CN100349647C - Multi-segment insulation fix bed reactor - Google Patents
Multi-segment insulation fix bed reactor Download PDFInfo
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- CN100349647C CN100349647C CNB2004100676294A CN200410067629A CN100349647C CN 100349647 C CN100349647 C CN 100349647C CN B2004100676294 A CNB2004100676294 A CN B2004100676294A CN 200410067629 A CN200410067629 A CN 200410067629A CN 100349647 C CN100349647 C CN 100349647C
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Abstract
The present invention relates to a multi-segment insulation fix bed reactor which mainly solves the defect that gas mixing functions of a pipe internal type material feeding distributor of inner segments of the existing industrial multi-segment insulation fix bed reactor are bad. The present invention adopts the reactor which is provided with a built-in catalyst bed and a gas mixing device of segment internal beds, wherein the segment internal gas mixing device is mainly composed of a material inlet 9 of a first type of materials, a reactor shell 4, a material inlet 6 of a second type of materials, a conical body 10, a straight pipe 11, a lateral annular space 12 and a sieve plate 13, which fine solves the problem. The reactor has the advantages of simple structure and small pressure drop, and can complete quick and uniform mixing of two paths of materials and the uniform distribution of the materials. The present invention can be used for industrial production for making ethylenzene by the gas phase alkylation of the benzene and ethene molecular sieves.
Description
Technical field
The present invention relates to a kind of multistage insulation fixed bed reactor.Specifically, relate to a kind of multistage insulation fixed bed reactor that is used for benzene and ethylene molecule sieve producing ethyl benzene through alkylation in gas phase.
Background technology
Multistage insulation formula fixed bed reactors have simple in structure, easy to operate, can adapt to the characteristics that big system produces, and therefore obtain to use widely in petrochemical industry.Add by between two sections of the reactor catalysts for multistage insulation formula fixed bed reactors parts reaction mass, at this moment just produce the equally distributed problem of evenly mixed and mixed back material with the preceding paragraph material.Intersegmental mixed requirement is mixed fast and even distribution of realizing two strands of reaction masses in limited time and space, makes the material that enters next section beds accomplish that radially concentration is even, temperature is even, speed is even.
Ethylbenzene is important chemical material, is mainly used in dehydrogenation and produces styrene.In the course of reaction of benzene and ethylene alkylation system ethylbenzene, mainly by ethylene concentration control, the higher reaction speed of ethylene concentration is very fast for alkylating reaction rate, the adiabatic temperature rise of beds increases, coking speeds up, and catalyst life shortens, and increases accessory substance.In order to reduce the ethylene concentration that enters beds, multistage insulation formula fixed bed reactors have been selected from side entry feed.But if enter the material (second gas) of reactor from side line mixed inhomogeneous with the interior principal goods material (first gas) of reactor, the excessive concentration place, it is too much that reaction speed is emitted heat soon, unfavorable to catalyst; And concentration is crossed lower, and reaction speed is low, and catalyst does not make full use of, and has reduced the efficient of catalyst.Therefore the intersegmental mixed effect of multistage insulation formula fixed bed reactors has determined the quality of reactor design.
Disclosing the feed distributor in a kind of gas-solid phase multistage cold shock formula fixed bed reactors among the Chinese patent CN2218599Y, is the normal a kind of intersegmental charging pipe distributor that adopts in the present industrial multistage insulation formula fixed bed reactors.This distributor comprises circular house steward and arm, and each arm is same cross section equal angles or equidistantly arrangement in reactor, has 1 to 2 row and upwards obtain downward aperture on each arm, and aperture evenly distributes along pipe range.But this distributor requires upper strata principal goods material evenly to distribute, and could guarantee that two strands of materials are evenly mixed.Such condition is not to satisfy in commercial plant.Disclose a kind of gas gas mixing apparatus among the Chinese patent CN1030284C, be characterized in utilizing the bump of jet and porous plate to produce strong main diffusion and DIFFUSION IN TURBULENCE, thereby realize the mixed fast of gas gas material.Though this device can effectively carry out the evenly mixed of two strands of materials, really can not guarantee the even distribution of mixed back material.
Summary of the invention
Technical problem to be solved by this invention is to be present in the mixed inhomogeneous or skewness of the intersegmental two strands of materials of multistage insulation formula fixed bed reactors in the prior art, influence the problem of catalyst utilization and selectivity and conversion ratio, a kind of new multistage insulation fixed bed reactor that is used for is provided.This multistage insulation fixed bed reactor has the mixed all even even advantage that distributes and enter next section beds of back material of mixing of material (second gas) that makes interior principal goods material (first gas) of reactor and side line enter reactor.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of multistage insulation fixed bed reactor, comprise reactor inlet 3, reactor shell 4, reactor outlet 8, be provided with 2～10 beds 5 in the reactor shell, 5 of beds are provided with intersegmental gas mixing apparatus 7, wherein each intersegmental gas mixing apparatus 7 comprises first kind of material inlet 9, second kind of material inlet 6, reactor shell 4, the built-in back taper body 10 of reactor, straight tube 11, side direction annular space 12 and sieve plate 13, first kind of material inlet 9 and second kind of material inlet 6 lay respectively at the top of back taper body 10, the upper end of straight tube 11 links to each other with the lower end of back taper body 10, form side direction annular space 12 in the middle of the lower end of straight tube 11 and the sieve plate 13, and fix straight tube 11 diameter d by vertical lacing wire
1With the ratio of reactor diameter D be 10～40%, back taper body 10 is 15～75 ° with the angle α of horizontal level, the diameter d of sieve plate 13
2With the ratio of reactor diameter D be 10～45%, the percent opening of sieve plate 13 is 0～75%, the area ratio of the perforated area of sieve plate 13 and side direction annular space 12 is 0～35%, reactor shell 4, straight tube 11 and sieve plate 13 have concentric shafts.
In the technique scheme, second kind of material inlet 6 has two in each intersegmental gas mixing apparatus 7, preferred version is that the Way in of two second kind of material inlets 6 is parallel to round tangential direction, and center symmetry, the horizontal range l that two second kind of material inlets are 6 is 50～95% of reactor diameter D, and preferable range is 70～90%; Straight tube 11 diameter d
1With the ratio preferable range of reactor diameter D be 15～30%; Back taper body 10 is 30～60 ° with the angle α preferable range of horizontal level; The diameter d of sieve plate 13
2With the ratio preferable range of reactor diameter D be 15～35%; The percent opening preferable range of sieve plate 13 is 15～50%; The area ratio preferable range of the perforated area of sieve plate 13 and side direction annular space 12 is 10～30%.
The present invention is that six sections insulation fix bed reactor is an example with beds, six sections insulation fix bed reactors are capital equipments of benzene and ethylene molecule sieve producing ethyl benzene through alkylation in gas phase, it is made of first kind of gas inlet tube 3, reactor shell 4, beds 5, second kind of gas inlet tube 6, intersegmental gas mixing apparatus 7, gas outlet tube 8 etc., sees accompanying drawing 1.
Six sections insulation fix bed reactors at benzene and ethylene molecule sieve producing ethyl benzene through alkylation in gas phase have proposed intersegmental gas mixing apparatus, see accompanying drawing 2 and accompanying drawing 3.This type of new gas mixing apparatus is by the inlet 9 of first kind of material, the inlet 6 of 4, the second kinds of materials of reactor shell, and back taper body 10, straight tube 11, side direction annular space 12 and sieve plate 13 are formed.In order to guarantee that the gas mixing apparatus has the mixed effect of more satisfactory gas, need the distance of two material inlets of control and the angle [alpha] of bullet and horizontal level, the horizontal or vertical distance of two side line material inlets 6, the diameter of lower central place straight tube 11, the percent opening of sieve plate 13, the ratio of the perforated area of sieve plate 13 and side direction annular space 12 areas.Thereby two strands of gases can be mixed in cylindrical shell 4 and back taper body 10 evenly, and from sieve plate 13 and side direction annular space 12, flow into the lower section catalyst bed, in the lower section catalyst bed, form distribution of gas relatively uniformly in suitable ratio.
In six sections insulation fix bed reactors, alkylated reaction takes place and generates ethylbenzene in benzene and ethene in beds.This reactor is in series by six sections beds, and benzene and ethene enter every section beds successively.The ethene of introducing from the external world is divided into 6 strands, and wherein one converges with main flow benzene, and the logistics 1 after converging enters the mouth from reactor head and 3 enters reactor.All the other 5 strands of ethene converge with the logistics of corresponding chilling benzene respectively, 5 bursts then (ethene+chilling benzene) logistics 2 enter intersegmental space separately respectively, and, entering next section beds together with converging from the reactor content of upstream, end product leaves reactor by the bottom gas vent.
The said intersegmental gas mixing apparatus of the present invention is investigated through large-scale fixed bed cold model experiment, and the result shows to have following advantage: simple in structure, easy for installation; The current-sharing effect is better, can make between multi-stage fixed-bed reactor region gas evenly mixed and reach desirable distribution of gas effect, has obtained better technical effect.
Description of drawings
Fig. 1 is a multistage insulation fixed bed reactor schematic diagram of the present invention;
Fig. 2 is the intersegmental gas mixing apparatus structure chart of multistage insulation fixed bed reactor of the present invention;
Fig. 3 is the intersegmental gas mixing apparatus plan structure figure of multistage insulation fixed bed reactor of the present invention;
In Fig. 1,1 is first kind of material; 2 is second kind of material; 3 is first kind of material inlet pipeline; 4 is reactor shell; 5 is beds; 6 is second kind of material inlet pipeline; 7 is intersegmental gas mixing apparatus; 8 is the gas vent pipeline.
In Fig. 2,9 is first kind of material inlet; 4 is reactor shell; 6 is the inlet of second kind of material; 10 is the back taper body; 11 is straight tube; 12 is the side direction annular space; 13 is sieve plate.D is the diameter of reactor, d
1Be the diameter of straight tube, d
2Be the diameter of sieve plate, Φ is the diameter of sieve aperture on the sieve plate, h
1Be the height of straight tube, h
2Be the height of side direction annular space passage, α is the angle of bullet and horizontal level.The percent opening of sieve plate is the perforated area of sieve plate and the ratio of sieve plate area.
In Fig. 3,4 is reactor shell; 6 is the inlet of second kind of material; 13 is sieve plate, and l is the horizontal range of two second kind of material inlet pipes.
The invention will be further elaborated below by embodiment.
The specific embodiment
[embodiment 1]
Adopt intersegmental as shown in Figure 1 gas mixing apparatus, reactor diameter D=600 millimeter, the diameter d of straight tube
1=140 millimeters, the diameter d of sieve plate
2=160 millimeters, the diameter of phi of sieve aperture=6 millimeter on the sieve plate, the height h of straight tube
1=100 millimeters, the height h of side direction annular space passage
2=65 millimeters, the horizontal range l=450 millimeter of two second kind of material inlet pipes, the angle [alpha] of bullet and horizontal level=45 °, the horizontal range of two second kind of material inlets is 75% with the ratio of reactor diameter, the straight tube diameter is 23.3% with the ratio of reactor diameter, the diameter of sieve plate is 26.7% with the ratio of reactor diameter, and the perforated area of sieve plate is 18.5% with the ratio of side direction annular space area, and the percent opening of sieve plate is 26.3%.
Under above condition and structural parameters, carry out intersegmental gas mixing apparatus design by the method for the invention, just can obtain more satisfactory gas flow effect.
[embodiment 2]
Adopt intersegmental as shown in Figure 1 gas mixing apparatus, reactor diameter D=1000 millimeter, the diameter d of straight tube
1=168 millimeters, the diameter d of sieve plate
2=168 millimeters, the diameter of phi of sieve aperture=8 millimeter on the sieve plate, the height h of straight tube
1=160 millimeters, the height h of side direction annular space passage
2=75 millimeters, the horizontal range l=850 millimeter of two second kind of material inlet pipes, the angle [alpha] of bullet and horizontal level=60 °, the horizontal range of two second kind of material inlets is 85% with the ratio of reactor diameter, the straight tube diameter is 16.8% with the ratio of reactor diameter, the diameter of sieve plate is 16.8% with the ratio of reactor diameter, and the perforated area of sieve plate is 25.3% with the ratio of side direction annular space area, and the percent opening of sieve plate is 45.1%.
Under above condition and structural parameters, carry out intersegmental gas mixing apparatus design by the method for the invention, just can obtain more satisfactory gas flow effect.
[embodiment 3]
Adopt intersegmental as shown in Figure 1 gas mixing apparatus, reactor diameter D=600 millimeter, the diameter d of straight tube
1=165 millimeters, the diameter d of sieve plate
2=165 millimeters, the diameter of phi of sieve aperture=6 millimeter on the sieve plate, the height h of straight tube
1=120 millimeters, the height h of side direction annular space passage
2=60 millimeters, the horizontal range l=420 millimeter of two second kind of material inlet pipes, the angle [alpha] of bullet and horizontal level=30 °, the horizontal range of two second kind of material inlets is 70% with the ratio of reactor diameter, the straight tube diameter is 27.5% with the ratio of reactor diameter, the diameter of sieve plate is 27.5% with the ratio of reactor diameter, and the perforated area of sieve plate is 12.6% with the ratio of side direction annular space area, and the percent opening of sieve plate is 18.4%.
Under above condition and structural parameters, carry out intersegmental gas mixing apparatus design by the method for the invention, just can obtain more satisfactory gas flow effect.
[comparative example 1]
Certain benzene is all identical with embodiment 1 with structural parameters with the condition of six sections insulation fix bed reactors of ethylene molecule sieve producing ethyl benzene through alkylation in gas phase, and unique difference is intersegmental employing tubular gas distributor.By analog computation, carrying out two strands of materials by the method for the invention mixes, same cross section uniformity maximum deviation adopts simple tubular type gas distributor less than 4.0% in its lower section catalyst bed, and same cross section uniformity maximum deviation is 7.2% in its lower section catalyst bed.
[comparative example 2]
The intersegmental gas mixing apparatus of six sections insulation fix bed reactors of the benzene of embodiment 2 and ethylene molecule sieve producing ethyl benzene through alkylation in gas phase makes simple tubular gas distributor into, and all conditions all condition with embodiment 2 is identical.Same cross section uniformity maximum deviation is less than 4.6% in the lower section catalyst bed of embodiment 2, and the same cross section of this comparative example uniformity maximum deviation is 8.8%.
[comparative example 3]
The intersegmental gas mixing apparatus of six sections insulation fix bed reactors of the benzene of embodiment 3 and ethylene molecule sieve producing ethyl benzene through alkylation in gas phase makes simple tubular gas distributor into, and all conditions all condition with embodiment 2 is identical.Same cross section uniformity maximum deviation is less than 4.3% in the lower section catalyst bed of embodiment 3, and the same cross section of this comparative example uniformity maximum deviation is 8.0%.
Claims (9)
1, a kind of multistage insulation fixed bed reactor, comprise reactor inlet (3), reactor shell (4), reactor outlet (8), be provided with 2～10 beds (5) in the reactor shell, intersegmental gas mixing apparatus (7) is set between beds (5), wherein each intersegmental gas mixing apparatus (7) comprises first kind of material inlet (9), reactor shell (4), second kind of material inlet (6), the built-in back taper body of reactor (10), straight tube (11), side direction annular space (12) and sieve plate (13), first kind of material inlet (9) and second kind of material inlet (6) lay respectively at the top of back taper body (10), the upper end of straight tube (11) links to each other with the lower end of back taper body (10), form side direction annular space (12) in the middle of the lower end of straight tube (11) and the sieve plate (13), and fix straight tube (11) diameter d by vertical lacing wire
1With the ratio of reactor diameter D be 10～40%, the angle α of back taper body (10) and horizontal level is 15～75 °, the diameter d of sieve plate (13)
2With the ratio of reactor diameter D be 10～45%, the percent opening of sieve plate (13) is 0～75%, the area ratio of the perforated area of sieve plate (13) and side direction annular space (12) is 0～35%, reactor shell (4), straight tube (11) and sieve plate (13) have concentric shafts.
2,, it is characterized in that second kind of material inlet (6) has two in each intersegmental gas mixing apparatus (7) according to the described multistage insulation fixed bed reactor of claim 1.
3, according to the described multistage insulation fixed bed reactor of claim 2, the Way in that it is characterized in that above-mentioned two second kind material inlet (6) is parallel to round tangential direction, and the center symmetry, the horizontal range 1 between two second kind material inlet (6) is 50～95% of reactor diameter D.
4,, it is characterized in that the horizontal range 1 between two second kind material inlet (6) is 70～90% of reactor diameter D according to the described multistage insulation fixed bed reactor of claim 3.
5,, it is characterized in that straight tube (11) diameter d according to the described multistage insulation fixed bed reactor of claim 1
1With the ratio of reactor diameter D be 15～30%.
6,, it is characterized in that the back taper body (10) and the angle α of horizontal level are 30～60 ° according to the described multistage insulation fixed bed reactor of claim 5.
7,, it is characterized in that the back taper body (10) and the angle α of horizontal level are 30～60 ° according to the described multistage insulation fixed bed reactor of claim 1.
8, according to the described multistage insulation fixed bed reactor of claim 1, the percent opening that it is characterized in that sieve plate (13) is 15～50%.
9,, it is characterized in that the perforated area of sieve plate (13) and the area ratio of side direction annular space (12) are 10～30% according to the described multistage insulation fixed bed reactor of claim 1.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2004100676294A CN100349647C (en) | 2004-10-29 | 2004-10-29 | Multi-segment insulation fix bed reactor |
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|---|---|---|---|
| CNB2004100676294A CN100349647C (en) | 2004-10-29 | 2004-10-29 | Multi-segment insulation fix bed reactor |
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| CN1765481A CN1765481A (en) | 2006-05-03 |
| CN100349647C true CN100349647C (en) | 2007-11-21 |
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Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101147852B (en) * | 2006-09-20 | 2010-09-01 | 中国石油化工股份有限公司 | Multistage insulation fixed bed reactor |
| KR20130077842A (en) | 2010-05-24 | 2013-07-09 | 엑스턴도 인코포레이티드 | Device for loading catalyst into a reactor vessel |
| US9149778B2 (en) | 2010-05-24 | 2015-10-06 | Extundo Incorporated | Device and method for dispensing catalyst pellets |
| US9138709B2 (en) | 2010-05-24 | 2015-09-22 | Extundo Incorporated | Device and method for dispensing pellets |
| CN101857808B (en) * | 2010-06-17 | 2014-02-26 | 宁夏宝塔石化集团有限公司 | Method for preparing gasoline from liquefied gas through aromatization and fixed bed reactor |
| CN107213853A (en) * | 2016-03-22 | 2017-09-29 | 河南永大化工有限公司 | A kind of laboratory multistage insulation fixed bed reactor |
| CN109351288A (en) * | 2018-10-18 | 2019-02-19 | 中石化广州工程有限公司 | A kind of technique controlling the temperature rise of alkylation reactor bed |
| CN109925972B (en) * | 2019-04-23 | 2019-12-31 | 宁波巨化新材料有限公司 | Multi-section fixed bed reactor for reaction of synthesizing n-propanol |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6265735A (en) * | 1985-09-18 | 1987-03-25 | Mitsubishi Heavy Ind Ltd | Reaction vessel |
| CN1033753A (en) * | 1987-08-14 | 1989-07-12 | 戴维麦基公司 | The gas that is used for reactor mixes, distributor |
| CN2603688Y (en) * | 2003-02-26 | 2004-02-18 | 浙江大学 | Fluidized bed polymerization reaction equipment |
-
2004
- 2004-10-29 CN CNB2004100676294A patent/CN100349647C/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6265735A (en) * | 1985-09-18 | 1987-03-25 | Mitsubishi Heavy Ind Ltd | Reaction vessel |
| CN1033753A (en) * | 1987-08-14 | 1989-07-12 | 戴维麦基公司 | The gas that is used for reactor mixes, distributor |
| CN2603688Y (en) * | 2003-02-26 | 2004-02-18 | 浙江大学 | Fluidized bed polymerization reaction equipment |
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| CN1765481A (en) | 2006-05-03 |
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