CN2705231Y - Gas distributor for axial flow fixed bed reactor - Google Patents
Gas distributor for axial flow fixed bed reactor Download PDFInfo
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- CN2705231Y CN2705231Y CN 200420023151 CN200420023151U CN2705231Y CN 2705231 Y CN2705231 Y CN 2705231Y CN 200420023151 CN200420023151 CN 200420023151 CN 200420023151 U CN200420023151 U CN 200420023151U CN 2705231 Y CN2705231 Y CN 2705231Y
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- sieve plate
- distributor
- fixed bed
- axial flow
- bed reactor
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Abstract
The utility model relates to a kind of gas distributor that is used for axial flow fixed bed reactor.Main improvement was adopted in the axial flow fixed bed reactor of single-stage Flapper type inlet gas distributor in the past, the flow pattern of inlet gas behind single-stage Flapper type gas distributor is not good enough, form and reflux, must eliminate the gas uneven distribution that forms because of gas backstreaming by relative thicker top inertia packed layer, cause the bigger problem of droop loss.The utility model passes through to adopt by distributor cylindrical shell 1, side direction annular space 2, and annular vertical baffle 3, annular baffle 4 and sieve plate 5 are formed the technical scheme of gas distributors, have solved this problem preferably, can be used in the industrial design of axial flow fixed bed reactor.
Description
Technical field
The utility model relates to a kind of gas distributor that is used for axial flow fixed bed reactor, particularly about the gas distributor of the axial flow fixed bed reactor of a kind of disproportionation that is used for toluene and C9 aromatic and transalkylation reaction (abbreviation toluene disproportionation).
Background technology
The major advantage of axial flow fixed bed reactor is flowing near piston flow of bed inner fluid, and chemical reaction velocity is very fast; Available more a spot of catalyst and less reactor volume obtain bigger production capacity; The time of staying of fluid can strict be controlled, and Temperature Distribution can suitably be regulated, and helps improving the conversion ratio and the selectivity of chemical reaction.In addition, axially-located bed structure of reactor is simple, easy to operate, and investment cost is low, and catalyst mechanical wear is little in the bed, can operate under HTHP, therefore obtains to use widely in petrochemical industry.
Along with the development of petro chemical industry and the expansion of scale, the diameter of axial flow fixed bed reactor constantly increases in recent years, and the uniform problem of reactor inner fluid just becomes one of key issue of engineering development.Fluid distribution in the bed directly influences the processes such as heat transfer, mass transfer and chemical reaction in the bed, influences the utilization ratio of catalyst and reactor.When reacting gas entered fixed bed reactors by pipeline, because the sudden enlargement of channel cross-section forms one jet, the fluid velocity distributed pole that causes flowing to bed was inhomogeneous.The uneven distribution of fluid not only influences the reactor utilization rate, and influences selection of catalysts and conversion ratio.Therefore, the uniform fluid distribution technology in the fixed bed reactors is more and more paid attention to by people.The fluid distributed architecture that occurs can be divided into two big classes now: a class is to increase fluid flow resistance, as packing layer or the porous plate that percent opening is less are set before beds.The essence of this kind method is that the impinging jet of formation causes the radial pressure gradient when making gas enter reactor by inlet pipeline on packing layer or porous plate, forces air-flow to change and flows to, and is dispersed to the whole reactor cross section.Since have in the air-flow quite a few energy dissipation with the irrelevant friction and eddy loss of uniform effect in, efficient is lower; And be not suitable for the thin layer reaction device.Another kind of is at the fluid inlet place of fixed bed reactors fluid distributor to be set, and as CN2075277U, US4938422, US368597, its advantage is that fluid is distributed on the reactor cross section more equably, does not cause excessive energy loss again.But the fluid distributor that the Reactor inlet place is provided with is required than higher the structure of distributor more complicated.
Summary of the invention
Technical problem to be solved in the utility model is to exist in the conventional art because reactant flow skewness in axial flow fixed bed reactor, influence the problem of reactor utilization rate and selection of catalysts and conversion ratio and bed pressure drop, a kind of new gas distributor that is used for axial flow fixed bed reactor is provided.This distributor has the fluid of making and be distributed in reactor cross section more equably in axial flow reactor when being used for axial flow fixed bed reactor, thereby make catalyst can give play to its good selectivity and conversion ratio and the little advantage of bed pressure drop, this distributor has characteristic of simple structure simultaneously.
For solving the problems of the technologies described above, the technical solution adopted in the utility model is as follows: a kind of gas distributor that is used for axial flow fixed bed reactor, comprise top distributor cylindrical drum and bottom single-stage baffle plate, be connected by the vertical lacing wire that is distributed in the cylindrical drum inboard between cylindrical drum and single-stage baffle plate, and form the side direction annular space, wherein have sieve aperture on the single-stage baffle plate.
In the technique scheme, single-stage baffle plate preferred version comprises annular baffle and the sieve plate that has sieve aperture, and sieve plate is horizontal positioned, and annular baffle is in the sieve plate outside, and closely link to each other with sieve plate, the angle α between annular baffle and sieve plate is that 0～60 ° of preferable range is 10～45 °; The percent opening of sieve plate is 20～80%, and the area of sieve plate is 0.1～14% of a side direction annular space area, and preferable range is 3.1～9.5%; The diameter of sieve plate is 1～64% of a distributor cylindrical drum diameter, and preferable range is 14～58%; The diameter of sieve aperture is 0.1～9.0% of a distributor cylindrical drum diameter on the sieve plate, and preferable range is 1.2～6.0%.In distributor, also linking on the sieve plate has an annular vertical baffle vertical with sieve plate, and the height of annular vertical baffle is 10～150% of a side direction annular space height, and preferable range is 50～95%; Cylindrical drum upright projection area preferred version is to equate with the single-stage baffle plate.
Toluene disproportionation axial flow insulation fix bed reactor is the capital equipment in the toluene disproportionation process, it is made of gas inlet tube, gas distributor, reactor shell, top inertia packed layer, catalyst, bottom inertia packed layer, exit gas gatherer and gas outlet tube etc., sees accompanying drawing 1.The distribution device in gas-fluid of toluene disproportionation axial flow insulation fix bed reactor employing at present is a single-stage Flapper type distributor, sees accompanying drawing 2.This type of distributor is that a simple single-stage circular baffle plate is set near the port of export of Reactor inlet pipe, and the distribution of gas that causes to prevent gas jet is inhomogeneous.But this type of distributor has formed new gas uneven distribution again in the gas uneven distribution of eliminating gas jet formation, and promptly gas forms two very big recirculating zones in single-stage circular baffle plate bottom.Must eliminate the gas uneven distribution that forms because of gas backstreaming by thicker relatively top inertia packed layer (inertia packed layer height is 300～450 millimeters usually), energy loss is bigger.Particularly to the major diameter reactor, the effect of top inertia packed layer is just more important.
At toluene disproportionation axial flow insulation fix bed reactor, the utility model proposes the circular baffle plate type gas distributor of band sieve aperture, see accompanying drawing 3.This type of new gas distributor is by distributor cylindrical drum 1, side direction annular space 2, and annular vertical baffle 3, the sieve plate 5 of annular baffle 4 and band sieve aperture is formed.In order to guarantee that gas distributor has more satisfactory distribution of gas effect, the ratio that needs control sieve plate 5 areas and side direction annular space 2 areas, the percent opening of sieve plate 5, the diameter of sieve plate 5, the parameters such as angle that the height of annular vertical baffle 3, annular baffle 4 and sieve plate are 5.Thereby make gas in reactor, form distribution of gas relatively uniformly in suitable ratio inflow reactor from side direction annular space 2 and sieve plate 5.
The above-mentioned gas distributor is united use with thin top inertia packed layer just can reach desirable even gas distribution effect.
The said gas distributor of the utility model is investigated through large-scale axial flow fixed bed test, and the result shows to have following advantage:
1, current-sharing effect is better, can make the distribution of gas effect that reaches desirable in the axial flow fixed bed reactor, and bed pressure drop is little;
2, simple in structure, easy for installation, energy loss is less;
Obtained better technical effect.
Description of drawings
Fig. 1 is typical toluene disproportionation axial flow fixed bed reactor schematic diagram;
Fig. 2 is the single-stage Flapper type structure of distributor figure that present toluene disproportionation axial flow fixed bed reactor adopts;
Fig. 3 is the annular vertical baffle type gas distributor structure chart of the utility model band sieve aperture;
In Fig. 1,1 is the gas feed pipeline; 2 is the inlet gas distributor; 3 is top inert filler layer; 4 is beds; 5 is bottom inert filler layer; 6 is the exit gas gatherer; 7 is the gas vent pipeline; 8 is the catalyst discharge port.
In Fig. 2,1 is the distributor cylindrical shell; 2 is the side direction annular space; 3 is bottom single-stage baffle plate.D is the diameter of gas distributor cylindrical shell, and h is the height of side direction annular space.
In Fig. 3,1 is the distributor cylindrical shell; 2 is the side direction annular space; 3 is the annular vertical baffle; 4 is annular baffle; 5 is sieve plate.D is the diameter of gas distributor cylindrical shell, and h is the height of side direction annular space, h
1Be the height of annular vertical baffle, d is the sieve plate diameter, and Φ is the diameter of sieve aperture on the sieve plate, and α is the angle between annular baffle 4 and sieve plate.
Below by embodiment the utility model is further elaborated.
The specific embodiment
[embodiment 1]
The axial flow fixed bed reactor internal diameter is 4.0 meters, the inlet tube internal diameter is 700 millimeters, adopts as shown in Figure 3 the annular vertical baffle type gas distributor with sieve aperture, distributor barrel diameter D=660 millimeter, side direction annular space height h=310 millimeter, annular vertical baffle height h
1=200 millimeters, the diameter d of sieve plate=270 millimeter, the diameter of phi of sieve aperture=14 millimeter on the sieve plate, angle [alpha] between annular baffle and sieve plate=45 °, the area of sieve plate is 4.8% with the ratio of side direction annular space area, and the diameter ratio of the diameter of sieve plate and gas distributor cylindrical shell is 40.9%, and the percent opening of sieve plate is 53.5%, the diameter ratio of the diameter of sieve aperture and gas distributor cylindrical shell is 2.1% on the sieve plate, and the height of annular vertical baffle is 64.5% with the ratio of the height of side direction annular space.
Under above condition and structural parameters, carry out distributor designs by method described in the utility model, reactor is used 120 millimeters high top inertia packed layers, just can obtain desirable gas flow effect.
[embodiment 2]
The axial flow fixed bed reactor internal diameter is 2.0 meters, the inlet tube internal diameter is 400 millimeters, adopts as shown in Figure 3 the annular vertical baffle type gas distributor with sieve aperture, distributor barrel diameter D=360 millimeter, side direction annular space height h=135 millimeter, annular vertical baffle height h
1=100 millimeters, the diameter d of sieve plate=200 millimeter, the diameter of phi of sieve aperture=8 millimeter on the sieve plate, angle [alpha] between annular baffle and sieve plate=30 °, the area of sieve plate is 12.5% with the ratio of side direction annular space area, and the diameter ratio of the diameter of sieve plate and gas distributor cylindrical shell is 55.6%, and the percent opening of sieve plate is 60.6%, the diameter ratio of the diameter of sieve aperture and gas distributor cylindrical shell is 2.2% on the sieve plate, and the height of annular vertical baffle is 74.1% with the ratio of the height of side direction annular space.
Under above condition and structural parameters, carry out distributor designs by method described in the utility model, reactor is used 100 millimeters high top inertia packed layers, just can obtain desirable gas flow effect.
[embodiment 3]
The axial flow fixed bed reactor internal diameter is 2.0 meters, the inlet tube internal diameter is 400 millimeters, adopts as shown in Figure 3 the annular vertical baffle type gas distributor with sieve aperture, distributor barrel diameter D=360 millimeter, side direction annular space height h=135 millimeter, annular vertical baffle height h
1=127 millimeters, the diameter d of sieve plate=120 millimeter, the diameter of phi of sieve aperture=7 millimeter on the sieve plate, angle [alpha] between annular baffle and sieve plate=15 °, the area of sieve plate is 3.1% with the ratio of side direction annular space area, and the diameter ratio of the diameter of sieve plate and gas distributor cylindrical shell is 33.3%, the percent opening 41.9% of sieve plate, the diameter ratio of the diameter of sieve aperture and gas distributor cylindrical shell is 1.9% on the sieve plate, the ratio 94.1% of the height of annular vertical baffle and the height of side direction annular space.
Under above condition and structural parameters, carry out distributor designs by method described in the utility model, reactor is used 100 millimeters high top inertia packed layers, just can obtain desirable gas flow effect.
[embodiment 4]
The axial flow fixed bed reactor internal diameter is 1.0 meters, the inlet tube internal diameter is 170 millimeters, adopts as shown in Figure 3 the annular vertical baffle type gas distributor with sieve aperture, distributor barrel diameter D=158 millimeter, side direction annular space height h=75 millimeter, annular vertical baffle height h
1=45 millimeters, the diameter d of sieve plate=62 millimeter, the diameter of phi of sieve aperture=8 millimeter on the sieve plate, angle [alpha] between annular baffle and sieve plate=15 °, the area of sieve plate is 5.5% with the ratio of side direction annular space area, the diameter ratio of the opening diameter of sieve aperture and gas distributor cylindrical shell is 39.2% on the sieve plate, the percent opening of sieve aperture is 68.3% on the sieve plate, the diameter ratio of the diameter of sieve aperture and gas distributor cylindrical shell is 5.1% on the sieve plate, and the height of annular vertical baffle is 60.0% with the ratio of the height of side direction annular space.
Under above condition and structural parameters, carry out distributor designs by method described in the utility model, reactor is used 100 millimeters high top inertia packed layers, just can obtain desirable gas flow effect.
[comparative example 1]
The condition of certain toluene disproportionation axial flow fixed bed reactor is all identical with embodiment 1 with structural parameters, and unique difference is to adopt simple single-stage circular baffle plate type inlet gas pre-distributor.Reactor need be used at least 450 millimeters high top inertia packed layers, just can obtain more satisfactory gas flow effect.Carry out verification experimental verification by method described in the utility model, adopt the pressure drop of pressure drop ratio embodiment 1 of simple single-stage circular baffle plate type inlet gas pre-distributor big by 73.3%.
[comparative example 2]
The inlet gas pre-distributor of embodiment 2 or 3 toluene disproportionation axial flow fixed bed reactor makes simple single-stage circular baffle plate type inlet gas pre-distributor into, all the condition with embodiment 2 or 3 is identical at all conditions, and reactor need be used 450 millimeters high top inertia packed layers.This comparative example of pressure drop ratio of embodiment 2 is little by 77.8%.
[comparative example 3]
The inlet gas pre-distributor of the toluene disproportionation axial flow fixed bed reactor of embodiment 4 makes simple single-stage circular baffle plate type inlet gas pre-distributor into, all the condition with embodiment 4 is identical at all conditions, and reactor need be used 450 millimeters high top inertia packed layers.This comparative example of pressure drop ratio of embodiment 2 is little by 77.8%.
Claims (7)
1, a kind of gas distributor that is used for axial flow fixed bed reactor, comprise top distributor cylindrical drum and bottom single-stage baffle plate, be connected by the vertical lacing wire that is distributed in the cylindrical drum inboard between cylindrical drum and single-stage baffle plate, and form the side direction annular space, it is characterized in that having sieve aperture on the single-stage baffle plate.
2, according to the described gas distributor that is used for axial flow fixed bed reactor of claim 1, it is characterized in that the single-stage baffle plate comprises annular baffle and the sieve plate that has sieve aperture, sieve plate is horizontal positioned, annular baffle is in the sieve plate outside, and closely link to each other with sieve plate, angle α between annular baffle and sieve plate is 0～60 °, and the percent opening of sieve plate is 20～80%.
3, according to the described gas distributor that is used for axial flow fixed bed reactor of claim 2, it is characterized in that the angle α between annular baffle and sieve plate is 10～45 °, the area of sieve plate is 0.1～14% of a side direction annular space area, the diameter of sieve plate is 1～64% of a distributor cylindrical drum diameter, and the diameter of sieve aperture is 0.1～9.0% of a distributor cylindrical drum diameter on the sieve plate.
4, according to the described gas distributor that is used for axial flow fixed bed reactor of claim 3, the area that it is characterized in that sieve plate is 3.1～9.5% of a side direction annular space area, the diameter of sieve plate is 14～58% of a distributor cylindrical drum diameter, and the diameter of sieve aperture is 1.2～6.0% of a distributor cylindrical drum diameter on the sieve plate.
5, according to the described gas distributor that is used for axial flow fixed bed reactor of claim 1, it is characterized in that in distributor, also linking on the sieve plate has an annular vertical baffle vertical with sieve plate, and the height of annular vertical baffle is 10～150% of a side direction annular space height.
6, according to the described gas distributor that is used for axial flow fixed bed reactor of claim 5, the height that it is characterized in that the annular vertical baffle is 50～95% of a side direction annular space height.
7,, it is characterized in that cylindrical drum upright projection area equates with the single-stage baffle plate according to the described gas distributor that is used for axial flow fixed bed reactor of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200420023151 CN2705231Y (en) | 2004-05-28 | 2004-05-28 | Gas distributor for axial flow fixed bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200420023151 CN2705231Y (en) | 2004-05-28 | 2004-05-28 | Gas distributor for axial flow fixed bed reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2705231Y true CN2705231Y (en) | 2005-06-22 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200420023151 Expired - Fee Related CN2705231Y (en) | 2004-05-28 | 2004-05-28 | Gas distributor for axial flow fixed bed reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2705231Y (en) |
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2004
- 2004-05-28 CN CN 200420023151 patent/CN2705231Y/en not_active Expired - Fee Related
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20050622 Termination date: 20110528 |