CN114682172B - Catalytic distillation reactor and internals therefor - Google Patents

Catalytic distillation reactor and internals therefor Download PDF

Info

Publication number
CN114682172B
CN114682172B CN202011603476.6A CN202011603476A CN114682172B CN 114682172 B CN114682172 B CN 114682172B CN 202011603476 A CN202011603476 A CN 202011603476A CN 114682172 B CN114682172 B CN 114682172B
Authority
CN
China
Prior art keywords
reactor
catalyst
wire mesh
shaft
reactor internals
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN202011603476.6A
Other languages
Chinese (zh)
Other versions
CN114682172A (en
Inventor
王晶晶
郭兵兵
徐彤
宣根海
刘涛
马蕊英
吴锐
桂兴华
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sinopec Dalian Petrochemical Research Institute Co ltd
China Petroleum and Chemical Corp
Original Assignee
China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Dalian Research Institute of Petroleum and Petrochemicals filed Critical China Petroleum and Chemical Corp
Priority to CN202011603476.6A priority Critical patent/CN114682172B/en
Publication of CN114682172A publication Critical patent/CN114682172A/en
Application granted granted Critical
Publication of CN114682172B publication Critical patent/CN114682172B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/085—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00893—Feeding means for the reactants
    • B01J2208/00911—Sparger-type feeding elements
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

The invention discloses a reactor internals, comprising: a catalyst layer formed by arranging a plurality of catalyst strings, each catalyst string including: a shaft rod arranged in a horizontal direction; one or more wire mesh containers detachably disposed through the shaft, the wire mesh containers being rotatable about the shaft; and a filler filled in the wire container, the filler including a catalyst; and a support assembly for mounting the catalyst layer within the reactor. The invention also discloses a catalytic distillation reactor, comprising: the reactor body is provided with a liquid inlet at the upper part and a gas inlet at the lower part; and at least one reactor internals mounted in the reactor body. The catalytic distillation reactor and the internal components thereof have good gas-liquid distribution effect in the reaction zone through the rotatable wire mesh container, are beneficial to full contact of gas-liquid reactants and the surface of the catalyst, and avoid channeling and other phenomena caused by uneven catalytic reaction.

Description

Catalytic distillation reactor and internals therefor
Technical Field
The invention relates to the technical field of catalytic distillation equipment, in particular to a gas-liquid-solid three-phase catalytic distillation reactor and an internal component thereof.
Background
The catalytic distillation technology is to organically couple the catalytic reaction and the rectification separation in the same equipment, so that the catalytic reaction and the rectification separation can be simultaneously completed. The key of the catalytic distillation technology lies in the construction mode of the catalytic distillation component in the catalytic distillation tower, including the factors of the catalyst used in the catalytic distillation component, the configuration of the packing, the filling mode of the catalyst and the packing and the like. The gas-liquid-solid three-phase mixed contact type filling method belongs to a filling mode with a large application range, and can be applied to various types of catalytic reactions. For some catalysts widely used in industry, if the catalyst is directly loaded into a catalyst rectifying tower, the high bulk density directly causes the too small void ratio and the too large pressure drop, so that the mass transfer efficiency is reduced, and sufficient space for the gas phase reaction product to rise cannot be provided. Therefore, the catalyst is packaged and processed to form an internal component to be loaded into the catalytic distillation tower at many times.
Patent document US4443559 proposes a catalytic distillation column internal member composed of a catalyst element and an elastic element, wherein catalyst particles are filled in the element composed of a plurality of layers of silk screens, and because the redistribution capability of the fluid is poor due to the silk screens, reactants are not easy to enter and exit, channeling is easily caused, and the mass transfer and the catalytic effect are influenced. Patent documents US5275790 and US5262012 respectively propose that porous inert pellets and a catalyst are uniformly mixed and then are filled into metal boxes with mesh or porous walls with different structures, and the metal boxes form the internal part of the catalytic distillation tower, and the internal part is easy to generate channeling in a bed layer to influence mass transfer and reaction effects.
The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and should not be taken as an acknowledgement or any form of suggestion that this information forms the prior art that is already known to a person skilled in the art.
Disclosure of Invention
One of the objectives of the present invention is to provide a catalytic distillation reactor and its internal components, so as to improve the problems of non-uniform reaction and easy channeling of the catalyst bed layer of the existing catalytic distillation reactor.
To achieve the above object, according to a first aspect of the present invention, there is provided a reactor internals, comprising: a catalyst layer formed by arranging a plurality of catalyst strings, each catalyst string including: a shaft rod arranged in a horizontal direction; one or more wire mesh containers detachably disposed through the shaft, the wire mesh containers being rotatable about the shaft; and a filler filled in the wire container, the filler including a catalyst; and a support assembly for mounting the catalyst layer within the reactor.
Further, in the above technical scheme, the wire mesh container is of a rotational symmetric structure.
Further, in the above technical solution, the cross section of the wire mesh container perpendicular to the shaft rod is circular, regular polygon, star, flower or cam.
Further, in the technical scheme, the filling rate of the filler in the wire mesh container is 20% -80%.
Further, in the technical scheme, the equivalent diameter of the wire mesh container is 1 mm-100mm.
Further, in the above technical scheme, the wire mesh container is mounted on the shaft rod through a bearing, and the dynamic friction coefficient of the bearing is less than or equal to 0.2.
Further, in the above technical scheme, the catalyst is a solid catalyst or a porous catalyst; the particle size of the catalyst is phi 1-phi 15mm.
Further, in the above technical solution, the filler further includes an inert filler.
Further, in the above technical solution, the wire mesh container is made of a metal wire or a non-metal wire.
Further, in the above technical solution, the mesh size of the wire mesh container is smaller than the size of the filler.
Further, among the above-mentioned technical scheme, the bracket component includes: a mesh plate disposed under the catalyst layer; and a support plate supporting the shaft on the mesh plate.
Further, in the above technical solution, the reactor inner member further comprises: the distribution plate is arranged above the catalyst layer and is provided with a plurality of first diameter-variable pore channels and a plurality of second diameter-variable pore channels, the diameters of the first diameter-variable pore channels are gradually reduced from bottom to top, and the diameters of the second diameter-variable pore channels are gradually increased from bottom to top.
Further, in the technical scheme, the diameters of the small ends of the first diameter-variable channel and the second diameter-variable channel are phi 1 mm-phi 25mm, the included angle of the first diameter-variable channel is 20 to 70 degrees, and the included angle of the second diameter-variable channel is 20 to 70 degrees.
According to a second aspect of the present invention, there is provided a catalytic distillation reactor comprising: the reactor body is provided with a liquid inlet at the upper part and a gas inlet at the lower part; and at least one reactor internals as in any one of the previous claims, mounted in the reactor body.
Further, in the above technical solution, when the number of the reactor internals is plural, the plural reactor internals are integrally installed in the reactor body or installed in the reactor body layer by layer.
Further, in the technical scheme, when a plurality of reactor internals are provided, the wire mesh containers of two adjacent layers of reactor internals are distributed in a staggered manner.
Further, in the above technical scheme, the liquid phase reactant and the gas phase reactant flow reversely and enter the wire mesh container from both sides of the shaft rod respectively, so as to drive the wire mesh container to swing or rotate around the shaft rod.
Compared with the prior art, the invention has the following beneficial effects:
1. the catalytic distillation reactor and the internal components thereof have a good gas-liquid distribution effect in the reaction area through the rotatable wire mesh container, are beneficial to full contact of gas-liquid reactants and the surface of a catalyst, and avoid bad mass transfer phenomena such as channeling and the like caused by uneven catalytic reaction.
2. The reactor inner member of the invention realizes back mixing of gas phase and liquid phase, can utilize the kinetic energy of gas phase reactants, and has small pressure drop and large circulation in a reaction area, and is not easy to cause flooding.
3. In the catalytic distillation reactor, liquid phase and gas phase reactants simultaneously flow into the wire mesh container from the left side and the right side of the shaft rod in a counter-flow manner, so that the wire mesh container is promoted to swing or rotate to realize the self-turning of the filler, and further, the void ratio of the catalyst layer is increased.
4. The screen plate and the distribution plate can play a role of fixing a screen container and have a mass transfer separation function.
5. The silk screen container can be worn to establish on the axostylus axostyle with dismantling, conveniently changes the filler.
The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical means of the present invention more clearly understood and to make the technical means implementable in accordance with the content of the description, and to make the above and other objects, technical features, and advantages of the present invention more comprehensible, one or more preferred embodiments are listed below, and are described in detail below with reference to the accompanying drawings.
Drawings
FIG. 1 is an axial cross-sectional partial schematic view of a catalytic distillation reactor according to an embodiment of the present invention.
FIG. 2 is a schematic radial cross-sectional view of a catalytic distillation reactor according to an embodiment of the present invention.
Fig. 3 is a schematic cross-sectional view of a wire mesh container according to an embodiment of the present invention.
Fig. 4 is a schematic sectional view of a wire mesh container according to another embodiment of the present invention.
FIG. 5 is a schematic cross-sectional view of a catalyst string according to an embodiment of the present invention.
FIG. 6 is a schematic cross-sectional view of a catalyst string according to another embodiment of the present invention.
Description of the main reference numerals:
10-a reactor body, 20-a catalyst layer, 21a, 21 b-a catalyst string group, 211-a shaft rod, 212-a screen container, 212 a-a cylindrical screen container, 212 b-a prismatic screen container, 213-a filler, 214-a bearing, 31-a screen plate, 32-a support plate, 40-a distribution plate, 41-a first variable diameter pore canal and 42-a second variable diameter pore canal.
Detailed Description
Specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings, but it should be understood that the scope of the present invention is not limited to the specific embodiments.
Throughout the specification and claims, unless explicitly stated otherwise, the term "comprise" or variations such as "comprises" or "comprising", etc., will be understood to imply the inclusion of a stated element or component but not the exclusion of any other element or component.
Spatially relative terms, such as "below," "lower," "upper," "above," "upper," and the like, may be used herein for ease of description to describe one element or feature's relationship to another element or feature in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the article in use or operation in addition to the orientation depicted in the figures. For example, if the items in the figures are turned over, elements described as "below" or "beneath" other elements or features would then be oriented "above" the elements or features. Thus, the exemplary term "below" can encompass both an orientation of below and above. The articles may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative terms used herein should be interpreted accordingly.
As used herein, the terms "first," "second," and the like are used to distinguish two different elements or regions, and are not intended to define a particular position or relative relationship. In other words, the terms "first," "second," and the like may also be interchanged with one another in some embodiments.
As shown in fig. 1 to 6, the reactor internals according to embodiments of the present invention are used in a catalytic distillation reactor. The reactor internals include a catalyst layer 20 and a support assembly that mounts it within the reactor. The catalyst layer 20 is formed by arranging a plurality of catalyst strings. Illustratively, as shown in fig. 5, the catalyst string 21a may include a shaft 211 and a wire mesh container 212. Alternatively, as shown in fig. 6, the catalyst string 21b may include a shaft 211 and three wire mesh containers 212. It should be understood that the present invention is not limited thereto, and the number of the wire mesh containers 212 penetrating through each shaft 211 is not limited thereto, and can be selected by those skilled in the art according to actual needs. The shaft 211 is arranged in a horizontal direction, the screen container 212 is detachably inserted into the shaft 211 and can rotate around the shaft 211, and the screen container 212 is filled with filler 213, wherein the filler 213 includes a catalyst. When only one wire mesh container 212 is pierced through one shaft 211 as shown in fig. 5 and 2, the arrangement of the wire mesh containers is more flexible; when a plurality of wire mesh containers are arranged on one shaft rod in a penetrating mode, the wire mesh containers in the same row can share one shaft rod, and the catalyst layer formed by the catalyst series is simpler in structure.
Further, in one or more exemplary embodiments of the invention, the wire mesh container 212 is a rotationally symmetric structure. Further, in one or more exemplary embodiments of the present invention, a cross-section of the screen container perpendicular to the shaft 211 may be a circle, i.e., a cylindrical screen container 212a (shown in fig. 3); the cross section of the screen container perpendicular to the shaft 211 may be a regular pentagon, i.e., a prismatic screen container 212b (shown in fig. 4). It should be understood that the present invention is not limited thereto, and the cross-section of the wire container perpendicular to the shaft 211 may be circular, regular polygonal, star-shaped, flower-shaped, or cam-shaped.
Further, in one or more exemplary embodiments of the present invention, the filler 213 may be filled in the wire mesh container, and a filling rate of 20% to 80% may be selected. Further, in one or more exemplary embodiments of the invention, the equivalent diameter of the wire mesh container 212 is 10mm to 100mm. Further, in one or more exemplary embodiments of the present invention, the wire mesh container 212 is mounted on the shaft 211 through a bearing 214, and a dynamic friction coefficient of the bearing 214 is less than or equal to 0.2, thereby enabling the wire mesh container 212 to swing or rotate under the action of the gas-liquid two-phase.
Further, in one or more exemplary embodiments of the present invention, the packing 213 may be any catalyst used for catalyzing a distillation reaction, and the catalyst particles may be a solid catalyst or a porous catalyst. Preferably, but not limitatively, the catalyst used is spherical, cylindrical, clover-shaped, polyhedral or cross-cylindrical, etc. The particle size of the catalyst can be determined according to the specific selected catalyst particle configuration, and the particle size can be phi 1-phi 15mm. Further, in one or more exemplary embodiments of the present invention, the filler 213 may also be a mixture of catalyst particles and inert filler, which has a similar shape and size to the catalyst particles.
Further, in one or more exemplary embodiments of the present invention, the wire mesh container 212 is made of a metal wire or a non-metal wire, and has a strength to support the filler 213, and to ensure that the wire mesh container 212 is not deformed after filling. Further, in one or more exemplary embodiments of the present invention, the mesh size of the wire mesh container 212 is slightly smaller than the size of the filler 213, and the mesh size of the wire mesh container 212 is as large as possible while ensuring that the filler 213 does not leak out.
Further, in one or more exemplary embodiments of the present invention, the bracket assembly may include a mesh plate 31 and a support plate 32. The mesh plate 31 is disposed below the catalyst layer 20; the support plate 32 supports and fixes the shaft 211 to the mesh plate 31. The net plate 31 is a grid support with certain strength.
Further, in one or more exemplary embodiments of the present invention, the reactor internals further include a distribution plate 40, as shown in FIG. 1. The distribution plate 40 is arranged above the catalyst layer 20, the distribution plate is provided with a plurality of first diameter-variable pore canals 41 and a plurality of second diameter-variable pore canals 42, the diameter of the first diameter-variable pore canals 41 is gradually reduced from bottom to top, and the diameter of the second diameter-variable pore canals 42 is gradually increased from bottom to top. Further, in one or more exemplary embodiments of the present invention, the diameters of the small ends of the first diameter-varying hole 41 and the second diameter-varying hole 42 are phi 1mm to phi 25mm, the included angle of the first diameter-varying hole 41 is 20 to 70 °, and the included angle of the second diameter-varying hole 42 is 20 to 70 °. The first diameter-varying pore passage 41 forms a gas phase passage from bottom to top, and the second diameter-varying pore passage 42 forms a liquid phase passage from top to bottom. The liquid phase from the upper part is guided by the distribution plate 40 and enters the wire mesh container 212; the gas phase from below is guided through the distribution plate 40 (distribution plate of the lower reactor internals) and also into the wire mesh vessel 212. The gas phase and the liquid phase counter flow and respectively enter the screen container 212 from two sides of the shaft 211, so that the screen container 212 is driven to swing or rotate around the shaft, and accordingly, the fillers 213 in the screen container 212 are self-turned. If the wire mesh container 212 is not filled with the filler 213, the filler 213 can also be redistributed in the wire mesh container 212.
Referring to fig. 1, a catalytic distillation reactor according to an embodiment of the present invention includes a reactor body 10 and at least one reactor internals of the present invention. The reactor body 10 is provided with a liquid inlet at the upper part and a gas inlet (not shown) at the lower part, and the gas phase and the liquid phase are in countercurrent contact reaction in the reactor inner member.
Further, in one or more exemplary embodiments of the present invention, when the reactor internals are plural, the plural reactor internals may be fabricated as a bundle pack, installed in the reactor body 10 as a whole; a plurality of reactor internals may also be installed layer by layer in the reactor body 10, and the invention is not limited thereto.
Further, in one or more exemplary embodiments of the present invention, when the reactor internals are plural, the wire mesh containers 212 of two adjacent layers of the reactor internals may be staggered.
Further, in one or more exemplary embodiments of the present invention, the liquid-phase reactant and the gas-phase reactant flow in counter-current and enter the screen container 212 from both sides of the shaft 211, respectively, thereby driving the screen container 212 to swing or rotate about the shaft 211.
The catalytic distillation reactor and its internals of the present invention are described in more detail below by way of specific examples, it being understood that the examples are exemplary only and that the invention is not limited thereto.
Example 1
Referring to fig. 1, 2 and 5, this example uses the reactor internals provided by the present invention in a catalytic distillation reactor for the synthesis of methyl tert-butyl ether (MTBE). In this embodiment, each shaft 211 is provided with a wire mesh container, the arrangement of the reactor internals is shown in fig. 1 and 2, three layers of reactor internals are arranged in the reactor body 10, thirty-four catalyst string groups are arranged in each layer, a gap of about 10mm is left between adjacent catalyst string groups, a distribution plate 40 is arranged above the catalyst layer 20, and the arrangement of the reactor internals in the adjacent upper and lower layers is the same. The screen container 212 is a cylindrical screen container with a diameter of 50mm, and the screen container 212 is mounted on the shaft 211 through a bearing 214 and is fixed in the axial direction and rotated in the circumferential direction. The mesh container 212 was filled with a mixture of catalyst and inert filler, and the filling rate of the filler 213 was 70%. The catalyst is D005-II sulfonic acid resin with the particle size of about 0.8 +/-0.4 mm and the specific surface area of 70m 2 ·g -1 The aperture is 25 to 50nm, the inert filler is a triangular spiral stainless steel wire mesh filler, and the volume ratio of the catalyst to the inert filler is about 3. Methanol was heated to 70 ℃ and fed into the catalytic distillation reactor from the upper portion of the reactor body at a flow rate of 300kg/h, while a mixture of normal butenes and isobutene containing 50wt% of isobutene was fed into the catalytic distillation reactor from the lower portion of the reactor body at 650 kg/h. The operating pressure was set at 0.4MPag, a C4 olefin mixture could be produced at the top of the catalytic distillation reactor, a mixture of MTBE and methanol was produced at the bottom of the catalytic distillation reactor, the isobutene conversion was 86%, and flooding did not occur.
Example 2
Referring to fig. 1, 2 and 5, this example uses the reactor internals provided by the present invention in a catalytic distillation reactor for the synthesis of methyl tert-butyl ether (MTBE). In this embodiment, each shaft 211 is provided with a wire mesh container, the arrangement of the reactor internals is shown in fig. 1 and fig. 2, three layers of reactor internals are disposed in the reactor body 10, thirty-four catalyst string groups are arranged in each layer, a gap of about 10mm is left between adjacent catalyst string groups, a distribution plate 40 is disposed above the catalyst layer 20, and the arrangement of the reactor internals in the adjacent upper and lower layers is the same. The silk screen container 212 is a cylindrical silk screen container with a diameter of 60mm, and the silk screen container 212 is mounted on the shaft 211 through a bearing 214 and is fixed along the axial direction and rotates along the circumferential direction. The wire container 212 was filled with a mixture of catalyst and inert filler, and the filling rate of the filler 213 was 75%. The catalyst is NKC-9 sulfonic acid resin with the particle size of about 0.8 +/-0.4 mm and the specific surface area of 76m 2 ·g -1 The aperture is 25 to 50nm, the inert filler is a triangular spiral stainless steel wire mesh filler, and the volume ratio of the catalyst to the inert filler is about 5. Methanol was heated to 60 ℃ in a stream of 400kg/hThe catalytic distillation reactor was fed at a high rate from the upper part of the reactor body, while a mixture of n-butene and isobutene containing 50wt% of isobutene was fed at a rate of 900kg/h from the lower part of the reactor body. The operating pressure was set at 0.6MPag, a C4 olefin mixture was produced at the top of the catalytic distillation reactor and a mixture of MTBE and methanol was produced at the bottom of the catalytic distillation reactor, with an isobutene conversion of 90% and no flooding.
The foregoing descriptions of specific exemplary embodiments of the present invention have been presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain certain principles of the invention and its practical application to enable one skilled in the art to make and use various exemplary embodiments of the invention and various alternatives and modifications. Any simple modifications, equivalent changes and modifications made to the above exemplary embodiments shall fall within the scope of the present invention.

Claims (17)

1. A reactor internals, comprising:
a catalyst layer formed by arranging a plurality of catalyst strings, each of the catalyst strings including:
a shaft rod arranged in a horizontal direction;
one or more wire mesh containers removably threaded onto the shaft, the wire mesh containers being rotatable about the shaft; and
a filler filled in the wire mesh container, the filler including a catalyst; and
a support assembly for mounting the catalyst layer within a reactor.
2. The reactor internals according to claim 1, wherein the wire mesh vessel is a rotationally symmetric structure.
3. The reactor internals according to claim 2, wherein the cross-section of the wire mesh container perpendicular to the shaft is circular, regular polygonal, star-shaped, flower-shaped or cam-shaped.
4. The reactor internals according to claim 1, wherein the packing ratio of the packing in the wire mesh container is between 20% and 80%.
5. The reactor internals according to claim 1, wherein the wire mesh container has an equivalent diameter of 10mm to 100mm.
6. The reactor internals according to claim 1, wherein the wire mesh container is mounted on the shaft by means of bearings having a coefficient of dynamic friction less than or equal to 0.2.
7. The reactor internals according to claim 1, wherein the catalyst is a solid catalyst or a porous catalyst; the particle size of the catalyst is phi 1-phi 15mm.
8. The reactor internals according to claim 1, wherein the packing further comprises an inert packing.
9. The reactor internals according to claim 1, wherein the wire mesh container is made of wire or non-wire.
10. The reactor internals according to claim 1, wherein the mesh size of the wire mesh container is smaller than the size of the packing.
11. A reactor internals according to claim 1, wherein the rack assembly comprises:
a mesh plate disposed under the catalyst layer; and
a support plate supporting the shaft on the mesh plate.
12. The reactor internals according to claim 1, further comprising:
the distribution plate is arranged above the catalyst layer and provided with a plurality of first diameter-variable pore channels and a plurality of second diameter-variable pore channels, the diameters of the first diameter-variable pore channels are gradually reduced from bottom to top, and the diameters of the second diameter-variable pore channels are gradually increased from bottom to top.
13. The reactor internals according to claim 12, wherein the diameters of the small ends of the first variable diameter channel and the second variable diameter channel are phi 1mm to phi 25mm, the included angle of the first variable diameter channel is 20 to 70 degrees, and the included angle of the second variable diameter channel is 20 to 70 degrees.
14. A catalytic distillation reactor, comprising:
the reactor body is provided with a liquid inlet at the upper part and a gas inlet at the lower part; and
at least one reactor internals as claimed in any one of claims 1 to 13, mounted in the reactor body.
15. The catalytic distillation reactor according to claim 14, wherein when the reactor internals are plural, the plural reactor internals are integrally installed in the reactor body or installed in the reactor body layer by layer.
16. The catalytic distillation reactor according to claim 14, wherein when the reactor internals are plural, the wire mesh containers of two adjacent layers of the reactor internals are staggered.
17. The catalytic distillation reactor of claim 14 wherein liquid and gas phase reactants enter the wire mesh container in countercurrent flow from both sides of the shaft, thereby driving the wire mesh container to oscillate or rotate about the shaft.
CN202011603476.6A 2020-12-30 2020-12-30 Catalytic distillation reactor and internals therefor Active CN114682172B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202011603476.6A CN114682172B (en) 2020-12-30 2020-12-30 Catalytic distillation reactor and internals therefor

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202011603476.6A CN114682172B (en) 2020-12-30 2020-12-30 Catalytic distillation reactor and internals therefor

Publications (2)

Publication Number Publication Date
CN114682172A CN114682172A (en) 2022-07-01
CN114682172B true CN114682172B (en) 2023-01-10

Family

ID=82132909

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202011603476.6A Active CN114682172B (en) 2020-12-30 2020-12-30 Catalytic distillation reactor and internals therefor

Country Status (1)

Country Link
CN (1) CN114682172B (en)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5189001A (en) * 1991-09-23 1993-02-23 Chemical Research & Licensing Company Catalytic distillation structure
CN101745245A (en) * 2010-02-05 2010-06-23 北京化工大学 Multi-level countercurrent rotating bed reaction and rectification device and application thereof
CN101827664A (en) * 2007-10-19 2010-09-08 草津电机株式会社 Catalyst circulating waste plastic/organic matter decomposition apparatus and decomposition system
CN104353255A (en) * 2014-11-07 2015-02-18 安徽泰合森能源科技有限责任公司 Filling device of catalytic distillation catalyst
CN108993325A (en) * 2018-08-28 2018-12-14 福州大学 A kind of rotary-catalytic bed and its application method

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9943819B2 (en) * 2014-11-03 2018-04-17 Singh Instrument LLC Small-scale reactor having improved mixing

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5189001A (en) * 1991-09-23 1993-02-23 Chemical Research & Licensing Company Catalytic distillation structure
CN101827664A (en) * 2007-10-19 2010-09-08 草津电机株式会社 Catalyst circulating waste plastic/organic matter decomposition apparatus and decomposition system
CN101745245A (en) * 2010-02-05 2010-06-23 北京化工大学 Multi-level countercurrent rotating bed reaction and rectification device and application thereof
CN104353255A (en) * 2014-11-07 2015-02-18 安徽泰合森能源科技有限责任公司 Filling device of catalytic distillation catalyst
CN108993325A (en) * 2018-08-28 2018-12-14 福州大学 A kind of rotary-catalytic bed and its application method

Also Published As

Publication number Publication date
CN114682172A (en) 2022-07-01

Similar Documents

Publication Publication Date Title
US20060251547A1 (en) Family of stationary film generators and film support structures for vertical staged polymerization reactors
US6824749B2 (en) Stacked monolith reactor and process
US20150328612A1 (en) Multi-tube radial bed reactor
CN100551478C (en) Catalyze rectification packing tower
US20160001245A1 (en) Apparatuses for distributing fluids in fluidized bed reactors
CN104368301A (en) Hyper-gravity reactor and reaction method
CN109985570B (en) Hydrogenation reactor with impact reduction element
JPH08332374A (en) High performance tray assembly of multiple down comer
WO2014070324A2 (en) Vortex-type mixing device for a down-flow hydroprocessing reactor
KR20150067330A (en) Multiple-bed downflow reactor comprising a mixing device, use of said reactor, as well as mixing method
US11896970B2 (en) Gas and liquid distributor for bubble column reactor
CN114682172B (en) Catalytic distillation reactor and internals therefor
KR102553411B1 (en) Fixed bed or moving bed reactors with a radial flow of process stream to be treated, comprising improved internals
AU2015413163A1 (en) Column for heat and/or mass exchange between two fluids comprising a collection tray and gas mixing means
CN102675495A (en) Olefinic polymerization reactor and polymerization method
CN1274381C (en) Catalyst distillation component and catalyst distillation method used said component
US20160256812A1 (en) Collector assembly for a gaseous fluid for a radial reactor
US4493735A (en) Device and method for forming a fluidized bed
CN211754821U (en) Self-heating type fixed bed reactor and system
CN216419330U (en) Novel falling film reactor
CN112705114B (en) Heat exchange type multiphase reactor, application method thereof and light gasoline etherification method
CN114432971B (en) Catalytic reactor and distillation tower using same
CN114452900B (en) Catalytic reaction unit and reactive distillation tower
CN212369587U (en) Catalytic distillation tower with modular catalyst filling modification
US10974163B2 (en) Structured packing for catalytic distillation

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant
TR01 Transfer of patent right
TR01 Transfer of patent right

Effective date of registration: 20231117

Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen

Patentee after: CHINA PETROLEUM & CHEMICAL Corp.

Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd.

Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen

Patentee before: CHINA PETROLEUM & CHEMICAL Corp.

Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp.