CN103071431A - Axial and radial reactor structure for sulfur-tolerant conversion process - Google Patents
Axial and radial reactor structure for sulfur-tolerant conversion process Download PDFInfo
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- CN103071431A CN103071431A CN2013100488595A CN201310048859A CN103071431A CN 103071431 A CN103071431 A CN 103071431A CN 2013100488595 A CN2013100488595 A CN 2013100488595A CN 201310048859 A CN201310048859 A CN 201310048859A CN 103071431 A CN103071431 A CN 103071431A
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Abstract
The invention relates to an axial and radial reactor structure for a sulfur-tolerant conversion process. The axial and radial reactor structure comprises a casing, wherein a gas flow inlet is arranged on the top of the casing, and a gas flow outlet is arranged at the bottom of the casing. The axial and radial reactor structure is characterized in that the reactor structure also comprises a first gas distributor, a second gas distributor and a gas collector, the second gas distributor is used for carrying out secondary redistribution on the gas flow, then, the gas flow enters a catalyst bed layer, a gap is formed between an outer tube body of the second gas distributor and the inner wall of the casing, the gas collector is arranged in the second gas distributor, a gap is formed between a sealing cover of the second gas distributor and a cover net of the first gas distributor, a grating is also arranged above the second gas distributor, and a second heat insulation layer formed by fire-resistant balls is filled between the grating and the cover net. Compared with the prior art, the reactor provided by the invention has the characteristics that the casing wall temperature is low, the pressure drop is low, the equipment diameter is small, the catalyst dead region is small, the reactor space utilization rate is high, the equipment material requirement is low, the equipment weight is light, and the like.
Description
Technical field
The present invention relates to the chemical industry equipment field, specifically refer to a kind of axial-radial flow reactor structure for sulfur resistant conversion process.
Background technology
Growing along with Coal Gasification Technology, and oil price can be in any more, so that the C1 chemical industry fast development in recent years take coal as the source, and scale increases day by day.Along with starting of the large-scale Coal Chemical Engineering Projects such as the supporting device for producing hydrogen of large quantities of oil refining, MTO and coal-ethylene glycol, pass through actual engineering design, find that converter unit ratio in gross investment almost is equivalent to the low-temperature rectisol unit progressively increasing, even surpass its investment.Why this phenomenon appears, be because the amplification of scale so that the investment of equipment pipe significantly increase.Can wherein change furnace be exactly to increase maximum one, therefore design the key point that rational change furnace has just become to reduce energy consumption and reduce cost.
Current, the sulfur-tolerant water gas shift device adopts fixed bed reactors mostly, can be divided into axial flow reactor, radial reactor and axial-radial flow reactor according to fluid-flow mode.Wherein, axial flow reactor, gas is entered by the top, axially passes beds from top to bottom, and reacted gas leaves reactor from lower part outlet; Radial reactor, gas is entered by the top, enters catalyst by the gas distributor between bed and reactor, radially by beds, goes out reactor by interior collector at last; Axial-radial flow reactor, gas is entered by the top, and the hole wall that primary air passes collector enters bed, and radially by bed, another part is still according to axially entering the bed top, and the hole wall that the conversion gas that leaves bed penetrates interior collector leaves reactor.
Axially change furnace is used in sulfur resistant conversion process widely owing to its version, but along with scale constantly enlarges, its pressure drop is large, reactor diameter is large, and the demanding shortcoming of equipment material shows especially out gradually; Radial reactor is by increasing circulation area, reduce the airflow path, well solved the problem of pressure drop, equipment size and material, but catalyst shrinks and easily causes air flow shortcircuit in the radial reactor, must leave on radial bed top one section not aperture area, claim catalyst sealing, this part catalyst sealing does not participate in transformationreation yet, will cause like this waste of catalyst and reactor dischargeable capacity.
Granted publication number has proposed a kind of axial-radial flow reactor in the Chinese invention patent disclosed " method of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation " of CN1141279C, the radially conversion zone of this axial-radial flow reactor is positioned at the below of axial conversion zone, be connected with an annular flange flange of going deep into beds at the axial segmental wall of inside distributor, wherein annular flange flange is goed deep into the top of beds, with the rectilineal interval of inside distributor periphery be 50% of 5mm～catalyst bed layer thickness, the lower extreme point of annular flange flange links to each other with the junction of inside distributor radial section and axial direction part, the inseparable aperture of axial direction part section of inside distributor.This reactor only is that axial flow reactor and radial reactor are serially connected up and down simply, catalyst in the reactor divides axially and radial filling, the axial direction part top drilling, but catalyst housing and central tube are in not perforate of axial direction part, the form of this kind design and radial reactor is basically identical, extremely a small amount of fluid can enter beds by the passage at axial top, axially DeGrain; The catalyst housing directly contacts with the cylindrical shell low head in addition, the temperature of whole reactor shell is still very high, not only require high to equipment material, and high to the requirement on machining accuracy of equipment, still there is the catalyst sealing that does not participate in reacting in it simultaneously, and the volume of whole reactor still can not be fully utilized.
Summary of the invention
Technical problem to be solved by this invention is that the present situation for prior art provides a kind of axial-radial flow reactor structure that is used for sulfur resistant conversion process that can take full advantage of the internal capacity of reactor and can effectively reduce the reactor cylinder wall temperature.
The present invention solves the problems of the technologies described above the technical scheme that adopts: should be used for the axial-radial flow reactor structure of sulfur resistant conversion process, and comprise:
Housing, the top of housing is provided with air flow inlet, and the bottom of housing is provided with air stream outlet;
It is characterized in that this structure of reactor also comprises:
The first gas distributor is arranged in the described housing, is used for the air-flow that enters in the housing is once distributed again, and the entrance of this first gas distributor connects described air flow inlet;
The second gas distributor is arranged in the described housing, is used for carrying out secondary and distributing entering air-flow in the housing, so that air-flow evenly enters beds; This second gas distributor comprises the outer cylinder body and the cover net and the base plate that are separately positioned on the outer cylinder body upper/lower terminal of tubular structure, and described outer cylinder body is provided with pore, and the middle part of described base plate is provided with connecting hole, and this base plate is seated on the first thermal insulation layer; Described the first thermal insulation layer is made of the flame-proof sphere that is filled in described housing bottom; The interval is gapped between the inwall of described outer cylinder body and described housing;
Gas collector, be set in the described outer cylinder body, be used for collect air-flow after the reaction, comprise inner barrel and be arranged on capping on the upper port of this inner barrel, the lower port of this inner barrel is passed described connecting hole and is communicated with described air stream outlet, and described inner barrel is provided with air admission hole; The interval is gapped between described capping and the described cover net;
Grid radially is arranged in the described housing, is positioned at the top of described the second gas distributor, is filled with the second thermal insulation layer that is made of flame-proof sphere between described grid and the described cover net.
Distance between described capping and the described cover net is 0.5 ~ 2.0 times of distance between described inner barrel and the described outer cylinder body.
In above-mentioned each scheme, in order to guarantee that each is to the uniformity of reaction in the beds, the size of described pore and the distribution on described outer cylinder body thereof enter beds with the control air-flow with uniform speed and are advisable, and this speed is 2～20 meter per seconds; The size of described air admission hole and the distribution on described inner barrel thereof enter flow velocity in the described inner barrel as 10 ~ 30m/s take the control air-flow.
Described housing comprises cylindrical body and the upper cover and the low head that are arranged on the upper/lower terminal of this cylindrical body, and the draw ratio of described cylindrical body is 1.0 ~ 5.0.The draw ratio of housing is considered definite by the weight of loadings, bed pressure drop and the equipment of catalyst, draw ratio except under the condition that can satisfy technological requirement and pressure drop, can make the weight of whole reactor the lightest in this scope.
On the inwall of described outer cylinder body, be equipped with the silk screen for the backstop catalyst on the outer wall of described inner barrel.
Compared with prior art, axial-radial flow reactor provided by the present invention, fluid can axially and radially pass through beds simultaneously, by regulating the distance between cover net and the capping, but the utilization rate of Effective Raise catalyst, take full advantage of the space in the housing, solved the catalyst sealing that occurs in the pure radial reactor and do not participated in reaction, cause the problem of the waste of catalyst and reactor dischargeable capacity; Gap between the second gas distributor and the housing is not so that the reaction heat that reaction produces is directly delivered on the housing simultaneously, housing is cold wall housing, has reduced the design temperature of housing, thereby reduces reactor to the requirement of equipment material, reduce weight of equipment, reduced investment; Primary air radially effectively reduces the reaction pressure drop by beds by gas collector on the other hand, can reduce by increasing draw ratio the diameter of reactor, reduces the wall thickness of pressure-bearing shell, thereby reduces equipment investment.
Description of drawings
Fig. 1 is the longitudinal sectional view of embodiment of the invention assembly structure;
Fig. 2 is the planar structure schematic diagram of grid in the embodiment of the invention.
The specific embodiment
Embodiment is described in further detail the present invention below in conjunction with accompanying drawing.
As depicted in figs. 1 and 2, should be used for the axial-radial flow reactor structure of sulfur resistant conversion process, comprise:
Housing 1, the top of housing is provided with air flow inlet 11, and the bottom of housing is provided with air stream outlet 12; Housing in the present embodiment comprises cylindrical body 13 and the upper cover 14 and the low head 15 that are arranged on the upper/lower terminal of this cylindrical body, and the draw ratio of cylindrical body is 2.The draw ratio of cylindrical body can be decided as required, preferably, can be 1.0 ~ 5.0, under the condition of this scope internal satisfaction technique and pressure drop, can make the weight of whole reactor the lightest.Be filled with flame-proof sphere in the low head 15, these flame-proof spheres consist of the first thermal insulation layer 16 in the present embodiment.
The first gas distributor 2 is arranged in the space of upper cover, is used for the air-flow that enters in the housing is once distributed again, and the entrance of this first gas distributor connects described air flow inlet.The first gas distributor can use of the prior art any one.
The second gas distributor 3 is arranged in the cylindrical body 13 of housing, is used for carrying out secondary and distributing entering air-flow in the housing, so that air-flow evenly enters beds; This second gas distributor comprises outer cylinder body 31 upper and lower cover net 32 and the base plates 33 of tubular structure, wherein, pore is all arranged on the outer cylinder body 31, the size of pore and the distribution on outer cylinder body thereof enter beds with the control air-flow with the uniform speed of 2～20 meter per seconds and are advisable, and this structure can guarantee that each is to the uniformity of reaction in the beds.Specifically can calculate according to the pressure drop in arts demand and the reactor and decide.
Base plate is plate-like structure, and its middle part is provided with connecting hole, is used for the gas collector lower end and passes.
The inner surface of the second gas distributor is laid with woven wire 34, and the size of screen opening is decided according to catalyst particle size, lives with backstop that catalyst granules does not spill and the circulation that do not affect again air-flow is as the criterion.
The second gas distributor 3 is seated on the first thermal insulation layer 16, and interval gapped 35 between the outer cylinder body 31 of the second gas distributor and the housing.The existence in gap is so that housing becomes cold wall housing, and this design can effectively reduce the material requirement of equipment, reduces equipment investment.The large I in gap is decided according to process requirements.
Except the supporting of the first thermal insulation layer, also be provided with other support member in the housing for the location between the second gas distributor and the housing.Support member itself and assembly structure can use of the prior art any one.
Gas collector 4, be set in the outer cylinder body 31, be used for collect air-flow after the reaction, comprise inner barrel 41 and be arranged on capping 42 on the upper port of this inner barrel, the lower port of this inner barrel is passed connecting hole and is communicated with described air stream outlet 12, is equipped with a plurality of equally distributed air admission holes on the inner barrel; Not perforate in the capping.The size of air admission hole and the distribution on inner barrel thereof evenly enter in the inner barrel with the flow velocity of 10 ~ 30m/s with the control air-flow and are advisable, and can in time remove to guarantee the synthesis gas that reaction generates.The gapped L1 in interval between capping and the cover net.Distance between inner barrel 41 and the outer cylinder body 31 is L2.L1=0.5L2 in the present embodiment.
The size of L1 can be selected between 0.5 ~ 2.0 times of L2, in this scope, on the one hand can so that the mean residence time of gas by catalyst sealing with pass through the bed mean residence time and equate, thereby make gas on radial and axial direction, enter more equably beds with identical speed; The existence of L1 has been avoided because the gas short circuit problem that the sedimentation of catalyst causes on the other hand, can make the catalyst granules that is filled in the reactor all participate in reaction, take full advantage of the space of reactor, increased respond in the situation that do not change the reactor size.
The diameter of inner barrel, air admission hole perforate size, density and arrangement mode can be decided according to process requirements, are advisable so that process gas can enter equably in the interior collector and go out reactor with suitable flow velocity.Be laid with woven wire 43 on the gas collector outer surface relative with the second gas distributor, decide according to catalyst particle size in the aperture of woven wire, lives catalyst granules with backstop and it is leaked in be as the criterion.
Catalyst 6 is filled in the gap between the second gas distributor and the gas collector.
The operation principle of being somebody's turn to do the axial-radial flow reactor that is used for sulfur resistant conversion process is as follows:
The gas that the upstream is come enters in the housing 1 by air flow inlet, is scattered in uniformly in the housing through the first gas distributor; Because stopping of grid and the second thermal insulation layer, main fluid at first enters in the space between housing and the second distributor, then radially enters beds by the second gas distributor pore; A small amount of gas axially axially enters beds by grid, the second thermal insulation layer, and the air-flow that generates behind the beds internal reaction passes beds and enters in the gas collector from air admission hole and go out reactor via air stream outlet.
Technical problem to be solved by this invention is for the problems referred to above, and provides a kind of novel diameter of axle to change furnace.
Claims (5)
1. axial-radial flow reactor structure that is used for sulfur resistant conversion process comprises:
Housing, the top of housing is provided with air flow inlet, and the bottom of housing is provided with air stream outlet;
It is characterized in that this structure of reactor also comprises:
The first gas distributor is arranged in the described housing, is used for the air-flow that enters in the housing is once distributed again, and the entrance of this first gas distributor connects described air flow inlet;
The second gas distributor is arranged in the described housing, is used for carrying out secondary and distributing entering air-flow in the housing, so that air-flow evenly enters beds; This second gas distributor comprises the outer cylinder body and the cover net and the base plate that are separately positioned on the outer cylinder body upper/lower terminal of tubular structure, and described outer cylinder body is provided with pore, and the middle part of described base plate is provided with connecting hole, and this base plate is seated on the first thermal insulation layer; Described the first thermal insulation layer is made of the flame-proof sphere that is filled in described housing bottom; The interval is gapped between the inwall of described outer cylinder body and described housing;
Gas collector, be set in the described outer cylinder body, be used for collect air-flow after the reaction, comprise inner barrel and be arranged on capping on the upper port of this inner barrel, the lower port of this inner barrel is passed described connecting hole and is communicated with described air stream outlet, and described inner barrel is provided with air admission hole; The interval is gapped between described capping and the described cover net;
Grid radially is arranged in the described housing, is positioned at the top of described the second gas distributor, is filled with the second thermal insulation layer that is made of flame-proof sphere between described grid and the described cover net.
2. the axial-radial flow reactor structure for sulfur resistant conversion process according to claim 1 is characterized in that distance between described capping and the described cover net is 0.5 ~ 2.0 times of distance between described inner barrel and the described outer cylinder body.
3. the axial-radial flow reactor structure for sulfur resistant conversion process according to claim 1 and 2, the size and the distribution on described outer cylinder body thereof that it is characterized in that described pore enter beds with the control air-flow with uniform speed, and this speed is 2～20 meter per seconds; The size of described air admission hole and the distribution on described inner barrel thereof enter flow velocity in the described inner barrel as 10 ~ 30 meter per seconds take the control air-flow.
4. the axial-radial flow reactor structure for sulfur resistant conversion process according to claim 3, it is characterized in that described housing comprises cylindrical body and the upper cover and the low head that are arranged on the upper/lower terminal of this cylindrical body, the draw ratio of described cylindrical body is 1.0 ~ 5.0.
5. the axial-radial flow reactor structure for sulfur resistant conversion process according to claim 4 is characterized in that on the inwall of described outer cylinder body, is equipped with the silk screen for the backstop catalyst on the outer wall of described inner barrel.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310048859.5A CN103071431B (en) | 2013-02-07 | 2013-02-07 | A kind of axial-radial flow reactor structure for sulfur resistant conversion process |
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| CN201310048859.5A CN103071431B (en) | 2013-02-07 | 2013-02-07 | A kind of axial-radial flow reactor structure for sulfur resistant conversion process |
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| CN103071431A true CN103071431A (en) | 2013-05-01 |
| CN103071431B CN103071431B (en) | 2015-10-28 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105664804A (en) * | 2016-01-27 | 2016-06-15 | 中石化宁波工程有限公司 | Axial-radial isothermal reactor |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1043918A (en) * | 1988-12-09 | 1990-07-18 | 阿莫尼·卡萨尔公司 | Be used for improving the system of pre-existing reactors carbon monoxide transformation efficiency and the reactor that so obtains |
| CN2291201Y (en) * | 1997-04-28 | 1998-09-16 | 华东理工大学 | Radial fixed bed catalytic reactor for co-producing steam |
| CN200954444Y (en) * | 2006-09-27 | 2007-10-03 | 吕仲明 | Radial baffle shell-type reactor |
| CN203123947U (en) * | 2013-02-07 | 2013-08-14 | 中石化宁波工程有限公司 | Axial-radial reactor structure for sulfur-resisting conversion process |
-
2013
- 2013-02-07 CN CN201310048859.5A patent/CN103071431B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1043918A (en) * | 1988-12-09 | 1990-07-18 | 阿莫尼·卡萨尔公司 | Be used for improving the system of pre-existing reactors carbon monoxide transformation efficiency and the reactor that so obtains |
| CN2291201Y (en) * | 1997-04-28 | 1998-09-16 | 华东理工大学 | Radial fixed bed catalytic reactor for co-producing steam |
| CN200954444Y (en) * | 2006-09-27 | 2007-10-03 | 吕仲明 | Radial baffle shell-type reactor |
| CN203123947U (en) * | 2013-02-07 | 2013-08-14 | 中石化宁波工程有限公司 | Axial-radial reactor structure for sulfur-resisting conversion process |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105664804A (en) * | 2016-01-27 | 2016-06-15 | 中石化宁波工程有限公司 | Axial-radial isothermal reactor |
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| CN103071431B (en) | 2015-10-28 |
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