Patent Grant
8435401
1. The Field of the Invention
The present invention relates generally to fluidized catalytic crackers and methods for upgrading hydrocarbons using novel fluidized catalytic crackers. More particularly, the present invention relates to a staged fluidized catalytic cracker that has a plurality of reactors that are fed fluidized catalyst in series and where an active stripper is positioned between each reactor to strip the fluidized catalyst between reactors.
2. The Related Technology
Catalytic cracking is the backbone of many refineries. It converts heavy feeds into lighter products by catalytically cracking large molecules into the smaller molecules that are found in highly valued transportation fuels. Catalytic cracking operates at low pressures, without significant hydrogen addition, in contrast to hydrocracking, which operates at high hydrogen pressures.
The most widely used process for catalytic cracking is fluidized catalytic cracking. In fluidized catalytic cracking (FCC), a catalyst, having particle sizes between about 20-100 microns circulates between a cracking reactor and a catalyst regenerator. In the reactor, hydrocarbon feed contacts hot, regenerated catalyst. The hot catalyst vaporizes and cracks the feed at 800-1100° F. (425-600° C.), usually 860-1040° F. (460-560° C.). The cracking reaction deposits carbonaceous hydrocarbons, which eventually turn to coke on the catalyst, thereby deactivating it. The cracked products are separated from the coked catalyst, usually with the aid of a catalyst stripper, and the stripped catalyst is then regenerated within the regenerator. A catalyst regenerator burns coke from the catalyst with oxygen containing gas, usually air. Regeneration of the catalyst by oxidation restores catalyst activity and simultaneously heats the catalyst to, e.g., 930-1650° F. (500-900° C.), usually 1110-1380° F. (600-750° C.). This heated catalyst is recycled to the cracking reactor to crack more fresh feed. Flue gas formed by burning coke in the regenerator may be treated for removal of sulfur oxides, nitrogen oxides, and particulates and for oxidation of carbon monoxide, after which the flue gas is normally discharged into the atmosphere. Catalytic cracking is an endothermic reaction. The heat for cracking and vaporization of the feed is supplied at first by the hot regenerated catalyst from the regenerator. In actuality, it is a portion of the feed that becomes coke which, when oxidized, provides the heat needed to crack the feed.
Catalytic cracking has undergone much development since its introduction over fifty years ago. The trend of development of the FCC process has been to use riser cracking with zeolite catalysts. Zeolite based catalysts of high activity and selectivity are now used in most FCC units. These catalysts have allowed refiners to increase throughput and conversion, compared to operation with amorphous catalysts. Use of zeolite catalysts effectively debottlenecked the reactor section, especially when a riser reactor was used.
Today, regenerators operate at very high temperatures. Most FCC units are heat balanced; the endothermic heat of cracking is supplied by burning the coke deposited on the catalyst. With poorer feeds, more coke is deposited on the catalyst than is needed for the cracking reaction. The regenerator operates at higher temperatures and excess heat is emitted in the form of high temperature flue gas. Regenerator temperature now limits many refiners in the amount of residue or high carbon residue feeds which can be tolerated by the unit. Special coolers to moderate the heat produced in regerators have become more common as deeper cuts of petroleum are fed to catalytic crackers.
The present invention is directed to a staged fluidized catalytic cracker (FCC unit) and method for cracking a hydrocarbonaceous material. The FCC unit of the invention includes a plurality of staged reactors that have catalyst particles flowing in series from one reactor to the next and hydrocarbon feed that is delivered in parallel to the reactors. Between reactors, the catalyst is stripped using an active stripper. Surprisingly, active stripping of the catalyst between reactors has been found to have a profound impact on the activity of the catalyst in the second reactor and any subsequent reactors. Testing using active stripping in the staged FCC unit of the invention has shown that active stripping between reactors improves yields of the desired products and allows an operator to adjust process conditions to achieve desired conditions within the reactor.
In one embodiment of the invention, the FCC unit includes a first reactor, a second reactor, and optionally any number of additional reactors. Each reactor has one or more inlets for receiving a hydrocarbon feedstock and a cracking catalyst. Each reactor also has one or more outlets for discharging the cracking catalyst and the cracked hydrocarbons.
The FCC unit also includes a hydrocarbon stripping vessel in fluid communication with an outlet of the first reactor for receiving the catalyst after it is partially spent. In the stripping vessel, stripping gases are injected through the catalyst bed. The action of the stripping gas moving through the catalyst bed removes cracked hydrocarbons, which are discharged from the FCC unit with the stripping gas. This stripping action rejuvenates the catalyst to some extent and significantly improves catalytic performance compared to previous FCC units.
An active stripper is positioned within the stripping vessel. The active stripper is positioned in a region of the stripping vessel where the stripping gas and the partially spent catalyst come into contact. The active stripper has a plurality of structures with features that enhance stripping of the partially spent catalyst. Examples of suitable structures for actively stripping the catalyst include plates, rings, caps, particulate, trays, packing, wire and the like.
The enhanced stripping is typically caused by turbulence and/or contact between the catalyst particles, the stripping gas, and the structural features of the active stripper. The active stripping partially reactivates the catalyst by removing a significant portion of the labile hydrocarbonaceous deposits from the catalyst—in addition to removing hydrocarbons and sweeping the hydrocarbons from between the fluidized catalyst particles.
In one embodiment, the inlet for the stripping gas is a distribution plate with a plurality of nozzles and the active stripper is positioned above the nozzles so as to be within the flow pattern and/or spray pattern of the gases ejected from the nozzles. This configuration of the active stripper is particularly advantageous for partially reactivating the catalyst by, for example, removing coke deposits.
The stripping vessel is also in fluid communication with an inlet of the second reactor for feeding partially spent catalyst to the second reactor after it has been stripped in the active stripper. The partially regenerated catalyst from the active stripper is more active and thus produces higher yields in the second and subsequent reactors than would otherwise be achieved in a serial conventional system. After flowing through the second reactor, the catalyst can be fed to any number of subsequent stripping vessels and/or reactors until the catalyst is fully spent or near fully spent. The spent catalyst is then delivered to a regenerator.
The FCC unit includes a regenerator configured to receive the fully spent catalyst from the last reactor and regenerate the catalyst for reuse in the first reactor. One or more strippers (active and/or non-active strippers) can be positioned immediately before the regenerator. The catalyst is typically regenerated and recycled through the FCC unit numerous times before it is replaced. The catalyst is typically replaced at a fixed rate that depends on a number of factors such as poisons in the feed, thermal degradation of the catalyst activity, and/or selectivity maintenance, and the like.
The present invention also includes a method for upgrading a hydrocarbonaceous material. The method includes the following steps: a) passing hot regenerated catalyst particles from a catalyst regenerator to the bottom portion of a first reactor and injecting a first portion of a hydrocarbon feedstock into the reactor with the catalyst particles; b) passing the catalyst particles and the first feed portion up through the first reactor and into a stripping vessel, whereby the first feed portion is cracked and the catalyst particles are partially spent in the first reactor; c) separating the cracked first feed portion from the catalyst particles and discharging the cracked first feed portion, wherein the separation is at least partially carried out by passing the catalyst particles through an active stripper; d) passing the catalyst particles from the first reactor vessel to the bottom portion of a second reactor and injecting a second portion of the hydrocarbon feedstock into the second reactor; e) passing the catalyst particles and second feed portion up through the second reactor and into a second stripping vessel whereby the second feed portion is cracked and the catalyst particles are further spent; f) separating the cracked second feed portion from the catalyst particles and discharging the cracked second feed portion; and g) returning the catalyst particles to the regenerator and regenerating the catalyst particles. Optionally, a third, fourth, or even more additional reactors can be included and can have active strippers therebetween.
Stripping the partially spent catalyst between stages of a staged catalytic process allows for significantly different process conditions in the downstream stages compared to staged reactor systems where the catalyst is only stripped after the final stage. This is in contract to the methods known in the prior art where stripping is performed before the regenerator to maximize the recovery of the final hydrocarbon product and/or to reduce heat production in the catalyst regeneration unit. (Although known FCC systems use stripping, known FCC systems do not strip between reactors).
The use of the active stripper in the stages of the catalytic cracking unit has a significant positive effect on the activity of the catalyst in the second reactor and subsequent reactors. The partial reactivation of the catalyst is in addition to the removal of hydrocarbons, which would be expected with stripping. As described above, coke deposits are undesirable because they reduce catalytic activity. However, coke buildup is unavoidable and is needed to heat the catalyst in the regeneration unit. Partially reactivating the catalyst between reactors has a substantial impact on the FCC process. One effect is that active stripping substantially delays the complete deactivation of the catalyst to a later point in the catalyst cycle in the FCC unit. This delay results in higher yields and allows better control of cracking in individual reactors. For example, in the first reactor, hard-to-crack materials, including lighter feedstocks such as naphthas with boiling ranges from 100° F. to 400° F. (38° C. to 204° C.) can be cracked while only partially deactivating the catalyst. This allows other higher coking materials to be cracked in downstream reactors with high conversion rates.
The improved catalytic performance of the actively stripped catalyst can also allow for a higher catalyst-to-oil ratio in the reactor. All things being equal, a higher catalyst-to-oil ratio results in faster cracking rates, but with increased coking. However, because the active stripping partially reactivates the catalyst particles, the higher catalyst to oil ratio can be used without disrupting reaction conditions or thermal equilibrium. In one embodiment of the invention, high conversion rates are achieved by using a catalyst to oil ratio in a range from about 12 to about 40, and more preferably in a range from about 15 to about 30, with a staged FCC unit having one or more intermediate active strippers.
These and other advantages and features of the present invention will become more fully apparent from the following description and appended claims as set forth hereinafter.
To further clarify the above and other advantages and features of the present invention, a more particular description of the invention will be rendered by reference to specific embodiments thereof which are illustrated in the appended drawings. It is appreciated that these drawings depict only typical embodiments of the invention and are therefore not to be considered limiting of its scope. The invention will be described and explained with additional specificity and detail through the use of the accompanying drawings, in which:
Embodiments of the invention are directed to a fluidized catalytic cracking unit that includes two or more staged reactors that have catalyst particles flowing in series from one reactor to the next and hydrocarbon feed that is delivered in parallel to the reactors. Between reactors, the catalyst is stripped using an active stripper. The active stripper includes a plurality of structures (e.g., plates or packing) that are positioned within the flow of a stripping gas so as to increase the contact between the structures and the catalyst, thereby facilitating stripping. The active stripping can be implemented in any type of staged FCC unit where catalyst flows in series and hydrocarbon feed is delivered in parallel to the reactors. Examples of suitable reactor types that can be used in accordance with the present invention include low profile FCC units, such as those described in U.S. Pat. No. 4,999,100, and staged vertical FCC units, such as those described in U.S. Pat. No. 5,314,610, both of which are incorporated herein by reference.
The partially spent catalyst is then fed through an active stripping vessel 120a (also referred to as “active stripping compartment”) and stripped of hydrocarbons. The hydrocarbon product 118a is collected and used or transported and/or further processed using refining techniques known in the art. It has been found that active stripping accomplishes more than just effectively removing hydrocarbon product. The active stripping also restores a significant portion of the activity lost in first reactor 112a.
The partially reactivated catalyst from active stripping vessel 120a is then introduced into the second reactor 112b along with a second hydrocarbon feed 116b under fluidized catalytic cracking conditions. Second hydrocarbon feed 116b is broken down into catalytically cracked second products 118b and the catalyst is further spent. Since this particular embodiment includes three stages of reactors, the cracking conditions in the second reactor 112b would typically produce a partially spent catalyst that can be partially reactivated for use in third reactor 112c. However, the present invention also includes embodiments with two stages, in which the second stage would typically produce a fully spent catalyst suitable for regeneration in regenerating unit 1.
The partially spent catalyst from second reactor 112b is then fed through a second active stripping vessel 120b and stripped of hydrocarbons. The second hydrocarbon product 118b is collected and used or transported and/or further processed using refining techniques known in the art.
In yet a third stage, the partially reactivated (i.e., reactivated from the activity lost in second reactor 112b) is introduced into a third reactor 112c with a third hydrocarbon feed 116c under fluidized catalytic cracking conditions and partially or fully spent. The partially or fully spent catalyst from reactor 112c can optionally be fed through active stripping vessel 120c where hydrocarbons are removed. The partially or fully spent catalyst from stripping vessel 120c is then returned to the regenerating unit 114 to be regenerated in an oxidative process (i.e., the coke is burned off to heat the catalyst to a desired temperature).
As discussed more fully below, hydrocarbon 116a, 116b, and 116c, can be the same or different and the catalytic cracking conditions in reactors 112a, 112b, 112c, can be the same or different.
The staged fluidized catalytic cracking unit of the invention can have any configuration that allows for cracking a plurality of feeds using a plurality of reactors while actively stripping partially spent catalyst between the fluidized reactors. The plurality of fluidized catalytic cracking reactors can be separate vessels, as illustrated in
The expanding gases from the feed (and the fluidizing medium if present) convey the catalyst up the reactor 216a. As the catalyst and feed pass up the reactor under fluidized catalyst cracking conditions, the hydrocarbon feed cracks into lower boiling hydrocarbon products. The ratio of catalyst to hydrocarbon feed in the reactor 212a can be within a range from about 3 to about 40 (weight of catalyst per weight of feed). The reactor 212a discharges the catalyst and cracked hydrocarbon into a separation zone, which is provided by vessel 224a. The direction of the flow of the catalyst through the low-profile staged FCC unit, including vessel 224, is indicated by the arrow labeled “A.”
In the separation zone, the majority of the solids are separated from the gases. Partially spent catalyst is allowed to fall toward the bottom of the vessel 224a. Separated gaseous products are collected and removed from product outlet 226a in the top of vessel 224a. While the embodiment illustrated in
The separation vessel 224a also includes an active stripper 220a. The active stripper 220a includes a plurality of structures (one of which is labeled 226a) that are positioned within the flow of the catalyst and within the flow of a stripping gas 228a.
The active stripper structures can be any material shaped and sized to provide a surface area that significantly increases the collisions the catalysts particles have as they travel through active stripper 220a. The particles of catalyst are typically caused to collide with stripping gas, one another, and with the surface of the active stripper structures. The active stripper structures can be a packing material or other shaped structures such plates, rings, caps, particulate, trays, packing, wire, including, but not limited to, sieve trays, baffling, shaped rods, balls, bubble cap trays, packing material such as rings, saddles, shaped cylinders, particulate materials, and or fibrous materials such as steel wool. Any material can be used to make the structures so long as the material is compatible with the conditions within the active stripper (i.e., compatible with the temperature, hydrocarbons, catalyst, etc. within the active stripper).
To increase the collisions of catalyst particles moving through the active stripper 220a, a stripping gas 228a is injected into the active stripper counter to the flow of the catalyst. The stripping gas fluidizes the catalyst, which allows the particles to flow through the active stripper at a desired rate. The fluidization in the stripping vessel 224a is typically less compared to the fluidization in reactor 212a to ensure that the catalyst flows in the desired direction (i.e., from reactor 212a to the stripping vessel 224a). The stripping gas can be introduced into the bottom of vessel 224a using any known technique.
With reference again to
The partially reactivated catalyst from vessel 224a is discharged to reactor 212b. The catalytic activity of the catalyst discharged from vessel 224a is sufficiently high that the catalyst is not regenerated using oxidative treatments (i.e., the catalyst from vessel 224a is not delivered to a regeneration unit such as regeneration unit 14 shown in
Partially reactivated catalyst from separation vessel 224b is introduced into reactor 212c along with a third hydrocarbon feed 216c and under catalytic cracking conditions. The process for cracking and optionally active stripping can be carried out in the final reactor and separation vessel in a manner similar to that described above with respect to reactor 212b and separation vessel 224b.
Following catalytic cracking in reactor 212c, and optionally stripping in stripper 220c, the catalyst is essentially spent. Spent catalyst is delivered to a regenerator where it is heated to burn off coke and to regenerate the catalyst. While the catalyst sent to the regenerator may have an insignificant amount of catalytic activity, those skilled in the art are familiar with the amount of catalytic activity that results in a catalyst being essentially spent (i.e., the catalytic activity is essentially to low for its use to be economically valuable).
In the regenerator, air or oxygen or a mixture thereof is introduced and coke is removed from the catalyst by combustion with the oxygen. The combustion by-products typically rise upwardly along with any entrained catalyst and into a cyclone separator where the catalyst is recovered for continued use in the FCC unit. The burning of the coke heats the catalyst back up to the required cracking temperature and the catalyst is then once again introduced into the first catalytic cracking reactor 212a.
The present invention is not limited to any particular number or repeating stages of catalytic cracking and active stripping vessels so long as at least one active stripper is positioned between the two reactors and the catalyst is not regenerated by an oxidative process between the first and second reactor. However, it can be preferred to have at least three stages to benefit from the differing conditions that can be used for catalytic cracking in three or more stages. Moreover, for staged FCC Units with three or more stages, it is preferably to actively strip the catalyst after each reactor, but not required.
The catalytic cracking conditions used in the staged FCC unit of the present invention will depend on a number of factors, including the particular type of catalyst and the particular feedstock being used. The present invention can be carried out using traditional catalysts for fluidized catalytic cracking of hydrocarbons. In addition, any hydrocarbon feedstock suitable for cracking in a traditional catalytic cracker can be cracked in the staged FCC unit of the present invention. Those skilled in the art are familiar with adjusting process conditions to account for the differences in hydrocarbons and catalyst that have traditionally been used in fluidized catalytic cracking processes.
The conditions in the staged FCC units of the present invention can also be optimized to improve the yields of high value products in ways that cannot be done in traditional FCC units and even staged FCC units lacking the active stripper. The total reaction in any fluidized catalytic cracking is a summation of thermal and catalytic reactions. Thermal reactions are driven by temperature and catalytic reactions are a function of both temperature level and the number and strength of the catalytic sites. The active stripping carried out in the staged FCC unit of the present invention increases the catalytic sites in catalyst, which increases the catalytic sites on the catalyst for all the reactors downstream from the active stripper. This reactivation results in higher catalytic activity and allows the reaction conditions in those reactors to be adjusted accordingly.
In one embodiment of the invention, catalytic cracking is favored over thermal cracking by using a relatively high catalyst to oil ratio. With a higher catalyst to oil ratio (C/O) at a given heat balance, there will be a greater amount of catalytic reactions compared to thermal reactions. Furthermore, there will be higher conversions at any given temperature. The catalytic reactions are preferred since they provide isomerization and result in the desired C3 olefins and iso C4 and C5 compounds as opposed to the thermal reaction products of C2 and lighter compounds. The C/O ratio in each individual reactor can typically be in a range from 3 to 40, but is preferably at least greater than about 8, more preferably greater than about 12, and even more preferably greater than about 15 and most preferably greater than 24.
The use of the active stripper allows for these higher local C/O ratios. Because the active stripper partially reactivates the catalyst, the C/O ratio can be increased while maintaining the same activity over a period of time. Alternatively, the increased activity caused by active stripping can be advantageous for increasing the number of staged reactors in the FCC unit.
Since there is independent staging with only a portion of the total feed going to each stage and with product removal from each stage, it can be seen that the amount of feed to each stage is small as compared to the amount of catalyst flowing through the system. Since the catalyst flows through the entire system the overall C/O will be one third of the individual stage C/O for a three stage system. This example assumes equal feed flow per stage. Variations in feed flow in each stage can be used without departing from the spirit of the invention.
The residence time for each of the separate feed can also be relatively short since the feed only passes through one stage (unlike a single riser system where the initial feed passes through all subsequent stages). The reduced residence time will reduce secondary hydrogen transfer reactions thus favoring the production of olefins and reducing the production of aromatics. Also, the shorter residence times reduce the degradation of product when operating at the higher temperatures which are used to maximize the olefin production. In a preferred embodiment, the residence time of the feed, defined as the volumetric flow rate of the exit gas divided by the reactor volume, is less than 2 seconds, more preferably less than 1.5 seconds, and most preferably less than 1 seconds.
The high catalyst activity due to active stripping, the high C/O ratio, and the short residence time means that the amount of thermal cracking is kept low compared to the amount of catalytic cracking. These improved conditions can be used to achieve higher conversions and higher catalytic content at the same temperature compared to a conventional system or alternatively, these improved conditions can be used achieve similar conversions at lower temperatures while minimizing thermal reactions.
In another embodiment of the invention, the conditions in the staged FCC unit of the invention can be optimized by fractionating the whole feedstock and optimally delivering specific fractions to the different stages of the FCC unit. The processing conditions can be optimized, for example, by cracking hydrocarbons that are more difficult in the earlier staged reactors that have higher catalytic activity. In one embodiment, the fractionation of the feedstock is carried out by fractionating according to boiling point and the lower boiling fractions are processed in earlier stages of the FCC Unit than the heavier boiling fractions. Processing the lighter fractions first can be advantageous because the catalyst will retain more of its catalytic activity throughout the process since the heavier hydrocarbons are known to be coke precursors. In later stages, it can be desirable to use heavier feed fractions with the intent of coking the catalyst just before the regenerator to ensure that catalyst has sufficient coke to be reheated to a proper temperature in the regenerator. In one embodiment of the invention, the feed used in the FCC unit includes at least two fractions, more preferably at least three fractions. In one embodiment, the two or more fractions can be fractionated according to temperature. In one embodiment the feed oil is cut into two or more fractions within a range between 300° F. (148.9° C.) to the endpoint (e.g., 1200° F. [648.9° C.]).
An FCC unit according to the present invention was used to crack a heavy feed. The feed was fractioned into Fraction A with a boiling point below 650° F. (343° C.) and Fraction B having a boiling point above 650° F. (343° C.). The FCC unit used to crack Fractions A and B was configured according to the schematic drawing shown in
In the test runs equilibrium FCC catalyst was charged to the ACE reactor, then the light fraction (Fraction A) was fed into the reactor and the reaction carried out at temperature and a catalyst to oil ratio of approximately 12; then the reactor was stripped with nitrogen and the products collected during both reaction and stripping. The heavy fraction (Fraction B) was then fed into the second reactor at an approximate catalyst to oil ratio of 12 and then stripped once more in a similar fashion as the first stripping and the products collected for analysis.
Subsequently the process was repeated with the same catalyst in a simulation of a low profile FCC process. The reaction in each reactor was carried out similar to the ACE procedures. The test run was carried out by charging a fresh regenerated catalyst into the first reactor with Fraction A at a C/O ratio of approximately 12 and under cracking conditions. Hydrocarbon product was collected and the partially spent catalyst was stripped to partially reactivate the partially spent catalyst (hereinafter the “1× coked catalyst). The 1× coked catalyst was then used in a second run with a first portion of Faction B at a C/O ratio of about 12 and under cracking conditions. The hydrocarbon product from this reaction was collected and the catalyst was stripped to yield a partially spent, partially reactivated catalyst (hereinafter the “2× coked catalyst”). The 2× coked catalyst was then used in a third run with the second portion of Fraction B at a C/O ratio of about 12 under cracking conditions.
Hydrocarbon product was collected from the third run and compared to the hydrocarbon product of the second run and the first run to evaluate the performance of the 1× coked catalyst with the 2× coked catalyst.
As illustrated in
The present invention may be embodied in other specific forms without departing from its spirit or essential characteristics. The described embodiments are to be considered in all respects only as illustrative and not restrictive. The scope of the invention is, therefore, indicated by the appended claims rather than by the foregoing description. All changes which come within the meaning and range of equivalency of the claims are to be embraced within their scope.
| Number | Name | Date | Kind |
|---|---|---|---|
| 2883332 | Wickham | Apr 1959 | A |
| 2900324 | Patton et al. | Apr 1959 | A |
| 3008896 | Lawson | Nov 1961 | A |
| 3964876 | James | Jun 1976 | A |
| 4424116 | Hettinger | Jan 1984 | A |
| 4572780 | Owen et al. | Feb 1986 | A |
| 4863585 | Herbst et al. | Sep 1989 | A |
| 4925632 | Thacker et al. | May 1990 | A |
| 4990314 | Herbst et al. | Feb 1991 | A |
| 4999100 | Thacker et al. | Mar 1991 | A |
| 5059305 | Sapre | Oct 1991 | A |
| 5128109 | Owen | Jul 1992 | A |
| 5284575 | Owen | Feb 1994 | A |
| 5314610 | Gartside | May 1994 | A |
| 5316662 | Cetinkaya | May 1994 | A |
| 5380426 | Johnson et al. | Jan 1995 | A |
| 5498326 | Galtier et al. | Mar 1996 | A |
| 5565177 | Cetinkaya | Oct 1996 | A |
| 5716585 | Senegas et al. | Feb 1998 | A |
| 5858207 | Lomas | Jan 1999 | A |
| 6248298 | Senior et al. | Jun 2001 | B1 |
| 6267873 | Das et al. | Jul 2001 | B1 |
| 7029571 | Bhattacharyya et al. | Apr 2006 | B1 |
| 7261807 | Henry et al. | Aug 2007 | B2 |
| 20040121898 | Mayes | Jun 2004 | A1 |
| 20040182747 | Chen et al. | Sep 2004 | A1 |
| 20050163674 | Letzsch | Jul 2005 | A1 |
| 20060108260 | Henry | May 2006 | A1 |
| 20070251863 | Cunningham et al. | Nov 2007 | A1 |
| Number | Date | Country |
|---|---|---|
| 1185477 | Jun 1998 | CN |
| 1387919 | Mar 1975 | GB |
| 56-004686 | Jan 1981 | JP |
| 06-313176 | Nov 1994 | JP |
| 10-195454 | Jul 1998 | JP |
| 11-043678 | Feb 1999 | JP |
| 2007-177193 | Jul 2007 | JP |
| Entry |
|---|
| Arajulo-Monroy, C. and Felipe Lopez-Isunza; Modeling and Simulation of an Industrial Fluid Catalytic Cracking Riser Reactor Using a Lump-Kinetic Model for a Distinct Feedstock; ACS Publications; Ind. Eng. Chem. Res.; 2005; vol. 45, No. 1; http://pubs.acs.org. |
| UOP Fluid Catalytic Cracking (FCC) and Related Processes; www.uop.com. |
| Number | Date | Country | |
|---|---|---|---|
| 20100174125 A1 | Jul 2010 | US |
