Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
  • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
  • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
• • 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
  • B01J8/38—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
  • B01J8/384—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
  • B01J8/388—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
• • 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
• • 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
  • B01J8/1818—Feeding of the fluidising gas
• • 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
  • B01J8/1818—Feeding of the fluidising gas
  • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
• • 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
  • B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
  • B01J8/1863—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement outside the reactor and subsequently re-entering it
• • 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
• • 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
  • B01J8/38—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it

Definitions

• the invention generally relates to the Fluid Catalytic Cracking (FCC) process and more particularly to an apparatus and method for processing feed streams having very different compositions or boiling ranges in the same FCC unit.
• FCC Fluid Catalytic Cracking
• feed streams that have very different properties or boiling point ranges in the same FCC unit.
• These streams can be straight run or cracked materials from other conversion units, or recycled materials from the same FCC unit.
• One of the streams is generally the main feed while others are supplemental feeds intended to maximize production of a certain product from the FCC unit.
• the various feed streams may require very different cracking conditions due to very different molecular size/structure.
• a number of modifications to the conventional FCC process have been developed in which these streams are fed at different locations in the riser reactor.
• the lower boiling or lower molecular weight materials require more severe conditions to crack, while higher boiling materials require less severe conditions. Materials rich in aromatics are difficult to crack and form increased quantities of coke, which reduces the effectiveness of the catalyst.
• U.S. Patent No. 4,051,013, issued September 27, 1977 is directed to a fluid catalytic cracking process for simultaneously cracking a gas oil feed and upgrading a gasoline-range feed to produce high quality motor fuel.
• the lower boiling gasoline-range feed is contacted with freshly regenerated catalyst in a portion of the riser reaction zone that is relatively upstream from the portion of the riser reaction zone in which the higher boiling gas oil feed is injected.
• the lighter gasoline feed is injected at a single point that does not provide uniform and thorough contact of the catalyst and the feed.
• U.S. Patent No. 4,892,643, issued January 9, 1990 discloses a catalytic cracking operation using a single riser reactor in which two different types of cracking catalysts are employed. In this process, heavy hydrocarbon feed is introduced to the riser reactor upstream from the lighter feed. Cracking of the heavy feed produces a significant quantity of naphtha, which is then combined with a downstream naphtha feed.
• U.S. Patent No. 5,846,403, issued December 8, 1998 discloses a method of improving the yield of light olefins in a FCC process while simultaneously increasing the octane rating of gasoline produced in the process.
• a light catalytic naphtha feed and steam are injected upstream of the conventional FCC feed injection point.
• the lighter feed is injected at a single point of injection.
• This method does not provide uniform and thorough contact between the catalyst and the light feed, and, as a result, conversion and yield of the desired products are not maximized.
• the heavier feed is mixed with conventional FCC feed, i.e. gas oil, and is injected in the riser through the same feed injectors as the main feed. This design does not provide optimum conditions for heavier feed to vaporize and undergo the desirable catalytic cracking reactions.
• the invention optimizes the precise location, and the method and apparatus for injection of different feeds in a single riser reactor of a FCC unit.
• An object of the invention is to provide a method for improving the yield of C3 and C 4 , and optionally also gasoline range hydrocarbons in a FCC process.
• Another object of the invention is to provide an apparatus that can be used for efficiently processing hydrocarbon streams of various feed types to obtain higher yields of C3 and C 4 hydrocarbons.
• the feeds can all be from an external source, or can be a combination of external feeds and recycle streams from the same FCC unit.
• a further object of the invention is to provide a method for improving the conversion rate in a fluid catalytic cracking process and hence improving the yield of gasoline range material.
• Another object of the invention is to recycle a heavier fraction of the product stream from a FCC unit back to the riser to increase conversion and/or to return solid catalyst particles back to the reaction system.
• Another object of the invention is to recycle a relatively lighter fraction of the product stream from the FCC unit back to the riser to increase the yield of C 3 and C 4 olefins.
• Yet another object of the invention is to provide a method of reducing the formation of coke and other low value products, e.g. compounds with two or fewer carbon atoms, in a FCC process.
• the invention in a preferred form is a fluid catalytic cracking process for increasing yields of C3 and C4 hydrocarbons, comprising the steps of injecting a main feed comprising hydrocarbons with boiling points in the range of 40O 0 F to 1150 0 F (when measured at atmospheric pressure) into a riser reactor of a FCC apparatus through a set of main feed injectors, and injecting a light feed comprising hydrocarbons with boiling points which are no more than about 440 0 F (when measured at atmospheric pressure) into the fluid catalytic cracking apparatus through a plurality of light feed injectors disposed upstream from the main feed injectors proximate locations at which the catalyst flow changes direction.
• a set of injectors for light feed are positioned upstream of the injectors for main feed in such a way as to follow the contour I of the catalyst flow so that the contact of the lighter feed with the catalyst is maximized.
• the light feed is injected into a conduit portion of the riser reactor.
• the conduit usually develops a lower catalyst density region and a higher catalyst density region.
• the light feed is injected through multiple injectors, which are positioned such that a larger portion of the light feed is injected into the higher catalyst density region than the lower catalyst density region.
• the process preferably further comprises the step of injecting a heavy feed comprising hydrocarbons with boiling points in the range of 57O 0 F to 1275 0 F (when measured at atmospheric pressure) through a set of injectors for heavy feed.
• injectors are usually located approximately at the same elevation on the riser reactor as the main feed injectors.
• the heavier or difficult to vaporize/crack feed is separately injected through a separate set of feed injectors that may be specially designed to take into account the unique properties of this material, e.g. the presence of some solid particles.
• the heavier/difficult to crack feed is generally recycle of the heavy fraction of the products from the FCC unit.
• the mass flow rate of the heavy feed through the heavy feed injectors is about 1-10 wt % of the mass flow rate of the main feed through the main feed injectors, preferably 3-7 wt % and more preferably about 5 wt %. In one embodiment, about 1 to 10 wt % of the main feed is recycled and injected as heavy feed through the heavy feed injectors.
• the light feed usually is injected downstream from a control valve, which is positioned between the catalyst regenerator and the conduit portion of the riser reactor.
• the control valve preferably is a regenerated catalyst slide valve.
• the yield of C 3 and C4 hydrocarbons from the process of the invention typically is at least 2% higher than the yield of C 3 and C 4 hydrocarbons in a process that is substantially identical with the exception that the light feed is injected at a single location upstream from the main feed.
• the yield of propylene usually is at least 2% higher than the yield of propylene in a process in which the light feed is injected at one location upstream from the main feed, but otherwise seems identical.
• the yield of C 4 olefins preferably is at least 1% higher than the yield of olefins in a process in which the light feed is injected at one location upstream from the main feed.
• the catalyst used is typically of the range of catalysts usually employed in a FCC process and preferably is a zeolite.
• Another preferred form of the invention is a fluid catalytic cracking process for increasing yields of C3, C 4 and gasoline range hydrocarbons, comprising injecting a main feed comprising hydrocarbons with boiling points in the range of 40O 0 F to 115O 0 F (when measured at atmospheric pressure) into a riser reactor of a fluid catalytic cracking apparatus through a set of main feed injectors, and injecting a heavy feed comprising hydrocarbons with boiling points in the range of 570 0 F to 1275°F (when measured at atmospheric pressure) through a set of heavy feed injectors positioned at approximately the same elevation on the riser reactor as the set of main feed injectors.
• the process further comprises the step of injecting a light feed comprising hydrocarbons with boiling points of no more than about 44O 0 F into the fluid catalytic cracking apparatus through multiple injectors positioned upstream from the main feed injectors.
• the light feed usually is injected into a conduit portion of the riser reactor.
• a further preferred form of the invention is a fluid catalytic cracking apparatus comprising a catalyst regenerator and a riser reactor having a set of main hydrocarbon feed injectors connected thereto.
• the riser reactor includes a conduit portion fluidiy connected to the catalyst regenerator for receiving regenerated catalyst.
• the conduit portion includes an angled section located upstream from the set of main hydrocarbon feed injectors.
• the angled section has a plurality of light hydrocarbon feed injectors formed thereon.
• the angled section is configured to change the direction of catalyst flow.
• the injectors are configured to inject light hydrocarbon feed generally in the same direction in as the flow of the catalyst.
• the injectors for light feed can be positioned to inject the feed in a direction which is countercurrent to the direction of the catalyst flow.
• the invention is a fluid catalytic cracking apparatus comprising a catalyst regenerator and a riser reactor having a set of main hydrocarbon feed injectors connected thereto.
• the riser reactor includes a conduit portion fluidiy connected to the catalyst regenerator for receiving regenerated catalyst.
• a set of heavy hydrocarbon feed injectors is positioned at approximately the same elevation on the riser reactor as the set of main hydrocarbon feed injectors.
• the heavy feed injectors can be set up in a way as to inject the feed countercurrent to the direction of the catalyst flow.
• the fluid catalytic cracking apparatus preferably further comprises a plurality of light hydrocarbon feed injectors positioned upstream from the main hydrocarbon feed injectors.
• Figure 1 is a side elevational view of a portion of a fluid catalytic cracking unit including the connection between the riser reactor and the regenerated catalyst standpipe;
• Figure 2 is a sectional view taken along line 2-2 of Figure 1;
• Figure 3 is a sectional view taken along line 3-3 of Figure 1;
• Figure 4 is a sectional view taken along line 4-4 of Figure 1;
• Figure 5 is a side elevational view of a second embodiment of a portion of a fluid catalytic cracking unit including the connection between the riser reactor and the regenerated catalyst standpipe;
• Figure 6 is a lower end view of the embodiment shown in Fig. 5;
• Figure 7 is a side elevational view of a third embodiment of a portion of a fluid catalytic cracking unit including the connection between the riser reactor and the regenerated catalyst standpipe;
• Figure 8 is a sectional view taken along line 8-8 of Figure 7.
• various feed streams are injected at appropriate points in the conduit portion of the riser reactor such that the process conditions available at those points match the cracking requirements for the injected streams.
• Inlet streams are fed in such a way that there is uniform and thorough mixing of the feed streams with the catalyst at each point of injection so that conversion of these materials is maximized.
• the heavier feed stream which may be a recycle stream
• the lighter feed which also can be recycled product from the FCC unit, is injected upstream of the main injection point where cracking severity is very high in order that cracking of the lower molecular weight hydrocarbon compounds is maximized.
• the technique for injecting the light feed upstream from the main feed injectors takes into consideration the catalyst flow pattern around the injection points.
• the catalyst flow undergoes a change of direction as it flows from the regenerated catalyst standpipe to the riser. As the catalyst changes direction, its flow is not uniform across the cross section of the conduit. Thus, the way the lighter feed is injected is important.
• the lighter feed is injected at number of points downstream of the regenerated catalyst slide valve, keeping in view the catalyst flow pattern.
• the feed is injected in a distributed way and not at one location such that the areas with greater concentration of the catalyst particles get a greater amount of feed. In other words, the dispersed feed injection follows the density contour of the catalyst in the conduit. This uniform injection of the feed with respect to the catalyst maximizes catalyst effectiveness due to increased contact of the feed with the catalyst. If the feed is injected at one location as is done in the conventional process, the catalyst effectiveness is reduced as the feed contacts only a smaller number of catalyst particles.
• the heavy feed does not vaporize properly due to a lower temperature at that point.
• the unvaporized liquid feed can result in coke deposits on the equipment downstream.
• some of the unvaporized and unconverted feed ends up in the regenerator where it can burn and increase the catalyst temperature, adversely affecting the performance of the FCC unit.
• the conversion and the yield of lighter products will be reduced due to a reduced catalyst circulation rate as a result of the increased regenerator temperature. If the heavy feed is injected upstream from the main feed injection point, a larger amount of coke is formed on the regenerated catalyst before it meets the main feed. This reduces the catalyst activity and hence the conversion of the main feed and the yield of valuable products.
• This portion 10 includes a riser reactor 12 and a regenerated catalyst standpipe 14.
• the lower portion of the riser reactor 12 is a Y-shaped conduit 16 which connects the regenerated catalyst standpipe 14 to the main section 15 of the riser reactor 12, which is above the main feed injectors.
• the riser reactor 12, including the conduit 16, is filled with catalyst.
• the catalyst density profile is such that the vertex portion 36 of the conduit 16 is a high catalyst density region 38, and the vertical portion 40 of the conduit downstream from the vertex portion 36 includes a low catalyst density region 42.
• Catalyst 13 flows from the regenerator (not shown) to the regenerated catalyst standpipe 14, through the regenerated catalyst slide valve 17, into the conduit 16, and up into the main section 15 of the riser reactor 12.
• the flow rate of the regenerated catalyst into the riser reactor 12 is controlled by the regenerated catalyst slide valve 17.
• the catalyst moves from the downwardly slanted portion 32 of the conduit 16 to the vertex portion 36 and vertically upward, its density within the cross section of the vertical portion 40 of the conduit 16 is not uniform. This is because of the momentum with which the catalyst is flowing down and the force it exerts on the far wall while changing direction in order to move vertically upward.
• the light feed is injected at various points along the vertex portion 36 of the conduit to take advantage of the high catalyst concentration in this high density area.
• the catalyst flow becomes uniform as it moves up the vertical portion of the conduit 16.
• a plurality of main feed injectors 18 are connected to the riser reactor 12 at the downstream end of the conduit 16, where the catalyst flow is usually uniform.
• the injectors 18 are slanted upwardly to direct the main feed generally in the direction of catalyst flow.
• these injectors could be slanted downwardly.
• a plurality of injectors 20 for heavier feed also can be disposed.
• the heavy feed injectors 20 also are slanted upwardly to direct the heavy feed generally in the direction of catalyst flow. However these could also be positioned to inject the feed downwardly.
• the heavier hydrocarbons are more difficult to vaporize or crack than the hydrocarbons in the main feed. It is advantageous for the heavy feed to be injected separately from the main feed instead of blending it with the main feed and feeding it through the same injectors.
• the inventors have found that by injecting the heavy feed separately, the larger/heavier molecules see or meet the high temperature catalyst particles separately and get vaporized quickly.
• the larger/heavier molecules see or meet the catalyst particles that have been quenched or cooled by the lighter/smaller molecules of the main feed. Thus, some heavier molecules may not vaporize. This leads to higher coke formation and deterioration of the FCC unit performance.
• the heavier feed may sometimes contain catalyst or solid particles, particularly if it constitutes a recycle of the heavier fraction from the FCC product slate.
• Such situations require special or different design of the injectors for the heavy feed. If the heavier feed with solids in it is mixed with the injectors designed for the main feed, the injectors will be eroded by the catalyst particles and the unit performance will deteriorate.
• the "main feed” has a boiling point in the range of 400 0 F to 1150 0 F if measured at atmospheric pressure, more preferably 430 0 F to 1100 0 F, and most preferably 460°F-1050°F.
• the "heavy feed” has a boiling point when measured at atmospheric pressure in the range of 570-1275 0 F typically 600 0 F to 125O 0 F, and more preferably 65O 0 F to 1250 0 F.
• the "light feed” has a lower boiling point than the main feed and typically has a boiling point when measured at atmospheric pressure of 44O 0 F or less, more preferably 43O 0 F or less and most preferably 400 0 F or less.
• FCC catalysts can be used in accordance with the invention, including but not limited to those with a crystalline tetrahedral framework oxide component.
• the catalyst is selected from the group consisting of catalysts based on zeolite crystalline structure. More preferably, the catalyst is based on an Ultra stable Y (USY) Zeolite with a high Silica to Alumina ratio.
• USY Ultra stable Y
• This FCC catalyst may be used either alone or in combination with a shape selective pentasil zeolite catalyst structure like ZSM-5 that converts larger linear hydrocarbon compounds, such as olefins, to smaller olefins.
• Light feed injectors 22 are positioned on the vertical wall of the vertex portion 36 of conduit 16 at or proximate locations at which catalyst flow changes direction. As indicated above, the catalyst density in the vertex portion 36 is the highest.
• the injectors 22 are shown in Fig. 1 as being slanted upwardly in the direction of catalyst flow through the riser but could be directed horizontally or downwardly.
• Injectors 24 are positioned at the bottom of the vertex portion 36 and inject light feed upwardly in a vertical direction.
• Light feed injectors 26 are disposed on the upstream end of the vertex portion 36 on the lower wall of the conduit 16 and are angled slightly downwardly relative to a horizontal direction. As a result of the multiple feed injector configuration provided by light feed injectors 22, 24 and 26, the light feed is distributed along the path of catalyst flow in such a manner that the region 38 of higher catalyst density in vertex portion 36 gets a higher flow of the feed than regions with lower catalyst density.
• One of the important advantages of providing separate feed injectors for the main, heavy and light feeds is that the apparatus and method of the present invention can be used for cracking feeds of various boiling ranges in a single FCC unit and achieve high performance by producing high value products.
• the conduit portion of the riser reactor can have any of a variety of different configurations. Several additional non-limiting examples are shown in Figures 5 to 8. Figures 5 and 6 show a conduit portion 116 with a first portion 130 extending vertically downward from a regenerated catalyst slide valve 117 which is below a regenerated catalyst standpipe 114, a second portion 132 slanted upwardly relative to the first portion 130, and a vertical third portion 134 which connects the upper end of the second portion 132 to the main part of the riser reactor.
• the lower end 136 of the second portion 132 is below the point of connection between the first portion 130 and the second portion 132 and has a plurality of light feed injectors 122 formed on the side wall 126, and a plurality of light feed injectors 124 formed on the lower end wall 128.
• Figures 7 and 8 depict a conduit 216 with a similar shape as conduit 116 in that a first portion 230 extends vertically downward from a regenerated slide valve and a second portion 232 is slanted upwardly from the first portion and is connected to the lower end of a vertically extending third portion 234, which is connected to the main part of the riser reactor.
• Multiple injectors 226 enter the conduit 216 at the vertex between the first portion 230 and the second portion 232.
• the principal basis of this invention remains the same, i.e. the lighter feed is injected upstream of the main feed injection point and in a dispersed way such that the higher catalyst density regions get a greater amount of this lighter feed, and the contact time of the lighter feed with the catalyst before this mixture meets the main feed injectors is optimized.
• the heavy feed is injected at approximately the same location as the main feed but through separate injectors.
• the invention typically results in an increase in conversion of the lighter hydrocarbon feed by at least 15% as compared to conventional methods of injection or processing of this feed. This conversion increase in turn results in an increase in yields of C 3 and C 4 hydrocarbons by at least 11%, and often as much as 18%.
• the injection of the heavier recycle stream as described in this invention results in a conversion increase of the main feed by about 2%. Gasoline plus C3 and C4 yield increases by at least 5% and often by 8% as compared to the conventional processes.
• main feed with a boiling range of 460 0 F to 1000 0 F is processed along with a lighter feed of a boiling range 145°F to 375°F in conventional manner.
• the riser reactor is operated at a temperature of 1015 0 F at its outlet and a pressure of 25 psig using USY catalyst without any addition or use of shape selective pentasil zeolite. This cracking process yields the product slate shown below in Table 1:
• Example 1 The remaining 5 wt % is coke that deposits on the catalyst and is burned off in the regenerator.
• Example 1 The remaining 5 wt % is coke that deposits on the catalyst and is burned off in the regenerator.
• Comparative Example 1 The process of Comparative Example 1 is repeated with the exception that the light feed is injected upstream of the main feed in the light feed injectors 22, 24 and 26 shown on Figure 1.
• the increase in yield of light components as compared to the process of Comparative Example 1 is summarized in Table 2.
• the increase in production of light components is due to the increase in conversion of the lighter feed.
• Comparative Example 1 The process of Comparative Example 1 is repeated with the exception that the heavier feed (the heaviest fraction of the product from the first pass conversion) that is recycled from the same FCC unit is injected through multiple injectors at the same height as the main feed, but through separate injectors. The conversion of the main feed is improved over the conversion rate of Comparative Example 1. Improvements in yield of C 3 , C 4 , and gasoline range hydrocarbons as compared to the process of Comparative Example 1 are shown in Table 3 below:

Landscapes

• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Combustion & Propulsion (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• General Chemical & Material Sciences (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Catalysts (AREA)

Priority Applications (9)

Applications Claiming Priority (2)

Publications (2)

Family

ID=36440962

Family Applications (1)

Country Status (15)

Cited By (1)

Families Citing this family (40)

Citations (7)

Family Cites Families (22)

• 2004
  • 2004-12-23 US US11/021,274 patent/US7682501B2/en active Active
• 2005
  • 2005-12-15 MY MYPI20055925A patent/MY148557A/en unknown
  • 2005-12-21 AR ARP050105436A patent/AR053106A1/es active IP Right Grant
  • 2005-12-22 JP JP2007548518A patent/JP5312796B2/ja not_active Expired - Lifetime
  • 2005-12-22 RU RU2007117646/04A patent/RU2391382C2/ru active
  • 2005-12-22 CA CA2587794A patent/CA2587794C/en not_active Expired - Lifetime
  • 2005-12-22 CN CN201410135789.1A patent/CN103897723B/zh not_active Expired - Lifetime
  • 2005-12-22 EP EP05855354A patent/EP1828346B1/en not_active Expired - Lifetime
  • 2005-12-22 DK DK05855354.6T patent/DK1828346T3/da active
  • 2005-12-22 BR BRPI0519353A patent/BRPI0519353B1/pt not_active IP Right Cessation
  • 2005-12-22 CN CN200580044843.0A patent/CN101087865B/zh not_active Expired - Lifetime
  • 2005-12-22 MX MX2007006541A patent/MX2007006541A/es active IP Right Grant
  • 2005-12-22 KR KR1020077013803A patent/KR101145196B1/ko not_active Expired - Lifetime
  • 2005-12-22 AU AU2005322126A patent/AU2005322126B2/en not_active Ceased
  • 2005-12-22 WO PCT/US2005/046778 patent/WO2006071771A1/en not_active Ceased
  • 2005-12-23 TW TW094146392A patent/TWI481702B/zh not_active IP Right Cessation
• 2010
  • 2010-03-08 US US12/719,325 patent/US8986617B2/en not_active Expired - Lifetime
• 2013
  • 2013-10-03 AR ARP130103589A patent/AR092894A2/es active IP Right Grant

Patent Citations (7)

Also Published As

Similar Documents

Legal Events