CN105536654A - Large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene - Google Patents
Large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene Download PDFInfo
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/42—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor
- C07C5/48—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00327—Controlling the temperature by direct heat exchange
Abstract
The invention relates to a large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene. The reactor comprises a reactor housing, a mixing arrangement which is arranged at the upper part of the reactor housing, at least two axial catalyst bed layers in the reactor housing, and at least one direct heat exchange segment; the direct heat exchange segment is located between the two axial catalyst bed layers, a cold torrent is introduced into the direct heat exchange segment in the reactor casing, the cold torrent and outlet materials which are reacted with the axial catalyst bed layer above the direct heat exchange segment are mixed for direct heat exchange, and a mixture enters the axial catalyst bed layer below the direct heat exchange segment for carrying out a reaction. Compared with the prior art, the reactor has the advantages of large-scale, effective control of reaction temperature, reduced bed layer pressure, high energy utilization rate, and good production capacity.
Description
Technical field
The present invention relates to Chemical Reaction Engineering technical field, be specifically related to a kind of large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor.
Background technology
Butadiene is the base stock producing styrene butadiene rubber sbr, ABS resin, polybutadiene rubber BR etc., is also the key intermediate producing the chemicals such as adiponitrile, chlorobutadiene, sulfolane, VCH, of many uses.Butylene oxidation-dehydrogenation is a kind of important method of producing butadiene, and butylene generates butadiene mainly through following main reaction partial oxidation dehydrogenation:
C
4H
8+0.5O
2＝C
4H
6+H
2O
Butylene and butadiene are oxidized further respectively by following side reaction and generate accessory substance CO
2:
C
4H
8+6O
2＝4CO
2+4H
2O
C
4H
6+5.5O
2＝4CO
2+3H
2O
Oxidative Dehydrogenation of Butene into Butadiene is under a large amount of water vapour exists, and butylene carries out dehydrogenation reaction with the oxygen in air under catalyst action, generation butadiene and water.Butylene oxidation-dehydrogenation reaction major influence factors respond temperature, reaction pressure, water alkene ratio, oxygen alkene than etc.Because Oxidative Dehydrogenation of Butene into Butadiene is exothermic reaction, is guard catalyst and controls reaction temperature, need in course of reaction to introduce a large amount of water vapour, slightly high for energy consumption single stage adiabatic formula reactor.Butylene oxidation-dehydrogenation generates butadiene reaction, wherein oxygen alkene ratio is crucial, pulp furnish can not be made to fall in explosion limit, the too high meeting of oxygen content causes the increase of accessory substance carbon dioxide, also easily cause temperature runaway, too low meeting seriously reduces butene conversion, and this reaction is more responsive to pressure ratio in addition, lower pressure is conducive to the raising of butene conversion and butadiene selective, and safety, stable operation are most important under appropriate conditions therefore how to ensure butylene oxidation-dehydrogenation reactor.
It is the consistent butylene oxidation-dehydrogenation fixed bed radial reactor of flow direction in flow manifold and afflux runner that patent CN103721643B discloses a kind of Z-type and reactant gas flow mode, wherein conical baffle is set in flow manifold, inside and outside distributing barrel is high opening rate, cylindrical shell self is not implemented to control to reacting gas, although bed pressure drop is low, but the conical baffle of simple dependence cannot ensure fluid being uniformly distributed in radial reactor inside, and butylene oxidation-dehydrogenation reaction is very high to the uniformity requirement of fluid chemical field, not only relate to the stable of reactor temperature and also have security, this reactor need the checking of commercial Application in the feasibility of butylene oxidation-dehydrogenation reaction system.
Patent CN102442874A discloses a kind of method of constant temperature fixed bed preparing butadiene with butylene oxo-dehydrogenation; adopt tube-shell type fixed bed reactor; wherein loading catalyst in pipe; heat transferring medium is adopted to move heat between pipe; for butylene oxidation-dehydrogenation reaction temperature control out of question; but the scale of this reactor can be restricted, and the pressure drop of tube-shell type fixed bed reactor is large, cannot meet the requirement of larger-scale unit.
Patent CN101367702 discloses a kind of method of preparing butadiene with butylene oxo-dehydrogenation of axially-located bed, its flow process is employing two sections of axial restraint bed bioreactors, butene feedstock, water vapour and air segmenting enter, reactor outlet is cooled by heating steam, next section of reactor is entered after reaching next section of reactor inlet temperature, even but adopt the method small-scale production also to need two reactors, just need multiple stage reactor in parallel as enhanced production capacities, from the viewpoint of equipment investment and floor space all uneconomical.
Patent CN102675027A discloses a kind of preparing butadiene with butylene oxo-dehydrogenation technique, and adopt adiabatic radial fixed-bed by preparing butadiene with butylene oxo-dehydrogenation, radial adiabatic fixed bed forms by three sections, but the unexposed reacting appliance body structure of patent.Patent CN103071429A and CN103071430A discloses a kind of for butylene oxidation-dehydrogenation radial fixed-bed reactor, and it adopts radial adiabatic fixed bed reactors, and catalyst is contained between runner and mass flow pathway.Although adopt radial fixed-bed reactor can reduce bed pressure drop in theory, but in order to ensure reacting gas being uniformly distributed in reactor, the distributor of low percent opening must be adopted, distributor certainly will be caused to produce very large pressure drop, can not well be applicable to butylene oxidation-dehydrogenation reaction system.
At present, industrial Oxidative Dehydrogenation of Butene into Butadiene device generally adopts multiple axial insulation fix bed reactor series connection, although structure of reactor is simple, but separate unit production capacity is limited, and Oxidative Dehydrogenation of Butene into Butadiene system adopt radial reactor carry out industrial production mainly due to uniform fluid distribution problem restriction also have no report, increase to change to adopt the present situation that reactor number of units solves production capacity, the reactor that development of new is easy to maximize is very necessary.
Summary of the invention
Object of the present invention is exactly providing to overcome defect that above-mentioned prior art exists one to be easy to realize to maximize, effectively can control reaction temperature, reducing bed pressure drop, thus obtains that capacity usage ratio is high, large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor that production capacity is large.
Mentality of designing of the present invention is: by investigating the intrinsic of Oxidative Dehydrogenation of Butene into Butadiene and reaction macrokinetics, grasp the reaction rule of this reaction system.Based on its response characteristic, a kind of large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of design: be provided with the inlet gas distributor, adiabatic catalyst bed, cold shock distributor and the beds containing indirect heat exchange that are applicable to major diameter reactor in reactor, distributor pipe containing cold shock nozzle is set in adiabatic catalyst bed lower end, distributor pipe keeps enough distances apart from next beds, for abundant, the Homogeneous phase mixing of gas provide space.Diameter based on reactor is comparatively large, for ensureing fluid being evenly distributed by the cross section of adiabatic catalytic bed being divided into equal-sized square or equilateral triangle with reactor axial parallel baffle plate in radial direction, and along arranging nozzle on baffle plate.Like this by inlet gas distributor and cold shock distributor, blending space, baffle plate guarantee fluid uniformity in this reactor, the temperature of reactor controlled, regulate by the cold shock nozzle and indirect heat exchange being distributed in beds lower end, the use amount reducing water saves energy consumption, make reactor each section of beds reach optimum response operating mode, greatly can improve the separate unit production capacity of the axial restraint bed bioreactor comparatively easily amplified.
Object of the present invention can be achieved through the following technical solutions: a kind of large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor, comprise reactor shell, this reactor shell top arranges mixing arrangement, two axial catalyst beds are at least provided with, at least containing a direct heat transfer section in described reactor shell; Described direct heat transfer section is positioned between two axial catalyst beds, cold shock stream stock passes into the direct heat transfer section in reactor shell, after carrying out mixing direct heat transfer with its upper shaft to the outlet material after catalyst bed reaction, enter axial catalyst bed below it and react.
Described mixing arrangement comprises straight tube or the conically shaped that sidewall is equipped with opposed type nozzle arranged in parallel from top to down, and form blending space, raw material enters mixing arrangement by described opposed type nozzle, fully mixes in blending space;
Import distributor is connected under described mixing arrangement.
Multiple axial catalyst bed parallel arrangement in reactor shell from top to down, the height of each axial catalyst bed is 30 ~ 90cm, and diameter is 750 ~ 1200cm, and at first paragraph axial catalyst bed upper ends porcelain circular layer, porcelain circular layer thickness is 18 ~ 22cm.
Described axial catalyst bed comprises adiabatic catalytic bed or adiabatic catalytic bed and the combination containing indirect heat exchange beds, described adiabatic catalytic bed height is 30 ~ 70cm, catalyst bed layer height containing indirect heat exchange is 50 ~ 90cm, and described direct heat transfer section height is 150 ~ 180cm.
Described adiabatic catalytic bed comprises supporting screening plate, upper edge with the baffle plate of nozzle and crossbeam, Catalyst packing between supporting screening plate and crossbeam, and by baffle plate, catalyst being divided into area equation and the beds of isolating each other, the cross section of this axial catalyst bed is divided into equal-sized square or equilateral triangle.
Described comprises heat exchanger tube, catalyst and heat-exchange system containing indirect heat exchange beds, and heat exchanger tube is arranged with parallel or vertical mode with axial catalyst bed, and lead to cooling medium in heat exchanger tube or fill out catalyst, every root heat exchanger tube is provided with some fins.
Described heat exchanger tube is axial heat exchanger tube or radial heat exchanger tube;
When heat exchanger tube is axial heat exchanger tube, Catalyst packing is in heat exchanger tube, and cooling medium flows outward at heat exchanger tube, forms the heat-exchange system of the outer logical heat transferring medium of pipe; Heat exchanger tube arranged outside three fins of described axially-aligned are mutually 120 ° of settings, and each fin points to the central point of positive triangle or concentric arrays, guarantees the heat transfer effect of axial flow reactor;
When heat exchanger tube is radial heat exchanger tube, Catalyst packing is between heat exchanger tube, cooling medium is at heat exchange Bottomhole pressure, form the heat-exchange system of logical heat transferring medium in pipe, described radial heat exchanger tube arranged outside ring fin, every sheet interval 2 ~ 3cm, each ring fin is parallel to the cross section of heat exchanger tube, guarantees the heat transfer effect of axial flow reactor.
Described cooling medium comprises the one in fused salt, desalted water or conduction oil.
Described direct heat transfer section comprises the space of the horizontal cold shock material distributor pipe with cold shock nozzle, gas distributor, gas uniform mixing, distributed by gas distributor through cold shock nozzle and the outlet material from the axial catalyst bed above direct heat transfer section cold shock stream stock enters the cold shock material distributor pipe in reactor by cold shock material inlet after, enter the space of gas uniform mixing, in this space, hot and cold stream stock directly contacts fully to mix and carries out heat exchange, and the cold shock nozzle pitch on every root cold shock material distributor pipe is 40 ~ 80cm; The cold shock stream stock component of described direct heat transfer section is the mixture of butylene, air and water or butylene and air mixture.
Containing 2 ~ 5 axial catalyst beds in described reactor shell.
Above-mentioned large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor, can one be used alone, conveniently catalyst regeneration does not affect production, can multiple stage parallel connection use, according to integrated artistic requirement, heat exchanger can be set between two large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactors, optimize overall energy consumption.
Compared with prior art, the present invention combines the advantage of axial adiabatic reactor and shell-and-tube reactor, have be easy to realize maximize, effectively can control reaction temperature, bed pressure drop is low, the advantage that capacity usage ratio is high, production capacity is large, beneficial effect is embodied in following several respects:
(1) maximization process units is adapted to, as produced 100000 tons of butadiene product equipments per year, only need a diameter to be about 7.5m, height is about the axial backmixing heat exchange type reactor of 5m, and adopt conventional axial fixed bed reactors about to need 3 ~ 5 cover two-stage series connection reactors, approximately need 6 ~ 10 reactors.
(2) effectively can control reaction temperature, can control reaction temperature by changing the thickness of axial catalyst bed, the temperature of cold shock reaction gas and flow, the temperature of heat transferring medium and flow, general axis is 30 ~ 90cm to catalyst bed layer thickness.
(3) reactor monolith pressure drop is low, and because axial catalyst bed is not thick, reactor diameter is large, and can slightly make up part droop loss by cold shock nozzle, can effectively reduce the bed pressure drop that reactor is total.
(4) capacity usage ratio is high, because direct heat transfer and indirect heat exchange combine, effectively can control each section of reaction bed temperature on the one hand, can reduce the consumption of water on the other hand, save energy consumption.
(5) production capacity is large, adopts major diameter axial backmixing heat exchange type structure of reactor, can effectively improve space reactor utilization rate, improve the loadings of catalyst, improve the production capacity of separate unit reactor.
Accompanying drawing explanation
Fig. 1 is the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor schematic diagram being provided with a direct heat transfer section;
Fig. 2 is that top is provided with a direct heat transfer section, and bottom is provided with the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor schematic diagram that catalyst is loaded on the indirect heat exchange section in pipe;
Fig. 3 is that top is provided with a direct heat transfer section, and bottom is provided with the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor schematic diagram that catalyst is loaded on the indirect heat exchange section between pipe;
Fig. 4 is that top is provided with a direct heat transfer section, and middle part is provided with catalyst and is loaded on indirect heat exchange section in pipe, and bottom arranges the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor schematic diagram of a direct heat transfer section again;
Fig. 5 is that top is provided with a direct heat transfer section, and middle part is provided with catalyst and is loaded on indirect heat exchange section between pipe, and bottom arranges the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor schematic diagram of a direct heat transfer section again;
Fig. 6 is for be disposed with a direct heat transfer section from top to bottom, catalyst is loaded on the indirect heat exchange section between pipe, a direct heat transfer section, a catalyst is loaded on the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor schematic diagram of the indirect heat exchange section between pipe;
Wherein, 1 is air intlet, and 2 is opposed type nozzle, and 3 is Reactor inlet gas distributor, 4 is porcelain circular layer, and 5 is catalyst, and 6 is cold shock material inlet, and 7 is blending space, 8 is a manhole, and 9 is baffle plate, and 10 is supporting screening plate, 11 is cold shock nozzle, and 12 is No. two manholes, and 13 is cooling medium inlet, 14 is No. three manholes, and 15 is reactor outlet, and 16 is cold shock material distributor pipe, 17 is the space that gas uniform mixes, and 18 is heat exchanger tube, and 19 is No. four manholes.
Detailed description of the invention
Elaborate to embodiments of the invention below, the present embodiment is implemented under premised on technical solution of the present invention, give detailed embodiment and concrete operating process, but protection scope of the present invention is not limited to following embodiment.
Embodiment 1
As shown in Figure 1, for there being the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of a direct heat transfer section, this reactor shell top arranges mixing arrangement, is provided with two axial catalyst beds in reactor shell, containing a direct heat transfer section; Described direct heat transfer section is positioned between two axial catalyst beds, cold shock stream stock is passed in reactor shell and is uniformly distributed by gas distributor to the outlet material after catalyst bed reaction through cold shock nozzle and upper shaft after cold shock material distributor pipe, hot and cold stream stock is after the blending space of direct heat transfer section carries out mixing direct heat transfer, enter axial catalyst bed below it to react, the concrete structure of this reactor is as follows:
Described mixing arrangement comprises straight tube or the conically shaped that sidewall is equipped with opposed type nozzle 2 arranged in parallel from top to down, and form blending space 7, reactor head arranges air intlet, is connected with blending space 7; The bottom coupled reaction device inlet gas distributor 3 of blending space 7, air enters blending space 7 by air intlet 1, water vapour and butylene mixing gained raw material spray into blending space 7 by opposed type nozzle 2, the full and uniform mixing of three by Reactor inlet gas distributor 3, enters beds afterwards.
Be provided with two sections of axial catalyst beds in reactor shell, be adiabatic catalyst bed.Adiabatic catalyst bed comprises supporting screening plate 10, upper edge with the baffle plate 9 of nozzle and crossbeam, and catalyst 5 is seated between supporting screening plate 10 and crossbeam, and by baffle plate 9, catalyst 5 is divided into area equation and the beds of isolating each other.The porcelain circular layer 4 of one deck 18cm thickness is covered in addition on the top of first paragraph axial catalyst bed.
A direct heat transfer section is set between two sections of adiabatic catalyst beds, this direct heat transfer section comprises horizontally with the cold shock material distributor pipe 16 of cold shock nozzle 11, gas distributor, the space 17 of gas uniform mixing, cold shock stream stock enters in cold shock material distributor pipe 16 from cold shock material inlet 6, sprayed and the space 17 entering gas uniform from the reacted outlet material of first paragraph axial catalyst bed mix after gas distributor distributes by cold shock nozzle 11, in this space, hot and cold stream stock directly contacts after fully heat exchange is carried out in mixing and enters second segment axial catalyst bed, finally by reactor outlet 15 outflow reactor.
In addition, because this reactor volume is comparatively large, for the ease of maintenance, a manhole 8, No. two manholes 12 and No. three manholes 14 are set respectively in the top of reactor shell, middle part, bottom.
Certain 100,000 tons/year of Oxidative Dehydrogenation of Butene into Butadiene device, reactor adopts the structural shape shown in Fig. 1.Reactor diameter is 7.5m, and upper and lower adiabatic catalyst bed height is 0.5m, and loading catalyst is about 44m altogether
3reactor inlet temperature is 320 DEG C, pressure is 0.14MPa, the outlet temperature of first paragraph beds is about 500 DEG C, guarantee after cold shock that the inlet temperature of second segment beds is in 335 DEG C of situations, the outlet temperature of two sections of beds is about 510 DEG C, and the pressure drop of first paragraph beds is 0.78kPa, and butylene volume space velocity is 185h
-1, two sections of beds pressure drops are 1.66kPa, and butylene volume space velocity is 225h
-1, so large-scale axial backmixing heat exchange type fixed bed reactors can produce butadiene 100,000 tons (calculating by 300 days) per year, and butene conversion is 80%, and butadiene selective is 94%.
Embodiment 2
As shown in Figure 2, for top is provided with a direct heat transfer section, bottom is provided with the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor that catalyst is loaded on the indirect heat exchange section in pipe, adopt the structure similar to embodiment 1, but its second segment axial catalyst bed is the beds containing indirect heat exchange, heat exchanger tube 18 is comprised containing indirect heat exchange beds, catalyst 5 and heat-exchange system, heat exchanger tube 18 and axial catalyst bed are arranged in a vertical manner, wherein Catalyst packing is in heat exchanger tube 18, the outer logical cooling medium of heat exchanger tube 18, form the heat-exchange system of the outer logical heat transferring medium of pipe.
Embodiment 3
As shown in Figure 3, for top is provided with a direct heat transfer section, bottom is provided with the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor that catalyst is loaded on the indirect heat exchange section between pipe, adopt the structure similar to embodiment 1, but second segment axial catalyst bed is the beds containing indirect heat exchange, heat exchanger tube 18 is comprised containing indirect heat exchange beds, catalyst 5 and heat-exchange system, heat exchanger tube 18 and axial catalyst bed are arranged in parallel, wherein Catalyst packing is between heat exchanger tube 18, logical cooling medium in heat exchanger tube 18, form the heat-exchange system of logical heat transferring medium in pipe.
Embodiment 4
As shown in Figure 4, for top is provided with a direct heat transfer section, middle part is provided with catalyst and is loaded on indirect heat exchange section in pipe, bottom arranges the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of a direct heat transfer section again, adopts air intake 1, mixing arrangement, Reactor inlet gas distributor 3, porcelain circular layer 4 and the reactor outlet 15 identical with embodiment 1.
3 sections of axial catalyst beds are provided with in this reactor shell inside, 2 direct heat transfer sections and an indirect heat exchange section, first paragraph and the 3rd section of axial catalyst bed are adiabatic catalyst bed, first direct heat transfer section is arranged on the bottom of first paragraph axial catalyst bed, second direct heat transfer section is arranged on the bottom of second segment axial catalyst bed, direct heat transfer segment structure is identical with embodiment 1, the cold shock nozzle wherein arranged below second segment axial catalyst bed can be selected whether add water and regulate butylene according to actual conditions, air, mol ratio between water, second segment axial catalyst bed is the beds containing indirect heat exchange, heat exchanger tube 18, catalyst 5 and heat-exchange system is comprised containing indirect heat exchange beds, heat exchanger tube 18 and axial catalyst bed are arranged in a vertical manner, wherein Catalyst packing is in heat exchanger tube 18, the outer logical cooling medium of heat exchanger tube 18, forms the heat-exchange system of the outer logical heat transferring medium of pipe.
In addition, because the height of reactor shell increases, in order to the convenience of overhauling, on the basis of embodiment 1, No. four manholes 19, No. four manholes 19 are set at the middle part of reactor shell again and are positioned at below No. two manholes 12.
Embodiment 5
As shown in Figure 5, for top is provided with a direct heat transfer section, middle part is provided with catalyst and is loaded on indirect heat exchange section between pipe, bottom arranges the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of a direct heat transfer section again, adopt the structure similar to embodiment 4, a direct heat transfer section is provided with below first paragraph axial catalyst bed, second segment axial catalyst bed is the beds containing indirect heat exchange, heat exchanger tube 18 is comprised containing indirect heat exchange beds, catalyst 5 and heat-exchange system, heat exchanger tube 18 and axial catalyst bed are arranged in parallel, wherein Catalyst packing is between heat exchanger tube 18, logical cooling medium in heat exchanger tube 18, form the heat-exchange system of logical heat transferring medium in pipe, a direct heat transfer section is set below second segment axial catalyst bed again, the cold shock nozzle wherein arranged below second segment beds can be selected whether add water and regulate butylene according to actual conditions, air, mol ratio between water.Embodiment 6 adopts reactor mutually isostructural with embodiment 2, but some parameters wherein adjust, and adjust as follows:
(1) the porcelain circular layer of 18cm thickness is provided with in the top of first paragraph axial catalyst bed (adiabatic catalyst bed), in order to the distribution of stable material mixed gas;
(2) thickness of adiabatic catalyst bed is 30cm, and the baffle plate axially parallel with reactor is provided with in inside, the cross section of axial catalyst bed is divided into equal-sized equilateral triangle, and along arranging nozzle on baffle plate, the diameter of adiabatic catalyst bed is 750cm;
(3) below adiabatic catalyst bed, arrange direct heat transfer section, direct heat transfer section comprises cold shock material inlet, cold shock material distributor pipe, cold shock nozzle and blending space; Cold shock material distributor pipe is parallel with adiabatic catalyst bed, and is positioned at the lower end of axial catalyst bed; Cold shock material inlet is positioned at the two ends of cold shock material distributor pipe, cold shock nozzle is positioned on cold shock material distributor pipe, spacing between two cold shock nozzles is 40cm, axial Jet with downward flow direction cold shock material, blending space is positioned at the below of described cold shock nozzle, come from the reacted outlet thermal material of adiabatic catalyst bed and after gas distributor distributes, in blending space, fully contact mixing with the cold shock material coming from cold shock nozzle, carry out heat exchange; This direct heat transfer section height is 150cm;
(4) below above-mentioned direct heat transfer section, arrange second segment axial catalyst bed, this axial catalyst bed is the beds containing indirect heat exchange, and it is highly 50cm;
(5) but second segment axial catalyst bed is beds containing indirect heat exchange, indirect heat exchange section is vertical with axial catalyst bed, and wherein Catalyst packing is in heat exchanger tube, and heat exchanger tube leads to cooling medium outward.
Embodiment 7
Adopt reactor mutually isostructural with embodiment 2, but some parameters wherein adjust, adjust as follows:
(1) the porcelain circular layer of 22cm thickness is provided with in the top of first paragraph axial catalyst bed (adiabatic catalyst bed), in order to the distribution of stable material mixed gas;
(2) thickness of adiabatic catalyst bed is 70cm, and the right baffle plate axially parallel with reactor is established in inside, the cross section of axial catalyst bed is divided into equal-sized equilateral triangle, and along arranging nozzle on baffle plate, the diameter of adiabatic catalyst bed is 1200cm;
(3) below adiabatic catalyst bed, arrange direct heat transfer section, direct heat transfer section comprises cold shock material inlet, cold shock material distributor pipe, cold shock nozzle and blending space; Cold shock material distributor pipe is parallel with adiabatic catalyst bed, and is positioned at the lower end of axial catalyst bed; Cold shock material inlet is positioned at the two ends of cold shock material distributor pipe, cold shock nozzle is positioned on cold shock material distributor pipe, spacing between two cold shock nozzles is 80cm, axial Jet with downward flow direction cold shock material, blending space is positioned at the below of described cold shock nozzle, come from the reacted outlet thermal material of adiabatic catalyst bed and after gas distributor distributes, in blending space, fully contact mixing with the cold shock material coming from cold shock nozzle, carry out heat exchange; This direct heat transfer section height is 180cm;
(4) below above-mentioned direct heat transfer section, arrange second segment axial catalyst bed, this axial catalyst bed is the beds containing indirect heat exchange, and it is highly 90cm;
(5) but second segment axial catalyst bed is beds containing indirect heat exchange, indirect heat exchange section is vertical with axial catalyst bed, and wherein Catalyst packing is in heat exchanger tube, and heat exchanger tube leads to cooling medium outward.
Embodiment 8
As shown in Figure 6, be provided with 1 adiabatic catalyst bed from top to bottom respectively, 1 containing indirect heat exchange beds, 1 adiabatic catalyst bed, 1 containing indirect heat exchange beds, the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of 1 adiabatic catalyst bed totally five axial catalyst beds, adopt the structure similar to embodiment 5, a direct heat transfer section is provided with below first paragraph axial catalyst bed, second segment axial catalyst bed is the beds containing indirect heat exchange, heat exchanger tube 18 is comprised containing indirect heat exchange beds, heat exchanger tube 20, catalyst 5 and heat-exchange system, heat exchanger tube 18 and axial catalyst bed are arranged in parallel, wherein Catalyst packing is between heat exchanger tube 18, logical cooling medium in heat exchanger tube 18, form the heat-exchange system of logical heat transferring medium in pipe, unlike, a direct heat transfer section is no longer set below second segment axial catalyst bed, and below the 3rd section of adiabatic catalyst bed, be provided with a direct heat transfer section, the cold shock nozzle wherein arranged below the 3rd section of adiabatic catalyst bed can be selected whether add water and regulate butylene according to actual conditions, air, mol ratio between water.
Claims (11)
1. one kind large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor, comprise reactor shell, this reactor shell top arranges mixing arrangement, it is characterized in that, two axial catalyst beds are at least provided with, at least containing a direct heat transfer section in described reactor shell; Described direct heat transfer section is positioned between two axial catalyst beds, cold shock stream stock passes into the direct heat transfer section in reactor shell, after carrying out mixing direct heat transfer with its upper shaft to the outlet material after catalyst bed reaction, enter axial catalyst bed below it and react.
2. the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of one according to claim 1, it is characterized in that, described mixing arrangement comprises straight tube or the conically shaped that sidewall is equipped with opposed type nozzle (2) arranged in parallel from top to down, form blending space (7), raw material enters mixing arrangement by described opposed type nozzle (2), fully mixing in blending space (7);
Coupled reaction device import distributor (3) under described mixing arrangement.
3. the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of one according to claim 1, it is characterized in that, multiple axial catalyst bed parallel arrangement in reactor shell from top to down, the height of each axial catalyst bed is 30 ~ 90cm, and diameter is 750 ~ 1200cm.
4. the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of the one according to claim 1 or 3, it is characterized in that, described axial catalyst bed comprises adiabatic catalytic bed or adiabatic catalytic bed and the combination containing indirect heat exchange beds, described adiabatic catalytic bed height is 30 ~ 70cm, catalyst bed layer height containing indirect heat exchange is 50 ~ 90cm, and described direct heat transfer section height is 150 ~ 180cm.
5. the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of one according to claim 4, it is characterized in that, described adiabatic catalytic bed comprises supporting screening plate (10), upper edge with the baffle plate (9) of nozzle and crossbeam, catalyst (5) is seated between supporting screening plate (10) and crossbeam, and by baffle plate (9), catalyst (5) is divided into area equation and the beds of isolating each other.
6. the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of one according to claim 4, it is characterized in that, described comprises heat exchanger tube (18), catalyst and heat-exchange system containing indirect heat exchange beds, heat exchanger tube (18) is arranged with parallel or vertical mode with axial catalyst bed, lead to cooling medium in heat exchanger tube (18) or fill out catalyst, every root heat exchanger tube (18) is provided with some fins.
7. the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of one according to claim 6, it is characterized in that, described heat exchanger tube is axial heat exchanger tube or radial heat exchanger tube;
When heat exchanger tube (18) is for axial heat exchanger tube, Catalyst packing is in heat exchanger tube (18), and cooling medium flows outward at heat exchanger tube (18), forms the heat-exchange system of the outer logical heat transferring medium of pipe;
When heat exchanger tube (18) is for radial heat exchanger tube, Catalyst packing is between heat exchanger tube (18), and cooling medium flows in heat exchanger tube (18), forms the heat-exchange system of logical heat transferring medium in pipe.
8. the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of the one according to claim 6 or 7, it is characterized in that, described cooling medium comprises the one in fused salt, desalted water or conduction oil.
9. the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of one according to claim 1, it is characterized in that, described direct heat transfer section comprises horizontally with the cold shock material distributor pipe (16) of cold shock nozzle (11), gas distributor, the space (17) of gas uniform mixing, after cold shock stream stock enters the cold shock material distributor pipe (16) in reactor by cold shock material inlet (6), the space (17) that gas uniform mixes is entered after cold shock nozzle is distributed by gas distributor with the outlet material from the axial catalyst bed above direct heat transfer section, in this space, hot and cold stream stock directly contacts fully to mix and carries out heat exchange.
10. the large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of the one according to claim 1 or 9, is characterized in that, the cold shock stream stock component of described direct heat transfer section is the mixture of butylene, air and water or butylene and air mixture.
The large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor of 11. one according to claim 1, is characterized in that, containing 2 ~ 5 axial catalyst beds in described reactor shell.
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