CN216367904U - Gas-solid two-phase fluidized bed reaction device - Google Patents
Gas-solid two-phase fluidized bed reaction device Download PDFInfo
- Publication number
- CN216367904U CN216367904U CN202122536111.2U CN202122536111U CN216367904U CN 216367904 U CN216367904 U CN 216367904U CN 202122536111 U CN202122536111 U CN 202122536111U CN 216367904 U CN216367904 U CN 216367904U
- Authority
- CN
- China
- Prior art keywords
- reactor
- gas
- distribution ring
- solid
- pipe
- 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.)
- Expired - Fee Related
Links
- 239000007787 solid Substances 0.000 title claims abstract description 44
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 38
- 238000009826 distribution Methods 0.000 claims abstract description 144
- 239000003054 catalyst Substances 0.000 claims abstract description 63
- 239000007795 chemical reaction product Substances 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 8
- 230000007423 decrease Effects 0.000 claims description 2
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 claims description 2
- 238000004939 coking Methods 0.000 abstract description 12
- 238000003786 synthesis reaction Methods 0.000 abstract description 3
- 239000012071 phase Substances 0.000 description 21
- 239000007789 gas Substances 0.000 description 11
- 239000002994 raw material Substances 0.000 description 11
- 238000005299 abrasion Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 5
- 238000004064 recycling Methods 0.000 description 5
- 239000000376 reactant Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 230000001737 promoting effect Effects 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- 230000016507 interphase Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 150000002894 organic compounds Chemical class 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000008247 solid mixture Substances 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model provides a gas-solid two-phase fluidized bed reaction device, belonging to the field of organic synthesis. Comprises a reactor consisting of a first reactor and a second reactor, at least two feeding nozzles, a pre-lifting distribution ring and a catalyst feeding pipe; the second reactor is coaxially communicated with the first reactor and is connected with the first reactor through a reducing nozzle, the opening of the feeding nozzle is downwards arranged on the wall of the first reactor and forms a certain included angle with the axial direction of the first reactor, and the pre-lifting distribution ring is arranged at the bottom of the first reactor and is of a spiral structure; the catalyst feed pipe is arranged on the wall of the first reactor and is positioned between the pre-lifting distribution ring and the feed nozzle. The axial distance between the pre-lifting distribution ring and the feeding nozzle is 1 meter, and the pre-lifting distribution ring is used for avoiding the inner part of the gas distribution ring from coking. The utility model can effectively improve the radial distribution of the main air and avoid gas distribution ring coking caused by secondary air back mixing, thereby improving the gas and solid contact efficiency of the feeding section of the reactor and prolonging the operation period of the reactor.
Description
Technical Field
The utility model relates to production equipment of organic compounds containing carbon and hydrogen, in particular to a gas-solid two-phase fluidized bed reaction device, belonging to the field of organic synthesis.
Background
In the field of organic compound synthesis, the feedstock is often fed in gaseous form and different compounds are synthesized under the catalytic action of a solid particulate catalyst. Such processes are carried out in a fluidized bed reactor, the gas phase feed being generally introduced by a gas distribution device located at the bottom of the reactor. In order to optimize the distribution of reaction products, a secondary air is introduced into the downstream of the reaction device in a secondary feeding mode in part of the reaction. Due to the existence of secondary air, when the air quantity of the secondary air is high, the secondary air can cause abrasion to the pre-lifting distribution ring in a jet flow mode. On the other hand, for raw materials with unstable chemical properties, the back mixing of secondary air can cause the raw materials to generate side reactions in the pre-lifting distribution ring area to cause coking, and the yield of reaction products is reduced. Meanwhile, the existence of secondary air complicates the flow in the feeding area, and the mixing of gas and solid phases is not uniform.
