CA1243597A - Multi-phase countercurrent reactor process and apparatus - Google Patents
Multi-phase countercurrent reactor process and apparatusInfo
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- CA1243597A CA1243597A CA000491887A CA491887A CA1243597A CA 1243597 A CA1243597 A CA 1243597A CA 000491887 A CA000491887 A CA 000491887A CA 491887 A CA491887 A CA 491887A CA 1243597 A CA1243597 A CA 1243597A
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Abstract
MULTI-PHASE COUNTERCURRENT REACTOR PROCESS AND APPARATUS
ABSTRACT OF THE DISCLOSURE
A countercurrent continuous catalytic reactor and process for treating a liquid phase, such as oil, with a gaseous reactant.
An enclosed reactor shell 10 contains a fixed porous bed 12 of solid catalyst, an upper liquid inlet 14 for introducing a stream of liquid substantially above the catalyst bed 12 for downward gravity flow through the bed, and a lower liquid outlet 16 for withdrawing treated liquid prom the reactor shell 10. A gaseous reactant is dispersed through the liquid phase in intimate contact with the solid catalyst, and withdrawn above the catalyst bed 12. A level detector 30 is disposed in a froth zone above the catalyst bed 12 for detecting level of a mixed gas-liquid froth. Fluid handling control 32 responsive to a level signal controls fluid stream flow for regulating froth level above the catalyst bed 12.
ABSTRACT OF THE DISCLOSURE
A countercurrent continuous catalytic reactor and process for treating a liquid phase, such as oil, with a gaseous reactant.
An enclosed reactor shell 10 contains a fixed porous bed 12 of solid catalyst, an upper liquid inlet 14 for introducing a stream of liquid substantially above the catalyst bed 12 for downward gravity flow through the bed, and a lower liquid outlet 16 for withdrawing treated liquid prom the reactor shell 10. A gaseous reactant is dispersed through the liquid phase in intimate contact with the solid catalyst, and withdrawn above the catalyst bed 12. A level detector 30 is disposed in a froth zone above the catalyst bed 12 for detecting level of a mixed gas-liquid froth. Fluid handling control 32 responsive to a level signal controls fluid stream flow for regulating froth level above the catalyst bed 12.
Description
35g'7 MULTI-PHASE COUNTERCURRENT REACTOR PROCESS AND APPARATUS
This invention relates to catalytic reactor operation wherein a liquid phase is treated with a gaseous reactant. In particular it relates to a technique for contacting multi-phase reactants in a fixed porous catalyst bed under continuous countercurrent conditions, including methods and apparatus for controlling frothing in the reactor.
Chemical reactions between liquid and gaseous reactants present difficulties in obtaining intimate contact between phases.
Such reactions are further complicated when the desired reaction is catalytic, and requires contact of both fluid phases with a solid catalyst. Numerous multi-phase reactor systems have been developed wherein a fixed porous bed of solid catalyst is retained in a reactor. Typically, fixed bed reactors have been arranged with the diverse phases being passed cocurrently over the catalyst, for instance as shown in U.S. Patents No. 4,126,539 (Derr et al), 4,235,847 (Scott), 4,283,271 (Garwood et al), and 4,396, 538 (Chen et al). In the petroleum refining industry, multi-phase catalytic reactor systems have been employed for dewaxing, hydrogenation, desulfurizing, hydrocracking, isomerization and other treatments of liquid feedstocks, especially distillates, lubricants, heavy oil fractions, residuum, etc,. Other known techniques for contacting liquid-gas mixtures with solid catalysts include slurry catalyst, ebullated bed and countercurrent systems, such as disclosed in U. S.
Patents 2,717,202, 3,186,935, 4,221,653, and 4,269,805. While prior ~2435~7 reactor systems are satisfactory for certain needs, efficient multi-phase contact has been difficult to achieve for many fixed bed applications.
It would be beneficial to have a multi-phase reactor operating under controlled flow conditions to maintain a gas-liquid froth, which could minimize flow maldistribution patterns and provide optimum volumetric proportions of upwardly moving gas dispersed in a downwardly gravitating liquid phase.
Accordingly, the present invention provides a countercurrent continuous catalytic reactor for treating a liquid phase with a gaseous reactant characterized by an enclosed reactor shell containing a fixed porous bed of solid catalyst, an upper liquid inlet for introducing a stream of liquid substantially above the catalyst bed for downward gravity flow of liquid through the bed, a lower liquid outlet for withdrawing treated liquid from the reactor shell, a gas inlet disposed below the catalyst bed for introducing a gaseous reactant stream under pressure for countercurrently contacting downwardly flowing liquid in a mixed phase reaction zone, whereby gaseous reactant is dispersed through the liquid phase in intimate contact with the solid catalyst, an upper gas outlet for withdrawing gas from the reactor shell above the catalyst bed, a level detector disposed in a froth zone above the catalyst bed for detecting level of a mixed gas-liquid froth and generating a signal representative of froth level, and a fluid handling control operatively connected to the level detector and responsive to the level signal to control fluid stream flow for regulating froth level above the catalyst bed thereby permitting disengagement of dispersed gas from the liquid phase of the froth and preventing excessive liquid entrainment in the gas outlet.
In another embodiment, the present invention provides a process for catalytic hydrocracking dewaxirg or desulfurizing of heavy petroleum feedstock in a multi-phase catalytic reactor containing a fixed porous bed of solid particles characterized by using the above-described reactor.
3~
Figure l is a simplified process diagram showing a vertical reactor with fixed catalyst bed, major flow streams, and control elements;
Figure 2 is a segmented vertical cross-section view of a reactor showing stripping and distributor sections;
Figure is a countercurrent catalyst bed, according to the present invention, shown in segmented vertical cross section aligned with the optional top section of Figure 2; and Figure 4 is a process diagram for an integrated heavy oil lo repining process.
Cnuntercurrent processes for contacting reactant fluids have several advantages. In a single point gas entry system, as the reactant gas rises upwardly from its point of introduction at the bottom of a vertical reactor below the porous bed, it contacts a lower concentration of reactive liquid components. At the point of entry the reactant gas has its greatest concentration. Depletion of the gaseous reactant upwardly will increase the relative concentration of inerts and/or byproduct vapors. Likewise, the liquid being treated is generally more reactive at the upper end of the reactor system where it contacts the depleted rising gaseous phase. Thus, the reactant concentration gradients for countercurrent two-phase systems are opposing. In a typical multi-phase reactor system, the average gas-liquid volume ratio in the catalyst zone is about i to 4:1 under process conditions.
In those reactions wherein the volume of gas decreases due to reactant depletion, the volumetric ratio or liquid to gas can increase markedly as the liquid feedstock gravitates downwardly through the reactor. In reactions which consume large amounts of hydrogen it may be desirable to have multiple reaction gas feed grids at various levels in the catalyst bed. In general, the quantity of unreacted gas at any particular level should be adequate to provide a mixed phase bulk density of at least 20% of the bulk density of the liquid phase (at reaction conditions). Vapor production, adiabatic heating or expansion can also affect the volume.
~35~
Advantageously, the multi-phase reactor system is operated to achieve uniform distribution. If too little liquid flux is maintained, the catalyst surface in the porous bed will be coated with a liquid film; however, this trickle mode will permit excessive channeling of the gas phase instead of the desired dispersion characteristics of a reactant froth. Flow rates for both reactant phases are controlled within constraints. Froth formation and disengagement is a function of the liquid viscosity, surface tension and composition. By detecting and controlling froth level, the lo proper operation of the reactor can be assured.
In order to maintain a desirable uniform flow of reactant streams through the fixed catalyst bed, adequate flow paths for liquid and gaseous phases must be provided. In a continuous process the ratio of reactant gas to liquid feedstock and the space velocity of reactants relative to catalyst must be carefully considered.
Achievement of uniform vertical flow through a porous bed of solids can be obtained if the catalyst is properly distributed and shaped.
The void volume in a reaction zone is a function of catalyst configuration and loading technique. While a densely packed bed of spherical solids may be employed to place a maximum amount of catalyst in a predetermined reactor volume, the low void fraction may interfere with fluid flow, especially where countercurrent flow of two phases is required. Advantageously, the catalyst bed has a high void volume, typically greater than one half of the bed. Void fractions from 0.5 to 0.9 can be achieved using loosely packed polylobal or cylindrical extrudates. Hollow ring-type supported catalysts, such as Raschig rings or the like, permit liquids to flow downwardly through the porous bed by gravity while the gas phase reactant rises through the denser liquid, forming dispersed bubbles which contact the wetted catalyst to enhance mass transfer and catalytic phenomena.
Catalyst size can vary widely within the inventive concept, depending upon process conditions and reactor structure. If a low space velocity or long residence in the catalytic reacton zone is ~.2~3~
.
permissible, small catalysts having an average maximum dimension of l to 5 mm may be employed. However, it is preferred to use larger sizes, e.g., 0.5-2 cm or more, especially when extrudates, rings, saddles or other contact materials are desired. Relatively small catalyst particles may be loaded randomly to assure uniformity and larger supported catalysts may be stacked in a geometric pattern to achieve optîmum bed utilization.
Reactor conFiguration is an important consideration in the design of a continuously operating system. In its simplest form, a lo vertical cylindrical pressure vessel is provided with a catalyst retaining device and operatively connected for countercurrent fluid flow. A typical vertical reactor having a catalyst bed length to effective diameter (L:D) ratio of about l:l to 20:1 is preferred. A
single bed or a stacked series of beds may be retained within the same reactor shell. While a reactor of uniform horizontal cross section is disclosed herein, other non-uniform configurations, such as spherical reactors9 tapered vessels, etc., may be employed.
Referring to Figure l, a countercurrent continuous catalytic reactor system is shown for treating a liquid phase with a gaseous reactant. An enclosed reactor shell lO contains a fixed porous bed 12 of solid catalyst. Upper liquid inlet 14 is provided for introducing a stream of liquid substantially above the catalyst bed for downward gravity flow through the bed toward lower liquid outlet 16 for withdrawing treated liquid from the reactor shell.
Gas inlet 20 is disposed below the catalyst bed for introducing a gaseous reactant stream under pressure for countercurrently contacting downwardly flowing liquid in a mixed phase reaction zone, whereby gaseous reactant is dispersed through the liquid phase in intimate contact with the solid catalyst. After passing through a reactant disengagement zone 22 above the catalyst bed 12 through upper gas outlet 24, gas is withdrawn From the reactor shell lO.
Level detector 30 is disposed in a froth zone between interface levels Hl and H2 above the catalyst bed for detecting the level of a mixed gas-liquid froth and generating a signal ~LX~5~3~
representative of the froth level. Fluid handling control is provided by control module ~27 responsive to the level signal to control fluid stream flow for regulating froth level above the catalyst bed, thereby permitting disengagement of dispersed gas from the liquid phase of the froth and preventing excessive liquid entrainment in the gas outlet. The fluid handling control may include liquid outlet valve 34 for withdrawing treated liquid at increased rate with increased froth level. Liquid and gas reactant feed rates may be controlled proportionally or as otherwise predetermined by setting control module 32 to operate liquid feed valve 36 and/or gas feed valve 38. Inlet flow control may be employed to vary the interface or froth level, as well as reactant proportions.
A more detailed depiction of a catalytic reactor system, lS for use with the present invention is shown in Figs. 2 and 3, both of which are segments of a vertical reactor. Fig. 2 is a top segment of a reactor 110 having upper liquid feed inlet 114 for introducing the charged feed to an optional stripping section 120.
In a typical application, such as lube oil dewaxing or mild desulfurization, the preheated liquid feed is introduced into the upper part oF a stripping section, where the feed is stripped of volatile components, dissolved and entrained contaminants by countercurrent stripping with the product gas stream rising from the catalyst bed. The gas stream is removed from the reactor through top gas outlet 125, which may have a back pressure regulator 130 responsive to pressure of the enclosed reactor. Additional stripping gas may be introduced via inlet 118 into the lower part of the stripping section, if desired. The quantity of stripping gas should be sufficient to saturate the entering liquid feed with the gas plus enough additional gas to achieve the desired removal of contaminants such as entrained water, H2S, water vapor, and the like. The temperature and pressure in the stripping zone approximate the conditions desired in the catalyst bed. It is understood that the feed stripping feature may not be required in all instances.
9~7 The liquid feed flowing down from the stripper (or directly from the feed source if a stripper is not employed) passes to a horizontal distributor tray 130 which spreads the liquid across the catalyst bed. The distributor tray is provided with gas risers 132 to allow rising gas to pass through the tray and proceed upwardly.
A typical distributor tray has a spaced array of perforations or orifices 135 sized to allow even liquid stream flow from the upper surface of the horizontal tray 130 into the disengagement zone below, further depicted in Fig. 3.
ReFerring to Fix. 3, the bottom segment of a typical vertical reactor shell 210 is shown in broken vertical cross section view. A bed of catalyst particles 212 is maintained within the main central portion of reactor 210 by a catalyst support grid 214, having retainer 215 to prevent loss of particles from the bed. A
plurality of liquid collector pipes 217 recover treated liquid via plenum chamber 218, outlet conduit 216 and liquid control valve 234. Flow equalizing restrictions may be ernployed with the collector pipes to assure even withdrawal. Reaction gas is injected into the lower part of the catalyst bed through a gas sparger-type inlet 220. This device may employ a grid with nozzles in a known manner to obtain substantially uniform gas bubble streams. Gas injected into the lower part of the catalyst bed rises through the descending column of liquid and creates a froth or foam. This froth can have a bulk density of between 20% and 80% of the density of the liquid feed (at reaction conditions), and normally consists essentially of a continuous liquid phase with gas bubbles dispersed therein. Above the catalyst bed 212, the rising gas becomes disengaged from the two phase froth in zone 222. Interface level controller 230 senses the density by measuring differential pressure of the fluids between its pressure taps and regulates the flow of liquid from valve 234 at the bottom of the reactor and/or reactant gas inlet valve 238 to maintain the froth-to-gas interface at the desired level H above the top of the catalyst bed.
~L2~3~ii9~
It should be understood that a sharp interface may not exist, but rather a vertical gradient in bulk density can prevail in the disengagement zone. This gradient in density can be used to regulate flow of liquid from the bottom of the reactor. The froth level detector may employ any oF several techniques for locating the interface within the disengagement zone. While differential pressure taps disposed at upper and lower points on the reactor shell adjacent the disengagement zone are suitable, other detectors, such as radiation gauges and the like, may be employed.
Catalyst particles should be of a size, e.g., 6mm (l/4") that they will not easily be dislodged by the rising gas bubbles.
Catalyst holddown screens across the top and perhaps at intermediate points in the reactor bed may be helpful in minimizing catalyst motion. Multiple catalyst beds with redistributors between beds may be useful in some applications. Likewise a mechanical device for creating and maintaining the desired froth bulk density may be usefulv Devices, such as rotating disc contactors, may be adapted for this purpose.
The present technique is adaptable to a variety of interphase catalytic reactions, particularly for treatment oF heavy oils with hydrogen-containing gas at elevated temperature.
Industrial processes employing hydrogen, especially petroleum refining, employ recycled impure gas containing lO to 50 mole % or more of impurities, usually light hydrocarbons and nitrogen. Such reactant gases are available and useful herein, especially for high temperature hydrogenation or hydrogenolysis at superatmospheric pressure.
In the refining of lubricants derived from petroleum by fractionation oF crude, a series of catalytic reactions are employed to severely hydrotreat, convert and remove sulfur and nitrogen contaminants, hydrocracking and isomerizing components of the lubricant charge stock in one or more catalytic reactors. This can be followed by hydrodewaxing and/or hydrogenation (mild hydrotreating) in contact with different catalysts under varying ~%~ 9i7 reacton conditions. An integrated three-step lube refining process disclosed by Garwood et al, in U.S. Patent No. 4,283,271 is adaptable to countercurrent processing according to the present invention. This modification is depicted schematically in Figure 4, wherein a waxy lubricant oil petroleum fraction is introduced to stage I (severe hydrotreating, cracking, etc.) countercurrently with a gas stream containing hydrogen reactant Product gas from the first stage may contain converted sulfur and/or nitrogen which can be removed by a sorber prior to introduction to the bottom of the Stage II hydrodewaxing reactor for countercurrent contact with liquid from the bottom of Stage I. Following dewaxing, the gas and liquid streams are then combined for cocurrent downflow through the mild hydrotreating reactor in Stage III~ Treated lube oil liquid product is recovered from a phase separator. Spent hydrogen may be -15 recovered as off gas or purified for recycle in a known manner.
The advantages of the present invention include: (l) longer liquid residence time in contact with the catalyst than with a typical cocurrent downflow reactor or in an entrained up-flow reactor; (2) countercurrent flow pattern will lessen the need for large volumes of gas and alleviate flow maldistribution characteristic of prior art mixed phase cocurrent tlow; (3) upward flowing gas bubbles serve to agitate the downward moving froth and thus facilitate intimate contact between the gas, liquid, and solid (catalyst) phases.
This invention relates to catalytic reactor operation wherein a liquid phase is treated with a gaseous reactant. In particular it relates to a technique for contacting multi-phase reactants in a fixed porous catalyst bed under continuous countercurrent conditions, including methods and apparatus for controlling frothing in the reactor.
Chemical reactions between liquid and gaseous reactants present difficulties in obtaining intimate contact between phases.
Such reactions are further complicated when the desired reaction is catalytic, and requires contact of both fluid phases with a solid catalyst. Numerous multi-phase reactor systems have been developed wherein a fixed porous bed of solid catalyst is retained in a reactor. Typically, fixed bed reactors have been arranged with the diverse phases being passed cocurrently over the catalyst, for instance as shown in U.S. Patents No. 4,126,539 (Derr et al), 4,235,847 (Scott), 4,283,271 (Garwood et al), and 4,396, 538 (Chen et al). In the petroleum refining industry, multi-phase catalytic reactor systems have been employed for dewaxing, hydrogenation, desulfurizing, hydrocracking, isomerization and other treatments of liquid feedstocks, especially distillates, lubricants, heavy oil fractions, residuum, etc,. Other known techniques for contacting liquid-gas mixtures with solid catalysts include slurry catalyst, ebullated bed and countercurrent systems, such as disclosed in U. S.
Patents 2,717,202, 3,186,935, 4,221,653, and 4,269,805. While prior ~2435~7 reactor systems are satisfactory for certain needs, efficient multi-phase contact has been difficult to achieve for many fixed bed applications.
It would be beneficial to have a multi-phase reactor operating under controlled flow conditions to maintain a gas-liquid froth, which could minimize flow maldistribution patterns and provide optimum volumetric proportions of upwardly moving gas dispersed in a downwardly gravitating liquid phase.
Accordingly, the present invention provides a countercurrent continuous catalytic reactor for treating a liquid phase with a gaseous reactant characterized by an enclosed reactor shell containing a fixed porous bed of solid catalyst, an upper liquid inlet for introducing a stream of liquid substantially above the catalyst bed for downward gravity flow of liquid through the bed, a lower liquid outlet for withdrawing treated liquid from the reactor shell, a gas inlet disposed below the catalyst bed for introducing a gaseous reactant stream under pressure for countercurrently contacting downwardly flowing liquid in a mixed phase reaction zone, whereby gaseous reactant is dispersed through the liquid phase in intimate contact with the solid catalyst, an upper gas outlet for withdrawing gas from the reactor shell above the catalyst bed, a level detector disposed in a froth zone above the catalyst bed for detecting level of a mixed gas-liquid froth and generating a signal representative of froth level, and a fluid handling control operatively connected to the level detector and responsive to the level signal to control fluid stream flow for regulating froth level above the catalyst bed thereby permitting disengagement of dispersed gas from the liquid phase of the froth and preventing excessive liquid entrainment in the gas outlet.
In another embodiment, the present invention provides a process for catalytic hydrocracking dewaxirg or desulfurizing of heavy petroleum feedstock in a multi-phase catalytic reactor containing a fixed porous bed of solid particles characterized by using the above-described reactor.
3~
Figure l is a simplified process diagram showing a vertical reactor with fixed catalyst bed, major flow streams, and control elements;
Figure 2 is a segmented vertical cross-section view of a reactor showing stripping and distributor sections;
Figure is a countercurrent catalyst bed, according to the present invention, shown in segmented vertical cross section aligned with the optional top section of Figure 2; and Figure 4 is a process diagram for an integrated heavy oil lo repining process.
Cnuntercurrent processes for contacting reactant fluids have several advantages. In a single point gas entry system, as the reactant gas rises upwardly from its point of introduction at the bottom of a vertical reactor below the porous bed, it contacts a lower concentration of reactive liquid components. At the point of entry the reactant gas has its greatest concentration. Depletion of the gaseous reactant upwardly will increase the relative concentration of inerts and/or byproduct vapors. Likewise, the liquid being treated is generally more reactive at the upper end of the reactor system where it contacts the depleted rising gaseous phase. Thus, the reactant concentration gradients for countercurrent two-phase systems are opposing. In a typical multi-phase reactor system, the average gas-liquid volume ratio in the catalyst zone is about i to 4:1 under process conditions.
In those reactions wherein the volume of gas decreases due to reactant depletion, the volumetric ratio or liquid to gas can increase markedly as the liquid feedstock gravitates downwardly through the reactor. In reactions which consume large amounts of hydrogen it may be desirable to have multiple reaction gas feed grids at various levels in the catalyst bed. In general, the quantity of unreacted gas at any particular level should be adequate to provide a mixed phase bulk density of at least 20% of the bulk density of the liquid phase (at reaction conditions). Vapor production, adiabatic heating or expansion can also affect the volume.
~35~
Advantageously, the multi-phase reactor system is operated to achieve uniform distribution. If too little liquid flux is maintained, the catalyst surface in the porous bed will be coated with a liquid film; however, this trickle mode will permit excessive channeling of the gas phase instead of the desired dispersion characteristics of a reactant froth. Flow rates for both reactant phases are controlled within constraints. Froth formation and disengagement is a function of the liquid viscosity, surface tension and composition. By detecting and controlling froth level, the lo proper operation of the reactor can be assured.
In order to maintain a desirable uniform flow of reactant streams through the fixed catalyst bed, adequate flow paths for liquid and gaseous phases must be provided. In a continuous process the ratio of reactant gas to liquid feedstock and the space velocity of reactants relative to catalyst must be carefully considered.
Achievement of uniform vertical flow through a porous bed of solids can be obtained if the catalyst is properly distributed and shaped.
The void volume in a reaction zone is a function of catalyst configuration and loading technique. While a densely packed bed of spherical solids may be employed to place a maximum amount of catalyst in a predetermined reactor volume, the low void fraction may interfere with fluid flow, especially where countercurrent flow of two phases is required. Advantageously, the catalyst bed has a high void volume, typically greater than one half of the bed. Void fractions from 0.5 to 0.9 can be achieved using loosely packed polylobal or cylindrical extrudates. Hollow ring-type supported catalysts, such as Raschig rings or the like, permit liquids to flow downwardly through the porous bed by gravity while the gas phase reactant rises through the denser liquid, forming dispersed bubbles which contact the wetted catalyst to enhance mass transfer and catalytic phenomena.
Catalyst size can vary widely within the inventive concept, depending upon process conditions and reactor structure. If a low space velocity or long residence in the catalytic reacton zone is ~.2~3~
.
permissible, small catalysts having an average maximum dimension of l to 5 mm may be employed. However, it is preferred to use larger sizes, e.g., 0.5-2 cm or more, especially when extrudates, rings, saddles or other contact materials are desired. Relatively small catalyst particles may be loaded randomly to assure uniformity and larger supported catalysts may be stacked in a geometric pattern to achieve optîmum bed utilization.
Reactor conFiguration is an important consideration in the design of a continuously operating system. In its simplest form, a lo vertical cylindrical pressure vessel is provided with a catalyst retaining device and operatively connected for countercurrent fluid flow. A typical vertical reactor having a catalyst bed length to effective diameter (L:D) ratio of about l:l to 20:1 is preferred. A
single bed or a stacked series of beds may be retained within the same reactor shell. While a reactor of uniform horizontal cross section is disclosed herein, other non-uniform configurations, such as spherical reactors9 tapered vessels, etc., may be employed.
Referring to Figure l, a countercurrent continuous catalytic reactor system is shown for treating a liquid phase with a gaseous reactant. An enclosed reactor shell lO contains a fixed porous bed 12 of solid catalyst. Upper liquid inlet 14 is provided for introducing a stream of liquid substantially above the catalyst bed for downward gravity flow through the bed toward lower liquid outlet 16 for withdrawing treated liquid from the reactor shell.
Gas inlet 20 is disposed below the catalyst bed for introducing a gaseous reactant stream under pressure for countercurrently contacting downwardly flowing liquid in a mixed phase reaction zone, whereby gaseous reactant is dispersed through the liquid phase in intimate contact with the solid catalyst. After passing through a reactant disengagement zone 22 above the catalyst bed 12 through upper gas outlet 24, gas is withdrawn From the reactor shell lO.
Level detector 30 is disposed in a froth zone between interface levels Hl and H2 above the catalyst bed for detecting the level of a mixed gas-liquid froth and generating a signal ~LX~5~3~
representative of the froth level. Fluid handling control is provided by control module ~27 responsive to the level signal to control fluid stream flow for regulating froth level above the catalyst bed, thereby permitting disengagement of dispersed gas from the liquid phase of the froth and preventing excessive liquid entrainment in the gas outlet. The fluid handling control may include liquid outlet valve 34 for withdrawing treated liquid at increased rate with increased froth level. Liquid and gas reactant feed rates may be controlled proportionally or as otherwise predetermined by setting control module 32 to operate liquid feed valve 36 and/or gas feed valve 38. Inlet flow control may be employed to vary the interface or froth level, as well as reactant proportions.
A more detailed depiction of a catalytic reactor system, lS for use with the present invention is shown in Figs. 2 and 3, both of which are segments of a vertical reactor. Fig. 2 is a top segment of a reactor 110 having upper liquid feed inlet 114 for introducing the charged feed to an optional stripping section 120.
In a typical application, such as lube oil dewaxing or mild desulfurization, the preheated liquid feed is introduced into the upper part oF a stripping section, where the feed is stripped of volatile components, dissolved and entrained contaminants by countercurrent stripping with the product gas stream rising from the catalyst bed. The gas stream is removed from the reactor through top gas outlet 125, which may have a back pressure regulator 130 responsive to pressure of the enclosed reactor. Additional stripping gas may be introduced via inlet 118 into the lower part of the stripping section, if desired. The quantity of stripping gas should be sufficient to saturate the entering liquid feed with the gas plus enough additional gas to achieve the desired removal of contaminants such as entrained water, H2S, water vapor, and the like. The temperature and pressure in the stripping zone approximate the conditions desired in the catalyst bed. It is understood that the feed stripping feature may not be required in all instances.
9~7 The liquid feed flowing down from the stripper (or directly from the feed source if a stripper is not employed) passes to a horizontal distributor tray 130 which spreads the liquid across the catalyst bed. The distributor tray is provided with gas risers 132 to allow rising gas to pass through the tray and proceed upwardly.
A typical distributor tray has a spaced array of perforations or orifices 135 sized to allow even liquid stream flow from the upper surface of the horizontal tray 130 into the disengagement zone below, further depicted in Fig. 3.
ReFerring to Fix. 3, the bottom segment of a typical vertical reactor shell 210 is shown in broken vertical cross section view. A bed of catalyst particles 212 is maintained within the main central portion of reactor 210 by a catalyst support grid 214, having retainer 215 to prevent loss of particles from the bed. A
plurality of liquid collector pipes 217 recover treated liquid via plenum chamber 218, outlet conduit 216 and liquid control valve 234. Flow equalizing restrictions may be ernployed with the collector pipes to assure even withdrawal. Reaction gas is injected into the lower part of the catalyst bed through a gas sparger-type inlet 220. This device may employ a grid with nozzles in a known manner to obtain substantially uniform gas bubble streams. Gas injected into the lower part of the catalyst bed rises through the descending column of liquid and creates a froth or foam. This froth can have a bulk density of between 20% and 80% of the density of the liquid feed (at reaction conditions), and normally consists essentially of a continuous liquid phase with gas bubbles dispersed therein. Above the catalyst bed 212, the rising gas becomes disengaged from the two phase froth in zone 222. Interface level controller 230 senses the density by measuring differential pressure of the fluids between its pressure taps and regulates the flow of liquid from valve 234 at the bottom of the reactor and/or reactant gas inlet valve 238 to maintain the froth-to-gas interface at the desired level H above the top of the catalyst bed.
~L2~3~ii9~
It should be understood that a sharp interface may not exist, but rather a vertical gradient in bulk density can prevail in the disengagement zone. This gradient in density can be used to regulate flow of liquid from the bottom of the reactor. The froth level detector may employ any oF several techniques for locating the interface within the disengagement zone. While differential pressure taps disposed at upper and lower points on the reactor shell adjacent the disengagement zone are suitable, other detectors, such as radiation gauges and the like, may be employed.
Catalyst particles should be of a size, e.g., 6mm (l/4") that they will not easily be dislodged by the rising gas bubbles.
Catalyst holddown screens across the top and perhaps at intermediate points in the reactor bed may be helpful in minimizing catalyst motion. Multiple catalyst beds with redistributors between beds may be useful in some applications. Likewise a mechanical device for creating and maintaining the desired froth bulk density may be usefulv Devices, such as rotating disc contactors, may be adapted for this purpose.
The present technique is adaptable to a variety of interphase catalytic reactions, particularly for treatment oF heavy oils with hydrogen-containing gas at elevated temperature.
Industrial processes employing hydrogen, especially petroleum refining, employ recycled impure gas containing lO to 50 mole % or more of impurities, usually light hydrocarbons and nitrogen. Such reactant gases are available and useful herein, especially for high temperature hydrogenation or hydrogenolysis at superatmospheric pressure.
In the refining of lubricants derived from petroleum by fractionation oF crude, a series of catalytic reactions are employed to severely hydrotreat, convert and remove sulfur and nitrogen contaminants, hydrocracking and isomerizing components of the lubricant charge stock in one or more catalytic reactors. This can be followed by hydrodewaxing and/or hydrogenation (mild hydrotreating) in contact with different catalysts under varying ~%~ 9i7 reacton conditions. An integrated three-step lube refining process disclosed by Garwood et al, in U.S. Patent No. 4,283,271 is adaptable to countercurrent processing according to the present invention. This modification is depicted schematically in Figure 4, wherein a waxy lubricant oil petroleum fraction is introduced to stage I (severe hydrotreating, cracking, etc.) countercurrently with a gas stream containing hydrogen reactant Product gas from the first stage may contain converted sulfur and/or nitrogen which can be removed by a sorber prior to introduction to the bottom of the Stage II hydrodewaxing reactor for countercurrent contact with liquid from the bottom of Stage I. Following dewaxing, the gas and liquid streams are then combined for cocurrent downflow through the mild hydrotreating reactor in Stage III~ Treated lube oil liquid product is recovered from a phase separator. Spent hydrogen may be -15 recovered as off gas or purified for recycle in a known manner.
The advantages of the present invention include: (l) longer liquid residence time in contact with the catalyst than with a typical cocurrent downflow reactor or in an entrained up-flow reactor; (2) countercurrent flow pattern will lessen the need for large volumes of gas and alleviate flow maldistribution characteristic of prior art mixed phase cocurrent tlow; (3) upward flowing gas bubbles serve to agitate the downward moving froth and thus facilitate intimate contact between the gas, liquid, and solid (catalyst) phases.
Claims (10)
1. A countercurrent continuous catalytic reactor for treating a liquid phase with a gaseous reactant characterized by:
an enclosed reactor shell containing a fixed porous bed of solid catalyst;
an upper liquid inlet for introducing a stream of liquid substantially above the catalyst bed for downward gravity flow of liquid through the bed;
a lower liquid outlet for withdrawing treated liquid from the reactor shell;
a gas inlet disposed below the catalyst bed for introducing a gaseous reactant stream under pressure for countercurrently contacting downwardly flowing liquid in a mixed phase reaction zone, whereby gaseous reactant is dispersed through the liquid phase in intimate contact with the solid catalyst;
an upper gas outlet fox withdrawing gas from the reactor shell above the catalyst bed;
a level detector disposed in a froth zone above the catalyst bed for detecting level of a mixed gas-liquid froth and generating a signal representative of froth level; and a fluid handling control operatively connected to the level detector responsive to the level signal to control fluid stream flow for regulating froth level above the catalyst bed, thereby permitting disengagement of dispersed gas from the liquid phase of the froth and preventing excessive liquid entrainment in the gas outlet.
an enclosed reactor shell containing a fixed porous bed of solid catalyst;
an upper liquid inlet for introducing a stream of liquid substantially above the catalyst bed for downward gravity flow of liquid through the bed;
a lower liquid outlet for withdrawing treated liquid from the reactor shell;
a gas inlet disposed below the catalyst bed for introducing a gaseous reactant stream under pressure for countercurrently contacting downwardly flowing liquid in a mixed phase reaction zone, whereby gaseous reactant is dispersed through the liquid phase in intimate contact with the solid catalyst;
an upper gas outlet fox withdrawing gas from the reactor shell above the catalyst bed;
a level detector disposed in a froth zone above the catalyst bed for detecting level of a mixed gas-liquid froth and generating a signal representative of froth level; and a fluid handling control operatively connected to the level detector responsive to the level signal to control fluid stream flow for regulating froth level above the catalyst bed, thereby permitting disengagement of dispersed gas from the liquid phase of the froth and preventing excessive liquid entrainment in the gas outlet.
2. The reactor of claim 1 wherein the fluid handling control includes a liquid outlet valve disposed in the lower liquid outlet for withdrawing treated liquid at increased rate with increased froth level.
3. The reactor of claim 2 wherein the reactor shell comprises a vertical cylindrical pressure vessel containing catalyst.
4. The reactor of claim 1, 2 or 3 wherein the catalyst solids have an average size greater than about 0.5 cm and a void fraction greater than about 0.5.
5. The reactor of claim 1, 2 or 3 wherein the reactor shell has a top stripping section for contacting liquid feed with exiting gas.
6. The reactor of claim 1 wherein a distributor is disposed in an upper portion of the reactor shell above the froth zone for uniformly applying liquid across the reactor cross-section.
7. The reactor of claim 6 wherein the distributor comprises a horizontal distributor plate having a plurality of liquid orifices disposed therein at uniformly spaced points and risers for permitting disengaged gas to exit from the lower reactor section.
8. The reactor of claim 1, 2 or 3 wherein the level detector measures differential pressure to detect froth level between predetermined vertical points in the froth zone.
9. A process for catalytic hydrocracking, dewaxing or desulfurizing of heavy petroleum feedstock in a multi-phase catalytic reactor containing a fixed porous bed of solid catalyst particles characterized by using the reactor of claim 1.
10. The process of claim 9 wherein the feedstock is waxy oil and the catalyst comprises ZSM-5 zeolite.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000491887A CA1243597A (en) | 1985-09-30 | 1985-09-30 | Multi-phase countercurrent reactor process and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000491887A CA1243597A (en) | 1985-09-30 | 1985-09-30 | Multi-phase countercurrent reactor process and apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1243597A true CA1243597A (en) | 1988-10-25 |
Family
ID=4131498
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000491887A Expired CA1243597A (en) | 1985-09-30 | 1985-09-30 | Multi-phase countercurrent reactor process and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1243597A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113735250A (en) * | 2021-09-03 | 2021-12-03 | 泸州市兴泸环保发展有限公司 | Foam liquid level monitoring device for aerobic reaction tank |
| CN114849595A (en) * | 2021-02-04 | 2022-08-05 | 北京化工大学 | Hypergravity heterogeneous catalytic reactor device and application thereof |
-
1985
- 1985-09-30 CA CA000491887A patent/CA1243597A/en not_active Expired
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114849595A (en) * | 2021-02-04 | 2022-08-05 | 北京化工大学 | Hypergravity heterogeneous catalytic reactor device and application thereof |
| CN114849595B (en) * | 2021-02-04 | 2024-02-02 | 北京化工大学 | Supergravity heterogeneous catalytic reactor device and application thereof |
| CN113735250A (en) * | 2021-09-03 | 2021-12-03 | 泸州市兴泸环保发展有限公司 | Foam liquid level monitoring device for aerobic reaction tank |
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