JP2001504517A - Process for obtaining olefins from residual and other heavy feeds - Google Patents

Abstract

(57) Abstract: Significant amounts of olefinic products from resids and other heavy feedstocks can be obtained by using steam short contact thermal processing equipment that includes a horizontal moving bed of fluidized heat transfer solids. How to get. The solid bed may also contain components having catalytic activity for the production of olefins.

Description

DETAILED DESCRIPTION OF THE INVENTION           Process for obtaining olefins from residual and other heavy feeds Field of the invention   The present invention relates to a short steam contact time conversion process comprising a moving bed of hot solids. The use of equipment allows significant amounts of Ore from residual and other heavy materials. A method for obtaining a fin-based product. Steam short contact time conversion process equipment Operated under conditions that can include steam dilution to reduce the partial pressure of hydrogen vapor; The moving bed of hot solids contains components that have catalytic activity for the production of olefins. Can also be.Background of the Invention   In a typical refinery, crude oil is subjected to atmospheric distillation to obtain light oil, kerosene, and gasoline. Produces lighter fractions such as phosphorus, straight run naphtha, and others. Like naphtha Gasoline is easily spilled by heat or catalysts such as gasoline boiling range petroleum fractions and gas oils. The fractions that can be converted to products in the boiling range are the most valuable products in the refinery. It is a flow. The bottoms from the atmospheric distillation process are then distilled at subatmospheric pressure . The latter distillation step is a vacuum gas oil distillate and vacuum reduced resid. sidual oils), which are typically significantly cheaper than light oils. Residual feed Typically contains significant amounts of asphaltene molecules, which are usually present in the feed. Significant amounts of Conradson carbon residue and metal components Is the cause. They also have relatively high concentrations of sulfur and nitrogen Including atoms. Such supplies have little commercial value. Because the Lord In addition, they may be used as fuel oils due to more stringent environmental regulations Is not possible. They are also used in refinery processes such as catalytic cracking of fluids. There is little value as a feedstock for the production. Because they are too much gas And coke are generated. Also, their high metal content makes the catalyst deactivated Bring. They are generally used in steam cracking process equipment. Not suitable. Because excessive coke is formed in the pyrolysis tube This causes overheating. Thus, for example, such supplies can be made more valuable. By modifying such feeds into higher clean, lighter feeds, Great demand for greater use of feedstock in oil refining I do.   Most refinery processes use waste logistics with desired higher value products. Manufacture it. One particularly troublesome waste stream is the lube oil extract stream (lube e xtract stream), which itself has little commercial value . Such streams can remove unwanted molecules, such as relatively high concentrations of polycyclic compounds. Including. The lube oil extract stream, as well as the resid stream described above, It has little value as a feedstock for local processes. because, Because they produce excess gas and coke. Also those high gold The metal content leads to catalyst deactivation. Therefore, the utilization of such feedstocks will be greater. Or to make such supplies more valuable, cleaner and lighter. There is a great demand in petroleum refining for reforming to make.   Significant amounts of feedstock in the gas oil boiling range can be found in fired tubes or Produces olefins in steam cracking process equipment, including coil furnace Wherein the feed is from about 540 ° C. to 76 ° C. in the presence of steam. Pyrolyzed at a temperature of 0 ° C. Gas oil is a suitable feedstock for such purposes. But they are preferred for use in the production of transportation fuels Therefore, it is also a relatively expensive feedstock. Residual oil supplies that are significantly cheaper than diesel Not suitable for use in steam crackers. Because in the furnace tube Cracking and coke formation in the tank causes overheating and equipment blockage It is.   One attempt to overcome these problems is disclosed in U.S. Pat. No. 2,768,127. Which produces aromatic and olefinic product streams. Teaches the use of resid feedstocks. This is about 675 ° C to 7 ° C. The resid feed is fed into a fluidized bed of coke particles maintained at a temperature of 60 ° C. This is done by contact. Such attempts have overcome these problems. Improved but with better control of the residence time of solids and vapors There remains a need for a process.   