For solving the problems caused by secondary air feeding of the existing gas-solid two-phase fluidized bed reaction device, a form of optimizing a secondary air feeding structure is generally adopted, for example, Chinese patent CN201940218U (application No. 201020623000.4) discloses a feeding mixing section structure of a catalytic cracking riser reactor, a guide plate inner member is arranged at the downstream of secondary air, the inner member promotes the gas-solid two-phase flow of the mixing section to be rapidly changed into a ring-nucleus structure, the back mixing of a catalyst is reduced, the mixing of the gas-solid two phases is improved, the product distribution is optimized, but the patent does not solve the problem that the secondary air influences a large area. Chinese patent publication CN 104774641 a (application No. 201410014516.1) discloses a riser feeding mixed structure, this structure adopts the feeding nozzle that sets up downwards for the overgrate air contacts with promoting the incoming flow in advance with the form of adverse current, overgrate air feeding influence area has been reduced, and the contact efficiency of gas-solid phase has been improved to the adverse current contact, and then the final yield of reactor has been improved, however this patent technique does not solve probably to promoting the distribution ring in advance when overgrate air proportion is great and causes wearing and tearing, lead to promoting the problem such as distribution ring peripheral region coking in advance even. Chinese patent publication CN 108543501 a (application No. 201810455805.3) discloses a gas-solid fluidized bed reactor, which reduces the temperature of the secondary air feed by arranging a cooling jacket outside the secondary air feed nozzle, thereby solving the problem of coking of the secondary air feed in the mixing area, however, the technology does not mention the situation of coking and abrasion caused by the secondary air in the pre-lifting distribution ring.
The patent technologies improve the current situation that the gas-solid contact efficiency of a mixing section is low by optimizing a secondary air feeding structure, but do not solve the problems of abrasion and possible coking caused by the secondary air to a pre-lifting distribution ring. On the other hand, the pre-lifting distributor has great influence on the gas-solid contact efficiency of the mixing section, and the factor is not considered in the design of the mixing structure in the prior patent technology.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems of abrasion and coking possibly existing in the pre-lifting distribution ring under the influence of secondary air feeding jet flow, the utility model provides a gas-solid two-phase fluidized bed reaction device which can avoid abrasion and coking caused by secondary air jet flow to the pre-lifting distribution ring and promote the contact efficiency of gas and solid in a mixing section by optimizing the pre-lifting distribution ring structure.
In order to realize the aim, the utility model provides a gas-solid two-phase fluidized bed reaction device, which comprises a reactor, at least two feeding nozzles, a pre-lifting distribution ring and a catalyst feeding pipe, wherein the reactor consists of a first reactor and a second reactor; the second reactor is positioned above the first reactor and is coaxially communicated with the first reactor, the second reactor and the first reactor are connected through reducing, the feeding nozzle is arranged on the wall of the first reactor and forms a certain included angle with the axial direction of the first reactor, the opening of the feeding nozzle is downward and is communicated with the interior of the first reactor, and the pre-lifting distribution ring is arranged at the bottom of the first reactor and is of a spiral structure; the catalyst feeding pipe is arranged on the wall of the first reactor and is positioned between the pre-lifting distribution ring and the feeding nozzle;
promote the distribution ring in advance including spiral distribution pipe, air-out nozzle, distribution ring backup pad and promote the distribution ring intake pipe in advance, wherein, spiral distribution pipe links to each other through the wall of distribution ring backup pad with first reactor, and air-out nozzle evenly arranges on spiral distribution pipe and communicates with each other with spiral distribution pipe, promotes the distribution ring intake pipe in advance and communicates with each other with spiral distribution pipe.
In one embodiment of the utility model, the feed nozzle is used to provide secondary air so that the secondary feed enters the reactor in the form of a jet.
In one embodiment of the utility model, there are optionally a plurality of feed nozzles, preferably a plurality of feed nozzles arranged centrally symmetrically with respect to the axis of the first reactor on the wall of the first reactor.
In one embodiment of the utility model, the pre-lift distribution ring is arranged at the bottom of the first reactor, the pre-lift distribution ring introduces reactants (or auxiliary gas) into the reactor in the form of a plurality of jets through the openings (air outlet nozzles), and the distribution ring feed can be reactants or auxiliary fluidizing air.
