CN221085574U - High-temperature pressurized fluidized bed reactor without dilute phase zone - Google Patents
High-temperature pressurized fluidized bed reactor without dilute phase zone Download PDFInfo
- Publication number
- CN221085574U CN221085574U CN202322899246.4U CN202322899246U CN221085574U CN 221085574 U CN221085574 U CN 221085574U CN 202322899246 U CN202322899246 U CN 202322899246U CN 221085574 U CN221085574 U CN 221085574U
- Authority
- CN
- China
- Prior art keywords
- nozzle
- distribution plate
- air inlet
- corrugated
- reactor
- 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
Links
- 238000009826 distribution Methods 0.000 claims abstract description 260
- 238000007667 floating Methods 0.000 claims abstract description 92
- 239000002131 composite material Substances 0.000 claims abstract description 52
- 239000011343 solid material Substances 0.000 claims abstract description 33
- 239000000463 material Substances 0.000 claims description 40
- 238000007789 sealing Methods 0.000 claims description 20
- 238000005266 casting Methods 0.000 claims description 16
- 239000000110 cooling liquid Substances 0.000 claims description 16
- 238000009434 installation Methods 0.000 claims description 12
- SAPGTCDSBGMXCD-UHFFFAOYSA-N (2-chlorophenyl)-(4-fluorophenyl)-pyrimidin-5-ylmethanol Chemical compound C=1N=CN=CC=1C(C=1C(=CC=CC=1)Cl)(O)C1=CC=C(F)C=C1 SAPGTCDSBGMXCD-UHFFFAOYSA-N 0.000 claims description 4
- 150000001875 compounds Chemical class 0.000 abstract description 10
- 239000007789 gas Substances 0.000 description 140
- 239000012071 phase Substances 0.000 description 69
- 238000006243 chemical reaction Methods 0.000 description 46
- 239000007787 solid Substances 0.000 description 34
- 239000002245 particle Substances 0.000 description 29
- 239000010410 layer Substances 0.000 description 23
- 239000010935 stainless steel Substances 0.000 description 20
- 229910001220 stainless steel Inorganic materials 0.000 description 20
- 238000000926 separation method Methods 0.000 description 19
- 239000003054 catalyst Substances 0.000 description 17
- 238000004519 manufacturing process Methods 0.000 description 16
- 238000004364 calculation method Methods 0.000 description 15
- 238000005984 hydrogenation reaction Methods 0.000 description 12
- 239000000843 powder Substances 0.000 description 11
- 229910000831 Steel Inorganic materials 0.000 description 9
- 239000010959 steel Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 8
- 239000007790 solid phase Substances 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- 238000009413 insulation Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- 239000012495 reaction gas Substances 0.000 description 6
- 239000012530 fluid Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 230000007704 transition Effects 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000003466 welding Methods 0.000 description 4
- 229910000990 Ni alloy Inorganic materials 0.000 description 3
- 238000005452 bending Methods 0.000 description 3
- 230000005465 channeling Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000033001 locomotion Effects 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910021420 polycrystalline silicon Inorganic materials 0.000 description 3
- 229920005591 polysilicon Polymers 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000009491 slugging Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- VXEGSRKPIUDPQT-UHFFFAOYSA-N 4-[4-(4-methoxyphenyl)piperazin-1-yl]aniline Chemical compound C1=CC(OC)=CC=C1N1CCN(C=2C=CC(N)=CC=2)CC1 VXEGSRKPIUDPQT-UHFFFAOYSA-N 0.000 description 2
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 208000012839 conversion disease Diseases 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 239000012809 cooling fluid Substances 0.000 description 2
- PMHQVHHXPFUNSP-UHFFFAOYSA-M copper(1+);methylsulfanylmethane;bromide Chemical compound Br[Cu].CSC PMHQVHHXPFUNSP-UHFFFAOYSA-M 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 description 2
- 239000005049 silicon tetrachloride Substances 0.000 description 2
- 239000011863 silicon-based powder Substances 0.000 description 2
- 239000002356 single layer Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- ZDHXKXAHOVTTAH-UHFFFAOYSA-N trichlorosilane Chemical compound Cl[SiH](Cl)Cl ZDHXKXAHOVTTAH-UHFFFAOYSA-N 0.000 description 2
- 239000005052 trichlorosilane Substances 0.000 description 2
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005315 distribution function Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000000265 homogenisation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005121 nitriding Methods 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- FDNAPBUWERUEDA-UHFFFAOYSA-N silicon tetrachloride Chemical class Cl[Si](Cl)(Cl)Cl FDNAPBUWERUEDA-UHFFFAOYSA-N 0.000 description 1
- 238000004544 sputter deposition Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model discloses a high-temperature pressurized fluidized bed reactor without a dilute phase zone, which comprises a detachable air inlet pipe, a reactor main body, a composite gas distribution plate, a floating nozzle, a solid material inlet, a first fold type redistribution plate and a second fold type redistribution plate; the detachable air inlet pipe is arranged on the air inlet of the reactor main body and is communicated with the reactor main body; the compound gas distribution plate is arranged at the lower part of the reactor main body, a plurality of floating nozzles and a plurality of float nozzles are arranged on the compound gas distribution plate, and the float nozzles are distributed at the outer sides of the floating nozzles; the solid material inlets are arranged at the lower part of the detachable air inlet pipe in pairs and are communicated with the reactor main body, and the solid material inlets are higher than the composite gas distribution plate; a plurality of first pleated redistribution plates and second pleated redistribution plates are disposed between the solid material inlet and the gas phase outlet at the top of the reactor body.
Description
Technical Field
The utility model relates to the technical field of chemical gas-solid two-phase reaction equipment, in particular to a high-temperature pressurized fluidized bed reactor without a dilute phase zone.
Background
The fluidized bed is a bed form in which fluid is utilized to pass through a granular solid bed, and when the resistance of the fluid flowing through the bed is greater than the weight of the bed particles, the solid particles are in a suspension motion state and can flow like the fluid. The corresponding reactor is a fluidized bed reactor, and particles in the fluidized bed reactor can flow freely as fluid, so that the fluidized bed reactor has the following main advantages: the bed layer has high-efficiency heat transfer performance, the temperature inside the bed layer is uniform and easy to control, and the method is particularly suitable for a strong heat release (heat absorption) reaction system; the continuous reaction and the regeneration circulation operation of solid powder materials or catalyst particles can be realized, and the catalyst is suitable for reactions with faster catalyst deactivation; the continuous input and output of the solid materials can be realized through a separation system. Based on the advantages, the fluidized bed reactor is rapidly developed in the fields of chemical engineering, petrochemical industry and coal chemical industry.
The gas-solid two-phase fluidized bed reactor has a plurality of structural types, but is generally composed of a gas distribution device, an internal member, a heat exchange device, a gas-solid separation device and the like no matter what the types are. The fluidized bed is divided into a dense phase zone (dense phase section), a transition zone and a dilute phase zone (separation section) along the height direction. The region below the bed interface of the fluidized bed is called dense phase region, and the region above the bed interface is called dilute phase region. Because some fluidized beds have higher fluidization gas velocity and larger diameter, bed interfaces are not obvious, so that the area between the dense-phase area and the dilute-phase area is often called a transition area, and the total height of the fluidized bed is the sum of the heights of the dense-phase area, the transition area and the dilute-phase area. The solid particles (powder materials or catalysts) in the fluidized bed have certain particle size distribution, and meanwhile, during the operation of the fluidized bed, some fine particles are generated due to collision and abrasion among the particles, so that the sedimentation speed of a part of fine particles in the particles of the fluidized bed is lower than the airflow speed, and the particles are carried out of the reactor by gas after passing through a dilute phase zone when being carried out of a dense phase zone. In addition, as the gas passes through the fluidised bed, the bubbles break up at the bed surface and throw some of the solid particles into the dilute phase zone, most of these particles settling at a rate greater than the gas flow rate, and so they fall back to the bed after reaching a certain height. Thus, the concentration of the solid particles in the region which is far away from the bed surface is smaller, and the concentration of the solid particles is basically unchanged after a certain distance from the bed surface. The minimum distance that the concentration of solid particles begins to remain unchanged is called the separation zone height (also called the TDH height). A freeboard zone must be present above the bed interface (or transition zone) of a conventional fluidized bed to allow particles having a settling velocity greater than the velocity of the gas stream to redeposit into the dense phase zone without being carried away by the gas stream. In order to reduce the TDH height of the fluidized bed, the upper part of many fluidized beds is also provided with an expansion section, i.e. the diameter of the dilute phase zone of the fluidized bed is larger than that of the dense phase zone.
Because the solids (or catalyst) concentration in the freeboard zone is still relatively high, if the solids (or catalyst) are not recovered by the gas-solids separation device, a large amount of solids will escape from the outlet of the fluidized bed reactor, which will not only result in a loss of useful unreacted solids but also contaminate the final product, so that the conventional fluidized bed reactor typically has a gas-solids separation device in the freeboard zone to trap the solids (or catalyst). For example, the high-efficiency cyclone separator and the high-temperature filter are the most common and practical, and the high-efficiency cyclone separator arranged in the dilute phase zone can also adopt a multi-stage multi-group mode to improve the solid particle separation efficiency in consideration of the use limitation of the high-temperature filter. In order to meet the requirements of a built-in cyclone separator on solid particle (powder material or catalyst) separation and circulating returning, the traditional fluidized bed reactor is designed with a dilute phase zone which occupies 1/2-2/3 of the total height of the reactor and occupies a considerable part of the investment of the reactor.
For example, chinese patent CN111054280B discloses a reaction device and a reaction method for preparing aniline by hydrogenation of multi-zone nitrobenzene, which adopts a plurality of groups of combined devices of two central reaction zones, two downlink zones and three circulation zones, and meanwhile, a sputtering separation member is arranged in a fluidized bed reactor, so that mass transfer and heat transfer in the reactor can be enhanced, deactivation of a catalyst can be effectively slowed down, consumption of the catalyst can be greatly reduced, and reaction efficiency can be improved. However, the reaction device of the utility model is internally provided with a plurality of cyclone separators, the designed dilute phase area occupies a large part of the total height of the reactor, and the dilute phase area adopts an expansion section mode, thus greatly increasing the investment of equipment.
As another example, chinese patent No. CN109894059B discloses a process for producing (meth) acrylonitrile, which comprises a fluidized bed reactor and a fluidized bed reactor having a heat exchanger connected to the fluidized bed reactor by a reaction gas outlet pipe, the process comprising: introducing a raw material gas into the fluidized bed reactor, and performing an ammoxidation reaction in the presence of a catalyst to obtain a reaction gas; and a step of introducing powder into a reaction gas outlet pipe, and discharging the reaction gas to the heat exchanger while cleaning the heat exchanger, wherein the reaction gas outlet pipe has a first portion extending from the upper portion of the fluidized bed reactor in the height direction of the fluidized bed reactor and reaching the highest point of the reaction gas outlet pipe, and a second portion connected to the highest point and extending to the heat exchanger, and the powder introduction position is a position in the second portion and is lower than the highest point. The reaction device of the utility model is also internally provided with a plurality of cyclone separators, and the designed dilute phase area occupies a large part of the total height of the reactor, thereby greatly increasing the investment of equipment.
Currently, along with the development of the production device towards large-scale and large-scale production, the diameter and the height of a single fluidized bed reactor device are larger and larger, and a plurality of reaction processes are simultaneously subjected to high-temperature and pressure working conditions, for example, the polysilicon process mostly adopts a hydrogenation technology, and the principle of the hydrogenation technology is as follows: raw materials such as hydrogen, silicon powder, silicon tetrachloride and the like produce trichlorosilane under the conditions of catalyst and high temperature (500-600 ℃) and pressure (2.5-4.0 MPa). The hydrogenation fluidized bed reactor is core equipment of the hydrogenation technology, and the fluidized bed reactor shell adopts high-nickel alloy steel (such as N08810 stainless steel) which is resistant to high temperature and hydrogen corrosion due to high temperature and high pressure hydrogen. As reactor units continue to be larger, the fluidized bed reactors also have increasingly larger diameters and thicknesses, and obviously, the manufacturing costs and processing difficulties will be higher and higher. At present, the fluidized bed reactors are all single-layer containers, namely, the container shell can bear the actions of high temperature, high pressure and hydrogen environment, so that the container shell is required to be made of thick-wall high-temperature-resistant high-nickel alloy steel plates, for the pressure-bearing containers, the larger the diameter of equipment is, the thicker the thickness of the plates is, the higher the cost and the manufacturing and processing difficulty of the plates are, the purchasing period is long, and the large-scale of the hydrogenated fluidized bed reactor is seriously affected. Therefore, the design scheme of the traditional fluidized bed reactor is difficult to meet the working condition of high temperature and pressure, and the high manufacturing cost can lead manufacturers to be unable to bear.
For example, chinese patent No. CN105502411B discloses a hydrogenation fluidized bed reactor and a polysilicon production system having the same, comprising a mixed gas inlet section, a reaction section and a gas-solid separation section connected in sequence, wherein the mixed gas inlet section forms a mixed gas cavity, an air inlet device and a gas distribution device are arranged in the mixed gas cavity, the gas distribution device is connected with the mixed gas inlet section, and the gas distribution device is close to the reaction section; a material feed port is formed in the wall of the reaction cylinder section; the wall of the gas-solid separation barrel section is provided with a generated gas outlet, a cyclone separator is arranged in the gas-solid separation barrel section, and the gas outlet of the cyclone separator is communicated with the generated gas outlet. The hydrogenation fluidized reactor can solve the problems of complex process and high recovery difficulty of hydrogenated silicon tetrachloride in the prior art. However, the reactor is a single-layer container, the container shell can bear high temperature, high pressure and hydrogen environment at the same time, the container shell is required to be made of thick-wall high-temperature-resistant high-nickel alloy steel plates, for the pressure-bearing container, the larger the diameter of the equipment is, the thicker the thickness of the plates is, the cost is high, the manufacturing and processing difficulty is high, the purchasing period is long, and the large-scale of the hydrogenation fluidized bed reactor is seriously affected.
Therefore, it is necessary to provide a high-temperature pressurized fluidized bed reactor without a dilute phase zone, which can solve the problems of high manufacturing cost and great difficulty of the fluidized bed reactor in the prior art.
Disclosure of utility model
The utility model aims to provide a high-temperature pressurized fluidized bed reactor without a dilute phase zone, which can solve the problems of high manufacturing cost and high difficulty of the fluidized bed reactor in the prior art.
The utility model is realized in the following way:
A high-temperature pressurized fluidized bed reactor without a dilute phase zone comprises a detachable air inlet pipe, a reactor main body, a composite gas distribution plate, a floating nozzle, a float nozzle, a solid material inlet and a second fold type redistribution plate; an air inlet is formed at the bottom of the reactor main body, and a detachable air inlet pipe is detachably arranged on the air inlet and communicated with the reactor main body; the compound gas distribution plate is arranged at the lower part of the reactor main body, a plurality of floating nozzles and a plurality of float nozzles are respectively arranged on the compound gas distribution plate at intervals, and the plurality of float nozzles are distributed at the outer sides of the plurality of floating nozzles; the solid material inlets are arranged at the lower part of the detachable air inlet pipe in pairs and are communicated with the reactor main body, and the solid material inlets are higher than the composite gas distribution plate; the second fold type redistribution plates are respectively arranged in the reactor body at intervals and are positioned between the solid material inlet and the gas phase outlet at the top of the reactor body.
The reactor main body comprises a lower seal head, a main shell, an upper seal head, a feed back port and a safety valve port; the lower end enclosure and the upper end enclosure are respectively connected to the bottom and the top of the main shell to form a closed shell structure of the reactor; the gas phase outlet, the feed back opening and the safety valve port are arranged on the upper sealing head, and the detachable air inlet pipe is arranged on the lower sealing head through the air inlet;
The lower seal head, the main shell and the upper seal head are all of a multilayer structure, and the multilayer structure comprises a pressure-bearing shell, an inner shell, an anchor nail and a heat-insulating casting material; the inner shell is arranged in the pressure-bearing shell, the heat-insulating casting material is filled in a gap between the inner shell and the pressure-bearing shell, one end of the anchor nail is fixedly connected with the pressure-bearing shell, and the other end of the anchor nail is anchored in the heat-insulating casting material to form a heat-insulating lining structure; the composite gas distribution plate and the second fold type redistribution plate are both arranged on the inner wall of the inner shell, and the heat exchange tube system is arranged on the main shell;
the upper end socket is provided with an access hole, and the main shell is provided with a plurality of pressure measuring holes at intervals; the lower part of the main shell is provided with a manhole, and the manhole comprises a distribution plate upper manhole positioned above the composite gas distribution plate and a distribution plate lower manhole positioned below the composite gas distribution plate; a plurality of ring seats are arranged on the outer wall of the pressure-bearing shell at intervals.
The composite gas distribution plate comprises an inverted cone-shaped distribution plate and a spherical crown-shaped distribution plate; the spherical crown-shaped distribution plate is of a spherical structure, the inverted cone-shaped distribution plate is of an inverted cone-shaped structure with a wide upper part and a narrow lower part, the upper end of the inverted cone-shaped distribution plate is fixedly connected to the inner wall of the inner layer shell, and the lower end of the inverted cone-shaped distribution plate is connected with the edge of the spherical crown-shaped distribution plate to form a composite gas distribution plate of a sunken cambered surface structure; nozzle mounting holes are uniformly distributed on the inverted cone-shaped distribution plate and the spherical crown-shaped distribution plate, floating type nozzles are mounted on the nozzle mounting holes of the spherical crown-shaped distribution plate, and float type nozzles are mounted on the nozzle mounting holes of the inverted cone-shaped distribution plate.
Each floating nozzle comprises a first locking piece, a nozzle tail part, a nozzle middle part and a nozzle head part; the tail part, the middle part and the head part are coaxially connected in sequence and are internally provided with a central tube, the lower end of the central tube penetrates through the tail part, and the upper end of the central tube extends into the head part; the outer diameter of the middle part of the nozzle is smaller than the aperture of the nozzle mounting hole, and the length of the middle part of the nozzle is larger than the thickness of the spherical crown-shaped distribution plate, so that the middle part of the nozzle can movably penetrate through the spherical crown-shaped distribution plate; the diameters of the first locking piece and the nozzle head are larger than those of the nozzle mounting hole, the tail of the nozzle is mounted on the spherical crown-shaped distribution plate in a limiting manner through the first locking piece, and the first locking piece and the nozzle head are respectively positioned below and above the spherical crown-shaped distribution plate;
An annular gap is formed in the nozzle head, one end of the annular gap is communicated with the top of the central tube, and the other end of the annular gap downwards penetrates through the nozzle head and faces the top surface of the spherical crown-shaped distribution plate.
Each float type nozzle comprises a second locking piece, a nozzle upper section, a hollow floating ball and a nozzle lower section; the bottom of the lower section of the nozzle vertically penetrates through the nozzle mounting hole and is locked on the inverted cone-shaped distribution plate through a second locking piece; cavities with narrow ends and wide middle are formed in the top parts of the upper nozzle section and the lower nozzle section, the hollow floating ball can be arranged in the wide part of the cavity in a floating mode, and the narrow ends of the cavity penetrate through the upper nozzle section and the lower nozzle section respectively.
The floating nozzles are arranged in a plurality of circles along the circumferential direction of the spherical crown-shaped distribution plate from inside to outside, and the diameters of the central tubes of the plurality of circles of floating nozzles are sequentially increased from inside to outside; the multi-turn floating nozzle divides the spherical crown-shaped distribution plate into three concentric circles/rings with equal areas; the plurality of float-type nozzles are arranged in a plurality of circles from inside to outside along the annular direction of the inverted cone-shaped distribution plate, and the diameters of the narrow parts at the top of the cavities of the plurality of circles of float-type nozzles are sequentially increased from inside to outside; the multi-turn float-type nozzle divides the inverted cone-shaped distribution plate into three concentric circles/rings with equal areas; the float type nozzle has a higher air velocity than the float type nozzle.
A heat exchange tube system is arranged in the reactor main body, a plurality of first fold type redistribution plates are arranged at intervals in the installation height range of the heat exchange tube system, and the heat exchange tube system penetrates through holes in the plurality of first fold type redistribution plates; the first corrugated redistribution board has the same structure as the second corrugated redistribution board.
Each second corrugated redistribution board comprises a support calandria, a short cylindrical section and a second corrugated redistributor; the second corrugated redistributors are embedded in the short cylinder section and are placed on the plurality of support calandria; the short cylinder sections are arranged on the inner wall of the inner shell through redistribution board brackets;
The second corrugated redistributor comprises a first corrugated single sheet and a second corrugated single sheet, and the first corrugated single sheet and the second corrugated single sheet are arranged in opposite oblique stagger;
In the two adjacent upper and lower second fold type redistribution plates, the arrangement directions of the second fold type redistributors are staggered by 90 degrees; in the two vertically adjacent first corrugated redistribution plates, the arrangement directions of the first corrugated redistributors thereof are staggered by 90 degrees.
The heat exchange pipe system comprises a cooling liquid inlet, an inlet annular distributing pipe, a lower heat compensation pipe, a heat exchange vertical pipe, an upper heat compensation pipe, an outlet annular distributing pipe and a cooling liquid outlet; the plurality of heat exchange vertical pipes are vertically and uniformly arranged in the inner-layer shell and penetrate through the plurality of first corrugated redistribution plates, one ends of the plurality of lower heat compensation pipes are respectively and correspondingly communicated with the lower ends of the plurality of heat exchange vertical pipes, and one ends of the plurality of upper heat compensation pipes are respectively and correspondingly communicated with the upper ends of the plurality of heat exchange vertical pipes; the other ends of the lower thermal compensation pipes are respectively communicated with an inlet annular distributing pipe, and a cooling liquid inlet is arranged on the inlet annular distributing pipe; the other ends of the upper thermal compensation pipes are respectively communicated with an outlet annular distribution pipe, and a cooling liquid outlet is arranged on the outlet annular distribution pipe; the inlet annular distributing pipe and the outlet annular distributing pipe are respectively of annular structures and are fixedly arranged on the outer wall of the pressure-bearing shell, and a plurality of lower thermal compensation pipes and a plurality of upper thermal compensation pipes penetrate through the main shell.
The detachable air inlet pipe comprises an air inlet pipe and an umbrella cap distributor; the air inlet pipe penetrates through the air inlet, one end of the air inlet pipe is positioned in the lower sealing head, and the umbrella cap distributor is arranged at one end of the air inlet pipe and positioned in the lower sealing head; the middle part of intake pipe and air inlet match and install, and the other end of intake pipe is located the outside of reactor main part and external air supply pipe.
Compared with the prior art, the utility model has the following beneficial effects:
1. The upper part of the reactor main body is only provided with the second fold type redistribution board, and the traditional gas-solid separation equipment is not arranged, so that the traditional dilute phase area is eliminated, only the core reaction function is reserved, the structure of the reactor main body is greatly simplified, and the manufacturing cost and the manufacturing difficulty are reduced.
2. The reactor main body adopts a multi-layer structure, and the pressure-bearing shell is only made of common steel plates through the arrangement of the heat insulation lining structure, and the inner shell is only made of high-temperature-resistant steel plates, so that the severe technical requirements of the high-temperature pressurized reactor shell on the adoption of high-temperature-resistant stainless steel materials are obviously reduced, the manufacturing cost is also greatly reduced, and the problem of large-scale hydrogenation fluidized bed reactors is thoroughly solved.
3. The utility model has the advantages that the inverted cone-shaped distribution plate and the spherical crown-shaped distribution plate are arranged, the sinking cambered surface structure has good compression resistance, meanwhile, the whole flow of the gas in the gas chamber is in a complete plug flow state, the phenomena of channeling, slugging and the like are thoroughly avoided, the continuous reaction of gas and solid phases is facilitated, and the conversion rate of products is improved.
4. The utility model has the advantages that the first fold type redistribution board and the second fold type redistribution board are arranged, so that large bubbles generated in the dense phase region of the reactor by the fold single-chip broken gas which is oppositely and obliquely staggered can be greatly increased, the contact opportunity between the gas phase and the solid phase is greatly increased, the back mixing among materials is obviously reduced, the reaction rate is further increased, and the conversion rate is improved.
Drawings
FIG. 1 is a front cross-sectional view of a high temperature pressurized fluidized bed reactor without a dilute phase zone according to the present utility model;
FIG. 2 is a front cross-sectional view of a removable air inlet pipe in a high temperature pressurized fluidized bed reactor without a dilute phase zone according to the present utility model;
FIG. 3 is a top cross-sectional view of a removable gas inlet tube in a freeboard high temperature pressurized fluidized bed reactor according to the present utility model;
FIG. 4 is a front cross-sectional view of a composite gas distribution plate in a non-dilute phase zone high temperature pressurized fluidized bed reactor according to the present utility model;
FIG. 5 is a top view of a composite gas distribution plate in a non-dilute phase zone high temperature pressurized fluidized bed reactor according to the present utility model;
FIG. 6 is a sectional view of a floating nozzle mounted on a spherical crown-shaped distribution plate in a high-temperature pressurized fluidized bed reactor without a dilute phase zone according to the present utility model, wherein the direction of the arrow in the figure is the gas flow direction;
FIG. 7 is a cross-sectional view of a floating nozzle (first lock not shown) in a non-dilute phase zone high temperature pressurized fluidized bed reactor according to the present utility model;
FIG. 8 is a sectional view showing the installation of float-type nozzles on an inverted cone-shaped distribution plate in a high-temperature pressurized fluidized bed reactor without a dilute phase zone according to the present utility model, wherein the direction of the arrow in the figure is the direction of the gas flow;
FIG. 9 is an exploded view of a floating nozzle (second lock not shown) in a freeboard zone high temperature pressurized fluidized bed reactor according to the present utility model;
FIG. 10 is a front view of a heat exchange tube system in a non-dilute phase zone high temperature pressurized fluidized bed reactor according to the present utility model, with the direction of the arrows in the direction of coolant flow;
FIG. 11 is a top view of the heat exchange tube system in a non-dilute phase zone high temperature pressurized fluidized bed reactor according to the present utility model;
FIG. 12 is a front cross-sectional view of a second pleated redistribution plate in a freeboard high temperature pressurized fluidized bed reactor according to the present utility model;
FIG. 13 is a bottom view of a second pleated redistribution plate in a non-dilute phase zone high temperature pressurized fluidized bed reactor according to the present utility model;
FIG. 14 is a schematic view of a corrugated redistributor in a high temperature pressurized fluidized bed reactor without dilute phase zone according to the present utility model, wherein the direction of the arrows in the figure is the gas flow direction;
FIG. 15 is a schematic view of the structure of a corrugated monolith in a freeboard high temperature pressurized fluidized bed reactor according to the present utility model;
FIG. 16 is a schematic view of the arrangement direction of two upper and lower adjacent second corrugated redistribution plates in a high temperature pressurized fluidized bed reactor without dilute phase zone according to the present utility model;
FIG. 17 is a schematic view of the arrangement direction of two upper and lower adjacent first corrugated redistribution plates in a high-temperature pressurized fluidized bed reactor without dilute phase zone according to the present utility model; .
In the figure, 1a detachable air inlet pipe, 101 an inlet flange, 102 an installation fixing flange, 103 an air inlet pipe, 104 a rib plate, 105 an umbrella cap distributor, 2 an air inlet, 3 a lower sealing head, 4 a composite gas distribution plate, 401 an inverted cone distribution plate, 402 a spherical crown distribution plate, 403 a nozzle installation hole, 5 a floating nozzle, 501 a first locking piece, 502 a nozzle tail, 503 a nozzle middle part, 504 a nozzle head, 505 an annular gap, 506 a central pipe, 6 a floating nozzle, 601 a second locking piece, 602 a nozzle upper section, 603 a hollow floating ball, 604 a nozzle lower section, 605 a cavity, 7 a solid material inlet, 8 a heat exchange pipe system, 801 a cooling liquid inlet, 802 an inlet annular distribution pipe, 803 a lower thermal compensation pipe, 804 heat exchange riser, 805 upper heat compensation tube, 806 outlet annular distribution tube, 807 coolant outlet, 808 distribution tube fixing plate, 9 pressure bearing housing, 10 inner housing, 11 anchor nails, 12 heat insulation casting material, 13 redistribution board support, 14 first fold redistribution board, 141 through hole, 1403 first fold redistribution board, 15 circle seat, 16 second fold redistribution board, 1601 support calandria, 1602 short cylinder section, 1603 second fold redistributor, 16031 first fold monolithic, 16032 second fold monolithic, 17 upper head, 18 gas phase outlet, 20 feed back port, 21 safety valve port, 22 detection port, 23 distribution board upper manhole, 24 distribution board lower manhole.
Detailed Description
The utility model will be further described with reference to the drawings and the specific examples.
Referring to fig. 1, a high-temperature pressurized fluidized bed reactor without a dilute phase zone comprises a detachable air inlet pipe 1, a reactor main body, a composite gas distribution plate 4, a floating nozzle 5, a floating nozzle 6, a solid material inlet 7 and a second fold type redistribution plate 16; an air inlet 2 is formed at the bottom of the reactor main body, and a detachable air inlet pipe 1 is detachably arranged on the air inlet 2 and communicated with the reactor main body; the compound gas distribution plate 4 is arranged at the lower part of the reactor main body, a plurality of floating type nozzles 5 and a plurality of float type nozzles 6 are respectively arranged on the compound gas distribution plate 4 at intervals, and the plurality of float type nozzles 6 are distributed at the outer sides of the plurality of floating type nozzles 5; the solid material inlets 7 are arranged at the lower part of the detachable air inlet pipe 1 in pairs and are communicated with the reactor main body, and the solid material inlets 7 are higher than the composite gas distribution plate 4; a plurality of second pleated redistribution plates 16 are respectively arranged in the reactor body at intervals by the redistribution plate brackets 13 and are positioned between the solid material inlet 7 and the gas phase outlet 18 at the top of the reactor body.
The upper part of the reactor body is provided with only the second pleated redistribution plate 16 without the conventional gas-solid separation equipment (such as cyclones and filters), i.e. the conventional dilute phase zone (separation zone) is eliminated. The separation zone of relatively irrelevant reaction can be moved to the outside of the reactor main body, so that the reactor main body only comprises a dense-phase zone (dense-phase section), namely a reaction zone (or part of transition zone), and the function of the separation zone can be installed and realized in an external form by the cyclone separator and a dipleg (a return system) of the prior art, thereby reducing the volume of the reactor main body, reducing the manufacturing difficulty and the cost and ensuring that the structural arrangement is simpler.
Preferably, the solid material inlets 7 may be arranged in pairs above and near the composite gas distribution plate 4, so that the solid material enters the reactor body and is evenly distributed in the reactor body, preferably the solid material inlets 7 are 1-2 pairs.
The floating nozzle 5 and the floating nozzle 6 on the composite gas distribution plate 4 can uniformly distribute the raw gas entering the reactor main body and can also make the distribution of solid materials more uniform, thereby improving the reaction rate and the conversion rate.
Referring to fig. 1, the reactor main body includes a lower seal head 3, a main housing, an upper seal head 17, a feed back port 20 and a safety valve port 21; the lower seal head 3 and the upper seal head 17 are respectively connected to the bottom and the top of the main shell to form a closed shell structure of the reactor; the gas phase outlet 18, the feed back opening 20 and the safety valve port 21 are arranged on the upper sealing head 17, and the detachable air inlet pipe 1 is arranged on the lower sealing head 3 through the air inlet 2.
Referring to fig. 1, the lower seal head 3, the main housing and the upper seal head 17 are all of a multi-layer structure, and the multi-layer structure comprises a pressure-bearing housing 9, an inner housing 10, an anchor nail 11 and a heat-insulating casting material 12; the inner shell 10 is arranged in the pressure-bearing shell 9, the heat-insulating casting material 12 is filled in a gap between the inner shell 10 and the pressure-bearing shell 9, one end of the anchor nail 11 is fixedly connected with the pressure-bearing shell 9 through welding, and the other end of the anchor nail 11 is anchored in the heat-insulating casting material 12 to form a heat-insulating lining structure; the composite gas distribution plate 4 and the second corrugated redistribution plate 16 are both mounted on the inner wall of the inner shell 10, and the heat exchange tube system 8 is mounted on the main shell.
By the arrangement of the heat insulating lining structure, heat insulation, heat preservation and pressure transmission can be realized, and meanwhile, the loss of heat in the inner layer shell 10 is greatly reduced. The pressure-bearing shell 9 can be manufactured by adopting a common container steel plate, and the common container steel plate only needs to bear pressure by virtue of the heat insulation effect of the heat insulation lining structure, and does not need to bear a high-temperature working condition, so that the technical requirements and the manufacturing cost of the steel plate of the pressure-bearing shell 9 are greatly reduced.
The inner shell 10 can be made of a high-temperature resistant stainless steel (such as N08810 stainless steel) plate, the inner shell 10 does not need to bear pressure, only needs to bear high temperature and meet the requirement of supporting internal components, and certain trace impurities in the heat insulation lining structure can be prevented from being mixed into a reaction system, so that the influence on the product quality is thoroughly avoided. The thickness of the steel plate of the inner shell 10 can meet the use requirement by only 4-8mm, and the manufacturing cost is low. The reactor body of the multilayer structure can thoroughly solve the problem such as the enlargement of the hydrogenation fluidized bed reactor.
Referring to fig. 1, the upper end enclosure 17 is provided with an access hole 19, and the main housing is provided with a plurality of pressure measuring holes 22 at intervals; the lower part of the main shell is provided with manholes, and the manholes comprise a distribution plate upper manhole 23 positioned above the composite gas distribution plate 4 and a distribution plate lower manhole 24 positioned below the composite gas distribution plate 4; a plurality of ring seats 15 are arranged on the outer wall of the pressure-bearing shell 9 at intervals.
Preferably, the pressure measuring ports 22 may be arranged at equal intervals along the height direction of the main housing and communicate with the inside of the inner housing 10, for detecting the air pressure in the inner housing 10, and ensuring the safety of the reaction process.
Referring to fig. 4 and 5, the composite gas distribution plate 4 includes an inverted cone-shaped distribution plate 401 and a spherical crown-shaped distribution plate 402; the spherical crown-shaped distribution plate 402 is in a spherical structure, the inverted cone-shaped distribution plate 401 is in an inverted cone-shaped structure with a wide upper part and a narrow lower part, the upper end of the inverted cone-shaped distribution plate 401 is fixedly connected to the inner wall of the inner layer shell 10, and the lower end of the inverted cone-shaped distribution plate 401 is connected with the edge of the spherical crown-shaped distribution plate 402 to form a composite gas distribution plate 4 with a sunken cambered surface structure; nozzle mounting holes 403 are uniformly distributed on the inverted cone-shaped distribution plate 401 and the spherical crown-shaped distribution plate 402, floating nozzles 5 are mounted on the nozzle mounting holes 403 of the spherical crown-shaped distribution plate 402, and floating nozzles 6 are mounted on the nozzle mounting holes 403 of the inverted cone-shaped distribution plate 401.
The diameter of the edge of the spherical crown-shaped distribution plate 402 is D2, and the top area of the spherical crown-shaped distribution plate 402 is 85% of the cross-sectional area of the inner shell 10; the diameter of the upper end of the inverted cone-shaped distribution plate 401 is consistent with the inner diameter of the inner layer shell 10 and is D1, and the diameter of the lower end of the inverted cone-shaped distribution plate 401 is consistent with the diameter of the edge of the spherical crown-shaped distribution plate 402; the included angle between the plate surface of the inverted cone-shaped distribution plate 401 and the horizontal plane is alpha, and the value of alpha is 45-75 degrees; the aperture of the nozzle mounting holes 403 is d0, d0 takes a value of 12-36mm, and the center-to-center distance between two adjacent nozzle mounting holes 403 on the same circumference is s, and s takes a value of 50-150mm.
Preferably, the spherical crown-shaped distribution plate 402 and the inverted cone-shaped distribution plate 401 can be made of high-temperature resistant stainless steel materials, and can be integrally formed or welded into an integral structure, and the whole composite gas distribution plate 4 is a revolution body with uniform thickness.
Referring to fig. 6 and 7, each of the floating nozzles 5 includes a first locking member 501, a nozzle tail 502, a nozzle middle 503, and a nozzle head 504; the nozzle tail 502, the nozzle middle 503 and the nozzle head 504 are sequentially and coaxially connected and are internally provided with a central tube 506, the lower end of the central tube 506 penetrates through the nozzle tail 502, and the upper end of the central tube 506 extends into the nozzle head 504; the outer diameter d4 of the nozzle middle part 503 is slightly smaller than the aperture d0 of the nozzle mounting hole 403, and the length of the nozzle middle part 503 is longer than the thickness of the spherical crown-shaped distribution plate 402, so that the nozzle middle part 503 can movably penetrate through the spherical crown-shaped distribution plate 402; the diameters of the first locking piece 501 and the nozzle head 504 are larger than the aperture d0 of the nozzle mounting hole 403, the nozzle tail 502 is mounted on the spherical crown-shaped distribution plate 402 in a limiting mode through the first locking piece 501, and the first locking piece 501 and the nozzle head 504 are located below and above the spherical crown-shaped distribution plate 402 respectively.
Preferably, the outer wall of the nozzle tail 502 is provided with external threads, and the first locking member 501 may be a nut matched with the nozzle tail 502, so that the first locking member 501 is screwed and locked on the nozzle tail 502. The first locking member 501 has an outer diameter larger than the aperture d0 of the nozzle mounting hole 403, and can play a limiting role to prevent the floating nozzle 5 from coming out of the nozzle mounting hole 403.
An annular gap 505 is formed in the nozzle head 504, one end of the annular gap 505 is communicated with the top of the central tube 506, and the other end of the annular gap 505 penetrates the nozzle head 504 downwards and faces the top surface of the spherical crown-shaped distribution plate 402.
After entering the central tube 506 from the nozzle tail 502, the air flow flows downwards out of the nozzle head 504 through the annular gap 505 and is sprayed onto the top surface of the spherical crown-shaped distribution plate 402, so that the air flow is utilized to form a reaction force on the floating nozzle 5, the floating nozzle 5 is pushed upwards, and the nozzle middle 503 moves upwards relative to the spherical crown-shaped distribution plate 402 through the nozzle mounting hole 403. The relative distance between the floating nozzle 5 and the spherical crown distribution plate 402 can be adjusted according to the air flow, so that the floating nozzle 5 can float freely up and down.
Preferably, the relationship between the inner ring diameter d5 of the annular gap 505 and the outer ring diameter d6 of the annular gap 505 and the diameter d3 of the center tube 506 is: (d 6) 2-(d5)2＝(d3)2.
Referring to fig. 4, a plurality of floating nozzles 5 are arranged in a plurality of circles along the circumferential direction of the spherical crown-shaped distribution plate 402, and the diameter d3 of the central tube 506 of the plurality of circles of floating nozzles 5 increases sequentially from inside to outside; the multi-turn floating nozzle 5 divides the spherical crown-shaped distribution plate 402 into three concentric circles/rings of equal area.
Referring to fig. 8 and 9, each of the float-type nozzles 6 includes a second locking member 601, an upper nozzle section 602, a hollow float 603 and a lower nozzle section 604; the upper nozzle section 602 is coaxially connected with the top of the lower nozzle section 604, the bottom of the lower nozzle section 604 is bent and extended towards the inner wall direction of the inner shell 10, and the bottom of the lower nozzle section 604 penetrates through the nozzle mounting hole 403 and is locked on the inverted cone-shaped distribution plate 401 through the second locking piece 601; a hollow cavity 605 with narrow ends and wide middle is formed in the top of the upper nozzle section 602 and the lower nozzle section 604, and a hollow floating ball 603 is floatably arranged in the wide part of the hollow cavity 605, and the narrow ends of the hollow cavity 605 respectively penetrate through the upper nozzle section 602 and the lower nozzle section 604.
Preferably, the relationship between the inner diameter d11 and the outer diameter d10 of the hollow floating ball 603 is: d11/d10=0.65 to 0.9, and the outer diameter d10 of the hollow floating ball 603 is smaller than the wide diameter d9 of the cavity 605. The hollow floating ball 603 can be made of high-temperature resistant stainless steel material.
Preferably, the top narrow diameter d12 and the bottom narrow diameter d7 of the cavity 605 are smaller than the wide diameter d9; the bottom of the lower nozzle section 604 vertically penetrates through the inverted cone-shaped distribution plate 401, and the included angle between the top central line and the bottom central line of the lower nozzle section 604, namely the bottom bending angle of the lower nozzle section 604, is 180 degrees to alpha, and the alpha takes a value of 45 degrees to 75 degrees.
Preferably, the bottom of the lower nozzle section 604 is provided with external threads, and the second locking member 601 is screwed and locked on the bottom of the lower nozzle section 604 by adopting a nut matched with the bottom of the lower nozzle section 604.
Referring to fig. 4, a plurality of the float-type nozzles 6 are arranged in a plurality of circles along the circumferential direction of the inverted cone-shaped distribution plate 401 from inside to outside, and the diameter d12 of the narrow part at the top of the cavity 605 of the plurality of circles of float-type nozzles 6 is sequentially increased from inside to outside; the multi-turn float nozzle 6 divides the inverted cone-shaped distribution plate 401 into three concentric circles/rings of equal area; when the float-type nozzle 6 and the float-type nozzle 5 are selected, the air velocity of the float-type nozzle 6 is 5 to 15% higher than that of the float-type nozzle 5.
The structure of the spherical crown-shaped distribution plate 402 and the inverted cone-shaped distribution plate 401 has good compression resistance, and can bear enough material weight without deformation under the high-temperature condition. The composite gas distribution plate 4 thoroughly avoids the phenomena of channeling, slugging and the like, is favorable for continuous reaction of gas phase and solid phase, and improves the conversion rate of products. After the float type nozzles 6 and 5 are arranged through the nozzle mounting holes 403, the gas distribution is more uniform, and the whole flow of the gas in the gas chamber can be in a complete plug flow state. Particularly, when the air inflow fluctuates, the floating type nozzle 5 floats up and down relative to the spherical crown-shaped distribution plate 402 through the middle part 503 of the nozzle, the hollow floating ball 603 floats up and down in the cavity 605, which is equivalent to a floating valve structure, and can play a role in slowing down the fluctuation of the air inflow, so that the floating type nozzle 6 and the floating type nozzle 5 have the function of automatically adjusting the opening degree, ensure that a bed layer is more stable, thoroughly avoid the plate surface leakage phenomenon of powder materials, and have long service life and convenient maintenance and overhaul.
Referring to fig. 1, a heat exchange tube system 8 is disposed in the reactor main body, a plurality of first corrugated redistribution plates 14 are disposed at intervals within a height range of the heat exchange tube system 8, and the heat exchange tube system 8 penetrates through holes 141 on the plurality of first corrugated redistribution plates 14.
The first corrugated redistribution board 14 has the same structure as the second corrugated redistribution board 16, and is installed in the inner layer subject 10 in the same manner, except that: since the heat exchange tube system penetrates through the first corrugated redistribution board 14, through holes 141 for the heat exchange tube system 8 to penetrate through are reserved on the first corrugated redistribution board 14, so as to replace the second corrugated redistribution board 16 within the installation height range of the heat exchange tube system 8, and avoid interference between the second corrugated redistribution board 16 and the heat exchange tube system 8. Only the structure of the second corrugated redistribution board 16 will be described in detail below, and the first corrugated redistribution board 14 may be provided with through holes 141 according to the installation requirements of the heat exchange tube system 8 on the basis of the second corrugated redistribution board 16.
Referring to fig. 11 and 12, each of the second pleated redistribution plates 16 includes a support gauntlet 1601, a short cylindrical section 1602, and a second pleated redistributor 1603; a plurality of support gauntlets 1601 are arranged in the short cylinder section 1602 at intervals, and a second corrugated redistributor 1603 is embedded in the short cylinder section 1602 and is placed on the plurality of support gauntlets 1601; the short cylinder segments 1602 are mounted on the inner wall of the inner housing 10 by redistribution board brackets 13.
Preferably, the support tube 1601 may be made of a high temperature resistant stainless steel tube, and two ends of the support tube 1601 are welded to the inner wall of the short cylinder section 1602, and a plurality of support tube 1601 are arranged in parallel and equidistant. The edge of the second corrugated redistributor 1603 is welded and fixed to the inner wall of the short cylinder section 1602, and a plurality of support gauntlets 1601 are used for supporting and mounting the second corrugated redistributor 1603.
Referring to fig. 14, the second corrugated redistributor 1603 includes a first corrugated sheet 16031 and a second corrugated sheet 16032, and the first corrugated sheet 16031 and the second corrugated sheet 16032 are staggered in opposite directions.
Preferably, the first corrugated sheet 16031 and the second corrugated sheet 16032 are each a fold-line shaped sheet-like structure formed of high temperature resistant stainless steel metal. The folded portions of the adjacent first and second corrugated sheets 16031, 16032 are joined, and a plurality of quadrangular through grooves are formed between the adjacent first and second corrugated sheets 16031, 16032 for allowing the flow of air therethrough. Because the first corrugated single sheets 16031 and the second corrugated single sheets 16032 are oppositely and obliquely staggered, the air flow directions on two adjacent rows of quadrilateral through grooves are different, and the effect of uniform air flow is achieved.
Referring to fig. 15 and 16, in two adjacent second corrugated redistribution boards 16, the arrangement directions of the second corrugated redistributors 1603 are staggered by 90 °; in the two above-described first corrugated redistribution boards 14 adjacent to each other in the upper and lower direction, the arrangement directions of the first corrugated redistributors 1403 thereof are staggered by 90 °.
Referring to fig. 15, the following geometric relationship is preferably satisfied at the fold surface of the first and second corrugated sheets 16031, 16032:
The calculation formula of the surface-to-surface crease length L is as follows:
The calculation formula of the single piece width x of the folding surface is as follows: x= Lsin (+_a1).
The calculation formula of the single sheet height H of the folding surface is as follows: h= Lsin (+_a3).
The calculation formula of the relative single piece width of the folding surface is as follows:
the calculation formula of the relative monolithic height of the folding surface is as follows:
In the fluidized bed reactors of the prior art, after the gas leaves the gas distribution plate to a certain height, the mixing of the gas and solid phases again occurs unevenly. The solid particles are in a continuous motion state, so that the gas is backmixed, generated bubbles are continuously grown, particles are dense, and the like, poor gas-solid contact and short circuit of the gas are caused, the diameter of the solid particles is continuously increased along with the large-scale development of equipment, the situation is obviously worsened, the conversion rate of the reaction is reduced, and the solid particles are also serious defects of the fluidized bed reactor. In order to increase the conversion and throughput of the fluidized bed reactor, it is necessary to enhance gas exchange between the gas bubbles and the continuous phase, reduce back mixing of the gas, and break up the gas bubbles so as to increase the contact between the gas and the solid phase.
The utility model is formed by welding and connecting the first folding single sheets 10631 and the second folding single sheets 10632 in opposite oblique staggered arrangement, so that the gas flows from bottom to top in staggered oblique manner along the folding direction of the folding surface, and the powder particles flow from top to bottom in staggered oblique manner or are entrained by the gas to flow upwards together with the powder particles. Due to the oblique arrangement of the fold surfaces, the first 14 and second 16 corrugated redistribution panels are not bottomed out in plan view, and may all catch particles that fall vertically by gravity, while the obliquely rising gas may pass substantially all. Because of the staggered diagonal movement of the bubbles and particles, the first 14 and second 16 corrugated redistribution plates create small and large volumes of vortices, which are very advantageous for homogenization of the bed. Meanwhile, the first corrugated redistribution plates 14 and the second corrugated redistribution plates 16 can crush large bubbles generated by gas in a dense phase zone of the reactor, so that the contact opportunity between gas and solid phases is greatly increased, the back mixing among materials is obviously reduced, and the reaction rate and the conversion rate are increased.
Referring to fig. 10 and 11, the heat exchange tube system 8 includes a cooling fluid inlet 801, an inlet annular distribution tube 802, a lower heat compensation tube 803, a heat exchange riser 804, an upper heat compensation tube 805, an outlet annular distribution tube 806, and a cooling fluid outlet 807; the heat exchange risers 804 are vertically and uniformly arranged in the inner shell 10 and penetrate through the through holes 141 reserved on the first corrugated redistribution plates 14, one ends of the lower heat compensation pipes 803 are correspondingly communicated with the lower ends of the heat exchange risers 804 respectively, and one ends of the upper heat compensation pipes 805 are correspondingly communicated with the upper ends of the heat exchange risers 804 respectively; the other ends of the plurality of lower thermal compensation pipes 803 are respectively communicated with an inlet annular distribution pipe 802, and a cooling liquid inlet 801 is arranged on the inlet annular distribution pipe 802; the other ends of the upper heat compensation pipes 805 are respectively communicated with an outlet annular distribution pipe 806, and the outlet annular distribution pipe 806 is provided with a cooling liquid outlet 807; the inlet annular distribution pipe 802 and the outlet annular distribution pipe 806 are respectively of annular structure and fixedly arranged on the outer wall of the pressure-bearing shell 9 through a distribution pipe fixing plate 808, and a plurality of lower thermal compensation pipes 803 and a plurality of upper thermal compensation pipes 805 penetrate through the main shell.
Preferably, the lower thermal compensation tube 803 and the upper thermal compensation tube 805 are of a bent structure for compensating thermal expansion. The heat required for the reaction can be taken out or supplied by the circulating flow of the cooling liquid in the inlet annular distribution pipe 802, the lower thermal compensation pipe 803, the heat exchange riser 804, the upper thermal compensation pipe 805 and the outlet annular distribution pipe 806 for maintaining an optimal, constant reaction temperature to obtain the highest reaction conversion, which is applicable to most reaction systems. In a few reaction systems which can self-maintain the reaction temperature, the heat exchange tube system 8 is not required, so that the volume of the main shell is further reduced.
Referring to fig. 2 and 3, the detachable air inlet pipe 1 includes an air inlet pipe 103 and an umbrella cap dispenser 105; the air inlet pipe 103 penetrates through the air inlet 2, one end of the air inlet pipe 103 is positioned in the lower seal head 3, and the umbrella cap distributor 105 is arranged at one end of the air inlet pipe 103 through a plurality of rib plates 104 and positioned in the lower seal head 3; the middle part of the air inlet pipe 103 is matched and installed with the preassembled flange on the air inlet 2 through the installation fixing flange 102, and the other end of the air inlet pipe 103 is positioned outside the reactor main body and externally connected with an air supply pipe through the inlet flange 101.
Preferably, three rib plates 104 are provided, and are uniformly arranged along the circumferential direction of the end of the air inlet pipe 103 for installing the umbrella hat distributor 105. The umbrella cap dispenser 105 is a common device for dispensing fluids, and the model and specification of the umbrella cap dispenser 105 can be selected according to actual use requirements.
Referring to fig. 1 to 17, the working principle of the present utility model is:
On the one hand, the raw material gas enters from the detachable air inlet pipe 1 at the bottom of the reactor main body, and the inlet raw material gas is uniformly distributed in the space between the lower sealing head 3 and the composite gas distribution plate 4 due to the pre-distribution function of the umbrella cap distributor 105, and then the raw material gas is uniformly distributed again through the floating type nozzles 5 and the floating type nozzles 6 on the composite gas distribution plate 4.
The gas distribution plates of the prior art mostly adopt planar circular plates, so that in the gas chamber of the fluidized bed reactor, the gas with the fastest flow rate is positioned in the center of the whole flow field, i.e. the gas in the gas chamber flows in an elliptical-like flow layer as a whole. The gas flow rate of the solid powder material entering the fluidized bed reactor through the plane circular gas distribution plate and the gas participating in the reaction is always larger than the gas flow rate at the edge of the fluidized bed, the gas flow rate is very uneven, phenomena such as channeling, slugging and the like are easily generated in the fluidized bed reactor, and the reaction of the gas phase and the solid phase is not facilitated. Along with the large-scale of the reactor in the prior art, the diameter of the reactor is larger and larger, the quality of solid particle materials or catalysts filled in the reactor is also larger and larger, the planar circular gas distribution plate in the prior art can not meet the production requirements obviously, and the gas distribution plate has poor bearing capacity, serious deformation and worsening under the high-temperature working condition.
In order to avoid the phenomenon that the whole flow of the gas in the gas chamber is not uniform, the utility model ensures that the gas in the central area of the gas chamber in the reactor body is properly decelerated after passing through the spherical crown-shaped distribution plate 402 by arranging the spherical crown-shaped distribution plate 402 and the plurality of circles of floating nozzles 5, and the gas in the peripheral area leaving the central area is gradually accelerated, so that the gas speed in the whole spherical crown-shaped distribution plate 402 area is more uniform.
It is known that the annular region near the reactor wall is a relatively special region and that the gas is easily disturbed by the viscous forces of the wall and is decelerated. Since the floating nozzle 5 does not work properly in a ring-shaped special area close to the reactor wall. According to the utility model, through the arrangement of the inverted cone-shaped distribution plate 401 and the plurality of circles of float-type nozzles 6, after the gas passes through the inverted cone-shaped distribution plate 401, the gas close to the inner wall of the inner layer shell 10 is accelerated in a strengthening way, namely, the gas velocity in the area of the inverted cone-shaped distribution plate 401 is more uniform, so that the gas velocity of the gas passing through the whole composite gas distribution plate 4 is ensured to be uniform, and the whole flow of the gas in the gas chamber is in a complete plug flow state.
On the other hand, the reaction solid particle materials or catalysts enter the reactor from the solid material inlets 7 which are symmetrically arranged in pairs, and the symmetrical addition of the reaction solid particle materials or catalysts is equivalent to the pre-distribution once, so that the interference on the whole bed layer is small.
The combination of the uniform air flows of the floating nozzle 5 and the floating nozzle 6 ensures that solid particle materials or catalysts distributed in the air flows are uniformly dispersed, ensures that the gas phase and the solid phase in a part of the space area at the upper part of the composite gas distribution plate 4 can be fully contacted, greatly increases the reaction rate and improves the reaction conversion rate.
Referring to fig. 1 to 17, embodiment 1:
The utility model relates to a high-temperature pressurized fluidized bed reactor without dilute phase zone for producing aluminum nitride powder products, which adopts the technical process of aluminum powder direct nitriding method, and the principle is as follows: and placing the dried aluminum powder into a high-temperature high-pressure fluidized bed reactor, and obtaining aluminum nitride powder under the operation conditions of 600-630 ℃ and 3.5 MPa.
The high-temperature pressurized fluidized bed reactor without dilute phase zone comprises a detachable air inlet pipe 1, a reactor main body, a composite gas distribution plate 4, a floating nozzle 5, a floating nozzle 6, a solid material inlet 7, a heat exchange pipe system 8, a first fold type redistribution plate 14 and a second fold type redistribution plate 16; an air inlet 2 is formed at the bottom of the reactor main body, and a detachable air inlet pipe 1 is detachably arranged on the air inlet 2 and communicated with the reactor main body; the compound gas distribution plate 4 is arranged at the lower part of the reactor main body, a plurality of floating type nozzles 5 and a plurality of float type nozzles 6 are respectively arranged on the compound gas distribution plate 4 at intervals, and the plurality of float type nozzles 6 are distributed at the outer sides of the plurality of floating type nozzles 5; two pairs of solid material inlets 7 are arranged at the lower part of the detachable air inlet pipe 1 and are communicated with the reactor main body, and the solid material inlets 7 are higher than the composite gas distribution plate 4; a plurality of first corrugated redistribution plates 14 and a plurality of second corrugated redistribution plates 16 are respectively arranged in the reactor body at intervals through the redistribution plate brackets 13 and are positioned between the solid material inlet 7 and the gas phase outlet 18 at the top of the reactor body; the heat exchange tube system 8 is arranged in the upper middle part of the reactor body and extends through several first corrugated redistribution plates 14. The upper part of the reactor body is not provided with a dilute phase zone (separation zone).
The reactor main body comprises a lower seal head 3, a main shell, an upper seal head 17, a feed back opening 20 and a safety valve port 21; the lower seal head 3 and the upper seal head 17 are respectively connected to the bottom and the top of the main shell to form a closed shell structure of the reactor; the gas phase outlet 18, the feed back opening 20 and the safety valve port 21 are arranged on the upper sealing head 17, and the detachable air inlet pipe 1 is arranged on the lower sealing head 3 through the air inlet 2.
The lower seal head 3, the main shell and the upper seal head 17 are all of a multi-layer structure, and the multi-layer structure comprises a pressure-bearing shell 9, an inner shell 10, an anchor nail 11 and a heat-insulating casting material 12; the inner shell 10 is arranged in the pressure-bearing shell 9, the heat-insulating casting material 12 is filled in a gap between the inner shell 10 and the pressure-bearing shell 9, one end of the anchor nail 11 is fixedly connected with the pressure-bearing shell 9 through welding, and the other end of the anchor nail 11 is anchored in the heat-insulating casting material 12 to form a heat-insulating lining structure; the composite gas distribution plate 4, the first corrugated redistribution plate 14 and the second corrugated redistribution plate 16 are all mounted on the inner wall of the inner shell 10, and the heat exchanger tube system 8 is mounted on the main shell.
The inner housing 10 is made of 4mm thick S31008 high temperature resistant stainless steel material.
The upper seal head 17 is provided with an overhaul port 19, and 6 pressure measuring ports 22 are arranged on the main shell at equal intervals along the height direction; the lower part of the main shell is provided with manholes, and the manholes comprise a distribution plate upper manhole 23 positioned above the composite gas distribution plate 4 and a distribution plate lower manhole 24 positioned below the composite gas distribution plate 4; a plurality of ring seats 15 are arranged on the outer wall of the pressure-bearing shell 9 at intervals.
The composite gas distribution plate 4 comprises an inverted conical distribution plate 401 and a spherical crown distribution plate 402; the spherical crown-shaped distribution plate 402 is in a spherical structure, the inverted cone-shaped distribution plate 401 is in an inverted cone-shaped structure with a wide upper part and a narrow lower part, the upper end of the inverted cone-shaped distribution plate 401 is fixedly connected to the inner wall of the inner layer shell 10, and the lower end of the inverted cone-shaped distribution plate 401 is connected with the edge of the spherical crown-shaped distribution plate 402 to form a composite gas distribution plate 4 with a sunken cambered surface structure; nozzle mounting holes 403 are uniformly distributed on the inverted cone-shaped distribution plate 401 and the spherical crown-shaped distribution plate 402, floating nozzles 5 are mounted on the nozzle mounting holes 403 of the spherical crown-shaped distribution plate 402, and floating nozzles 6 are mounted on the nozzle mounting holes 403 of the inverted cone-shaped distribution plate 401.
The composite gas distribution plate 4 is made of an S31008 high temperature resistant stainless steel material.
The diameter of the edge of the spherical crown-shaped distribution plate 402 is D2, and the top area of the spherical crown-shaped distribution plate 402 is 85% of the cross-sectional area of the inner shell 10; the diameter of the upper end of the inverted cone-shaped distribution plate 401 is consistent with the inner diameter of the inner layer shell 10 and is D1, and the diameter of the lower end of the inverted cone-shaped distribution plate 401 is consistent with the diameter of the edge of the spherical crown-shaped distribution plate 402; the included angle between the plate surface of the inverted cone-shaped distribution plate 401 and the horizontal plane is alpha, and the alpha takes a value of 45 degrees; the aperture of the nozzle mounting holes 403 is d0, d0 takes a value of 12mm, and the center-to-center distance between two adjacent nozzle mounting holes 403 on the same circumference is s, s takes a value of 50mm.
Each of the floating nozzles 5 includes a first locking member 501, a nozzle tail 502, a nozzle middle 503, and a nozzle head 504; the nozzle tail 502, the nozzle middle 503 and the nozzle head 504 are sequentially and coaxially connected and are internally provided with a central tube 506, the lower end of the central tube 506 penetrates through the nozzle tail 502, and the upper end of the central tube 506 extends into the nozzle head 504; the outer diameter d4 of the nozzle middle part 503 is slightly smaller than the aperture d0 of the nozzle mounting hole 403, and the length of the nozzle middle part 503 is longer than the thickness of the spherical crown-shaped distribution plate 402, so that the nozzle middle part 503 can movably penetrate through the spherical crown-shaped distribution plate 402; the diameters of the first locking piece 501 and the nozzle head 504 are larger than the aperture d0 of the nozzle mounting hole 403, the nozzle tail 502 is mounted on the spherical crown-shaped distribution plate 402 in a limiting mode through the first locking piece 501, and the first locking piece 501 and the nozzle head 504 are located below and above the spherical crown-shaped distribution plate 402 respectively.
An annular gap 505 is formed in the nozzle head 504, one end of the annular gap 505 is communicated with the top of the central tube 506, and the other end of the annular gap 505 penetrates the nozzle head 504 downwards and faces the top surface of the spherical crown-shaped distribution plate 402.
Preferably, the relationship between the inner ring diameter d5 of the annular gap 505 and the outer ring diameter d6 of the annular gap 505 and the diameter d3 of the center tube 506 is: (d 6) 2-(d5)2＝(d3)2.
The floating nozzles 5 are arranged in three circles along the circumferential direction of the spherical crown-shaped distribution plate 402, and the diameters d3 of the central tubes 506 of the three circles of floating nozzles 5 are sequentially increased from inside to outside. The three-turn floating nozzle 5 divides the spherical crown-shaped distribution plate 402 into three concentric circles/rings of equal area.
Each float-type nozzle 6 comprises a second locking piece 601, a nozzle upper section 602, a hollow floating ball 603 and a nozzle lower section 604; the upper nozzle section 602 is coaxially connected with the top of the lower nozzle section 604, the bottom of the lower nozzle section 604 is bent and extended towards the inner wall direction of the inner shell 10, and the bottom of the lower nozzle section 604 penetrates through the nozzle mounting hole 403 and is locked on the inverted cone-shaped distribution plate 401 through the second locking piece 601; a hollow cavity 605 with narrow ends and wide middle is formed in the top of the upper nozzle section 602 and the lower nozzle section 604, and a hollow floating ball 603 is floatably arranged in the wide part of the hollow cavity 605, and the narrow ends of the hollow cavity 605 respectively penetrate through the upper nozzle section 602 and the lower nozzle section 604.
The relationship between the inner diameter d11 and the outer diameter d10 of the hollow floating ball 603 is: d11/d10=0.65, and the outer diameter d10 of the hollow float 603 is smaller than the wide diameter d9 of the cavity 605. The hollow floating ball 603 can be made of S31008 high temperature resistant stainless steel material.
The top narrow diameter d12 and the bottom narrow diameter d7 of the cavity 605 are smaller than the wide diameter d9; the bottom of the lower nozzle section 604 vertically penetrates through the inverted cone-shaped distribution plate 401, and the included angle between the top central line and the bottom central line of the lower nozzle section 604, namely the bottom bending angle of the lower nozzle section 604, is 180 degrees to alpha, and the alpha takes a value of 45 degrees.
The bottom of the lower nozzle section 604 is provided with external threads, and the second locking member 601 is screwed and locked on the bottom of the lower nozzle section 604 by adopting a nut matched with the bottom of the lower nozzle section 604.
The float-type nozzles 6 are arranged in a plurality of circles along the annular direction of the inverted cone-shaped distribution plate 401 from inside to outside, and the diameters d12 of the narrow parts at the top of the cavity 605 of the float-type nozzles 6 in the plurality of circles are sequentially increased from inside to outside; when the float-type nozzle 6 and the float-type nozzle 5 type are selected, the float-type nozzle 6 has a gas velocity 5% higher than that of the float-type nozzle 5.
The first plurality of corrugated redistribution panels 14 are arranged within the installation height of the heat exchanger tube system 8 and the second plurality of corrugated redistribution panels 16 are arranged within the area between the bottom of the heat exchanger tube system 8 and the solid material inlet 7 and between the top of the heat exchanger tube system 8 and the gas phase outlet 18. The first corrugated redistribution board 14 is identical to the second corrugated redistribution board 16 in structure, with the only difference that: since the heat exchange tube system penetrates through the first corrugated redistribution board 14, through holes 141 for the heat exchange tube system 8 to penetrate through are reserved on the first corrugated redistribution board 14. Only the structure of the second corrugated redistribution board 16 will be described in detail below, and the first corrugated redistribution board 14 may be provided with through holes 141 according to the installation requirements of the heat exchange tube system 8 on the basis of the second corrugated redistribution board 16.
Each of the second pleated redistribution plates 16 includes a support gauntlet 1601, a short cylindrical section 1602 and a second pleated redistributor 1603; a plurality of support gauntlets 1601 are arranged in the short cylinder section 1602 at intervals, and a second corrugated redistributor 1603 is embedded in the short cylinder section 1602 and is placed on the plurality of support gauntlets 1601; the short cylinder segments 1602 are mounted on the inner wall of the inner housing 10 by redistribution board brackets 13.
The support calandria 1601 can be made of high temperature resistant stainless steel pipe, and two ends are welded and fixed with the inner wall of the short cylinder section 1602, and a plurality of support calandria 1601 are arranged in parallel and equidistant. The edge of the second corrugated redistributor 1603 is welded and fixed to the inner wall of the short cylinder section 1602, and a plurality of support gauntlets 1601 are used for supporting and mounting the second corrugated redistributor 1603.
The second corrugated redistributor 1603 includes a first corrugated sheet 16031 and a second corrugated sheet 16032, the first corrugated sheet 16031 and the second corrugated sheet 16032 being staggered in opposite oblique directions.
The first corrugated sheet 16031 and the second corrugated sheet 16032 are each a fold-line-shaped sheet-like structure formed of a high temperature resistant stainless steel metal. The folded portions of the adjacent first and second corrugated sheets 16031, 16032 are joined, and a plurality of quadrangular through grooves are formed between the adjacent first and second corrugated sheets 16031, 16032 for allowing the flow of air therethrough. Because the first corrugated single sheets 16031 and the second corrugated single sheets 16032 are oppositely and obliquely staggered, the air flow directions on two adjacent rows of quadrilateral through grooves are different, and the effect of uniform air flow is achieved.
In the two upper and lower adjacent second corrugated redistribution boards 16, the arrangement directions of the second corrugated redistributors 1603 thereof are staggered by 90 °; in the two above-described first corrugated redistribution boards 14 adjacent to each other in the upper and lower direction, the arrangement directions of the first corrugated redistributors 1403 thereof are staggered by 90 °. The second corrugated redistribution board 16 and the first corrugated redistribution board 14 are manufactured from S31008 high temperature resistant stainless steel material.
Referring to fig. 15, the following geometric relationship is preferably satisfied at the fold surface of the first and second corrugated sheets 16031, 16032:
The calculation formula of the surface-to-surface crease length L is as follows:
The calculation formula of the single piece width x of the folding surface is as follows: x= Lsin (+_a1).
The calculation formula of the single sheet height H of the folding surface is as follows: h= Lsin (+_a3).
The calculation formula of the relative single piece width of the folding surface is as follows:
the calculation formula of the relative monolithic height of the folding surface is as follows:
The heat exchange tube system 8 comprises a cooling liquid inlet 801, an inlet annular distribution tube 802, a lower heat compensation tube 803, a heat exchange vertical tube 804, an upper heat compensation tube 805, an outlet annular distribution tube 806 and a cooling liquid outlet 807; the heat exchange risers 804 are vertically and uniformly arranged in the inner shell 10 and penetrate through the through holes 141 reserved on the first corrugated redistribution plates 14, one ends of the lower heat compensation pipes 803 are correspondingly communicated with the lower ends of the heat exchange risers 804 respectively, and one ends of the upper heat compensation pipes 805 are correspondingly communicated with the upper ends of the heat exchange risers 804 respectively; the other ends of the plurality of lower thermal compensation pipes 803 are respectively communicated with an inlet annular distribution pipe 802, and a cooling liquid inlet 801 is arranged on the inlet annular distribution pipe 802; the other ends of the upper heat compensation pipes 805 are respectively communicated with an outlet annular distribution pipe 806, and the outlet annular distribution pipe 806 is provided with a cooling liquid outlet 807; the inlet annular distribution pipe 802 and the outlet annular distribution pipe 806 are respectively of annular structure and fixedly arranged on the outer wall of the pressure-bearing shell 9 through a distribution pipe fixing plate 808, and a plurality of lower thermal compensation pipes 803 and a plurality of upper thermal compensation pipes 805 penetrate through the main shell.
The detachable air inlet pipe 1 comprises an air inlet pipe 103 and an umbrella hat distributor 105; the air inlet pipe 103 penetrates through the air inlet 2, one end of the air inlet pipe 103 is positioned in the lower sealing head 3, and the umbrella cap distributor 105 is arranged at one end of the air inlet pipe 103 through three rib plates 104 which are circumferentially and equidistantly arranged and positioned in the lower sealing head 3; the middle part of the air inlet pipe 103 is matched and installed with the preassembled flange on the air inlet 2 through the installation fixing flange 102, and the other end of the air inlet pipe 103 is positioned outside the reactor main body and externally connected with an air supply pipe through the inlet flange 101.
Referring to fig. 1 to 17, embodiment 2:
The high-temperature pressurized fluidized bed reactor without dilute phase zone is used for producing 10 ten thousand tons of polysilicon products per set of annual production, adopts a hydrogenation process, and has the following principle: raw materials such as hydrogen, silicon powder, silicon tetrachloride and the like produce trichlorosilane under the conditions of a catalyst and high temperature (550 ℃) and pressure (2.65 MPa).
The high-temperature pressurized fluidized bed reactor without dilute phase zone comprises a detachable air inlet pipe 1, a reactor main body, a composite gas distribution plate 4, a floating nozzle 5, a floating nozzle 6, a solid material inlet 7 and a second fold type redistribution plate 16; an air inlet 2 is formed at the bottom of the reactor main body, and a detachable air inlet pipe 1 is detachably arranged on the air inlet 2 and communicated with the reactor main body; the compound gas distribution plate 4 is arranged at the lower part of the reactor main body, a plurality of floating type nozzles 5 and a plurality of float type nozzles 6 are respectively arranged on the compound gas distribution plate 4 at intervals, and the plurality of float type nozzles 6 are distributed at the outer sides of the plurality of floating type nozzles 5; a pair of solid material inlets 7 are arranged at the lower part of the detachable air inlet pipe 1 and are communicated with the reactor main body, and the solid material inlets 7 are higher than the composite gas distribution plate 4; a plurality of second pleated redistribution plates 16 are respectively arranged in the reactor body at intervals by the redistribution plate brackets 13 and are positioned between the solid material inlet 7 and the gas phase outlet 18 at the top of the reactor body. The upper part of the reactor body is not provided with a dilute phase zone (separation zone).
Since the hydrogenation fluidized bed reactor is a reaction system capable of self-maintaining the reaction temperature, the heat exchange tube system 8 is not provided in this embodiment.
The reactor main body comprises a lower seal head 3, a main shell, an upper seal head 17, a feed back opening 20 and a safety valve port 21; the lower seal head 3 and the upper seal head 17 are respectively connected to the bottom and the top of the main shell to form a closed shell structure of the reactor; the gas phase outlet 18, the feed back opening 20 and the safety valve port 21 are arranged on the upper sealing head 17, and the detachable air inlet pipe 1 is arranged on the lower sealing head 3 through the air inlet 2.
The lower seal head 3, the main shell and the upper seal head 17 are all of a multi-layer structure, and the multi-layer structure comprises a pressure-bearing shell 9, an inner shell 10, an anchor nail 11 and a heat-insulating casting material 12; the inner shell 10 is arranged in the pressure-bearing shell 9, the heat-insulating casting material 12 is filled in a gap between the inner shell 10 and the pressure-bearing shell 9, one end of the anchor nail 11 is fixedly connected with the pressure-bearing shell 9 through welding, and the other end of the anchor nail 11 is anchored in the heat-insulating casting material 12 to form a heat-insulating lining structure; both the composite gas distribution plate 4 and the second corrugated redistribution plate 16 are mounted on the inner wall of the inner shell 10.
The inner shell 10 is made of an N08810 high temperature resistant stainless steel material with a thickness of 8 mm.
The upper seal head 17 is provided with an overhaul port 19, and the main shell is provided with 8 pressure measuring ports 22 at equal intervals along the height direction; the lower part of the main shell is provided with manholes, and the manholes comprise a distribution plate upper manhole 23 positioned above the composite gas distribution plate 4 and a distribution plate lower manhole 24 positioned below the composite gas distribution plate 4; a plurality of ring seats 15 are arranged on the outer wall of the pressure-bearing shell 9 at intervals.
The composite gas distribution plate 4 comprises an inverted conical distribution plate 401 and a spherical crown distribution plate 402; the spherical crown-shaped distribution plate 402 is in a spherical structure, the inverted cone-shaped distribution plate 401 is in an inverted cone-shaped structure with a wide upper part and a narrow lower part, the upper end of the inverted cone-shaped distribution plate 401 is fixedly connected to the inner wall of the inner layer shell 10, and the lower end of the inverted cone-shaped distribution plate 401 is connected with the edge of the spherical crown-shaped distribution plate 402 to form a composite gas distribution plate 4 with a sunken cambered surface structure; nozzle mounting holes 403 are uniformly distributed on the inverted cone-shaped distribution plate 401 and the spherical crown-shaped distribution plate 402, floating nozzles 5 are mounted on the nozzle mounting holes 403 of the spherical crown-shaped distribution plate 402, and floating nozzles 6 are mounted on the nozzle mounting holes 403 of the inverted cone-shaped distribution plate 401.
The composite gas distribution plate 4 is made of an N08810 high-temperature resistant stainless steel material.
The diameter of the edge of the spherical crown-shaped distribution plate 402 is D2, and the top area of the spherical crown-shaped distribution plate 402 is 85% of the cross-sectional area of the inner shell 10; the diameter of the upper end of the inverted cone-shaped distribution plate 401 is consistent with the inner diameter of the inner layer shell 10 and is D1, and the diameter of the lower end of the inverted cone-shaped distribution plate 401 is consistent with the diameter of the edge of the spherical crown-shaped distribution plate 402; the included angle between the plate surface of the inverted cone-shaped distribution plate 401 and the horizontal plane is alpha, and the alpha takes a value of 75 degrees; the aperture of the nozzle mounting holes 403 is d0, d0 takes a value of 36mm, and the center-to-center distance between two adjacent nozzle mounting holes 403 on the same circumference is s, and s takes a value of 150mm.
Each of the floating nozzles 5 includes a first locking member 501, a nozzle tail 502, a nozzle middle 503, and a nozzle head 504; the nozzle tail 502, the nozzle middle 503 and the nozzle head 504 are sequentially and coaxially connected and are internally provided with a central tube 506, the lower end of the central tube 506 penetrates through the nozzle tail 502, and the upper end of the central tube 506 extends into the nozzle head 504; the outer diameter d4 of the nozzle middle part 503 is slightly smaller than the aperture d0 of the nozzle mounting hole 403, and the length of the nozzle middle part 503 is longer than the thickness of the spherical crown-shaped distribution plate 402, so that the nozzle middle part 503 can movably penetrate through the spherical crown-shaped distribution plate 402; the diameters of the first locking piece 501 and the nozzle head 504 are larger than the aperture d0 of the nozzle mounting hole 403, the nozzle tail 502 is mounted on the spherical crown-shaped distribution plate 402 in a limiting mode through the first locking piece 501, and the first locking piece 501 and the nozzle head 504 are located below and above the spherical crown-shaped distribution plate 402 respectively.
An annular gap 505 is formed in the nozzle head 504, one end of the annular gap 505 is communicated with the top of the central tube 506, and the other end of the annular gap 505 penetrates the nozzle head 504 downwards and faces the top surface of the spherical crown-shaped distribution plate 402.
Preferably, the relationship between the inner ring diameter d5 of the annular gap 505 and the outer ring diameter d6 of the annular gap 505 and the diameter d3 of the center tube 506 is: (d 6) 2-(d5)2＝(d3)2.
The floating nozzles 5 are arranged in three circles along the circumferential direction of the spherical crown-shaped distribution plate 402, and the diameters d3 of the central tubes 506 of the three circles of floating nozzles 5 are sequentially increased from inside to outside. The three-turn floating nozzle 5 divides the spherical crown-shaped distribution plate 402 into three concentric circles/rings of equal area.
Each float-type nozzle 6 comprises a second locking piece 601, a nozzle upper section 602, a hollow floating ball 603 and a nozzle lower section 604; the upper nozzle section 602 is coaxially connected with the top of the lower nozzle section 604, the bottom of the lower nozzle section 604 is bent and extended towards the inner wall direction of the inner shell 10, and the bottom of the lower nozzle section 604 penetrates through the nozzle mounting hole 403 and is locked on the inverted cone-shaped distribution plate 401 through the second locking piece 601; a hollow cavity 605 with narrow ends and wide middle is formed in the top of the upper nozzle section 602 and the lower nozzle section 604, and a hollow floating ball 603 is floatably arranged in the wide part of the hollow cavity 605, and the narrow ends of the hollow cavity 605 respectively penetrate through the upper nozzle section 602 and the lower nozzle section 604.
The relationship between the inner diameter d11 and the outer diameter d10 of the hollow floating ball 603 is: d11/d10=0.9, and the outer diameter d10 of the hollow float 603 is smaller than the wide diameter d9 of the cavity 605. The hollow floating ball 603 can be made of an N08810 high-temperature resistant stainless steel material.
The top narrow diameter d12 and the bottom narrow diameter d7 of the cavity 605 are smaller than the wide diameter d9; the bottom of the lower nozzle section 604 vertically penetrates through the inverted cone-shaped distribution plate 401, and the included angle between the top central line and the bottom central line of the lower nozzle section 604, namely the bottom bending angle of the lower nozzle section 604, is 180 degrees to alpha, and the alpha takes a value of 75 degrees.
The bottom of the lower nozzle section 604 is provided with external threads, and the second locking member 601 is screwed and locked on the bottom of the lower nozzle section 604 by adopting a nut matched with the bottom of the lower nozzle section 604.
The float-type nozzles 6 are arranged in a plurality of circles along the annular direction of the inverted cone-shaped distribution plate 401 from inside to outside, and the diameters d12 of the narrow parts at the top of the cavity 605 of the float-type nozzles 6 in the plurality of circles are sequentially increased from inside to outside; when the float-type nozzle 6 and the float-type nozzle 5 were selected, the air velocity of the float-type nozzle 6 was 15% higher than that of the float-type nozzle 5.
The second pleated redistribution plates 16 are arranged in the area between the solid material inlet 7 and the gas phase outlet 18.
Each of the second pleated redistribution plates 16 includes a support gauntlet 1601, a short cylindrical section 1602 and a second pleated redistributor 1603; a plurality of support gauntlets 1601 are arranged in the short cylinder section 1602 at intervals, and a second corrugated redistributor 1603 is embedded in the short cylinder section 1602 and is placed on the plurality of support gauntlets 1601; the short cylinder segments 1602 are mounted on the inner wall of the inner housing 10 by redistribution board brackets 13.
The support calandria 1601 can be made of high temperature resistant stainless steel pipe, and two ends are welded and fixed with the inner wall of the short cylinder section 1602, and a plurality of support calandria 1601 are arranged in parallel and equidistant. The edge of the second corrugated redistributor 1603 is welded and fixed to the inner wall of the short cylinder section 1602, and a plurality of support gauntlets 1601 are used for supporting and mounting the second corrugated redistributor 1603.
The second corrugated redistributor 1603 includes a first corrugated sheet 16031 and a second corrugated sheet 16032, the first corrugated sheet 16031 and the second corrugated sheet 16032 being staggered in opposite oblique directions.
The first corrugated sheet 16031 and the second corrugated sheet 16032 are each a fold-line-shaped sheet-like structure formed of a high temperature resistant stainless steel metal. The folded portions of the adjacent first and second corrugated sheets 16031, 16032 are joined, and a plurality of quadrangular through grooves are formed between the adjacent first and second corrugated sheets 16031, 16032 for allowing the flow of air therethrough. Because the first corrugated single sheets 16031 and the second corrugated single sheets 16032 are oppositely and obliquely staggered, the air flow directions on two adjacent rows of quadrilateral through grooves are different, and the effect of uniform air flow is achieved.
In the two above-described second corrugated redistribution boards 16 adjacent to each other in the upper and lower direction, the arrangement directions of the second corrugated redistributors 1603 thereof are staggered by 90 °. The second corrugated redistribution board 16 is fabricated from N08810 high temperature resistant stainless steel material.
Referring to fig. 15, the following geometric relationship is preferably satisfied at the fold surface of the first and second corrugated sheets 16031, 16032:
The calculation formula of the surface-to-surface crease length L is as follows:
The calculation formula of the single piece width x of the folding surface is as follows: x= Lsin (+_a1).
The calculation formula of the single sheet height H of the folding surface is as follows: h= Lsin (+_a3).
The calculation formula of the relative single piece width of the folding surface is as follows:
the calculation formula of the relative monolithic height of the folding surface is as follows:
The detachable air inlet pipe 1 comprises an air inlet pipe 103 and an umbrella hat distributor 105; the air inlet pipe 103 penetrates through the air inlet 2, one end of the air inlet pipe 103 is positioned in the lower sealing head 3, and the umbrella cap distributor 105 is arranged at one end of the air inlet pipe 103 through three rib plates 104 which are circumferentially and equidistantly arranged and positioned in the lower sealing head 3; the middle part of the air inlet pipe 103 is matched and installed with the preassembled flange on the air inlet 2 through the installation fixing flange 102, and the other end of the air inlet pipe 103 is positioned outside the reactor main body and externally connected with an air supply pipe through the inlet flange 101.
The foregoing description of the preferred embodiments of the utility model is not intended to limit the scope of the utility model, and therefore, any modifications, equivalents, improvements, etc. that fall within the spirit and principles of the utility model are intended to be included within the scope of the utility model.
Claims (10)
1. A high-temperature pressurized fluidized bed reactor without a dilute phase zone is characterized in that: comprises a detachable air inlet pipe (1), a reactor main body, a composite gas distribution plate (4), a floating nozzle (5), a float nozzle (6), a solid material inlet (7) and a second fold type redistribution plate (16); an air inlet (2) is formed at the bottom of the reactor main body, and a detachable air inlet pipe (1) is detachably arranged on the air inlet (2) and is communicated with the reactor main body; the composite gas distribution plate (4) is arranged at the lower part of the reactor main body, a plurality of floating type nozzles (5) and a plurality of float type nozzles (6) are respectively arranged on the composite gas distribution plate (4) at intervals, and the plurality of float type nozzles (6) are distributed at the outer sides of the plurality of floating type nozzles (5); the solid material inlets (7) are arranged at the lower part of the detachable air inlet pipe (1) in pairs and are communicated with the reactor main body, and the solid material inlets (7) are higher than the composite gas distribution plate (4); a plurality of second fold type redistribution plates (16) are respectively arranged in the reactor body at intervals and are positioned between the solid material inlet (7) and the gas phase outlet (18) at the top of the reactor body.
2. The freeboard zone high temperature pressurized fluidized bed reactor of claim 1, wherein: the reactor main body comprises a lower seal head (3), a main shell, an upper seal head (17), a feed back opening (20) and a safety valve port (21); the lower seal head (3) and the upper seal head (17) are respectively connected to the bottom and the top of the main shell to form a closed shell structure of the reactor; the gas phase outlet (18), the feed back opening (20) and the safety valve port (21) are arranged on the upper sealing head (17), and the detachable air inlet pipe (1) is arranged on the lower sealing head (3) through the air inlet (2);
The lower seal head (3), the main shell and the upper seal head (17) are all of a multi-layer structure, and the multi-layer structure comprises a pressure-bearing shell (9), an inner shell (10), an anchor nail (11) and a heat-insulating casting material (12); the inner shell (10) is arranged in the pressure-bearing shell (9), the heat-insulating casting material (12) is filled in a gap between the inner shell (10) and the pressure-bearing shell (9), one end of the anchor nail (11) is fixedly connected with the pressure-bearing shell (9), and the other end of the anchor nail (11) is anchored in the heat-insulating casting material (12) to form a heat-insulating lining structure; the composite gas distribution plate (4) and the second fold type redistribution plate (16) are both arranged on the inner wall of the inner shell (10), and the heat exchange tube system (8) is arranged on the main shell;
an overhaul port (19) is arranged on the upper seal head (17), and a plurality of pressure measuring ports (22) are arranged on the main shell at intervals; the lower part of the main shell is provided with a manhole, and the manhole comprises a distribution plate upper manhole (23) positioned above the composite gas distribution plate (4) and a distribution plate lower manhole (24) positioned below the composite gas distribution plate (4); a plurality of ring seats (15) are arranged on the outer wall of the pressure-bearing shell (9) at intervals.
3. The freeboard zone high temperature pressurized fluidized bed reactor of claim 2, wherein: the composite gas distribution plate (4) comprises an inverted conical distribution plate (401) and a spherical crown distribution plate (402); the spherical crown-shaped distribution plate (402) is in a spherical structure, the inverted cone-shaped distribution plate (401) is in an inverted cone-shaped structure with a wide upper part and a narrow lower part, the upper end of the inverted cone-shaped distribution plate (401) is fixedly connected to the inner wall of the inner shell (10), and the lower end of the inverted cone-shaped distribution plate (401) is connected with the edge of the spherical crown-shaped distribution plate (402) to form a composite gas distribution plate (4) with a sunken cambered surface structure; nozzle mounting holes (403) are uniformly distributed on the inverted cone-shaped distribution plate (401) and the spherical crown-shaped distribution plate (402), floating nozzles (5) are mounted on the nozzle mounting holes (403) of the spherical crown-shaped distribution plate (402), and floating nozzles (6) are mounted on the nozzle mounting holes (403) of the inverted cone-shaped distribution plate (401).
4. A freeboard zone high temperature pressurized fluidized bed reactor according to claim 3, characterized by: each floating nozzle (5) comprises a first locking piece (501), a nozzle tail (502), a nozzle middle (503) and a nozzle head (504); the nozzle tail (502), the nozzle middle (503) and the nozzle head (504) are sequentially and coaxially connected, a central tube (506) is arranged in the nozzle tail, the lower end of the central tube (506) penetrates through the nozzle tail (502), and the upper end of the central tube (506) extends into the nozzle head (504); the outer diameter of the middle part (503) of the nozzle is smaller than the aperture of the nozzle mounting hole (403), and the length of the middle part (503) of the nozzle is larger than the thickness of the spherical crown-shaped distribution plate (402), so that the middle part (503) of the nozzle can movably penetrate through the spherical crown-shaped distribution plate (402); the diameters of the first locking piece (501) and the nozzle head (504) are larger than those of the nozzle mounting hole (403), the nozzle tail (502) is mounted on the spherical crown-shaped distribution plate (402) in a limiting manner through the first locking piece (501), and the first locking piece (501) and the nozzle head (504) are respectively positioned below and above the spherical crown-shaped distribution plate (402);
An annular gap (505) is formed in the nozzle head (504), one end of the annular gap (505) is communicated with the top of the central tube (506), and the other end of the annular gap (505) downwards penetrates through the nozzle head (504) and faces the top surface of the spherical crown-shaped distribution plate (402).
5. A freeboard zone high temperature pressurized fluidized bed reactor according to claim 3, characterized by: each float type nozzle (6) comprises a second locking piece (601), a nozzle upper section (602), a hollow floating ball (603) and a nozzle lower section (604); the upper section (602) of the nozzle is coaxially connected with the top of the lower section (604), the bottom of the lower section (604) of the nozzle is bent and extended towards the inner wall direction of the inner shell (10), and the bottom of the lower section (604) of the nozzle vertically penetrates through the nozzle mounting hole (403) and is locked on the inverted cone-shaped distribution plate (401) through the second locking piece (601); a hollow cavity (605) with narrow two ends and wide middle is formed in the top of the upper nozzle section (602) and the lower nozzle section (604), a hollow floating ball (603) can be arranged in the wide part of the hollow cavity (605) in a floating mode, and the narrow two ends of the hollow cavity (605) respectively penetrate through the upper nozzle section (602) and the lower nozzle section (604).
6. A freeboard zone high temperature pressurized fluidized bed reactor according to claim 3, characterized by: the floating nozzles (5) are arranged in a plurality of circles along the circumferential direction of the spherical crown-shaped distribution plate (402), and the diameters of the central tubes (506) of the floating nozzles (5) are sequentially increased from inside to outside; the multi-ring floating nozzle (5) divides the spherical crown-shaped distribution plate (402) into three concentric circles/rings with equal areas; the float-type nozzles (6) are arranged in a plurality of circles along the annular direction of the inverted cone-shaped distribution plate (401), and the diameters of the narrow parts at the top of the cavities (605) of the float-type nozzles (6) in the plurality of circles are sequentially increased from inside to outside; the multi-turn float-type nozzle (6) divides the inverted cone-shaped distribution plate (401) into three concentric circles/rings with equal areas; the float type nozzle (6) has a higher air velocity than the float type nozzle (5).
7. The freeboard zone high temperature pressurized fluidized bed reactor of claim 2, wherein: a heat exchange tube system (8) is arranged in the reactor main body, a plurality of first fold type redistribution plates (14) are arranged at intervals in the installation height range of the heat exchange tube system (8), and the heat exchange tube system (8) penetrates through holes (141) in the plurality of first fold type redistribution plates (14); the first corrugated redistribution board (14) is identical in structure to the second corrugated redistribution board (16).
8. The freeboard zone high temperature pressurized fluidized bed reactor of claim 7, wherein: each second corrugated redistribution board (16) comprises a support gauntlet (1601), a short cylindrical section (1602) and a second corrugated redistributor (1603); the plurality of support gauntlets (1601) are arranged in the short cylinder section (1602) at intervals, and the second corrugated redistributors (1603) are embedded in the short cylinder section (1602) and are placed on the plurality of support gauntlets (1601); the short cylinder sections (1602) are arranged on the inner wall of the inner shell (10) through redistribution board brackets (13);
The second corrugated redistributor (1603) comprises a first corrugated sheet (16031) and a second corrugated sheet (16032), the first corrugated sheet (16031) and the second corrugated sheet (16032) being staggered in opposite oblique directions;
In the two adjacent second fold type redistribution plates (16), the arrangement directions of the second fold type redistributors (1603) are staggered by 90 degrees; in two first corrugated redistribution plates (14) adjacent to each other in the upper and lower direction, the arrangement directions of the first corrugated redistributors (1403) thereof are staggered by 90 °.
9. The freeboard zone high temperature pressurized fluidized bed reactor of claim 2, wherein: the heat exchange pipe system (8) comprises a cooling liquid inlet (801), an inlet annular distributing pipe (802), a lower heat compensating pipe (803), a heat exchange vertical pipe (804), an upper heat compensating pipe (805), an outlet annular distributing pipe (806) and a cooling liquid outlet (807); the plurality of heat exchange vertical pipes (804) are vertically and uniformly arranged in the inner shell (10) and penetrate through the plurality of first corrugated redistribution plates (14), one ends of the plurality of lower heat compensation pipes (803) are respectively and correspondingly communicated with the lower ends of the plurality of heat exchange vertical pipes (804), and one ends of the plurality of upper heat compensation pipes (805) are respectively and correspondingly communicated with the upper ends of the plurality of heat exchange vertical pipes (804); the other ends of the plurality of lower heat compensation pipes (803) are respectively communicated with an inlet annular distribution pipe (802), and a cooling liquid inlet (801) is arranged on the inlet annular distribution pipe (802); the other ends of the upper heat compensation pipes (805) are respectively communicated with an outlet annular distribution pipe (806), and a cooling liquid outlet (807) is arranged on the outlet annular distribution pipe (806); the inlet annular distributing pipe (802) and the outlet annular distributing pipe (806) are respectively of annular structures and are fixedly arranged on the outer wall of the pressure-bearing shell (9), and a plurality of lower thermal compensation pipes (803) and a plurality of upper thermal compensation pipes (805) penetrate through the main shell.
10. The freeboard zone high temperature pressurized fluidized bed reactor of claim 2, wherein: the detachable air inlet pipe (1) comprises an air inlet pipe (103) and an umbrella cap distributor (105); the air inlet pipe (103) penetrates through the air inlet (2), one end of the air inlet pipe (103) is positioned in the lower sealing head (3), and the umbrella cap distributor (105) is arranged at one end of the air inlet pipe (103) and positioned in the lower sealing head (3); the middle part of the air inlet pipe (103) is matched with the air inlet (2), and the other end of the air inlet pipe (103) is positioned outside the reactor main body and externally connected with an air supply pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322899246.4U CN221085574U (en) | 2023-10-27 | 2023-10-27 | High-temperature pressurized fluidized bed reactor without dilute phase zone |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322899246.4U CN221085574U (en) | 2023-10-27 | 2023-10-27 | High-temperature pressurized fluidized bed reactor without dilute phase zone |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN221085574U true CN221085574U (en) | 2024-06-07 |
Family
ID=91308583
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322899246.4U Active CN221085574U (en) | 2023-10-27 | 2023-10-27 | High-temperature pressurized fluidized bed reactor without dilute phase zone |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN221085574U (en) |
-
2023
- 2023-10-27 CN CN202322899246.4U patent/CN221085574U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2020143140A1 (en) | Separation system for slurry bed reactor | |
| CN101391198B (en) | Slurry bed ft synthetic reactor and technique | |
| CN107281981B (en) | Inner member, fluidized bed reactor and application method | |
| WO2018076962A1 (en) | Internal loop reactor having both reaction and separation functions | |
| CN109282679B (en) | Fluidized bed external heat collector reinforced by baffle plate | |
| CN105080433B (en) | A kind of New-type plate axial flow reactor | |
| CN1094781C (en) | Circulating fluidised bed apparatus for chemical and physical processes | |
| CN106890602A (en) | A kind of gas-solid fluidized bed reactor gas-solid preseparator | |
| CN102336849B (en) | Olefin polymerization reactor | |
| CN221085574U (en) | High-temperature pressurized fluidized bed reactor without dilute phase zone | |
| CN101322924B (en) | Equipment for mixing catalyst | |
| CN206980687U (en) | Chlorination fluidized-bed reactor | |
| CN117244484A (en) | High-temperature pressurized fluidized bed reactor without dilute phase zone | |
| CN113244801A (en) | Multi-fluid mixing equipment | |
| CN209197538U (en) | A kind of fluidized bed external warmer that baffle plate is strengthened | |
| US6467438B1 (en) | Circulating bed reactor | |
| CN202983653U (en) | Fluidized bed reactor for preparing butadiene by oxidizing and dehydrogenizing butene | |
| CN114425283B (en) | Hydrocarbon ammoxidation reaction device, oxygen-containing gas distributor and application thereof | |
| US7901640B2 (en) | Optimized counter-current flow baffle | |
| CN205109603U (en) | Novel fluidized bed reactor | |
| CN112708447B (en) | Riser reactor capable of reducing back mixing of side wall area | |
| CN107551961B (en) | High-temperature high-pressure slurry bed reaction device | |
| CA3027702A1 (en) | System components of fluid catalytic reactor systems | |
| CN109207187A (en) | Solid particle heat collector inlet device | |
| CN114832730B (en) | Fluidized bed reaction device and method for synthesizing organochlorosilane monomer |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |