CN206996524U - A kind of combined type fixed bed reactors - Google Patents
A kind of combined type fixed bed reactors Download PDFInfo
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- CN206996524U CN206996524U CN201720585471.2U CN201720585471U CN206996524U CN 206996524 U CN206996524 U CN 206996524U CN 201720585471 U CN201720585471 U CN 201720585471U CN 206996524 U CN206996524 U CN 206996524U
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Abstract
The utility model provides a kind of combined type fixed bed reactors, including, housing, charging aperture, discharging opening, isothermal reaction bed, upper adiabatic reaction bed, lower adiabatic reaction bed and cold shock formula heat exchange layer, the fixed bed reactors set cold shock formula heat exchange layer between upper adiabatic reaction bed and lower adiabatic reaction bed, so that reaction mass enters before lower adiabatic reaction bed by upper adiabatic reaction bed and after producing certain adiabatic temperature rise, with being sufficiently mixed by the cold raw material of cold shock formula heat exchange layer to be lowered into the inlet temperature of the reactant of lower adiabatic reaction bed, so that catalyst uses in rational temperature range, extend the service life of catalyst；In addition, the cold raw material entered by cold shock formula heat exchange layer in lower adiabatic reaction bed can increase reactant concentration, and then main reaction speed and reaction selectivity are improved, thus improve the conversion ratio of W-response.
Description
Technical field
The utility model belongs to chemical industry equipment and Design of Chemical Machinery and manufacturing field, and in particular to a kind of combined type is fixed
Bed reactor.
Technical background
Fixed bed reactors are also known as packed bed reactor, are filled with solid catalyst or solid reactant to realize multiphase
A kind of reactor of course of reaction.Solids is generally in granular form, and particle diameter is 2~15mm, is piled into certain altitude (or thickness)
Bed, bed transfixion, fluid reacted by bed.Fixed bed reactors are mainly used in realizing that gas and solid phase catalyzing is anti-
Should, such as ammonia convertor, sulfur dioxide contact oxidation device and hydrocarbon steam converting furnace, it is widely used in petroleum refining industry, nothing
The field such as machine chemical engineering industry, organic chemical industry's industry.
At present, traditional fixed bed reactors use calandria type fixed bed reactor more, and the reactor heat transfer area is big, pass
The thermal efficiency is high, and the bed temperature of catalyst easy to control, but shell and tube reactor difficulty of processing it is larger, it is necessary to material it is more,
Cost is higher, and requires that the differential pressure of every pipe is essentially identical during Catalyst packing, to ensure material in every pipe
Flow is identical with air speed, to obtain preferable reaction effect.But in fact, for most of reactions, with entering for reaction
OK, concentration of the reactant in material gradually reduces, and reaction speed slows down gradually, thus reacts liberated heat and also significantly subtract
It is few, it is not necessary to continue to move out reaction heat, therefore the distribution of reaction heat vertically is also uneven in tubulation, is moved in the axial direction
The demand for going out heat is also different；In addition, the shell side volume ratio tube side volume of shell and tube reactor goes out greatly a lot, therefore for
The catalyst of same volume is loaded, the volume of shell and tube reactor is much larger than adiabatic reactor.
Therefore, the A of Chinese patent literature CN 102794138 disclose a kind of reactor for exothermic reaction, row are included
Pipe fixed bed section and heat-insulating fixed bed section, the heat-insulating fixed bed section are located at the downstream of tubulation fixed bed section, two-stage catalytic
Agent admission space ratio is (0.2~5)：1, above-mentioned reactor by tubulation fixed bed lower end set heat-insulating fixed bed section, by
This is carried out when with reaction, and reactant concentration reduces, and when reaction liberated heat reduces, material is entered heat-insulating fixed bed anti-
Should, thus can solve that shell and tube reactor volume is big and shell and tube reactor in extent of reaction skewness and move heat demand not
The problem of same.But the set-up mode of reactor in said apparatus, on the one hand, when reaction mass enter heat-insulating fixed bed section and with
The continuous progress of reaction, it is excessive the adiabatic temperature rise scope of heat-insulating fixed bed section to be inevitably present, causes heat-insulating to be consolidated
Fixed bed layer local overheating and cause catalyst member inactivation caking, reduce the service life of catalyst；On the other hand, with anti-
The progress answered, concentration of the reactant in material gradually reduce, and reaction speed slows down gradually so that main reaction speed reduce and
Side reaction speed of contacting increase, reaction selectivity decline, so as to cause the conversion ratio of reaction low.Therefore, how to existing solid
Fixed bed reactor is improved to overcome the above insufficient, and this is a technology urgently to be resolved hurrily to those skilled in the art
Problem.
Utility model content
What the utility model solved is that catalyst easy in inactivation, reaction conversion ratio present in existing fixed bed reactors are low
The defects of, so as to provide a kind of combined type fixed bed reactors.
The utility model realizes that the technical scheme of above-mentioned purpose is：
A kind of combined type fixed bed reactors, including：Housing, charging aperture is set at the top of the housing, in the shell
The bottom of body sets discharging opening；
Be divided into from top to bottom in the inside of the housing be sequentially connected isothermal reaction bed, on adiabatic reaction bed and
Lower adiabatic reaction bed, the heat exchange of cold shock formula is provided between adiabatic reaction bed and the lower adiabatic reaction bed on described
Layer；
Heat exchange structure is provided with the isothermal reaction bed, it is included axially through the isothermal reaction bed
For some heat exchanging pipes of loading catalyst, axial direction of the heat exchanging pipe along the isothermal reaction bed is uniformly arranged, and
The upper and lower ends of the heat exchanging pipe are respectively arranged with upper perforated plate and lower perforated plate, the both ends of the heat exchanging pipe respectively with charging
Mouth, upper adiabatic reaction bed are connected, and cooling is collectively forming between the two neighboring heat exchanging pipe, between heat exchanging pipe and housing
But the heat transfer space of flow of media；
Cooling medium inlet is being set on housing corresponding to isothermal reaction bed end, it is corresponding at isothermal reaction bed top
Housing on set cooling medium export.
The height ratio of the isothermal reaction bed, upper adiabatic reaction bed and lower adiabatic reaction bed for (0.55~
4.1)：1：(0.35~2.0).
The admission space ratio of the catalyst of the isothermal reaction bed, upper adiabatic reaction bed and lower adiabatic reaction bed is
(10~35)：(25~55)：(20~40).
The height of the isothermal reaction bed is 1~6 meter.
Also include first gas mixed distribution device, the first gas mixed distribution device and the thing being arranged on the housing
Material import is connected；
It is provided with stomata on the perisporium of the first gas mixed distribution device, and the first gas mixed distribution device is opened
Porosity is more than 50%.
Also include being arranged at the porous of the bottom of adiabatic reaction bed and the upper and lower ends portion of lower adiabatic reaction bed
Wallboard, and the percent opening of the porous structure is not more than 30%.
The perforate size of the stomata of the porous structure is 1-10mm.
Second charging aperture is being set on the housing corresponding to described cold shock formula heat exchange layer one end.
The combined type fixed bed reactors also include being separately positioned on the isothermal reaction bed, upper adiabatic reaction bed
With the thermocouple and in-line analyzer at the material outlet of lower adiabatic reaction bed lower end.
The in-line analyzer is near infrared detection instrument.
Above-mentioned technical proposal of the present utility model has the following advantages that：
(1) in combined type fixed bed reactors described in the utility model, the inside of the housing is divided into from top to bottom
Isothermal reaction bed, upper adiabatic reaction bed and the lower adiabatic reaction bed being sequentially connected；Wherein, it is cold in isothermal reaction bed
But Absorption of Medium heat, on the one hand the reaction temperature of material in shell-and-tube reactor can be kept to maintain fixed range, makes catalysis
Agent uses in rational temperature range, so as to improve reaction efficiency；On the other hand, reaction heat can be converted into steam by cooling medium
Heat, it is possible thereby to which steam heat easily is used for into subsequent reactions, so as to advantageously reduce system energy consumption, avoid the energy unrestrained
Take；In addition, most reaction heat is moved out of in isothermal reaction bed, so as to ensure that the overall temperature stabilization of reactor；It is logical
Cross between upper adiabatic reaction bed and lower adiabatic reaction bed setting cold shock formula heat exchange layer, thus when reaction mass pass through it is upper absolutely
Thermal response bed, enter after producing certain adiabatic temperature rise before lower adiabatic reaction bed, with passing through the cold of cold shock formula heat exchange layer
Raw material is sufficiently mixed to be lowered into the inlet temperature of the reactant of lower adiabatic reaction bed so that catalyst is in rational temperature
Section uses, and avoids the inactivation of catalyst, extends the service life of catalyst；In addition, when with the progress of reaction, reaction
When concentration of the thing in material gradually reduces, the cold raw material entered by cold shock formula heat exchange layer in lower adiabatic reaction bed can increase
Reactant concentration, and then main reaction speed and reaction selectivity are improved, thus improve the conversion ratio of W-response.
To sum up, the combined type fixed bed reactors in the utility model are by by isothermal reaction bed, upper adiabatic reaction bed
Layer and lower adiabatic reaction bed effectively combine, with reactor size is small, shifting thermal effect is good, catalyst service life is long, anti-
Answer the advantages such as conversion ratio height.
(2) in combined type fixed bed reactors described in the utility model, by by isothermal reaction bed, upper adiabatic reaction
The height ratio of bed and lower adiabatic reaction bed maintains (0.55~4.1)：1：Within the scope of (0.35~2.0), simultaneously will
The Catalyst packing volume ratio of isothermal reaction bed, upper adiabatic reaction bed and lower adiabatic reaction bed is controlled in (10~35)：
(25~55)：Within the scope of (20~40) so that material respectively by isothermal reaction bed, upper adiabatic reaction bed and
Conversion ratio during lower adiabatic reaction bed reaches highest, improves the production capacity of reactor, while reduces to greatest extent
The size of reactor.
(3) in combined type fixed bed reactors described in the utility model, first gas mixed distribution device is with being arranged at shell
Material inlet on body is connected, and is provided with stomata on the perisporium of first gas mixed distribution device, can so make reacting gas
It is uniformly distributed, prevents gas bias current, ensures that axially the load of beds is consistent everywhere in reactor.
(4) in combined type fixed bed reactors described in the utility model, upper adiabatic reaction bed bottom with it is lower absolutely
The upper and lower ends portion of thermal response bed is respectively arranged with porous structure, and the percent opening of porous structure is not more than 30%, so may be used
Reaction gas and catalyst is had the time of contact of abundance, improve catalytic efficiency.
Brief description of the drawings
Fig. 1 is the structural representation for the combined type fixed bed reactors that embodiment 1 provides；
Fig. 2 is Fig. 1 A-A sectional views；
Wherein, reference is as follows：
1- housings；2- charging apertures；3- discharging openings；4- isothermal reaction beds；The upper adiabatic reaction beds of 5-；It is adiabatic anti-under 6-
Answer bed；7- cold shock formula heat exchange layers；8- heat exchanging pipes；9- upper perforated plates；10- lower perforated plates；11- first gas mixed distribution devices；
12- porous structures；13- second charging apertures；14- cooling medium inlets；15- cooling mediums export.
Embodiment
The technical solution of the utility model is clearly and completely described below in conjunction with accompanying drawing, it is clear that described
Embodiment is the utility model part of the embodiment, rather than whole embodiments.Based on the embodiment in the utility model, sheet
The every other embodiment that field those of ordinary skill is obtained under the premise of creative work is not made, belongs to this practicality
Novel protected scope.
, it is necessary to explanation, the orientation of the instruction such as term " interior ", " outer ", " on ", " under " in description of the present utility model
Or position relationship is based on orientation shown in the drawings or position relationship, is for only for ease of description the utility model and simplification is retouched
State, rather than instruction or imply signified device or element there must be specific orientation, with specific azimuth configuration and operation,
Therefore it is not intended that to limitation of the present utility model.In addition, term " connected ", " connection " should be interpreted broadly, for example, can be with
It is to be fixedly connected or be detachably connected, or is integrally connected；Can be mechanical connection or electrical connection；Can be with
It is to be joined directly together, can also be indirectly connected by intermediary, can is the connection of two element internals.For the general of this area
For logical technical staff, concrete meaning of the above-mentioned term in the utility model can be understood with concrete condition.
Embodiment 1
As shown in figure 1, the combined type fixed bed reactors described in the present embodiment include：
Housing 1, charging aperture 2 is set at the top of the housing 1, and discharging opening 3 is set in the bottom of the housing 1；Institute
The inside for stating housing 1 is divided into the isothermal reaction bed 4 being sequentially connected, upper adiabatic reaction bed 5 and lower thermal insulation instead from top to bottom
Bed 6 is answered, please referring also to Fig. 2, be provided with heat exchange structure in the isothermal reaction bed 4, it is included axially through institute
State some heat exchanging pipes 8 for loading catalyst of isothermal reaction bed 4, heat exchanging pipe 8 is along the isothermal reaction bed 4
Axially it is uniformly arranged, and the upper and lower ends of the heat exchanging pipe 8 are respectively arranged with upper perforated plate 9 and lower perforated plate 10, material is from heat exchange
The top of tubulation 8, which enters, carries out catalytic reaction inside the pipe of heat exchanging pipe 8, then discharged and entered by the bottom of heat exchanging pipe 8
Upper adiabatic reaction bed 5 carries out adiabatic catalytic reaction, in the present embodiment, between two neighboring heat exchanging pipe 8, heat exchanging pipe 8
The heat transfer space of cooling but flow of media is collectively forming between housing 1, corresponding to the end of isothermal reaction bed 4 on housing 1
Cooling medium inlet 14 is set, is setting cooling medium to export 15, such one on housing 1 corresponding to the top of isothermal reaction bed 4
Aspect, both the reaction temperature of material in shell-and-tube reactor can be kept to maintain fixed range by cooling medium heat absorption, and make to urge
Agent uses in rational temperature range, so as to improve reaction efficiency；On the other hand, cooling medium can be by the reaction of catalytic reaction
Thermal transition is steam heat, it is possible thereby to steam heat is easily used for subsequent reactions, so as to advantageously reduce system energy consumption,
Energy waste is avoided, in addition, most reaction heat is moved out of in isothermal reaction bed, so as to ensure that the overall temperature of reactor
Degree is stable；
The present embodiment is provided with cold shock formula heat exchange layer 7 between upper adiabatic reaction bed 5 and lower adiabatic reaction bed 6, this
Sample enters before lower adiabatic reaction bed 6 after producing certain adiabatic temperature rise when reaction mass is by upper adiabatic reaction bed 5,
Cold raw material with entering cold shock formula heat exchange layer 7 from the second charging aperture 13 on housing 1 is sufficiently mixed lower adiabatic anti-to be lowered into
Answer the inlet temperature of the reactant of bed 6 so that catalyst uses in rational temperature range, avoids the inactivation of catalyst,
Extend the service life of catalyst；In addition, when with the progress of reaction, when concentration of the reactant in material gradually reduces,
Enter cold shock formula heat exchange layer 7 from second charging aperture 13, can increase reactant subsequently into the cold raw material in lower adiabatic reaction bed 6
Concentration, and then main reaction speed and reaction selectivity are improved, thus improve the conversion ratio of W-response.
Further, in the combined type fixed bed reactors described in the present embodiment, isothermal reaction bed 4, upper adiabatic reaction
The height ratio of bed 5 and lower adiabatic reaction bed 6 is 2：1：0.5, in other embodiments, isothermal reaction bed 4, upper thermal insulation are anti-
It can be (0.55~4.1) to answer the height ratio of bed 5 and lower adiabatic reaction bed 6：1：Arbitrary Digit within the scope of (0.35~2.0)
Value；In the present embodiment, the catalyst of isothermal reaction bed 4, upper adiabatic reaction bed 5 and lower adiabatic reaction bed 6 simultaneously
Admission space ratio is 25：35：30, in other embodiments, isothermal reaction bed 4, upper adiabatic reaction bed 5 and lower thermal insulation are anti-
The admission space ratio for answering the catalyst of bed 6 can be (10~35)：(25~55)：Any number within the scope of (20~40)；
The height of isothermal reaction bed is 3 meters in the present embodiment, and in other embodiments, the height of isothermal reaction bed can be 1~5 meter
Between any number, the present embodiment is by controlling the height ratio of each bed of reactor and Catalyst packing volume ratio so that thing
Material reaches highest by conversion ratio when isothermal reaction bed 4, upper adiabatic reaction bed 5 and lower adiabatic reaction bed 6 respectively, by
This improves the production capacity of reactor, while reduces the size of reactor to greatest extent.
At the same time, the fixed bed reactors in the present embodiment also include first gas mixed distribution device 11, first gas
Body mixed distribution device 11 is connected with the material inlet being arranged on housing 1, and is provided with stomata on its perisporium, in the present embodiment
In, the percent opening of the perisporium stomata of first gas mixed distribution device 11 is 70%, in other embodiments, first gas mixing point
The percent opening of the perisporium stomata of cloth device 11 may be greater than 50% any number, thus can be uniformly distributed reacting gas, prevent
Gas bias current, ensure that axially the load of beds is consistent everywhere in reactor.
Further, the present embodiment also includes being arranged at the bottom of adiabatic reaction bed 5 and lower adiabatic reaction bed 6
Upper and lower ends portion porous structure 12, the porous structure 12 can be used for fixed upper adiabatic reaction bed 5 and lower adiabatic reaction bed
Catalyst in layer 6, in the present embodiment, the percent opening of porous structure 12 is 20%, in other embodiments, porous structure
12 percent opening can be any number no more than 30%；And the perforate size of the stomata of porous structure 12 is 5mm, in other realities
Apply in example, any number of the big I of perforate of the stomata of porous structure 12 between 1-10mm, can so make reaction gas with urging
Agent has the time of contact of abundance, improves catalytic efficiency.
The present embodiment provide reactor also include be separately positioned on isothermal reaction bed 4, upper adiabatic reaction bed 5 and under
Thermocouple and in-line analyzer at the lower end material outlet of adiabatic reaction bed 6, in the present embodiment, in-line analyzer is specially
Near infrared detection instrument, the temperature and materials conversion rate of each reaction bed thus can be monitored at any time.
Obviously, above-described embodiment is only intended to clearly illustrate example, and is not the restriction to embodiment.It is right
For those of ordinary skill in the art, can also make on the basis of the above description it is other it is various forms of change or
Change.There is no necessity and possibility to exhaust all the enbodiments.And the obvious change thus extended out or
Among the protection domain that variation is created still in the utility model.
Claims (10)
1. a kind of combined type fixed bed reactors, including：Housing (1), charging aperture (2) is set at the top of the housing (1),
The bottom of the housing (1) sets discharging opening (3)；Characterized in that,
It is divided into the isothermal reaction bed (4) being sequentially connected, upper adiabatic reaction bed from top to bottom in the inside of the housing (1)
(5) and lower adiabatic reaction bed (6), set on described between adiabatic reaction bed (5) and the lower adiabatic reaction bed (6)
There is cold shock formula heat exchange layer (7)；
Heat exchange structure is provided with the isothermal reaction bed (4), it is included axially through the isothermal reaction bed (4)
Some heat exchanging pipes (8) for loading catalyst, axial direction of the heat exchanging pipe (8) along the isothermal reaction bed (4)
It is uniformly arranged, and the upper and lower ends of the heat exchanging pipe (8) are respectively arranged with upper perforated plate (9) and lower perforated plate (10), the heat exchange
The both ends of tubulation (8) connect with charging aperture (2), upper adiabatic reaction bed (5) respectively, the two neighboring heat exchanging pipe (8) it
Between, the heat transfer space of cooling but flow of media is collectively forming between heat exchanging pipe (8) and housing (1)；
Cooling medium inlet (14) is being set corresponding to isothermal reaction bed (4) end on housing (1), in isothermal reaction bed
(4) cooling medium is set to export (15) on housing corresponding to top (1).
2. combined type fixed bed reactors according to claim 1, it is characterised in that the isothermal reaction bed (4), on
Adiabatic reaction bed (5) and the height ratio of lower adiabatic reaction bed (6) are (0.55~4.1)：1：(0.35~2.0).
3. combined type fixed bed reactors according to claim 1 or 2, it is characterised in that the isothermal reaction bed
(4), the admission space ratio of the catalyst of upper adiabatic reaction bed (5) and lower adiabatic reaction bed (6) is (10~35)：(25~
55)：(20~40).
4. combined type fixed bed reactors according to claim 3, it is characterised in that the isothermal reaction bed (4)
Highly it is 1~6 meter.
5. according to the combined type fixed bed reactors described in claim 1,2 or 4, it is characterised in that
Also include first gas mixed distribution device (11), the first gas mixed distribution device (11) is with being arranged at the housing
(1) material inlet on is connected；
Stomata, and the first gas mixed distribution device (11) are provided with the perisporium of the first gas mixed distribution device (11)
Percent opening be more than 50%.
6. combined type fixed bed reactors according to claim 5, it is characterised in that also include being arranged at adiabatic reaction
The porous structure (12) of the bottom of bed (5) and the upper subordinate both ends of lower adiabatic reaction bed (6), and the porous structure
(12) percent opening is not more than 30%.
7. combined type fixed bed reactors according to claim 6, it is characterised in that the stomata of the porous structure (12)
Perforate size be 1-10mm.
8. combined type fixed bed reactors according to claim 5, it is characterised in that in the cold shock formula heat exchange layer (7)
Second charging aperture (13) is set corresponding to one end on the housing (1).
9. combined type fixed bed reactors according to claim 8, it is characterised in that the combined type fixed bed reactors
Also include being separately positioned on the isothermal reaction bed (4), upper adiabatic reaction bed (5) and lower adiabatic reaction bed (6) lower end
Thermocouple and in-line analyzer at material outlet.
10. combined type fixed bed reactors according to claim 9, it is characterised in that the in-line analyzer is near red
Outer detector.
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| CN201720585471.2U CN206996524U (en) | 2017-05-24 | 2017-05-24 | A kind of combined type fixed bed reactors |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108993370A (en) * | 2018-10-18 | 2018-12-14 | 辽宁石油化工大学 | A kind of spiral coil isothermal reactor and its application method |
| CN113511951A (en) * | 2020-04-10 | 2021-10-19 | 中国石油化工股份有限公司 | Method for deoxidizing unsaturated hydrocarbon gas |
| CN113522010A (en) * | 2020-04-10 | 2021-10-22 | 中国石油化工股份有限公司 | Deoxygenating device for unsaturated hydrocarbon gas |
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- 2017-05-24 CN CN201720585471.2U patent/CN206996524U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108722180A (en) * | 2018-07-23 | 2018-11-02 | 唐山钢铁集团有限责任公司 | A kind of smoke catalytic denitration device and catalytic denitration method |
| CN108722180B (en) * | 2018-07-23 | 2024-09-27 | 唐山钢铁集团有限责任公司 | Flue gas catalytic denitration device and catalytic denitration method |
| CN108993370A (en) * | 2018-10-18 | 2018-12-14 | 辽宁石油化工大学 | A kind of spiral coil isothermal reactor and its application method |
| CN113511951A (en) * | 2020-04-10 | 2021-10-19 | 中国石油化工股份有限公司 | Method for deoxidizing unsaturated hydrocarbon gas |
| CN113522010A (en) * | 2020-04-10 | 2021-10-22 | 中国石油化工股份有限公司 | Deoxygenating device for unsaturated hydrocarbon gas |
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