SA112330738B1 - A catalytic cracking process for producing propylene - Google Patents

Abstract

The present invention discloses a catalytic cracking process for producing propylene, wherein a heavy feedstock and a catalyst are introduced into a first riser; a cracked heavy oil and a catalyst are introduced into a second riser communicated with a fluidized bed; a light hydrocarbon is introduced into a second riser after introducing the heavy oil; the reaction mixture from the second riser is introduced into the fluidized bed; the reaction mixtures from the first riser and the fluidized bed are separated in a product separation system to obtain a cracked heavy oil, which can be recycled back to the second riser. Said process is useful in the propylene production, and has a good conversion for heavy oil, high yields of propylene and butylene, and a good selectivity for dry gas and coke.

Description

_— \ _ A catalytic cracking process for producing propylene Full Description BACKGROUND BACKGROUND The present invention relates to a catalytic cracking process; specifically; A catalytic cracking process to produce propylene from a heavy feedstock. The catalytic cracking of heavy oil is an important process for the production of small-molecule olefins (Jie ethylene); © PP; and butylene. Industrial heavy oil catalytic cracking processes to obtain low olefins include catalytic cracking technology; which aims to maximize the production of propylene; catalytic pyrolysis technology; Which aims to maximize ethylene production. For these two technologies; The reactor design of a single bed reactor or a combination of a single bed and fluidized bed reactor together with a special catalyst is used to conduct the reaction at a higher temperature. 0 Although these two techniques above can improve the production of low olefins “Jie ethylene and propylene” nonetheless; Dry gas and dry coke yields are very high; Hence, it is difficult to further increase the output of propylene. Chinese Patent 110304 (corresponding to US Patent Application 10949987 process for cooling the catalyst ol cad) discloses the cooling of part of the regenerated catalyst. A portion of the cooled (Aad) catalyst 0 and the uncooled high temperature regenerated catalyst is mixed in the initial lift section of the upper reactor. The mixed catalyst having a relatively low temperature is brought into contact with the hydrocarbon stream to react. The other part of the cooled regeneration catalyst is sold (sale) back to the regenerator (sale) to regulate the temperature of the regeneration process. This process says nothing about increasing propylene yield. Chinese Patent 0180777 (corresponding to US Patent Application 14986748) discloses a catalytic Yo-cracking process for reducing the olefin content of liquefied gas and gasoline. Said process is suggested to be in a reactor

b single top reactor or in a combined reactor of single top reactor and fluidized bed reactor; The preheated hydrocarbon feedstock is introduced into the lower part of the upper reactor and comes into contact with the catalyst. The reacted hydrocarbon stream flows up into the middle or the top of the upper reactor to come into contact with the cooled catalyst for them to react. The reaction stream leaves the reaction system via a release device to separate the 0 products obtained. The spent catalyst is subjected to coke burning at elevated temperatures to be regenerated and divided into two parts. One of the two parts enters the lower part of the upper reactor; The other part is cooled and then fed into the middle or upper part of the upper reactor. This process is not recommended for the production of propylene and other small-molecule olefins. Chinese patent discloses 1,778,467 combined catalytic cracking processes; Includes insert 780-11 wt. of regenerated catalyst; after cooling; In Jolie fluidized bed has a circular flow to come into contact with the gasoline feedstock to react. after the reaction; The spent catalyst is introduced into the separation zone of the fluidized bed reactor having circulating flow to be separated. 7950-40 sale) by weight of the separated catalyst is returned to the reaction zone for recycling use; The remainder is sent to a location prior to the initial lift section of the heavy oil upper reactor and mixed with the cooled non-NO high temperature regenerated catalyst followed by contact with the heavy hydrogen to react. The said process involves a relatively low yield of propylene; And don't mention the increase in propylene production and the reduction of dry gas. Chinese Patent 117,767,060 discloses a modification and device for low-grade gasoline. Said process suggests that the regenerated catalyst is cooled to a temperature of 0-5 Ten C and then sent to a separating section to be mixed with the catalyst (Mita) in contact with low quality gasoline in a counterflow 0 stream. The olefin content and sulfur content of gasoline can be reduced” and RON of gasoline can be increased. It does not mention anything about increasing the production of gasoline. Chinese Patent 010011747497 discloses a method for producing propylene and oil-diesel gasoline by a two-section catalytic cracking pattern; Performed using the Bink process using a two-section lift tube and catalyst enriched with a shape-selective molecular sieve; Takes heavy petroleum hydrocarbons or animal oils

_ _

And diversified vegetable containing hydrocarbon as raw materials. The mentioned method includes a toll

Low polypropylene and low heavy oil conversion capacity.

General description of the invention

The present invention is intended to remedy existing deficiencies in the prior art of producing propylene by cracking

catalytic It provides a catalytic cracking process to produce propylene that improves propylene yield and has selectivity

Low for dry gas.

Specifically » 1 of the present invention provides a catalytic cracking process for the production of z-propylene » comprising:

(1) Introduce the feedstock Jal and a first catalytic cracking catalyst into a first upper reactor to perform a cracking reaction

catalytic separation of the resulting hydrocarbon stream and resulting shuttle catalyst by means of a separator at the first top 0 reactor tip; introduction of a hydrocarbon stream into a separation system for a subsequent product to be separated; Either directly enter

The shuttle catalyst is in a separator to be separated. Or not to insert the catalyst shuttle into the Jolie layer

fluidized and then by inserting it into the separating device to be separated; Introducing the separated catalyst into the sell device).

generation to be regenerated;

The first mentioned catalytic cracking catalyst contains a shape-selective zeolite having an average pore size of less than 10 nm;

Amorphous has an average pore size of less than 0.7 nm;

(T) Introducing a light hydrocarbon into the top reactor GB at a location after the heavy oil fractured JAY; Ys Mixing a light hydrocarbon with a mixture consisting of the contact and reaction of a heavy oil fractured and a catalyst

second catalytic cracking; interact;

Said light hydrocarbon includes hydrocarbon 4© and/or a gasoline fraction obtained

of said product separation system;

Qo _ _ (?) introduction of a hydrocarbon stream and a catalyst obtained after the reaction in the second upper reactor into the fluidized bed reactor connected in series with the second upper reactor to react; (5) after the reaction in the Jolie fluidized bed; Introducing the resulting hydrocarbon stream into the product separation system to be separated; © Introducing the resulting fusible catalyst into a separator to be separated; And then

Introducing the separated catalyst into the regenerator to be regenerated. In one embodiment z the present invention provides a catalytic cracking process for the production of propylene” comprising: (1) introducing a heavy feedstock and a first catalytic cracking catalyst into a first upper Jolie to perform a catalytic cracking reaction ¢

A where »; an upper reactor outlet temperature is about A m the reaction time is about SY the catalyst/oil ratio is about 1001 w/w the ratio of steam atomized to heavy feedstock is about 78 by weight; Separation of the resulting hydrocarbon stream and resulting spool catalyst by means of a separator at the top reactor end

Ye first; introduction of a hydrocarbon stream into a separation system for a subsequent product to be separated; either directly feeding the shuttle catalyst into a separator to be separated; or first to insert the shuttle catalyst into a fluidized bed Jolie; and then by inserting it into the separating device to be separated; introduction of the separated catalyst into the regenerator to be regenerated; The first mentioned catalytic cracking catalyst contains a shape-selective zeolite having an average pore size of less than nm;

Y (1) Introducing fractured Jad oil into an overhead reactor ob; contacting with catalytic cracking catalyst ob and then introducing selective morphology having an average pore size of less than 0.7 nm;

The ne the catalyst inlet temperature of the second upper reactor is about 145 C; of the outlet temperature of the second upper reactor is about 001:# is about Jal The weight ratio of the cracked heavy oil to the feedstock is the input of the oil The heavy fractionated at a location at the bottom of the second upper reactor © 0131 sec The total reaction time of the fractured heavy oil in the upper reactor is about 701 by weight The ratio of steam atomized to the fractionated heavy oil is about The ratio of the catalyst /oil for fractionated heavy oil about 77.7 w/w; introduction of a gasoline fraction as a light hydrocarbon into a second upper reactor at a location after the introduction of oil ((fracturing agglomeration; mixing of the light hydrocarbon with a mixture formed by the contact and reaction of the heavy oil 0 fractured and the cracking catalyst The second catalyst; reaction; 17 seconds The reaction time of the heavy oil fractured before contact with the light hydrocarbon is about The reaction temperature of the heavy oil fractured before contact with the light hydrocarbon is about m Vo 70077 The amount of coking on the catalyst After initial contact with a light hydrocarbon of approx By weight 001 VY The weight ratio of the light hydrocarbon to the heavy feedstock is about 1119 w/w The catalyst/oil ratio for the light hydrocarbon is about 0001 sec The reaction time of the light hydrocarbon in the upper reactor is about 0 the

to

The ratio of vapor to aerosol to light hydrocarbon is about 795 by weight

The light hydrocarbon contains the gasoline fraction obtained from the product separation system

aforementioned;

(?) The introduction of a hydrocarbon stream and a catalyst obtained after the reaction into the second upper reactor at

© A fluidized bed reactor connected in series with the second upper reactor to interact;

The temperature of the layer is about 570 °C

The gravimetric velocity per hour of the layer is about 01-1 hour

(0) After the reaction in the fluidized bed reactor, introduce the resulting hydrocarbon stream into the product separation system Vo to be separated;

Introduce the resulting shuttle catalyst into a separator to be separated; And then

Introducing the separated catalyst into the regenerator to be regenerated

In the Al embodiment the present invention provides a catalytic cracking process for the production of propylene” comprising:

(i) Introduce Ji feedstock and a first catalytic cracking catalyst into a first upper reactor to perform a catalytic cracking reaction;

The upper reactor outlet temperature is about 60 °C;

The reaction time is approx. seconds;

The catalyst/oil ratio is approximately 11117 w/w; Yo The ratio of aerosolized vapor to the heavy feedstock is about ZA by weight;

the

A —_ Separation of the resulting hydrocarbon stream and resulting shuttle catalyst by means of a separation device at the first upper reactor tip; introduction of a hydrocarbon stream into a separation system for a subsequent product to be separated; either directly inserting the catalyst (IA) into a separator to be separated; or not to insert the shuttle catalyst into a fluidized bed Jolie; and then by inserting it into the separating device to be separated; introduction of the separated catalyst into the generating device (sale) to be regenerated; The first mentioned catalytic cracking catalyst contains a shape-selective zeolite having an average pore size of less than nm; Eclemorphic has an average pore size of less than 0.7 nm; 0 where; The Jalal catalyst temperature of the second upper reactor is about 155 °C; The outlet temperature of the second upper reactor is about 2.4 C. The weight ratio of the fractured heavy oil to the feedstock, BED, is approximately #: 001. The introduction of the fractured heavy oil is at a location at the bottom of the second upper reactor. 10 is the total reaction time of the oil. The heavy fractionated in the upper reactor is about 0101 sec. The ratio of steam aerosolized to the heavy oil fractionated is about 701 by weight. The ratio of catalyst/oil to the heavy oil fractionated is about Yeo w/w?; (“” Introduction of a gasoline fraction and C4 hydrocarbon as a light hydrocarbon in a second upper reactor at the same level after the introduction of the fractured Jail oil; mixing of the light hydrocarbon with a mixture consisting of contact 0 and reaction of the fractured heavy oil and the second catalytic cracking catalyst; and reaction;” Cua ae 1.5 seconds The reaction time of the heavy oil, which is fractured before contact with the light hydrocarbon, is about The reaction temperature of the heavy oil, which is fractured before contact with the light hydrocarbon, is about

AY

70017 The amount of coke on the catalyst after initial contact with the light hydrocarbon is about 5 by weight The reaction time for the light hydrocarbon in the upper reactor is about 0.10 seconds The weight ratio of the gasoline fraction to the feedstock GE is about 001 BY The catalyst ratio is / Oil for the gasoline fraction is about 16.4 w/w The ratio of the steam aerosolized to the gasoline fraction is about 701 w/w 8:00 The weight ratio of the 04 fraction to the heavy feedstock is about Ys 016 w/w The catalyst/oil ratio of the 4© fraction is approximately The ratio of aerosolized vapor to the 4© fraction is approximately 75 by weight The light hydrocarbon contains a 4© hydrocarbon and/or a gasoline fraction obtained from said product separation system; Vo (£) Introduce a hydrocarbon stream and catalyst obtained after the reaction in the second upper reactor into the fluidized bed reactor connected in series with the second upper reactor to react; layer temperature is about +59 C. vacuum gravimetric velocity per hour of the bed is about 6 h 1- Al

=« \ _ (0) After the reaction in the fluidized bed reactor; the resulting hydrocarbon stream is introduced into the product separation system to be separated; the resulting shuttle catalyst is introduced into a separator to be separated; and then the separated catalyst is introduced into the generation device (sale) to be regenerated in another z J gal; The present invention provides a catalytic cracking process for the production of “z-propylene” comprising:

(1) Introduce a heavy feedstock and a first catalytic cracking catalyst into a first upper Jolie to perform a catalytic cracking reaction ¢ “Cua The outlet heat of the upper reactor is about a Ou

0 the reaction time is about; seconds; the catalyst/oil ratio is about 1 w/w; the ratio of steam to aerosol to heavy feedstock is about 75 by weight; Separation of the resulting hydrocarbon stream and resulting shuttle catalyst by means of a separator at the first upper reactor tip; introduction of a hydrocarbon stream into a separation system for a subsequent product to be separated; Either directly insert the catalyst

Vo the shuttle is in a separator to be separated; or not to insert the shuttle catalyst into a fluidized bed Jolie; and then by inserting it into the separating device to be separated; introduction of the separated catalyst into the (sale) generating device to be regenerated; The first mentioned catalytic cracking catalyst contains a shape-selective zeolite having an average pore size of less than nm;

A) in the second upper reactor Litfa Sle ¢ the catalyst for said second catalytic cracking contains a shape-selective zeolite having an average pore size of less than 0.7 nm;

-11- The temperature of the catalyst inside the second upper reactor shall be about 145 °C; 0710 °C; the outlet temperature of the second upper reactor shall be approximately 001:01. Introducing the fractured heavy oil into a location at the bottom of the second upper reactor © 0.80 sec. The total reaction time of the fractured heavy oil in the upper reactor is about The ratio of steam aerosolized to the fractionated heavy oil is about 75 by weight. The catalyst/oil ratio of the fractionated heavy oil is approximately 8.7 w/w; the introduction of a gasoline fraction as a light hydrocarbon into the second upper reactor at a location after the introduction of (T) the fractionated heavy oil; mixing the light hydrocarbon with a mixture consisting of the contact and reaction of the heavy oil 0 cracker and the second catalytic cracking catalyst; and reaction; 00 seconds The reaction time of the heavy oil broken before contact with the light hydrocarbon is about The reaction temperature of the heavy oil broken before contact with the light hydrocarbon is about aod os Yo 7977 The amount of coke on the catalyst after its initial contact With light hydrocarbon about 7:001 by weight The weight ratio of light hydrocarbon to heavy feedstock is about 1.7 w/w The catalyst/oil ratio for light hydrocarbon is about LY seconds Reaction time The light hydrocarbon in the upper reactor is about Yo Al

-1?-

The ratio of atomized vapor to light hydrocarbon is about 7710 by weight

Said light hydrocarbon contains the gasoline fraction obtained from a separation system

said product;

(4) Introduce a hydrocarbon stream and a catalyst obtained after the reaction into the second upper reactor at

© A fluidized bed reactor connected in series with the second upper reactor to interact;

The temperature of the layer is about 501 C

The gravimetric velocity per hour for the layer is about 11 hours -1

(0) After the reaction in the fluidized bed reactor, introduce the resulting hydrocarbon stream into the product separation system Vo to be separated;

Introduce the resulting shuttle catalyst into a separator to be separated; And then

Introducing the separated catalyst into the regenerator to be regenerated

In the AT embodiment, the present invention provides a catalytic cracking process for the production of "propylene" comprising:

(0) introduce Jif feedstock and a first catalytic cracking catalyst into a first upper reactor to perform a catalytic cracking reaction 0;

The upper reactor outlet temperature is about 005 °C;

The reaction time is about Yoo seconds;

The catalyst/oil ratio is approximately VE w/w; 0 The ratio of steam atomized to heavy feedstock is about 701 by weight;

the

— \ _ Separation of the resulting hydrocarbon stream and resulting shuttle catalyst by means of a separation device at the first upper reactor tip; introduction of a hydrocarbon stream into a separation system for a subsequent product to be separated; Either Sale Enter the shuttle catalyst into a separator to be separated; or first to insert the shuttle catalyst into a fluidized bed Jolie; and then by inserting it into the separating device to be separated; 2 Introduce the separated catalyst into the (sale) generating device to be regenerated; The first mentioned catalytic cracking catalyst contains a shape-selective zeolite with an average pore size of less than 1.7 nm; Eclemorphic has an average pore size of less than 0.7 nm; 0 where; The temperature of the catalyst entering the second upper reactor is about 145 °C; The outlet temperature of the second upper reactor is about 250 C The weight ratio of the fractured heavy oil to the feedstock (JEN) is about 100:1 The introduction of the fractured heavy oil is at a location at the bottom of the second upper reactor VO The total reaction time is For heavy oil fractured in the upper reactor is about 0.45 sec. The ratio of steam aerosolized to fractured heavy oil is about 78 by weight. The catalyst/oil ratio for heavy oil fractionation is about 116116 w/w?; (?) the introduction of a gasoline fraction as a light hydrocarbon into the second upper reactor at a site after the introduction of the fractionated heavy oil; Mixing the light hydrocarbon with a mixture consisting of the contact and reaction of the cracked heavy oil Yo and the second catalytic cracking catalyst »and reaction; where; the

The reaction time of the Jl oil fractured before contact with the light hydrocarbon is about 0.05 seconds The reaction temperature of the heavy oil fractured before contact with the light hydrocarbon is about alto 0 The amount of coking on the catalyst after its initial contact with The light hydrocarbon is about 70.267

By weight the weight ratio of the light hydrocarbon to the heavy feedstock is about Verde the catalyst/oil ratio for the light hydrocarbon is about 1111 w/w the reaction time for the light hydrocarbon in the upper reactor is about 1.8 seconds

0 The ratio of aerosolized vapor to light hydrocarbon is about 795 by weight. Said light hydrocarbon contains the gasoline fraction obtained from said product separation system; (?) introducing a hydrocarbon stream and a catalyst obtained after the reaction into the second upper reactor into a fluidized bed reactor connected in series with the second upper reactor to react;

VO where; The temperature of the bed is about 5718 C, the gravimetric velocity per hour of the bed is about 11 hours 1- (©) after the reaction in the fluidized bed reactor; Introducing the resulting hydrocarbon stream into the product separation system to be separated;

0 The resulting shuttle catalyst is fed into a separator to be separated; Then the separated catalyst is introduced into the sale) generating device to be regenerated

j \ _ in z J ga another; The present invention provides a catalytic cracking process for the production of “z-propylene” comprising: (1) Introducing a feedstock Ji and a first catalytic cracking catalyst into a first upper reactor to perform a catalytic cracking reaction ¢ “Cua© The outlet temperature of the upper reactor is about 8900 m; reaction time is about 0. sec; catalyst/oil ratio is about 01 w/w; the ratio of vapor to aerosol to feedstock (Jil) is about 7010 by weight; Separation of the resulting hydrocarbon stream and resulting shuttle catalyst by means of a separator at the first 0 top reactor tip; Jad is the hydrocarbon stream in a separating system for a subsequent product to be separated; either directly feeding the shuttle catalyst into a separator to be separated; or not to insert the shuttle catalyst into a fluidized bed Jolie; and then by inserting it into the separating device to be separated; introduction of the separated catalyst into the (sale) generating device to be regenerated; The first mentioned catalytic cracking catalyst contains a shape-selective zeolite having an average pore size of less than nm; Y (Yo) Introducing cracked Jad oil into an overhead reactor ob; contacting with catalytic cracking catalyst ob and then introducing selective shape having an average pore size of less than 0.7 nm; “Cua” The catalyst inlet temperature of the second upper reactor is about 145 °C; the outlet temperature of the second upper reactor is about ove °C; the weight ratio of the fractionated heavy oil to the feedstock JEN is about 3.5 ?: 001 L

— a \ — The introduction of the fractured heavy oil is at a location at the bottom of the second upper reactor The total reaction time of the fractured heavy oil in the upper reactor is about 0101 seconds The ratio of steam aerosolized to the fractionated heavy oil is about 701 by weight The catalyst ratio is /oil for heavy, cracked oil is approximately 597.5 w/w?; © (©) Introduce a gasoline fraction as a light hydrocarbon into the second upper reactor at a location after the introduction of the fractionated heavy oil; Mixing the light hydrocarbon with a mixture consisting of the contact and reaction of the cracked heavy oil and the second catalytic cracking catalyst and the “Cua” reaction The reaction time of the cracked heavy oil before contact with the light hydrocarbon is about CAT 0 seconds The reaction temperature of the cracked heavy oil before contact with Light hydrocarbon is about a Vo The amount of coke on the catalyst after initial contact with the light hydrocarbon is about 70.77 by weight Ve The weight ratio of light hydrocarbon to heavy feedstock is about 17:001 The catalyst/oil ratio for light hydrocarbon is about 17094 w/w Reaction time for light hydrocarbon in upper reactor is about 17 seconds Ratio of vapor atomized to light hydrocarbon is about 715 w/w Said light hydrocarbon contains the gasoline fraction obtained from the Yo separation system of said product;

(?) introducing a hydrocarbon stream and a catalyst obtained after the reaction into the second upper reactor into a fluidized bed reactor connected in series with the second upper reactor to react; “Cua the temperature of the bed is about 576 m 0 the vacuum gravimetric velocity per hour of the bed is about 1 h 1- (5) after the reaction in the Jolie fluidized bed; Introducing the resulting hydrocarbon stream into the product separation system to be separated; Introduce the resulting shuttle catalyst into a separator to be separated; and then the separated catalyst is introduced into the sale generation device to be sale generated in the five embodiments as above; The term “approximately”” denotes a deviation of JV vk JAE y y y yy yy yyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyyy The present invention also provides an apparatus for the above process; The equipment includes: first upper reactor, upper ou reactor, YEP layer reactor, separator, product separation system release device, and regeneration device; where the second upper reactor and the fluidized bed reactor are touched respectively; 1 Jolie fluidized bed is connected with separator and release device; The first upper reactor and release device are connected to each other (andl) the generation device is connected to the separator; The first upper reactor and the second upper reactor respectively through the catalyst pipelines The first upper reactor is supplied with the inlet of the heavy feedstock; The second upper reactor is provided with a reaction section for the fractured oil, Jl, an inlet for the heavy oil fractionation, and an inlet for the light hydrocarbon; An inlet 00 for light hydrocarbon is provided between the inlet of the heavy oil fraction and the outlet of the second upper reactor; The aforementioned reaction section of the heavy oil fraction is located between the inlet of the heavy oil fraction and the inlet of the light hydrocarbon.

M \ _ The catalytic cracking process for the production of propylene according to the present invention is based on a reactor combination of two overhead reactors and a fluidized YET reactor. process improvement; selection of suitable catalyst 3 and selective conversion of different feedstocks; The process according to the present invention can have a relatively high heavy oil conversion depth and a relatively high yield of a high quality product. In the meantime; Dry gas and coke yields do not increase. The process according to the present invention has relatively high yields of propylene and butylene;

Relatively low selectivity of dry gas and coke. Brief description of the drawings

1 for a schematic flow diagram according to the catalytic cracking process of the present invention; In it, le 1 Fig. 0 represents the first upper reactor; 7 represents the second upper reactor; and represents a separating device; And the; represent a product separation system; 7 represents Regeneration Device 1 Release Device 6 and Jide Fluidized Bed Reactor and Regenerated Catalyst Pipelines Represent Yes gc Represents Spent Catalyst Pipeline A 9 Generation where; The upper reactor is connected? respectively with the fluidized bed; connected in parallel with

0 upper reactor 1 by launcher ©; Jolie is placed in the fluidized bed; And the separator? At high level and low level respectively and connected with each other. Detailed description: The best methods of implementation of the present invention

0 in the catalytic cracking process to produce propylene according to the present invention; A heavy feedstock and a first catalytic cracking catalyst are introduced into a first upper reactor; The heavy feedstock and the first catalytic cracking catalyst are contacted and reacted to obtain a hydrocarbon stream and a shuttle catalyst. The hydrocarbon stream and the shuttle catalyst are separated by a separator at the first upper reactor tip. The hydrocarbon stream is introduced into a subsequent product separation system for the purpose of separation. The first catalytic cracking catalyst is introduced

the

q —_ \ _ shuttle in a fluidized bed Jolie or separator as discussed below in the order; preferably in a fluidized bed reactor. The separator at the top end of the first reactor is useful for separating the hydrocarbon stream and the shuttle catalyst after the reaction; which is in favor of reducing dry gas yield and inhibiting further conversion of low yielding olefins; Specifically, propylene. The above © separation method is preferably a quick method. Existing quick disconnect method can be used. The preferred rapid separator is a primary vortex separator. The reaction process conditions for the first upper reactor include: The reaction temperature ranges ol (upper reactor outlet temperature) Te vA from eg l sp b m i.e. about 'a ve about Vo © 0 about OF 0 0 about Te © 0 about a a0 Yo The catalyst/oil ratio (weight ratio of catalyst to heavy feedstock) ranges from Yeo to milliliters such as about 7 about 0 and l about NYY and about 1; The reaction time ranges from 0.1-2.6 seconds, for example 1-sec, which is about 10 seconds, or about 2 seconds, which is about Apt Yio, about IST, about . Seconds; “The ratio of steam atomized to the heavy feedstock is used in a ratio of weight to the heavy feedstock of approximately 100% by weight”; for example JE .2 by weight”; That is, about m by weight.” about ZA by weight” and about 700 by weight; The reaction pressure ranges from 1-7 MPa (absolute) ie .7-5 MPa (absolute). Yo The feedstock (Jaa) of the present invention contains ALE hydrocarbons or animal or vegetable oils rich in hydrocarbons. Said heavy hydrocarbon is selected from one or more petroleum hydrocarbons; Mineral oils and industrial oils. The aforementioned petroleum hydrocarbons are well known to those experienced in the art; they include vacuum wax oil; atmospheric residual oil; vy mix. residual oil; or other hydrocarbon oils produced by SIA processing from a second wax oil. Other mentioned hydrocarbon oils produced by second processing include one or more coking wax oil; de-asphalt oil; Furfural purified by dissolution. Oils include coal liquefaction oil; Oil sands oil and shale oil. HAST includes one of the listed mineral or industrial oils, fractional oils produced by Fischer-Tropsch synthesis from coal; Natural gas 0 and asphalt. Animal or vegetable oils rich in said hydrocarbons are, for example, one or more animal or vegetable fats and oils. According to the present invention; In general, the heavy feedstock has an initial boiling point of more than 1077 °C in the range of atmospheric distillation; The first 700 of the distillate in the atmospheric distillation range has a boiling point of more than 000 m of 0 A fractionated heavy oil is introduced into (Jal in the catalytic cracking process to produce propylene according to the invention to react; the Hal mixture flows) A GB grade regenerated catalyst top reactor produced from the fractured heavy oil and this second catalytic cracking catalyst is contacted in the second top reactor and subjected to the reaction for a period of time. After the reaction time period; It comes into contact with and mixes with the hydrocarbon in the second upper reactor. The mixture formed in the upper light allay reactor flows into the second Yo and undergoes the reaction”; And eventually it comes out of the second upper reactor. The second upper reactor may include one or more light hydrocarbon inlets. In the case where the second upper reactor has two or more inlets for fractionated heavy oil, these inlets can be located at the same level or at different levels. In the case where the second upper reactor has two or more inlets of _ light hydrocarbon; These inlets can be located at the same level or at different levels. 0 The aforementioned light hydrocarbon is introduced at one or more locations between the inlet of the fractured heavy oil in the second upper reactor (upper inlet) and the outlet of the second upper reactor. In this request; The section between the fracked heavy oil inlet in the second upper reactor (upper inlet) and the light hydrocarbon inlet in the second upper reactor (lower inlet) is called; yy Cracked heavy oil reaction zone (or cracked heavy oil reaction section). The cracking reaction of the catalyst oil is carried out in the cracked heavy oil reaction zone. Jul In this order; The effective length of the second upper reactor refers to the distance from the inlet of the fractured heavy oil in the second upper reactor (upper inlet) to the outlet of the second upper reactor. In this application; The light hydrocarbon induction height refers to the distance from the light hydrocarbon inlet in the second upper reactor to the fractured heavy oil inlet in the second upper reactor (upper inlet).

