JPS63500599A - Method and device for decomposing pot residual oil - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

[Detailed description of the invention] Method and device for decomposing pot residual oil In the known technology, the residual oil in the tank is classified as the residual oil in the tank, selected crude oil, normal pressure column bottom oil, normal pressure prefixed crude oil, vacuum distillation tank oil, etc. It is also known that residual oils, or simply oils, consist of large amounts of oil on the catalyst. Gasoline and low- and high-boiling carbonization by catalytic cracking due to coke deposits Achieving high yields of hydrogen fractions is considered difficult. more crude oil Metal impurities consisting of vanadium, nickel, copper, iron, etc. in the oil fraction are deposits on and/or into the pores of the catalyst, thereby further poisoning the used catalyst. and/or inactivated. In fact, in the known technology, 1 oil has 7 lacs of oil. The effect of the tendency to carbonate and the effect of heavy metals is that the recovery of the resulting products is important for the industrial economy. considered to be unacceptably large from a public standpoint.

For processing low-grade crude oil and its bottom fraction with such contaminants Considering the problems evident from the prior art, the remaining or least the separation of materials consisting of a number of components, or the preliminary conversion of the most undesired components. It has already been suggested that it be implemented. Extreme techniques to implement the desired separation, e.g. Vacuum distillation, solvent extraction, hydrogenation or certain thermal separation methods are useful for contaminant separation or control. Reliance was placed on known law.

Granules with little or no decomposition activity of undesirable components, especially metal components Adsorption onto materials was also used.

Pyrolysis and visbreaking operations such as grade and fluid coking are It was adopted to upgrade the residual oil left in the pot. However, it boiled over 4001. The resulting product contains a high degree of polycyclic compounds, making it difficult to perform fluid catalytic cracking. It turned out that it is not a particularly good feedstock for

obtained as atmospheric bottom product and/or vacuum distillation bottom product contained therein. The bottom oil, which consists of relatively high boiling point crude oil, is generally in the form of coke. Oil 1 East contains a large amount of components thought to have vertical orientation and heavy metal components. In this case, it is possible to consider i-fees that are difficult to process. For example, the residual oil in the pot is charcoal containing more than 0.6N%. Contains elementary residue, which generates a large amount of additional coke during cracking. and together with high metal levels act to rapidly deactivate the decomposition catalyst, It is believed in the industry that this will lead to undesirable soil accumulation. Therefore, the known technology There was a tendency to remove this material from the feedstock for fluid cracking.

Residues for purposes of this invention are from 400"F to over 1800"F of crude oil. Including printing material that boils to the maximum temperature. For this wide boiling point range raw material, approximately 400~ Light gas oil boils at 700″F, medium gas oil boils at about 600-850″F. heavy gas oil boiling between 600 and 1200”P, and over 1200’F. Components that boil up to the highest boiling point of crude oil, such as polycyclic aromatics and asphaltones. This includes longitudinal chordogenic components and metal impurities as well as all crude oils. Hydrogenation Separately produced materials, such as those obtained by solvent extraction of added raw materials, are also subject to this method. Included as a fee.

invention The present invention converts both the high and low boiling point components contained in the kettle residue into gasoline and light components. A simultaneous conversion method with high selectivity and low coke production for related. Past problems with recirculation equipment and high catalyst temperatures are eliminated by uninvented process concepts can almost be avoided.

In fact, the present invention facilitates high catalyst regeneration temperatures and utilizes this high temperature of the catalyst to achieve desired fractionation. The cracking reaction can be carried out without excessive coke formation in gasoline and pre-gasoline on a one-pass basis. The precursor is generated with a high conversion vehicle and high selectivity to the product. fluid contact Catalytic cracking involves distillation and solvent extraction up to the distillation range that can be instantaneously evaporated using high-temperature regenerated catalysts. It is carried out satisfactorily using raw materials which are oxidized by extraction and hydrogenation. High boiling point residue The actual decomposition of distillate hydrocarbon components hardly meets the desired results mainly due to the following facts. Didn't do it: Until now, the people who have laughed at it have found that instantaneous and complete atomization/evaporation is not the case with oils. , the first contact with very hot catalyst particles at a temperature above the tentative critical temperature of the feedstock residual oil. could only forcefully assess that success is possible only if achieved by . This is because the boiling point range of the raw gas oil increases due to the inclusions of the residual oil in the kettle, and This means that the medium temperature must also rise. Known technology can recognize this concept. Not only did they ignore this fact, but they also calculated the required height based on the following two factors. This method was intentionally suppressed from achieving high catalyst temperatures: (1) Metallurgical limitations of regeneration equipment; (2) Thermal stability of the catalyst.

Currently available fluidized cracking methods are therefore limited by the maximum operating temperature of regeneration and the resulting regeneration. Catalyst temperatures of up to 1500 and 1600"74' have been widely disclosed. However, it is recognized that the There is a tendency to In fact, a temperature limit of 1300-1400'F is therefore necessary. , to achieve the desired conversion level of feedstock to be charged to the catalytic cracker, 1025”F Solvent-extracted and hydrogenated #resist gas separated from kettle residual oil boiling over ’ The amount is limited to 100% oil raw material.

In particular, at least 1800" without unduly impairing the catalytic activity The use of equipment that allows the temperature to spread up to F. Targeting technology. Non-inventive survives severe temperature manipulations contemplated by non-inventive It also shows the location of the equipment or equipment that will be used.

Thus, for example, as obtained by atmospheric prefixed crude oil from about 400'F and above, Achieving high conversion of raw oil from undistilled fraction of crude oil that boils up to the maximum crude oil distillation temperature Comparable to known gas oil cracking conditions, including comparable coke generation. low-boiling materials including gasoline and light hydrocarbons, with possible gasoline collection results. can form a fee. Distillation, solvent extraction, hydrogenation or various thermal processes The need for expensive raw material purification or preparation techniques and equipment in the form of 51C can thus be avoided. Ru.

The products produced from the process of the present invention are widely used as fluid catalytic converters of relatively clean gas oils. It is similar to what can be obtained from solution work. That is, light gases below 02, C3 and Maximum distillation temperature from C4 olefins and paraffins, C5 4.30'F' A boiling gasoline and a cracked salmon and l-cycle oil are obtained. light and 1 cycle oil or decanted oil The cracked cycle oil or gas oil obtained in this way is known as a low sulfur fuel oil. It is then hydrogenated for sale and slowly converted into gasoline. It can be hydrogenated and returned to the fluid catalytic cracker, or in particular Part of the product is of such quality that it can be completely hydrogenated and cracked to produce gasoline boiling components. It is something.

Hydrocracking the cracked cycle oil obtained as above to form gasoline. As a result of the combination with the catalytic alkylation of C4 and C4, the 4 up to 125% gasoline and 3-4 per barrel of crude oil residue above 00°lF1 % propane is obtained. This entire series of treatments If no energy is taken out for other uses, the energy balance is balanced. energy -The income and expenditures include those necessary for crude oil atmospheric distillation work.

A very important parameter for the success of kettle residue cracking is the relationship between the fluidized catalyst particles and the feedstock heavy oil. The purpose is to ensure that a very complete and intimate flood evaporation contact is achieved. i.e. The feedstock, particularly the high molecular weight components, undergoes near-complete contact almost immediately with the high-temperature catalyst particles. The conversion operation is improved by achieving atomization/evaporation. Remaining height of raw materials The point component is a high-temperature regenerated catalyst with a temperature exceeding the tentative critical temperature of the raw material, along with a low-boiling point gas oil component. Upon contact, it is almost completely evaporated. It allows the atomization and evaporation of raw material components to be more complete. It is only by achieving this that many raw materials can be more completely converted into gasoline-producing components. This is because it can be decomposed into What does not evaporate remains almost unconverted; As a result of the contact cycle, significant amounts of oil are generated and/or adsorbed onto the hot catalyst surface. K, is particularly susceptible to conversion to coke, thereby causing losses in gasoline yield and catalytic loss. A rapid decline in medium activity is noted. Mixing of feedstock and catalyst to achieve the highest desired conversion The combined temperature is at least equal to the tentative critical temperature of the charged raw material pot residual oil, especially at this temperature. , but not so high as to cause undesired over-decomposition.

The raw material preheating temperature, the temperature of high-temperature regenerated catalyst particles, the decomposition activity of the catalyst, and the the amount of diluent such as water vapor, the residence time and unit of hydrocarbon vapor in contact with the catalyst. Knit working pressure is a key operating variable that is readily available to oil refiners. , thereby providing the reaction conditions necessary to achieve almost complete evaporation of the raw materials. Hydrogenated or Gasoline combined with the production of quality heavy cycle oil suitable for hydrocracking Highly selective conversion to carbon and light hydrocarbons is achieved.

Additional desired working parameters can be achieved through well-designed and arranged feed injection nozzles. The purpose is to obtain an equilibrium temperature approximately in the Ripe cross section. at the exit Raw material discharge rate in the range of 10 to 1300 ft/sec, especially 300 to 500 ft /θθC or more is particularly desirable, and the jet is applied to a circle with at least the same area as the cross section of lie + j'. A feed nozzle outlet is provided which is rigidly arranged relative to the live cross-section. each supply The nozzle is used for coking all the raw material hydrocarbons charged through the nozzle tube. A water vapor jacket may or may not be provided, if desired, to reduce this. water Steam or other suitable diluting material can be used to add up to about 71% diluent to the raw pot residue. are injected together, and their equilibrium flood temperature is lowered to yield the best result for a given nozzle design. A high oil channeling effect is achieved. Typical feedstock oil dispersion steam or diluent ratio is ranging from 1 to 151 lid% of

The above factors regarding contact and mixing of the atomized feedstock and fluidized catalyst particles are Accelerate the compound relatively uniformly and rapidly through the live evaporation zone within a minimal time frame. catalytic slippage, thereby ensuring very little catalyst slippage, if any. and therefore promotes rapid heat transfer from the high temperature catalyst to the atomized heavy feedstock, Localized increases in the catalyst-to-oil ratio exhibited by dense catalyst phase conditions are prevented. i.e. The condition is such that the live evaporation zone is opposed to the locally busy phase contact condition within the rise. selected to ensure lean phase contact between the catalyst and the feedstock at and downstream of the catalyst. .

A typical example is Fi raw material Boutouliangyu 17i1 [containing 1-12% hydrogen in its molecular structure.

The light fraction is generally richer in hydrogen than the lighter fraction. generally large The molecular structure is thought to be low in hydrogen. The light fraction rich in hydrogen is relatively hot. Stable but relatively easy to use with special catalyst compositions such as zeolite-containing catalysts It is catalytically cracked. The high molecular weight or hydrogen-poor fraction of the feedstock is Considered thermally unstable and in contact with solids at temperatures in the range of 1000-1800''F. It is easily thermally decomposed during heating. In fact, the instantaneous complete evaporation of the first fraction is a small amount. Promote simultaneous thermal decomposition of high molecular weight components including asphaltenes. High gasoline and cycle oil yields with mostly low coke and gas evolution This ultimately leads to a satisfactory transformation.

