JP2003517491A - Improved fluid catalytic cracking process for converting hydrocarbon mixtures - Google Patents

Abstract

  (57) [Summary] The present invention relates to a fluid catalytic cracking process performed in a fluid catalytic cracking unit (FCCU), which comprises at least one riser having a plurality of injection nozzles and at least one raw material (α). Including at least one reaction zone including a step of spatially non-uniformly injecting a plurality of raw materials including two other raw materials (β), wherein the raw materials (α) and (β) are (a) Conradson The residual carbon differs by at least about 2 wt% points, (b) the hydrogen content differs by at least about 0.2 wt%, (c) the API weight differs by at least about 2 points, and (d) the nitrogen content Differ by at least about 50 ppm, (e) differ by at least about 0.3, or (f) have an average boiling point of at least about 200 ° F. The different, yet spatially non-uniform injections include: (i) the feed (α) from at least one injection nozzle of the riser and the feed from the remaining nozzles of the riser into a single reaction zone in a single riser. (Ii) simultaneously injecting the raw material (α) into at least one reaction zone of the FCCU riser and the raw material (β) into another reaction zone of the FCCU riser; or (Iii) Achieved by simultaneously injecting the raw material (α) into at least one riser of the FCCU and the raw material (β) into the second riser of the FCCU, and wherein spatially non-uniform injection is performed (iii). When achieved by the above, the feed is a substantially non-paraffinic feed.

Description

Detailed Description of the Invention

[0001]Field of the invention   The present invention relates to liquid fuels and light olefins from liquid hydrocarbon mixtures such as petroleum fractions.
It relates to fluid catalytic cracking (FCC) for producing fins. More specifically, the present invention provides
Improved FCC process especially for converting hydrocarbon mixtures using process non-linearity
Regarding

[0002]BACKGROUND OF THE INVENTION   The FCC process has been, and is now, a major conversion process in oil refining.
It will continue to be such a process for quite some time thereafter. Typical present
In existing FCC processes, the liquid feedstock mixture is sprayed from a nozzle to a line.
A droplet is formed at the bottom of the screen. The droplets contact the hot regenerated catalyst, vaporize and decompose.
To produce a light product and coke. Evaporated product rises up the riser.
The catalyst is separated from the hydrocarbon stream by a cyclone. Once separated, the catalyst
Removed hydrocarbons absorbed by the steam stripper, then burned out the coke
Sent to the playback device. The product is sent to a fractionator to produce several products.
Fractionated. Once regenerated, the catalyst is then sent back to the riser. Riser
In the integrated device of the regenerator and the regenerator, the heat is balanced and it is generated by burning the coke.
The generated heat is used for vaporization and decomposition of the raw material. By far the most common FCC feedstock is about 6
Gas oil or vacuum gas oil (VGO) which is a mixture of hydrocarbons with boiling points above 50 ° F.
). At the refinery, transfer heavy, highly contaminated oil such as residual oil.
In general, a small amount of such heavy oil is mixed with the gas oil feedstock when it needs to be converted.
Be done. In the petroleum industry, the FCC
There is a tendency that increasingly heavy pollutant feedstocks have to be converted. This
Raw materials include nitrogen, sulfur, metals, polycyclic aromatics and Conradson residual carbon (CC
Containing high levels of pollutants such as R, an index of asphaltene content). Below, heavy
The term quality components includes residual oil, deasphalted oil, lubricating oil extract, tar.
Including highly contaminated hydrocarbons such as sand, coal liquefied oil, and the like
Used. Such heavy components are added to other raw materials with less heavy components,
It becomes a raw material for FCC. Such heavy components will be an important part of FCC feedstock in the coming years.
Will be part.

The technical challenges faced by FCC feedstocks containing heavy components have been reviewed by Otterstedt et al. (Otterstedt, JE, Gevert, S.
． B. , Jaras, S .; G. And Menon, P .; G. , Applied
Catalysis, 22, 159, 1986). The main challenge in their high yields of coke and gas, catalyst deactivation, and SO _X in the flue gas. The coke forming propensity of these heavy ingredient containing feedstocks has traditionally been evaluated by CCR content. VGO feedstocks typically contain less than 0.5 wt% CCR. On the other hand, the atmospheric and vacuum residues are typically 1-15 wt% and 4-
Contains 25 wt% CCR. Since the decomposition of these heavy components produces levels of coke much higher than the existing FCC unit's required or limit values, the maximum allowable level of heavy components in the FCC is often the unit's coke. Limited by burning capacity. Currently, many FCC units have only 5
Only 15 wt% of residual oil, that is, heavy components can be decomposed. From the viewpoint of raw material price, there is a strong demand for an economical method that can increase the allowable operating range of FCC and increase the amount of heavy components that can be used for raw materials processed by existing FCC equipment. There is.

In FCC, a substantial fraction of the cracking and coking of the catalyst occurs at the bottom of the riser where the feed is injected through multiple nozzles. Current FCC feedstock injection equipment typically consists of an annulus around the riser wall with 6-10 nozzles.
These nozzles can be at the same height or in two rows, one above the other.
If the FCC feedstock contained heavy components such as residual oil, according to standard practice, the heavy components were premixed with the gas oil and the resulting mixture was injected through all nozzles. A major achievement in FCC has been to improve spray morphology to minimize catalyst-to-oil ratio variations in riser cross sections. The reason for this is that raw material nozzles that form a flat fan of liquid are widely accepted today (RJG).
lending, T.W. Y. Chan, and C.I. D. Fochtman, N
PRA Paper AM-96-25, San Antonio, Texas
, March 17, 1996).

Much work has also been devoted to improving the selectivity of decomposition by separating the raw materials. For example, in U.S. Pat. No. 3,424,672, gasoline yield was improved by cracking topped crude oil and low octane reformed gasoline in separate risers. U.S. Pat. No. 3,617,496 improves gasoline selectivity by fractionating an FCC feed into low and high molecular weight fractions and then cracking the fractions in a separate riser reactor. did. In U.S. Pat. No. 3,448,037, straight run gas oil and cracking recycle gas oil were each cracked in separate reaction zones to highly recover gasoline products. In U.S. Pat. No. 3,993,556, heavy and light gas oils were cracked in separate risers to improve the yield of high octane naphtha. For recovering highly volatile gasoline, high octane mixed base stocks, and light olefins for alkylation, U.S. Pat. No. 3,928,172 discloses gas oil feedstock and heavy naphtha and / or straight run naphtha fractions. It has been proposed to decompose the in a separate decomposition zone. In U.S. Pat. No. 3,801,493, gas oils, top crude oils and the like, and slack wax are cracked in a separate riser to produce a light cycle gas oil fraction for furnace oils and for vehicle fuels. A suitable high octane naphtha fraction was recovered. U.S. Pat. No. 5,009,769 discloses that a first riser decomposes naphtha and a second riser decomposes gas oil and residual oil. To improve conversion to gasoline and olefins, US Pat. No. 5,565
, 176, separate cracking of the paraffin-rich fraction and the CCR-rich fraction is disclosed.

The market demands for producing high octane gasoline have largely led to prior art research. What is needed in the art is a method that can increase the use of alternative feedstocks, including heavy components by way of example, and can extend the operating limits of existing FCC units while improving yield.

[0007]Summary of the invention   Applicants have found that non-linear phenomena in FCC are related to FCC processes and raw materials.
It has been found that this leads to improvement of the injection method. In particular, the applicants have
Heavy components in raw materials (for example, residual oil, deasphalted oil, lubricating oil extract,
When the amount of tar sand, coal liquefied oil, etc.) increases, the liquid yield deteriorates linearly.
It was found that there was no increase in coke yield and there was no linear increase in coke yield.
Physically, this is the marginal effect of the raw material contaminants on the FCC catalyst.
The sound is meant to become weaker as the amount of heavy components increases.
Therefore, according to the present invention, an improved F for decomposing FCC feedstocks containing heavy components
A CC process and feedstock injection method are provided. In one embodiment of the invention
, At least one nozzle in the device is used to inject the first raw material,
The remaining nozzles in the equipment are used to inject a second raw material of different quality.
It In another embodiment, two separate risers convert the two feeds separately.
Used for. In yet another embodiment, the riser is divided into two sections,
Decomposition of the feed is divided into at least a portion of the riser. Prior art methods and ratios
In comparison, the present invention results in higher total liquid yield and lower coke selectivity.
To be done. As shown in the examples, at least one containing Conradson carbon residue
The advantage of using these raw materials is that the conversion rate is lower than that of the raw materials with high CCR.
The origin of the CCR raw material is that it increases the conversion to a much higher degree.

Accordingly, the present invention relates to a fluid catalytic cracking process carried out in a fluid catalytic cracking unit (FCCU), the process comprising one or more risers having a plurality of injection nozzles and at least one feedstock ( including at least one reaction zone including a step of spatially non-uniform injection of a plurality of raw materials including α) and at least one other raw material (β), and the raw materials (α) and (β) Whether (a) the Conradson residual carbon differs by at least about 2 wt% points, (b) the hydrogen content differs by at least about 0.2 wt%, or (c) the API weight differs by at least about 2 points. d) the nitrogen content differs by at least about 50 ppm, (e) the carbon hydrogen ratio differs by at least about 0.3, or (f)
The average boiling points differ by at least about 200 ° F., and the spatially non-uniform injection is: (i) into a single reaction zone in a single riser, from at least one injection nozzle of the riser (Α) and the raw material (β) are simultaneously injected from the remaining nozzle of the riser, (ii) the raw material (in the at least one reaction zone of the FCCU in the riser).
α) and the raw material (β) into the other reaction zone of the riser of the FCCU at the same time, or (iii) the raw material (α) and the FCCU of at least one riser of the FCCU. The raw material is substantially non-paraffinic when achieved by simultaneously injecting the raw material (β) with a second riser and when the spatially non-uniform injection is achieved by (iii). It is a quality raw material.

Such an operation results in a high overall conversion and a low coke make selectivity. This advantage translates into a higher cracking capacity for heavy component-containing feedstocks at a constant liquid yield.

The present invention additionally provides for the selection of two feedstocks α and β in a fluid catalytic cracking unit (FCCU) for use in a fluid catalytic cracking process, for a given liquid yield increase and a given coke make. Defining a method for obtaining a reduction in the flow rate, the method comprising injecting the feedstocks α and β non-uniformly, the spatially non-uniform injection further comprising: (I) simultaneously injecting the raw material (α) from at least one injection nozzle of the riser and the raw material (β) from the remaining nozzles of the riser into a single reaction zone in a single riser, (ii) ) The raw material is provided in at least one of the reaction zones in the riser of the FCCU (
α) and the raw material (β) into the other reaction zone of the riser of the FCCU at the same time, or (iii) the raw material (α) and the FCCU of at least one riser of the FCCU. Achieved by simultaneously injecting the raw material (β) into a second riser, and the selection was done by creating a conversion rate vs. coke make diagram for the raw material quality index from which the liquid yield increase And reduction of coke make are achieved by selecting two feedstocks equal to the given increase and decrease indicated by DF and GE in FIGS. 1a and 1b, respectively, and the feedstock (α) (Β
) Means that (a) the Conradson residual carbon differs by at least about 2 wt% points, (b) the hydrogen content differs by at least about 0.2 wt%, or (c) AP.
I weights differ by at least about 2 points, (d) nitrogen contents differ by at least about 50 ppm, (e) carbon hydrogen ratios differ by at least about 0.3, or (f) average boiling points are at least about They differ by 200 ° F.

The present invention further defines a fluid catalytic cracking process carried out in a fluid catalytic cracking unit (FCCU), the process comprising one or more risers having a plurality of injection nozzles and at least one feedstock ( α) and at least one other raw material (β), and at least one reaction zone including a step of spatially non-uniform injection of a plurality of raw materials, wherein the raw materials (α) and (β) are , (A) the Conradson residual carbon differs by at least about 2 wt% points, (b) the hydrogen content differs by at least about 0.2 wt%, (c) the API weight differs by at least about 2 points, (d) ) Nitrogen content differs by at least about 50 ppm, (
e) the carbon-hydrogen ratios differ by at least about 0.3, or (f) the average boiling points differ by at least about 200 ° F., and the spatially non-uniform injection is: (i) a single riser Simultaneously injecting the raw material (α) from the at least one injection nozzle of the riser and the raw material (β) from the remaining nozzles of the riser into a single reaction zone in (ii) the riser of the FCCU. In at least one of the reaction zones in
α) and the raw material (β) into the other reaction zone of the riser of the FCCU at the same time, or (iii) the raw material (α) and the FCCU of at least one riser of the FCCU. This is achieved by simultaneously injecting the raw material (β) into a second riser, and the raw materials (α) and (β) are prepared by forming a conversion rate diagram and a coke make diagram with respect to the raw material quality index. From the figure, an increase in liquid yield and a decrease in coke make are selected by selecting two feedstocks equal to the given increase and decrease indicated by DF and GE in FIGS. 1a and 1b, respectively.

As used herein, the given increase in liquid yield and reduction in coke make will be obtained when the two feedstocks are mixed before being injected into the riser of the FCC unit. It is an increase or decrease with respect to one.

[0013]Detailed Description of the Invention   The present invention can be used in laboratory and / or small-scale equipment designed in the usual way.
It can be more easily understood from the drawings that are easily obtained by: In Figure 1
, The non-linear dependence of conversion and coke yield on the residual oil content in the feedstock
Indicated. The conversion curve is convex, whereas the coke yield curve is
It has a concave shape. For example, the coke burning capacity of an FCC unit depends on the maximum allowable content of residual oil.
Is 10 wt%, refineries usually use 10 w of residual oil in VGO.
A feedstock containing t% (point C in FIG. 1a) is fed to the device. In the present invention, completely different
An approach is used. Rather than trying to make the oil composition uniform across the riser
Rather, the present invention requires a spatially non-uniform implantation scheme. Implementation of the present invention
In the form, a considerable number of nozzles of the FCC device are used to inject the heavy component rich raw material.
The remaining nozzles are used to inject the heavy component lean raw material. Rich ingredients
, Having a high Conradson carbon value. For example, 10 nozzles
Suppose we have a hypothetical FCC riser. Straight run VGO to 6 adjacent nozzles
Pour, while pouring the VGO mixture containing 25% residual oil into the remaining 4 adjacent nozzles.
You may enter. This means that when all nozzles have the same flow rate
This means that the concentration is 10%. But all other possible schemes
The nozzles need not have the same flow rate. If the mixing speed is finite,
These two streams remain locally separated in the region downstream of the injection zone.
Let's do it. In such an area, the system is as if there were two risers.
Behave. Does most cracking and catalyst coking occur near the feed injection zone?
The conversion and coke yield obtained in the zone by the decomposition of the two streams are
And is represented by the points A'and B'in FIGS. 1a and 1b.
it can. The mixture of the two products is indicated by points D and E, respectively, with total conversion and
Represents coke make. Separation of raw material injection compared to points F and G
Shows that a high total conversion and a low coke make are obtained. This advantage
As for the conversion of the heavy component rich raw material, the conversion rate decreases, but the conversion of the heavy component lean raw material
It derives from the fact that it is greater than compensated by the increase in rates. Changing perspectives, raw materials
Separation of injections protects most of the catalyst at the expense of a small portion of the catalyst
To be done. The net effect is increased conversion and reduced coke selectivity.

Those skilled in the art will know how to select raw materials that can be used in the present invention in relation to the present invention. In essence, the raw material is selected from the conversion to raw material quality index and the non-linear curve of coke make. The feedstock quality index is, for example, the wt% residual oil shown in Figures 1a and 1b, or the wt% feedstock hydrogen shown in Figure 3b. As mentioned above, these figures can be obtained a priori in routine small scale experiments. Understanding the residual oil capacity of an FCC unit helps to select the two feedstocks (α) and (β) used in the present invention. For example, if one predicts that a 3 wt% increase in liquid yield is desired, any two feedstocks that result in a 3 wt% increase [see, for example, (DF) in FIG. Will be selected.] Will be selected. Preferably, the increase in liquid yield is at least about 0.5 with respect to the feed.
%, and the reduction in coke make is at least about 0.
It will be 2 wt%. The wt% reduction in coke yield would be represented by G-E in Figure 1b. By selecting two such raw materials, a liquid product mixture (D) obtained by separately cracking the two raw materials is obtained when the two raw materials are first mixed and then cracked. It's higher than the one (F). Note that any raw material quality index is used to create the diagram. For example,% residual oil, hydrogen content, AP
I weight, nitrogen content, C / H ratio, and boiling point. Diagrams will typically be made using at least three sources. For injection systems using two separate risers, preferably the feedstock is substantially non-paraffinic. In addition, the substantially non-paraffinic feedstock may be used in any of injection modes (i)-(iii). As used herein, substantially non-paraffinic refers to Wats
A raw material having a K factor of on of less than 12.2. More preferably, injection schemes (i) and (ii) using a single riser will be employed.

[0015]   The variety of raw materials that can be selected is easily understood from the above discussion.

For example, referring again to the above hypothetical case, straight run VGO may be injected into seven nozzles, while mixed oil containing 20% residual oil in VGO may be injected into the remaining three nozzles. . The desired total residual oil concentration, for example, 10 wt% can be obtained by adjusting the feed rate of the raw materials into the two sets of nozzles. As a result, the local catalyst-to-oil ratios for the two streams will be different, which will optimize the cracking of each stream individually.

Preferably, in the nozzle, the raw material (α) is injected through an adjacent nozzle, and the raw material (α)
β) will be selected so that it is injected through the adjacent nozzle. In fact, the more the raw materials (α) and (β) are separated, the more effective this process is.

The two feed streams can be injected into the two reaction zones of the riser obtained by splitting at least the bottom of the riser.

If the FCC unit in question has two risers, then separate risers can be used according to the invention for cracking the separate feeds (α) and (β).

[0020]   The process uses FCC conditions and catalysts known to those skilled in the art.

From the above discussion, it is believed by Applicants that the advantages of the present invention result from the bumpy behavior illustrated in FIGS. 1a and 1b. Therefore, the following illustrative, non-limiting examples were obtained in experiments aimed at clarifying the ruggedness response to changes in the level of heavy components in the feed for various feed materials, catalysts and cracking conditions. It was FIG. 1 shows that wt% residual oil in the feedstock is used as a measure of the heavy feedstock component level, while other measures can also be used. Some are, for example, CCR, hydrogen, nitrogen, polar substances and polycyclic aromatics, to mention a few.

The above is for the decomposition of heavy feedstocks, but those skilled in the art
It will be readily appreciated that the present invention is applicable to any pair of raw materials, as long as the raw material properties are sufficiently different. For example, the feedstock pair may include a naphtha rich base and a naphthalene base for maximum olefin production. As a non-limiting example of a raw material property scale, with respect to raw materials having a CCR difference of less than 2 wt% or containing no CCR (including a heavy component-containing raw material containing no CCR),
Hydrogen content (by at least about 0.2 wt% different), carbon hydrogen ratio (by at least about 0.3 different), API weight (by at least about 2 points different), nitrogen content (by at least about 50 ppm different), intermediate Boiling point (at least about 20
0 ° F is different) and the like. If only one of the feedstocks used has CCR, that feedstock has about 2 wt% CCR as compared to other feedstocks without CCR.
The inclusion of the above or any of the other measures satisfy the criteria of the present invention. If at least one ingredient comprises CCR, the ingredient is AP
It may be preferred that the I weights differ by at least about 3 points. Preferably, only two raw materials will be used.

[0023]   The desired non-linearity is observed in all the examples presented below.

Example 1 In this series of experiments, pure VGO and VGO and vacuum resid (VR) were used.
Two raw material mixed oils containing and were prepared (one containing 16 wt% of residual oil and the other containing 32 wt%). In Table 1, the properties of the raw material mixed oil are described at the levels of CCR (wt%) and intrinsic nitrogen (wppm). An equilibrium catalyst impregnated with Ni at 3500 ppm was used.

[0025]

[Table 1]

Decomposition experiments were carried out in an FCC pilot unit at 515 ° C. and catalyst to oil (C /
O) performed at a ratio of 8. During operation, catalyst is metered into the riser from the regenerated catalyst hopper using a screw feeder. The heated catalyst contacts the incoming oil and gaseous nitrogen and rises up the riser where the oil is cracked. At the end of the riser, spent catalyst and reactor product enter the separation zone. Here, the gas continuously flows overhead to enter the product recovery system and the catalyst descends the stripper into the waste catalyst hopper. The gaseous products are cooled, C ₅ ⁺ liquid product and C ₅ ^- to produce the product gas.

Since decomposition follows second-order kinetics, a measure of the degree of decomposition is the so-called kinetic conversion ξ. X ₄₃₀ is expressed as wt% conversion to <430 ° F. product on a coke-free basis, ξ ₄₃₀ = X ₄₃₀ / (100-X ₄₃₀ ).
The coke selectivity S is calculated as S = Y / ξ ₄₃₀ . Here, Y is the weight% coke yield with respect to the raw material. The straight conversion VGO and the% conversion of the VGO raw material containing 32% of VR are designated as X ₁ and X ₂ , respectively. The average kinetic conversion is ξ = (X ₁ +
X ₂ ) / 2 / [100− (X ₁ + X ₂ ) / 2] and the corresponding average coke selectivity is S = (Y ₁ + Y ₂ ) / 2 / ξ.

[0028] Figures 2a and 2b show coke-free kinetic conversion to <430 ° F and <650 ° F products as a function of residual oil content of the total feed, respectively. In Figure 2c,
A similar plot for coke yield is shown. From these plots, the average kinetic conversion and coke selectivity can be determined. 2a to 2c, ξ (<
It can be seen that the 430.degree. F. and <650.degree. F. product conversions) are higher and the S is lower than that obtained from the VGO feed containing 16% VR. Each data point is the average of two or three runs. In particular, the cokeless kinetic conversions of 430 and 650 were improved by 5.3% and 7.5%, respectively. That is, for the 430 cokeless kinetic conversion, the ξ to ξ ratio (for VGO feed containing 16% VR) is 1.053. The coke selectivity is 12.2.
% Lower.

Example 2 The above experiment was repeated with a C / O of 5. It was observed that the 430 and 650 kinetic conversions increased by 10.2% and 11.7%, respectively. further,
The coke selectivity is 9.3% lower.

Example 3 The experiment shown in Example 2 was repeated at 650 ° C. and C / O 5. in this case,
The 430 and 650 kinetic conversions were improved by 3.7% and 4.9%, respectively.
Also, the coke selectivity decreased by 21.5%.

Example 4 In this case, the catalyst used was the same as in Example 1, except that it was not impregnated with Ni. The decomposition conditions are 5 C / O and 515 ° C. 430 and 650 kinetic conversions increased by 8.9% and 10.7% respectively, coke selectivity 4.4%.
Diminished. The propylene yield is improved by 6.5%.

Example 5 The raw material components used in this example are hydrotreated VGO (HTGO) and butane deasphalted residual oil (DAO). Table 2 describes the composition and properties of the raw material mixed oil.

[0033]

[Table 2]

Decomposition experiments were carried out on an equilibrium catalyst different from the one used in Example 4 at 530 ° C., 8
It was done by C / O. The 430 and 650 kinetic conversions were 4.9% and 1 respectively.
It improved by 0.8%. Coke selectivity is reduced by 7.4%.

Example 6 Vacuum gas oil was separated by solvent extraction into different fractions with varying hydrogen content. These resulting fractions were each cracked with several commercial catalysts (designated as Catalysts A, B and C) at 496 ° C., 6.5 C / O and an oil rate of 80 g / m 2. Table 3 describes the properties of these catalysts. The hydrogen content of the raw material was used as a measure of raw material quality. The data shown in Figures 3a to 3h show that the hydrogen content is 10.4, 1
Obtained for raw materials that are 2.1, 13.6, and 13.8 wt%. The results shown in the figure clearly show the desired non-linearity.

[0036]

[Table 3]

[Brief description of drawings]

FIG. 1a represents conversion as a function of wt% bottoms in total feed.             FIG. 1b represents coke yield as a function of wt% bottoms in total feed.

FIG. 2a represents cokeless kinetic conversion (515 ° C., 8 C / O) to <430 ° F. product for wt% bottoms feedstock. FIG. 2b represents cokeless kinetic conversion (515 ° C., 8 C / O) to <650 ° F. product for feed wt% bottoms. FIG. 2c shows the coke selectivity for the raw material wt% residual oil (515 ° C., 8 C).
/ O).

FIG. 3a is a conversion of <430 ° F. product to wt% feed hydrogen (
496 ° C., 6.5 C / O, represents catalyst A). Figure 3b shows conversion to <430 ° F product for wt% feed hydrogen (
496 ° C., 6.5 C / O, represents catalyst B). FIG. 3c shows a coke yield (496 ° C., 6.5 C) with respect to wt% of raw material hydrogen.
/ O, catalyst C). FIG. 3d shows the propylene yield (496 ° C., 6.
5C / O, catalyst B). FIG. 3e is a distillate oil yield (496 ° C., 6.5 C, based on wt% raw material hydrogen).
/ O, catalyst C). Figure 3f shows naphtha yield (496 ° C, 6.5C) with respect to wt% of raw material hydrogen.
/ O, catalyst C). Fig. 3g shows a bottom oil yield (496 ° C, 6.5C) with respect to wt% of raw material hydrogen.
/ O, catalyst C). FIG. 3h shows a butylene yield (496 ° C., 6.5% with respect to wt% raw material hydrogen).
C / O, catalyst C).

[Procedure for Amendment] Submission for translation of Article 34 Amendment of Patent Cooperation Treaty

[Submission date] July 14, 2000 (2000.7.14)

[Procedure Amendment 1]

[Document name to be amended] Statement

[Name of item to be amended] Claims

[Correction method] Change

[Contents of correction]

[Claims]

9. The process of claim 1, wherein the feedstocks (α) and (β) are injected according to step (i).

[Procedure amendment]

[Submission date] December 12, 2001 (2001.12.12)

[Procedure Amendment 1]

[Document name to be amended] Statement

[Name of item to be amended] Claims

[Correction method] Change

[Contents of correction]

[Claims]

─────────────────────────────────────────────────── ─── Continued front page    (81) Designated countries EP (AT, BE, CH, CY, DE, DK, ES, FI, FR, GB, GR, IE, I T, LU, MC, NL, PT, SE), CA, JP (72) Inventor Hwang Shun Chung             New Jersey, United States             08807 bridge water pay pen             Road 855 (72) Inventor Stunts Gordon Frederick             Louisiana, United States 70816             Baton Rouge Lake Lingham             Circle 12217 (72) Inventor Welch Robert Charles Willi             Am             70808-Louisiana, United States             5122 Bayton Rouge Woodruff             Drive 542 (72) Inventor Letta Daniel Paul             New Jersey, United States             08822 Flemington Rustic             Rail 15 F-term (reference) 4H029 BB03 BD08 BD20

Claims (10)

[Claims] 1. One or more risers having a plurality of injection nozzles, and spatially non-uniform injection of a plurality of raw materials including at least one raw material (α) and at least one other raw material (β). A fluid catalytic cracking process (FCCU) comprising at least one reaction zone comprising the steps of:
The raw materials (α) and (β) are such that (a) Conradson residual carbon is at least about 2 wt.
% Difference, (b) hydrogen content difference of at least about 0.2 wt%, (c) API weight difference of at least about 2 points, or (d) nitrogen content difference of at least about 50 ppm. , (E) the carbon-hydrogen ratios differ by at least about 0.3, or (f) the average boiling points differ by at least about 200 ° F., and the spatially non-uniform implants are: Simultaneously injecting the raw material (α) from at least one injection nozzle of the riser and the raw material (β) from the remaining nozzles of the riser into a single reaction zone in one riser, (ii) In the at least one reaction zone of the riser, the raw material (
α) and the raw material (β) into the other reaction zone of the riser of the FCCU at the same time, or (iii) the raw material (α) and the FCCU of at least one riser of the FCCU. The raw material is substantially non-paraffinic when achieved by simultaneously injecting the raw material (β) with a second riser and when the spatially non-uniform injection is achieved by (iii). A process that is a quality ingredient. 2. A fluid catalytic cracking unit (FCCU) for selecting two raw materials α and β for use in a fluid catalytic cracking process to obtain a given liquid yield increase and a given coke make reduction. Of the raw material α
And β are non-uniformly injected, wherein the spatially non-uniform injection further comprises: (i) into a single reaction zone in a single riser from at least one injection nozzle of the riser; (Α) and the raw material (β) are simultaneously injected from the remaining nozzle of the riser, (ii) the raw material (in the at least one reaction zone of the FCCU in the riser).
α) and the raw material (β) into the other reaction zone of the riser of the FCCU at the same time, or (iii) the raw material (α) and the FCCU of at least one riser of the FCCU. Achieved by simultaneously injecting the raw material (β) into a second riser, the selection producing a plot of conversion versus raw material quality index and a plot of coke make from which the increase in liquid yield and Reduction of coke make is achieved by selecting two feedstocks equal to the given increase and decrease indicated by DF and GE in FIGS. 1a and 1b, respectively, and the feedstocks (α) and ( β) differs from (a) Conradson residual carbon by at least about 2 wt% points,
(B) the hydrogen content differs by at least about 0.2 wt%, (c) the API weight differs by at least about 2 points, or (d) the nitrogen content is at least about 50.
ppm differences, (e) carbon hydrogen ratios differ by at least about 0.3, or (f) mean boiling points differ by at least about 200 ° F. 3. One or more risers having a plurality of injection nozzles and spatially non-uniform injection of a plurality of raw materials containing at least one raw material (α) and at least one other raw material (β). In a fluidized catalytic cracking unit (FCCU) in which at least one reaction zone including the steps of: (a) Conradson residual carbon is at least about 2 wt%
Point difference, (b) hydrogen content difference of at least about 0.2 wt%, (c) API weight difference of at least about 2 points, (d) nitrogen content difference of at least about 50 ppm, (E) the carbon-hydrogen ratios differ by at least about 0.3, or (f) the average boiling points differ by at least about 200 ° F., and the spatially non-uniform implants are: (i) a single Simultaneously injecting the raw material (α) from at least one injection nozzle of the riser and the raw material (β) from the remaining nozzles of the riser into a single reaction zone in the riser, (ii) the FCCU In the at least one reaction zone of the riser, the raw material (
α) and the raw material (β) into the other reaction zone of the riser of the FCCU at the same time, or (iii) the raw material (α) and the FCCU of at least one riser of the FCCU. It is achieved by simultaneously injecting the raw material (β) into a second riser, and further, the raw materials (α) and (β) are used to prepare a conversion rate diagram and a coke make diagram with respect to the raw material quality index, From that figure, an increase in liquid yield and a decrease in coke make are selected by selecting two feedstocks equal to the given increase and decrease indicated by DF and GE in FIGS. 1a and 1b, respectively. process. 4. When at least one of said feedstocks (α) and (β) contains Conradson residual carbon, said feedstocks (α) and (β) differ in Conradson residual carbon by at least about 4 wt% points. The process of claim 1. 5. The API weights of the feedstocks (α) and (β) differ by at least about 3 points when at least one of the feedstocks (α) and (β) contains Conradson carbon residue. Process 1 6. The raw material (α) is injected through an adjacent nozzle, and the raw material (α)
The process of claim 1, wherein β) is injected through adjacent nozzles. 7. Where at least one of said feedstocks (α) and (β) is a feedstock containing Conradson residual carbon, said feedstock differs from said feedstock in that Conradson residual carbon differs by at least about 2 wt% points. The process of claim 1, wherein the process is injected through at least one fewer nozzle. 8. The process of claim 1, wherein the plurality of feedstocks comprises two feedstocks. 9. The quality of the raw materials (α) and (β) is measured by (a), (b), (c), (d), (e) or (f), and the difference becomes large. The process of claim 1 wherein the greater the liquid yield increase and the less coke make in the fluid catalytic cracking process. 10. The process of claim 1, wherein the raw materials (α) and (β) are injected according to step (i).