CN1546217A - Catalytic reforming and catalytic dehydrogenation centrifugal type fixed bed radial reactor - Google Patents
Catalytic reforming and catalytic dehydrogenation centrifugal type fixed bed radial reactor Download PDFInfo
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- CN1546217A CN1546217A CNA2003101093236A CN200310109323A CN1546217A CN 1546217 A CN1546217 A CN 1546217A CN A2003101093236 A CNA2003101093236 A CN A2003101093236A CN 200310109323 A CN200310109323 A CN 200310109323A CN 1546217 A CN1546217 A CN 1546217A
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Abstract
The invention discloses a kind of fixed bed reactor for catalytic reforming and dehydrogenation, the reactor uses a round pressure container which has a catalytic bed. The inlet and the outlet is at one side of the container, the catalytic bed is made up of outer multi-hole wall and round inner multi-hole wall, catalyst is filled in them, there has a cover sealing structure on the catalyst, the round inner multi-hole wall can uses variable hole-rate or zone structure. The reacting gas in the device flows centrifugally, the gas in the centre inner barrel and multi-hole outer barrel flow reversely.
Description
Technical field
The invention belongs to the hydro carbons processing technique field, relate in a kind of being applicable to, the fixed bed gas-solid catalysis device of low pressure or negative pressure, particularly a kind of fixed bed that is applicable to catalytic reforming and catalytic dehydrogenation is reaction unit radially.
Background technology
For catalytic reforming and catalytic dehydrogenation, contain a large amount of hydrogen in its reaction medium, its hydrogen hydrocarbon mol ratio is up to 6-10 times or higher, and a large amount of gas circulation makes the pressure drop that reduces reactor become raising catalyst utilization and energy-conservation key point.In the reaction method of existing catalytic reforming and catalytic dehydrogenation,, adopt the catalyzer of small grain size usually for improving catalyst utilization; For reducing the pressure drop of reactor, reduce the power consumption of recycle compressor, adopt radial reactor usually.And existing radial reactor technology, U.S. Pat 2,683,654, US4,244,922 and US5,202,097 have introduced following structural response device: reactor comprises annular catalyst in a cylindrical vessel and the container, on the end socket of the top of this cylindrical vessel, be provided with reacting gas inlet, on bottom head, be provided with reaction gas outlet; Comprise with the coaxial setting of cylindrical vessel in cylindrical vessel, the inner core of the porous wall that is arranged in order from inside to outside and porous wall urceolus (or sector drum) form the ring catalyst bed between porous wall inner core and the porous wall urceolus; Communicate with the import of top reactant gases between cylindrical vessel sidewall and the porous wall urceolus, constitute the flow manifold of reactant gases; Inner core is connected with placing cylindrical vessel bottom reaction gas outlet, constitutes reactant gases afflux runner.Reactant gases is such mobile, reactant gases enters the upper space of reactor from reacting gas inlet, enter the flow manifold that the porous urceolus constitutes downwards, radially the outer wall from reactor passes through the annular beds, enter the afflux runner that constitutes by the center inner core, flow out by the outlet of reactant gases downwards then, form the enterprising radial inflow Z type flow pattern that goes out down.
Investigate the flow pattern of above-mentioned structure of reactor and reactant gases, there are the following problems:
1. reactant gases is coflow at flow manifold and afflux runner, is unfavorable for fluid uniform distribution vertically thus.Be to realize the fluidic uniform distribution, have to adopt the very big gas distributor of control pressure drop, 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 GB1118750 and the Chinese patent CN7102931.Or adopt as U.S. Pat 5,885 444 and the taper baffle of Chinese patent CN961143630 or the structure of tapered runner.
2. U.S. Pat 3,099, and 208 think that there is the dead band in the part in catalyst sealing, for fear of coking, improve the utilization ratio of this place's catalyzer, propose catalyst sealing place cone structure, but cause the increase and the inside reactor structure complicated of catalyst sealing height like this.
3. reactor entad adopts and flows, and the flow manifold of reactant gases between cylindrical vessel sidewall and porous wall urceolus flows downward, and owing to calorific loss, can cause the difference of bed axial temperature, and is particularly unfavorable to thermo-negative reaction.
4. the radial inflow of ecto-entad is flowed, the incompatible requirement that increases volumetric reaction catalytic reforming and catalytic dehydrogenation that increases along the reaction process molecular weight, thereby U.S. Pat 5,885,442 adopt the centrifugal flow pattern of reactant gases, help obtaining higher octane value gasoline and improve operational load, but do not solve because of the big defective of Z type flow pattern sparger control pressure drop.
Summary of the invention
The technical issues that need to address of the present invention are:
(1) provides the reaction method of high catalytic reforming of a kind of catalyst utilization and catalytic dehydrogenation, guarantee reactant gases uniform distribution vertically;
Guarantee under the equally distributed vertically condition of reactant gases that (2) percentage of open area of porous tube further reduces the pressure drop of reactor in improving;
(3) avoided the thermosteresis of reactant gases in the flow manifold of center, made the axial temperature of catalytic bed more even.
(4) diameter of axle improves the utilization ratio of catalyst sealing to flowing in the catalyst sealing.
The present invention solves the problems of the technologies described above with this by a kind of centrifugal radial catalytic reforming and catalytic dehydrogenating reaction device are provided, and overcomes the defective that exists in the prior art simultaneously.
Design of the present invention is such:
1. gas feed and outlet are positioned at the same end of reactor, it is reverse relative mobile that gas is done in flow manifold and afflux runner, form and go out or advance down the П type flow pattern that goes out down on enterprising, because the difference of static pressure difference is vertically very little between two runners, thereby very help the uniform distribution of gas;
2. the cross section of fluid channel of having optimized flow manifold and afflux runner is long-pending, can use the interior porous barrel that has than large opening rate as gas distributor thus, has further reduced the pressure drop of radial reactor.
3. flow manifold adopt to become percentage of open area or becomes the diameter technology, has overcome the bed voidage variation defective vertically that the long-term operation of catalyzer causes, and makes fluid more even along the reactor axial distribution.
4. gas is done 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;
5. gas is done centrifugal flow from inside to outside, matches with the characteristics of reformation that increases volume or dehydrogenation reaction, very helps the carrying out that reacts.
According to above-mentioned design, the present invention proposes technical scheme as described below:
Centrifugal fixed bed of the present invention radially catalytic reforming, catalytic dehydrogenating reaction device is to be made of the round pressure container that has annular catalytic bed, comprising:
Be provided with reacting gas inlet, reaction gas outlet and catalyzer discharge tube on the wall of this cylindrical vessel, it is characterized in that: described reacting gas inlet and reaction gas outlet all place the top or the bottom of cylindrical vessel simultaneously.
In cylindrical vessel, comprise: with the coaxial setting of cylindrical vessel, the porous wall inner core of not perforate of upper portion side wall and the urceolus of vesicular structure arranged from inside to outside according to this; The urceolus of said vesicular structure is the porous wall urceolus or makes adjacent circumferential by a plurality of fan-shaped, hollow components along nearly wall place in the bulge and arrange the urceolus that is constituted, and wherein offers the distribution hole by catalyzer one side, and by cylindrical vessel one not perforate of side.Said porous wall inner core is for to be close to multihole lamina by the porous slab, or by built on stilts with support bar in the middle of porous slab and the multihole lamina, or is close to structure by the bilayer that porous slab and grid are formed, the identical up and down or difference up and down of the percentage of open area of said porous slab; The shape of inner core can be cylinder, cone or become the trapezoidal cylinder of diameter.Described inner core is connected with the reacting gas inlet that places cylindrical vessel top (or bottom), constitutes the reactant gases flow manifold.Loading catalyst between inner core and the urceolus; Catalyst sealing is established in the catalytic bed top, the certain thickness inert solid particle material of catalyst sealing top loading, the cover plate for sealing structure is set above, and there is certain height at the outer gland sealing tube edge of cover plate for sealing structure far from the inner core aperture area, a mobile radial flow that is of catalyst sealing inner fluid.Between porous wall urceolus and the cylindrical vessel sidewall or segmental porous hollow component constitute reactant gases afflux runner, reactant gases afflux runner is connected with the reaction gas outlet that places cylindrical vessel top (or bottom).
Description of drawings
Fig. 1 centrifugal fixed bed of the present invention is catalytic reforming, catalytic dehydrogenating reaction device structural representation radially
Wherein: the 1-reacting gas inlet; The 2-reaction gas outlet; 3-reactant gases flow manifold;
4-reactant gases afflux runner; The 5-catalytic bed; The 6-inner core;
7-porous wall urceolus; The 8-cylindrical vessel; The 9-catalyst sealing
The 10-inert particle material; 11-catalytic bed top seal structure; 12-catalyzer discharge tube;
The centrifugal П type of Fig. 2 another kind of the present invention fixed bed is catalytic reforming, catalytic dehydrogenating reaction device structural representation radially
Wherein: the 1-reacting gas inlet; The 2-reaction gas outlet.3-reactant gases flow manifold;
4-reactant gases afflux runner; 5-catalytic bed 6-inner core;
7-porous wall urceolus 8-cylindrical vessel; The 9-catalyst sealing
The 10-inert particle material; 11-catalytic bed top seal structure; 12-catalyzer discharge tube;
The centrifugal П type of Fig. 3 another kind of the present invention fixed bed is catalytic reforming, catalytic dehydrogenating reaction device structural representation radially
Wherein: 1-reacting gas inlet 2-reaction gas outlet.3-reactant gases flow manifold;
4-reactant gases afflux runner; The 5-catalytic bed; The 6-inner core;
7-porous wall urceolus 8-cylindrical vessel 9-catalyst sealing; The 10-inert particle material;
11-catalytic bed top seal structure; 12-catalyzer discharge tube 13-manhole
The change percentage of open area porous slab synoptic diagram in a kind of rectangular cloth of Fig. 4 hole
Wherein: 14-porous slab; 15-distribution hole;
The change percentage of open area porous slab synoptic diagram in the another kind of equilateral triangle cloth of Fig. 5 hole
Wherein: 14-porous slab; 15-distribution hole;
Porous tube synoptic diagram in a kind of taper of Fig. 6
Wherein: 14-porous slab; 15-distribution hole;
The another kind of interior porous tube synoptic diagram of diameter that becomes of Fig. 7
Wherein: 14-porous slab; 15-distribution hole;
A kind of fan-shaped porous hollow component cross sectional representation of Fig. 8.
The fan-shaped porous hollow component of 16-; 17-distribution hole.
The another kind of fan-shaped porous hollow component cross sectional representation of Fig. 9.
The fan-shaped porous hollow component of 16-; 17-distribution hole
The present invention is further illustrated below in conjunction with accompanying drawing, and institute's accompanying drawing of painting just helps to understand the present invention, and it does not limit protection scope of the present invention:
As seen from Figure 1, said centrifugal radial catalytic reforming of the present invention and catalytic dehydrogenating reaction device comprise:
In cylindrical vessel 8, comprise: with cylindrical vessel 8 coaxial settings, arrange according to this from inside to outside not perforate of upper portion side wall, bottom perforate highly for the porous wall inner core 6 of H and all perforate highly be the urceolus 7 of the vesicular structure of H ';
Described inner core 6 is connected with placing cylindrical vessel 8 top reacting gas inlets 1, constitute the flow manifold 3 of reactant gases, form catalytic bed 5 between inner core 6 and the urceolus 7, form reactant gases afflux runner 4 between porous wall urceolus and cylindrical vessel 8 sidewalls, or itself constitute reactant gases afflux runner 4 by segmental porous hollow component 16, reactant gases afflux runner 4 is connected with the reaction gas outlet 2 that places cylindrical vessel 8 tops, and the ratio of the cross-sectional area of reaction aerogenesis body afflux runner 4 and the cross-sectional area of reactant gases flow manifold 3 is advisable with 1～3;
Described catalytic bed 5 tops are provided with one section catalyst sealing 9 and inert particle material 10, the height Δ H of catalyst sealing 9 is 0.2～5 times of bed radial thickness, the thickness of inert particle material 10 is 0.1～0.5 times of bed radial thickness, the inert material top is provided with beds sealed structure 11, the outer gland sealing tube of sealed structure is Δ H ' apart from the height of inner core 6 aperture area, Δ H ' is 0.2～1.0 times of catalyst sealing height Δ H, with the diameter of axle the making full use of to mobile and catalyst sealing of guaranteeing reactant gases.
Inner core 6 is by porous slab 14 and multihole lamina is middle forms with built on stilts the rolling of horizontal and vertical support bar, and the percentage of open area of multihole lamina is 20～40%; Or be close to structure by the bilayer that porous slab 14 and grid are formed and roll and form, the voidage of grid is 25～50%; The percentage of open area of described porous slab 14 is 1%～15%, the perforate 15 of porous slab 14 can be adopted even perforate from top to bottom, also can adopt the piecewise uniform perforate, segmentation from top to bottom increases percentage of open area, the bottom opening rate is 100～200% of a top percentage of open area, be illustrated in figure 4 as the change percentage of open area porous slab synoptic diagram in a kind of rectangular cloth hole, top-portion apertures spacing a1 is 100～150% of underpunch spacing a2; Be illustrated in figure 5 as the change percentage of open area porous slab synoptic diagram in another kind of equilateral triangle cloth hole, top-portion apertures spacing a1 is 100～150% of underpunch spacing a2.Described inner core 6 also can adopt and become the diameter technology, and the top of inner core is different with base diameter, and base diameter is greater than top diameter, and the catalyst thickness of top bed is 100～200% of a bottom thickness; Shown in Figure 6 is a kind ofly rolls the taper inner tube structure that forms by porous slab 14, and shown in Figure 7 is another kind ofly rolls the trapezoidal change diameter inner tube structure that forms by porous slab 14.
Since the invention process reactant gases reverse relative mobile structure in flow manifold 3 and afflux runner 4, interior porous wall tube 6 as the reactant gases sparger can keep sizable percentage of open area, make the control pressure drop of reactant gases sparger only be the 10-50% of catalytic bed pressure drop or lower, when realizing low control pressure drop, guaranteed reactant gases uniform distribution vertically.Simultaneously inner core 6 adopts and becomes percentage of open area or become the diameter technology, has overcome the phenomenon that bed voidage variation vertically that the long-term operation of catalyzer causes causes the bed pressure drop inequality, makes fluid more even along the reactor axial distribution.
Said urceolus 7 is made adjacent circumferential along nearly wall places in the bulge 8 and is arranged the urceolus that is constituted for the porous wall urceolus or by a plurality of fan-shaped, hollow components 16, wherein offers distribution hole 17 by catalyzer one side, and by cylindrical vessel 8 one not perforates of side; Said porous wall urceolus can be by forming with built on stilts the rolling of horizontal and vertical support bar in the middle of porous slab and the multihole lamina, and the percentage of open area of multihole lamina is 20～40%, and the percentage of open area of porous slab is 20%～40%; Or form by grid, the voidage of grid is 25～50%.Fig. 8 and Fig. 9 are respectively the cross sectional representation of two kinds of difform porous hollow components 16, porous hollow component 16 is a long strip shape, aspect ratio catalyzer cover plate for sealing structure is slightly high, the height of opening area is H ', be close to a side of catalyzer and offer outer distribution hole 17, its percentage of open area is 20～40%, and hole shape is circular hole or bar hole, and a side of pressing close to pressurized vessel 8 is not perforates.
Structure and Fig. 1 of Fig. 2 are basic identical, but gas inlet tube 1 places the upper side of cylindrical vessel 8, and the outlet pipe 2 of reactant gases places on the top end socket of cylindrical vessel 8.
Structure and Fig. 1 of Fig. 3 are basic identical, but the outlet pipe 2 of gas inlet tube 1 and reactant gases places on the bottom bulkhead of cylindrical vessel 8, and manhole 13 is offered on the top of cylindrical vessel 8, are used for loading catalyst.
The reaction method and the reaction unit that adopt the present invention to propose compared with prior art have the following advantages:
1. П type structure can be eliminated the static pressure difference between flow manifold and afflux runner two runners fully, can reduce the control pressure drop of sparger significantly, and reactor pressure decrease is low, can guarantee reactant gases uniform distribution vertically fully;
2. reactant gases owing to do not have thermosteresis at the center flow manifold, has guaranteed that axial temperature is even in the reactor by the outside centrifugal flow in center;
3. reactant gases is done centrifugal flow at bed, and the utilization ratio of catalyzer has been improved in the dead band of having reduced catalyzer significantly;
4. flow manifold adopt to become percentage of open area or becomes the diameter technology, has overcome the bed voidage variation defective vertically that the long-term operation of catalyzer causes, and makes fluid more even along the reactor axial distribution.
Embodiment:
The reaction method of catalytic reforming of the present invention and catalytic dehydrogenation and reaction unit can carry out in a kind of centrifugal radial reactor in the following processing parameter condition that provides;
Hydrogen hydrocarbon mol ratio is 6～10 in embodiment 1 raw material, weight liquid air speed is 1.0～3.0h
-1, temperature of reaction is that 450～550 ℃, reaction pressure are that the semi-regenerating catalytic reforming reaction process of 1.2～3.0MPa can adopt any one mode in Fig. 1, Fig. 2 or the three kinds of modes shown in Figure 3 to implement.
H in embodiment 2 raw materials
2The mol ratio of O/ ethylbenzene is 8～10, ethylbenzene liquid air speed is 0.35～0.45h
-1, temperature of reaction is that 550～645 ℃, reaction pressure are that the ethylbenzene dehydrogenation reaction technology of 45～80Kpa (absolute pressure) can adopt any one mode in Fig. 1, Fig. 2 or the reactor shown in Figure 3 to implement.
The flow manifold 3 that porous wall tube 6 constituted in reactant gases was entered by reacting gas inlet 1, by the bed district 5 radially of interior distribution hole 15 radial inflows on the interior porous wall tube 6, and then enter reactant gases collection flow channels 4 by outer porous wall 7 from inside to outside and make centrifugal flow, reactant gases is to do reverse relative mobilely in afflux runner 4 and flow manifold 3, flows out by the outlet 2 of reactant gases along the afflux runner then.
Claims (10)
1, the centrifugal fixed bed radial reactor of a kind of catalytic reforming, catalytic dehydrogenating reaction, comprise catalytic bed (5) in a cylindrical vessel (8) and the container, on the wall of this cylindrical vessel (8), be provided with reacting gas inlet (1), reaction gas outlet (2), catalyzer discharge tube (12);
In cylindrical vessel (8), comprise: with the coaxial setting of cylindrical vessel (8), be arranged in order the urceolus (7) of porous wall inner core (6) and vesicular structure from inside to outside; The urceolus of described vesicular structure (7) is a porous wall circular outer cylinder or makes adjacent circumferential by a plurality of fan-shaped, hollow components (16) along nearly wall place in the bulge (8) and arrange the urceolus that is constituted, it offers distribution hole (17) by catalyzer one side, and by cylindrical vessel (8) one not perforates of side;
Described porous wall inner core (6) not perforate of upper portion side wall, inner core (6) is connected with the reacting gas inlet that places cylindrical vessel (8) one ends (1), constitute the flow manifold (3) of reactant gases, form annular catalytic bed (5) between inner core (6) and the urceolus (7), form the annular space space between porous wall urceolus (7) and cylindrical vessel (8) sidewall or by segmental porous hollow component (16) formation reactant gases afflux runner (4) itself, and with place cylindrical vessel (8) and reacting gas inlet (1) be connected in the reaction gas outlet (2) of same end;
It is characterized in that described reacting gas inlet (1) and reaction gas outlet (2) place the top or the bottom of cylindrical vessel (8) simultaneously; The inner core of porous wall structure (6) adopts and becomes percentage of open area or become the diameter technology, and inner core (6) bottom opening rate is 100%～200% of a top percentage of open area, or the thickness of bed top catalyzer is 100%～200% of bottom thickness.
2, reactor as claimed in claim 1 is characterized in that, the perforate (15) of porous slab (14) can be adopted even perforate from top to bottom, and percentage of open area is a definite value.
3, reactor as claimed in claim 1 is characterized in that, the perforate (15) of porous slab (14) is the piecewise uniform perforate, and segmentation from top to bottom increases percentage of open area, and the bottom opening rate is 100%～200% of a top percentage of open area.
4, reactor as claimed in claim 1 is characterized in that, the inner core of being made by porous slab (14) (6) can adopt the taper inner tube structure, and base diameter is greater than top diameter, and the thickness of bed top catalyzer is 100%～200% of bottom thickness.
5, reactor as claimed in claim 1 is characterized in that, the inner core of being made by porous slab (14) (6) can adopt trapezoidal change diameter inner tube structure, and base diameter is greater than top diameter, and the thickness of bed top catalyzer is 100%～200% of bottom thickness.
6, reactor as claimed in claim 1, the porous wall structure of its inner core (6) is that porous slab (14) is close to multihole lamina, or by the structure of making somebody a mere figurehead with support bar between porous slab (14) and the multihole lamina, or be close to structure by the bilayer that porous slab (14) and grid are formed, it is characterized in that, the percentage of open area of porous slab is 1～15%, and the percentage of open area of multihole lamina is 20～40%, and the porosity of grid is 25～50%.
7, reactor as claimed in claim 1, its urceolus (7) can by a plurality of fan-shaped, porous hollow components (16) do along nearly wall place in the bulge (8) adjacent circumferential arrange constituted, it is characterized in that, porous hollow component (16) aspect ratio catalyzer cover plate for sealing structure is slightly high, the height of opening area is H ', and its percentage of open area is 20～40%.
8, reactor as claimed in claim 1, its porous wall urceolus (7) is by forming with horizontal or built on stilts the rolling of longitudinal ligament bar in the middle of porous slab and the multihole lamina, and the percentage of open area of multihole lamina is 20～40%, and the percentage of open area of porous slab is 20～40%; Or form by grid, the porosity of grid is 25～50%.
9, reactor as claimed in claim 1 is characterized in that: gas inlet tube (1) places the upper side of cylindrical vessel (8), and the outlet pipe of reactant gases (2) places on the upper end end socket of cylindrical vessel (8).
10, reactor as claimed in claim 1 is characterized in that, gas inlet tube (1) places the lower end of cylindrical vessel (8), and the outlet pipe of reactant gases (2) places the lower side of cylindrical vessel (8).
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| CN 200310109323 CN1232341C (en) | 2003-12-12 | 2003-12-12 | Catalytic reforming and catalytic dehydrogenation centrifugal type fixed bed radial reactor |
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| CN 200310109323 CN1232341C (en) | 2003-12-12 | 2003-12-12 | Catalytic reforming and catalytic dehydrogenation centrifugal type fixed bed radial reactor |
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