CN1219736C - Reaction method of dimethyl benzene isomerization and methylbenzene disproportionation and its equipment - Google Patents
Reaction method of dimethyl benzene isomerization and methylbenzene disproportionation and its equipment Download PDFInfo
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- CN1219736C CN1219736C CN 01126968 CN01126968A CN1219736C CN 1219736 C CN1219736 C CN 1219736C CN 01126968 CN01126968 CN 01126968 CN 01126968 A CN01126968 A CN 01126968A CN 1219736 C CN1219736 C CN 1219736C
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Abstract
The present invention discloses a reaction method and reaction equipment for xylene isomerization and toluene disproportionation. The reaction equipment of the reaction method is a circular pressure container (8) provided with a catalytic bed (5), a gas inlet (1) and a gas outlet (13) are positioned at the same end of the reaction equipment, the catalytic bed (5) is composed of an external porous wall (7) and an internal circular porous wall cylinder (6) and is filled with catalysts, and gas can flow in a backward centrifugal type in the reaction equipment. The reaction method has the advantages high catalyst utilization rate, and the reaction equipment has the advantages of low pressure drop, simple structure and convenient catalyst loading and unloading. The reaction method and the reaction equipment are also suitable for other middle-pressure, low-pressure or negative-pressure gas solid phase catalytic reactions.
Description
Technical field
The invention belongs to the hydro carbons processing technique field, relate in a kind of being applicable to, the gas-solid catalysis method and the reaction unit of low pressure or negative pressure, particularly a kind of reaction method and reaction unit that is applicable to xylene isomerization, toluene disproportionation and ethyl benzene dehydrogenation preparation of styrene.
Background technology
Existing xylene isomerization, toluene disproportionation, and in the reaction method of ethyl benzene dehydrogenation preparation of styrene, generally adopt radial reactor, gas is coflow at flow manifold and afflux runner, is unfavorable for gas uniform distribution vertically thus.And radial reactor adopts control pressure drop very big gas distributor to realize the uniform of gas usually, as causing 1 times or be several times as much as the pressure drop of catalytic bed pressure drop by porous tube among English Patent 1118750 and the patent CN87102931.Or employing is as the measure of Chinese patent 96114363.0 baroque taper baffles or tapered runner.
And all kinds of axle radial flow two dimension flow reactors that adopted in the existing improved reaction method, as United States Patent (USP) 4372920,4405562, Chinese patent ZL96114363.0 is than traditional radial reactor, as United States Patent (USP) 3918918,4181701, Chinese patent ZL86200368.7 technical development major step, simplified structure of reactor, improved the utilization ratio of catalyzer, but still there is the unreasonable part of streamline in the catalyst sealing district, or there is a local stagnant area, maybe channel might appear, risk of short-circuits, for safe consideration to reactor, increase the height in catalyst sealing district so that have to, so reduced the utilization ratio of reactor catalyst, may cause the increase of side reaction or the aggravation of coking again.
Summary of the invention
One of technical issues that need to address of the present invention provide the high xylene isomerization of a kind of catalyst utilization, toluene disproportionation, and the reaction method of ethyl benzene dehydrogenation preparation of styrene, to overcome the above-mentioned defective that prior art exists.
Another technical problem that the present invention need solve provides and a kind ofly can realize aforesaid method, and realizes low control pressure drop, simple in structure and loading and unloading catalyzer reaction unit easily under the uniform fluid distribution condition simultaneously satisfying.
For xylene isomerization and toluene disproportionation process, contain a large amount of hydrogen in its reaction medium, its hydrogen hydrocarbon mol ratio is up to 4～6 times or higher, and a large amount of gas circulation makes the pressure drop that reduces reactor become energy-conservation key point; Ethylbenzene dehydrogenation reaction is the reaction of carrying out under the negative pressure, contains a large amount of water vapors in the reaction medium as thermal barrier, and its water hydrocarbon mol ratio is up to 7～9 times, therefore, for satisfying under the low control pressure drop condition, gas is axially uniform in reactor, and the contriver thinks can adopt following design:
1. gas feed and outlet are positioned at the same end of reactor, and it is reverse relative mobile that gas is done in flow manifold and afflux runner, because the difference of static pressure difference is vertically very little between two runners, thereby very helps the uniform distribution of gas;
2. gas is done radially centrifugal flowing from inside to outside, has avoided ecto-entad to make the mobile high-temperature gas that causes of radial inflow and has been positioned at the outside thermosteresis of housing, helps the even of the interior axial temperature of reactor;
3. the interior porous wall tube that has suitable large opening rate when realizing lower control pressure drop, has guaranteed gas uniform distribution vertically as gas distributor;
4. the top of catalytic bed is unlimited fully, and not only apparatus structure is simple, and the loading and unloading catalyzer is very convenient;
5. between catalyst sealing district and radial bed district, the current control section is set, can reduces catalyst sealing district height thus, optimized the streamline distribution of this district's bed, thereby improved the utilization ratio of catalyzer.
According to above-mentioned design, the present invention proposes technical scheme as described below:
The reaction method of xylene isomerization of the present invention and toluene disproportionation and ethylbenzene dehydrogenation can carry out in a kind of reverse centrifugal radial reactor in the following processing parameter condition that provides;
Said reverse centrifugal radial reactor is made of the round pressure container that has catalytic bed;
Said catalytic bed comprises:
One with the axis coaxle of pressurized vessel and be connected with gas feed circular in the porous wall tube, the porous wall tube constitutes the flow manifold of a gas in this circle, porous wall tube top is provided with the catalyst sealing district of one section not perforate in circular, is radially bed district of catalyzer below the catalyst sealing district;
Outer porous wall axis coaxle and that be connected with pneumatic outlet with pressurized vessel, outer porous wall is done adjacent circumferential arrangement institute by a plurality of segmental porous hollow components along nearly wall place in the round pressure container and is constituted, and a plurality of segmental porous hollow components constitute an afflux runner;
Gas feed and pneumatic outlet are arranged at the same end of pressurized vessel;
Solid catalyst is loaded in space in circular between porous wall tube and the outer porous wall, and its top is opened wide.
Porous wall tube in gas is entered by gas feed, by the interior distributed aperture on the interior porous wall tube to flowing into catalytic bed, and then enter outer porous wall by outer distribution hole from inside to outside and make centrifugal flow, flow out by the outlet that is positioned at same end with import then, this shows, gas flow manifold and afflux runner be do reverse relative mobile.
Accompanying drawing and explanation
Fig. 1 gas feed of the present invention and pneumatic outlet are arranged on the structure of reactor synoptic diagram at top.
Fig. 2 gas feed of the present invention and pneumatic outlet are arranged on the structure of reactor synoptic diagram of bottom.
Reaction unit cross-sectional structure synoptic diagram among Fig. 3 Fig. 1.
Porous wall barrel structure synoptic diagram in Fig. 4 is a kind of.
Porous wall barrel structure synoptic diagram in Fig. 5 another kind.
Fig. 6 cell structure synoptic diagram.
A-A is to synoptic diagram among Fig. 7 Fig. 6.
A kind of fan-shaped porous hollow component cross sectional representation of Fig. 8.
The another kind of fan-shaped porous hollow component cross sectional representation of Fig. 9.
Embodiment
In the raw material hydrogen hydrocarbon mol ratio be 6～8, toluene/C
9Aromatic hydrocarbons is that 60/40～100/0 (wt), temperature of reaction are that 350～450 ℃, reaction pressure are that hydrogen hydrocarbon mol ratio is 4～6 in the toluene disproportionation process method of 3.0～3.2MPa and the raw material, hydro carbons is C
8Aromatic hydrocarbons, temperature of reaction are that 385～430 ℃, reaction pressure are the reactor that the xylene isomerization reaction method of 0.8～1.5MPa adopts Fig. 1 or two kinds of embodiments shown in Figure 2.
By Fig. 1 and Fig. 3 as seen, said reverse centrifugal radial reactor is made of the round pressure container 8 that has catalytic bed;
Said catalytic bed comprises:
One with the axis coaxle of pressurized vessel 8 and be connected with gas feed 1 circular in porous wall tube 6, porous wall tube 6 constitutes the flow manifold 3 of a gas in this circle, porous wall tube 6 tops are provided with the catalyst sealing district 12 of one section not perforate in circular, and the catalyst sealing district is radially bed district 5 below 12;
Outer porous wall 7 axis coaxle and that be connected with pneumatic outlet 13 with pressurized vessel 8, outer porous wall 7 is done adjacent circumferential arrangement institute by a plurality of segmental porous hollow components 15 along nearly wall place in the round pressure container 8 and is constituted, and a plurality of segmental porous hollow components 15 constitute an afflux runner 4;
Gas feed 1 and pneumatic outlet 13 are arranged at the upper end of pressurized vessel;
The cross-sectional area of afflux runner 4 is 1～5 with the ratio of the cross-sectional area of flow manifold 3;
As Fig. 4, Fig. 5, Fig. 6 and Fig. 7 as seen, interior porous wall tube 6 can adopt the porous plate of multiple structure to roll to form.Fig. 4 is that bilayer is close to porous plate, is made up of slab 16 and multihole lamina 17.Fig. 5 is double-deck built on stilts porous plate, make somebody a mere figurehead with horizontal and vertical support bar 18 in the middle of slab 16 and the multihole lamina 17, multihole lamina 17 is close to a side of catalyzer, the aperture in the distribution hole 2 of being opened is less than the size of granules of catalyst, can open circular hole, bar hole etc., or adopt silk screen or adopt as shown in Figure 6 grid, the gap between the grizzly bar 19 of grid is less than the size of granules of catalyst, Fig. 7 be among Fig. 6 A-A to synoptic diagram.The percentage of open area of thin plate 17 generally remains between 20～40%, and the percentage of open area of grid 16 remains between 20～60%, and slab 16 is opened circular hole usually, and percentage of open area is generally between 0.5%～20%.Since the invention process gas reverse relative mobile structure in flow manifold 3 and afflux runner 4, interior porous wall tube 6 as gas distributor can keep sizable percentage of open area, the control pressure drop that makes gas distributor only for the catalytic bed pressure drop 50% or lower, when realizing low control pressure drop, guaranteed gas uniform distribution vertically.
Interior porous wall tube 6 equates with the height H of outer porous wall 7, but the height of opening area and inconsistent, the height H of the opening area of interior porous wall tube 6
iBe lower than the height H of the opening area of outer porous wall 7, promptly outer porous wall 7 inboards are all perforates from top to bottom, and the height in catalyst sealing district 12 is Δ H
i, radially the height in bed district 5 is H
i, the height Δ H in catalyst sealing district 12
iBe 0.2～5 times of bed district 5 radial thicknesss radially.In catalyst sealing district 12, there are the gas axial flow and the two-dimentional flow region of radial flow from inside to outside from bottom to top simultaneously, therefore, simplify structure of reactor, improved catalyst utilization.
In catalyst sealing district 12 with current control section 11 radially also is set, its height Δ H ' between the bed district 10
iGenerally be catalyst sealing district 12 height Δ H
i0.2～2.0 times.The percentage of open area of the slab 16 on the interior porous wall tube 6 of current control section 11 be the slab 16 on the interior porous wall tube 6 in radially bed district 5 percentage of open area 20%～80%, or from bottom to top by progressively increasing progressively.The purpose that current control section 11 is set is the streamline distribution of further optimizing in the catalyst sealing district 12, reduces the height of catalyst sealing, more helps improving the utilization ratio of catalyzer.
Fig. 8 and Fig. 9 are respectively the cross sectional representation of two kinds of difform porous hollow components 15, porous hollow component 15 is a long strip shape, identical with the height of catalytic bed, be close to a side of catalyzer and offer outer distribution hole 9, its percentage of open area is generally 20～40%, can open circular hole or bar hole, and a side of pressing close to pressurized vessel 8 is not perforates.
Gas is such mobile in the reactor of Fig. 1, the flow manifold 3 that porous wall tube 6 constituted in gas was entered by gas feed 1, by the bed district 5 radially of interior distribution hole 2 radial inflows on the interior porous wall tube 6, and then enter the afflux runner 4 that outer porous wall 7 constitutes by the outer distribution hole 9 on the outer porous wall 7 from inside to outside and make centrifugal flow, gas is to make reverse relative mobile in flow manifold 3 and afflux runner 4.
Structure and Fig. 1 of Fig. 2 are basic identical, but gas inlet tube 1 and outlet pipe 13 are located on the lower end of pressurized vessel 8.
The reaction method and the reaction unit that adopt the present invention to propose compared with prior art have the following advantages:
1. the control pressure drop of interior porous wall gas distributor when realizing lower control pressure drop, has guaranteed gas uniform distribution vertically less than 50% of catalytic bed pressure drop;
2. optimized the streamline distribution in the catalyst sealing district, the ratio of effectively regulating axial flow and radial flow had both been avoided channel or stagnant area in the catalyst sealing district, can effectively reduce the height in catalyst sealing district again, had improved the utilization ratio of catalyzer;
3. avoided high-temperature gas to be positioned at the outside thermosteresis of housing, axial temperature is even in the reactor.
4. reaction unit is simple in structure, and the loading and unloading catalyzer is very convenient;
Claims (12)
1. the reaction method of xylene isomerization that in reactor, carries out and toluene disproportionation, it is characterized in that, this method is carried out in a kind of reverse centrifugal radial reactor, and this reverse centrifugal radial reactor is made of the round pressure container (8) that has catalytic bed;
Said catalytic bed comprises:
One with the axis coaxle of pressurized vessel (8) and be connected with gas feed (1) circular in porous wall tube (6), porous wall tube (6) constitutes the flow manifold (3) of a gas in this circle, porous wall tube (6) top is provided with the catalyst sealing district (12) of one section not perforate in circular, and catalyst sealing district (12) following to be radially bed district (5);
Outer porous wall (7) axis coaxle and that be connected with pneumatic outlet (13) with pressurized vessel (8), outer porous wall (7) is made adjacent circumferential by a plurality of segmental porous hollow components (15) nearly wall place in the round pressure container (8) and is arranged institute and constitute a plurality of segmental porous hollow components (15) formation afflux runner (4);
Gas feed (1) and pneumatic outlet (13) are arranged at the upper end or the lower end of pressurized vessel (8) simultaneously.
2. the method for claim 1 is characterized in that, the ratio of the cross-sectional area of the cross-sectional area of afflux runner (4) and flow manifold (3) is 1～5.
3. the method for claim 1 is characterized in that, the height Δ H of catalyst sealing district (12)
iBe 0.2～5 times of bed district (5) radial thickness radially.
4. the method for claim 1 is characterized in that, catalyst sealing district (12) and current control section (11) radially is set between bed district (10), its height Δ H '
iBe catalyst sealing district (12) height Δ H
i0.2～2.0 times, the percentage of open area of the slab (16) on the interior porous wall tube (6) of current control section (11), be the radially slab (16) on the interior porous wall tube (6) of bed district (5) percentage of open area 20%～80%, or from bottom to top by progressively increasing progressively.
5. the method for claim 1 is characterized in that, interior porous wall tube (6) is close to porous plate for the bilayer of being made up of slab (16) and multihole lamina (17), and slab (16) percentage of open area is 0.5%～20%.
6. the method for claim 1 is characterized in that, interior porous wall tube (6) is by the porous plate of making somebody a mere figurehead with horizontal and vertical support bar (18) in the middle of slab (16) and the multihole lamina (17) or adopts grid that slab (16) percentage of open area is 0.5%～20%.
7. the used device of the arbitrary described method of claim 1～6 is characterized in that, this device is made of the round pressure container (8) that has catalytic bed;
Said catalytic bed comprises:
One with the axis coaxle of pressurized vessel (8) and be connected with gas feed (1) circular in porous wall tube (6), porous wall tube (6) constitutes the flow manifold (3) of a gas in this circle, porous wall tube (6) top is provided with the catalyst sealing district (12) of one section not perforate in circular, and catalyst sealing district (12) following to be radially bed district (5);
Outer porous wall (7) axis coaxle and that be connected with pneumatic outlet (13) with pressurized vessel (8), outer porous wall (7) is made adjacent circumferential by a plurality of segmental porous hollow components (15) nearly wall place in the round pressure container (8) and is arranged institute and constitute a plurality of segmental porous hollow components (15) formation afflux runner (4);
Gas feed (1) and pneumatic outlet (13) are arranged at the upper end or the lower end of pressurized vessel (8) simultaneously.
8. device as claimed in claim 7 is characterized in that, the ratio of the cross-sectional area of the cross-sectional area of afflux runner (4) and flow manifold (3) is 1～5.
9. device as claimed in claim 8 is characterized in that, the height Δ H of catalyst sealing district (12)
iBe 0.2～5 times of bed district (5) radial thickness radially.
10. device as claimed in claim 8 is characterized in that, catalyst sealing district (12) and current control section (11) radially is set between bed district (10), its height Δ H '
iBe catalyst sealing district (12) height Δ H
i0.2～2.0 times, the percentage of open area of the slab (16) on the interior porous wall tube (6) of current control section (11), be the radially slab (16) on the interior porous wall tube (6) of bed district (5) percentage of open area 20%～80%, or from bottom to top by progressively increasing progressively.
11. device as claimed in claim 8 is characterized in that, interior porous wall tube (6) is close to porous plate for the bilayer of being made up of slab (16) and multihole lamina (17), and slab (16) percentage of open area is 0.5%～20%.
12. device as claimed in claim 8 is characterized in that, interior porous wall tube (6) is by the porous plate of making somebody a mere figurehead with horizontal and vertical support bar (18) in the middle of slab (16) and the multihole lamina (17) or adopts grid that slab (16) percentage of open area is 0.5%～20%.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01126968 CN1219736C (en) | 2001-10-08 | 2001-10-08 | Reaction method of dimethyl benzene isomerization and methylbenzene disproportionation and its equipment |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01126968 CN1219736C (en) | 2001-10-08 | 2001-10-08 | Reaction method of dimethyl benzene isomerization and methylbenzene disproportionation and its equipment |
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| CN1341585A CN1341585A (en) | 2002-03-27 |
| CN1219736C true CN1219736C (en) | 2005-09-21 |
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| CN 01126968 Expired - Fee Related CN1219736C (en) | 2001-10-08 | 2001-10-08 | Reaction method of dimethyl benzene isomerization and methylbenzene disproportionation and its equipment |
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| CN102258962B (en) * | 2011-05-24 | 2013-07-31 | 徐志刚 | Gas solid phase catalytic reactor |
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