CN205435687U - Radial fixed bed reactor of indirect heat transfer of multistage - Google Patents
Radial fixed bed reactor of indirect heat transfer of multistage Download PDFInfo
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- CN205435687U CN205435687U CN201521101075.5U CN201521101075U CN205435687U CN 205435687 U CN205435687 U CN 205435687U CN 201521101075 U CN201521101075 U CN 201521101075U CN 205435687 U CN205435687 U CN 205435687U
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- 239000003054 catalyst Substances 0.000 claims abstract description 77
- 238000006243 chemical reaction Methods 0.000 claims abstract description 65
- 238000000034 method Methods 0.000 claims abstract description 23
- 230000008676 import Effects 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 238000009826 distribution Methods 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 4
- 239000004744 fabric Substances 0.000 claims description 4
- 229930195733 hydrocarbon Natural products 0.000 claims description 4
- 150000002430 hydrocarbons Chemical class 0.000 claims description 4
- 239000011229 interlayer Substances 0.000 claims description 2
- 238000003466 welding Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000010276 construction Methods 0.000 abstract description 6
- 238000006555 catalytic reaction Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 17
- 238000002156 mixing Methods 0.000 description 9
- 239000000376 reactant Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 230000035939 shock Effects 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000004320 controlled atmosphere Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—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
- B01J8/0449—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 in two or more cylindrical beds
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a radial fixed bed reactor of indirect heat transfer of multistage, it is used for exothermic chemical reaction, and it includes cylindrical casing, catalytic reaction device, double pipe heat exchanger and establishes the fin on double pipe heat exchanger. In the basis the utility model discloses a reactor's of above -mentioned type regional inlet temperature and the exit temperature of differential response controls in near the limited range predetermined optimum value. The utility model discloses it has such advantage to compare prior art: can use simple means in in a big way stable with catalyst bed temperature control near predetermined optimum value, the catalyst availability factor is high, loads than greatly, loads and unloads easily, simple structure, manufacturing and mounting process require relatively lowly, and capital construction cost and running cost are low, heat energy scatters and disappears for a short time, and utilization coefficient is high.
Description
Technical field
This utility model relates to a kind of Radial Flow fixed bed reactors for heat-producing chemical reaction.Specifically, this utility model relates to the such a Radial Flow fixed bed reactors for heat-producing chemical reaction, it has the cylinder blanket of upper low head, have in described cylinder blanket and be defined at least one or more that device divides there is the catalyst reaction region of reaction-ure inlet and reacting product outlet so that the inlet temperature in differential responses region and outlet temperature control in the limited range near predetermined optimum.
Background technology
Radial fixed-bed reactor has an advantage in that 1, flow area is big, pressure drop is little, can use catalyst particle, thus reaction rate compared with high, to produce intensity big；2, simple in construction, capital expenditure is little；3, air-flow is forced to be uniformly distributed.
In recent years, radial fixed-bed reactor is widely used on commercial plant, but is limited to radial fixed-bed construction features and flow feature, and when it is applied to strong exothermal reaction, radial fixed-bed reactor has clearly disadvantageous.How the reaction heat in radial fixed-bed beds to remove reactor with simple effective method, controls bed temperature near predetermined optimum, those skilled in the relevant art have carried out substantial amounts of work.
Method known to a kind of specialty is to be taken away by the heat of generation by the reaction logistics of flowing in beds, in order to strengthen this effect, needs to increase non-principal reaction component in reaction logistics.It is limited to physical characteristic and the flow feature of radial reactor of described stream stock, in order to reach effectively to control the purpose of bed temperature, the non-principal reaction component increased in reactor stream stock have to reach the biggest amount, and circulate in systems and take away heat, the several times of dominant response component quality to be reached, to decades of times, make the power consumption of circulator in system be greatly increased.
Chinese patent CN10455731A discloses a kind of method reducing circulator energy consumption, adds two kinds for the non-principal reaction components taking away reaction generation heat: dry gas and water in reaction logistics.Dry gas is reaction by-product, and water it is possible to additionally incorporate.After separation circuit, dry gas circulator is delivered to catalytic bed entrance point, with water pump, water is recycled to catalytic bed entrance point simultaneously, and enter reactor bed after mixing with reactant, dry gas after the gasification that again heats up, its essence is the operating power consumption having shared gas circulator with the liquid pump that efficiency is higher, but the increase of moisture in reactant, brings restriction to the application of this method, constantly cooling and the gasification of water also consumes substantial amounts of energy.
Chinese patent CN203916626U, CN203944358U, CN201088911Y and CN203075923U disclose the method laying heat exchange cold management and control reaction bed temperature in radial fixed-bed beds.Control the temperature of beds in this way, the structure complexity of reactor, manufacturing process can be made to require height, improve manufacture difficulty and construction cost, the most also bring the problems such as catalyst loading and unloading is difficult, packing factor is low, especially deteriorate in beds the flow condition reacting logistics, add flow resistance, back mixing and wall effect.Due to the flow feature of radial reactor, using the method laying cold pipe in beds to remove heat, efficiency is the lowest, in order to reach the set goal, need to use special equipment or lay substantial amounts of cold pipe so that the problem thus caused is more serious.
Chinese patent CN201978732U discloses a kind of by beds axial segmentation, at the fixed bed reactors of intersegmental addition cold shock gas control catalyst bed temperature, and it can effectively control the temperature of reactor bed.But in order to make hot and cold stream stock in intersegmental good mixing, must be accorded to the blending space of necessity or corresponding mixing apparatus so that intersegmental space increases, equipment is complicated, if using unstripped gas to implement cold shock, also can cause back mixing, affect the yield of target product and the service efficiency of catalyst.Multistage reactor is controlled to the temperature rise of bed by cold shock controlled atmosphere joint inlet temperature, also have certain limitation, interfere in the distribution existence of imports at different levels mainly due to cold shock gas, it is difficult to ensure that steady operation, the most also have impact on the use in main equipment.
Chinese patent CN101616730B, CN202570121U and CN202570115U are disclosed that a kind of radial fixed-bed reactor controlling temperature in the intersegmental heat exchange of mutil-stage adiabatic reactor.Heat exchanger is the tube bank of the compositions such as light pipe, finned tube, serpentine pipe or shape tube.By tube bank by the heat technologic gas (reactant) flowed out by beds and cold process gas (non-reaction component: the circulating air) heat exchange being introduced into bed, on the one hand cold process gas is warming up to beds import temperature required, on the other hand the process gas of partial reaction is made suitably to lower the temperature, to enter next section of beds continuation reaction.The method effectively make use of the heat energy that reaction produces, but still the problem having that recycle ratio is big, heat exchange efficiency is low etc. and bringing, make that equipment is complicated, processing technology require high, heat exchanger volume is big, Catalyst packing is than the problem such as low, and, restriction due to technique, opereating specification is narrower, and temperature is wayward near predetermined value.
Utility model content
The purpose of this utility model is to provide a kind of multistage indirect heat exchange radial fixed-bed reactor that can catalytic reaction bed temperature controlled in predetermined optimum environs.This multistage indirect heat exchange radial fixed-bed reactor, while possessing bigger production capacity and conversion yield, has that capacity usage ratio is high, easily operated and advantages of simple structure and simple, is particularly suited for the large-scale plant that oxygenatedchemicals is raw material liquid hydrocarbon technique.
According to an aspect of the present utility model, it is provided that a kind of multistage indirect heat exchange radial fixed-bed reactor, it is characterised in that comprising:
Housing, it is cylindrical, the upper low head of described housing, arranges at least one raw material gas inlet and reacting product outlet, heat transferring medium import and heat transferring medium outlet on the housing；
At least one or more catalyst reaction device, it is arranged in described housing, and at least one or more catalyst reaction device described is placed on catalyst reaction device base plate, and catalyst reaction device base plate is connected with housing by welding or alternate manner；At least one or more catalyst reaction device described is made up of catalyst basket and the catalyst being placed in one, and described catalyst basket is Radial Flow structure；
Double pipe heat exchanger, it is arranged on casing center, and its outer tube wall constitutes catalyst basket collection air flue baffle plate and catalyst reaction device inner edge, and described double pipe heat exchanger is made up of bilayer sleeve, and two interlayers leave annular space, forms heat exchanging medium passage；The lower end of described double pipe heat exchanger is provided with heat transferring medium import uniform device and inlet header；The upper end of double pipe heat exchanger is provided with heat transferring medium outlet uniform device and outlet header；Inlet header and outlet header are imported and exported relevant device outer with housing by the heat transferring medium on housing and are connected.
An embodiment according to multistage indirect heat exchange radial fixed-bed reactor of the present utility model, it is characterized in that the outer wall of double pipe heat exchanger is provided with fin, in the range of double pipe heat exchanger and each catalyst basket height quite or slightly extend, described fin is parallel to described double pipe heat exchanger longitudinal center line, and the fin exceeding this scope forms oblique angle with heat exchanger longitudinal center line；Fin surface on double pipe heat exchanger outer wall and outer wall is all made annular knurl and is processed；Annular space sets in double pipe heat exchanger turbolator, in double pipe heat exchanger pipe, sets twisted shape flow deflector or swirl vane.
An embodiment according to multistage indirect heat exchange radial fixed-bed reactor of the present utility model, it is characterised in that described catalyst basket by interior screen cloth, outer screen cloth, interior airflow-distribution board, outer airflow-distribution board, constitute.
An embodiment according to multistage indirect heat exchange radial fixed-bed reactor of the present utility model, it is characterised in that described catalyst basket farther includes gas-distributing channel baffle plate, described gas-distributing channel baffle plate constitutes the outer rim of at least one or more catalyst reaction device described.
An embodiment according to multistage indirect heat exchange radial fixed-bed reactor of the present utility model, it is characterised in that the element that described housing or other airflow-distribution board outer with catalyst basket form annular space constitutes the outer rim of described catalyst basket.
An embodiment according to multistage indirect heat exchange radial fixed-bed reactor of the present utility model, it is characterised in that described catalyst basket is Axial and radial structure so that the reaction logistics flowed wherein does Z-type flowing along the radial direction of reactor.
An embodiment according to multistage indirect heat exchange radial fixed-bed reactor of the present utility model, it is characterised in that the heat transferring medium of circulation is in water or the conduction oil of saturation in described double pipe heat exchanger annular space.
An embodiment according to multistage indirect heat exchange radial fixed-bed reactor of the present utility model, it is characterised in that when reaction process needs environment under high pressure, saturation water is as heat transferring medium.
An embodiment according to multistage indirect heat exchange radial fixed-bed reactor of the present utility model, it is characterised in that when reactor is applied to normal pressure or low pressure process, conduction oil is as heat transferring medium.
According to multistage indirect heat exchange radial fixed-bed reactor of the present utility model be for be raw material liquid hydrocarbon technique with oxygenatedchemicals large-scale plant.
This utility model has the following advantages compared to existing technology:
1, stably reaction bed temperature can be controlled near predetermined optimum in a big way by simple means.
2, catalyst service efficiency is high, and filling ratio is big, and handling are easily.
3, simple in construction, manufactures and mounting process requires relatively low, and capital construction cost and running cost are low.
4, heat energy dissipation is little, and coefficient of heat utilization is high.
Accompanying drawing explanation
Method and apparatus of the present utility model has further feature and advantage, these feature and advantage are by the accompanying drawing included in herein and manifest in being used for explaining the detailed description of the invention of some principle of the present utility model subsequently together with accompanying drawing or illustrate in more detail, in the drawings:
Fig. 1 is according to multistage heat exchange radial fixed-bed reactor schematic diagram of the present utility model；
Fig. 2 is the multistage heat exchange radial fixed-bed reactor schematic diagram according to one embodiment of this utility model；
Fig. 3 is the multistage heat exchange radial fixed-bed reactor schematic diagram according to this utility model another embodiment.
Should be appreciated that, accompanying drawing need not necessarily be drawn to scale, it illustrates in a way through each preferred feature disclosed herein of the present utility model of simplifying, including such as certain size, orientation, position and shape, by partly by the application of specific purpose with use environment to be determined.
Detailed description of the invention
According to multistage indirect heat exchange radial fixed-bed reactor of the present utility model, arranging double pipe heat exchanger in housing on central axis, the outer wall of described double pipe heat exchanger constitutes inner edge and the collection air flue baffle plate of catalyst basket of catalytic reactor device.
Circulate in described double pipe heat exchanger annular space heat transferring medium.Heat transferring medium carries out heat exchange by the outer tube wall of double pipe heat exchanger with the reactant stream flowed out from beds, enters next catalyst reaction device after making reaction logistics cooling.By temperature and the flow of regulation heat transferring medium, the temperature of the reaction logistics entering next catalyst reaction device can be efficiently controlled.Non-principal reactant composition (also referred to as circulating air) the stream stock flowing to mouth introducing from the reactant being arranged on housing through double pipe heat exchanger inner tube passes through inner tubal wall and heat transferring medium heat exchange, makes this stream stock heat up and enters first catalyst reaction device with reacting after logistics mixes.
Described double pipe heat exchanger upper end is provided with heat transferring medium outlet uniform device and outlet header, and lower end is provided with heat transferring medium import uniform device and inlet header.Heat transferring medium outlet uniform device and header make heat transferring medium flow distribution in double pipe heat exchanger uniform, reduce the circumferential non-uniform temperature of double pipe heat exchanger.
The outer tube wall of described double pipe heat exchanger is provided with longitudinal fin, to increase heat exchanger area.It is provided with turbolator, to improve flow regime when heat transferring medium flows in double pipe heat exchanger annular space in the annular space of described double pipe heat exchanger.Double pipe heat exchanger inner tube is provided with double-helix flow deflector or swirl vane, flows the mixing between each component of stock in increasing tube fluid and the heat exchange effect of inner tubal wall and pipe.
Catalyst needed for production scale is placed in one or more catalyst reaction devices, is placed in vertically in housing.Reaction logistics is radially flowed to inner edge by catalyst reaction device outer rim along beds, belongs to radial centripetal flow model.Reaction logistics sequentially passes through each section of catalyst reaction device, in the case of total treating capacity is constant, total reaction heat is undertaken respectively by each catalyst reaction device, for the catalyst amounts needed for total production scale, catalyst amounts in each catalyst reaction device decreases, both increase relative to the mass flowrate in each beds, the heat making beds produce can more effectively be moved out of catalyst reaction equipment, and each catalyst reaction device is centripetal Radial Flow.The heat reacting generation in each catalyst reaction device carried by reactor stream stock, by the catalyst reaction device inner edge being made up of double pipe heat exchanger outer wall, removes outside housing after heat exchange.Reaction stream temperature after heat exchange is reduced near predetermined value, enters next reaction unit and continues reaction, or the reactant flow export outflow reactor on housing.Therefore, integral reactor heat leakage is little, and capacity usage ratio is high, and exotic material consumption is few, and manufacturing cost is relatively low.
The outer tube wall of described double pipe heat exchanger constitutes the collection air flue baffle plate of catalyst basket, in double pipe heat exchanger annular space, flow and the temperature of heat transferring medium can be manufactured at sleeve pipe easily and be regulated by conventional means in the range of material permission, the low temperature-controlled environment of catalyst basket inner edge is constituted with nearest distance, for the heat that beds produces, enhance radiant heat transfer effect, be effectively improved moving the thermal efficiency and improving the temperature controlled ability of reaction logistics entering next catalyst reaction device of beds.
Will be described in the most now each embodiment of the present utility model, the embodiment of described embodiment illustrates and in the accompanying drawings described herein below.Although this utility model combines with exemplary embodiment and is described, it will be understood that this specification is not meant to be limited to this utility model those exemplary embodiments.On the contrary, this utility model is intended to not only cover these exemplary, and covers and can be included in various replacements within the spirit and scope of the present utility model being defined by the appended claims, revise, be equal to and other embodiment.
Embodiment 1
As shown in Figure 2, it is a kind of year according to an embodiment of the present utility model to process oxygen-containing compound material 25,000 ton of multistage heat exchange radial fixed-bed reactor producing liquid hydrocarbon, it includes cylindrical housings 1, housing 1 has upper low head 2,3, upper cover 2 is provided with material inlet 4 and circulating air by-pass import 5, low head 3 is provided with reactant outlet 7, circulating air main line import 6 and heat transferring medium import 9.Additionally, housing 1 can include the conventional plants such as manhole, pressure sensing port, thermocouple string holes.
4 sections of catalyst reaction devices it are provided with, including catalyst basket 13 and catalyst reaction device base plate 15 in housing 1.
Arranging double pipe heat exchanger 12 along axis in housing, the upper and lower side of double-tube heat exchanger is provided with double-tube heat exchanger exit port distributor 8 and exit port header 11.
In the present embodiment, catalyst basket total height 4.8 meters, it is divided into 4 sections, thickness 0.3 meter.Commercially available ZSM-5 catalyst is placed, altogether 8.5m in catalyst basket3。
Above-mentioned multistage heat exchange radial fixed-bed reactor work process is as follows:
Temperature is 120 DEG C-250 DEG C, the unstripped gas of preferably 120 DEG C-150 DEG C, through raw material gas inlet 4 and temperature be 15 DEG C-30 DEG C enter into double-tube heat exchanger 12 and heat exchange wherein is warming up to 200 DEG C-420 DEG C through circulating air import 6, the circulating air mixing of preferably 200 DEG C-300 DEG C, the SAPMAC method gas mixing homoiothermic of 15 DEG C-30 DEG C entered via circulating air by-pass 5 is at 250 DEG C-400 DEG C, catalyst basket 13 is entered after preferably 250 DEG C-300 DEG C, carry out reacted gas heating to 300 DEG C-450 DEG C, preferably 300 DEG C-350 DEG C, this stream plume is cooled to 280 DEG C-400 DEG C after going out catalyst basket after double-tube heat exchanger outer wall heat exchange, after preferably 280 DEG C-320 DEG C, enter next catalyst basket.Until after passing sequentially through the gentle heat exchange cooling of the reacted liter of all of catalyst basket, reacting product outlet 7 flowing out housing.
Embodiment 2
As it is shown on figure 3, its be according to another embodiment of the present utility model for be raw material production gasoline with oxygenatedchemicals multistage heat exchange radial fixed-bed reactor.
The present embodiment is identical with embodiment 1 structure, but has 5 catalyst reaction devices axially disposed in housing.The total height of 4 catalyst baskets is 4.8 meters above, thick 0.3 meter.Load commercially available ZSM-5 catalyst total amount 8.5m3.Nethermost catalyst basket is high 2.4 meters, thick 0.4 meter, fills modified ZSM-5 catalyst total amount 9.6m3。
Work process is same as in Example 1.
As the oxygenatedchemicals of raw material in the various embodiments described above, can be methanol, ethanol, dimethyl ether etc., and they mixture or with other C1-C8Hydro carbons and the mixture of water.
Claims (10)
1. a multistage indirect heat exchange radial fixed-bed reactor, it is characterised in that comprising:
Housing, it is cylindrical, the upper low head of described housing, arranges at least one raw material gas inlet and reacting product outlet, heat transferring medium import and heat transferring medium outlet on the housing；
At least one or more catalyst reaction device, it is arranged in described housing, and at least one or more catalyst reaction device described is placed on catalyst reaction device base plate, and catalyst reaction device base plate is connected with housing by welding or alternate manner；At least one or more catalyst reaction device described is made up of catalyst basket and the catalyst being placed in one, and described catalyst basket is Radial Flow structure；
Double pipe heat exchanger, it is arranged on casing center, and its outer tube wall constitutes catalyst basket collection air flue baffle plate and catalyst reaction device inner edge, and described double pipe heat exchanger is made up of bilayer sleeve, and two interlayers leave annular space, forms heat exchanging medium passage；The lower end of described double pipe heat exchanger is provided with heat transferring medium import uniform device and inlet header；The upper end of double pipe heat exchanger is provided with heat transferring medium outlet uniform device and outlet header；Inlet header and outlet header are imported and exported relevant device outer with housing by the heat transferring medium on housing and are connected.
Multistage indirect heat exchange radial fixed-bed reactor the most according to claim 1, it is characterized in that the outer wall of double pipe heat exchanger is provided with fin, in the range of double pipe heat exchanger and each catalyst basket height quite or slightly extend, described fin is parallel to described double pipe heat exchanger longitudinal center line, and the fin exceeding this scope forms oblique angle with heat exchanger longitudinal center line；Fin surface on double pipe heat exchanger outer wall and outer wall is all made annular knurl and is processed；Annular space sets in double pipe heat exchanger turbolator, in double pipe heat exchanger pipe, sets twisted shape flow deflector or swirl vane.
Multistage indirect heat exchange radial fixed-bed reactor the most according to claim 1, it is characterised in that described catalyst basket by interior screen cloth, outer screen cloth, interior airflow-distribution board, outer airflow-distribution board, constitute.
Multistage indirect heat exchange radial fixed-bed reactor the most according to claim 1, it is characterised in that described catalyst basket farther includes gas-distributing channel baffle plate, described gas-distributing channel baffle plate constitutes the outer rim of at least one or more catalyst reaction device described.
Multistage indirect heat exchange radial fixed-bed reactor the most according to claim 3, it is characterised in that the element that described housing or other airflow-distribution board outer with catalyst basket form annular space constitutes the outer rim of described catalyst basket.
Multistage indirect heat exchange radial fixed-bed reactor the most according to claim 3, it is characterised in that described catalyst basket is Axial and radial structure so that the reaction logistics flowed wherein does Z-type flowing along the radial direction of reactor.
Multistage indirect heat exchange radial fixed-bed reactor the most according to claim 3, it is characterised in that the heat transferring medium of circulation is in water or the conduction oil of saturation in described double pipe heat exchanger annular space.
Multistage indirect heat exchange radial fixed-bed reactor the most according to claim 7, it is characterised in that when reaction process needs environment under high pressure, saturation water is as heat transferring medium.
Multistage indirect heat exchange radial fixed-bed reactor the most according to claim 7, it is characterised in that when reactor is applied to normal pressure or low pressure process, conduction oil is as heat transferring medium.
Multistage indirect heat exchange radial fixed-bed reactor the most according to claim 1 be for be raw material liquid hydrocarbon technique with oxygenatedchemicals large-scale plant.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2015105483811 | 2015-08-31 | ||
| CN201510548381 | 2015-08-31 |
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| CN205435687U true CN205435687U (en) | 2016-08-10 |
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| CN201510993799.3A Expired - Fee Related CN105457564B (en) | 2015-08-31 | 2015-12-25 | Multistage indirect heat exchange radial fixed-bed reactor |
| CN201521101075.5U Expired - Fee Related CN205435687U (en) | 2015-08-31 | 2015-12-25 | Radial fixed bed reactor of indirect heat transfer of multistage |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105457564A (en) * | 2015-08-31 | 2016-04-06 | 张淮海 | Multi-section indirect heat exchange type radial fixed bed reactor |
| CN118949859A (en) * | 2024-10-09 | 2024-11-15 | 浙江长城搅拌设备股份有限公司 | Reactor with catalyst turbulence temperature control structure |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105925301B (en) * | 2016-07-08 | 2017-07-04 | 鲁盈 | Combination cot preparing gasoline by methanol technique |
| CN106831306B (en) * | 2017-01-05 | 2020-01-14 | 中石化上海工程有限公司 | Reaction process for preparing ethylene by oxidative coupling of methane |
| CN114570289B (en) * | 2020-12-01 | 2023-04-07 | 中国科学院大连化学物理研究所 | Fixed bed catalytic reactor and application thereof in removal of hydrazine nitrate and hydroxylamine nitrate |
| CN116037004A (en) * | 2023-02-08 | 2023-05-02 | 重庆双象电子材料有限公司 | Radial catalyst bed |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2243938Y (en) * | 1995-07-12 | 1997-01-01 | 孔繁修 | Multi-layer radial synthetic reactor |
| CN201664604U (en) * | 2009-08-20 | 2010-12-08 | 上海国际化建工程咨询公司 | Built-in cold-wall shift reactor of heat exchanger |
| CN102029129B (en) * | 2009-09-25 | 2013-01-23 | 华东理工大学 | Axial-radial flow gas-solid phase fixed bed catalytic reactor |
| CN105457564B (en) * | 2015-08-31 | 2018-02-16 | 张淮海 | Multistage indirect heat exchange radial fixed-bed reactor |
-
2015
- 2015-12-25 CN CN201510993799.3A patent/CN105457564B/en not_active Expired - Fee Related
- 2015-12-25 CN CN201521101075.5U patent/CN205435687U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105457564A (en) * | 2015-08-31 | 2016-04-06 | 张淮海 | Multi-section indirect heat exchange type radial fixed bed reactor |
| CN105457564B (en) * | 2015-08-31 | 2018-02-16 | 张淮海 | Multistage indirect heat exchange radial fixed-bed reactor |
| CN118949859A (en) * | 2024-10-09 | 2024-11-15 | 浙江长城搅拌设备股份有限公司 | Reactor with catalyst turbulence temperature control structure |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105457564A (en) | 2016-04-06 |
| CN105457564B (en) | 2018-02-16 |
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