CA1177385A - Gas-pocket distributor for an upflow reactor - Google Patents
Gas-pocket distributor for an upflow reactorInfo
- Publication number
- CA1177385A CA1177385A CA000377087A CA377087A CA1177385A CA 1177385 A CA1177385 A CA 1177385A CA 000377087 A CA000377087 A CA 000377087A CA 377087 A CA377087 A CA 377087A CA 1177385 A CA1177385 A CA 1177385A
- Authority
- CA
- Canada
- Prior art keywords
- gas
- combination
- recited
- plate
- vessel
- 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
Links
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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0492—Feeding reactive fluids
-
- 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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
-
- 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
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
Disclosed is a distributor for a multiphase upflow reactor. The distributor comprises a horizontally disposed plate mounted in the vessel above the feed inlet port. The plate has a plurality of perforations there-through and at least one downwardly extending tube passing through the plate. The perforations and tube are sized such that under equilibrium feed conditions a gas pocket forms below the plate having a height less than or sub-stantially equal to the tube length. Substantially all of the feed gas passes through the plate perforations and substantially all of the feed liquid or liquid and solids, passes through the tube.
Disclosed is a distributor for a multiphase upflow reactor. The distributor comprises a horizontally disposed plate mounted in the vessel above the feed inlet port. The plate has a plurality of perforations there-through and at least one downwardly extending tube passing through the plate. The perforations and tube are sized such that under equilibrium feed conditions a gas pocket forms below the plate having a height less than or sub-stantially equal to the tube length. Substantially all of the feed gas passes through the plate perforations and substantially all of the feed liquid or liquid and solids, passes through the tube.
Description
11773F~S
BACKGROUND OF THE INVENTION
1. Field of the Invention 05 This invention pertains to a reactor feed dis-tributor that is useful in upflow reactors for mixed phase feed streams. The distributor is particularly useful in catalytic coal liquefaction reactors which must be capable of accommodating feeds comprising gases, liquids and solids.
BACKGROUND OF THE INVENTION
1. Field of the Invention 05 This invention pertains to a reactor feed dis-tributor that is useful in upflow reactors for mixed phase feed streams. The distributor is particularly useful in catalytic coal liquefaction reactors which must be capable of accommodating feeds comprising gases, liquids and solids.
2. Prior Art For many processes an upflow reactor is superior to the more common downflow reactors. This is partic-ularly true in those situations in which a liquid feed also contains solids since the solids tend to pack and form obstructions in the downflow mode. The problems are further amplified if the feed stream is comprised of gases as well as solids and liquids.
Upflow reactors are commonly employed in coal liquefaction systems such as the liquefaction process disclosed in U.S. Patent No. 4,083,769, issued to Hildebrand et al on April 8, 1978. As taught in the ref-erence, hydrogen, ground coal and solvent are preheated and passed to a dissolver wherein the coal is substan-tially dissolved at a temperature in the range 750-900F
(379-482C) and at a pressure in the range 3100-5000 psi (217 kg/cm2-350 kg/cm2). The dissolver is an empty upflow reactor vessel which provides sufficient residence time for the dissolution of the ground coal particles to occur.
Solvent, dissolved coal, coal residue and hydrogen from the dissolver are passed to an upflow catalytic hydro-genation reactor operating at a temperature 25-150F
(13.9-83.3C) lower than the dissolver.
Since the hydrogen is mixed with the coal slurry prior to the preheating step to avoid coking in the q~
,~
., 01 heater, little or no control is exerted over the degree of liquid and gas mixing which occurs in the dissolver or catalytic reactor. With multiphase flow, gas channeling and/or slugging in these units may occur. The presence of either condition is undesirabl~ since both result in inadequate contacting of the reactants and the slugging may also create damaging equipment vibrations. Further-more, inadequate hydrogen mixing can lead to coking of the reactants and equipment fouling at the described process conditions.
Thus, it is apparent that a need exists for a distributor which will accept feed streams comprising liquids, gases and solids and evenly distribute the phases without plugging or suffering undue erosion.