Mechanism of sufficiently high catalyst temperature, low hydrocarbon partial pressure and atomized feedstock oil nozzle injection system. Through use, the heavy components of the raw buckwheat residue are almost instantaneously removed when they come into contact with the fluidized catalyst particles. Complete atomization/evaporation is achieved by avoiding localized decomposition of the dense phase and avoiding large aspirate particles. Promotes the desired thermal decomposition of some of the phalt-forming constituents and achieves low boiling temperatures without coking. Based on forming cru oil. If the above is not achieved, the phenomenon of coke closure @' lives there. This is due to hydrogen-poor heavy molecules depositing in the active decomposition zone of the catalyst and closing the pores. chain and transfer the feedstock from the light and/or heavy components of the feedstock to the desired product. It is a phenomenon that makes the catalyst relatively thermally stable during a long active life that allows for conversion of Ru.

In the design and operation of a unit of said type according to the invention, one essential basis for operation is As a general consideration, the temperature of the fluidized catalyst regeneration operation should be at least about 1800"F'. , carbon combustion should not be inherently limited until the Raw material preheating temperature, Ripe temperature If the feedstock injection and distribution method is specific to the hydrocarbon partial pressure, However, each of these is bound by practical constraints; The temperature of the 118 media regenerator is optimized for specific feedstock oil composition requirements. must be unlimited in terms of carbon combustion so that it can rise to levels suitable for This enables catalytic cracking and simultaneous thermal cracking of large, less stable molecular structures in raw materials. It should be noted that the desired instantaneous atomization-evaporation contact with the catalyst particles promoting Must be.

Table 1 shows how to limit the temperature of the regenerator for decomposition of special atmospheric pressure pot residual oil without any regeneration temperature limit. shows the effectiveness of gasoline and coke generation compared to cracking. These tasks are Vacuum prefixing and known conditions of the resulting gas oil for removing asphalt-forming components The lower fraction kK is then compared to the cracking of gas oil obtained from the same crude oil.

Table 1 shows that when the regenerator or catalyst temperature is limited during the process of cracking residual oil in the kettle, the amount of gasoline recovered is shows a significant decrease in coke generation and a corresponding increase in coke generation. Remains of pot The oil has a high gasoline yield and a coke production comparable to that obtained from conventional gas oil feedstocks. It must also be pointed out that it can be decomposed while alive.

Table 2 shows gas oil cracking data for the same feedstock gas oil at 10 volume% and 20 volume f%. The same factor is shown to be stronger by comparing it with that of JE with still residual oil added. will be adjusted. This table shows that under optimal conditions the presence of residual oil in the kettle will result in a brighter overall conversion and a higher gun level. Coke generation with the same or slightly lower phosphorus yield and enrichment than oil cracking is achieved. Show what will be done.

Table 1 Effect of regenerator temperature restriction and comparison of normal pressure bottom oil and gas oil only Normal pressure bottom oil, gas oil only Playback device temperature: High, low, normal use Gasoline straw capacity t%: 67.7 63.5 61.5 Cox weight% 5.3 8.0 6.1 Table 2 Well-known soot oil decomposition vs. kettle residual oil decomposition Gentle conversion work Conversion capacity % 66.0 71.0 79.0 Ganlin yield capacity % 59.8 6 1.8 66.1 cox l child% 3.0 3.6 5.6 Optimal conversion work east Conversion capacity % 76.5 77 79.5 Gasoline yield volume f% 61.5 67. 4　67.7Cover %　6.1　4.3　5.3 Total normal pressure bottom oil was separated into coke. The analysis of the products produced during the process is of interest when comparing only gas oil from the same crude oil. Properties revealed: (1) The generated liquid product has a high average hydrogen at.

(2) The research octane of gasoline is significantly higher.

(3) The motor octane of gasoline is significantly higher; As a result, a significantly improved t'L-(R0M)/2 ratio was obtained for unleaded gasoline. Ru.

(4) Cracked gas oil raw material, commonly referred to as light and heavy cycle oil or decant oil. The compounds are significantly more sensitive to di- and tri-fused aromatics than to 4-, 5-, and 6-fused aromatic ring compounds. abundant. The high concentration of 2- and 3-ring fused aromatics in the decomposition products makes these raw materials gas making it a highly desirable feedstock for hydrogenolysis to phosphorus.

(5) The coke generated under optimal working conditions has a very low hydrogen content. known gas Hydrogen levels in the range of 3-6xf% for 8-10xf% obtained in oil cracking operations. be measured. The low hydrogen level in the generated coke is due to the working conditions used on the catalyst surface. promotes the coupling of polycyclic compounds attracted to 1~, thereby generating a significant amount of additional hydrogen used in hydrogen transfer reactions to obtain liquid products with high hydrogen content, where release of It can only be explained by the fact that

This phenomenon is not observed in current gas-oil spectroscopy. These reactions are exothermic, so - This is significantly offset by the endothermic reaction heat of the -order decomposition reaction. As a result, the overall reaction heat is 40~ 50% decrease. This results in a lower catalyst circulation rate, which in turn contributes to lower coke generation. stand. Even low hydrogen levels in coke can be regenerated using the means embodied in the present invention. If so, there are seven main actors to consider.

with or having a catalytically active crystalline aluminosilicate or crystalline zeolite It consists of one of alumina or magnesia, especially about 20 to 20 Cl.

Highly siliceous catalysts with fluidizable particle sizes in the range of and the levels of metal contaminants concentrated in the cracking rows vary considerably. metal on catalyst If deposits of Continuous or semi-continuous catalyst replenishment and removal of contaminated catalyst to maintain deactivation. Removal or disposal may be considered. Storage type m is used after long-term work or The most suitable method for achieving the desired transformation of raw materials according to changes in raw material composition so that they can be replaced almost completely or partially as changing conditions demand. can.

Money! per gram was recognized as a major obstacle to long-open can residue decomposition. But these metals Contaminants are passivated to a significant extent at high regeneration temperatures and their negative effects are It is clear that even if coke is maintained below approximately o, osiiit%, it decreases steadily. Or it becomes. In addition to the expected coke-induced inertization, metal contamination causes regeneration. It has become clear that there is a conversion loss of approximately 5% per 0.11% of coke on the catalyst. Ta. However, in the case of the occipital crude oil cracking operation according to the present invention, nickel, vanadium and Metals such as iron have beneficial properties such as dehydrogenation, activating or promoting hydrogen transfer reactions. It exhibits a Low coke on the medium is achieved. On the contrary, sodium and all alkalis Metals are particularly sensitive to zeolite-containing catalysts (7), which are considered highly pollutants. Ru. In this way, raw material desalination is a 1-ndashink'scaven solution to solve the sodium problem. This is a much more economical option than using it manually. From suitable desalination of raw materials, The sodium content of the former can be controlled to be sufficiently lower than 1 ppm.

Desired high catalytic temperature required for proper and satisfactory decomposition of oil consisting of pot residue % specifically designed and employed in conjunction with special equipment or work equipment to achieve Special regeneration techniques are required. The high temperature decomposition pressure of the present invention is the target where the catalyst is exposed to the feedstock oil. , promotes the deposition of relatively high levels of coke or hydrocarbonaceous material on the am proceed. Levels usually exceed 11t%, and in some cases exceed 2λfir%. . However, if the catalyst is IJ, the carbon level is less than 10% by weight, preferably at least 0. It is particularly desirable to regenerate the amount of 0.05 to approximately 0.02% by weight. Gas oil current minutes The regeneration methods and equipment or facilities used for decomposition are necessary for kettle residual oil decomposition for the following reasons: It is unsuitable for achieving serious catalyst regeneration: (1) formed on the catalyst; High coke levels are promoted by low catalyst circulation ratios, i.e. low catalyst-to-oil ratios. It will be done. Automatically high regeneration temperatures due to the combination of low catalyst-to-oil ratio and high carbon levels is born. Temperatures are used in the design of current regenerators, cyclone systems, and catalyst collection systems. This temperature exceeds the normal limits imposed on the stainless steel used. expected temperature The temperature also exceeds the current temperature limit of about 1400'F for current power recovery systems.

(2) Highly active catalysts currently used in catalytic cracking undergo this severe regeneration in the Koichi process. or when multiple steps are included in one volume even in a multi-stage regeneration device, non-invention The structure is not thermally stable at high regeneration temperatures. Two very fundamental factors Affects catalyst stability during regeneration. Coke level on spent catalyst becomes higher and higher Increasingly, even using multi-step single container recycling, high levels of CO2 can be achieved within a single container. As the gas burns, a progressively higher catalyst particle temperature occurs. This high surface temperature The body deactivates the catalyst. Second, the catalyst is molecular hydrogen that is entrained during coke combustion. If water vapor formed from the highest temperature IIe can remain in contact with the medium, It is rapidly inactivated at that high temperature.

Special embodiments of the invention are designed with special means to overcome the difficulties of known catalyst regeneration. A two-valley system consists of a two-step catalyst fluidization thread that is used to measure and work the spent catalyst. The medium will be regenerated. Undesirable metallurgical limitations or is applied on the circulating catalyst without exceeding the thermal stability of the catalyst, especially from 0.02 wt. Low coke levels are achieved.

The catalytic cracking process of the present invention produces gasoline, low- and high-boiling hydrocarbon components; Low oil, commonly referred to as kettle residue, obtained from crude oil, shale oil and tar sands. Pertains to the cracking of high-boiling hydrocarbons that boil at 400"F or higher. Residue from the feedstock is recovered from the regeneration zone at a temperature above the feedstock low critical temperature. The active fractionated catalyst is mixed in a live reaction zone. Temperatures greater than approximately 400′″F The feedstock expanded hydrogen forms a highly oxidized, nearly vaporous hydrocarbon-catalyst suspension. under conditions, the feedstock is mixed with a high temperature regenerated catalyst at a temperature at least equal to the feedstock low critical temperature. . Mffi body separator or dispensing vaporized material to catalyst used at the reactor exit. About 70-90% of the The unique features of the special turbidity separator used are Relatively high vapor surface velocities are obtained during separation from the catalyst solids in a separate container. The steam then enters a reactor cyclone to further separate the entrained catalyst solids. Ru. Hydrocarbons leaving the reactor cyclone are separated in a downstream fractionation column. Rise decomposition Spent catalyst particles recovered from confectionery are steamed at high temperatures in the range of approximately 900-1100"F'. tripped, coke 1.0 to about 2.5: [+-% or more inert carbon Has quality residue. S) IJ Tsude Touch H: Approximately 1500″IP, 4 and Shinto After a temperature limited first catalyst regeneration zone maintained at a temperature not exceeding approximately 1400” F. It is sent to a dense first catalyst stream J-. Temperature limitation of catalyst regeneration [also carried out in the first step] The combustion of hydrocarbonaceous material in the Burning at a relatively mild temperature sufficient to burn approximately 10-80% of the total carbon in the instep It is. The temperature of the regenerator is within the range of 1150 to 1500”F, with hot water of the catalyst in the layer phase. Limited to temperatures that do not exceed the metallurgical limits of stability or conventional low temperature reconstitution operations.

The CO-rich flue gas is recovered from the first stage regenerator, and the resulting CO is sent to a CO boiler to generate steam by promoting complete combustion. It will be done. Can be sent via a power recovery prime mover before being sent to the exhaust gas CO boiler . The limited mild catalyst regeneration regime is due to the presence of water vapor formed during hydrogen combustion. Helps limit local hot spots on the catalyst and the water vapor formed The temperature is not such that the catalytic activity is significantly reduced. At limited temperature with carbon immersion The partially regenerated catalyst, containing mostly hydrogen, is recovered from the first Kashu unit.

Catalysts with residual carbon from which hydrogen has been removed are subjected to a second catalyst regeneration process at high temperatures without uniformity. Delivered to the east, where the TA carbon is almost completely burned to CO3, with 140 Achieved in an atmosphere that does not contain high pffi medium temperature resistance ranging from 0 to approximately 1800”F. will be accomplished.

High temperature W? , a separate second step consisting of a mortar storage device stores the catalyst and the catalytic converter at high temperature. more preferably about 0.05 mt% on the circulated hot catalyst particles to limit medium retention. is about 0.023E! % to enable carbon burn rates to achieve carbon residuals lower than It can be designed.

Catalyst regeneration equipment of conventional design used in fluid catalytic cracking operations of the prior art is capable of satisfying the method. It contains a variety of internal components that are of particular concern to demanding work demands. These are usually catalyst processing losses. Multi-stage cyclone designed to limit loss of catalyst from cyclone to catalyst bed Includes a return conduit (dip leg), various supports and place members for the inscription housing.

Hoppers or similar devices and conduits and A return path to the disassembly step of the method is attached. In the case of known yarns, these various devices are necessary. of metal construction, usually stainless steel construction, and is directly exposed to the combustion temperature of the regenerator. be done. BE reburning to limit the maximum temperature that can be entrained or maintained during catalyst regeneration. It is the presence of equipment that exposes these metals in the burn zone.

Generally it is above legal working temperature by K 1400”F or #’11500’F is born.

According to an embodiment of the separate second step high temperature 1@media regeneration device according to the invention, the cyclo The outside of the tank, dip leg, take-off hopper or pool as well as the combustion tank, in practice the recycler. Said limitations due to the placement of all metal exposed devices such as support threads external to the raw device itself Problems related to hair removal.

The regeneration vessel, said internal cavity of the catalytic combustion zone, has all connecting conduits, external Fireproof lined as well as long and immersed legs. Setting up such a playback device combination The method is considered to be a significant improvement over all known techniques. at the desired high temperature The regenerated catalyst is transferred from the relatively dense fluidized catalyst bed in the second stage regenerator to the outside of the regenerator. It is taken out by a specialist in charge of taking out. The removed catalyst is heated to the desired high evaporation temperature and A sufficient amount to evaporate residual hydrocarbons in the charged feedstock according to the method of operation of the invention. It is then introduced into a stripping zone before being sent to the live reactor. 2nd playback The high-temperature exhaust gas obtained from the equipment is passed through an external cyclone to collect the fine catalysts. for example by passing it to a waste heat recovery system and an expansion turbine. further utilized or released into the atmosphere. Cyclone in the second regeneration process with the highest temperature Due to the fact that is located externally, significant advantages in addition to those mentioned above are obtained. sa When the Iklon separation can is moved from the inside of the catalyst regeneration device to the outside, the cyclone separation can actually As the diameter and/or length of the separation device increases, its separation efficiency improves. , a single-stage cyclone separator can be used instead of a two-stage cyclone separator. However, improved separation efficiency is still achieved. This is a straight cylindrical pipe or exhaust gas A support is placed on the outside of the transition pipe or cyclone to approximately match the curvature of the cyclone. Close to Ikron? -m was achieved by using the curved part connecting in the 1M direction. Ru. This curved exhaust gas transfer conduit device allows the transfer of the tIX particle suspension into the hot exhaust gas. Initial centrifugal motion is induced, which initiates the concentration of entrained particles and the separation of gases and solids. This promotes significantly improved cyclone separation efficiency between the cyclone/design significant changes are possible. Furthermore, extremely advantageous use of external cyclones An important factor is Since there is no need to adapt the cyclone to the outside, the total length of the cyclone can be increased and the The purpose of this invention is to significantly improve the ion separation efficiency. The exhaust gas transfer conduit and cycle The net effect of the Ron device is that the 1st stage external Zyclone and the 2nd stage internal Zyclone This means that it can be operated in the same way as a separate separation system. Externally placed fire-resistant lined cylinder Chron is a regenerator that operates at temperatures above 140C1'F and up to 1800'F. It can be manufactured from carbon steel even when used in other applications. Furthermore, the external cyclone Monitored with an infrared camera during use and relatively easy to replace before stopping or changing rapidly can be repaired.

The kettle residual oil decomposition method of the present invention is compared to the conventional Fea method that processes relatively clean feedstock gas oil. and have a high boiling point residual fraction of feedstock boiling above 1000''F. gas oil y A working environment that is thermally harmless to the catalysts used in the process compared to what appears in CC confectionery. Since it is possible to achieve this at the same time as attaining the boundaries, it is thought that there will be significant progress. Place of the invention The desired final high temperature catalytic regeneration operation is in barrel bottoms or other heavy polymer reservoirs such as crude oil, shale oil, etc. Many of the liquid hydrocarbonaceous materials are catalyzed with 51C to form low-boiling materials, including gasoline. Near instantaneous atomization/evaporation of heavy kettle bottom feedstock components due to substantial conversion by medium It is necessary to achieve the following. This is considered a major advance in the petroleum N manufacturing industry, and Reduce the dependence of the world's walls on imported crude oil. Low-grade crude oil obtained at low cost processing becomes possible.

An additional advantage derived from the kettle residue cracking process of the present invention is that Achieve reduced energy consumption and reduced air and water pollution. Regarding things. Some of these savings come from vacuum distillation units, asphalt extraction units. types such as silage caulking, thermal visbreaking etc. This is achieved by discontinuing each heat treatment. These other known methods generally use atmospheric pressure pot residual oil. is used for further processing.

Typical energy savings from vacuum unit removal in crude oil unit operations are charging It is about 0.6-1.0% by volume of crude oil. The method of removing the chopsticks is accompanied by an empty Air and water pollution is also avoided.

Another important advantage of the inventive kettle residue cracking operation is that there is no separate chemical hydrogenation process. In this case, approximately 60-70% sulfur removal is achieved. Shaped by disassembly work The H2S produced is removed from the vaporous hydrocarbons by amine scrubbing and the elemental The sulfur is sent to the Claus device for sulfur recovery, and almost all of it is released as 802 using the regenerative combustion method. Unlike publishing, it can be published as elemental sulfur.

Live cracking with multiple feedstock hydrocarbon inlet devices, especially for the conversion of digested pot residue hydrocarbons A number of different equipment configurations consisting of zones are carried out to ensure sufficient contact and flow with the fluidized catalyst particles. and before discharge to a separation zone with or without a relatively shallow, compact fluidized catalyst bed. It will be clear to those skilled in the art that the desired short contact times within the riser contact zone can be achieved. It is clear. Separation of hydrocarbon products from the catalyst discharged from the live is by mechanical means or facilitated by any device suitable for this purpose disclosed in the known art. I can do it. But in all of these hydrocarbon conversion equipment there used Catalyst regeneration is very effectively achieved using the sequential regeneration method of the present invention. So Therefore, all regeneration concepts and working methods designed and determined in particular according to the invention are It is used with the advantage of a fairly quick response in catalytic cracking operations.

Figure 1 shows a two-step catalyst regeneration operation adjacent to and combined with a live hydrocarbon conversion operation. FIG. Catalyst collection and recovery of restricted cylindrical dimensions centered around the live exit The collection zone expands horizontally apocryphally from the riser reactor outlet and extends from the fruit thinning container. Includes an upper cyclone separator kK adjacent catalyst-steam separator nothing.

Figure 2 shows a comparison of the same size with ILt placed outside the vessel for the second step of high-temperature catalyst regeneration. Parallel connection that realizes a stacked arrangement of two-step P6 medium reconstitution that complements the high cyclone separator. FIG. 2 is a schematic elevational view of the Asahi separation-catalyst regeneration operation.

Water in one arrangement of the 7th power separator at the riser outlet of the 3rd b + 1st and 2nd stage It has a horizontal cross-sectional height.

Figure 4 is a live version of Figures 1 and 2 showing details of the multi-nozzle raw material inlet device. Figure 1 is a detail #1 view of the lower part of the hydrocarbon conversion line.

Figure 5 is a graphical representation of the conversion achieved with two different threads of feedstock atomization. . Yarn 2 uses raw materials that have been atomized more highly than Yarn 1 or the first system.

Figure 6 shows the regenerated catalyst inlet conduit, fluidizing gas inlet conduit and highly refined raw material. A lamp with a nozzle device that forms feedstock oil and then discharges it into the live at a relatively high speed. Figure 3 is a schematic elevational view of the bottom of the Eve decomposition zone.

Description of special embodiments In the treatment method described below, the arrangement t1t of the equipment is a material with a convex boiling range of gasoline. and hydrocarbon materials that are easily converted into gasoline boiling components and fuel oil. In order to do this, it is equipped to carry out relatively high temperature catalytic cracking of the kettle residue. This way The regeneration of cracking catalysts used in The first regeneration zone in Separate 1b is maintained under temperature-limited conditions to remove the hydrogen produced. In particular, the two-step catalyst is used in actual production. CO shadow shape in the first regeneration zone The deactivation of the catalyst by water vapor, which is not pressure limited and is formed during hydrogen combustion operations, is maintained at the desired low level.

The hydrogen-free residual class is then exposed to further elevated temperatures and residual carbon deposition on the catalyst. The temperature is sufficiently high to prevent the formation of significant amounts of Co or water vapor during the combustion process. Partially regenerated catalyst in a second, separate, relatively dense fluidized catalyst system at low oxygen concentrations removed from The catalyst regeneration temperature in the second step is high enough to obtain the desired oil contact temperature. It can rise very high. Generally, the temperature range for regenerated catalysts is about 1400'P to 18 00″F+. The regeneration exhaust gas of the second stage regeneration operation is therefore completely Co-free. Even if it does not contain Co, it is almost free of Co. The exhaust gas from the second stage of regeneration east is enriched with CO2. Such CO2-rich gas is then used as a catalyst for steam generation and between steps of the process). It can be used for IJ pipping and other uses of such gases if desired. , or may not be used. Approximately 0.203N on the catalyst! lower than %, especially 0 ．． Such regenerated fibers with residual carbon lower than O5mm-% are subjected to decomposition work. recycled to

The treatment method of the present invention reduces the deactivation of catalysts due to high temperature steam, and energy conservation tF:, ti!t, which is particularly desired in scarcity conditions is clear to those skilled in the art. In other words, the two-step recycling process of the present invention produces complete coke. For one-step regeneration while achieving removal and heating of catalyst particles to the desired high temperature This reduces the need for air blowers. Limited relatively low-temperature regeneration in the first step The process is not limited to CO shadow formation, usually water vapor is formed, and the second step high temperature regeneration operation is The remainder of the total carbon initially deposited on the catalyst is carried out in the absence of water vapor formed. only are removed. These energy conserving working conditions are based on the water vapor used in the method. A small Co boiler is used to process the amount of exhaust gas obtained from the first working process. This is a significant economic advantage for disassembly operations. Separate second regeneration step The very high temperature CO2 exhaust gas that does not contain a significant amount of combustion retained CO recovered from It is cooled in a suitable device or heat exchanger can with additional steam release.

According to the kettle residual oil processing apparatus of the present invention, the normal pressure kettle residual oil of crude oil is further charged into the cracking process. Vacuum distillation, de-asphalting, and Schiller coke with high energy costs processing and other forms of raw material preparation that require large amounts of energy are eliminated. Important energy conservation: 11! will be accomplished. Generated by exhaust gas enriched with the above CO. The steam produced and/or the usually gaseous hydrocarbons obtained in the process are It can be used as a diluent to improve the oxidation of raw materials that come into contact with high temperature regenerated catalysts. can.

The high-temperature catalyst particles obtained as described above are charged to the separation operation using a known method @summer limited 1 operation. The desired high temperature is higher than normally obtained in the production process. Furthermore, this catalyst It is obtained without causing water vapor and (also Fi) hydrothermal degradation to the medium. Sara The sequential regeneration of the present invention involves the desired evaporative and endothermic catalytic conversion of the pot resid hydrogen feedstock. It also provides a large amount of heat economically. Other energy conservation benefits include 1025″ Residue from crude oil, which consists of difficult-to-process components of crude oil with a boiling point exceeding Asphalt, visbreaking, silage coking, hydrogen enrichment work for raw materials, etc. High-efficiency, high-efficiency By eliminating energy-consuming operations, products in the gasoline boiling range and pre-gasoline This is achieved due to the fact that the precursor is processed to the desired low-boiling product.

With the treatment method combination of the present invention, the circulating catalyst in the system can be used, for example, as a new catalyst or Catalysts with low metal loading obtained as equilibrium catalysts from cracking operations of other clean feedstocks It is considered to maintain the desired equilibrium catalyst in the system by replacing particles with fIt. be done. In this way, the first step of low-temperature regeneration work or the second step of high-temperature regeneration work or Some of the catalyst particles separated from both or as normal catalyst loss or special removal. The device has moderately high decomposition activity and low levels of deposited metal contaminants. Can be replaced with new catalyst particles.

The working concept of the present invention is useful in designing basal filaments and is useful for live disassembly or dense One-step regeneration operations can be achieved by combining hydrocarbon conversion operations such as fluidized bed cracking operations. The existing various refining operations are busy. In any of these operations High temperature for decomposition catalyst due to energy conservation and presence of water vapor formed To achieve the advantages of the present invention with respect to the elimination of hot water loss, the regeneration temperature must be low @ first It is desirable to limit the process to a second, separate high temperature regeneration operation.

The sequential catalyst regeneration concept of the present invention allows the hydrocarbons charged to the cracking operation to be contains altoic components and metal contaminants, or only contains significant amounts of metal contaminants and ( or) whether the asphalton is a disproportionately high coking charge material It is immediately clear that almost all hydrocarbon conversion methods, regardless of the be. However, as mentioned above, the advantage of the innovative treatment method of the present invention is that the hydrocarbon feedstock The method is significantly improved as additional processing to remove these materials is reduced. Is Rukoto.

Furthermore, existing temperature-limited contact and regeneration equipment can be replaced with extremely low investment capital and A stacked single step reactor is used to achieve unbeatable high temperature operation in a timely and timely manner. Reactor regeneration equipment, modernized side-by-side single-step reaction waste regeneration equipment or upper Rise reactor charcoal in combination with a dense catalyst bed communicating with a live catalyst regeneration operation Whether it is one of the more modern units consisting of a hydrogen conversion zone or not. O that can be modernized According to the example in Figure 1, the coal recovered from the IJ pinning operation (residual hydrocarbon conversion process) The spent catalyst particles with hydrohydride deposits were placed in a regeneration vessel 5 via conduit 1. The catalyst is sent to a dense first fluidized bed 3. The recycling container 5 is a relatively low temperature recycling container. and the temperature is maintained below about 1500'11i', conduit 1 and distributor 9, the concentration of oxygen introduced by the regeneration gas immediately increases the hydrogen and pot residue decomposition. Re-HE temperature generated during combustion or incineration of 5R elemental sediments associated with hydrocarbonaceous sediments In order to limit the degree as desired, it is limited. The first step was carried out in the East The combustion is carried out under conditions which form a repopulated exhaust gas rich in water vapor and CO. child The exhaust gas generated as shown in FIG. Passed through a separator to separate the entrained catalyst particles therefrom and then drawn through conduit 15. It gets pulled out. The catalyst thus separated from the CO-rich exhaust gas by a cyclone is It is returned to the catalyst bed by suitable dip legs.

For the 5 yen regeneration container, the regeneration conditions are particularly limited in terms of catalyst or carbonaceous deposit removal. is not regenerated and therefore sufficient residual carbon remains on the catalyst to remove the oxygen-containing regeneration gas of the supercharge When more completely removed by combustion with Higher catalyst particle temperatures in excess of 500''F' are selected to be achieved.

According to the arrangement shown in Figure 1, the first step of catalyst regeneration, which is carried out with a valley profit of 5 yen, is approximately 14 yen. It is a relatively low temperature operation limited to no more than 00'F or approximately 1500"F. and CO-rich exhaust gas is generated. There is hydrogen present that forms significant amounts of water vapor. The partially regenerated catalyst that is not used is sent to the adjacent IJ pump zone or vessel 19. It is extracted from the catalyst layer in the first regeneration step through the extraction groove '1f17.

A relatively compact fluid material flowing downwardly through the partially regenerated catalyst is introduced by conduit 21. The venting and stripping gases flow through the vessel 19 countercurrently to the venting and stripping gases. ventilation gas In particular, a relatively inert material with respect to deactivating at least a partially regenerated catalyst. and especially at temperatures above 1500'F when the moisture-forming components along with the catalyst This considerably limits the transition to the second stage of catalyst regeneration that takes place. zone Suitable venting gases for use in 19 are Co2, mostly water-free exhaust gases. , nitrogen, dry air and combinations thereof.

The partially regenerated catalyst is connected to a vertical conduit 23 that communicates with a catalyst transfer conduit 25 and a bean draining conduit 27. It is taken out from the container 19 by. such as air, nitrogen, CO□ and their mixtures. Such gases may be added via inlet conduits 29 and 31 to aid in catalyst transport. Can be done. A number of gas conduits represented by conduit 29 are connected to conduits 23 and 25. Bent conduit between and its downstream transport conduit! [Arranged to aid catalyst transport] Can be done. Air or oxygen-enriched gas steam can be used as a partially regenerated catalyst with 4 rising tubes for 27 yen. It is introduced by conduit 31 for contact. Conduit 27 has a relatively large diameter Exiting to a catalyst bed 33 held in the lower part of the zone or vessel 35. ethereal addition The regeneration gas is supplied by a conduit 37 communicating with an air distribution system suitable for the high temperature operations occurring. and introduced into the lower part of the catalyst layer 33.

In the case of second step regeneration, which is carried out in the regeneration container 35, the temperature is removed in the first step. 1, which is sufficiently higher than the first stage of regeneration to almost completely remove residual carbon within the range of 400°F1 to 1800″F+. It is a refractory-lined container and cyclone that has almost no circular surface. The desired high temperature regeneration can be carried out. This high-temperature operation removes residual carbon on the catalyst. 0.05i! % and the hot CO□ exhaust gas stream is passed through the outer cyclone. Collected by separator. It is a relatively large container that has been fireproofed for 2 innings. Single stage cyclone separation profit is used. That is, the outer solenum portion 39 is a radial aperture. from which cyclone separators are connected to cyclones 45 and 47, respectively. Suspended or arranged as shown by connecting arms 41 and 43 . On the other hand, it is possible to adopt the cyclone arrangement shown in FIG. You can do something like that. Catalysts separated from exhaust gas at high temperatures up to 1800"F are prepared. It will be rehydrated using the soaking paste. Exhaust gas enriched with high-temperature CO2 is collected in each cyclone separator. be individually recovered from and further used as desired or with equipment not shown. The combined hot exhaust gas stream 49 is used to generate water vapor at the site.

One or more cyclone separators can be used in sequence, with a series of cyclones It will be understood by those skilled in the art that the number will be determined by the respective size and the arrangement used. it is obvious.

Regenerated in the second regeneration step, the residual carbon is reduced to 0.10% by weight, especially from o, osite%. heated to a temperature above the first stage regeneration temperature by combustion to a lower level The catalyst is removed from bed 33 by conduit 51 and transferred to an adjacent vessel 53. Take out The catalyst is introduced by conduit 55 in an adjacent contact and collection zone or vessel 53. In particular, when a water-free gas or at least one substantially water-free gas is blown. be included. The blowing gas is drawn out through four pipes 57 and introduced into the upper part of the container 35. .

High temperature regenerated catalyst above 1400'''F has a flow control valve 61 from sea 753. It is taken out by the vertical conduit 59. The hot catalyst is then lit by transport conduit 63. The flow then moves to the lower bottom 65 of the hydrocarbon conversion door 67. Downstream not shown Blowing or rising gases such as light hydrocarbons recovered from battle-end recovery operations or other suitable fluidized gaseous material to the inlet to the catalyst pipe via conduit 69. Supplied below.

Especially in the case of favorable hydrocarbon conversion lies, high temperature catalysts with low residual carbon flow upward. The live fireproof lining is placed adjacent to the wall but away from it on the inside. A large number of hydrocarbon streams introduced through a large number of feed nozzles 71 and a live cross section Mix. More specifically, the Raiji-Dan is equipped with a swollen wall section 73, and has many horizontally separated walls. The supply nozzle passes upwardly and circularly through this section. water vapor, light hydrocarbons Diluent gas such as or mixture thereof is atomized, dispersed and evaporated with high temperature fluidized catalyst particles. It is added with the charged kettle residual oil to facilitate mixing. Output of raw material injection nozzle The live part near the mouth button is expanded into a live container with a particularly large diameter, and this area is evaporated. A suspension of oil and catalyst passes through. Furthermore, the desired mixture of the charged pot residual oil components is obtained. Multiple small streams of atomized feedstock are placed above to promote coalescence and near-instantaneous evaporation. Mixed with the co-flowing catalyst charge. From decomposition products mixed with catalyst M cloudy particles The vaporized hydrocarbon material passes above the riser 61 and exits from the top of the riser. Discharged via a suspension separator. Various means known in the art may be used for this purpose. can be done. Rise's Hydrocarbon Conversion Zone Ami's Rough Cut Separator The first turbidity separator is placed on a relatively large wall of the live near the capped top of the live. It is shown as an appendage extending outward from the live to the wing shape of the section that cooperates with the borehole.

In other words, the rough-cut separator at the live end has a butterfly-shaped device when viewed from the side and top. It's similar to. The adduct has a bottom that contains hydrocarbon vapors that are largely separated from the catalyst particles. It opens into a surrounding container 87 for drainage. As shown in FIG. The end wall 79 adjacent to the wall of the container 87 is curved approximately vertically. It is a bare board. The top of each addition is covered by a sloped roof 81, on which Reduces build-up of catalyst and coke particles. The slope of the roof shingles is an addition on the roof. In particular, the angle of repose of the catalyst used should be at least equal to, and In favor of this angle is larger. Other arrangements known to permit high steam evacuation rates Hydrocarbon vapors exiting from the live top - to carry out the first separation of the catalyst suspension Can be adopted.

During operation, a vaporous mixture consisting of hydrocarbons and diluent in the form of a mixture with suspended catalyst The material is discharged through the holes 75 in the rise and expands and mixes in each additional chamber A and B. The material slows down and separates from the vaporous material flooding the outer vertically curved wall 79 of each appendage. Also, the orientation of suspended components and concentrated catalyst particles changes. This way you can concentrate or min The separated catalyst particles fall down the wall and form a catalyst ring consisting of the IJ tzubing zone. It is collected as a layer 83. The vaporous material separated from the catalyst particles is through the open bottom close to the tube wall and from there to the top of the vessel 87 by a separator 85. Flows upwardly into one or more of a number of cyclone separators as shown. touch The hydrocarbon vapors separated from the medium, the thickening agent and the gaseous stripping material are carried in conduit 8. 9 and sent to a product recovery device, not shown. one or The catalyst separated by a large number of cyclones is transferred to the catalyst layer 83 by the provided immersion legs. . A stripping gas, such as water vapor, is introduced into bed 83 by conduit 91.

The stripped hydrocarbons leave the rough-cut separator with hydrocarbon vapors Enter the cyclone separator arrangement.

Containing hydrocarbonaceous products and metal impurities from the decomposition of residual oil from IJ The medium is removed by a conduit 93 with a valve 95, from where it is transferred to a first recycle by a conduit IK. Sent to raw processing.

Figure 2 shows individual regeneration vessels 2 and 4 on a common axis above and below each other for maximum temperature regeneration. The arrangement of the equipment is different from that shown in Figure 1 because the container 4 is stacked as the upper container. The placement is shown. Furthermore, high-temperature exhaust gas is transferred from 4 to refractory-lined conduit 6 to the regeneration system. and is pulled out through the arm conduit 8 arranged in a T-shape. large cyclone separation A vessel 10 is suspended in communication with each horizontal arm conduit of the T-shaped conduit.

In this equipment arrangement, multiple feedstock inlets and suspensions are represented by equipment 14. A hydrocarbon conversion rice reactor 12 having a turbid rough-cut separator 16 is shown in FIG. It is shown in the same way as explained in . However this thread or other arrangement can be used as a catalyst collection vessel. 1 disposed inside or outside the collection container 20 adjacent to the rice discharge port on the upper part of the collection container 20. Conceivable for use with one, two or multiple large cyclone separators 18 It will be done. Using a similar arrangement as shown for the upper regenerator 4 of the device You can also do that.

In the case of the equipment arrangement shown in Figure 2, the area exceeding approximately 14001 within the dedicated area 22 and at least the The high-temperature regenerated catalyst at a temperature equal to the tentative criticality of the residual oil in the reactor is charged into the bottom of the riser 12. , where the rising or blowing which is done by the guide v24 is mixed with su and upwards. Form a flowing suspension.

Thus gassed or suspended I? ! The medium is equipped with a large number of supply nozzles K14 PBi is brought into contact with a large number of streams of atomized feedstock oil. In nine special cases In this case, six horizontally spaced nozzles penetrate the riser wall near the enlarged part, as shown in Figure 4. spread through. Water vapor and other diluting materials are used as raw materials for the purpose of atomization and dispersion as described above. Can be injected together with

The vaporous hydrocarbon catalyst suspension passes upwardly through riser 12 and into rough cut adduct 1 6 as described with respect to FIG. Charcoal separated from catalyst particles Hydrogen vapor is passed through one or more cyclone separators 18 for additional recovery of catalyst. The hydrogen ash-containing vaporous material is passed to a product (not shown) by conduit 26. Sent to fractionation process.

The catalyst separated by the device 16 and the cyclone 18 is placed in a catalyst layer at the bottom of the container 20. It is collected as n. Stripping such as water vapor is carried out by g28 to remove the layer. Introduced at the bottom. The stripped catalyst is evacuated by four pipes 30 with valves 12. It is sent to the catalyst bed 32 where it is regenerated in the vessel 2. Regeneration gas such as air is supplied to the air distribution ring It is introduced into the lower part of layer 32 by a conduit device k34 communicating with 36. Hakamou zone 2 is maintained as a regeneration operation with a specific soft temperature lower than 1500”E’i, and the gradual carbon Achieve partial removal of all hydrogen associated with decomposition and decomposition of decomposed hydrogen negative materials. under the conditions chosen to occur. During this work, exhaust gas containing COVC is formed. It will be done.

This gas can be used in cyclones 38 and 40 in parallel or in series with other cyclones. The catalyst is separated from the entrained finely divided catalyst by one or more cyclones.

The CO-rich waste gas is recovered from the cyclone separator by conduit 42 and is used as such.

The partially regenerated catalyst is passed from the bottom of bed 32 for upward passage through standpipe 44'. A separate upper second stage of catalyst regeneration with an upper interface 48 It is discharged to the bottom of the fluidized bed 46. Regeneration gas such as air or oxygen-enriched gas is R , the bottom entry of the upright W44 by means of a hollow stem plug valve 54 having a volume control device 74. Introduced into the mouth. Additional regeneration gas, such as air or oxygen-enriched gas, is It is introduced into layer 46 by a conduit 50 leading to ring 52 . Assudaniki 4 is as mentioned above. The container has a fireproof lining that does not expose any metal additions, so the internal temperature is lower than that of the metal. Unlimited by additives, VCl easily reaches high temperatures in excess of 500″F and 180 It can rise to 0'11ilE or as high as necessary for complete carbon combustion. this Temperature Limiting in Catalyst Regeneration Environment Residual carbon remaining on the catalyst following the 1b raw step limits temperature It is almost completely removed in the second regeneration step. In this way, the temperature inside the exogenous device 4 is There are no particular upper limits other than those limited by the carbon violet to be removed, Residual carbon on catalyst? ! ：By enjoying it, there is a wave of CO that supports ``'C combustion. Sufficient eR elements are supplied so that an exhaust gas rich in carbon dioxide is produced. This way The exhaust gas rich in CO2 generated in the same year forms a dense flow with a small amount of catalyst particles produced in the same year. The exhaust gas moves from the P8 medium layer 46 to the dispersed catalyst phase above it, and from there the exhaust gas is It is taken off by conduits 6 and 8 leading to more cyclones 10. Conduit device It is a straight line, and it is bent horizontally before connecting tangentially to the cyclone 10. There is. The curvature of the conduit 8 in particular matches the curvature of the cyclone wall, so the entrained A first centrifugation of the catalyst particles takes place in conduit 8 before entering the cyclone separator.

Due to this arrangement, the catalyst particles are separated from the exhaust gas with high efficiency and are separated from the cyclone. The efficiency of the separating device is further increased by lengthening the conical bottom of the cyclone. be able to. The catalyst particles separated in this way are lined with a leg device! t5 6 to the catalyst layer 46 of the high temperature regenerated catalyst. There is no Co of the combustion support award. The CO2-rich exhaust gas is transferred from the cyclone 10 through a dedicated pipe 58 and used as described above. It will be collected to do so. Regenerated in Shima On's zone or vessel 4 at 1800ft The catalyst particles are removed by a refractory lined conduit 60 to a vessel 62 from which 66 tl - to the dedicated pipe 22 leading to the riser reactor 12 through a standing conduit 64 Sent. The gas is supplied by a conduit device 68 passing through the distribution ring VC in the vessel 62. It is introduced into the lower part of the container 62. It was taken out from the top of the container 62 through the conduit 70. The solid material enters the upper dispersed catalytic phase of the vessel 4.

The arrangement of the apparatus shown in FIG. 2 is as follows: It is a compact array system arranged in pressure equilibrium to achieve the desired processing sap.

Yarn work is facilitated by the use of spherical catalyst particles smaller than 200 microns, The average particle size can be selected from within the range of 50 to 120 microns. Rai At the outlet of the cyclone conversion zone, an external support is placed in the vessel 20 with a hole to the cyclone centered at the top end. It is conceivable to improve the yarn shown in Figure 2 by providing an Ikron. External service The Ikron separation device is connected to the conduit 6.8 of the regenerator 4 and the cyclone 10! Indicated by fc It can also be arranged in much the same way that it is attached to the vertically narrowed container 20, It can be used instead of the internal cyclone 18. Catalyst particles separated in this way The sample is placed in the lower part of the container 20 in contact with the stripping gas supplied by the conduit 28. It is carried by a suitable ramming leg that connects to the collected particle layer.

According to the example of FIG. 4, the high temperature regenerated catalyst and the hydrocarbon conversion rice zone 65 of FIG. Alternatively, charge the residual oil raw material into the bottom of the riser 12 in Figure 2. One arrangement of the device is shown in detail. The residual oil is stored in many straight or curved pipes 1. 1. The pipe is a jacket pipe, and if desired, it can be used for water vapor heat retention. It has a massive zone. In the case of the arrangement shown in Figure 4, the tentative critical temperature of the pot residual oil feedstock [beyond] Is it true? ! The catalysts at temperature lj are each connected to a refractory lined pipe 63 The material is charged into the paper portion 65 of the ricer hydrocarbon R pipe 61 which has been used for two innings. p The Ba venting or inducing gas is introduced via conduit 69 to the gas distributor at the bottom of the live. be done. A hot suspension of catalyst and flotation gas forms at the live bottom, which in turn The material passes upward through the tube and reaches its enlarged portion, and is charged through a number of raw material inlet pipes 71. Contact with oil into the kettle. The raw material oil charged from the device 71r is introduced through the conduit 109. mixed with water vapor or light hydrocarbons, thereby charging The partial pressure of the hydrocarbon feedstock reduced significantly. The jacket water vapor of the oil supply nozzle is Steam is supplied from an inlet device 111 to a quay-like portion formed around the pipe 71. Lies a number of horizontally spaced such jacket nozzles discharging into a cross-section of the Oil charged with fluidized catalyst particles to achieve near-instantaneous steam-atomization of feedstock kettle residual oil. In particular, six such nozzles are arranged to achieve high temperature contact between the two. of In one configuration, the cracking device appears as a half-tube based on the refractory material of the ricer wall. After the bubbles are formed in the part 13, the bubbles are exposed to the live enlarged wall part. The nozzle is suspended to raise the live The isometric cross-section of the wafer is designed to improve sufficient atomization-evaporation contact with the cloudy catalyst particles. It is rearranged so that it protrudes toward the diameter. A large number of uterine tubes are especially enlarged. t1. Straighten the circular V shape and charge the pot. Approximately -III F of the residual oil, plus sufficient feedstock and cylinder contact to achieve evaporation. The desired mixing with the media particles is achieved. When the charged pot residual oil raw material is fully fruited. At least 14CiLl-'F' and 15[, IO~18 To provide more sufficient evaporative contact with the hot catalyst particles at temperatures in the range of 00'''F'. It is also clear that various known techniques with atomizing nozzles could be used.

The kettle residual oil cracking operation of the present invention achieves almost instantaneous evaporation of the charged raw material oil. A catalyst with a very low residual carbon content is obtained at a temperature exceeding the tentative critical temperature of the pot residue feedstock. based on very high temperature catalyst regeneration operations. Another hpl person who does combination work is The catalyst that was partially contaminated with Kanata was replaced with a new catalyst, and the first regeneration of the catalyst was carried out during the Kakuo period. carried out under limited temperature conditions that reduce steam deactivation of the catalyst particles. This is to maintain catalyst activity. The decomposition work of the present invention involves cycle oil carbonization. Since the hydrocarbon bottoms are not recirculated to the decomposition process, the hydrocarbon supply process can be carried out in a 10-minute period. It is. On the other hand, the light hydrocarbon products, which are usually in the form of gas, and the water vapor produced in the process Air and CO2Fi are recycled and used as described above.

Furthermore, the formed olefin component is made suitable for the purpose of downstream equipment, not shown. The sea urchin is algylated and added to the hydrocarbon product material above the formed gasoline point. hydrocracking to produce a gasoline and/or gas oil product. is possible. Hydrocarbon products above the boiling point of gasoline are acceptable fuel oil products. It can be hydrogenated to remove sulfur and nitride so as to obtain .

611 The analogy of the 611 rhyme and bibliophile is especially the decomposed Ganlin, gasoline precursor and In the catalytic conversion of high boiling point hydrocarbons and <IC kettle residual oil in catalytic cycle oil production proposed to achieve a high degree of product selectivity.

The processing concept described below improves the decomposition by paying special attention to another working variable. It is particularly directed towards achieving a high degree of product selectivity in the industry. Other works The industrial parameters are particularly the raw materials that are more suitable for the desired purpose.1. Oil atomization and nozzle injection system Regarding.

In this working concept, most of the atomized oil droplets come into contact with the highly atomized feedstock and the fluid catalyst at the point of contact between the particles. It is particularly desirable to achieve near-instantaneous evaporative-thermal and catalytic conversion. hydrocarbon vaporization The gas-catalyst suspension increases the velocity of its upward flow through the rise, causing 1 to 1 01bs/fz", usually within a range not exceeding 51bs/f- A dilute catalyst concentration of . In this way, instantaneous evaporation and conversion of feedstock oil is rapid. The closer the hook is achieved, the more the atomized raw material is adjacent to the inlet and the more the contact rises through the reactor. The pressure drop downstream of the contact with the media particles is lower.

Product selection by heat and contact means of converted kamaasa oil when working as described above The process is to make the feedstock oil come into contact with a high temperature catalyst to achieve evaporation of the charged feedstock oil. It can change depending on Cheng exhibition.

One favorable operating variable is particularly the high degree of atomization of the feedstock residue and the elevated temperature of the catalyst. Suitable atomizing nozzle feed inlet to achieve targeted contact with particles at relatively high speeds Regarding the use of the device VC. The heat and contact conversion of the evaporated feedstock to the desired product is This is achieved within a very short time frame with the temperature drop of the suspension formed as described above. It will be done. In this favorable working environment, the highly atomized feedstock oil is transferred to the live cracking zone. Q　Q　ft, /see at speeds up to 1300fz/sec (fps) The angle is approximately 10 to 15 degrees in the vertical direction and approximately 90 to 1200 degrees in the horizontal direction. distributed over the lie f cross-section in a fan-shaped pattern. It depends on the initial particle concentration due to VC. Upward finely divided high temperature catalyst particles ranging from 10 to 351 bs/ft3 This helps ensure better contact between the flowing suspension. formed suspension This velocity of the body disappears almost immediately and the hydrocarbon vapor/dispersed catalyst particle phase rises. A stream M1 body is formed. Since this is achieved quickly, approximately 60-120fz/ Comparison of product vapor and catalyst exiting the reactor at a rate in the range of sec. Since a high-velocity suspension is formed, the resulting pressure drop is reduced. formed suspension The concentration of the body is W (as required) to maximize the conversion of feedstock hydrocarbons. It can vary considerably. The suspended catalyst concentration is less than 51 bs/ft”; It is as low as 1 or 21 bs/ft" at the exit.

As mentioned above, the thermal and catalytic conversion is very V(− within a short time frame V()) Rapid V is achieved within the short vertical space of the reactor. . This is about 5ft%L or about 1Qfzr above the rise raw material inlet. associated with a small pressure drop across the section. The temperature of the formed @turbidity decreases rapidly. Measured at the exit casing or below the casing or rise, approximately 965 to 1[]00-! or to levels in the range of 1050°F.

In connection with achieving instantaneous evaporation of the atomized feedstock, up to about 50% of the atomized feedstock Thermal conversion occurs along with its catalytic conversion, gasoline, gasoline precursors and cycles A high yield of oil is formed. The decomposition reaction combination takes a very short time, within about 0.5 to 2.5 seconds. Observed to occur live within a short period of time, maximizing the yield of gasoline products Almost complete desired conversion is believed to occur in about 0.5 seconds to about 1-1.5 seconds. . High yields of gasoline and light cycle oil products live above the cording feedstock entry point Achieve a low pressure drop inside the reactor and keep suspended catalyst particles and hydrocarbons in the live obtained when contact with steam is limited to less than 1.5 seconds.

Furthermore, the aforementioned pot residue? 'During the development of the ItIK conversion concept, it corresponds to the fluidized catalyst particles used. droplet size or smaller, and approximately 20 to 150 microns. By having an average particle size selected from within the range, it is also possible to produce relatively high-speed raw materials for kettle residual oil. Achieve rapid evaporation at It is recognized that an eclipse with a small pressure drop is formed.

The graph in Figure 5 shows the conversion of oxygen between the first thread and the second system of the pot residual oil system. The relative softness is shown. The second system consists of mooring nozzles arranged in Figure 6, and the first system A much higher pressure level of raw material atomization can be achieved than previously achieved. Figure 5 is almost self-explanatory. , of the first and second atomization systems, although the same degree of heat conversion is achieved, respectively. The significant improvement in contact conversion achieved between

For the first system of FIG. 5 below the desired atomized kettle resid feed condition, at least about % thermal conversion achieved, reduced catalytic conversion to the desired phosphorus product and a reduction in desired product selectivity occurs. This observation indicates that the droplet size is the catalyst particle size. A second kettle residual oil raw material atomization nozzle system that obtains atomized raw material oil corresponding to giblets and goose bumps. compared to This system can be heated to a sufficiently high temperature to form a suspension of highly dispersed phases. A kettle with more complete steam distribution for intermittent mixing with suspended catalyst particles Guarantee residual oil feedstock. Each of these processing systems has similar thermal conversion, but different The achievement of overall product selectivity is illustrated graphically in FIG. The second source in Figure 6 Higher overall conversion is attributable to improved atomized oil catalytic conversion performance with the oil atomization system. achieved. In other words, when the catalytic activity is determined by the catalyst surface area x the ratio of catalyst to oil, the sixth As shown in the graph by the second atomization supply system in the figure') VC, depending on the raw material atomized in the A high level of Km is always achieved.

In this highly atomized and vaporized kettle oil hydrocarbon conversion environment, the catalyst average surface By continuously or intermittently increasing the product by increasing the surface area by increasing the surface area, The catalyst surface area is maintained at a level of at least 40 m”/9 Approximately 80 or 120 m2/, depending on the economics of elementary conversion and catalyst replacement! i’ It is advantageous to maintain this level at a high level.

Improved bottoms conversion, product selectivity and yield are achieved with System 1 Strand 2. The precise mechanism achieved is that the nozzle device of FIG. The highly atomized feedstock oil clearly achieves very rapid evaporation of the fine oil part and Enough evaporative contact with the fluidized catalyst particles at a temperature above the low critical temperature of the residual oil from the raw material pot. It cannot be fully explained except by pointing out that it does.

For the relatively harsh moxibustion residue-catalyst contact environment of system 2, the catalyst averages about 100 microns. Highly atomized below the particle size, homogeneous with catalyst particles at the temporary criticality of the raw material If the dispersed oil droplets are not almost completely converted by heat and contact, they will It is clear that within 1 VC evaporates almost completely. Contact with catalyst particles as described above. These operating conditions consist of highly atomized feedstocks that are in contact with It is clear that this has a decisively improved effect on the selectivity of the products Ru.

In catalytic cracking operations including the above-mentioned operations, at least The phenomenon of asphalt decomposition that produces the desired molecules lit@low is newer than known technology. This is the standard working concept. This working concept is particularly applicable to high-temperature thermal conversion of asphalt components. is associated with achieving decomposition. Achieve B's desired asphalt molecular weight reduction. temperatures higher than those normally used and achievable by the regeneration methods described above. Requires catalyst temperature.

Comparison of temperature, asphalt components and their structure in this new kettle residual oil catalytic cracking work Instant decomposition almost at the point of feedstock injection, especially promoting catalytic decomposition of atomized gas oil components to achieve a very short time frame of less than a fraction of a second before or at the same time as is considered important for the success of the task. Decomposition of raw material asphalt components is inevitable Generally speaking, the raw material is composed of aromatic or more cyclic compounds such as carbon dioxide and tree oil. , particularly enriching aromatic components that are young or do not contain significant amounts of 4- and 5-ring aromatics. Ru.

The driving force to achieve asphalt decomposition or molecular weight reduction is primarily thermal or The resistance to heat transfer from the hot catalyst particles to the asphalt molecules is temperature dependent2. Attributable to conductivity. The desired thermal conductivity depends on the particle or droplet size of the injected atomized oil. As it decreases, it increases exponentially. So super high temperature catalyst particles make super fog When in contact with oxidized oil, the moly-, di-, and tri-aromatics of asphalt molecules ・The desired decomposition of ~ is affected and leads to coke formation, such as that observed in coking processes. Without interlocking of the cyclic aromatic rings, delayed pregnancy can still be achieved efficiently.

This asphalt decomposition situation is achieved by a coke with a high cracking catalyst structure. The normal conversion of the light gas oil component of the feedstock is hindered or must be short enough so that it is not unduly restricted. There In addition to asphalt decomposition, the ratio of catalyst to oil plays a role in mixing temperature, A common endothermic catalytic conversion of the decomposable portion of the oil component below 1000°F' is accomplished. The goal is to maintain a sufficiently high or elevated position so that the Extremely high temperature regarding this This desired conversion can be achieved by small catalyst circulation rates or low temperature melt particles of the catalyst. The aim is to produce large sized catalyst particles at sufficient temperature with the desired high catalyst-to-oil ratio. It has become clear that this cannot be achieved effectively.

To carry out the desired conversion of a kettle residue feedstock of a given asphalt content, It is recognized that there is also a suitable desired catalyst temperature. This is the tentative critical temperature of the pot residual oil. can be called and expressed. In addition, the asphalt percentage in the raw material is With increasing to achieve the desired rapid or instantaneous vaporization of the feedstock in the presence of hot catalyst particles. must rise to the top. In this regard, the desired catalyst temperature is In the regeneration process, the asphalt content of the raw material increases, and the second industrial stock catalyst regeneration Occurs automatically if the raw equipment temperature is not limited by combustion of deposited carbon.

This is used Pff, and the Nix level on the medium increases the asphalt content of the raw material. This is because both prices will be higher.

This high coke level catalyst charged into the catalyst regenerator increases the temperature of the regenerated catalyst. raise to the level. Regeneration of catalyst particles above normal coke level increases catalyst activity This is a protection issue.

The spinning method combination is a recovery and processing method that helps improve gasoline and light cycle oil yields. As mentioned above, the high temperature of the asphalt components in the highly atomized kettle residual oil raw material Relies on rapid decomposition. The decomposition of the asphalt component of the pot residue raw material, especially the asphalt component, is caused by several types of high boiling It is of the nature to obtain significant amounts of C and T aromatics along with point polycyclic compounds. Ru. These components, which generally resist transformation by catalytic cracking, are ) Small agglomerates, especially mono- and di-rings, which help form low, poor, and high cetane distillate materials. The structure responds to hydrogenolysis in the form of hydrogenated products. Further hydrogen cracking The hydrogenated high-boiling products are recycled to the catalytic cracking operation and are then recycled to the kettle residue feedstock. It is a hydrogen donating material.

The above-mentioned pot residue catalytic cracking-catalyst regeneration method is an economical method for catalytic cracking technology. This represents a significant inventive step in eliminating the metallurgical limitations of thermal conductivity and thermal stability achieved. With this method hydrogen, including hydrogen cracking of polycyclic components in cycle oil products of catalytic cracking processes. Further improved phosphorus yield and light weight can be achieved when synergistically involved in addition operations. A reduction in asphalt molecular weight is achieved which aids in fuel oil yield. The above method combinations are Responds and adapts to changing feedstock properties. Another aspect of moxibustion is the unusually precise No instrumentation or control system is required to maintain smooth and stable operation. It is.

The pot residue is converted by the high temperature catalyst to form solin, low and high boiling hydrocarbons. The speed of conversion is further facilitated if one point is placed on the next working parameter. i.e. For example, in the riser decomposition system shown in Figure 2 above, high-temperature fluidized catalyst particles flowing upward in the live Shape the highly atomized raw pot residual oil droplets into fan-shaped contact at high speed with the child suspension. If modified to include the feed nozzle arrangement of Figure 6 for forming and charging, significant A significantly improved conversion is achieved. In this work the rising catalyst suspension was charged To ensure rapid and sufficient contact with the highly atomized feedstock, at least A concentration of catalyst particles of 10 to about 651 bs/f is desirable.

The improved pot residue conversion operation of the present invention is mainly performed on the above-mentioned highly oxidized pot residue. The oil raw material is in the range of about 20 to 150 microns or less, for example, about 120 microns or less. Catalyst particles with average particle size and surface area ranging from 40 to 120 m”/!! It is based on charging so that it comes into contact with the metal at a relatively high speed. 60-120 microns Particularly advantageous are catalyst particles having an average particle size selected from the range . atomized m The feed oil droplets are below the average particle size of the catalyst. However, turning raw material oil into noodles is a catalyst plate. It is advantageous to have a droplet size that is equal to or smaller than the average particle size. .

A very decisive aspect that brings about good results in the decomposition work of kettle residual oil is especially asphalt. Achieve rapid pyrolysis of tons of decomposable, catalytic cracking of decomposable vapor components, and Rapid suspension temperature drop which significantly reduces thermal degradation of the product in the form of gas generation related to achieving. With the improved kettle residue riser conversion operation of the present invention The following data were obtained in the experiments detailed.

Table 1 shows that prefixed crude oil or The kettle residue brings the catalyst particles into contact at a temperature at least equal to the temporary critical temperature of the feedstock. It is clear that this requires very fast evaporation times of less than 9 milliseconds.

The concept of catalyst regeneration-live cracking for treating the pot residue and VI crude oil is Achieving the desired high product selectivity by suppressing the formation of It has something to do with that.

All connections occur at the moment of atomized feedstock injection and contact with the suspension of hot catalyst particles. Chain reactions and interactions are influenced by temperature, feedstock atomization, and surface area. Catalytic activity and contact Depending on the working parameters of the touch time, it can range from milliseconds to about 1 second, which does not reach about 2 seconds. It is clear from the above description that this occurs within a very fast time frame that spans the entire range. difference Additionally, all of these conditions must be met to obtain rinsing, cycle oil and thermal equilibrium work. Live reactor flow to obtain the desired final product consisting of a matching small amount of coke. undergo changes over time. One particularly important aspect to avoid is and long contact of decomposition products consisting of tricyclic aromatic materials with high-temperature catalysts. It seems to be related. This is because it affects product degradation and coke formation. This is because there is a tendency. Therefore not more than about 2 seconds following evaporation and decomposition of the raw material , especially when very rapid temperature drops faster than about 1 second occur in gasoline and cycle oil production. The yield of product t- seems to be MW in order to maximize it. This is especially true for the improvements mentioned above. This is achieved by following a live working concept.

A rapid temperature drop to the range of 950-1050''F is desired.

Said advantageous working concept involves a significant increase in the speed of formation of the turbidity with the acceleration of catalyst particles. At the same time, the high temperatures used at the beginning are inherently useful to achieve within a fraction of a second. accompanied by rapid molecular expansion of the vaporous decomposition products. The kettle carried out within the said working concept Residual decomposition reduces the radial poor distribution of suspended solids in the live and therefore Medium agglomeration and other localized areas along the live walls affect undesirably high catalyst-to-oil ratios. Concentration of catalyst particles is avoided.

The rapid evaporation of the feedstock residual oil and its conversion under relatively fast conditions such as those described above is a live A limited vertical space circle of less than about 10 fz above the feed nozzle inlet within the It is recognized that it is always associated with low pressure drop operations.

This low pressure drop condition is consistent with the initial part of the live source at 5 or 1ofzt. It is clear that the opposite of what is experienced and disclosed is the lack of mixing of fuel oil and catalyst. be. Thus, a high degree of feedstock tinning is a key operating parameter, and its line 4 The distribution over the 11" cross section ensures sufficient instantaneous evaporative contact with the catalyst particles for the conversion. It is clear that the vertical direction IC10”E or 15°, and approximately 80 to 1500 fan-shaped patterns perpendicular to it. It became clear that close contact would be achieved.

Atomized feedstock at high speeds of around 500 fz/sec as desired here. Oil emissions are not found to be detrimental to the method. In other words, the flow at the nozzle exit When using a fossil oil discharge speed of 1300 fz/sec, 1 inch from the nozzle tip Approximately (55Q fz/sec) at a distance of 2 inches from the nozzle tip, only 3 A rapid decrease to 501/sec was measured. 6 inches and speed 130f z/sec. Method of the invention for carrying out live cracking of kettle residue feedstock The concept is that depending on the charged pot residue feedstock and below 800°F', it is common When using feedstock preheating not exceeding approximately 500° or 600″), the catalyst Therefore, depending on the temperature given, a very short time of about 2.5 seconds or less than about 1.5 seconds. It will be carried out within the specified time frame.

6, the live bottom 82 is smaller in diameter than its top 80, and the transition portion 8 Connected by 4.

The fluidized catalyst particles are charged by conduit 86 into the small diameter section at the bottom 111I of the two risers. Ru. The fluidizing gas is passed below by catalyst inlet conduit 86 to the distribution ring in the live cross section. It is introduced into the riser by shear conduit 881C. The valve 90 with valve 92 Acupuncture needles can be extracted from the bottom of the eve. The fluidization introduced by conduit 88 Gas is the solute product of catalytic cracking that separates gasoline precursors, or can be used. Gaseous fluidized materials such as low-grade naphtha may The high-temperature catalyst particles rise when they rise at the supply nozzle outlet f of the enlarged part without touching the bottom. As a transitional fluidizing medium for F1 clean direction exchange into the flow, alone or in decayed mass. The product hydrocarbons can be used in the form of a mixture with sulfur. Instrument type is work A provision is made on the live wall, particularly above the transition section 84, to measure the pressure drop and temperature of the system. You can get it.

The raw material injection nozzle is a cylindrical heat dissipation cover 98 with a narrow slit end opening that accommodates the internal pressure. It consists of a tube 94 having a diameter of 96. The nozzle points upwards above that near the live transition. Penetrate the live wall by tilting it at the desired angle. In this particular embodiment, approximately 60° It became clear that the angle was satisfactory. The raw oil is passed through a conduit leading to the oriice hole 102. 100 to lower the partial pressure and viscosity of the oil introduced, steam, light hydrocarbon water with or without the use of gaseous diluent materials such as pure or other suitable materials; It is introduced into the atomizing section of the nozzle. The oil exiting the orifice hits a flat surface 104. The droplets are formed into a conduit 106 leading to a small orifice 108. Thus, the incoming high speed material is sheared into fine droplet sizes by the sliver material. in rye The desired droplet size corresponds to the fluidized catalyst particle size as described above formed outside the reactor. Is the raw material oil that has been atomized into a cylindrical part of the nozzle system? I - passes at high speed and has a slit at its end. It can be discharged from the hole 96. A fan-shaped pattern of atomized oil droplets is created on the cross section of the beam. Therefore, one narrow slit hole in the IC is sufficient. The analogy is parallel to each other at 90° There may be two slits in the arrangement. For two or more such nozzle arrangements Advantageously, they are arranged horizontally and evenly spaced from one another around the live periphery. parable For example, there may be six or more such nozzle systems. At least temporary raw material Highly atomized feedstock in contact with upstream particles of catalyst at a desired high temperature equal to the critical occupancy Control of the live reactor above the transition zone to obtain a highly disturbed and intimate contact zone of the oil. It is also conceivable to arrange two or more of the nozzles vertically in a staggered manner within a limited vertical space. It will be done.

The oil supply nozzle arrangement is located on the live reactor wall approximately 13 fz or less below the live outlet. The heat and catalytic cracking product vapors live from the top outlet by providing at the top of the It is conceivable to quickly separate it from the catalyst during discharge.

This engine is used to improve the quality of heavy oil streams such as pot residue streams, prefixed crude oil, and atmospheric prefixed crude oil. Provides a general explanation of a number of work concepts useful for new combination work by Although specific embodiments have been described, other than those controlled by the following claims, It is clear that the reason does not imply an unreasonable restriction.

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Claims (31)

[Claims] 1. In a method of converting kettle residual oil using fluidized catalyst particles, (a) An upwardly flowing suspension of fluidized catalyst particles is passed upwardly through a riser reaction zone at an elevated temperature. height, (b) The feedstock residual oil to be converted is atomizes to a particle size of (c) Discharging the atomized pot residual oil at a speed exceeding 300 ft/sec to create the upward flow contact with a catalyst particle suspension; (d) Adjust the contact temperature between the catalyst particles and the atomized raw material pot residual oil to Heat conversion of up to 50% of feedstock and an order of magnitude greater than can be achieved with feedstocks with low degrees of atomization hold high enough to achieve tight contact conversion; (e) the vaporous product of the suspension of type (d) is combined with catalyst particles within a time frame of less than 2 seconds; To separate A method of converting kettle residual oil using fluidized catalyst particles. 2. The discharge speed of the atomized raw material oil is within the range of 300 to 1300 ft/sec. The method according to claim 1. 3. Claim 1, wherein the discharge speed of the atomized feedstock oil is approximately 500 ft/sec. Method described. 4. The mixing rate of contact between the atomized feedstock and the upflow catalyst suspension is controlled by the pressure drop downstream of the riser. 2. The method of claim 1, wherein the pressure is limited to no more than about 3 psig. 5. Claims where the pressure drop 10 feet downstream from the atomizing oil inlet is less than 1 psig. The method described in Scope 1. 6. Catalyst particle size selected from within the average particle size range of 20 to 150 microns. The atomized raw pot residual oil with a droplet size corresponding to It is charged as a fan-shaped droplet dispersion, and the upward flow of fluidized catalyst particles and feedstock oil are Claims that bring the asphaltenes into close contact with each other at a sufficiently high temperature to thermally decompose the asphaltenes. The method described in paragraph 1. 7. The average particle size of the catalyst was selected in the range of 60 to 120 microns, and the atomized oil droplets were 2. The method according to claim 1, wherein: 120 microns or less. 8. atomization of the feedstock is carried out in at least two sequential steps outside the riser cracking zone; An edge placed approximately horizontally within the riser cross-section for the subsequent discharge of the atomized droplets into the riser. The material is fed through an elongated narrow zone leading to a discharge hole with a slit in the middle. The method described in item 1 of the scope of the request. 9. Atomized feedstock oil is passed through the slit hole at high speed, tilting almost upward in the riser. 9. The method of claim 8, wherein the droplets are discharged in a fan-shaped drop pattern. 10. Thermal and catalytic conversion of the atomized raw pot residual oil is carried out for a time ranging from 0.5 to 1.5 seconds. 2. The method of claim 1, wherein the method is completed within a time frame. 11. The catalyst separated from the riser suspension is removed in two sequential steps of catalyst regeneration. containing hydrocarbonaceous deposits, the first step of which generates CO-rich exhaust gas and Temperature-limited and catalyst regenerated to reduce hydrothermal degradation due to generated water vapor The temperature is adjusted so that the second step obtains catalyst particles at a temperature higher than the tentative critical temperature of the raw pot residual oil. in a sufficient excess to almost completely remove the carbon on the catalyst in an unrestricted atmosphere. said first step to produce CO2-rich exhaust gas in the presence of oxygen-containing gas; 2. The method according to claim 1, wherein the temperature is sufficiently higher than . 12. Catalyst regeneration operations are performed in a stacked arrangement adjacent to the riser conversion operations, and this lamp A claim in which the diameter of the upper part of the iser is larger than the diameter above the lower atomized feedstock inlet. The method described in item 11. 13. A catalyst having a surface area in the range of 40 to 100 m2/g by converting the atomized raw material pot residual oil into particles and under conditions sufficient to achieve a transformation consistent with the upper curve of Fig. 5. 2. The method according to claim 1, wherein the method comprises contacting. 14. The temperature of the suspension formed by atomization of raw pot residual oil into small droplets and high temperature catalyst particles is Raw material components with a boiling point exceeding 1025F consisting of asphalt and asphaltene to achieve thermal decomposition and improve its quality by hydrogenation and/or hydrocracking claims sufficient to form mono-, di-, and tri-aromatic components that can be The method described in item 1. 15. The residual oil in the pot is atomized into droplets with a size of 100 microns or less, and the high-temperature evaporation takes less than 1 second. 2. The method of claim 1, wherein the method is sufficient for quickly completing the process. 16. Suspended high temperature catalytic and catalytic conversion of highly atomized feedstock residual oil completes in less than seconds and the temperature of the vaporized product suspension formed is about 935°F to 105°F. The method of claim 1, wherein the temperature is reduced to a range of 0°F. 17. The conversion temperature is increased with increasing asphalt content of the feedstock to regenerate the catalyst. is carried out at a temperature that satisfies the tentative critical conversion temperature of the raw pot residual oil. the method of. 18. In a method of converting crude oil tank residue using high temperature fluidized particles, (a) flowing a suspension of hot fluidized catalyst particles upwardly through a riser conversion zone; (b) Hot suspension of the raw residue to be converted in a size range of 20 to 200 microns. Atomizes to a droplet size smaller than catalyst particles, (c) Atomized pot residual oil in step (b) at 300 to 1300 to 1300 ft/sec at a speed in the range of at least equal to or above the preliminary critical temperature of the initial feedstock residual oil. introducing into contact with the upstream temperature catalyst particle suspension at a temperature exceeding (d) Adjust the contact temperature between the catalyst particles and the atomized raw material kettle residual oil to Decomposes asphalt components and achieves heat conversion of up to 50% of atomized feedstock oil. In order to carrying out, thereby lowering the temperature of the suspension; (e) discharging the vaporous hydrocarbon conversion product of step (d) into said column within a time frame of less than about 2 seconds; After passing through the isazone, it is separated from the catalyst particles. A method of converting crude oil tank residue by using high-temperature fluidized catalyst particles. 19. The discharge speed of the atomized feedstock oil to the catalyst suspension is approximately 500 ft/sec. The method according to claim 18. 20. The contact speed between the charged feedstock atomizing oil and the catalyst suspension reduces the pressure drop in the riser. 19. The method of claim 18, wherein the method is limited to no more than about 3 psig. 21. The pressure drop approximately 10 feet downstream from the atomized feedstock inlet is approximately 1 psig. 19. The method of claim 18, wherein: 22. Dispersion of atomized raw pot residual oil into a large number of separate fan-shaped droplets across the riser zone The upstream fluidized catalyst particles and asphragm in the feedstock are charged to the riser conversion zone as a In order to thermally decompose altene, sufficient contact is made at a temperature sufficiently higher than the temporary critical temperature of the feedstock oil. 19. The method according to claim 18, wherein the method comprises: 23. The average particle size of the catalyst is within the range of 20 to 120 microns, and the kettle residual oil is 19. The method of claim 18, wherein the method is atomized into droplets smaller than 0.00 microns. 24. Atomization of the feedstock oil is carried out outside the riser cracking zone, and the atomized oil droplets formed are Next, a narrow elongated hole at the end of the cross section, placed horizontally to the riser cross section, is opened. 19. The method of claim 18, wherein the method is fed through a long partitioned zone. 25. Atomized raw material oil is passed through the elongated hole at a speed exceeding 300 ft/sec, ejecting with a generally upwardly sloping horizontal fan-shaped drop pattern within said riser. 25. The method according to claim 24. 26. Thermal and catalytic conversion of atomized raw material pot residual oil by suspension catalyst is 0.5 to 1.5. 19. The method of claim 18, which is completed within the riser within a time frame in the range of seconds. 27. The catalyst with hydrocarbonaceous deposits from which the hydrocarbon products have been separated is subjected to catalyst regeneration. Two steps are carried out sequentially, the first step of which generates CO-rich exhaust gas. The combustion temperature is sufficiently limited and the catalyst is thereby reduced due to the presence of water vapor formed. Hydrothermal deterioration is reduced, and the second step of catalyst regeneration is performed using high-temperature exhaust gas rich in oxygen and CO2. combustion is promoted sufficiently to obtain carbon gas, thereby achieving almost complete removal of carbon on the catalyst. temperature is achieved and is at least equal to or above the temporary critical temperature of the feedstock residue. 19. The method according to claim 18, wherein catalyst particles are obtained at a temperature of . 28. Surface area of catalyst particles in the range from 40 to 100 m2/g and the upper curve in Figure 5 claim 1 having sufficient temperature conditions to effect a conversion of the feedstock consistent with The method according to item 18. 29. Atomization and atomization of raw pot residue to form droplets smaller than 100 microns. When the temperature of the oil and catalyst suspension is 10, which consists of asphalt and asphaltene, Thermal decomposition of feedstock components boiling above 25°F into hydrocarbons within a fraction of a second be sufficient to form mono-, di-, and tri-aromatic components in the product. Scope of Claim 18. The method according to item 18. 30. Thermal and catalytic conversion of highly atomized raw pot residual oil by a catalytic suspension results in The temperature of the vapor and catalyst suspension formed in the riser ranges from about 935 to 1050 degrees Fahrenheit. 19. The method of claim 18, wherein: 31. The conversion temperature increases as the asphalt content of the raw pot residual oil increases, and the catalyst Regeneration is completed at a temperature that satisfies the tentative critical conversion temperature of the raw pot residual oil with a high asphalt content. 19. The method according to claim 18.