CN202983653U - Fluidized bed reactor for preparing butadiene by oxidizing and dehydrogenizing butene - Google Patents
Fluidized bed reactor for preparing butadiene by oxidizing and dehydrogenizing butene Download PDFInfo
- Publication number
- CN202983653U CN202983653U CN 201220632592 CN201220632592U CN202983653U CN 202983653 U CN202983653 U CN 202983653U CN 201220632592 CN201220632592 CN 201220632592 CN 201220632592 U CN201220632592 U CN 201220632592U CN 202983653 U CN202983653 U CN 202983653U
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- straight section
- bed reactor
- butadiene
- butene
- fluidized
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Abstract
A fluidized bed reactor for preparing butadiene by oxidizing and dehydrogenizing butene comprises a shell, a gas inlet pipe, a gas outlet, feed ports, discharge ports, a gas distribution plate and manholes. The shell comprises a lower cone base (1), a middle straight section (8) and an upper expanding section (9), the gas inlet pipe (2) and one manhole (7) are arranged in the middle of the cone base (1), the cone base discharge port (19) is arranged at the bottom of the cone base (1), the recessed gas distribution plate (3) is arranged between the cone base (1) and the straight section (8), the straight section discharge ports (17) are arranged on the lower portion of the straight section (8), heat exchange tubes and transverse baffles (16) are arranged in the middle of the straight section (8), the heat exchange tubes are connected with water inlet ring pipes (5) and steam collecting ring pipes (6) outside the shell through heat transfer medium inlets and heat transfer medium outlets, and one manhole (7) and the feed ports (13) are arranged on the upper portion of the straight section (8). The fluidized bed reactor has the advantages of simple structure, low manufacturing cost, convenience in installation and maintenance and applicability to large-scale production.
Description
Technical field
The utility model belongs to a kind of fluidized-bed reactor, especially relates to a kind of fluidized-bed reactor of Oxidative Dehydrogenation of Butene into Butadiene.
Background technology
Butadiene is the simplest conjugated diene, and its structural formula is: CH
2=CH-CH=CH
2, belong to organic compound.Butadiene is a kind of important petrochemicals, is the important monomer of producing synthetic rubber and other high molecular synthetic materials, is also important basic chemical industry raw material.Also be widely used in the production of the synthetic and fine chemicals of engineering plastics and Organic chemical products.
At present, the production method of butadiene mainly contains C-4-fraction partition method and synthetic method (comprising catalytic dehydrogenation and oxidative dehydrogenation).
The C-4-fraction partition method once provided the butadiene supply more than 90%, but there is such problem in this technique: new cracker must be installed, and cost is higher; The cracking reaction energy consumption is excessive; And the independent process of nonproductive butadiene.Along with the swift and violent increase of butadiene demand, partition method can not be satisfied the demand.The catalytic dehydrogenation method is a kind of independent process of producing butadiene, but there are problems in this method: reaction conversion ratio is subject to Equilibrium limit and is lower; Energy consumption is high and steam consumption is large; Cracking and secondary response problem are serious; Under high temperature, catalyst surface is prone to coke laydown, and this can reduce catalyst activity.So the catalytic dehydrogenation method is not suitable for commercially producing of butadiene.Compare oxidative dehydrogenation method with the obvious advantage with the catalytic dehydrogenation method: in oxidative dehydrogenation, the equilibrium conversion of butylene is in theory near 100%, and this has significantly than catalytic dehydrogenation and improves; Oxidative dehydrogenation is exothermic reaction, need not extra heat supply, has reduced energy consumption; Oxidative dehydrogenation can obtain higher butadiene productive rate at lower temperature, and low temperature and oxygen can effectively suppress the deposition of cracking reaction and catalyst surface coke; Oxidative dehydrogenation has generated water, has reduced the water consumption.
The reactor of Oxidative Dehydrogenation of Butene into Butadiene mainly adopts two kinds of bed types, i.e. fixed bed and fluid bed, and fixed bed can be divided into again calandria type fixed bed two kinds of heat-insulating fixed bed and constant temperature.
Insulation fix bed feeding temperature requires high, and the steam consumption is also larger, and operating condition is harsh, and in reactor, local temperature is high, causes conversion ratio, yield lower, and production cost is too high.The calandria type fixed bed device structure of constant temperature is complicated, and material is had relatively high expectations, and catalyst is coking serious, and pipe easily stops up.In addition, there are many difficulties in fixed bed reactors on engineering is amplified, all be difficult to realize industrialization.The Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor operates in bubbling or turbulence fluidized state, and many advantages are arranged: simple in structure, easy to operate; Fluidisation is stable, and bed voidage is evenly distributed, and gas backmixing is little; Feeding temperature requires low, work simplification; Gas-solid heat transfer, mass transfer rate are high, and reactor temperature is evenly distributed; In bed, the heat exchanger tube heat-transfer effect is fine, and the heat exchanger metal consumption is little; Energy consumption, water consume few, and production cost is low; The industry amplification performance is excellent, is suitable for large-scale operation; The loading and unloading of catalyst replenish more convenient.
As fully visible, butylene oxidation-dehydrogenation is the advanced independent process of preparation butadiene, and fluidized-bed reactor is particularly suitable for such process system due to self advantage, therefore fluid bed Oxidative Dehydrogenation of Butene into Butadiene technology is widely applied, and is playing the part of important role in the butadiene industry.
Along with the increase of butadiene demand, its production equipment is also towards large scale development, and existing butadiene fluidized-bed reactor maximum gauge reaches 3.4m.Yet the equipment after amplifying is at present still indiscriminately imitated the structure of early stage mini-plant, and this has brought some new problems to industrial production:
At first, the small-sized fluidized bed reactor adopts flat type gas distribution grid simple in structure, yet in the major diameter fluidized-bed reactor, because the load of catalyst granules is heavier, adopt the flat type distributor unpredictable bend by pressure easily to occur, this stability to bed fluidization quality and fluidized bed process all can produce harmful effect, finally can cause the yield of synthetic reaction to reduce.
Can cause expanding with heat and contract with cold of equipment when secondly, fluctuation occurs Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor operating temperature.Temperature is lower owing to being subject to fluid scouring for distribution grid, may be up to 200 ℃ with the fluid bed cylindrical shell temperature difference, so between distribution grid and reactor shell, thermal stress damage the most easily occurs in connecting portion, and this is even more serious in large scale equipment.The flat type gas distribution grid is limit and can't effectively be absorbed thermal stress due to structure, and reliable thermal compensation can not be provided.Make thermal stress issues more outstanding in large-scale fluidized bed this structure of middle employing, all cause larger hidden danger for equipment and personal safety.
At last, the numerous and complex structure due to the inner member of oxidative dehydrogenation butadiene shelf fluidized bed processed reactor, for the ease of maintenance, the form that existing mini-reactor all adopts flange to connect.Gas distribution grid is clamped on reactor shell by flange plate, takes flange apart and just can carry out the service work of inside reactor.Yet connect at large-scale fluidized bed middle employing flange and can produce problems: flange plate thickness is excessive, and its material, processing, mounting cost significantly improve; The loading and unloading amount of large-sized flange is very large, and during operating cost, this can delay the progress of service work, and impact is normally produced.
Summary of the invention
The purpose of this utility model be propose a kind of simple in structure, cost is low, installation and repairing is convenient, be applicable to the fluidized-bed reactor of large-scale production.
In order to address the above problem, the technical solution adopted in the utility model is as follows:
a kind of fluidized-bed reactor of Oxidative Dehydrogenation of Butene into Butadiene, it is by housing, air inlet pipe, gas vent, charging aperture, discharge port, gas distribution grid and manhole form, housing is bored the end by the bottom, the middle part straight section, the top expanding reach consists of, the middle part at the cone end is provided with air inlet pipe and manhole, cone end discharge port is arranged at the bottom at the cone end, between the cone end and straight section, the up concave type gas distribution grid is arranged, the straight section discharge port is arranged at the straight section bottom, there are heat exchanger tube and transverse baffle in the straight section middle part, heat exchanger tube is connected with the collecting ring pipe with housing water inlet endless tube outward by the import of heat transferring medium and the outlet of heat transferring medium, manhole and charging aperture are arranged at straight section top, cyclone separator is arranged in expanding reach, the expanding reach top is provided with gas vent and hole for hoist.
The action of up concave type gas distribution grid sunken arcs as above is the 80-500 millimeter, and welded and installed is between the cone end and straight section.Have many apertures on the up concave type gas distribution grid, percent opening is 0.5%-5%, and the aperture is the 15-40 millimeter, and installing side-flow type blast cap in aperture is as latasuture formula conical cowl; A dumping pit is also offered at the distribution grid center, and the aperture is the 60-200 millimeter.
Adopt the inverted conical structure at the bottom of cone as above, boring the base angle degree is 45-60 °.
Transverse baffle as above adopts venetian blind type to revolve the deflector apron structure more, can the arranging multiplayer baffle plate along emulsion zone bed height direction, baffle spacing is the 100-400 millimeter, and described baffle plate is assembled by many little plate washer cells, and the cell size is at 300 * 300mm
2To 600 * 600mm
2Between, the oblique sheet thickness of baffle plate δ is the 2-6 millimeter, and tiltedly the sheet inclination angle [theta] is 45-55 °, and tiltedly sheet height h and oblique sheet distance s are the 20-60 millimeter.
Heat exchanger tube is double pipe heat exchanger, and heat exchanger tube can single-stage or multistage layout, and its inner sleeve internal diameter is the 15-50 millimeter, and the outer tube internal diameter is the 60-150 millimeter.
Cyclone separator as above adopts classification series connection, many groups arrangement form in parallel.
Gas distribution grid adopts the up concave type AND DEWATERING FOR ORIFICE STRUCTURE, and its Main Function is supporting catalyst layer, uniform distribution gas and utilizes resistance to keep the stable of fluidized-bed layer; In the middle of the up concave type design makes, the bed of material is thick, and this helps to prevent channel and improves fluidization quality; Concave plate heavy burden ability is strong, the thermal compensation performance is excellent, is suitable for the amplification scale oxidative dehydrogenation fluidized-bed reactor that load is large, thermal stress issues is outstanding; A discharge port is located to have offered in the center of described up concave type gas distribution grid (minimum), in order to be used in conjunction with discharge port on cylindrical shell, realizes complete unloading; Described gas distribution grid directly is welded on the reactor shell wall, the service work of inside reactor equipment is completed by being arranged on the reactor cone end, straight section and expanding reach manhole everywhere, adopt the distribution grid welding to coordinate the scheme of a plurality of manholes to substitute flange clamping scheme in large-scale plant and can guarantee that the normal maintenance of equipment effectively reduces again investment, the mounting cost of equipment, the more important thing is the workload of greatly having reduced maintenance and consuming time.
Described heat exchanger tube is positioned at the emulsion zone of reactor middle part straight section, and the cross section that pipe is covered with reaction bed uniformly evenly distributes to keep bed temperature; The waste heat that cooling medium in heat exchanger is constantly emitted catalytic reaction shifts out, and makes reaction temperature maintain optimum state, and heat exchanger tube can one-level or multistage layout, and they have also played the effect of vertical inner member.
Described baffle plate is that venetian blind type revolves deflector apron more, the baffle plate number of plies depends on the size of emulsion zone height and baffle spacing, the effect of baffle plate be in broken bed air pocket, improve gas-solid contact, improve fluidization quality, reduce the gas axial backmixing, thereby increase reaction rate and improve selective and conversion ratio; Leave certain gap between baffle plate and reactor shell inwall, to promote the inner loop (axial backmixing) of catalyst granules; Whole plate washer is assembled by many little cells, and each cell can carry out independently dismounting operation, and this makes the installation of baffle plate, service work more flexible and convenient.
The effect of described expanding reach is to reduce empty tower gas velocity, facilitates the sedimentation separation of catalyst granules, and the expanding reach size also need satisfy the requirements of installation space of cyclone separator; Described cyclone separator is infundibulate, and it realizes gas solid separation by centrifugal force, and cyclone separator can adopt classification series connection, many groups arrangement form in parallel according to actual needs; Described manhole is done maintenance; Described charging, discharge port are used for loading and unloading and the replacing of catalyst; Described hole for hoist is used for hanging device.
The utility model has the advantage of:
1. gas distribution grid adopts the up concave type design to make the middle bed of material thick, and this helps to prevent channel and improves fluidization quality; Concave plate can be born larger bed layer pressure and is not prone to unpredictable distortion, and this helps to guarantee the stable operation of large-scale reactor and the wherein even distribution of fluid.
2. the radian of up concave type distribution grid bending can effectively absorb thermal stress, has the effect of better thermal compensation, adopts this distribution grid to improve robustness and the security of equipment.
3. adopt the mode of distribution grid welded and installed, manhole maintenance effectively to shorten maintenance workload and the time of large-scale fluidized bed reactor when guaranteeing repair quality.
4. distribution grid adopts the assemble welding mode, compares with the flange clamping, and investment and mounting cost all decrease.
Description of drawings
Fig. 1 is the front view of the utility model transverse baffle.
Fig. 2 is the top view of the utility model transverse baffle.
Fig. 3 is longitudinal sectional view of the present utility model.
In figure: 1 for boring the end; 2 is air inlet pipe; 3 is the up concave type gas distribution grid; 4 is latasuture formula conical cowl; 5 are the water inlet endless tube; 6 is the collecting ring pipe; 7 is manhole; 8 is straight section; 9 is expanding reach; 10 is cyclone separator; 11 is hole for hoist; 12 is gas vent; 13 is charging aperture; 14 is the heat exchanger tube inner sleeve; 15 is the heat exchanger tube outer tube; 16 is transverse baffle; 17 is the straight section discharge port, and 18 is the distribution grid discharge port, and 19 are cone end discharge port, and δ is oblique sheet thickness, and θ is oblique sheet inclination angle, and h is oblique sheet height, and S is oblique sheet spacing.
The specific embodiment
Below in conjunction with accompanying drawing, this paper utility model is further described.
Housing is made of the bottom cone end 1, middle part straight section 8, top expanding reach 9, and the middle part at the cone end 1 is provided with air inlet pipe 2 and manhole 7, and cone end discharge port 19 is arranged at the bottom at the cone end 1, and the inverted conical structure is adopted at the cone end 1, and cone base angle degree is 45 °.Up concave type gas distribution grid 3 welded and installed are between the cone end 1 and straight section 8, the action of its sunken arcs is 80 millimeters, and percent opening is 0.5%, has the aperture on it and be the aperture of 15 millimeters, latasuture formula conical cowl 4 is housed in aperture, and it is the dumping pit 18 of 60 millimeters that an aperture is offered at its center.The heat exchanger tube that straight section 8 bottoms are comprised of inner sleeve 14 and outer tube 15 straight section discharge port 17, middle part, the inner sleeve internal diameter is 15 millimeters, the outer tube internal diameter is 60 millimeters, and inner sleeve 14 is connected with collecting ring pipe 6 with the outer water inlet endless tube 5 of heat transferring medium outlet and housing by the heat transferring medium import respectively with outer tube 15.The transverse baffle 16 at straight section 8 middle parts adopts venetian blind type to revolve the deflector apron structure more, can the arranging multiplayer baffle plate along emulsion zone bed height direction, baffle spacing is 100 millimeters, and baffle plate 16 is assembled by many little plate washer cells, and cell is of a size of 300 * 300mm
2, the oblique sheet thickness of baffle plate δ is 2 millimeters, and tiltedly the sheet inclination angle [theta] is 45 °, and tiltedly sheet height h and oblique sheet distance s are 20 millimeters.Manhole 7 and charging aperture 13 are arranged at straight section 8 tops, and cyclone separator 10 is arranged in expanding reach 9, and cyclone separator 10 adopts the arrangement form of classifications series connection, and expanding reach 9 tops are provided with gas vent 12 and hole for hoist 11.
the butadiene synthetic raw gas enters cone by air inlet pipe 2 to carry out gas in the end 1 and distributes in advance, carry out the gas reallocation by the latasuture formula conical cowl 4 on up concave type gas distribution grid 3 afterwards, equally distributed gas makes catalyst granules reach fluidized state at emulsion zone, gas-solid contact carries out catalytic reaction, gas continues upwards to flow in dense-phase bed, the gap of passing transverse baffle 16 enters dilute-phase zone, the gas of carrying subsequently catalyst granules secretly enters and carries out gas solid separation in cyclone separator 10, purified gas is by gas vent 12 outflow reactor bodies and enter lower procedure.The butadiene synthetic reaction can discharge very large heat, can shift out rapidly unnecessary heat by the heat exchanger tube 14,15 that is arranged in emulsion zone, guarantees that dehydrogenation reaction is under best temperature conditions to carry out.Cooling water is dispensed in inner sleeve 14 through water inlet endless tube 5, then is flowed in outer tube 15 by the bottom opening of inner sleeve 14, absorbs the bed thermal discharge and vaporizes and leave reactor and come together in dry pipe 6 by outer tube 15.Continue heat exchange between the cooling medium that circulates and bed, make bed temperature can maintain under best reaction condition.
The inverted conical structure is adopted at the cone end 1, and boring the base angle degree is 55 °.The action of gas distribution grid 3 sunken arcs is 300 millimeters, and percent opening is 2.5%, has the aperture on it and be the aperture of 30 millimeters, and it is the dumping pit 18 of 150 millimeters that an aperture is offered at the center.Heat exchange inner sleeve 14 internal diameters are 30 millimeters, and outer tube 15 internal diameters are 100 millimeters.Transverse baffle 16 spacings are 250 millimeters, and the baffle plate cell is of a size of 450 * 450mm
2, the oblique sheet thickness of baffle plate δ is 4 millimeters, and tiltedly the sheet inclination angle [theta] is 50 °, and tiltedly sheet height h and oblique sheet distance s are 40 millimeters.Remainder is identical with embodiment 1.
The inverted conical structure is adopted at the cone end 1, and boring the base angle degree is 60 °.The action of gas distribution grid 3 sunken arcs is 500 millimeters, and percent opening is 5%, has the aperture on it and be the aperture of 40 millimeters, and it is the dumping pit 18 of 200 millimeters that an aperture is offered at the center.Heat exchange inner sleeve 14 internal diameters are 50 millimeters, and outer tube 15 internal diameters are 150 millimeters.Transverse baffle 16 spacings are 400 millimeters, and the baffle plate cell is of a size of 600 * 600mm
2, the oblique sheet thickness of baffle plate δ is 6 millimeters, and tiltedly the sheet inclination angle [theta] is 55 °, and tiltedly sheet height h and oblique sheet distance s are 60 millimeters.Remainder is identical with embodiment 1.
Claims (8)
1. Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor, it is by housing, air inlet pipe, gas vent, charging aperture, discharge port, gas distribution grid and manhole form, it is characterized in that housing bores at the end (1) by the bottom, middle part straight section (8), top expanding reach (9) consists of, the middle part of the cone end (1) is provided with air inlet pipe (2) and manhole (7), cone end discharge port (19) is arranged at the bottom of the cone end (1), between the cone end (1) and straight section (8), up concave type gas distribution grid (3) is arranged, straight section discharge port (17) is arranged at straight section (8) bottom, there are heat exchanger tube and transverse baffle (16) in straight section (8) middle part, heat exchanger tube is connected with collecting ring pipe (6) with housing water inlet endless tube (5) outward by the import of heat transferring medium and the outlet of heat transferring medium, manhole (7) and charging aperture (13) are arranged at straight section (8) top, cyclone separator (10) is arranged in expanding reach (9), expanding reach (9) top is provided with gas vent (12) and hole for hoist (11).
2. a kind of Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor as claimed in claim 1, is characterized in that the action of described up concave type gas distribution grid (3) sunken arcs is the 80-500 millimeter.
3. a kind of Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor as claimed in claim 1, is characterized in that described up concave type gas distribution grid (3) has aperture, and percent opening is 0.5%-5%, and the aperture is the 15-40 millimeter.
4. a kind of Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor as claimed in claim 1 is characterized in that described up concave type gas distribution grid (3) aperture installing side-flow type blast cap, and a dumping pit is offered at the distribution grid center, and the aperture is the 60-200 millimeter.
5. a kind of Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor as claimed in claim 1, at the bottom of it is characterized in that described cone, (1) adopts the inverted conical structure, and cone base angle degree is 45-60 °.
6. a kind of Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor as claimed in claim 1, it is characterized in that described transverse baffle (16) adopts venetian blind type to revolve the deflector apron structure more, assembled by many little plate washer cells, baffle spacing is the 100-400 millimeter, and the cell size is at 300 * 300mm
2To 600 * 600mm
2Between, the oblique sheet thickness of baffle plate δ is the 2-6 millimeter, and tiltedly the sheet inclination angle [theta] is 45-55 °, and tiltedly sheet height h and oblique sheet distance s are the 20-60 millimeter.
7. a kind of Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor as claimed in claim 1, it is characterized in that described heat exchanger tube is double pipe heat exchanger, heat exchanger tube can single-stage or multistage layout, and its inner sleeve internal diameter is the 15-50 millimeter, and the outer tube internal diameter is the 60-150 millimeter.
8. a kind of Oxidative Dehydrogenation of Butene into Butadiene fluidized-bed reactor as claimed in claim 1, is characterized in that described cyclone separator (10) adopts classification series connection, many groups arrangement form in parallel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220632592 CN202983653U (en) | 2012-11-27 | 2012-11-27 | Fluidized bed reactor for preparing butadiene by oxidizing and dehydrogenizing butene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220632592 CN202983653U (en) | 2012-11-27 | 2012-11-27 | Fluidized bed reactor for preparing butadiene by oxidizing and dehydrogenizing butene |
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| Publication Number | Publication Date |
|---|---|
| CN202983653U true CN202983653U (en) | 2013-06-12 |
Family
ID=48554879
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220632592 Expired - Lifetime CN202983653U (en) | 2012-11-27 | 2012-11-27 | Fluidized bed reactor for preparing butadiene by oxidizing and dehydrogenizing butene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202983653U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105233766A (en) * | 2015-10-12 | 2016-01-13 | 南京佳业检测工程有限公司 | High-efficiency test reactor |
| CN105841537A (en) * | 2016-05-03 | 2016-08-10 | 华南理工大学 | Intermittent fluidization thermal energy and chemical energy storage and release reaction device and working method |
-
2012
- 2012-11-27 CN CN 201220632592 patent/CN202983653U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105233766A (en) * | 2015-10-12 | 2016-01-13 | 南京佳业检测工程有限公司 | High-efficiency test reactor |
| CN105841537A (en) * | 2016-05-03 | 2016-08-10 | 华南理工大学 | Intermittent fluidization thermal energy and chemical energy storage and release reaction device and working method |
| CN105841537B (en) * | 2016-05-03 | 2019-03-05 | 华南理工大学 | Reaction unit and working method are released in a kind of intermittent fluidization thermal energy and chemical energy storage |
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| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130612 |
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| CX01 | Expiry of patent term |