CA1201875A - Vapor-solid contacting device - Google Patents
Vapor-solid contacting deviceInfo
- Publication number
- CA1201875A CA1201875A CA000419394A CA419394A CA1201875A CA 1201875 A CA1201875 A CA 1201875A CA 000419394 A CA000419394 A CA 000419394A CA 419394 A CA419394 A CA 419394A CA 1201875 A CA1201875 A CA 1201875A
- Authority
- CA
- Canada
- Prior art keywords
- solids
- ordered array
- members
- zone
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
- B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/34—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
A multiple-zone reactor in which upper and lower zones are separated by an ordered array packing zone consisting of stationary, parallel members to provide controlled hindered mixing of particulate solids and a gas flowing therethrough.
The ordered array comprises multiple rows of stationary, parallel members, which can be varied in their size, shape, and spacing to provide a void volume of between about 20 and about 80%. In one embodiment, the stationary members are oriented substantially horizontally and particulate solids descend through the array in countercurrent flow against an upflowing hot gas. The reactor is generally operated at a temperature ranging from about 850°F
to about 1900°F and at a pressure of 0 to 1000 psig.
The horizontal rows of the members of the ordered array may be arranged to have an angle of rotation between them ranging from 0 to 90°.
A multiple-zone reactor in which upper and lower zones are separated by an ordered array packing zone consisting of stationary, parallel members to provide controlled hindered mixing of particulate solids and a gas flowing therethrough.
The ordered array comprises multiple rows of stationary, parallel members, which can be varied in their size, shape, and spacing to provide a void volume of between about 20 and about 80%. In one embodiment, the stationary members are oriented substantially horizontally and particulate solids descend through the array in countercurrent flow against an upflowing hot gas. The reactor is generally operated at a temperature ranging from about 850°F
to about 1900°F and at a pressure of 0 to 1000 psig.
The horizontal rows of the members of the ordered array may be arranged to have an angle of rotation between them ranging from 0 to 90°.
Description
S
V~POR-SOLID CONTACTING DEVICE
BACKGROUND OF INVENTION
This invention relates to vapor-solids contacting in a fluidized bed, and more particularly, it relates to gas-liquid-solids contacting in a fluldized bed in an ordered array devica arranged to provide uniform h;ndered mixing and avoid agglomera-tion of particulate solids in a reaction zone.
Fluidized beds are often used for contacting vapor and particulate solid materials. Such devices have well-known properties but the most important and significant is that the fluid bed is normally a well-mixed bed of solid particles and acts as a stirred tank reactor for chemical reaction purposes.
In the fluidlzed~bed cracking of heavy oils as described in U.S. Patent No. 2,861,943 to~Finneran, there is disclosed a multi-zone reactor having an intermediate zone for restricted fluidiæation of a particulate carrier and stripping of adsorbed hydrocarbons. This arrangement is illustrated in the attached FIG. l, labelled "Current Practice" having two zones of fluidized beds, which are each substantially isoth~rm~l but operate at different temperatures. In this reactor, vapor passes upwardly from zone 1 through a h;n~ered back-mixing zone comprising a packed bed, and particulate solids pass downwardly from zone 2 through the hindered back-mixing zone into zone 1 countercurrent to upflowing gas. This hindered, i.e., restricted zone, consists of a bed of random packings using materials, such as Raschig rings or spheres, supported on a grid plate having openings smaller than the random packing material. A typical dense phase fluidized bed exists in both zone 1 and zone 2.
~12a~ S
In some instances, the fluidized bed may be described as a fast fluidized bed having high superficial gas velocity, such as disclosed by Sc~uires in U.S. Pa~en~ 3,840,353. In this arrangement, the general direction o~ the solids movement is upward and solids are recirculated within the reactor to main-tain the bed at an appropriate density. In this type bed, there are some aspects of plug-flow behavior without any stationary packing to provide hindered mixing of gas ancl solids.
The use of such stationary packed beds places undesirable process restraints on those gas-solids cont~;ning processes in which it i5 desired to provide a substantial temperature difference across the packed bed, particularly processes for upgrading heavy hydrocarbon feedstocks. Also, use of such stationary packing material, for which the individual pieces touch adjacent pieces, can cause localized agglomeration of the particulate solids within or passing through and consequently undesired plugging of the becl.
SUMMARY OF THE INVENTION
This invention provides a process for contacting particulate solids with a gas within an ordered array packing zone. The pro-cess comprises: (a) passing particulate solids through the ordered array packing zone having multiple rows of stationary, parallel members providing a void volume ranging from about 20 to about 80%; (b) passing a gas through the ordered array pack-ing zone countercurrent to particuIa~e solids to fluidize the particulate solids and to provide intimate contact between the gas and the solids; and (c) maintaining a hindered mixing of the solids and gas withi~ the ordered array packing zone to provide a temperature of at least about 20F across the packing zone.
The particulate soli.ds may be passed either downward or upward through the ordered array packing zone while the gas is .
~Z018~
passed countercurrent to or co-current with the flow of the particulate solids. I'he particulate solids ha~e a diameter of at least about 0.002 inches and the superficla]. velocity of the gas ranges f.rom about 0.1 to ahout S.0 ft./sec. In the process, the particulate solids pass through the ordered array packing zone at a temperature of from about 850 to about 1400F and the gas passes through at a temperature ranging from about 1000 to about 1900F.
The invention also provides a reaction vessel which includes an upper zone for containing a fluidized bed of ~articulate solids, a lower zone for containing a fluidizPd bed of particulate solids and an intermediate packing zone which consists of an ordered array packing zone of stationary members separating the upper and lower zones and providing a void volume ranging from about 20% to about 80%~
said ordered array of stationary, parallel members comprising at least two rows of spaced, self-supporting horiz~ntal members, the members in each row having different horizontal spacing between the adjacent members. The members which are stationary are fixed in horizontal rows which are arranged at an angle of rotation between them of 0 to 90..
BRIEF DESCRIPTION OF DRAWINGS
FIG~ 1 is a schematic drawing of a prior art configuration of a packed bed containing a fluidized bed for gas-solids contacting;
FIG. 2 is several views illustrating typ~cal construction features for an ordered array packing zone according to the present invention; and FIG. 3 is a schematic drawing illustrating a multiple-zone reactor containing an ordered array packing zone.
~3 ~la,7~
DETAILED DESCRIPTION OF TH~ lNv4rl~lION
The vapor-solids contacting process of the present invention is generally carried out in a reactor having two reactor zones - 3a t~
lZ018~5 separated by an ordered array packing zone of stationary parallel members for providing intimate vapor/solids contacting and h1nd~red~ i.e., restricted, back-mix:Lng of the particulate solids and gas passing through -the array. The arrangement of the ordered array packing zone permits a temperature gradient to be established between khe reaction zone and across the ordered array.
In the ordered array packing zone the individual stationary m~mh~rs are horizontally spaced apart from each other, preferably by use of individual spacer elements. The members are usually arranged in a plurality of horizontal rows, which can each have variable cross-sectional shapes and spacing, the rows being spaced vertically.
The reactor vessel in which the process is carried out, has an upper and a lower zone which are separated by the packing zone which consists of the ordered array of members. The solids transfer in the reactor vessel can be upwardly from the lower ZQne through the upper zone, or downwardly from the upper zone through the lower zone, or there may be a net zero flux of solids between the upper and lower zones.
The particulate solids contained in or transferred through the ordered array packing zone can be catalytic or non-catalytic.
Also, the members of the ordered array packing zone may contain catalytic materials. Such catalytic materials would be selected to provide a typical chemical reaction desired. As an example of such a chemical reaction, a gas from the lower zone might consist of a synthesis gas cont~1n1ng C0, H2, H20, and a catalyst could be incorporated in or coated on the members of the packing zone to cause the reaction equilibrium to shift towards producing more hydrogen. Thus, the hydrogen might then be more useful in the upper zone.
~æ~Q~qS
As illustrated in FIG. 3, the entire reactor might consist substantially of sta~ionary packing so that zone 1 and zone 2 are reduced to near zero volume. The entire reactor would then con-sist essentially of a fluidized bed in an ordered array in which gradients could be obtained. Therefore, a fluid bed reactor would be provided having a gradient through it so as to obtain, for example, better yields of reacted products.
The present invention provides a novel reactor design con-figuration whereby a fixed bed of packed material is used in an ordered array configuration and vapor and solid particles are placed in intimate contact therein. The solid par~icles as well as being catalytic or non-catalytic, may be absorptive or non-absorptive.
This type of reactor system using an ordered array permits a fluid bed of solids to be used and to obtain intimate contact between the vapor and the solid particles. At the same time, it pennits gradients to exist within the bed which include tempera-ture, co~centration, solids age, and the solids dimensions, ei~her specific gravity or diametexs. Because the solids particles are in constant random motion, they may be added to or withdrawn from the ordered array at any point, or withdrawn from above or below the packing zone~
According to the present invention, various characteristics of ~he ordered array packing zone can be advantageously altered to suit specific applications. The e characteristics include the shape of ~he packing zone members which may be a circle, a square, a diamond, a rectangle or a triangle, or any other suitable geo-metric shape, the horizontal spacing between the packing members, and the vextical spacing between the rows of the members. The si~s of the members are additional factors of variability, as is the angle o~ rotation between rows a further design variable. The members may be solid, hollow, have a roughened surface or be finned.
~ 0~87~i Referring to FIG. 2, there are shown several construction features for an ordered array packing zone according to the present invention. In this fiyure, there iS illustrated two rows of rods arranged at an angle of rotation bel:ween them of 90~
The rows of members, e.g., rods, may be arranged at an angle of rotation between them of O to 90. Supports for the packing zone members might be braced on shelves from the vessel wall or can be supported directly from horizontal beams provided in the raactor. Rows of members may be supported on saddles which would maintain the internal dimensions of the packed array.
The appropriate choice of variables in the ordered array permits a wide range of packing void fractions to be achieved, such as a void volume ranging from about 5 to about 95~, and preferably from about 20 to about 80%.
As shown in FIG. 3, the members, e.g., rods, are extended completely across the reactor vessel, which eliminates the need for a grid beneath the ordered array of members. Each member, e.g., rod, being self-supporting permits a broader span to be handled with a given material and operating temperature.
Moreover, the dimensions and spacing of the members, e.g., rods, should be such that the fluidized solid particles will readily pass through them. The ordered array of members may be arranged to gradually increase the vertical spacing between adjacent rows of the members, e.g., rods, from the top to the bottom, thereby assuring that any particulate solids which enter the ordered array packing zone will pass on through.
Different sections of the ordered array might have different purposes. As illustrated in FIG. 3, Part A, which is immediately above the gasification or lower zone 1, could be designed to withstand high temperatures. In this zone, a packing material ...... ~.. `. ~L2Q~L~P~S .
having high mechanical strength in relation to i-ts weight would be used. Such a section o~ specially designed material would permit the hot gases from zone 1 to be cooled prior to entering the ordered array packing zone. In Part B, the rods might, for example, have a vertical spacing such that each rod is self-supporting and no rod could sag enough to touch another.
In Part C of the ordered array, the vertical spacing between members, e.g., rods, might be reduced to near zero. By doing this, all of the members could act together to support the weight of a slumped bed from zone 2.
The advantages of the invention described herein will be further illustrated by the following example which should not be construed as lLmiting in scope.
EXAMPLE
An ordered array according to the present-in~ention is con-structed which consists of three rows of horizontal rods,
V~POR-SOLID CONTACTING DEVICE
BACKGROUND OF INVENTION
This invention relates to vapor-solids contacting in a fluidized bed, and more particularly, it relates to gas-liquid-solids contacting in a fluldized bed in an ordered array devica arranged to provide uniform h;ndered mixing and avoid agglomera-tion of particulate solids in a reaction zone.
Fluidized beds are often used for contacting vapor and particulate solid materials. Such devices have well-known properties but the most important and significant is that the fluid bed is normally a well-mixed bed of solid particles and acts as a stirred tank reactor for chemical reaction purposes.
In the fluidlzed~bed cracking of heavy oils as described in U.S. Patent No. 2,861,943 to~Finneran, there is disclosed a multi-zone reactor having an intermediate zone for restricted fluidiæation of a particulate carrier and stripping of adsorbed hydrocarbons. This arrangement is illustrated in the attached FIG. l, labelled "Current Practice" having two zones of fluidized beds, which are each substantially isoth~rm~l but operate at different temperatures. In this reactor, vapor passes upwardly from zone 1 through a h;n~ered back-mixing zone comprising a packed bed, and particulate solids pass downwardly from zone 2 through the hindered back-mixing zone into zone 1 countercurrent to upflowing gas. This hindered, i.e., restricted zone, consists of a bed of random packings using materials, such as Raschig rings or spheres, supported on a grid plate having openings smaller than the random packing material. A typical dense phase fluidized bed exists in both zone 1 and zone 2.
~12a~ S
In some instances, the fluidized bed may be described as a fast fluidized bed having high superficial gas velocity, such as disclosed by Sc~uires in U.S. Pa~en~ 3,840,353. In this arrangement, the general direction o~ the solids movement is upward and solids are recirculated within the reactor to main-tain the bed at an appropriate density. In this type bed, there are some aspects of plug-flow behavior without any stationary packing to provide hindered mixing of gas ancl solids.
The use of such stationary packed beds places undesirable process restraints on those gas-solids cont~;ning processes in which it i5 desired to provide a substantial temperature difference across the packed bed, particularly processes for upgrading heavy hydrocarbon feedstocks. Also, use of such stationary packing material, for which the individual pieces touch adjacent pieces, can cause localized agglomeration of the particulate solids within or passing through and consequently undesired plugging of the becl.
SUMMARY OF THE INVENTION
This invention provides a process for contacting particulate solids with a gas within an ordered array packing zone. The pro-cess comprises: (a) passing particulate solids through the ordered array packing zone having multiple rows of stationary, parallel members providing a void volume ranging from about 20 to about 80%; (b) passing a gas through the ordered array pack-ing zone countercurrent to particuIa~e solids to fluidize the particulate solids and to provide intimate contact between the gas and the solids; and (c) maintaining a hindered mixing of the solids and gas withi~ the ordered array packing zone to provide a temperature of at least about 20F across the packing zone.
The particulate soli.ds may be passed either downward or upward through the ordered array packing zone while the gas is .
~Z018~
passed countercurrent to or co-current with the flow of the particulate solids. I'he particulate solids ha~e a diameter of at least about 0.002 inches and the superficla]. velocity of the gas ranges f.rom about 0.1 to ahout S.0 ft./sec. In the process, the particulate solids pass through the ordered array packing zone at a temperature of from about 850 to about 1400F and the gas passes through at a temperature ranging from about 1000 to about 1900F.
The invention also provides a reaction vessel which includes an upper zone for containing a fluidized bed of ~articulate solids, a lower zone for containing a fluidizPd bed of particulate solids and an intermediate packing zone which consists of an ordered array packing zone of stationary members separating the upper and lower zones and providing a void volume ranging from about 20% to about 80%~
said ordered array of stationary, parallel members comprising at least two rows of spaced, self-supporting horiz~ntal members, the members in each row having different horizontal spacing between the adjacent members. The members which are stationary are fixed in horizontal rows which are arranged at an angle of rotation between them of 0 to 90..
BRIEF DESCRIPTION OF DRAWINGS
FIG~ 1 is a schematic drawing of a prior art configuration of a packed bed containing a fluidized bed for gas-solids contacting;
FIG. 2 is several views illustrating typ~cal construction features for an ordered array packing zone according to the present invention; and FIG. 3 is a schematic drawing illustrating a multiple-zone reactor containing an ordered array packing zone.
~3 ~la,7~
DETAILED DESCRIPTION OF TH~ lNv4rl~lION
The vapor-solids contacting process of the present invention is generally carried out in a reactor having two reactor zones - 3a t~
lZ018~5 separated by an ordered array packing zone of stationary parallel members for providing intimate vapor/solids contacting and h1nd~red~ i.e., restricted, back-mix:Lng of the particulate solids and gas passing through -the array. The arrangement of the ordered array packing zone permits a temperature gradient to be established between khe reaction zone and across the ordered array.
In the ordered array packing zone the individual stationary m~mh~rs are horizontally spaced apart from each other, preferably by use of individual spacer elements. The members are usually arranged in a plurality of horizontal rows, which can each have variable cross-sectional shapes and spacing, the rows being spaced vertically.
The reactor vessel in which the process is carried out, has an upper and a lower zone which are separated by the packing zone which consists of the ordered array of members. The solids transfer in the reactor vessel can be upwardly from the lower ZQne through the upper zone, or downwardly from the upper zone through the lower zone, or there may be a net zero flux of solids between the upper and lower zones.
The particulate solids contained in or transferred through the ordered array packing zone can be catalytic or non-catalytic.
Also, the members of the ordered array packing zone may contain catalytic materials. Such catalytic materials would be selected to provide a typical chemical reaction desired. As an example of such a chemical reaction, a gas from the lower zone might consist of a synthesis gas cont~1n1ng C0, H2, H20, and a catalyst could be incorporated in or coated on the members of the packing zone to cause the reaction equilibrium to shift towards producing more hydrogen. Thus, the hydrogen might then be more useful in the upper zone.
~æ~Q~qS
As illustrated in FIG. 3, the entire reactor might consist substantially of sta~ionary packing so that zone 1 and zone 2 are reduced to near zero volume. The entire reactor would then con-sist essentially of a fluidized bed in an ordered array in which gradients could be obtained. Therefore, a fluid bed reactor would be provided having a gradient through it so as to obtain, for example, better yields of reacted products.
The present invention provides a novel reactor design con-figuration whereby a fixed bed of packed material is used in an ordered array configuration and vapor and solid particles are placed in intimate contact therein. The solid par~icles as well as being catalytic or non-catalytic, may be absorptive or non-absorptive.
This type of reactor system using an ordered array permits a fluid bed of solids to be used and to obtain intimate contact between the vapor and the solid particles. At the same time, it pennits gradients to exist within the bed which include tempera-ture, co~centration, solids age, and the solids dimensions, ei~her specific gravity or diametexs. Because the solids particles are in constant random motion, they may be added to or withdrawn from the ordered array at any point, or withdrawn from above or below the packing zone~
According to the present invention, various characteristics of ~he ordered array packing zone can be advantageously altered to suit specific applications. The e characteristics include the shape of ~he packing zone members which may be a circle, a square, a diamond, a rectangle or a triangle, or any other suitable geo-metric shape, the horizontal spacing between the packing members, and the vextical spacing between the rows of the members. The si~s of the members are additional factors of variability, as is the angle o~ rotation between rows a further design variable. The members may be solid, hollow, have a roughened surface or be finned.
~ 0~87~i Referring to FIG. 2, there are shown several construction features for an ordered array packing zone according to the present invention. In this fiyure, there iS illustrated two rows of rods arranged at an angle of rotation bel:ween them of 90~
The rows of members, e.g., rods, may be arranged at an angle of rotation between them of O to 90. Supports for the packing zone members might be braced on shelves from the vessel wall or can be supported directly from horizontal beams provided in the raactor. Rows of members may be supported on saddles which would maintain the internal dimensions of the packed array.
The appropriate choice of variables in the ordered array permits a wide range of packing void fractions to be achieved, such as a void volume ranging from about 5 to about 95~, and preferably from about 20 to about 80%.
As shown in FIG. 3, the members, e.g., rods, are extended completely across the reactor vessel, which eliminates the need for a grid beneath the ordered array of members. Each member, e.g., rod, being self-supporting permits a broader span to be handled with a given material and operating temperature.
Moreover, the dimensions and spacing of the members, e.g., rods, should be such that the fluidized solid particles will readily pass through them. The ordered array of members may be arranged to gradually increase the vertical spacing between adjacent rows of the members, e.g., rods, from the top to the bottom, thereby assuring that any particulate solids which enter the ordered array packing zone will pass on through.
Different sections of the ordered array might have different purposes. As illustrated in FIG. 3, Part A, which is immediately above the gasification or lower zone 1, could be designed to withstand high temperatures. In this zone, a packing material ...... ~.. `. ~L2Q~L~P~S .
having high mechanical strength in relation to i-ts weight would be used. Such a section o~ specially designed material would permit the hot gases from zone 1 to be cooled prior to entering the ordered array packing zone. In Part B, the rods might, for example, have a vertical spacing such that each rod is self-supporting and no rod could sag enough to touch another.
In Part C of the ordered array, the vertical spacing between members, e.g., rods, might be reduced to near zero. By doing this, all of the members could act together to support the weight of a slumped bed from zone 2.
The advantages of the invention described herein will be further illustrated by the following example which should not be construed as lLmiting in scope.
EXAMPLE
An ordered array according to the present-in~ention is con-structed which consists of three rows of horizontal rods,
2.0 inches in diameter, and arranged in a staggered triangular pitch pattern of about 2.6 inch center to center spacing. The rods are separated by angular-shaped spacers or washers circum-ferentially mounted on the rods to provide a void volume of about 50%. The rods are supported by structural beams attached to the reactor inner wall, to provide an array of about 8 feet diameter by 4 feet deep. The packed array contains a bed of inert ?articulate solids such as a clay or an alumina having a particle ~ize ,~ 0 005-0.050 inches which are fluidized by a hot reducing -;;.s s;is~ina apwardly through the ~ed. Particulate carrier solids -ontalning coke deposits with some hydrocarbon liquid on and withln the particles pass downwardly through the array counter-current to the upflowing gas. The particulate solids enter the ordered array at the top at about 1000F and exit the ordered ~ hA ~m ,~ , l~m7~Ql,~.,~Q cl; ~h~l ~7 lQCC ~h~n ~hQ ~c entering the array. The gas enters the ordered array at the bo~tom at about 1800F and exits the ordered array at the top a temperature slightly higher than the particulate solids enter-ing the array. The pressure is about 40() psig. In the ordered array, the particulate solids are fluidized by the upflowing reducing gas and the hydrocarbon liquid is stripped off the particulate solids. The particulatesolids then pass downwardly into the lower zone for combustion and gasification of the carbon deposits.
Claims (26)
1. A process for contacting particulate solids with a gas within an ordered array packing zone comprising:
(a) passing particulate solids having a diameter of at least about 0.002 inches at a temperature ranging from about 850° to about 1400°F.; through the ordered array packing zone having multiple rows of stationary, parallel members providing a void volume ranging from about 20 to about 80%;
(b) passing a gas at a superficial velocity ranging from about 0.1 to about 5.0 ft./sec.
and at a temperature ranging from about 1000° to about 1900°F. through said ordered array packing zone to fluidize said particulate solids and to provide intimate contact between the gas and the solids; and (c) maintaining a hindered mixing of the solids and gas within the ordered array packing zone to provide a temperature difference of at least about 20°F across the packing zone.
(a) passing particulate solids having a diameter of at least about 0.002 inches at a temperature ranging from about 850° to about 1400°F.; through the ordered array packing zone having multiple rows of stationary, parallel members providing a void volume ranging from about 20 to about 80%;
(b) passing a gas at a superficial velocity ranging from about 0.1 to about 5.0 ft./sec.
and at a temperature ranging from about 1000° to about 1900°F. through said ordered array packing zone to fluidize said particulate solids and to provide intimate contact between the gas and the solids; and (c) maintaining a hindered mixing of the solids and gas within the ordered array packing zone to provide a temperature difference of at least about 20°F across the packing zone.
2. The process of claim 1, wherein the particulate solids are passed downward through the ordered array packing zone and the gas is passed upward, countercurrent to said solids, through the ordered array packing zone.
3. The process of claim 1, wherein the particulate solids are passed upward through the ordered array packing zone and the gas is passed upward, co-current with said solids, through the ordered array packing zone.
4. The process of claim 1, wherein the particulate solids have thereon a hydrocarbon liquid and the flowing gas heats the solids and strips the liquid therefrom.
5. The process according to claim 1, wherein the rows of the members of the ordered array packing zone are arranged at an angle of rotation between them of 0 to 90°.
6. The process according to claim 1, wherein the members extend completely across the packing zone.
7. The process according to claim 1, wherein the shape of the members is a circle, a square, a diamond, a rectangle, or a triangle.
8. The process according to claim 1, wherein the members are solid, hollow, have a roughened surface or are finned.
9. A process for contacting particulate solids with a gas within an ordered array packing zone, comprising:
(a) passing particulate solids having a diameter of at least about 0.002 inches, at a temperature ranging from about 850° to about 1400°F., downwardly through the ordered array packing zone having multiple rows of stationary, parallel members providing a void volume ranging from about 20 to about 80%;
(b) passing a gas upwardly, countercurrent to the particulate solids, through the ordered array packing zone at a superficial velocity ranging from about 0.1 to about 5.0 ft./sec.
and at a temperature ranging from about 1000° to about 1900°F. to fluidize the solids and provide intimate contact with said solids; and (c) maintaining hindered mixing of the solids and gas within the ordered array packing zone to provide a temperature difference of at least about 20°F. across the packing zone.
(a) passing particulate solids having a diameter of at least about 0.002 inches, at a temperature ranging from about 850° to about 1400°F., downwardly through the ordered array packing zone having multiple rows of stationary, parallel members providing a void volume ranging from about 20 to about 80%;
(b) passing a gas upwardly, countercurrent to the particulate solids, through the ordered array packing zone at a superficial velocity ranging from about 0.1 to about 5.0 ft./sec.
and at a temperature ranging from about 1000° to about 1900°F. to fluidize the solids and provide intimate contact with said solids; and (c) maintaining hindered mixing of the solids and gas within the ordered array packing zone to provide a temperature difference of at least about 20°F. across the packing zone.
10. The process of claim 9, wherein the rows of the members of the ordered array packing zone are arranged at an angle of rotation between them of 0 to 90%.
11. The process according to claim 9, wherein the shape of the members is a circle, a square, a diamond, a rectangle, or a triangle.
12. The process according to claim 9, wherein the members are solid, hollow, have a roughened surface or are finned.
13. The process according to claim 9, wherein the solids are catalytic and absorptive.
14. The process according to claim 9, wherein the solids are non-catalytic and non-absorptive.
15. The process according to claim 9, wherein the solids are catalytic and non-absorptive.
16. The process according to claim 9, wherein the solids are non-catalytic and absorptive.
17. A reactor vessel for contacting fluids with particulate solids, comprising:
(a) an upper zone for containing a fluidized bed of particulate solids;
(b) a lower zone for containing a fluidized bed of particulate solids; and (c) an intermediate packing zone comprising an ordered array of stationary, parallel members separating said upper and lower zones and providing a void volume ranging from about 20% to about 80%, said ordered array of stationary, parallel members comprising at least two rows of spaced, self-supporting horizontal members, the members in each row having different horizontal spacing between the adjacent members.
(a) an upper zone for containing a fluidized bed of particulate solids;
(b) a lower zone for containing a fluidized bed of particulate solids; and (c) an intermediate packing zone comprising an ordered array of stationary, parallel members separating said upper and lower zones and providing a void volume ranging from about 20% to about 80%, said ordered array of stationary, parallel members comprising at least two rows of spaced, self-supporting horizontal members, the members in each row having different horizontal spacing between the adjacent members.
18. The reactor of claim 17, wherein the rows of the members of the ordered array are arranged at an angle of rotation between them of 0 to 90°.
19. The reactor of claim 17, wherein the members in each adjacent row have different diameters.
20. The reactor of claim 17, wherein the ordered array comprises at least three rows of rods and the vertical spacing is varied between adjacent rows of rods.
21. The reactor of claim 17, wherein the adjacent rows of members are separated by vertical spacers.
22. The reactor of claim 17, wherein the ordered array contains a catalytic material.
23. The reactor of claim 22, wherein the catalytic material comprises a coating of at least a portion of the horizontal members of the ordered array.
24. The reactor of claim 17, wherein particulate solids from the upper zone descend downwardly through the ordered array while the gas passes from the lower zone upward, countercurrent to said solids through the ordered array to fluidize the solids and provide intimate contact between the gas and solids therein.
25. The reactor of claim 17, wherein particulate solids pass from the lower zone upwardly through the ordered array, and a gas passes upward to the upper zone, co-current with the flow of solids, through the ordered array to fluidize the solids therein and to provide intimate contact therewith.
26. The reactor of claim 17, wherein the reactor internal pressure is from 0 to about 1000 psig and the ordered array temperature is between about 850° and about 1900°F.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US33936282A | 1982-01-15 | 1982-01-15 | |
| US339,362 | 1982-01-15 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1201875A true CA1201875A (en) | 1986-03-18 |
Family
ID=23328664
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000419394A Expired CA1201875A (en) | 1982-01-15 | 1983-01-13 | Vapor-solid contacting device |
Country Status (8)
| Country | Link |
|---|---|
| JP (1) | JPS58196840A (en) |
| BE (1) | BE895617A (en) |
| CA (1) | CA1201875A (en) |
| DE (1) | DE3301341A1 (en) |
| FR (1) | FR2519876A1 (en) |
| GB (1) | GB2113113A (en) |
| NL (1) | NL8300166A (en) |
| ZA (1) | ZA83282B (en) |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2536099A (en) * | 1947-08-18 | 1951-01-02 | American Metal Co Ltd | Means for forming stages in fluidized masses |
| US2885343A (en) * | 1953-07-01 | 1959-05-05 | Hydrocarbon Research Inc | Conversion of hydrocarbons |
| US2875150A (en) * | 1953-11-12 | 1959-02-24 | Hydrocarbon Research Inc | Heavy oil conversion with low coke formation |
| US3169835A (en) * | 1959-07-01 | 1965-02-16 | Exxon Research Engineering Co | Fluidized solids technique |
| DE2304762A1 (en) * | 1973-02-01 | 1974-08-15 | Degussa | PRODUCTION OF FORMALDEHYDE IN A FLUID LAYER WITH A CERTAIN TEMPERATURE GRADIENT |
-
1983
- 1983-01-13 CA CA000419394A patent/CA1201875A/en not_active Expired
- 1983-01-17 GB GB08301138A patent/GB2113113A/en not_active Withdrawn
- 1983-01-17 BE BE2/59996A patent/BE895617A/en not_active IP Right Cessation
- 1983-01-17 NL NL8300166A patent/NL8300166A/en not_active Application Discontinuation
- 1983-01-17 DE DE19833301341 patent/DE3301341A1/en not_active Withdrawn
- 1983-01-17 JP JP58005790A patent/JPS58196840A/en active Pending
- 1983-01-17 ZA ZA83282A patent/ZA83282B/en unknown
- 1983-01-17 FR FR8300646A patent/FR2519876A1/en not_active Withdrawn
Also Published As
| Publication number | Publication date |
|---|---|
| GB2113113A (en) | 1983-08-03 |
| FR2519876A1 (en) | 1983-07-22 |
| ZA83282B (en) | 1983-10-26 |
| NL8300166A (en) | 1983-08-01 |
| DE3301341A1 (en) | 1983-07-28 |
| BE895617A (en) | 1983-05-16 |
| JPS58196840A (en) | 1983-11-16 |
| GB8301138D0 (en) | 1983-02-16 |
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Legal Events
| Date | Code | Title | Description |
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| MKEX | Expiry |