottom of the inverted conical barrel section and is coaxial with the reactor; the inside of the draft tube can be provided with a sealing gas inlet, sealing gas nitrogen is sprayed to the catalyst discharge port from top to bottom, and the flow is 45m3/h。
The top end of the outer screen is fixedly connected with the reactor cylinder, and the bottom end is a free end; the bottom end of the perforated pipe is connected to the inverted cone-shaped section of the reactor barrel through a reinforcing rib, and the top end of the perforated pipe is a free end.
The diameter of the reactor is 4.5m, the diameter of the outer screen is 4.3m, the opening rate is 25%, the diameter of the inner perforated pipe is 3.5m, and the opening rate is 1.0%, and the reactor is used for controlling the uniform distribution of the fluid. The thickness B of the bed layer is 0.38 m; the upper parts of the inner perforated pipe and the outer screen mesh are not perforated, and the length h of the non-perforated area is 0.8 m. The feed distributor is located at the reactant inlet and is a baffle distributor.
The reaction raw material is propane gas, the propane dehydrogenation reaction is carried out, the catalyst is Pt supported spherical solid particles, the feeding flow is 200m3The circulating amount of the solid catalyst was 1.0 kg/h. The operation pressure is 0.13MPa, and the reaction temperature is 600 ℃ for gas-solid reaction. Light hydrocarbon gas enters the reactor through the reactant inlet and flows to the flow dividing channel after passing through the gas distributor. Then the catalyst uniformly flows into a catalyst bed layer after passing through an outer screen, enters a flow collecting channel through a porous pipe, and is discharged out of the reactor through a product outlet. The catalyst with high activity is stored in a hopper, enters the reactor through a catalyst feeding pipe, slowly moves downwards in the reactor by means of gravity, and is discharged from a catalyst discharging port through a catalyst filling area and a catalyst discharging area.
Compared with the existing radial moving bed reactor, when the radial moving bed reaction system of the embodiment is adopted to carry out alkylation reaction, the gas flow uniformity can be obviously improved, the catalyst flow dead zone is avoided, the reaction conversion rate can be improved from 25% to 30% or more, and the product selectivity is improved by 2-5%. Therefore, the radial moving bed reaction system and the flow-solid reaction method disclosed by the invention are beneficial to the flow-solid reaction and can effectively improve the product yield.
Example 2
This example illustrates the radial moving bed reaction system of the present disclosure and a method for performing a flow-solid reaction using the same.
As shown in fig. 2, the radial moving bed reaction system comprises a reactant inlet 3, a feed distributor 7, a diversion flow channel 8, a catalyst filling area 10, a flow collecting flow channel 9, a product outlet 4, a catalyst inlet 5, a hopper 2, a catalyst feeding pipe 15, a catalyst discharging port 6 and a catalyst blanking area 11. Among these, the reaction system differs from the reaction system of example 1 only in that: the reactant inlet 3 is located on the reaction cylinder at the same height as the lower portion of the catalyst loading zone. The diameter of the reactor is 4.0m, the diameter of the outer screen is 3.7m, the opening rate is 25%, the diameter of the inner perforated pipe is 3.0m, and the opening rate is 1.5%, and the reactor is used for controlling the uniform distribution of the fluid. The thickness B of the bed layer is 0.32 m; the upper parts of the inner perforated pipe and the outer screen mesh are not perforated, and the length h of the non-perforated area is 0.6 m. The feed distributor is located at the reactant inlet and is a baffle distributor.
The reaction raw material is butane gas, dehydrogenation reaction is carried out, the catalyst is Pt supported spherical solid particles, and the feeding flow rate is 180m3The circulating amount of the solid catalyst was 0.9 kg/h. The operation pressure is 0.09MPa, and the reaction temperature is 550 ℃ for gas-solid reaction. Light hydrocarbon gas enters the reactor through the reactant inlet and flows to the flow dividing channel after passing through the gas distributor. Then the catalyst uniformly flows into a catalyst bed layer after passing through an outer screen, enters a flow collecting channel through a porous pipe, and is discharged out of the reactor through a product outlet. The catalyst with high activity is stored in a hopper, enters the reactor through a catalyst feeding pipe, slowly moves downwards in the reactor by means of gravity, and is discharged from a catalyst discharging port through a catalyst filling area and a catalyst discharging area.
Compared with the existing radial moving bed reactor, when the radial moving bed reaction system of the embodiment is adopted to carry out alkylation reaction, the gas flow uniformity can be obviously improved, the catalyst flow dead zone is avoided, the reaction conversion rate can be improved from 25% to 30% or more, and the product selectivity is improved by 2-5%. Therefore, the radial moving bed reaction system and the flow-solid reaction method disclosed by the invention are beneficial to the flow-solid reaction and can effectively improve the product yield.
The preferred embodiments of the present disclosure are described in detail with reference to the accompanying drawings, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.
It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. In order to avoid unnecessary repetition, various possible combinations will not be separately described in this disclosure.
In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure, as long as it does not depart from the spirit of the present disclosure.
Claims (10)
1. A radial moving bed reaction system is characterized in that the reaction system comprises a reactor cylinder (12) and a hopper (2), wherein the hopper is integrally arranged at the upper part of the reactor cylinder; a catalyst filling area (10) is arranged in the reactor cylinder, the radial section of the catalyst filling area is annular, a shunt flow channel (8) is formed between the outer side wall of the catalyst filling area and one part of the inner wall of the reactor cylinder, a collecting flow channel (9) is formed between the inner side wall of the catalyst filling area and the other part of the inner wall of the reactor cylinder, and the shunt flow channel (8) is in fluid communication with the collecting flow channel (9) only through the catalyst filling area; the top of the catalyst filling area is sealed, the bottom of the catalyst filling area is communicated with a conical catalyst blanking area (11), a catalyst discharge hole (6) is formed in the bottom of the catalyst blanking area (11), an opening in the bottom end of the hopper is communicated with the catalyst filling area only through a catalyst feed pipe (15), and the catalyst feed pipe (15) is positioned in the reactor barrel; a reactant inlet (3) and a product outlet (4) are arranged on the reactor cylinder; the reactant inlet (3) is in fluid communication with the diverging flow channels (8), the product outlet (4) is in fluid communication with the collecting flow channels (9), and the product outlet (4) is located at an upper portion of the collecting flow channels (9).
2. The system according to claim 1, wherein the hopper (2), the catalyst loading zone (10) and the reactor barrel (12) are arranged coaxially; the top end of the catalyst filling area (10) is provided with an annular cover plate; the bottom end of the catalyst feeding pipe is opened to penetrate through the annular cover plate to be communicated with the catalyst filling area; the inner side wall of the catalyst filling area (10) is formed into a perforated pipe (14), the top end of the perforated pipe (14) is open, and the bottom end is closed; the outer side of the perforated pipe (14) is provided with an outer screen (13) or a fan-shaped cylinder module to form the outer side wall of the catalyst loading area (10); the fan-shaped cylinder module comprises 10-100 fan-shaped cylinders, the fan-shaped cylinders are vertically communicated, the radial sections of the fan-shaped cylinders are fan-shaped, the inner arc-shaped walls of the fan-shaped cylinders are provided with openings, and the fan-shaped cylinders are symmetrically distributed around the axial center of the reactor.
3. The system according to claim 2, wherein the reactor barrel comprises a conical barrel section, a cylindrical barrel section and an inverted conical barrel section (17) from top to bottom in sequence, and the bottom end of the hopper (2) is hermetically connected with the top end of the conical barrel section; the product outlet (4) is located in the conical barrel section, and the reactant inlet (3) is located in the upper part or the lower part of the cylindrical barrel section; the catalyst discharge hole (6) is arranged at the bottom of the inverted conical cylinder section (17);
the bottom of the perforated pipe (14) is provided with a catalyst guide assembly, and the catalyst guide assembly comprises a guide cylinder (16); the guide cylinder (16) and the perforated pipe (14) are coaxially arranged, the guide cylinder (16) is in an inverted cone shape, and the cone bottom of the inverted cone shape is aligned with the catalyst discharge hole (6);
and a gap between the inverted conical cylinder section (17) and the guide cylinder (16) is formed into the catalyst blanking area (11).
4. The system according to claim 3, wherein the conical bottom of the guide shell (16) is closed, and the catalyst discharge port (6) is provided with a sealing gas inlet for injecting sealing gas into the catalyst discharge port (6) from bottom to top; alternatively, the first and second electrodes may be,
the conical bottom of draft tube (16) has the opening, draft tube (16) inside is equipped with sealed gas entry to from top to bottom to catalyst discharge gate sprays sealed gas.
5. A system according to claim 3, wherein one of the upper and lower ends of the outer side wall of the catalyst loading zone (10) is fixed and the other end is a free end; one of the upper end and the lower end of the inner side wall of the catalyst filling area (10) is fixed, and the other end is a free end; the outer side wall and the inner side wall are not provided with expansion joints;
preferably, the top end of the outer screen (13) is fixedly connected with the reactor cylinder body, and the bottom end is a free end, or the bottom end of the fan-shaped cylinder module is fixedly connected with the reactor cylinder body, and the top end is a free end; the bottom end of the perforated pipe (14) is connected to the inverted cone-shaped section (17) of the reactor barrel, and the top end is a free end.
6. The system according to claim 5, wherein the bottom end of the perforated tube (14) is provided with a support cylinder; the supporting cylinder is coaxially arranged between the perforated pipe (14) and the guide cylinder (16), a plurality of axially extending reinforcing ribs are arranged on the outer side of the supporting cylinder, and the supporting cylinder is clamped and fixed with the inner wall of the inverted cone-shaped cylinder section (17) through the reinforcing ribs.
7. The system according to claim 1, wherein the radial width B of the catalyst loading zone (10) is comprised between 100 and 1500 mm; the opening rate of the outer side wall of the catalyst filling area is 15% -35%, and the opening rate of the inner side wall of the catalyst filling area is 0.5% -10%; the upper parts of the inner side wall and the outer side wall of the catalyst filling area respectively comprise a non-porous area, and the axial length of the non-porous area is 0.3B-5B.
8. The system of claim 1, further comprising a feed distributor (7), the feed distributor (7) being located within the flow diversion channel (8), the feed distributor being directed towards the reactant inlet (3); the feed distributor (7) is a baffle distributor, a blade distributor or a tangential circulation distributor, or a combination of two or three of them.
9. A method for conducting a flow-solid reaction using the system of any one of claims 1 to 8, the method comprising: continuously feeding the solid material in the hopper into the catalyst loading zone; and enabling the reaction material to enter the catalyst filling area through the reactant inlet to perform contact reaction with the solid material.
10. The method of claim 9, wherein the flow-solid reaction comprises at least one of a lower hydrocarbon dehydrogenation reaction, a reforming reaction, and a gas desulfurization reaction; the solid material comprises a solid catalyst and/or a solid adsorbent.
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Inventor after: Yuan Zhongxun Inventor after: Gao Liping Inventor after: Li Yuxin Inventor after: SiMa Jian Inventor after: Xu Wei Inventor after: Li Xiaodong Inventor before: Yuan Zhongxun Inventor before: Gao Liping Inventor before: Li Yuxin Inventor before: SiMa Jian Inventor before: Xu Wei Inventor before: Li Xiaodong |