Lighter production of hydrocarbons, such as paraffin, up to naphtha and light oil Pyrolysis to produce products, especially lighter olefins, is of commercial importance. You. Major commercial sources for the pyrolysis of such hydrocarbons into olefinic products A typical process is steam cracking, where the hydrocarbons are deposited in a tubular metal tube or coil in a furnace. Pyrolyzed in the presence of water vapor in a gas (pyrolysis tube). Research rises in temperature As the response time, measured in milliseconds, decreases This shows that a modest yield improvement can be obtained.   Traditional steam cracking is a single-phase process in which hydrocarbons and steam are mixed. The compound passes through the tubes in the furnace. Water vapor acts as a diluent, hydrocarbons are broken down To produce olefins, diolefins, and other by-products. Traditional steaming In a gas cracking reactor, the conversion of the feed is generally controlled by the permissible temperature of the tube metal. Additional sensible heat within a sufficiently short dwell time without exceeding temperature limits And the inability to supply heat of decomposition. Relatively high temperature Long residence times in the product are usually undesirable due to side reactions that degrade product quality. I don't. Another problem that arises is the coking of pyrolysis tubes. Should be disassembled The thickness of the coke on the inner wall of the metal surface in contact with the feedstock gradually increases. this Coke layers are preferred in terms of heat transfer losses resulting in high tube metal temperatures. Absent. The steam cracking process is described in U.S. Pat. Nos. 3,365,387 and 4,061, 562, and Chemical Week, Nov. 13, 1965, pp. 69-81, "Ethylene" table And all of which are incorporated herein by reference. Have been.   Typical supply to steam cracking process equipment for the purpose of producing olefins Feedstocks are relatively expensive feeds such as ethane, liquefied petroleum gas, naphtha, and diesel. Raw material. Olefin can be produced from heavier feedstocks such as resid feeds. This is a significant economic advantage.Summary of the Invention   According to the present invention, there is provided a method for producing an olefin from a resid feedstock, the method comprising: The method is       (i) Heat transfer solids containing carbonaceous deposits on the surface A heating zone, which is entered and heated in the presence of oxidizing gas,       (ii) Includes a bed of fluidized solid consisting of heat transfer solids recycled from the heating zone. Vapor short contact time reaction zone, and       (iii) solids having carbonaceous deposits on the surface are sent from the reaction zone and pass through, Additional lower boiling hydrocarbons and volatiles are recovered along with the stripping gas. Stripping area, Converting the feedstock in a process apparatus comprising:       (a) feeding the resid feed to the steam short contact time reaction zone (here The resid feedstock comes into contact with the fluidized heat transfer solids and catalyst components and The temperature range is from about 670 ° C to about 870 ° C and the residence time of solids and residence time of steam are independent. Operating under controlled conditions, the residence time of the steam is less than about 2 seconds, The dwell time of the hard rest is from about 5 to about 60 seconds, thereby depositing on the solid. A substance and a vaporized fraction containing olefinic products are obtained, and the substance is Characterized as a sinterable carbonaceous metal-containing material),       (b) separating the vaporized fraction from the solids;       (c) converting the vaporized fraction to a temperature low enough to stop the conversion. Quenching,       (d) sending the separated solid to the stripping zone, where the solid is stripped. Contact with the tripping gas, thereby removing any residual volatiles from the solid Removing,       (e) sending the stripped solid to the heating zone, where the solid is removed. Heating to an effective temperature that maintains the operating temperature of the reaction area; and       (f) Recycle the heated solid from the heating zone to the reaction zone where the solid Supplies the heat of reaction and comes into contact with the new feedstock, Are provided.   In a preferred embodiment of the present invention, the method of the present invention comprises about C_FiveHydrocarbon boiling A hydrocarbon feed having an average boiling point from about 545 ° C to about 545 ° C;       (i) introducing the feed into a steam cracking furnace where the feed is steamed; Departure Decompose to low boiling products in the presence of steam,       (ii) stopping the decomposition reaction of the vaporized and decomposed product stream. Quenching to a sufficiently low temperature; and       (iii) quenching the quenched steam flow from step (c) above. Air flow and separation, compression, contaminant scrubbing, and olefin recovery. Together in a typical downstream steam cracking facility selected from the group Further converting to lower boiling products.   In another preferred embodiment, the process of the present invention comprises an olefin-rich process. Further comprising separating the distillate fraction from the quenched vaporized fraction from step (c).   In another preferred embodiment of the present invention, the steam short contact time reaction zone is , Consisting of a horizontal moving bed of fluidized heat transfer solids.   In yet another preferred embodiment of the present invention, the reaction zone is provided by mechanical means and And vaporized normal gaseous hydrocarbons, hydrogen, hydrogen sulfide, and added steam Fluidized with the aid of a fluidizing gas consisting of It can consist of a set of screws arranged horizontally on the part.   In another preferred embodiment, the heat transfer solid has a catalytic component.   In another preferred embodiment of the invention, the dwell time in the reaction zone for the solid The duration is about 10 to 30 seconds and the residence time for the vapor is less than 1 second.   In yet another preferred embodiment of the present invention, the feed is a vacuum distillation bottoms (vacuum resids), atmospheric distillation resids (atmospheric resids), heavy and crude petroleum crudes , Pitch, asphalt, bitumen, tar sand oil, shale oil, coal, From the group consisting of coal slurries and coal liquefaction bottoms Selected.   In another preferred embodiment of the present invention, the catalyst component is magnesium oxide, Calcium oxide, manganese oxide, beryllium oxide, strontium oxide, Selected from the group consisting of lium, vanadium oxide, cesium oxide, and mixtures thereof. Selected.   In yet another preferred embodiment of the present invention, the catalyst component comprises a refractory metal acid Chloride, aluminate, zeolite, spent fluid catalytic cracking catalyst, rich in vanadium Selected from the group consisting of waste flue particles, spent bauxite, and mixtures thereof. Selected.BRIEF DESCRIPTION OF THE FIGURES   Accordingly, two schematic diagrams of a non-limiting preferred embodiment of the present invention are shown. The drawing is shown. FIG. 1 shows a heating zone, a steam short contact time reaction zone, and stripping. 1 illustrates one embodiment of the present invention that includes a logging region. FIG. 2 shows the above-mentioned characteristics with a steam cracker. The combined embodiment is shown.Detailed description of the invention   Residual feedstock suitable for use in the practice of the present invention is above about 480 ° C. Lower temperature, preferably higher than about 540 ° C, more preferably higher than about 560 ° C. Are also hydrocarbon streams that boil at elevated temperatures. A non-limiting example of such a flow is , Vacuum distillation residue, atmospheric distillation residue, heavy and outstanding petroleum crude oil, pitch, asphalt , Bitumen, tar sand oil, shale oil, coal slurry, and coal liquefaction residue Contains liquid. Such a stream may contain small amounts of lower boiling materials. these The stream is fed to a petrochemical process unit used to produce the olefin product. It is not normally used as a feed to some steam crackers. Because they are This is because a large amount of coke that pollutes the furnace tube is generated. Such supplies are usually At least 5% by weight, generally about 5 to 50% by weight, and typically about 7% by weight % Of Conradson carbon. Conrad Son carbon residue is measured according to ASTM test D189-65. The residual oil feedstock is as follows Light olefins in the steam short contact time mechanical fluidization process equipment described in Are converted to lower boiling products containing methane.   Co-feeds, preferably refinery waste streams, are also resid feeds in accordance with the present invention. Can be used with raw materials. Non-limiting examples of suitable sub-feeds include Effluent stream, deasphalted rock petrolatum, and 26 Fluidized catalytic cracking, fluidized coking, and delay boiling above 0 ° C It is a heavy product from delayed coking. Feed to reaction zone Up to about 50% by weight of the stream may be the sub-feed portion. About 10% by weight of the total feed stream The following is preferably the sub-feed portion, more preferably no more than about 25% by weight. You.   As used herein, a "lubricating oil extract" is dissolved in a selective solvent, thereby Is the portion of the lubricating oil feed that is removed. Typically, solvent extraction involves (i) Degree index, (ii) oxidation resistance, (iii) to improve the color of the lubricant base stock, and ( iv) lubrication by separating aromatic moieties from naphthenic and paraffinic moieties Used to reduce the tendency of the lubricant to form carbon and sludge. used The most common solvents are furfural, phenol, and N-methyl-2-pyrrolide (NMP). Lubricating oil extracts are typically about 10-30% by weight saturated. About 15 to 25% by weight of a monocyclic compound, about 20 to 30% by weight of a bicyclic compound About 10 to 20% by weight of a tricyclic compound, about 5 to 20% by weight of a tetracyclic compound. And about 1 to 10% by weight of a polar compound, wherein the weight percentage is Based on the total weight of the item. Petrolatum is a soft petroleum substance obtained from petroleum residues. Consisting of amorphous wax and oil.   Typical feedstocks suitable as feeds to the steam cracker of the present invention are ethanol Gas and liquid petroleum gas (LPG), gasoline, naphtha, and light oil (ie, middle distillates) )). As used herein, "light oil" Is a so-called light gas oil having an average boiling point of about 230 ° C to 340 ° C, Means both so-called heavy gas oils having an average boiling point of 315 ° C. to about 545 ° C. You. Middle distillates are typically used as kerosene, household heating oil, and diesel motor fuel. It is a fuel that is typically used.     The olefinic product is heated from the resid feedstock according to the invention in the heating zone Steam short contact time process including contact time fluidized bed reaction zone and stripping zone Manufactured in equipment. Reference is now made to FIG. This is a preferred feature of the present invention. 1 illustrates a simplified process embodiment in simplified form. The residual oil feedstock is Via an in 10 steam short containing a horizontal moving bed of fluidized hot heat transfer solids The contact time is supplied to the reaction zone 1. Solids in steam short contact time reactors are mechanical means It is preferably fluidized with the aid of Fluidization of solid bed vaporized Fluidization of normally gaseous hydrocarbons, hydrogen, hydrogen sulfide, and added steam Assisted by the use of gas. "Added steam" means that of the fluidizing gas. This means that, like the other components, no water vapor is produced during the process. further, Mechanical means has relatively high mixing efficiency with very little axial backmixing It is preferably a mechanically mixed system characterized by the following. Such a mixture The system has a flow pattern that ensures that the residence time is approximately equal for all particles. It acts like a plug flow system with a loop. Most preferred Mechanical mixing systems are called LR-Mixer or LR-Flash Coker by Lurgi AG of Germany Type of mixer, which was originally oil shale, coal, and tar Designed to handle the command. LR-Mixer rotates two horizontally oriented Consist of screws, which aid in the fluidization of the solids.   Heat transfer solids are typically substantially catalytically inert for olefin production. You. That is, the olefin is mainly produced by thermal conversion. Heat transfer solid is the catalyst component Is also within the scope of the present invention. Heat transfer solids produce olefins thermally Thus, it acts as a heat carrier for transferring heat from the heater to the reaction zone. Catalyst If more are present, more olefins are produced. That is, the olefin is heat It is produced by both catalytic and catalytic means. The catalytic activity of the catalyst component is an effective activity Having. Effective activity means that the catalytic activity is acceptable for relatively high concentrations of olefins. Produced without the formation of undesired amounts of undesired reaction products, e.g. methane Means to be controlled. Heat transfer solids are typically Petroleum coke from the refining process and recycle coke from the process equipment of the present invention. It is an inert substance such as dust or sand. Unlimited number of substances that can be used as catalyst components Typical examples are refractory metal oxides and aluminates, zeolites, used fluid contacts. Catalytic catalyst, vanadium-rich flue particles, used bauxite, and it And mixtures thereof. The term "used bauxite" is also called "red mud" However, in this specification, the bauxite waste remaining after the production of aluminum Means part. Spent bauxite is typically produced after aluminum production It is an inorganic substance in the form of an oxide that remains. A typical analysis of used bauxite is About 30 to 35% by weight of FeO (OH) -AlO (OH), about 15 to 20% by weight of Fe_TwoO_Three, About 3 ~ 7% by weight CaCO_ThreeAbout 2 to 6% by weight TiO_Two, And each less than about 3% by weight SiO_TwoAnd Mn_ThreeO_FourIt is. Other inorganic substances may also be present in variable amounts. Good Preferred refractory metal oxides are metals Ia, IIa, Va, VIa, VIIa, VIIb, and VIIIa and lanthanide groups. This specification The periodic table referred to in this document was prepared by Sargent-Welch Scientific Company. Published catalog No. S-18806, Copyright 1980. Preferred is oxidation Magnesium, calcium oxide, manganese oxide, beryllium oxide, stron oxide Select from the group consisting of Titium, Cerium Oxide, Vanadium Oxide, and Cesium Oxide Metal oxide.   If the catalyst component is used with a heat transfer solid, at least an effective amount of the catalyst component It is preferably used in the practice of the present invention. "Effective amount" means a relatively inert Olef chosen when using only heat transfer solids under the same reaction conditions without catalyst components At least 5%, preferably at least 10%, more preferably Means the minimum amount required to increase olefin yield by at least 20% I do. Typically, the catalyst component has a particle size substantially the same as or smaller than the heat transfer solid. And typically adheres to the surface of the heat transfer solid. Percentage of catalyst components in total solid At least 3% by weight, based on the total weight of solids in the reaction zone %, Preferably about 10 to 25% by weight. The catalyst component can be in any suitable position Can be introduced into the process. For example, the catalyst component reacts with the steam for short contact time. It can be introduced directly into the vessel and can be introduced with the feed. Izu Nevertheless, if a mixture of substantially inert solids and catalyst solids is used, the catalyst solids The body is preferably dispersed on the surface of an inert solid, especially where most of the solid is inert This is the case when the catalyst component is in powder form. The catalyst component is a relatively inert heat transfer solid. It may be incorporated or dispersed inside the body. The heat transfer solid is coke particles Preferably, they may be any suitable other refractory particulate material. That Non-limiting examples of other suitable refractory particulate materials, such as silica, alumina, di Luconia, and mullite, synthetic or natural substances such as pumice, clay, porous Diatomaceous earth, bauxite, etc. The heat transfer solid is preferably about 40 microns To 2000 microns, more preferably from about 200 microns to about 1000 microns Having an average particle size of from 400 microns to 800 microns. Touch It is also within the scope of the present invention that the medium component comprises 100% of the heat transfer solid.   The feed is preferably from about 670 ° C to about 870 ° C, more preferably 780 ° C. Contact with a fluidized hot heat transfer solid at a temperature of 乃至 850 ° C. Offering A significant portion of high Conradson carbon and metal-containing components from feed are on hot solids. Attached as high molecular weight combustible carbonaceous metal containing material to The rest is vaporized A significant amount, typically about 10 to 50, based on the total weight of the product stream. %, Preferably from about 20 to 50% by weight, and more preferably from about 3% by weight. It contains 0 to 50% by weight of olefin product. Raw material obtained by practicing the present invention The olefin portion of the product stream typically has about 5 to 15 % Methane, about 5 to 30% by weight, preferably about 10 to 30% by weight of ethylene. And about 5 to 20% by weight of propylene.   The residence time of the vapor product in the reaction zone 1 is an effective amount of time. That is, sub-decomposition The time is short enough that little reaction occurs. This time is typically Less than about 2 seconds, preferably less than about 1 second, and more preferably less than about 0.5 seconds. Full, and most preferably less than about 0.25 seconds. Solid stagnation in the reaction zone The residence time is about 5 to 60 seconds, preferably about 10 to 30 seconds. Of the present invention One of the new features is the short residence time of the solid and the steam This means that the residence time of the gaseous products can be controlled independently. Traditional fluid bed pro Process equipment, especially at relatively short vapor residence times It is such that the residence time cannot be controlled independently. For example, traditional Transfer line reactors have relatively short residence times However, it cannot be designed to independently control the residence time of solids and vapor. Conversely, Dense fluidized bed reactor is independent of vapor and solid residence time The control is flexible, but the residence time is relatively long. Steam short contact time The process equipment preferably has a ratio of solids to feed of about 40: 1 to 10: 1. Preferably, it is operated at about 25: 1 to 15: 1. Specific driving The exact ratio of solid to feed is mainly due to the short contact time Depends on the heat balance requirements. Relate solid to oil ratio with heat balance requirements It is within the skill of the artisan and therefore is not described in detail herein. No explanation. A small amount of the feedstock deposits on the solid in the form of a combustible carbonaceous material. Metallic components also adhere to the solid. Therefore, when compared to the original feed, Distillate Will have significantly lower amounts of both Conradson carbon and metal.   The vaporized fraction exits the reaction zone via line 11 and passes via line 12 The temperature at which substantial thermal decomposition occurs by using quenched liquid Rapidly cooled to a lower temperature. Preferred quenching liquids are water, and naphtha and distillate Hydrocarbon stream. The temperature at which the vaporized fraction is quenched depends on the reaction zone It is generally preferred that the temperature be about 50 ° C to 100 ° C below the temperature of Evaporated fraction Is then introduced into cyclone 2 where most of the solids or dust that have flowed in is removed. It is. The resulting dust-free steam is then passed through line 13 to scrubber 3 Where the light product stream is recovered overhead via line 28. The light product stream typically has an end boiling point of about 510 ° C. I do. This light product stream typically has a volume of about 7 to about 7%, based on the total weight of the feed. From about 10% by weight of methane, 5 to 30% by weight of ethylene, and 5 to 20% by weight of Propylene and 6-9% by weight of unsaturated C such as butane and butadiene_FourKind including. The remaining heavier stream is recovered from the scrubber via line 26 Is recirculated to the reaction zone 1.   The solids having carbonaceous material attached to the surface from reaction zone 1 via line 15 It is sent to the solid bed 17 in the stripper 4. The solid moves down the stripper Pass through the stripping zone, where any remaining volatiles or vaporized A possible substance is introduced into the stripping zone via line 16 into the stripping zone. Stripping is performed using a ping gas, preferably steam. Stripi Steamed product travels upward through stripper vessel 4 via line 19 To reaction zone 1 and then to cyclone 2 via line 11 and And is removed along with the light product stream via line 13. Stripped The solids are sent via line 18 to a heater 5 containing a heating zone. With heater 5 The heating area, which is a combination of the transport line 18a, is provided for the coke deposited on the solid. Combustion, preferably by air, increases the effective temperature, i.e. the thermal requirements of the reaction zone. Heat at a satisfactory temperature. Air goes to the line to help burn carbonaceous components Injected via 20. The heating zone is typically lower than the operating temperature of the reaction zone 1. About 40 ° C to 200 ° C, preferably about 65 ° C to 175 ° C, more preferably It operates at a high temperature of about 65 ° C to 120 ° C.   It should also be understood that pre-heated air can be introduced. Heater is typical Typically within the range of about 0 to 150 psig (0 to 1136 kPa), preferably about 15 It operates at a pressure in the range of from about 50 to about 45 psig (204.8 to 411.7 kPa). Some carbon residue burns from solids in the heating zone, but the solids pass through the heater After that, it is preferred that only partial combustion occur to have value as a fuel. New Excess solids can be removed from the process equipment via line 50 You. Flue gas is removed from the top of heater 5 via line 40. Flue gas Can be passed through a cyclone system (not shown) to remove particulates. dust Waste CO2 boiler containing waste heat recovery system (not shown) (Not cleaned), and scrape to remove contaminants and particles. You can bing. The heated solid is then reacted via line 14 to the reaction zone. Recirculated to zone 1. Introduce catalyst components anywhere in the process where practical can do. For example, the catalyst components can be supplied to the heater 5, the reactor 1, or the line 1 0 can be introduced with the feed.   Reference is now made to FIG. 2, which illustrates another preferred embodiment of the present invention. Already One feed is fed via line 44 to a conventional steam cracking process unit 6 Is entered. Suitable feedstocks for steam cracking according to the invention are ethane to gas oil boiling range. Within or above the box. Preferred feedstocks are naphtha and higher boiling Includes point feed, for example, middle distillate. A conventional steam cracker, i.e., steaming In an apparatus for pyrolysis using gas, the hydrocarbon feed is fed in a tube furnace. Heated slowly, where it is vaporized and decomposed. This reaction is endothermic, Occurs mainly in the hottest parts. The temperature of the process stream in these tubes is decomposed Determined by the nature of the hydrocarbon to be produced, such hydrocarbons usually being ethane or Liquefied petroleum gas, or gasoline or naphtha, and light oil. For example, naphtha The feed is typically cracked at higher temperatures in the cracking zone than gas oil. these The temperature is determined by fouling or coking of the decomposition tube, as well as by the decomposition reaction and the desired reaction. It is greatly influenced by the kinetics of the product. Regardless of the nature of the feedstock, its temperature The degree is always very high, typically above about 700 ° C. However, it is Limited by the high acceptable tube metal temperature, which is usually on the order of 1100 ° C. The vapor effluent exiting the steam cracker via line 46 passes via line 48 Quenched with a relatively cool liquid. The quenched steam flow passes through line 49 Rectification column 7 and compression, scrubbing, and olefin recovery via These are all sent to downstream equipment (represented by 8). Spirit A typical product fraction from the distillation tower contains heavy oil (above 340 ° C.), at least Some can be recycled to the steam short contact time process equipment. Other wishes The new product fraction can include light oil and naphtha. The steam product is then further To a further downstream facility as described above via line 56 for processing. It is. The feed to the steam cracker is C_FiveAnd higher boiling stream , The quenched steam flow is rectified in the rectification column 7 by the steam short contact time Preferably, it is combined with a cold steam stream, where the steam product is passed via line 56 And sent to a further downstream facility represented by 8. Feed stream to steam cracker C_FiveIf the stream is lighter than the stream, the two quenched streams are separated And downstream in a steam cracking facility. Such situation Is shown in FIG. 2, where C_FiveFrom a steam cracking feed lighter than the stream Quenched, vaporized and cracked stream of the rectifier 7 via line 54 It is sent to downstream steam cracking equipment. Line 54 is a compressor, contaminant scrubbing It should be understood that it can be supplied to one or more of the Must.   Short contact time process mode yields higher olefin yield from resid feedstock The following examples are provided to illustrate the importance ofExample   South Louisiana Vacuum R esidual) as a feedstock, short contact time fluid coking pilot equipment At a feed rate of 100 barrels / day. The operating temperature of the pilot device is 1 second 396 ° C. with a vapor residence time of less than 396 ° C. Evaluated conversion and product yield Are shown in Table I below.

────────────────────────────────────────────────── ─── Continuation of front page    (31) Priority claim number 60 / 026,416 (32) Priority date September 20, 1996 (September 20, 1996) (33) Priority country United States (US) (31) Priority claim number 60 / 026,427 (32) Priority date September 20, 1996 (September 20, 1996) (33) Priority country United States (US) (81) Designated countries EP (AT, BE, CH, DE, DK, ES, FI, FR, GB, GR, IE, IT, L U, MC, NL, PT, SE), EA (AM, AZ, BY) , KG, KZ, MD, RU, TJ, TM), AU, CA , CN, JP, SG (72) Inventor Jacobson, Mitchell             New Jersey, United States             07052, West Orange, Prospec             To Avenue 454 (72) Inventor Ludwig, Paul Kay             New Jersey, United States             07869, Randolph, Cottonwood de             Live 9 (72) Inventors Paijir, John F             New Jersey, United States             07950, Maurice Plains, Count             Leawood Drive 64 (72) Inventors Parish, Michael Earl             New Jersey, United States             07960, Morristown, Mills Street             Apartment 103, apartment 1 (72) Inventor Seymandy, Noel             Belgium, 1150 Brussels, Shoz             ー de Stockel 480 (72) Inventors Weissenberger, Hans Ay             Belgium, 3080 Turbulen, Rocca             ー Tran 6 (72) Inventor Chen, Tony Tea             Massachusetts, United States             02163-7803, Boston, HBI             Su Student Mail Center             233 (72) Inventor Davis, S Mark             77059, Texas, United States             Newton, Village Corner Dora             Eve 4410 (72) Inventor Lutzka, Philip A.             United States, Texas 77345, Ki             Ningwood, Wind Creek Dry             2010

Claims (1)

[Claims] 1. A process for producing an olefin from a resid feedstock comprising: (i) heating wherein a heat transfer solid containing carbonaceous deposits on a surface is received from a stripping zone and heated in the presence of an oxidizing gas. Zone, (ii) a vapor short contact time reaction zone containing a bed of fluidized solids consisting of heat transfer solids recycled from the heating zone, and (iii) solids with carbonaceous deposits on the surface sent from the reaction zone. A stripping zone wherein additional hydrocarbons and volatile components of lower boiling point are recovered with the stripping gas. a) feeding the resid feed to the steam short contact time reaction zone (where the resid feed contacts the fluidized heat transfer solids and catalyst components and the reaction zone is between about 670 ° C and about 670 ° C); 870 Operating under conditions in which the temperature of the solid and the residence time of the solid and the residence time of the vapor are independently controlled, the residence time of the vapor is less than about 2 seconds and the residence time of the solid is about 5 to about 60 seconds. Which results in a vaporized cut containing matter deposited on the solids and an olefinic product, which is characterized as a combustible carbonaceous metal-containing material); Separating the vaporized fraction from the solid; (c) quenching the vaporized fraction to a temperature low enough to stop conversion; (d) separating the separated solid into the stripping zone. Sending the stripped solids to the heating zone, where the solids are brought into contact with the stripping gas, thereby removing any residual volatiles from the solids; Operating temperature Heating to a temperature effective to lifting, and (f) the heated solid recycled from the heating region to the reaction region, where a method of solid supplies the heat of reaction, comprising, in contact with fresh feed. 2. The hydrocarbon feed boiling range of about C ₅ hydrocarbons having an average boiling point of up to about 545 ° C., (i) said feedstock is introduced to a steam cracking furnace, where the presence of water vapor was emitted vapor the feedstock (Ii) quenching the stream of vaporized and cracked product to a temperature low enough to stop the cracking reaction; and (iii) quenching the stream. Combining the quenched vapor stream from step (c) of claim 1 with a general downstream steam cracking selected from the group consisting of fractionation, compression, contaminant scrubbing, and olefin recovery. 2. The method of claim 1 further comprising converting to lower boiling products by combining in the facility. 3. The process of claim 1 or 2 further comprising separating an olefin-rich fraction from the quenched vaporized fraction from step (c). 4. The method of any of the preceding claims, wherein the short steam contact time reaction zone comprises a horizontal moving bed of fluidized heat transfer solids. 5. 5. The method according to any of the preceding claims, wherein the solids in the vapor short contact time reaction zone are fluidized with the aid of mechanical means and a fluidizing gas. 6. The method according to any of the preceding claims, wherein the mechanical means comprises a set of screws arranged horizontally inside the reactor. 7. The method of any one of claims 1 to 6, wherein the heat transfer solid is selected from the group consisting of petroleum coke from a delayed coking process, recycled coke, or an inert material such as sand. 8. The method according to claim 1, wherein the heat transfer solid comprises a catalytic component. 9. The catalyst component is a metal oxide selected from the group consisting of magnesium oxide, calcium oxide, manganese oxide, beryllium oxide, strontium oxide, cerium oxide, vanadium oxide, cesium oxide, and mixtures thereof. The method according to claim 8. Ten. The catalyst component is selected from the group consisting of refractory metal oxides, aluminates, zeolites, spent fluid catalytic cracking catalysts, vanadium-rich flue particulates, spent bauxite, and mixtures thereof. The method of claim 9. 11． The method of any one of claims 1 to 10, wherein the residence time of the vapor in the vapor short contact time reaction zone is less than about 1 second. 12． 11. The method of any one of claims 1 to 10, wherein the residence time of the vapor is less than about 0.5 seconds. 13. The method of any one of claims 1 to 10, wherein the residence time of the vapor is less than about 0.25 seconds. 14. 14. The method according to any one of claims 1 to 13, wherein the residence time of the solid in the vapor short contact time reaction zone is about 10 to 30 seconds. 15． The resid feedstock consists of vacuum resid, atmospheric resid, heavy and advanced petroleum crude, pitch, asphalt, bitumen, tar sands, shale oil, coal slurry, and coal liquefaction resid. 15. The method of any one of claims 1 to 14, wherein the method is selected from a group. 16． The method of any one of claims 1 to 14, wherein the resid feed is a vacuum distillation resid. 17． Sub-feeds selected from the group consisting of lubricating oil extract streams, deasphalted rock petrolatum, and heavy products from fluidized catalytic cracking, fluidized coking, and delayed coking boiling above 260 ° C. 17. The method according to any one of the preceding claims, wherein the method is added to a resid feedstock. 18． 18. The method according to any one of the preceding claims, wherein less than 50% by weight of the feed is the sub-feed. 19. The method according to claim 1, wherein the stripping gas is water vapor. 20. 20. The method according to any one of the preceding claims, wherein the fluidizing gas comprises hydrocarbons, gaseous, hydrogen, hydrogen sulphide, and added water vapor, usually in gaseous form. twenty one. The method of any one of claims 1 to 20, wherein the reaction zone is operated at a temperature from about 760C to about 790C. twenty two. 22. The method of any of the preceding claims, wherein steam is added to the resid feed at a rate of about 0.2 to 0.5 kg / kg of the sum of resid feed and sub-feed. twenty three. 23. The method according to any one of claims 1 to 22, wherein the fluidizing gas comprises a vaporized normally gaseous hydrocarbon, hydrogen, hydrogen sulfide, and water vapor.