In one embodiment of the utility model, the outlet of the air outlet nozzle faces downwards and forms an included angle of 5-15 degrees with the axial center line of the first reactor, the air outlet nozzle is provided with a circular cavity and is communicated with the cavity of the spiral distribution pipe, and the gas-phase feed is introduced by the spiral distribution pipe, flows through the cavity of the spiral distribution pipe and flows out from the air outlet nozzle. The spiral distribution pipe is used for buffering gas phase feeding, and the air outlet nozzle is used for evenly distributing the gas phase feeding in the mixing section.
In one embodiment of the present invention, the distribution ring support plate is directly connected to the spiral distribution pipe, two ends of the distribution ring distribution plate are in a trapezoidal structure, a central area of the distribution ring distribution plate is in a rectangular structure, and a 90 ° included angle is formed between the distribution ring support plate and the distribution ring support plate to fix the pre-lifting distribution ring.
In one embodiment of the utility model, the pre-lifting distribution ring gas inlet pipe is directly connected with the spiral distribution pipe, forms an included angle of 90 degrees along the axial direction of the first reactor, is internally provided with a cylindrical cavity, and is connected with the gas inlet end of the cylindrical cavity and the flange.
In an embodiment of the present invention, the cross-sectional area of the circular cavity of the air outlet nozzle is optionally gradually reduced from one end close to the spiral distribution pipe to one end close to the bottom of the reactor, so as to reduce the pressure drop and reduce the proportion of the dead zone on the distribution ring.
In an embodiment of the present invention, it is optional that the cross-sectional areas of the inlet and the outlet of the spiral distribution pipe gradually decrease from the inlet to one end of the outlet, and through the change of the flow velocity, it is ensured that the gas can have different pressures at different radial positions of the distribution pipe, so that the jet flow ejected from the air outlet nozzle has the same gas velocity.
In an embodiment of the present invention, a pitch of the spiral distribution pipe may be selected, and the pitch gradually increases from the center of the first reactor to the sidewall of the reactor, so as to ensure that the density of the air outlet nozzle matches with the corresponding air distribution area, and improve the radial air distribution uniformity.
In one embodiment of the utility model, the catalyst feed is provided to the first reactor wall for providing catalyst to the reactor.
In one embodiment of the utility model, the feed nozzle is optionally at a distance of 1 m or more from the pre-lift distribution ring.
In one embodiment of the present invention, the reducing is adjusted according to the characteristics of the reaction process, and when the reaction process is a volume reduction reaction, the reducing has the characteristics of small mouth and large inlet, and when the reaction process is a volume expansion reaction, the reducing has the characteristics of large outlet and small inlet.
In one embodiment of the present invention, a catalyst discharge pipe is disposed on a side wall of the first reactor, the catalyst discharge pipe is connected to a feed port of an external catalyst regenerator, and a catalyst feed pipe is connected to a discharge port of the catalyst regenerator.
In one embodiment of the utility model, the second reactor comprises a cyclone separator, and the cyclone separator is arranged at the top of the second reactor and is used for gas-solid separation of reaction products.
In one embodiment of the present invention, the second reactor further comprises a catalyst recycling line, the catalyst recycling line is located at the middle lower part of the second reactor and is connected with the catalyst feeding pipe of the first reactor, and when the catalyst concentration of the first reactor is low, a part of the spent catalyst extracted from the second reactor can be directly conveyed to the first reactor through the catalyst recycling line.
The operation principle of the gas-solid two-phase fluidized bed reaction device provided by the utility model is as follows: the device comprises a first reactor, a second reactor, at least two feeding nozzles, a pre-lifting distribution ring and a catalyst feeding pipe, the secondary air (feed) is provided downwards through a feed nozzle arranged on the wall of the reactor, a pre-lifting distribution ring is arranged at the bottom of the reactor for providing main air, the gas-solid contact efficiency of the mixing section is enhanced through the countercurrent contact of the secondary air and the main air, the direct influence of the secondary air on the pre-lifting distribution ring belt is avoided through adjusting the distance between the feeding nozzle and the pre-lifting distribution ring, the abrasion of the pre-lifting distribution ring is reduced, the possible coking problem of unstable raw materials in the distribution ring area is avoided, through will promote the distribution ring in advance and design into helical structure to evenly arrange a plurality of air-out nozzles on the main air pipe, improve the homogeneity that promotes the incoming flow in advance, and then improve the overgrate air and promote the contact efficiency who comes the flow in advance. Therefore, the utility model can ensure that the secondary air and the main air are fully mixed to complete the reaction on the basis of preventing the pre-lifting distribution ring from being worn or coked.
The utility model has the beneficial effects that:
the gas-solid fluidized bed reaction device comprises a reactor, at least two feeding nozzles, a catalyst feeding pipe and a pre-lifting distribution ring which are vertically arranged, wherein the spiral pre-lifting distribution ring is adopted to ensure that pre-lifting raw materials are uniformly distributed in a feeding section, so that non-target products such as coking and the like caused by over-reaction or insufficient reaction in a corresponding area are avoided; the feeding nozzle is arranged on the wall of the reactor, so that the second reactant is obliquely downward and is in countercurrent contact with the pre-lifting incoming flow, the interphase contact efficiency is improved, and the interphase mass transfer resistance is reduced; by adjusting the distance between the feeding nozzle and the pre-lifting distribution ring to be more than or equal to 1 m, possible impact abrasion of the jet flow of the feeding nozzle on the pre-lifting distribution ring is avoided, and coking side reaction caused by the fact that a second reactant is gathered in the area near the pre-lifting distribution ring is avoided; through the special feeding section structure of the novel gas-solid two-phase fluidized bed reactor, the selectivity of reaction products can be effectively improved, and the operation period of the device is prolonged.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a gas-solid two-phase fluidized bed reactor according to a first embodiment of the present invention;
fig. 2 is a schematic structural diagram of a pre-lifting distribution ring in a gas-solid two-phase fluidized bed reaction device according to a first embodiment of the present invention;
fig. 3 is a schematic structural view of a pre-lifting distribution ring main air pipe, a part of nozzles and a connecting rib plate in the gas-solid two-phase fluidized bed reaction device provided in the first embodiment of the present invention;
FIG. 4 is a schematic structural diagram of a gas-solid two-phase fluidized bed reactor according to a second embodiment of the present invention;
FIG. 5 is a schematic structural diagram of a gas-solid two-phase fluidized bed reactor provided in the third embodiment of the present invention;
FIG. 6 is a schematic structural diagram of a gas-solid two-phase fluidized bed reactor according to a fourth embodiment of the present invention;
the system comprises a first reactor, a second reactor, a feeding nozzle, a pre-lifting distribution ring, a spiral distribution pipe, an air outlet nozzle, a distribution ring support plate, a distribution ring air inlet pipe, a catalyst feeding pipe, a cyclone separator and a catalyst circulation pipeline, wherein the first reactor is 1, the second reactor is 2, the feeding nozzle is 3, the pre-lifting distribution ring is 4, the spiral distribution pipe is 4A, the air outlet nozzle is 4B, the distribution ring support plate is 4C, the distribution ring support plate is 4D, the distribution ring air inlet pipe is 4E, the catalyst feeding pipe is 5, and the cyclone separator is 6, and the catalyst circulation pipeline is 7.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer, the technical solutions in the embodiments of the present invention will be described in more detail below with reference to the accompanying drawings in the preferred embodiments of the present invention. In the drawings, the same or similar reference numerals denote the same or similar components or components having the same or similar functions throughout. The described embodiments are only some, but not all embodiments of the utility model. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the utility model and are not to be construed as limiting the utility model. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Embodiments of the present invention will be described in detail below with reference to the accompanying drawings. In the description of the present invention, it should be noted that unless otherwise specifically stated or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning a fixed connection, an indirect connection through intervening media, a connection between two elements, or an interaction between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Example one
When main raw materials for reaction are fed in a main air mode, the embodiment provides a gas-solid two-phase fluidized bed reaction device, as shown in fig. 1 to 3, the device comprises a reactor consisting of a first reactor 1 and a second reactor 2, a feeding nozzle 3, a pre-lifting distribution ring 4 and a catalyst feeding pipe 5, wherein the second reactor 2 is located above the first reactor 1 and connected and communicated through reducing, and the diameter of the second reactor 2 is 1.25 times that of the first reactor 1 and the two are coaxially arranged. The first reactor 1 is provided with a feeding nozzle 3, a catalyst feeding pipe 5 and a pre-lifting distribution ring 4, and the second reactor 2 is internally provided with a cyclone separator 6. The feed nozzles 3 are located on the wall of the first reactor 1, the outlet direction of the feed nozzles faces downwards to form an included angle of 30 degrees with the central line of the first reactor 1, the feed nozzles are arranged downwards, the two feed nozzles 3 are symmetrically arranged along the radial direction of the first reactor 1, and the distance from the feed nozzles 3 to the pre-lifting distribution ring 4 is 1 meter. A catalyst feed 5 is provided below the feed nozzle 3 on the wall of the first reactor 1 for providing catalyst. The pre-lift distribution ring 4 is arranged at the bottom of the first reactor 1 and is used for providing pre-lift air. The cyclone separator 6 is arranged at the top of the second reactor 2 and used for gas-solid separation of reaction products.
The pre-lifting distribution ring 4 comprises a spiral distribution pipe 4A, an air outlet nozzle 4B, distribution ring support plates 4C and 4D and a distribution ring air inlet pipe 4E; the air outlet nozzles 4B are uniformly arranged on the distribution pipe 4A, the distribution pipe 4A is connected to the wall 1 of the reactor through distribution ring supporting plates 4C and 4D, and a pre-lifting distribution ring air inlet pipe 4E is communicated with the interior of the spiral distribution pipe 4A and forms an included angle of 90 degrees along the axial direction;
the distribution pipe 4A is of a spiral structure, the center of the spiral is connected with the air inlet 4E of the pre-lifting distribution pipe, and the outlet of the outermost ring of the spiral is closed; the air outlet nozzle 4B is communicated with the inside of the spiral distribution pipe 4A and forms an included angle of 10 degrees with the axial center line of the first reactor 1, the outlet of the air outlet nozzle 4B faces downwards, and the inside of the air outlet nozzle is a cylindrical cavity;
the supporting plates 4C and 4D are directly connected with the spiral distribution pipe 4A, two ends of the distribution plate are in a trapezoidal structure, the central area is in a rectangular structure, and an included angle of 90 degrees is formed between the supporting plate 4C and the supporting plate 4D; distribution pipe air inlet 4E and spiral distribution pipe 4A lug connection are 90 contained angles along first reactor axial, and its inside is cylindrical cavity, its inlet end and flange joint.
The operation principle of the gas-solid two-phase fluidized bed reaction device is as follows: main air (accounting for about 80% of the raw material proportion) sequentially enters the first reactor through a distribution pipe air inlet 4E, a spiral distribution pipe 4A and an air outlet nozzle 4B, and is mixed with a catalyst from a catalyst feeding pipe 5 to form a pre-lifted incoming flow, and the pre-lifted incoming flow is contacted with two raw materials introduced by a feeding nozzle 3 and reacts; the gas-solid mixture in the first reactor 1 enters the second reactor 2 along the axial direction and continues to react, the reaction product carries partial catalyst to enter the cyclone separator 6, and the gas-solid separation is realized under the action of the cyclone separator 6; the reaction product enters a subsequent separation system, and the catalyst is circulated into the bed layer of the second reactor 2.
Example two
When main raw materials for reaction are fed in a secondary air mode, the gas-solid two-phase fluidized bed reaction device is shown in figure 4, and comprises a reactor consisting of a first reactor 1 and a second reactor 2, a feeding nozzle 3, a pre-lifting distribution ring 4 and a catalyst feeding pipe 5, wherein the second reactor 2 is positioned above the first reactor 1, the first reactor 1 and the second reactor 2 are connected and communicated through reducing, and the diameter of the second reactor 2 is 1.5 times of that of the first reactor 1. The second reactor 2 is arranged coaxially with the first reactor 1. The first reactor 1 is provided with a feeding nozzle 3, a catalyst feeding pipe 5 and a pre-lifting distribution ring 4, and the second reactor 2 is internally provided with a cyclone separator 6. The feed nozzles 3 are located on the wall of the first reactor 1, the outlet direction of the nozzles is downward and forms an included angle of 30 degrees with the central line of the first reactor 1, the nozzles are arranged downward, the number of the feed nozzles 3 is four, the nozzles are uniformly arranged along the radial direction of the first reactor 1, and the distance from the feed nozzles 3 to the pre-lifting distribution ring 4 is 1 meter. A catalyst feed 5 is provided below the feed nozzle 3 on the wall of the first reactor 1 for providing catalyst. The pre-lift distribution ring 4 is arranged at the bottom of the first reactor 1 and is used for providing pre-lift air. The cyclone separator 6 is arranged at the top of the second reactor 2 and used for gas-solid separation of reaction products.
The pre-lifting distribution ring 4 comprises a spiral distribution pipe 4A, an air outlet nozzle 4B, distribution ring support plates 4C and 4D and a distribution ring air inlet pipe 4E; the air outlet nozzles 4B are uniformly arranged on the distribution pipe 4A, the distribution pipe 4A is connected to the wall 1 of the reactor through distribution ring supporting plates 4C and 4D, and a pre-lifting distribution ring air inlet pipe 4E is communicated with the interior of the spiral distribution pipe 4A and forms an included angle of 90 degrees along the axial direction;
the distribution pipe 4A is of a spiral structure, the center of the spiral is connected with the air inlet 4E of the pre-lifting distribution pipe, and the outlet of the outermost ring of the spiral is closed; the air outlet nozzle 4B is communicated with the inside of the spiral distribution pipe 4A and forms an included angle of 10 degrees with the axial center line of the first reactor 1, the outlet of the air outlet nozzle 4B faces downwards, and the inside of the air outlet nozzle is a cylindrical cavity;
the supporting plates 4C and 4D are directly connected with the spiral distribution pipe 4A, two ends of the distribution plate are in a trapezoidal structure, the central area is in a rectangular structure, and an included angle of 90 degrees is formed between the supporting plate 4C and the supporting plate 4D; distribution pipe air inlet 4E and spiral distribution pipe 4A lug connection are 90 contained angles along first reactor axial, and its inside is cylindrical cavity, its inlet end and flange joint.
When the main raw materials for reaction are fed in the form of secondary air, the operation principle of the device is as follows: pre-lift air (accounting for about 20% of the total raw material proportion) sequentially enters the first reactor through a distribution pipe air inlet 4E, a spiral distribution pipe 4A and an air outlet nozzle 4B, is mixed with the catalyst from a catalyst feeding pipe 5 to form pre-lift incoming flow, and the pre-lift incoming flow is contacted with four strands of raw materials introduced by a feeding nozzle 3 and reacts; the gas-solid mixture in the first reactor 1 enters the second reactor 2 along the axial direction and continues to react, the reaction product carries partial catalyst to enter the cyclone separator 6, and the gas-solid separation is realized under the action of the cyclone separator 6; the reaction product enters a subsequent separation system, and the catalyst is circulated into the bed layer of the second reactor 2.
EXAMPLE III
When the catalyst concentration in the first reactor 1 is low, a catalyst circulation line 7 is added, and the catalyst circulation line 7 is located at the middle-lower part of the second reactor 2 and connected to the catalyst feeding pipe of the first reactor, and the rest of the apparatus is the same as that of the second embodiment, as shown in FIG. 5.
During the reaction, part of the spent catalyst is withdrawn from the bottom of the second reactor 2 and is directly transferred to the first reactor 1 through the catalyst recycling line 7.
Example four
When the catalyst concentration in the first reactor 1 is low, a catalyst circulation line 7 is added, and the catalyst circulation line 7 is located at the middle lower part of the second reactor 2 and is connected with the catalyst feeding pipe of the first reactor, so that the rest of the devices and the embodiments are consistent, as shown in fig. 6.
During the reaction, part of the spent catalyst is withdrawn from the bottom of the second reactor 2 and is directly transferred to the first reactor 1 through the catalyst recycling line 7.
Although the present invention has been described with reference to the preferred embodiments, it should be understood that various changes and modifications can be made therein by those skilled in the art without departing from the spirit and scope of the utility model as defined in the appended claims.
Claims (10)
1. A gas-solid two-phase fluidized bed reaction device is characterized by comprising a reactor consisting of a first reactor (1) and a second reactor (2), at least two feeding nozzles (3), a pre-lifting distribution ring (4) and a catalyst feeding pipe (5); the second reactor (2) is positioned above the first reactor (1) and is coaxially communicated with the first reactor (1) and connected with the first reactor (1) through reducing, the feeding nozzle (3) is arranged on the wall of the first reactor (1) and forms a certain included angle with the axial direction of the first reactor (1), the opening of the feeding nozzle (3) is downward and is communicated with the interior of the first reactor (1), and the pre-lifting distribution ring (4) is arranged at the bottom of the first reactor (1) and is of a spiral structure; the catalyst feeding pipe (5) is arranged on the wall of the first reactor (1) and is positioned between the pre-lifting distribution ring (4) and the feeding nozzle (3);
promote the distribution ring in advance including spiral distribution pipe (4A), air outlet nozzle (4B), distribution ring backup pad and promote distribution ring intake pipe (4E) in advance, wherein, spiral distribution pipe (4A) link to each other through the wall of distribution ring backup pad with first reactor (1), air outlet nozzle (4B) evenly arrange on spiral distribution pipe (4A) and communicate with each other with spiral distribution pipe (4A), promote distribution ring intake pipe (4E) in advance and communicate with each other with spiral distribution pipe (4A).
2. A gas-solid two-phase fluidized bed reactor according to claim 1, wherein said feed nozzle (3) is adapted to supply secondary air to make the secondary feed enter the reactor in the form of jet; a plurality of feed nozzles (3) are arranged on the wall of the first reactor (1) in a manner that they are centrosymmetric with respect to the axis of the first reactor (1).
3. The gas-solid two-phase fluidized bed reaction device according to claim 1, wherein the outlet of the air outlet nozzle (4B) is downward and forms an included angle of 5-15 degrees with the axial center line of the first reactor (1), and the air outlet nozzle (4B) has a circular cavity and is communicated with the cavity of the spiral distribution pipe (4A).
4. A gas-solid two-phase fluidized bed reactor as claimed in any one of claims 1 to 3, wherein the cross-sectional area of the circular cavity of the outlet nozzle (4B) gradually decreases from the end near the spiral distribution pipe (4A) to the end near the bottom of the reactor.
5. A gas-solid two-phase fluidized bed reactor according to claim 4, wherein the cross-sectional areas of the inlet and outlet of the spiral distribution pipe (4A) are gradually reduced from the inlet to the outlet.
6. A gas-solid two-phase fluidized bed reactor according to claim 5, wherein the distance between the feeding nozzle (3) and the pre-lifting distribution ring (4) is 1 m or more.
7. The gas-solid two-phase fluidized bed reaction device according to claim 6, wherein the variable diameter is adjusted according to the characteristics of the reaction process, and the variable diameter is characterized by small mouth and large inlet when the reaction process is a volume reduction reaction, and the variable diameter is characterized by large outlet and small inlet when the reaction process is a volume expansion reaction.
8. The gas-solid two-phase fluidized bed reaction device according to claim 7, wherein a catalyst discharge pipe is arranged on the side wall of the first reactor, the catalyst discharge pipe is connected with a feed port of an external catalyst regenerator, and a catalyst feed pipe is connected with a discharge port of the catalyst regenerator.
9. A gas-solid two-phase fluidized bed reactor according to claim 8, wherein the second reactor (2) comprises a cyclone separator (6), and the cyclone separator (6) is arranged on the top of the second reactor (2) for gas-solid separation of reaction products.
10. A gas-solid two-phase fluidized bed reactor according to claim 9, wherein the second reactor (2) further comprises a catalyst circulation line (7), and the catalyst circulation line (7) is located at the middle lower part of the second reactor (2) and is connected with the catalyst feed pipe (5) of the first reactor (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122536111.2U CN216367904U (en) | 2021-10-21 | 2021-10-21 | Gas-solid two-phase fluidized bed reaction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122536111.2U CN216367904U (en) | 2021-10-21 | 2021-10-21 | Gas-solid two-phase fluidized bed reaction device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216367904U true CN216367904U (en) | 2022-04-26 |
Family
ID=81246210
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122536111.2U Expired - Fee Related CN216367904U (en) | 2021-10-21 | 2021-10-21 | Gas-solid two-phase fluidized bed reaction device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216367904U (en) |
-
2021
- 2021-10-21 CN CN202122536111.2U patent/CN216367904U/en not_active Expired - Fee Related
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101376092B (en) | Novel bubbling bed reactor | |
| CN1321731C (en) | Reactor of organic silicon fluidized bed with cyclone separator | |
| CN108753356B (en) | Multistage countercurrent catalytic cracking/cracking system and method | |
| CN111054271B (en) | Low-agent-consumption reaction device and reaction method for preparing aniline by nitrobenzene hydrogenation | |
| CN110691643A (en) | Catalyst and transport gas distributor for dehydrogenation reactors with fluidized bed | |
| TWI451909B (en) | Gas phase reaction method | |
| CN216367904U (en) | Gas-solid two-phase fluidized bed reaction device | |
| CN101597071A (en) | The method that on particle heat transferring agent, prepares prussic acid as the guiding of conveying fluidized bed circulation | |
| CN109897662B (en) | Novel fluidized bed coupling reactor and system | |
| CN111054277A (en) | Reactor and method for producing low-carbon olefin | |
| CN114456846A (en) | Chemical chain gasification reaction device and method thereof | |
| CN111054280B (en) | Reaction device and reaction method for preparing aniline by hydrogenation of multi-zone nitrobenzene | |
| CN115253934B (en) | Propane catalytic dehydrogenation fluidized bed reaction-regeneration coupling device and propane catalytic dehydrogenation process method | |
| CN116020350A (en) | Reactor for synthesizing carbonic ester, system and method for synthesizing carbonic ester | |
| CN112169710A (en) | Methyl acetate hydrogenation reactor and heat exchange system of multistage cold hydrogen feeding | |
| CN214051563U (en) | Methyl acetate hydrogenation reactor and heat exchange system of multistage cold hydrogen feeding | |
| CN113750911B (en) | Multichannel riser reaction device and application thereof | |
| CN108636303A (en) | A kind of recirculating fluidized bed prepares the consersion unit of pyridine base | |
| CN210481242U (en) | Olefin production apparatus | |
| CN210700021U (en) | Olefin production apparatus | |
| CN107224939B (en) | Axial reactor | |
| CN114425248B (en) | Catalytic converter mixer, device for producing low-carbon olefin and method and application for producing low-carbon olefin | |
| CN210700020U (en) | Olefin production apparatus | |
| WO2022268151A1 (en) | Fluidized bed reactor, and device and method for preparing low-carbon olefin | |
| CN111889037B (en) | Moving bed reactor and reaction method suitable for heat coupling or reaction coupling |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20220426 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |