JPS58142979A - Manufacture of fcc charger by selective evaporation - 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 This invention relates to increasing the proportion of heavy crude oil that can be utilized as a catalytic cracking feedstock for the production of premium petroleum products, particularly high octane motor gasoline, and as a premium heavy fuel.

The heavy residues of many crude oils are high in conradnon carbon (sometimes referred to as ramsbottom carbon) and metals, which are undesirable in catalytic cracking feedstocks and in products such as heavy fuels. The present invention provides an economically attractive method for selectively removing and utilizing the above-mentioned unwanted components from whole crude oils and from atmospheric and vacuum distillation residues, commonly referred to as "atmospheric and vacuum residues" or "residues". ``Residual oil'', ``''
Remaining #! ", and similar terms are used herein in a somewhat broader sense than usual to include the oil fraction remaining after fractional distillation to remove larger amounts of volatile components. In this sense, gasoline and light oils are The ``1 Topped Crude'' that remains after 1 is played is a residue.

Most of the undesirable CC (con2donone carbon) and metal compounds in crude oil have low volatility and are therefore easily concentrated in the residue. 1 conradon capo/" and 1 ram spot carbon" refer to the two most commonly used test methods for this unwanted component. Slight differences in the numerical values of the results obtained from the painting methods indicate the same characteristics.

When catalytic cracking was first introduced to the petroleum industry in the 1980s, it was a major advance as it offered an advantage over traditional methods in increasing the yield of carcinol from petroleum to meet the rapidly growing demand for premium products. This catalytic process produces abundant high octane naphtha from petroleum fractions above about 400° F., which have boiling points above the gasoline range.

Catalytic cracking has been greatly improved through intense research and development efforts, and the installed capacity has been rapidly expanded to its current level, making catalytic cracking equipment the main equipment in oil refining, the "workhorse".
It is.

As catalytic cracker capacity increases, 4iIMs are increasingly charging the unit with a more generous portion of refined crude oil. There are eight strong constraints on this requirement: feedstock conradone/carbon and metal content. As these values increase, the capacity and efficiency of the catalytic cracker will be adversely affected.

CC of heavy fuels such as bunker oil and heavy gas oil
The quality of these fuels is also increasingly affected as they need to be produced from crude oils with high metal and salt contents.

The effect of high CG in catalytic cracking is to increase the charge that converts into 1" coke deposited on the catalyst. When coke forms on the catalyst, the active surface of the catalyst is stripped away and becomes inert to the desired conversion reaction. After combustion of the air-inert coke to regenerate the active surface, it is common practice to circulate the catalyst back to the reaction stage where it contacts and converts the next charge. The heat generated during the combustion regeneration stage is at least partially recovered and used to provide the heat of vaporization of the charge and the endothermic supply of the cracking reaction.

The regeneration step is conducted within high temperature limits that prevent thermal destruction of the catalyst. Since the coke burning rate is a function of temperature, the regeneration stage has a limit on the amount of coke that can be burned in a unit time. As the CC of the charge increases, the coke combustion capacity becomes an impediment to reducing the feed rate to the unit. This also has the disadvantage that part of the feedstock is converted into undesired reaction products.

The metal-containing fraction contains nickel and vanadium, which are potent catalysts for the production of coke and hydrogen in 411. If these metals are present in the charge, their molecules can be decomposed and deposited on the catalyst, forming highly troublesome molecules. The negative effects of increased coke are as described above. Excess hydrogen also causes interfering problems. The lighter residues of the cracked products, butane and lighter ones, are processed in a fractionator to separate the components of greater value than fuel to the furnace, primarily propane, butane and similar carbon number olefins. Hydrogen that cannot be condensed in the 'gas unit' will accumulate space as a gas in the compression and fractionation unit, and excess amounts produced by the high metal content catalyst will overload the AK unit and disrupt the operation of the FCC unit and auxiliary equipment. Reduce charging speed to maintain

Quality is important for heavy fuels used in fixed furnaces, turbines, marine and large fixed diesel engines! 1! It is basic.

For example, petroleum ash, especially vanadium (9um), attacks furnace refractories and turbine blades.

These problems are recognized in the art, and many treatments have been proposed. Thermal conversion of the residual liquid produces a large amount of solid fuel (
One process, characterized as coking, is currently practiced industrially.

- In the retarded coking process, the feed is heated in a furnace and sent to a long cylinder treatment at 780-840" F. During a long residence time at this temperature the charge is converted to coke and distilled. The products are recovered from the top of the cylinder as 1'coke oven gasoline', 'coke oven gas oil' and gas.Other coking processes currently in use
F uses a fluidized bed of small coke particles. The residue charge is converted on the surface of the coke particles with a residence time of about 2 minutes and is transferred to the surface of the particles in the fluidized bed Kll! Deposit coke on. The coke particles are transferred to an air fluidized bed and a small amount of coke is burned at 11 degrees above 1100 degrees Fahrenheit to heat the remaining coke, which is then returned to the coking vessel for further charge conversion.

This coking process is known to cause significant cracking of components that would be valuable in FCC charges, and lower octane gasoline (from pyrolysis) than the 5 that would be obtained by catalytic cracking of the same components. ). The product gas oil is olefinic, and it is often desirable to treat the gas oil by a front-end hydrogenation process in which it is mixed with a coke-crackable fuel fraction in the furnace tube and over a cracking catalyst. Although coking reduces metals and Conradoso/Karl, it still leaves a poor quality gas oil as a catalytic cracker charge.

Catalytic cracking charges and fuel feedstocks can also be produced from the residue by an asphalt removal process such as mixing an asphalt precipitant such as liquid propane with oil. Metals and conradon/carbon are significantly reduced, but the yield of de-asphalted oil is small. Other methods have been proposed, including the KIN medium extraction method for producing FCC charging raw materials, and the O2 residue. Propane deasphaltization and co-KfII extraction work by chemotype selection;
It does not accept aromatic compounds that decompose in the feedstock and produce high octane components of cracked naphtha. Low-temperature liquid phase sorption on catalytically inert silica has been proposed by Schumann and Brace, Ga5 Journal 1% April 6, 118 pages (196B). Also, U.S. Patent No. 18
No. 98.581, ia, 46 L891, and ia
, l! , No. 7118.

No. 8,46, No. 891 (by Knoll) and No. 2.8? No. 8.581 (by Pelaker) utilizes a body heat transfer medium for vaporization and uses heat from a catalytic regenerator to preheat the feedstock for catalytic cracking. Although the Patentee's intention is to minimize the total amount of the contact charge, the heavier portion of the charge remains in liquid form and, due to prolonged contact with the heat transfer material, produces a conversion similar to that associated with the above-mentioned coking process. It is recognized that the evaporated cracking products and coke can be converted into coke.

U.S. Patent No. 2,412. ? No. 18 proposes the addition of adsorbent clay to the charge for catalytic cracking. Clay is used only 11 times to adsorb polynuclear aromatic compounds that are believed to later become coke and to reduce the amount of coke deposited on the active cracking catalyst, which is also in the cracking zone.

It is known to use solid heat transfer agents to cause the gradual decomposition of a hydrocarbon charge at high temperatures and short periods of time to maximize ethylene and other olefins in the product. For example, the US TIII Patent No. 11B, O'1898 for t<pass announces this.

The present invention relates to a process for producing premium products from crude oil or resid material containing high boiling fractions contaminated with metals, high carbon contents, or both, which process involves subjecting said material to high temperatures in a rising closed column. Strict requirements for low decomposition with short hydrocarbon residence time (joy cracking 5ever4ty)
contact with an inert contacting solid finely powdered material under conditions to separate the vapor product from said contacting material having combustible deposits of non-vaporized high Conradson or high metal content components of said material; , the vaporized product is quenched to 1 degree below the temperature at which thermal decomposition occurs, and the quenched product is cooled to about 4 degrees
The naphtha fraction is separated into a normal liquid soot fraction with a boiling point below 50°F and a heavy fraction with a boiling temperature range above the naphtha fraction, and the naphtha fraction is passed through a catalytic cracking riser ( Ripe
r) injecting into the bottom of the reactor to create a closed column in which hydrocarbons rise in the reactor, and injecting an active fines cracking catalyst into the reactor to create a closed column in which hydrocarbons rise in the reactor; dispersing the catalyst and injecting the heavy fraction into a rising closed column of catalyst dispersed in hydrocarbons at a point above the injection point of the naphtha fraction and contacting it from the catalyst at the top of the riser reactor; It consists of a selective evaporation process by separating the vapor products of decomposition.

The present invention also relates to an apparatus for producing prebuild products from heavy hydrocarbon bulk charges with a high Conradson carbon or metal content, the apparatus comprising a vertical riser contactor, in which the hydrocarbon is loaded at the bottom of the contactor. means for introducing a hot inert fine contact material into the bottom of the contactor; means for separating the fine contact material from the hydrocarbon vapor at the top of the contactor; a fractionator; means for transferring the naphtha fraction to said fractionator for fractional distillation; means for separately withdrawing the naphtha fraction and the high-boiling bottoms fraction from said fractionator; a vertical tubular cracking reactor; means for introducing a hot finely divided cracking catalyst into the bottom of the cracking reactor; means above the bottom of the cracking reactor for introducing the bottom fraction into the cracking reactor; and a top portion of the cracking reactor. means for separating the vapor produced by decomposition from the finely divided catalyst.

Briefly, selective evaporation processes heavy components with high CC and/or metal content onto solids in a closed vertical column that ascends heavy materials such as whole crude oil, top crude, residues, etc. This is done by contacting an inert solid finely divided material under conditions that deposit and evaporate other components of the charge.

This can be done at a high enough il to provide the desired vaporization and very short hydrocarbon residence times to avoid substantial decomposition. The operation is therefore maintained at low decomposition stringency for the desired purpose of separating volatile, more valuable components from possible contaminants. Steam, light hydrocarbon rings, is added to the rising closed cylinder of the selective evaporator to lower the partial pressure of the hydrocarbons in the charge, thus aiding evaporation.

At the top of the column, the unevaporated components are separated from the overlying inert solids as hydrocarbon vapor chamber deposits.

The vapor is rapidly quenched to a temperature substantially below that at which pyrolysis occurs and processed as desired in a catalytic cracker or the like.

The separated inert solids with deposits of non-vaporizable components of the charge are transferred to a burner for combustion of the deposits in air or other oxygen-containing gas. The heat generated by deposit combustion raises the temperature of the inert solids, which are returned to the bottom of the rising closed column to provide further heat for selective evaporation of the heavy charge.

Riser tube FC for product decomposition from selective evaporation according to the invention
The operation of the C unit is improved by injecting the one solin fraction from the selective evaporation into the lower part of the FCC riser, where the gasoline fraction serves as a carrier for the FCC catalyst and improves gasoline quality. The heavier fraction from the selective evaporation is entered into the higher point of the FCC riser. This is F
By varying the residence time in the CC riser, approximately 40
Adds additional flexibility to heavy distillate cracking with boiling points above 0-460°F. A schematic diagram of an apparatus suitable for carrying out the present invention is shown in Figure IK in contact with the new FCC catalyst at a high catalyst/oil ratio for further conversion to low octane naph, LPG and high octane gasoline. FIG. 3 is a diagram of the preferred type of injection nozzle for charge injection into the FCC riser at a point above the point of entry of selectively evaporated gasoline.

As shown in Figure IK, the main equipment used is a riser l which brings the inert solid and the scissor material into brief hot contact, terminating in a separate chamber 3 and removing non-evaporable material deposits from the chamber. The inert solids are transferred to burner 8 by pipe 4.
will be moved to The high-temperature inert solids obtained by combustion in the burner 8 are returned to the lower part of the riser l by means of a pipe b passing through the regulating valve 6.

Charge material containing high-boiling components characterized by a high CC1 metal content or both enters riser 1 via pipe 5 and is raised at high speed through riser 1 while high-temperature inert material from pipe 5 I am forced to touch the solid *KW1. The bulk of the charge material is evaporated at the temperature in the riser tube by hot solids from pipe 5. This evaporation very quickly creates a rapidly rising column of vapor and inert solids suspended therein. The portion of the charge that does not evaporate becomes a combustible deposit that deposits on the inert solids and is composed primarily of the high CC and metal content components of the feed.

The solids are separated from the hydrocarbon vapors at the top of the riser tube by a suitable apparatus developed for the riser tube cracking of hydrocarbons in the presence of an active cracking catalyst. be done. Preferred methods for the present invention include Mayer et al. U.S. Pat. Nos. 4,066,588 and 4.0.
? 0. It is a riser pipe with an outlet as described in I I No. 9. The upper end of the riser tube 1 is open, and the solids are ejected into the container 2 due to the inertia of the suspended solids. The solids suspended in the steam entering the side hole glass separator 8 in the steam riser are removed and discharged by leg 9 to the lower part of vessel II3. The large solids ejected from the top of the riser and the solids exiting from the leg 9 go to the stripper 10 below.

The steam from the trowel tube 11 assists in the evaporation of any remaining volatile hydrocarbons before the solid-containing combustible deposits enter the pipe 4 leading to the burner 8.

The steam sent to cyclone 8 and separated from the large solids is sent to conduit 1! IK] transfer line 18 where the vapor is mixed with a suitable quenching medium such as a cold hydrocarbon waterfall or water and cooled to a temperature substantially below the temperature at which pyrolysis occurs.

The burner may be of any construction developed for the combustion of combustible deposits from field fines, such as a regenerator for a fluid cracking catalyst. Air admitted to the burner via tube 15 provides oxygen for the combustion of deposits on inert solids and becomes combustion product gas which is discharged through flue gas outlet 16. Burner 3 is/
It is advisable to work to keep the internal ilf at the maximum value normally limited by burner metallurgy. This gives the minimum temperature of the fuel (as a deposit of inert solids) which will give the maximum temperature of the riser pipe □ of p < - □ degrees! You can adjust it to As is common in thermally balanced nine-FcC systems, the valve 6 is adjusted in response to the temperature at the top of the riser to maintain the riser temperature at a predetermined value.

The predetermined temperature is reset 9 as necessary for selective evaporation to maintain the desired maximum temperature within the burner 8. A tendency toward lower temperatures in the burner 3 is compensated for by lowering the predetermined temperature of the riser 1, and vice versa. The inert solids heated (by combustion in burner 8) are returned to the riser IK before being returned to
(-Qi 3 is stripped with steam in the pipe 5.

Surrounding contact agents are used to reduce the minimum decomposition of heavy hydrocarbons by standard microactivity conversion tests that measure the amount of gas oil converted to gas, gasoline, and coke when the gas oil is brought into contact with solids in a fixed bed. It is essentially inert in the sense that it causes

The charge in this test was 0.8 g of Mido Continent gas oil of 3 mA API in contact with 4 g of catalyst during a 48 second oil run time at 91 G'PK. This results in a catalyst to oil ratio of 5 at a weight hourly air speed CWH8V)lh. In this test, the large solids used herein exhibit an electrochromic activity of slightly less than 80, preferably less than about 10. The preferred solid eat calcined kaolin clay microspheres. Other suitable inert solids include coke produced from petroleum or coal and solids generally meeting the above criteria.

The preferred calcined kaolin clay spheres used in the method of the invention are well known in the art and are
U.S. nationality Pestle II & 64? , 718, as a chemical reactant with Q-ram solution in the preparation of one-fluid zeolitic cracking catalysts. In the practice of the present invention, on the contrary, smoldered kaolin clay mold spheres are not used as chemical reactants. Therefore, the chemical composition of the chain kaolin clay microspheres used in the practice of this invention corresponds to the composition of dehydrated kaolin clay.

Generally, the analysis of snow-fired fine particles is S1Q about 51 to 5118% by weight - 1A1 snow 0.41 to 4.1% by weight, and H, o
o to 1% by weight, the remainder being small amounts of inherent impurities, especially iron, titanium and alkaline earth metals. Generally iron content CI'
hoe ) is about 0. The weight of titanium CTi (expressed as h) is approximately 2 weight.

The microspheres are preferably produced by spray drying an aqueous suspension of kaolin clay. As used herein, the term ``kaolin clay'' includes clays whose main mineral components are kaolinite, halloysite, nacrite, ditzite, anokite F, and mixtures thereof. It is preferred to use a clay containing a quantity of submicron-sized particles to form microspheres with adequate mechanical strength.

If you want to produce particles with maximum stiffness, use fine particles of about 1600
~! It can be smoked to a temperature of 1GO'P, but it can be fired at a low temperature, for example 1000 to 1600 °C, to dehydrate the microspheres and form a clay known as 1methakaolin.
It can be changed into quality. (2) It is necessary to cool the mold particles after sintering, and it is also necessary to round and sieve the mold particles in a desired size range, for example, from sO to 1SO microns, to collect them.

The pore volume of the microsphere is 11! Accumulates due to baking fatigue and time.

Pore size distribution analysis of a representative sample obtained using a desorber analyzer using nitrogen release revealed that most of the pores were IJO to 6.
It shows that it has a diameter of about 0.00 Angstrom.

The surface area of am mold spheres is the known B, E using nitrogen absorption.
,T.

Normally 10 to 1% is in the range of 79 when measured by method.
It is within. The surface area of commercially available fluidic biolitic catalysts is extremely large, with a surface area of 100 when measured by the general K B, I:, T method.
This exceeds the value of s-rich/g.

Although the above device superficially resembles an FCC device, its operation is very different from the FCC. Most importantly, the upright multitube contactor is operated to remove from the charge an amount that does not exceed the Conradson carbon number of the feed. This is in contrast to the normal FCCF conversion of 60 to 10 measured as per centimeter for the VhFCC product which boils within the range of the charge. The standard is at most 1G to z〇- and is composed of gases and deposited on solid catalysts. 8 to 4 times the amount of Conradson carbon.This result is observed due to the inertness of the solids and the very low uniformity of decomposition due to the very short residence time at the decomposition temperature [K]. In addition, the strict conditions for decomposition are a function of time and temperature; an increase in temperature can be compensated for by shortening the residence time, and vice versa.

The new method allows adjustments in the hydrocarbon or steam feed to the stand-up tube contactor that are not available in FCC units.

. When processing materials with high CC, the burner temperature increases as the fuel supply to the burner increases. This increases the feed hydrocarbon bulk or water vapor to increase the volume, lower the temperature or lower the hydrocarbon partial pressure in the riser contactor. Recirculation of water from the upper receiver evaporates in the riser for X-ray steam production. can be compensated by.

(rise) tube contact with inert solids and then leave #l! A novel sorption method is provided in which polynuclear aromatic compounds (high CC and metals) are removed while being transported to a low hydrocarbon partial pressure m by hydrocarbons or water vapor supplied to a rising low snowfall.

The carbon-, salt-removed and/or metal-removed residue can be transferred to an FCC feedstock system which is a high quality FCC equipment unit and operates in a conventional manner.

The properties of selective evaporation are determined by temperature, total pressure, partial pressure of hydrocarbon vapor,
It is known that it is a function of residence time, personnel department, etc. One effect of temperature is the tendency for combustible deposits on the contact material to decrease as the contact temperature increases. Therefore, at high temperatures, a large proportion of the charge (such as the charge) is fired, and at high temperatures the third effect of thermal decomposition of the deposited hydrocarbons increases. These high temperature effects reduce the amount of fuel delivered to the combustion zone in the form of combustible deposits before improving the product yield resulting from the operation.

Generally, selective evaporation is carried out by ASTM distillation of the temperature-controlled charge.
It will be greater than or equal to the average boiling point of the charge material calculated by dividing the sum of the points from 0- to 9011 by 9. The contact temperature of heavy materials contemplated in this invention is typically substantially 900'F.
The yield of olefins will be lower than, but not below, the temperature at which severe decomposition occurs. Therefore, even with a tkMi residence time of 0.1 seconds or less, the selected shot temperature will be less than about 1050''F.

Residence times for selective evaporation cannot be calculated accurately by methods commonly used in FCC cracking, where the vapor volume is greatly increased as the hydrocarbons are in contact with the active cracking catalyst along the tube length. In selective evaporation, contact with a highly inert solid causes a rapid generation of steam, which remains essentially constant along the length of the upper pipe, with a gentle heat that is believed to be due to the decomposition of deposits on the inert solid. It increases slightly with decomposition. The hydrocarbon residence time in selective evaporation is therefore divided by the apparent velocity of the steam (hydrocarbons, water vapor, etc.) at the riser top IIl and the riser length at the point where it leaves the inert body from the hydrocarbon injection point. Calculate and meet.

It is thus calculated that the bulk residence time of hydrocarbons in selective evaporation is substantially no greater than about a second, and is much more visible, 1 second or less, e.g. 0.1 seconds.As mentioned above, the residence time and temperature are low Given the stringent conditions, the amount removed from the charge will be approximately equal to the CC value of the charge when operated under favorable conditions, and the amount removed from the charge O
It is rare to exceed 1 to 4 times the value of CC. Furthermore, the hydrogen content of the deposit is #cruel! @X is less than the usual 7% in FCC Cortus.

According to Honji @, the generated products are fractionated and 1 energized liquid 0
``The bulk carb fraction is entered into the FCC riser at different points.

The present invention also includes a means of varying the carbide bulk residence time in the FCC riser while keeping the charge ratio constant, or a means of reducing the charge-brass to maintain a constant residence time. It will be clear that the invention is also flexible with respect to operation, i.e. the residence time and/or charge rate can be varied without keeping both constant. A pipe passes it to a fractionating column 1, from where the energized gaseous fraction is taken out from above by a pipe ls and processed in the usual manner, for example for refinery fuel. The intermediate ganosine fraction is sent by a pipe 20 to a settling drum 21, from where it is discharged by a water-drain pipe 2, and the upper napht is taken out by a pipe 8 which feeds a preheating furnace 14. The preheated tube is 7 tons!
The FCC riser pipe 2@Otakar: is supplied by Hiro, where Nafuna merges with the high-temperature gas coming from the two pipes and floats it to iI as a rising pipe.

The O-bottoms fraction from Column II is formed into a Select III acid product boiling above about 4 SO''P and is transferred to the pre-furnace gs by tube 8. The heated heavy fraction is se#
As shown in FIG. 1, from c, it is injected into the riser pipe 6 at a point above the Linafuna injection point. Feedstock for the YCC reactor reaction, such as nital oil, virgin gas oil, etc., is added to the transfer line 28 by line SL.

Selection 1 out of 28 tubes and 7 is tube S! It is supplemented by other low grade 7t supplied by. O-coatus furnace gasoline from steam cracking for ethylene production, gas spray gasoline fraction It is recognized that this is the case and is being considered in an OII-like manner.

With the exception of the lift gas at the bottom of riser 26 and the use of pyrolyzed gasoline as a feedstock, the operation of the FCC unit is essentially conventional. The FCC decomposition products are separated from the catalyst at the top of riser 26. This pipe may be of a riser section with an outlet at I11.
The catalyst is sent to a riser cyclone separator 84 and the suspended catalyst is separated into leg 8h and returned to vessel 81. The generated steam is sent from the cyclone 84 to a transfer pipe 86 for public guests.

The separated catalyst in vessel 88, including that discharged from the top of standpipe 26 and that from spout 8b, is transferred to vessel 88.
The volatile hydrocarbons fall through eight strippers at the bottom of the tube, where the volatile hydrocarbons are evaporated by the water vapor Ow'j introduced through tube 88. The stripped catalyst is sent via pipe 811 to a regenerator for coke combustion over the catalyst with air injected via pipe 4o. The waste gases resulting from the combustion of coke on the catalyst are discharged through a pipe 41, and the high temperature regenerated catalyst is returned to the riser pipe through a valve 42 (two pipes).

In the floor desk form of the present invention, pyrolyzed gasoline is
Injection into the CC riser reactor falcon and above 460″F
We are considering injection of boiling heavy charge. All of this operation converts low octane gasoline to LPG and high octane gasoline at a high catalyst/oil ratio over freshly regenerated catalyst. 11, the pyrolyzed gasoline becomes a lifting gas that is compatible with the cracking catalyst. The use of steam for this purpose severely damages the catalyst due to the harmful effects of high-temperature carbon steam.

The preferred apparatus for single fraction injection from tube 80 is shown schematically. Loading material from pipe 80 is supplied to ring manifold 4s around standpipe 2. A large number of nozzles 44 (
(four shown in the embodiment) are arranged symmetrically around the center of the riser pipe 26 and feed the material into the riser pipe, where the material is poured into the gasoline injected through pipe no. Me is injected upward into the upper and outer tubes together with the gasoline conversion products. Many nozzles 4
4 is directed inward and upward of the riser pipe 6 so that the injected streams from the nozzles intersect at a common point approximately on the center line of the riser pipe.

Table (Easy drawing 11!@) Figure 1 is a schematic diagram of the apparatus involved in implementing the present invention.

FIG. 2 is a diagram showing a nozzle for injecting raw materials into the riser of the present invention.

Number 4 #l in the diagram, laziness riser z, sss device $ burner 8.84iP'' return 18 minutes lN tower im, Fengden 44 nozzle FIG, 2 procedural correction view (method) % formula % 1, incident display 1986 Patent Application No. 22906 2, Name of the invention: 1m method a of FCC charging by selective evaporation, Relationship with @jEt Suiken case Name of patent applicant: Engel 11-de Coboreci Incident (2)
Drawing 6 of application form Kli, content of extraction

Claims (1)

[Claims] 1. Crude oil or residual oil feedstock containing high-boiling column parts contaminated with metals, high carbon contents, or both are processed in a closed column at high temperatures and with a short residence time of hydrocarbons. contact with an inert solid fine powder contacting material under strict decomposable conditions and separating the vapor produced by said contacting from said contacting material with combustible deposits of non-vaporizing high Conradson carbon or high metal content components of said raw material; The product vapor is then quenched to a temperature substantially below the temperature at which thermal decomposition occurs, and the quenched product is boiled at a temperature below about 450'F.
The naphtha fraction is fractionated into a heavy fraction with a boiling point above the naphtha fraction and 511[deg.], and the naphtha fraction is injected into the bottom of a catalytic cracking riser reactor and carbonized in the reactor A closed column in which hydrogen rises is produced, an active fine powder catalyst for decomposition is injected into the reactor, and the catalyst is dispersed within the sealing force of the rise in the hydrocarbons, and The catalyst dispersed in the rising closed column is injected at a point above the point where the upper 7-distillate fraction is injected, and the vapor produced by catalytic cracking is separated from the catalyst at the top of the riser reactor. A method for producing plenum products from crude oil or residual oil feedstocks containing high-boiling columnar parts contaminated with metals and high carbon content. 8. Vertical tubular rising contact arc above - means for introducing a hydrocarbon charge into the bottom of the contactor; means for introducing an inert hot fine powder contact material into the bottom of the contactor; means for separating the contacting substances, a fractionator, means for transferring said separated product vapor to said fractionator for fractional distillation, said fractionator to separate the glass fraction and the boiling point fraction; Means for taking out, vertical tubular cracking reactor, above 7'1
means for introducing the 1″ fraction into the bottom of the cracking reactor, means for putting a high-temperature fine powder cracking catalyst into the bottom of the cracking reactor, and means for putting the bottom fraction into the split reactor at the bottom of the cracking reactor. of a plenum product from a heavy hydrocarbon charge containing high Conradson carbon or metals, characterized in that Production equipment. 8. In the riser pipe cracking method in which the hydrocarbon charge is brought into contact with the activated fine powder cracking catalyst at a high temperature with an increasing sealing force, the high temperature active catalyst and pyrolyzed gasoline are subjected to a riser pipe reaction. The catalyst dispersed in the gasoline in the bottom of the machine generates an increasing sealing force of 2 m and about 450″F.
4. Injecting the charged raw material boiled above into the ascending closed column at a point above the point where the catalyst and the pyrolysis gasoline were introduced; Gasoline and distillate gas oil are separated from the residual oil fraction having Low cracking conditions with an inert surrounding material having no catalytic cracking microactivity and a temperature of at least about 900"F for a period of less than 3 seconds and less than the time to cause substantial thermal cracking of the residual oil fraction. at the end of said inert body, separating a decarburized resid fraction having a reduced Conradson carbon number than said resid fraction from said inert body; the crude oil obtained by reducing the temperature of the crude oil to a temperature substantially below that at which pyrolysis occurs and adding said decarburized residual fraction to said distillate gas oil as an additional charge for said catalytic cracking. In the method of manufacturing pre-oam products from
The normal liquid Nafuna fraction, which boils below about 450"F, and the heavy fraction, which boils in a higher temperature range than the 7-V' fraction, mentioned above. After fractional distillation, the above seven fractions are injected into the bottom of a riser reactor for catalytic cracking to create a closed column in which hydrocarbons rise inside the reactor, and fine catalyst powder for active cracking is injected into the reactor. and dispersing the catalyst in the increasing confinement force 2m of hydrocarbon;
The above-mentioned heavy fraction is injected into a closed column in which a catalyst dispersed in hydrocarbons rises at a point above the point where the above-mentioned 7-distillate fraction is injected, and the top IS of the upper single-tube reactor is An improved method characterized in that the vapor produced by catalytic cracking is separated from the catalyst. 5. Claim V, wherein said stringent conditions are such that the amount of said decarburized residual oil fraction is less than said residual oil fraction by a weight percentage not exceeding 8 times said Conradson carbon number. ! The method described in Section A 4, etc.