Although numerous mixed phase distributors are known in the art, such as those disclosed in U.~. Patents Nos. 3,524,731; 4,111,663; 3,146,189; 3,195,987 and 4,187,169, a need remains for an efficient and economical solution to the problem.
SUMMARY OF THE INVENTION
There is provided by the present invention a distributor for a gas-liquid or gas-liquid-solid feed upflow reactor vessel having a feed inlet port in the i lower portion thereof and an effluent outlet port in the i 25 upper portion thereof. The distributor is comprised of a substantially horizontally disposed plate mounted in the vessel between the inlet and outlet ports. The plate has a plurality of holes extending therethrough and at least one downwardly extending tube in open communication with the reactor vessel volume below said plate and in open communication with the reactor vesse1 volume above said plate~ The cross sectional area of the plate perforations - and the cross sectional area and length of the tube are designed such that under equilibrium feed conditions a gas pocket forms below the plate having a height less than or 01 equal to the length of the tube. Substantially all, i.e., at least 75% and preferably greater than 95~, of the feed gas will pass through the plurality of holes in the plate and substantially all, i.e., at least 75% and preferably 05 greater than 95%, of the feed liquid or feed liquid and solids will pass through the tube.
The distributor of the present invention will preferably be used in a reactor which contains a fixed or moving bed of particulate catalyst for evenly distributing the gas and liquid or gas, liquid and solids throughout the catalyst bed. However, it may advantageously be used in non-catalytic vessels such as dissolvers to insure good contacting of the hydrogen gas with the liquids and solids to prevent coking within the vessel.
Preferably, means are also provided for prevent-ing the direct vertical passage of feed gas bubbles into the lower end of the tube. If the distributor is used in a catalytic reaction vessel, the distributor should be located far enough below the lowest level of catalyst such that any gas fingering that occurs will be totally within the liquid volume situated immediately below the catalyst.
Although a single distributor can suffice in some reac-tors, in commercial practice multiple distributors will generally be vertically spaced throughout a reactor.
Furthermore, the distributor of the present invention is particularly suitable for gas quenching or gas withdrawal applications.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. l depicts an upflow fixed bed catalytic reactor having a single distributor.
FIG. 2 depicts an upflow fixed bed catalytic reactor having multiple distributors and adapted for the injection of gas between distributors.
~17'73~5 Referring to FIG.l there is shown a vertically oriented reactor vessel 10 having a lower feed inlet port 20 and an effluent outlet port 30. A fixed bed of porous S particulate catalyst 40 is maintained in the vessel between a lower support grid 50, attached to the inner wall of ve~sel 10, and, if desired, a catalyst retaining screen 60, also secured to the vessel inner wall.
The distributor of the present invention, generally characterized by reference numeral 70, is attached to the inner wall of vessel 10, between inlet port 20 and catalyst support grid 50. The distributor may be affixed to the vessel wall in any convenient or conven-tional manner such as by welding or bolting.
Distributor 70 is comprised of a plate 80 extending over the full cross sectional area of vessel 10.
The plate has a plurality of perforations or holes 90 extending therethrough. Preferably the perforations are evenly distributed over the total cross sectional area of the plate with about 20-250 or more preferably about 40-250 perforations per square meter. An open-ended tube 100 is conventionally affixed to plate 80 and extends downwardly from a central aperture in said plate.
Although only a single tube is shown in the drawing, it is within the scope of this invention to provide more than one tube if same is required by the feed conditions or reactor size. Preferably about ten or twenty tubes will be used per square meter of plate surface.
A cap 110 is provided at the lower end of tube 100 to prevent gases in the feed from passing directly up through the tube. Although cap 110 is shown as being con-ventionally secured to the end of tube 100 by extension 120, it may be replaced by an equivalent baffle secured to the vessel wall. It is also possible to offset the inlet port from the end of tube 100 in such a manner as to 11773~5 01 obviate the problem. In the event a cap is used as shown in the drawing it will preferably be about 20% larger than the tube diameter. When multiple distributors are employed in a vessel, the upper distributors may not 05 require a cap to prevent substantial gas from entering the - tube.
In operation a mixed phase feed stream, prefer-ably comprised of liquid, gas and solid components, such as might be introduced to a dissolver or catalytic reactor of a coal liquefaction unit, is pumped or otherwise intro-duced into the bottom of vessel 10 through inlet port 20.
In accordance with the invention, the distri-butor is designed for the feed conditions such that a gas pocket, or vapor space 130, having a height, h, which is substantially equal to or less than the length of tube 100 extending below the plate, is formed under steady state conditions and substantially all, i.e., at least 75%, of the gas and vapor components of the feed pass through holes 90 and substantially all of the liquid and solid components of the feed pass through tube 100.
It is observed that the required flow path of the gases and liquids will be realized if the pressure drop of the vapor flow through the plurality of holes, 90, is balanced by the pressure drop of the flow of liquids and solids through tube 100 plus the static pressure differential between the liquids and solids of height h and the gas pocket, i.e., the static head of the liquids and solids through the tube.
The pressure drop due to gas flow through a perforated plate may be predicted by the orifice equation.
If the liquid and solids pressure drop in the tube is negligible, the gas pressure drop may simply be balanced against the static pressure differential, equal to (pl-pg)h, wherein Pl is the density of the liquid and solids stream in the tube and pg is the gas density.
~1773~35 01 Preferably the distributor is designed with a minimum value for h of approximately 5-10 centimeters.
More preferably, h should be set at approximately 10-20 centimeters and a design tube length selected of approx-05 imately 20 centimeters. These values will allow forsubstantial variation in vapor rates and therefore gas pocket heights. At the design flow rates these values will also ensure that the lower end of the tube is substantially even with or below the liquid surface to prevent significant gas entry from the tube upon liquid surface disturbances.
The upper surface of the horizontal perforated plate should be preferably disposed approximately 3-10 centimeters below lower grid 50, depending upon gas bubble growth.
Although the preferred embodiment has been particularly described with reference to feeds for coal liquefaction units, it is apparent that the distributor of the present invention may be used in any system having gas-liquid or gas-solid-liquid feeds. Furthermore, if the unit is to be used as gas quenching apparatus, the gas need only be injected below plate 80 for even thorough distribution.
FIG. 2 depicts the apparatus of this invention having multiple distributors 70 and multiple catalyst beds 40. The catalyst beds 40 are drawn smaller than scale in order to depict the distributor detail. Quench gas, such as recycle gas containing hydrogen for a catalytic coal liquefaction process, is added through ports 150, into vapor spaces 130. Ports 150 can also be used to withdraw gas from vapor spaces 130. If desired, tube 100 can extend into the upper portion of catalyst beds 40, pref-erably with the catalyst in the tube at substantially the same level as the rest of the catalyst bed. Also, the gas pocket can contain a portion of the atalyst, if desirGd.
Upflow reactors are commonly employed in coal liquefaction systems such as the liquefaction process disclosed in U.S. Patent No. 4,083,769, issued to Hildebrand et al on April 8, 1978. As taught in the ref-erence, hydrogen, ground coal and solvent are preheated and passed to a dissolver wherein the coal is substan-tially dissolved at a temperature in the range 750-900F
(379-482C) and at a pressure in the range 3100-5000 psi (217 kg/cm2-350 kg/cm2). The dissolver is an empty upflow reactor vessel which provides sufficient residence time for the dissolution of the ground coal particles to occur.
Solvent, dissolved coal, coal residue and hydrogen from the dissolver are passed to an upflow catalytic hydro-genation reactor operating at a temperature 25-150F
(13.9-83.3C) lower than the dissolver.
Since the hydrogen is mixed with the coal slurry prior to the preheating step to avoid coking in the q~
,~
., 01 heater, little or no control is exerted over the degree of liquid and gas mixing which occurs in the dissolver or catalytic reactor. With multiphase flow, gas channeling and/or slugging in these units may occur. The presence of either condition is undesirabl~ since both result in inadequate contacting of the reactants and the slugging may also create damaging equipment vibrations. Further-more, inadequate hydrogen mixing can lead to coking of the reactants and equipment fouling at the described process conditions.
Thus, it is apparent that a need exists for a distributor which will accept feed streams comprising liquids, gases and solids and evenly distribute the phases without plugging or suffering undue erosion.
Although numerous mixed phase distributors are known in the art, such as those disclosed in U.~. Patents Nos. 3,524,731; 4,111,663; 3,146,189; 3,195,987 and 4,187,169, a need remains for an efficient and economical solution to the problem.
SUMMARY OF THE INVENTION
There is provided by the present invention a distributor for a gas-liquid or gas-liquid-solid feed upflow reactor vessel having a feed inlet port in the i lower portion thereof and an effluent outlet port in the i 25 upper portion thereof. The distributor is comprised of a substantially horizontally disposed plate mounted in the vessel between the inlet and outlet ports. The plate has a plurality of holes extending therethrough and at least one downwardly extending tube in open communication with the reactor vessel volume below said plate and in open communication with the reactor vesse1 volume above said plate~ The cross sectional area of the plate perforations - and the cross sectional area and length of the tube are designed such that under equilibrium feed conditions a gas pocket forms below the plate having a height less than or 01 equal to the length of the tube. Substantially all, i.e., at least 75% and preferably greater than 95~, of the feed gas will pass through the plurality of holes in the plate and substantially all, i.e., at least 75% and preferably 05 greater than 95%, of the feed liquid or feed liquid and solids will pass through the tube.
The distributor of the present invention will preferably be used in a reactor which contains a fixed or moving bed of particulate catalyst for evenly distributing the gas and liquid or gas, liquid and solids throughout the catalyst bed. However, it may advantageously be used in non-catalytic vessels such as dissolvers to insure good contacting of the hydrogen gas with the liquids and solids to prevent coking within the vessel.
Preferably, means are also provided for prevent-ing the direct vertical passage of feed gas bubbles into the lower end of the tube. If the distributor is used in a catalytic reaction vessel, the distributor should be located far enough below the lowest level of catalyst such that any gas fingering that occurs will be totally within the liquid volume situated immediately below the catalyst.
Although a single distributor can suffice in some reac-tors, in commercial practice multiple distributors will generally be vertically spaced throughout a reactor.
Furthermore, the distributor of the present invention is particularly suitable for gas quenching or gas withdrawal applications.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. l depicts an upflow fixed bed catalytic reactor having a single distributor.
FIG. 2 depicts an upflow fixed bed catalytic reactor having multiple distributors and adapted for the injection of gas between distributors.
~17'73~5 Referring to FIG.l there is shown a vertically oriented reactor vessel 10 having a lower feed inlet port 20 and an effluent outlet port 30. A fixed bed of porous S particulate catalyst 40 is maintained in the vessel between a lower support grid 50, attached to the inner wall of ve~sel 10, and, if desired, a catalyst retaining screen 60, also secured to the vessel inner wall.
The distributor of the present invention, generally characterized by reference numeral 70, is attached to the inner wall of vessel 10, between inlet port 20 and catalyst support grid 50. The distributor may be affixed to the vessel wall in any convenient or conven-tional manner such as by welding or bolting.
Distributor 70 is comprised of a plate 80 extending over the full cross sectional area of vessel 10.
The plate has a plurality of perforations or holes 90 extending therethrough. Preferably the perforations are evenly distributed over the total cross sectional area of the plate with about 20-250 or more preferably about 40-250 perforations per square meter. An open-ended tube 100 is conventionally affixed to plate 80 and extends downwardly from a central aperture in said plate.
Although only a single tube is shown in the drawing, it is within the scope of this invention to provide more than one tube if same is required by the feed conditions or reactor size. Preferably about ten or twenty tubes will be used per square meter of plate surface.
A cap 110 is provided at the lower end of tube 100 to prevent gases in the feed from passing directly up through the tube. Although cap 110 is shown as being con-ventionally secured to the end of tube 100 by extension 120, it may be replaced by an equivalent baffle secured to the vessel wall. It is also possible to offset the inlet port from the end of tube 100 in such a manner as to 11773~5 01 obviate the problem. In the event a cap is used as shown in the drawing it will preferably be about 20% larger than the tube diameter. When multiple distributors are employed in a vessel, the upper distributors may not 05 require a cap to prevent substantial gas from entering the - tube.
In operation a mixed phase feed stream, prefer-ably comprised of liquid, gas and solid components, such as might be introduced to a dissolver or catalytic reactor of a coal liquefaction unit, is pumped or otherwise intro-duced into the bottom of vessel 10 through inlet port 20.
In accordance with the invention, the distri-butor is designed for the feed conditions such that a gas pocket, or vapor space 130, having a height, h, which is substantially equal to or less than the length of tube 100 extending below the plate, is formed under steady state conditions and substantially all, i.e., at least 75%, of the gas and vapor components of the feed pass through holes 90 and substantially all of the liquid and solid components of the feed pass through tube 100.
It is observed that the required flow path of the gases and liquids will be realized if the pressure drop of the vapor flow through the plurality of holes, 90, is balanced by the pressure drop of the flow of liquids and solids through tube 100 plus the static pressure differential between the liquids and solids of height h and the gas pocket, i.e., the static head of the liquids and solids through the tube.
The pressure drop due to gas flow through a perforated plate may be predicted by the orifice equation.
If the liquid and solids pressure drop in the tube is negligible, the gas pressure drop may simply be balanced against the static pressure differential, equal to (pl-pg)h, wherein Pl is the density of the liquid and solids stream in the tube and pg is the gas density.
~1773~35 01 Preferably the distributor is designed with a minimum value for h of approximately 5-10 centimeters.
More preferably, h should be set at approximately 10-20 centimeters and a design tube length selected of approx-05 imately 20 centimeters. These values will allow forsubstantial variation in vapor rates and therefore gas pocket heights. At the design flow rates these values will also ensure that the lower end of the tube is substantially even with or below the liquid surface to prevent significant gas entry from the tube upon liquid surface disturbances.
The upper surface of the horizontal perforated plate should be preferably disposed approximately 3-10 centimeters below lower grid 50, depending upon gas bubble growth.
Although the preferred embodiment has been particularly described with reference to feeds for coal liquefaction units, it is apparent that the distributor of the present invention may be used in any system having gas-liquid or gas-solid-liquid feeds. Furthermore, if the unit is to be used as gas quenching apparatus, the gas need only be injected below plate 80 for even thorough distribution.
FIG. 2 depicts the apparatus of this invention having multiple distributors 70 and multiple catalyst beds 40. The catalyst beds 40 are drawn smaller than scale in order to depict the distributor detail. Quench gas, such as recycle gas containing hydrogen for a catalytic coal liquefaction process, is added through ports 150, into vapor spaces 130. Ports 150 can also be used to withdraw gas from vapor spaces 130. If desired, tube 100 can extend into the upper portion of catalyst beds 40, pref-erably with the catalyst in the tube at substantially the same level as the rest of the catalyst bed. Also, the gas pocket can contain a portion of the atalyst, if desirGd.
Claims (16)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. In combination with a gas-liquid or gas-liquid-solid feed upflow reaction vessel having feed inlet means in the lower portion of the vessel and effluent outlet means in the upper portion of said vessel, a distributor which comprises:
a substantially horizontally disposed plate mounted in said vessel between said inlet means and said outlet means, said plate having a plurality of holes therethrough and at least one downwardly extending tube in open com-munication with the reactor vessel volume below said plate and in open communication with the reactor vessel volume above said plate, the cross sectional area of the holes and of the tube being such that under equilibrium feed conditions a gas pocket forms below said plate having a height less than or substantially equal to the length of the tube and such that substantially all of the gas feed to said distributor passes through said plurality of holes and substantially all of the liquid feed to said distrib-utor passes through said tube.
a substantially horizontally disposed plate mounted in said vessel between said inlet means and said outlet means, said plate having a plurality of holes therethrough and at least one downwardly extending tube in open com-munication with the reactor vessel volume below said plate and in open communication with the reactor vessel volume above said plate, the cross sectional area of the holes and of the tube being such that under equilibrium feed conditions a gas pocket forms below said plate having a height less than or substantially equal to the length of the tube and such that substantially all of the gas feed to said distributor passes through said plurality of holes and substantially all of the liquid feed to said distrib-utor passes through said tube.
2. The combination as recited in Claim 1, wherein said reaction vessel further comprises a particulate bed of solids disposed below the effluent outlet means and above the distributor plate.
3. The combination as recited in Claim 1, further comprising means for preventing the direct vertical pas-sage of feed gas bubbles into said tube.
4. The combination as recited in Claim 1, compris-ing a plurality of said distributors spaced vertically apart within said reactor vessel.
5. The combination as recited in Claim 4, wherein said reaction vessel further comprises at least one particulate bed of solids disposed below said effluent outlet means and above one of said distributor plates.
6. The combination as recited in Claim 4, further comprising means for preventing the direct vertical passage of gas bubbles into said tubes.
7. The combination as recited in Claim 1, 2 or 3, further comprising means for introducing gas into one or more of said gas pockets.
8. The combination as recited in Claim 1, 2 or 3, further comprising means for withdrawing gas from one or more of said gas pockets.
9. The combination as recited in Claim 1, 2 or 3, wherein said horizontally disposed plate is fixedly mounted in said vessel.
10. The combination as recited in Claim 4, 5 or 6, further comprising means for introducing gas into one or more of said gas pockets.
11. The combination as recited in Claim 4, 5 or 6, further comprising means for withdrawing gas from one or more of said gas pockets.
12. The combination as recited in Claim 4, 5 or 6, wherein said horizontally disposed plate is fixedly mounted in said vessel.
13. The combination as recited in Claim 1, 2 or 3, further comprising means for introducing gas into one or more of said gas pockets and means for withdrawing gas from one or more of said gas pockets.
14. The combination as recited in Claim 4, 5 or 6, further comprising means for introducing gas into one or more of said gas pockets and means for withdrawing gas from one or more of said gas pockets.
15. The combination as recited in Claim 1, 2 or 3, further comprising means for introducing gas into one or more of said gas pockets and means for withdrawing gas from one or more of said gas pockets and wherein said horizontally disposed plate is fixedly mounted in said vessel.
16. The combination as recited in Claim 4, 5 or 6, further comprising means for introducing gas into one or more of said gas pockets and means for withdrawing gas from one or more of said gas pockets and wherein said horizontally disposed plate is fixedly mounted in said vessel.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US16079380A | 1980-06-19 | 1980-06-19 | |
| US160,793 | 1980-06-19 | ||
| US23865181A | 1981-03-09 | 1981-03-09 | |
| US238,651 | 1988-08-30 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1177385A true CA1177385A (en) | 1984-11-06 |
Family
ID=26857229
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000377087A Expired CA1177385A (en) | 1980-06-19 | 1981-05-07 | Gas-pocket distributor for an upflow reactor |
Country Status (6)
| Country | Link |
|---|---|
| AU (1) | AU537031B2 (en) |
| CA (1) | CA1177385A (en) |
| DE (1) | DE3123695A1 (en) |
| FR (1) | FR2484864B1 (en) |
| GB (1) | GB2078537B (en) |
| NL (1) | NL8102816A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4968409A (en) * | 1984-03-21 | 1990-11-06 | Chevron Research Company | Hydrocarbon processing of gas containing feed in a countercurrent moving catalyst bed |
| US5308476A (en) * | 1990-05-16 | 1994-05-03 | Amoco Corporation | Reduced gas holdup in an ebullated bed reactor |
| CN104789253A (en) * | 2015-04-20 | 2015-07-22 | 神华集团有限责任公司 | Coal liquefaction reactor and coal liquefaction production system |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2559074B1 (en) * | 1984-02-07 | 1988-05-20 | Inst Francais Du Petrole | METHOD AND APPARATUS FOR SUPPORTING CATALYTIC PARTICLES OUTSIDE A REACTION ZONE |
| US4988486A (en) * | 1985-08-02 | 1991-01-29 | The Boeing Company | Hydrogen generator |
| NL8600428A (en) * | 1986-02-20 | 1987-09-16 | Shell Int Research | METHOD AND APPARATUS FOR CONTACTING GAS, LIQUID AND PARTICLES |
| EP0359952A3 (en) * | 1988-08-05 | 1990-07-18 | Ammonia Casale S.A. | System for the improvement of reactors for the synthesis of methanol and reactors obtained therefrom |
| KR100298855B1 (en) * | 1996-08-07 | 2001-11-14 | 다나카 쇼소 | Gas-liquid dispersion device and gas-liquid contact device and wastewater treatment device |
| FR2919058B1 (en) * | 2007-07-17 | 2010-06-11 | Inst Francais Du Petrole | METHOD AND INSTALLATION FOR TESTING CATALYSTS |
| DE102009039644A1 (en) | 2009-09-01 | 2011-03-03 | Linde Aktiengesellschaft | Bubble-column reactor comprises a container that is partially filled with a fluid, a gas supply device arranged in lower portion of the container, and a gas discharge device in upper portion of the container |
| CN114733451A (en) * | 2022-04-15 | 2022-07-12 | 青岛科技大学 | Continuous gas-liquid reaction device with adjustable residence time |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1068650A (en) * | 1951-05-31 | 1954-06-29 | Houdry Process Corp | Improvements to apparatus for lifting granular solids in dense mass by means of gas |
| BE556022A (en) * | 1956-03-24 | 1900-01-01 | ||
| AT280964B (en) * | 1966-10-31 | 1970-05-11 | Albert Dipl Ing Dr Techn Hackl | Process for carrying out mass and / or heat exchange processes between gases and liquids |
| NL171233C (en) * | 1971-05-12 | 1983-03-01 | Comprimo N V | Apparatus for carrying out reactions in heterogeneous systems as well as a method for preparing hypochlorous acid using this apparatus. |
| DE2157737C3 (en) * | 1971-11-22 | 1981-10-29 | Schering Ag Berlin Und Bergkamen, 1000 Berlin | Continuous processes in a bubble column reactor |
| DE2157736B2 (en) * | 1971-11-22 | 1978-10-05 | Schering Ag, 1000 Berlin Und 4619 Bergkamen | Device for the continuous contacting of liquids with gases or of liquids in the presence of gases or of liquids with solids in the presence of gases or of liquids with gases and finely divided solids in cocurrent |
| DE2331195A1 (en) * | 1973-06-19 | 1975-01-30 | Bayer Ag | PROCESS FOR CONTROLLING MULTI-STAGE FUEL EXCHANGE PILLOWS WITH VARIABLE BUBBLE LAYER HEIGHTS |
| BE864590A (en) * | 1977-03-10 | 1978-09-06 | Inst Francais Du Petrole | METHOD AND APPARATUS FOR CARRYING OUT THREE-PHASE CATALYTIC REACTIONS |
-
1981
- 1981-05-07 CA CA000377087A patent/CA1177385A/en not_active Expired
- 1981-05-12 AU AU70485/81A patent/AU537031B2/en not_active Ceased
- 1981-06-11 NL NL8102816A patent/NL8102816A/en not_active Application Discontinuation
- 1981-06-12 GB GB8118041A patent/GB2078537B/en not_active Expired
- 1981-06-12 FR FR8111620A patent/FR2484864B1/en not_active Expired
- 1981-06-15 DE DE19813123695 patent/DE3123695A1/en active Granted
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4968409A (en) * | 1984-03-21 | 1990-11-06 | Chevron Research Company | Hydrocarbon processing of gas containing feed in a countercurrent moving catalyst bed |
| US5308476A (en) * | 1990-05-16 | 1994-05-03 | Amoco Corporation | Reduced gas holdup in an ebullated bed reactor |
| CN104789253A (en) * | 2015-04-20 | 2015-07-22 | 神华集团有限责任公司 | Coal liquefaction reactor and coal liquefaction production system |
Also Published As
| Publication number | Publication date |
|---|---|
| FR2484864B1 (en) | 1987-07-10 |
| FR2484864A1 (en) | 1981-12-24 |
| GB2078537A (en) | 1982-01-13 |
| AU537031B2 (en) | 1984-05-31 |
| DE3123695A1 (en) | 1982-05-06 |
| AU7048581A (en) | 1981-12-24 |
| GB2078537B (en) | 1984-01-25 |
| NL8102816A (en) | 1982-01-18 |
| DE3123695C2 (en) | 1992-11-12 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |