A CATALYTIC CRACKING PROCESS

Abstract: In a catalytic cracking process for a heavy feed comprising non-distillable and distillable hydrocarbons, the feed is initially fractionated into a heavy fraction comprising at least 10 % by weight non-distillable hydrocarbons and at least one lighter fraction containing distillable hydrocarbons. The heavy fraction is then contacted with hot regenerated cracking catalyst in a first zone of a riser reactor at a catalyst:feed weight ratio of a least 5:1 and a temperature of at least 565 DEG C (1050 DEG F), such that the heavy fraction undergoes both thermal and catalytic reactions. The catalyst/feed mixture is then quenched in a quench zone of said riser reactor within 2 seconds of said contacting step with an amount of the lighter fraction at least equal to 100 wt.% of said non-distillable hydrocarbons added to said first zone. Catalytically cracked products and spent cracking catalyst are subsequently removed from the riser reactor, the spent cracking catalyst is regenerated in a catalyst regeneration zone to produce hot regenerated cracking catalyst which is recycled to contact said heavy fraction and cracked products are recovered.

Description: A CATALYTIC CRACKING PROCESS This invention relates to a process of catalytically cracking hydrocarbon feedstocks. A number of processes for the cracking of hydrocarbon feedstocks via contact at appropriate temperatures and pressures with fluidized catalytic particles are known in the art. These processes are known generically as "fluid catalytic cracking" (FCC) processes. Relatively, lighter molecular weight and lower boiling point hydrocarbons, such as gas oils, are typically preferred feedstocks for FCC operations. Such hydrocarbons generally contain fewer contaminants and have a lower tendency to produce coke during the cracking operation than heavier hydrocarbons. However, the relatively low content of such light hydrocarbons in many current crude mixes has lead to the attractiveness of heavier hydrocarbons, for example residual oils, as feedstocks to the FCC operation. One problem with the heavier hydrocarbons, however, is that these materials generally contain a higher level of metals which tend to contaminate the catalyst and increase the yield of coke during the cracking operation. In addition, the heavier hydrocarbons also tend to contain a greater abundance of coke precursors such as asphaltenes and polynuclear aromatics which result in increased coke deposition. Several attempts have been made to minimize the negative impact that heavy hydrocarbon feedstocks tend to have on FCC operation. For example, U.S. Patent No. 4,552,645 eliminates the problem by avoiding the FCC unit altogether, instead routing the heavy hydrocarbon to a stripper/coker wherein such material is thermally cracked at high temperatures. U.S. Patent No. 4,818,372 discloses an FCC process for a heavy feed, such as a resid, in which the entire feed is mixed with regenerated catalyst in a inlet zone of a riser reactor at a temperature sufficient to vaporise and thermally crack the feed. An auxiliary fluid, such as water or a vaporisable hydrocarbon, is subsequently injected into the riser downstream of the inlet zone so that the temperature of the catalyst/feed mixture is rapidly reduced and subsequent conversion of the feed is effected by catalytic cracking. U.S. Patent No. 4,422,925 is directed to an FCC process having a plurality of hydrocarbon feedstocks introduced at diverse locations in a riser type reactor in the presence of a zeolite catalyst. The lowest molecular weight feedstock is introduced in the bottom of the reactor. Hydrocarbon feedstocks having the highest tendency to form coke are introduced in the uppermost section of the riser and are exposed to the lowest reaction temperature and the lowest catalyst to oil ratios. In typical FCC configurations the feedstocks to be cracked are introduced either all together at the bottom of the riser or with the heavier fractions being introduced into the upper portions thereof. In direct contrast to the state of the art as presented by the above described patents, applicants have discovered that it is beneficial and desirable that the heavier, higher molecular weight hydrocarbon feedstocks, i.e., those feedstocks generally having a relatively high tendency to produce coke, be introduced into the riser at a location which is relatively upstream of the location at which the lighter, lower molecular weight feedstocks are introduced. Accordingly the invention resides in a catalytic cracking process for a heavy feed comprising non- distillable and distillable hydrocarbons comprising the steps of: a) fractionating the feed into a heavy fraction comprising at least 10% by weight non-distillable hydrocarbons and at least one lighter fraction containing distillable hydrocarbons: b) contacting said heavy fraction with hot regenerated cracking catalyst in a first zone of a riser reactor at a catalyst:feed weight ratio of a least 5:1 and a temperature of at least 565°C (1050°F), such that the heavy fraction undergoes both thermal and catalytic reactions; c) quenching the catalyst/feed mixture in a quench zone of said riser reactor within 2 seconds of said contacting step with an amount of said at least one lighter fraction at least equal to 100 wt % of said non-distillable hydrocarbons added to said first zone; d) removing catalytically cracked products and spent cracking catalyst from the riser reactor; e) regenerating spent cracking catalyst in a catalyst regeneration zone to produce hot regenerated cracking catalyst which is recycled to contact said heavy fraction; and f) recovering cracked products. The method of the present invention may be used to optimize the slate of reaction products resulting from a single individual feedstock, independently of whether that feedstock is cracked alone or jointly with other individual feedstocks. For example, in certain refinery operating modes only a single unblended hydrocarbon stream may be available as FCC feedstock. According to the present invention, such a feedstock is first separated into light and heavy fractions. The separate fractions are then introduced into the reactor such that the heavy fraction enters the riser at a point relatively upstream of the light fraction. In this way, the conditions under which the light and heavy fractions are cracked may be optimally adjusted. Preferably, the temperature of the catalyst entering the riser is greater than 593 β C (1100°F), and is more preferably between 650 and 790°C (1200 and 1450 β F), while the temperature of the hydrocarbon feedstock is considerably less, generally less than 427°C (800 β F), preferably between 150 and 315°C (300 and 600 β F) . The method of the present invention allows the heavier hydrocarbons to be initially cracked at temperatures which are higher than would otherwise be possible in a typical FCC process. Since only a portion, preferably a minor portion, of the total hydrocarbon charged to the riser is initially contacted with the hot, freshly regenerated catalyst, the temperature of the initial catalyst/hydrocarbon suspension is higher than the temperature which would result if both the heavy hydrocarbon and light hydrocarbon feedstocks were introduced together at a single location in the riser. Accordingly, one important aspect of the present invention resides in subjecting the heavy hydrocarbon feedstock to catalyst mix temperatures which are higher than otherwise attainable without simultaneously subjecting the light feedstock or fractions to such unusually high temperatures. High temperature cracking of relatively heavy hydrocarbon feedstocks increases the production of preferred products at the expense of undesirable coke, without exposing the light hydrocarbons to such temperatures. Initial mix temperature in the heavy hydrocarbon reaction zone are preferably from 565 to 680°C (1050 to 1250 β F), and more preferably from 590 to 650°C (1100°F to 1200 β F). In the method of the present invention, the lighter hydrocarbon fraction is introduced into the riser at a location which is downstream with respect to the heavy hydrocarbon feed injection location. The injection point for the light hydrocarbon feed is preferably selected to ensure that the contact time for the heavy hydrocarbon reaction in the first zone of the riser is short relative to the contact time available in the entire riser. In this way, introduction of the lighter hydrocarbon feed into the suspension acts as a quench for the heavy hydrocarbon reaction and prevents overcracking which would otherwise occur at the relatively high temperatures existing in the heavy hydrocarbon reaction zone. It is believed that the high temperatures existing in the heavy hydrocarbon reaction zone result in vaporization and primary cracking of the asphaltenes, polynuclear aromatics, and other high molecular weight components to desirable products at the expense of coke. Moreover, by ensuring that the contact time in the heavy hydrocarbon reaction zone is relatively short, undesirable secondary cracking of the reaction products is minimized. Preferably, the contact time in the heavy hydrocarbon reaction zone is less than 1/2, more preferably less than 1/3, the contact time in the light hydrocarbon reaction zone. The introduction of the light hydrocarbon fraction into the mixture of catalyst and heavy hydrocarbon fraction is preferably sufficient to assure a reduction in the temperature of mixture of at least 28°C (50°F) , and more preferably at least 56°C (100°F) , with even better results being achieved with even more quenching, e.g., with 83 to 139 β C (150 to 250°F) of quench. The temperature of the mixture immediately after the introduction of the quench fraction is preferably from 510 to 566°C (950 to 1050°F), and more preferably from 527 to 549 β C (980 to 1020 β F) . Feedstock The present invention is applicable for use with any heavy hydrocarbon feedstock containing a mixture of distillable and non-distillable hydrocarbons, such as residual gas oils, topped crudes, deasphalted oils, HDT resids, hydrocracked resids, shale oil, hydrocarbons having an API gravity of less than about 20°, hydrocarbons having an average molecular weight of greater than about 300, hydrocarbons having an initial boiling point of greater than about 371 β C (700°F), hydrocarbons having a CCR content of greater than about 1 wt%, and mixtures of these. The feeds which will benefit most from the practice of the present invention are those which contain at least 10 wt % material boiling above 500 β C, and preferably those which contain 20, 25, 30 % or more of such high boiling material. Especially beneficial results are seen when the heavy feed contains 50 wt % or more material boiling above 500"C. Prior to catalytic cracking, the heavy hydrocarbon feedstock is fractionated by conventional methods into a heavy (relatively high molecular weight) fraction containing at least 10 wt% non- distillable hydrocarbons and at least one lighter (relatively low molecular weight fraction) containing distillable hydrocarbons, preferably in excess of 90wt% distillable hydrocarbons and most preferably 100wt% distillable hydrocarbons. The heavy fraction is then fed to the base of the FCC riser, while said at least one lighter fraction is introduced as a quench fluid further up the riser. The heavy fraction may be mixed with a conventional FCC recycle stream, such as light cycle oil, heavy cycle oil, or slurry oil. In this instance, the FCC recycle stream acts primarily as a diluent or cutter stock whose primary purpose is to thin the resid feed, to make it easier to pump and to disperse into the resid blasting zone. Catalytic Cracking For maximum effectiveness, it is beneficial if the heavy fraction of the feedstock is subjected to unusually severe processing in the base of the riser reactor. The unusual severity is achieved by using catalyst:oil ratios which are significantly higher than those used for conventional cracking. While cat:oil ratios vary greatly from refinery to refiner, and vary greatly in the same unit in response to changes in unit operation, catalyst activity, or demand for products, those skilled in the art will be readily able in a given unit to increase the cat to oil ratio over what had been conventionally used at that refinery for cracking of conventional feeds, e.g. , gas oils, vacuum gas oils, or gas oils containing minor amounts of resid. In particular, the process of the invention employs cat:oil ratios at least 5:1, although it will usually be preferred to operate with cat:oil ratios exceeding 10:1 or 15:1, or even higher. The cat:oil ratio in the base of the riser will usually not be the same as the cat:oil ratio exiting the riser. This is because the present invention will generally produce a non-constant catalyst/oil ratio profile along the length of the riser. That is, the catalyst/oil ratio will decrease as more hydrocarbon is introduced downstream of the base of the riser. Severe preheating will ameliorate to some extent the need for higher cat:oil ratios. Thus it is preferred to operate with heavy feed preheat exceeding the amount of preheat conventionally used, i.e., with a feed preheat from 260 to 430 β C (500 to 800°F) , and even higher if the unit can achieve it. Severe preheating not only reduces the viscosity of the heavy feed, but also generates a certain amount of cutter solvent, and reactive fragments which are amenable, for a short time, to catalytic upgrading in the FCC. Expressed as ERT severity (Equivalent Reaction Time at 427 β C (800°F), in seconds) it is preferred to operate with a feed which has been given a thermal treatment equivalent to from 100 to 1000 ERT seconds. In many units it will also be possible to use hotter catalyst to reduce the need for high cat:oil ratios. Because of the large amounts of Conradson Carbon Residue associated with the heavy feeds contemplated for use herein, the regenerator will probably be pushed to a very high temperature in trying to burn all the coke produced by cracking a heavy feed containing a large amount of resid. It is also possible, and will be preferred in many instances, to use a two stage regenerator, which can produce catalyst of extremely high temperature. Such a two stage approach allows catalyst to be regenerated at extremely high temperature by performing the regeneration in two stages, the first stage at relatively moderate temperature, to burn off the fast coke and remove most of the water precursors. The second stage of regeneration can be at a much higher temperature, because it can be a relatively dry regeneration. Thus catalyst need only be thermally stable to retain activity, not hydrothermally stable. Quench It is essential to rapidly quench the heavy feed within no more than 2 seconds, or preferably even less, of the contact with the hot regenerated catalyst. The amount of quench fluid can be selected to reduce temperatures of resid rapidly and profoundly, preferably to reduce the temperature by at least 56 β C (100"F), and more preferably by at least 83 β C (150°F), and most preferably by at least 111°C (200°F), or more, within a period of no more than a second, preferably 0.5 seconds maximum, and most preferably within 0.2 seconds or less. We have discovered that it is both possible, and beneficial, to use as the quench fluid the conventional feed to a catalytic cracking unit, e.g, a gas oil or vacuum gas oil, in this case derived from the initial distillation step. Use of a conventional feed as a quench liquid is beneficial for several reasons. The most significant reason is that most FCC units must crack a variety of feeds, ranging from resid rich feeds to more conventional stocks such as gas oils and vacuum gas oils and mixtures thereof, hereafter simply referred to as "VGO" for convenience. By using distillable, but crackable, stocks such as VGO as quench, overcracking of VGO in the base of the riser is prevented or at least minimized. The VGO is effective at preventing overcracking of resid, and the VGO is efficiently heated by superheated resid. The VGO, or other distillable, conventional feeds are never subjected to thermal cracking in the riser, because the temperatures experienced by the GO or VGO are similar to those experienced in conventional FCC units. It is preferred that the quench stream be at least 90% distillable, and preferably 95 % distillable, and most preferably 100 % distillable. This is achieved by providing a splitter column just upstream of the cat cracker, to split the total feed into at least a heavy fraction containing at least 10wt% of non-distillable material, and preferably containing over 90wt% of the non-distillable material fed to the cat cracker, and a lighter fraction, comprising at least 90wt% distillable hydrocarbons. The amount of quench should be at least equal to the amount of heavy feed added to the base of the riser. Preferably the quench is present in an amount equal to 100 to 1000 wt %, more preferably 150 to 750 wt%, and most preferably 200 to 600 wt %, of the non- distillable feed added to the base of the riser. If the heavy feed to the base of the riser comprises 50 wt% resid, and 50 wt% distillable material, then 1 to 10 weights of quench should be used for each weight of resid feed. Expressed as ratios of quench to heavy feed, where the heavy feed includes both the resid and any distillable material mixed in with the resid, the quench to heavy feed weight ratio, for the heavy feed just described, should be 0.5 to 5.0, preferably 0.75 to 3.75, and most preferably 1 to 3 weights of reactive quench per weight of total heavy feed to the base of the riser. An additive quench fluid, such as an alcohol, may be used in addition to quenching with VGO. Riser Top Temperature Although conditions at the base of the riser are far more severe than those associated with conventional FCC operations, the FCC unit at the top of the riser, and downstream of the riser, can and preferably does operate conventionally. When processing large amounts of resids, especially those which contain large amounts of reactive material which readily form coke in process vessels and transfer lines, it may be preferable to operate with conventional, or even somewhat lower than normal riser top temperatures. Riser top temperatures of 510-566°C (950-1050°F) will be satisfactory in many instances. Catalyst Activity Conventional FCC catalyst, i.e., the sort of equilibrium catalyst that is present in most FCC units, can be used herein, but will not lead to optimum results. For optimum results, it is preferable to use a catalyst which has a relatively high zeolite content, i.e. in excess of 30 wt%, and preferably approaching or even exceeding 50 wt%, large pore zeolite. The large pore zeolite preferably has a relatively small crystal size, to minimize diffusion limitations. The zeolites should be contained in a matrix which has a relatively high activity, such as a relatively large alumina content. Especially preferred is use of a high activity matrix comprising at least 40 wt% alumina, on a zeolite free basis and having sufficient cracking activity to retain at least a 50 FAI catalyst activity within said quench zone. Ideally, a catalyst is used which retains at least a 55 FAI cracking activity within said quench zone. The catalyst will also benefit from the presence of one or more metal passivating agents in the matrix. The catalyst should also be formulated to have a relatively large amount of its pore structure as large macropores. Many catalysts having at least some of these properties have been developed, primarily for cracking resids mixed with conventional feeds. These resid cracking catalyst are highly preferred for use in the process of the present invention, because conventional equilibrium FCC catalysts now widely used can be overwhelmed by cracking resid rich fractions. Use of a catalyst having the preferred characteristics described above allows significant cracking of resid or other heavy feed in the base of the riser, while retaining enough activity to permit vigorous conversion of the reactive quench, e.g., VGO, added higher up in the riser. Thermal Reactions Even if the catalyst is rapidly deactivated by cracking the resid, such that there is little or no overall gain in conversion or gasoline yield, the process of the present invention is still beneficial because of the improved properties of the heavy products. By subjecting the resid, or a resid rich fraction, to thermal cracking, the viscosity of the heavy product will be reduced. Conventional techniques can be used to calculate or estimate the amount of thermal reaction that occurs in the base of the riser, with some complications because of almost complete vaporization and endothermic catalytic reactions. In general, it is believed beneficial to achieve thermal conversion of resid equal to roughly 50 to 1000, and preferably 100 to 700 ERT seconds in the base of the riser. This will provide enough thermal cracking in the base of the riser to generate heavy "cutter stock" which will significantly reduce the viscosity of the heavy fuel oil product. Because of the difficulty of accurately determining ERT in the base of the riser, and the importance of heavy fuel oil viscosity as a product specification, it may be preferable to adjust the thermal cracking severity so as to obtain at least a 10 %, or 20 %, or even higher, reduction in the viscosity of a specified heavy fuel oil fraction. Additive Catalysts In many instances it will be beneficial to use one or more additive catalysts, which may either be incorporated into the conventional FCC catalyst, added to the circulating inventory in the form of separate particles of additive, or added in such a way that the additive does not circulate with the FCC catalyst. ZSM-5 is a preferred additive, whether used as part of the conventional FCC catalyst or in the form of a separate additive. EXAMPLE 1 A relatively light FCC hydrocarbon feedstock consisting essentially of 100% vacuum gas oil is provided. A relatively heavy FCC hydrocarbon feedstock consisting essentially of 25 vol. % vacuum resid and 75 vol. % vacuum gas oil is also provided. The heavy feedstock and the light feedstock, each at approximately 149°C (300°F), are introduced together in the bottom of a riser reactor in a heavy feedstock: light feedstock ratio of about 4:6 on a volume basis. The feedstocks are contacted with an equilibrium catalyst at a temperature of about 710°C (1310°F). Sufficient catalyst is introduced into the riser to produce a catalyst/oil weight ratio of about 7.4 and an initial catalyst/ hydrocarbon mix temperature of about 571°C (1060°F) . The length of the riser is sufficient to give a total contact time of approximately 2 seconds. The conversion, gasoline, alkylate, 343°C+ (650 β F+) and coke yields expected from such an operation are as follows: 71 vol% conversion; 52 vol% gasoline; 28 vol% alkylate; 10 vol% 343 β C+ (650°F+) and 6 wt % coke. EXAMPLE 2 The heavy and light hydrocarbon feedstocks described in Example 1 are provided. The heavy hydrocarbon feed, i.e., the feed comprising 25 vol% vacuum resid, is injected at the bottom of the same riser into the same catalyst circulation stream described in Example 1. The contact between the heavy hydrocarbon feed at 149°C (300 β F) and the recirculating catalyst at 710 β C (1310°F) produced a initial heavy hydrocarbon mix temperature of about 660° (1220°F) and a catalyst/oil ratio of about 18.5. At a second injection point located approximately one-tenth of the total reactor length above the bottom injection nozzles, the relatively light hydrocarbon feed is introduced into the suspension, thereby quenching the reaction temperature to about 549°C (1020°F) . Accordingly, the heavy hydrocarbon feedstock is cracked in the heavy hydrocarbon reaction zone at relatively elevated temperatures for approximately 0.2 seconds. On the other hand, the light hydrocarbon feed will experience essentially conventional cracking for about 1.8 seconds in the light hydrocarbon reaction zone. The expected conversion, and gasoline, alkylate, 343°C+ (650°F+) , and coke yields resulting from this operation are as follows: 72.51 vol% conversion; 52 vol% gasoline; 34 vol% alkylate; 9.4 vol% 343 β C+ (650°F+) ; and 6 wt% coke.

Claims: CLAIMS : 1. A catalytic cracking process for a heavy feed comprising non-distillable and distillable hydrocarbons comprising the steps of: a) fractionating the feed into a heavy fraction comprising at least 10% by weight non-distillable hydrocarbons and at least one lighter fraction containing distillable hydrocarbons: b) contacting said heavy fraction with hot regenerated cracking catalyst in a first zone of a riser reactor at a catalyst:feed weight ratio of a least 5:1 and a temperature of at least 565°C (1050°F), such that the heavy fraction undergoes both thermal and catalytic reactions; c) quenching the catalyst/feed mixture in a quench zone of said riser reactor within 2 seconds of said contacting step with an amount of said at least one lighter fraction at least equal to 100 wt % of said non-distillable hydrocarbons added to said first zone; d) removing catalytically cracked products and spent cracking catalyst from the riser reactor; e) regenerating spent cracking catalyst in a catalyst regeneration zone to produce hot regenerated cracking catalyst which is recycled to contact said heavy fraction; and f) recovering cracked products. 2. The process of claim 1 wherein said lighter fraction is selected from hydrocarbon feeds boiling in the gas oil and vacuum gas oil range, naphtha boiling range hydrocarbons, and normally gaseous hydrocarbons. 3. The process of claim 1 wherein the heavy fraction comprises at least 50 wt% material boiling above 500°C. 4. The process of claim 1 wherein said lighter fraction is added in an amount equal to 100 to 1000 wt % of said non-distillable hydrocarbons added to said first zone. 5. The process of claim 1 wherein said lighter fraction is added in an amount equal to 200 to 750 wt % of said non-distillable hydrocarbons added to said first zone. 6. The process of claim 1 wherein the quenching step reduces the temperature in the riser reactor by at least 56°C (100"F) within 0.5 seconds. 7. The process of claim 1 wherein the quenching step reduces the temperature in the riser reactor by at least 83°C (150"F) within 0.5 seconds. 8. The process of claim 1 wherein the quenching step reduces the temperature in the riser reactor by at least lll β C (200 β F) within 0.5 seconds.

Inventors: KRAMBECK FREDERICK JOHN, NACE DONALD MILLER, SAPRE AJIT VISHWANATH, SCHIPPER PAUL HERBERT, KRAMBECK, FREDERICK, JOHN, NACE, DONALD, MILLER, SAPRE, AJIT, VISHWANATH, SCHIPPER, PAUL, HERBERT
Applicants: MOBIL OIL CORP, MOBIL OIL CORPORATION
Application year: 1993
Main classification: C10G11
IPC codes: C10G11