DE2063990B - Process for the catalytic cracking of gas oils - Google Patents

Description

a) maintaining a higher by 11 to 110 ° C temperature in at least one elongated reaction zone as in at least one other elongate ^ao reaction zone and

b) the one consisting of the gaseous reaction mixture and the catalyst, the elongated one The stream exiting from the reaction zones is passed into a catalyst layer located in the reactor will.

2. The method according to claim 1, characterized in that cracking is carried out in a two elongated reaction zones having fluidized bed catalyst cracking plant, wherein in the first elongated reaction zone at a higher, but not exceeding 625 ° C temperature and in the second elongated reaction zone at temperatures from 425 to 61O ⁰ C is cracked with a conversion of 30 to 80 percent by volume.

3. The method according to claim 2, characterized in that that the exiting from the first and second elongate reaction zone flows into one diluted catalyst layer are passed and the conversion per pass in the first elongated reaction zone by 0 to 35 volume percent lower than that in the second elongated Reaction zone kept wild.

4. The method according to claim 2, characterized in that the stream emerging from the first elongated reaction zone is passed into a dilute catalyst layer and the stream emerging from the second elongated reaction zone is passed into a dense catalyst layer, the gaseous reaction mixture from the second reaction zone under conditions for catalytic cracking is passed through the dense catalyst layer and an additional conversion of 5 to 30 volume percent is effected and the conversion per pass in the first elongated reaction zone is kept 0 to 35 volume percent lower than the conversion per pass resulting from the conversion Conversions in the second elongate reaction zone and in the dense catalyst layer composed, the total conversion in the second elongate reaction zone and the dense catalyst layer being kept below 80 percent by volume.

5. The method according to claim 2, characterized in that from the second elongate reaction zone exiting stream into a thinned catalyst layer and that from the first elongated The stream exiting the reaction zone is passed into a dense catalyst layer, the gaseous reaction mixture from the first elongated Reaction zone under conditions for catalytic cracking through the dense catalyst layer passed through and an additional conversion of 5 to 30 percent by volume is effected, the total conversion per pass in the first elongate reaction zone and the dense Catalyst layer lower than the conversion in the second elongated by 0 to 35 volume percent Reaction zone and is kept below 80 percent by volume.

6. The method according to claim 2, characterized in that from the first and second elongate Exiting streams under catalytic cracking conditions through a reaction zone dense catalyst layer are passed through and an additional conversion of 5 to 30 percent by volume is effected, the conversion per pass in the first elongated Reaction zone lower by 0 to 35 volume percent than that in the second elongated reaction zone and the total conversion of that passed through the elongated reaction zones and the dense layer Gas oil is kept below 80 percent by volume.

7. The method according to any one of claims 2 to 6, characterized in that 20 to 80 percent by volume of the gas oil in the first elongated reaction zone and the remaining gas oil in the second elongated reaction zone is directed.

8. The method according to any one of the preceding claims, characterized in that gas oil with a boiling range of 220 to 570 ° C is cracked.

9. The method according to any one of the preceding claims, characterized in that 40 to 60 percent by volume of the gas oil are passed into the first elongated reaction zone, the temperature in the first elongated reaction zone by 25 to 85 ° C higher and the conversion by 10 to 20 ° / _{0 is} lower than in the second elongated reaction zone and the temperature in the second elongated reaction zone is maintained at 445 to 540 ° C.

10. The method according to any one of the preceding claims, characterized in that the Gasö! from the group of heavy normal pressure distillation gas oil, light and heavy vacuum distillation Gas oil, broken in viscosity! Gas oil, deasphalted gas oil, decarbonized! Gas oil, hydrotreated gas oil and solvent-extracted gas oil is taken out.

11. The method according to any one of the preceding claims, characterized in that a zeo lithic cracking catalyst is used, de crystalline aluminum silicate and SiOJAI ₂ O _{3 contains} ent.

In fluidized bed catalyst cracking processes, hydrocarbons are converted under appropriate conditions gen converted, so that considerable proportions of de

3 4

Starting hydrocarbons in desired products, the catalyst is then returned to the lower end of the elongated gasoline, liquefiable propellant gas, starting material reaction zone or the "booster", namely where materials for alkylation and for blending the starting material are introduced, from middle distillates By using several boosters it is possible to develop less desirable substances 5 at the same time, the individual "boosters" under conditions such as gas and coke. As soon as substantial amounts of coke are to be operated, which deposit a maximum formation of the coke, causes a reduction in the desired products with simultaneous minimal deactivation of the catalyst and especially its formation of undesired products and maximum selectivity ensures a hindrance to the hydrocarbon yields. Conversion, a decrease in gasoline formation and the more heat-resistant starting materials, such as, for example, at the same time an increasing formation of the less circulating gas oils, are usually caused by the "increase" in the case of higher-desired products. In order to deactivate the higher temperatures, the »riser« works as the catalyst to balance the catalyst as a result of coke deposits, which processes the fresh gas oil. The whole thing, the catalyst is usually from the effect should of course consist of removing an optimal off-reaction zone and pulling a stripping zone using both the cracking system for work, where it is initially carried out by means of a stripping medium, a fluidized bed catalyst and zeolite Steam, to obtain from penetrated and adsorbed shear cracking catalyst.
Hydrocarbons is freed. The steam and although state-of-the-art devices and hydrocarbons are withdrawn, and the catalyst released from processes that utilize the unique properties of the latter is placed in a regeneration zone of the zeclithic cracking catalysts, where it is supplied with oxygenated gas. Nevertheless, improvements in the process are brought together to at least part of the desires that regenerate the utilization of the plant, including burning the coke and thus increasing the catalyst quality and / or the quantity of the products. Thereafter, the regenerated catalyst is brought back into the reaction zone and brought into contact with a fluidized bed of other hydrocarbons by operating a cracking plant. catalytic converter directed, with the most substantial portion Recently, the catalytic cracking processes in a number of elongated drives have been significantly improved. The introduction of reaction zones or "increase" takes place. With existing zeolite cracking catalysts, higher heavy gasoline yields have been achieved with higher cracking systems for increased throughput and lower octane ratings by converting the feed gas oil into improved product quality. In addition, "risers" are also conducted, with at least one "riser" operating in improved devices for catalytic cracking at a temperature that is higher than that specially developed for the use of this improved catalyst temperature in at least one other "riser" analyzer whereby the overall and the conversion in the reactor with process has been improved in its performance. For example, in U.S. Patents 3,433,733 in the lower temperature reactor and 3,448,037 processes for cracking petroleum passage are either equal to or less than it is. Hydrocarbons Using Fluidized Bed Catalysts In a preferred embodiment, a fluidized bed catalyst cracking unit using zeolite cracking catalysts is described with two. Work parameters and tech- 40 "increase" are used.

Techniques that draw specifically on these new catalytic converters- The invention is illustrated on the basis of two drawings

are sections and at the same time cracking systems explained in more detail for that.

Cracking with Fluid Bed Catalysts Using F i g. 1 gives the example of a device by means of

of the desired typical advantages of the zeolite- the process of the invention can be carried out Make catalysts, explained in more detail. The device 45 can;

management is geared towards the so-called »Steigcr-Krak-F i g. Figure 2 is a graphical comparison of ken "where the original feedstock and heavy gasoline yield and research octane number, recycle material separated in separate elongated ones obtained by cracking a fluidized bed catalyst reaction zone, called" riser ", are cracked after different cracking plants Working methods or the "Steiger" operates in tapered reaction chambers, two of which are based on the invention, end chambers, one dense and one dilute. It has been found that when operating one phase of the catalyst and in which a fluidized bed catalyst Cracking plant with a further cracking in the fluidized dense phase lithic cracking catalyst and a number of takes place. By means of "increase cracking" it is possible to "increase" substantial improvements by selecting the working conditions in such a way that they can be aimed at making the gas oil in the "increase" suitable for the respective starting material, namely subjecting the conditions to catalytic cracking , while lent to the gas oil or the circulating material that is introduced into one in the "risers" at different temperatures of each "riser". The cracking device maintains and the conversion of the gas oil into the additionally contains a stripping section below higher temperature "increase" those in the lower fluidized dense bed, in which penetrated 60 riger temperature "increase" is equal or lower) and adsorbed hydrocarbons by means of steam as the latter is. This mode of operation enables the catalyst to be removed before the catalyst is passed on to the regeneration vessel to generate higher yields of higher-octane gasoline. How do we keep up with similar institutions
in conventional equipment for working The invention relates to a method for catalyti with a fluidized bed catalyst, the catalyst 65 will see cracking of gas oils in the presence of a zeo in the regeneration tank with oxygen-containing gas in a lithic catalyst in one of a one tight! brought stirring in order to burn at least part of the beaten coke containing low and a dilute catalyst phase. The regenerated reactor, a regenerator and a number before

elongated reaction zones ending at the reactor is subjected to aerator phase. The stream from the standing fluidized bed cracking plant and whereby the lower tempered »riser« is directly entangled in the of the gas oil with the catalyst is accessible through the thin catalyst phase in the reactor vessel Reaction zones under conditions for conducts, while the flow from the higher tempered catalytic cracking are fed to the reactor, 5 "risers" under catalytic cracking conditions which is characterized in that it is passed through the dense catalyst phase where

converted by an additional 5 to 30 percent by volume

a) at least in one of the elongated reaction areas. With the combination of conversion in the zonen a temperature is maintained, the higher tempered "riser" and conversion in the 11 to 110 ⁰ C higher than the temperature in ¹⁰ dense phase are not converted over 80 percent by volume of at least one other elongated reaction, but this conversion is total zone and ¹ ^ ® ^ ^s ^ 5 volume percent less than that in that

lower tempered »Steiger«.

b) of from gaseous reaction mixture and _{in emer we} i _direct embodiment, the existing in the catalyst stream from the elongated ₁₅ two "riser" introduced gas oil to both the "sti reaction zone into a catalyst phase in the _eng" -Kracken and the cracking in the sealed reactor is passed. p _nose subjected by the current from both

"Boost" under catalytic cracking conditions

In the simplest embodiment of the invention passed through the dense catalyst phase with a fluidized bed catalyst cracking plant with two *> and thus an additional conversion of 5 to "increase" the temperature in which the higher tempe- 30 percent by volume is brought about. In this execution "riser" limited to 621 ⁰ C, while in the form in the higher tempered "riser" 0 to second "riser" the conditions of catalytic 35 volume percent less per pass are converted to a temperature of 427 to 610 ° C and one delt than in the lower tempered "riser", and the conversion of 30 to 80 percent by volume a "5 total conversion of all by the" risers "and the close. dense phase conducted gas oils does not exceed

The cracking of the gas oil both in the »Steiger« as 80 percent by volume.

Even in the fluidized dense phase, the fresh feed oil according to the invention comprises gas

Procedures can be varied, so that there are many variants of the oil types. Among these starting oils the most expedient embodiment are possible. A number of these variants used in the process according to the invention are briefly described with reference to a process that uses oil fractions with a boiling range of a two-stage system. 220 to 57O ⁰ C. These include heavy gas oils from the

In one embodiment, the cracking of normal pressure distillation takes place, light and heavy gas oils Gas oil only takes place in the »risers« by removing from the vacuum distillation, gas oils with broken Flow of both enhancers into the dilute catalyst viscosity, deasphalted gas oils, of carbon satorphase is passed in the reactor vessel, in freed gas oils, and hydrogen-treated gas oils the higher tempered "riser" per pass 0 to a solvent extraction subjected gas oils. 35 percent by volume less than in the lower tempe- All of these feed oils are original oils that were previously used ried »Steiger« can be converted. The reactor - not cracked with the help of fluid bed catalysts boiler in this case serves as a separation zone, in which only 40 were.

little or no cracking occurs. The catalyst used for the invention is included Another embodiment is made up of large-pore, crystalline, active metal oxides Gas-containing aluminum silicates, usually called the oil another crack in the dense catalyst zeolites, such as naphase subject. This is achieved by using trium-aluminum-süikat-gel or clay-like Mineman the electricity from the higher-temperature "Steiger" ralien. The in the process according to the invention as have zeolites used in the dilute catalyst phase and the cracking catalyst stream the lower temperature "riser" into the dense, geometrically regular, rigid three-dimensional structural catalyst phase conducts and the gaseous reaction doors with uniform pore diameters, which are in the mixture from the lower tempered »Steiger« 50 range from about 5 to 15 Å. The in the invention the dense catalyst phase under conditions according to procedures used crystalline zeocatalytic Cracking passes through, making a lithic catalysts consist of about 1 to 25 additional Conversion of 5 to 30 volume percent weight percent zeolite, about 10 to 50 weight percent takes place. In this embodiment, in the aluminum oxide and the rest of silicon dioxide, higher temperature "risers" 0 to 35 percent by volume 55 Among the preferred zeolites are the as less converted than the total conversion into zeolite X and zeolite Y known types in which the lower tempered "riser" and in the dense at least a substantial proportion of the original Catalyst phase is. The conversion in the alkali metal ions by cations such as hydrogen both the latter zone does not exceed 80 volume proportions, has been replaced and / or by metal ions cent out. By adjusting the working conditions or combinations of ions of such metals as The conversion can be carried out in the lower barium, calcium, magnesium, manganese or less often tempered "risers" lower, equal to or higher than earths such as B. cerium, lanthanum, neodymium, praseodymium, set in the higher tempered »riser«. Samarium and Yttrium.

In a further embodiment that is shown in the The invention provides that gas oil in each of the lowering tempered "Steiger" led gas oil single 65 different, differently tempered elongated subject to "step-up cracking" while passing the reaction zone. At the simplest from gas oil In the higher temperature "riser" and the guide form there are two elongated reaction zones Kracken is used in the »Steiger« as well as in the dense Kataly- or »Steiger«. The working conditions are

7 ^ 8

as follows: 20 to 80, preferably 40 to 60 volume per input materials and / or product requirements

percent of the feed oil is used in the lower tempe- a distribution in a different ratio than

ized »Steiger« initiated, which with temperatures nis 1: 1 make it necessary for optimal results

between 427 and 610, preferably between 449 and can be achieved.

538 ⁰ C is operated, and the conversion is 5 By using the work according to the invention per pass 30 to 80, preferably 40 to 75 ° / ₀ . higher heavy gasoline yields can be achieved using parameters. The conversion is here as 100 minus the volume - with higher octane numbers than with other percentages of pro working methods boiling ^{above about 220 ° C.}

ducts defined. The remainder of the feed gas oil is fed into the verdening according to the invention with a higher temperature "riser" which is operated with an io drive in existing catalyst cracking plants at a temperature of 621 ° C and not using several "risers". Since there is a series of steps and the 11 to 110, preferably 25 to 85 ⁰ C of embodiments can be applied any higher than the temperature in the lower tempered, the application of the method is the "increase". In the higher temperature "Steiger" invention by the selected embodiment, the conversion is 0 to 35, preferably 10 to 15, perhaps limited to a specially designed An-20% less than the conversion in the lower position. In general, the increase leads to temperature-controlled "risers" if the cracking of the gas oil at the reactor temperature is limited to a simultaneous "riser" cracking. If the increase in the conversion per pass, which again in one or another embodiment leads to the fact that the higher-temperature "riser" with gas oil in the dense catalyst phase includes a higher conversion per pass, the conversion ratio between the , unless specific construction and details »increase« are somewhat different from the operational changes made beforehand. Instead of being written. Other working conditions, which are not decisive for the conversion in the higher temperature and which are reduced in the "Steiger" cracking in itself "Steiger", are perhaps more possible, which are also known, are the following: Dwell time of "5 process of the invention apply by increasing the 2 to 15, preferably 3 to 10 seconds, gas velocity conversion in the lower temperature "riser" from 450 to 1500, preferably 600 to 1200 cm / sec by increasing the amount of the use and space velocity from 10 to 100, preferred material in the lower temperature "Steiger" reduced from 40 to 65 parts by weight per hour per ornament. Although this is a very minor and undesirable part. 30 would cause linear velocity, the

When the gaseous reaction mixture and the introduction of steam into the lower temperature Catalyst existing stream from the higher or from "Steiger" mitigate this fact, but could the lower temperature "riser" no further dwell time and the conversion is excessive Requires cracking, it is reduced to the dilute phase and the activity of the catalyst is detrimental passed above the fluidized dense phase. When 35 are affected. To use the method of the invention in To use an additional cracking of one or the other existing plant, the working current must be used is required, the respective current is carefully checked and dated in the conditions if necessary lower section of the fluidized dense cata- lyst and perhaps some changes to it sator phase, where a further transformation of the facility will be carried out, gaseous products takes place. The from the »stone 40 is preferably the catalyst cracking plant for ger «in the reactor containing the dilute phase cut the operation according to the method of the invention entrained catalyst is constructed above the special. To be in the higher tempered dense phase of the gaseous reaction product- »increase« a lower conversion per pass ten separately and with the one from the "Steiger" to reach the, the time spent in this "Steiger" dense phase entrained catalyst combined. The «z. B. be shortened in that the length of the combined catalyst is reduced as a fluidized dense phase of higher temperature "riser"., or with the gaseous flow from the same "riser" that the higher tempered "riser * with a higher one for further conversion of the gas oil in contact ge linear velocity is operated than the lower The working conditions in the dense phase are tempered "climbers", or that in the lower tempe the following: Temperatures between 427 and 621 ° C, 50 "Steiger" ured the crack per pass Gas velocity is increased from 15 to 120, preferably by so that more remains in the dense phase 39 to 66 cm / sec and space velocity of 1 to the lower temperature "riser" is cracked, 40, preferably from 3 to 25 parts by weight per hour or any combination of these mepro Part by weight · By using the gaseous methods.

Products from a »Steiger« with the fluidized 55 The invention is based on the following a ·

Dense catalyst phase can come into contact, detailed description of one of the embodiments

there is a further conversion from 5 to 30 volume- will be explained in more detail with reference to FIG. 1

percent instead. which gives the example of a device with which dai

Although the advantages of the invention can be achieved by practicing the method of the invention

by considering the fresh feedstock in 60 The description of the invention with reference to this form

introducing each of the various "Steiger", the invention was by no means based on this system

with between 20 and 80% of the feed oil in the cabinets.

"Steiger" with lower temperatures and the rest in the As in FIG. 1 can be seen, is freshly used

higher tempered "risers" are passed, gas oil was passed through lines 10 and 22 in a ratio

found that in most cases one leads to the 65 nis of about: 1 in each of the two "Steiger"

Best results are obtained when the feed oil is about The feed material in line 10 is hot

is divided equally between the two »Steiger«. regenerated equilibrium molecular sieve zeolite

However, those skilled in the art will recognize that particular catalyst is brought into contact from standpipe 12

'10

wherein the catalyst has a temperature of about chamber 34, in which the gases from additional, not 621 ⁰ C has. The suspension obtained from the cyclones represented by the catalyst is collected and from there in oil vapor flows with a temperature of about the reactor through the line 36 to be removed. 510 ⁰ C and a gas velocity of about The gas line 36 transports the cracked products at 1200 cm / sec up the "riser" 14 and into the 5 not shown product collection points, in which the thin catalyst phase of the reactor 16 is obtained as products and through Higher temperature "Steiger" known per se, called "Steiger" 14 compression, absorption and / or distillation ends in a downwardly directed outlet with devices in the desired products on a toothed edge 18, which has the purpose of separating.

Flow of hydrocarbon vapors from "Steiger" 14 io. Steam flows through line 38 into the steam the dilute catalyst phase in the reactor 16 in ring 40 and from there to a point below to maintain a steady flow, especially when that of the outlet of the lower temperature "riser" 24 Mirror 20 of the dense phase below the serrated in the lower section of the reactor 16. The kata rim 18 due to random fluctuations closer to the dense phase in the lower section of the lysator the outlet of the "Steiger" 14 is passed through the reactor 16 through which the ring 40 flows Edge 18 is defined. In the higher tempered the steam is stripped off and trickles downwards through the "Steiger" the following conditions prevail: Standpipes 42 and 44 and via the slide valves 46 and Space velocity of 60 parts by weight per 48 into the stripper zone SO. The stripping zone 50 is with Hour per part by weight and gas speed of trickle plates 52, which are attached to the "Steiger" 24, and 1200 cm / sec, resulting in a dwell time of about ao with trickle plates 54 attached to the wall of the Ab-3.5 see results. The conversion of the gas oil in this strip 50 are attached. Through the line 56 is Under these conditions, "Steiger" amounts to steam via the steam ring 58 in the lower Ab-50 Volume percentage. cut the stripper zone 50 below the trickle

The remainder of the feed oil flows through line 22 to plate 52 and through line 60 via the "riser" 24, which is tempered by the steam lowering device, where it is blown in with the "5 ring 62" below the trickle plates 54. The hot zeolitic catalyst described above is loosened by steam rising through the scraper and brought into contact from standpipe 26. Adsorbed and the DA removed penetrated Kohlenwasserbei resultant catalyst-gas mixture with a fuel vapor flowing upwardly through the stripper-AbTemperatur of about 466 ⁰ C at a throughput line 63 into the dilute phase of the reactor 16 nick current speed of about 600 cm / sec at 30, where they are obtained together with the cracking products with an average residence time of about 8 sec th in the manner described above, through the lower temperature "riser" upwards. The stripped catalyst is removed from the bottom of the

To the further working conditions in the lower stripping zone 50 through the standpipe 64 for tempered "Steiger" counts a space-velocity catalytic converter withdrawn, in one speed of 45 parts by weight per hour per weight 35 speed divided by the slide valve 66. During the passage through which is placed lower. From there it flows through the standpipe 68 Tempered "riser" 24 is a conversion of in the regenerator 70. The used catalyst 55 percent by volume preserved. comes into contact with air in the regenerator 70

The current brought from the lower temperature "riser", which flows through the line 72 via the air ring 74 24 into the lower section of the reactor 16 and 40 is introduced. The one subjected to regeneration flows upwards through the dense phase of the cracking catalyst, forming in the regenerator a dense catalyst in the reactor 16, the gas oil phase having a level of 76. The carbon can be converted to another 11 ° / ₀ . To the rest of the catalyst surface is burned, and the ent working conditions in the dense catalyst phase flow through the in reactor 16 counting a catalyst oil ratio 45 regenerator 70 up and enter the cyclone 78 of 12 and a space velocity of 4 weight - One, in the entrained catalyst parts separated per hour per part by weight. The combination and, through the descending pipe 80, is fed back to the dense bed of cracking in the higher temperature "riser", in the lower in the regenerator. The combustion gases escaping from the riger tempered "riser" and in the dense phase cyclone 78 flow results in a total conversion of 58 percent by volume, 50 via the line 82 into the collecting chamber 84 and from where the conversion as 100 minus the volume - there to the outside through the Combustion gas line percentages of products 86 boiling above 221 ° C. to ventilating devices (not shown) are defined. The gas velocities in the reactor. The latter can be known devices to be at the point where the lower temperature utilization of the "riser" contained in the combustion gases flows into the dense phase, 45 cm / sec and have heat and energy. The regenerated at the level 20 of the dense catalyst phase, where the catalyst is separated from the gas through the lines 88 and 90, 36 cm / sec and at the point where the bottom of the regenerator 70 is withdrawn, namely in the higher temperature "riser" in the dilute phase speeds, which opens through the slide valves 92 and 94, are 75 cm / sec and can be set at the upper section of the, and from there the hot cyclone inlets are below 60 cm / sec. 60 regenerated catalyst the standpipes 12 and 26,

The cracked products escape from the kata- as mentioned above, supplied.

analyzer into the dilute phase above level 20 The following are examples of practical changes dense phase. The gases with any co-application of the invention on the basis of a series of dragged catalyst surfaces flow through the operations of a continuous fluidized bed kata-cyclone 28, in which the catalyst is separated 65 listed lysator-cracking plant. For the sake of simplicity and through the descending pipe 30 the bed will not be covered again in any of the different modes of operation is fed. The circulation and cracking escaping from the cyclone 28 in the dense phase Gases flow through line 32 into the collecting insert.

Table (state of the art)

FaUA

FaUB

Fresh feed oil (volume percentage):

»Steiger« 1

"Steiger" 2

Booster ^{temperature in 0} C:

»Steiger« 1

»Steiger« 2

Conversion at 221 ° C, in percent by volume:

»Steiger« 1

»Steiger« 2

Total ,

DP heavy ^{gasoline (x} ) yield, in percent by volume:

»Steiger« 1

»Steiger« 2

total

DB heavy ^{gasoline (8} ) yield, in percent by volume:

total

DP heavy petrol octane number (RON with 3 ml TÄB) (»)

»Steiger« 1

»Steiger« 2

total

DB heavy petrol octane number (RON with 3 ml TAB)

total

100 100 100

477 493 516

58 58 58

58 58 58

41.7 40.3 39.4 38.7

41.7 40.3 39.4 38.7

50.0 48.6 47.7 47.0

91.0 93.7 95.6 98.4

91.0 93.7 95.6 98.4

93.6 95.6 97.1 994

53.2
46.8 70
30th 449
516 449
516 49.6
67.6
58.0 53.8
67.7
58.0 37.4
40.6
38.9 39.6
40.6
40.0

47.2 48.3

91.1 90.9 99.8 99.8 95.1 93.5

96.6 95.3

Table (according to the invention)

FaUC

FaIlD

Fresh feed oil (volume percentage):

»Steiger« 1

»Steiger« 2

Booster temperature in ° C:

»Steiger« 1

»Steiger« 2

Conversion at 221 ° C, in percent by volume:

»Steiger« 1

»Steiger« 2

total

DP Heavy Benzrai ^ yield, in percent by volume:

»Steiger« 1

»Steiger« 2

total

DB heavy ^{gasoline (a} ) yield, in percent by volume:

total

DP heavy gasoline octane number
(RON with 3HUTABX ⁸ )

»Steiger« 1

»Steiger« 2

total

DB heavy petrol octane level
(RON with 3 ml TAB)

total

41.7
38.6
39.5

91.0
98.4
96.1

53.2
46.8

449
516

58
58 58

41.7
38.6
40.3

91.0
98.4
94.5

70
30th

449
516

58
58
58

41.7
38.6
40.8

47.8 48.6 49.1

91.0
98.4
93.3

97.5 96.2 95.6

30th
70 46.8
53.2 70
30th 449
516 449
516 449
516 67.7
53.8
58.0 67.7
49.6
58.0 61.6
49.6
58.0

45.6 45.6 43.3 37.5 36.6 36.6 40.0 40.9 41.4

48.3 49.2 49.7

91.5 91.5 91.1 97.9 97.7 97.7 96.0 94.8 93.1

97.3 96.5 95.1

Notes: 0) Pentane-free heavy fuel; (·) Butane-free heavy fuel; (*) Research octane number of heavy gasoline with 3 r Tetraethyl lead per 3.78 L.

2670

JS t

13 '14 y

In all cases an original gas oil was used. The products in the table above have an API gravity of 30.9 and lead to. The total conversion at 225 ° C was in ASTM distillation had the following characteristics: all cases 58 volume percent and the "Steiger" tem-boiling point at 233 ° C; at 50% the temperatures varied between 449 and 516 ° C. Except | temperature 330 ° C; End of boiling at over 404 ° C. In all cases 5 the was used in every case in which fresh use | if an equilibrium molecular sieve zeolite catalyst material was added to both "risers", the effect jj lyser used. a modification of the feed ratio at j

In case A, fresh gas oil was fed into one »riser« - the feed of fresh gas oil into both »risers« j

Fluidized Bed Catalyst Cracking Plant. In case B, the F i g based on this information. 2

an io that works according to the two »Steiger« principle shows a comparison of the heavy fuel consumption

Fluid bed catalyst cracking plant used. The prey curves and the octane number curves at the same

Cracking was in the two at different tem- peratures of permanent transformation in all of these cases. ]

temperature operated "increase" carried out, whereby when considering the F i g. 2 and table j

the conversion in the higher tempered "climber" shows that in case C and case D higher gravity j

per pass was greater than in the lower temperature 15 gasoline yields were obtained, the Aus j

perated »Steiger«. Case A and Case B were the state of the prey in Case D was best. It also shows that

Technology. In cases C and D a two- not always better yields were obtained when

"Steiger" fluidized bed catalyst cracking plant uses fresh feedstock to two reactor "risers"

det, in which the fresh feed is fed into the two, since in case B gives poorer results

"Steiger" was directed, of which one with an ao was considered in case A, in which the fresh Einsatzmate- _;

operated at a higher temperature than the other. rial was fed into only one "Steiger". Besides that

In case C the conversion was in the two stages, it can be seen that the yields correspond to the

like «the same per run, whereas the conversion ratio is better by using the fresh

Development in case D in the higher temperature riser per feed material is supplied to each reactor "riser". It

Passage was lower. 25 seems as if the fresh feed is in a

Both Case C and Case D are embodiments with a ratio of about 1: 1 that would need to be fed to

the invention. To achieve the heavy gasoline yields and the best results of case D. Octane numbers obtained in each case

1 sheet of drawings

Claims (1)

Patent claims: 1. Process for the catalytic cracking of gas oils in the presence of a zeolitic catalyst in one of a containing a dense and a dilute layer of the catalyst Reactor, a regenerator and a number of elongated reaction zones ending at the reactor existing fluidized bed cracking plant and wherein mixtures of the gas oil with the catalyst under catalytic cracking conditions through the elongated reaction zones Reactor are fed, characterized in that