SY JAA) Preferably according to the present invention the insertion height of the light hydrocarbon is about —0 sq. JYo=0 (JY 1=0 (Jtv=0 sq. m. INV =t JAY JA. from the effective length 20-5 or ZVe 0 in the heavy oil fractured reaction zone; the catalyst/oil ratio for the fractionated heavy oil reaction introduced in the second upper reactor to heavy oil is Gl (weight ratio of catalytic cracking catalyst o = the fractionated EAA introduced into the second upper reactor) 5-5; i.e. and about 7.0 ?; FELT a is used (about 7.7; OTT a about AY i.e. about 8 and about TA of about 5 7; about 0-0 dN Vapor to aerosol for cracked heavy oil in the amount of 05 by weight of heavy oil cracked; weight ratio of cracked heavy oil to heavy feedstock is 0

Vie ema) JB sip de) seo) that was inserted into the first upper reactor

OY Jam) se) Jam) see da) sao i.e. about 0 and 0.70-8.01: the reaction time of the fractured heavy oil and the second catalytic cracking catalyst in the second upper reactor before contact with the light hydrocarbon (which is termed In this application, the reaction time of the oil 0 fractured before contact with the light hydrocarbon, i.e. the reaction time of the heavy oil fractured in Ja sec and 7..- vom) sec; eg 0-1101 (heavy oil fracture reaction area) sec; 1.47 sec; about 1.7 seconds; about ve seconds; about 1.1 seconds; about lo seconds; The temperature of the second catalytic cracking catalyst to be fed into the reactor is v0 and approx

the second upper m to contact with the fracturing heavy oil 770-700 m; eg 00-7186 PM; For example (a 100-190 JE i.e. 140 2 mm or 140 2 in the second upper reactor; prior to contact with the light hydrocarbon'; the reaction temperature of the fractured heavy oil is ol) The reaction temperature of the fractured heavy oil in the heavy oil reaction zone © broken ALE as output ha of the heavy oil fracture reaction zone) 700-8800 m; E.g. 1704 m (a 1Y = o) ie about m or about 1 0 1 0 about 1 to 1 m or about m/m according to the present invention; the heavy fractionated oil has a distillation range of 880-7730 m or “von 0 m. The JE fractionated oil of the present invention can be a sha hydrocarbon having a Ys distillation range of 0 mF eh 0 m or less within this range. For example; the oil contains The fractionated fat on heavy oil available from the product separation system of the present invention" i.e., most of the liquid product remaining after the separation of the gasoline and diesel gas from the hydrocarbon stream introduced into the product separation system. The heavy oil fraction is initially introduced into the second upper reactor to come into contact with the regenerated catalyst The high temperature Vo to react. The mixture of hydrocarbon stream formed during the reaction is then contacted with the light hydrocarbon. On the “second” side of the heavy oil conversion increases the depth of the heavy oil conversion of the process/apparatus Jelly and the fractionated heavy oil fraction is used To increase the yield of propylene. On the OAV side, the coke formed during heavy oil cracking is selectively covered. E. The pore channels of the block and the 0 molecular sieve having large pores (in the presence of any zeolite 7 for example). Thus, the properties of the catalyst can be adjusted. The catalytic function of the selective zeolite is enhanced in the catalyst; The induced hydrogen transfer reaction is easily inhibited by the large pore molecular sieve (zeolite-7) and catalyst block. The amount of coking on the second catalytic cracking catalyst emerging from the cracked heavy oil reaction zone (ie; the amount of coking on the catalyst after initial contact with the

light hydrocarbon eg CLA 0.1 -29.9 or 0.9 -0.9 72 i.e. about 77 0017 about 0.77 7; about 720.77 and about 71.77 by weight of the catalyst. Contact and interaction between the fractured heavy oil and the regenerated high temperature da catalyst reduces the catalyst system heat and provides an efficient conversion medium for the subsequent reaction of the olefin-rich gasoline fraction 0 and/or hydrocarbon 04. Therefore; A catalytic Jol process can be optimized; It can increase the selectivity of propylene production with the possibility of inhibiting dry gas formation. In the catalytic cracking process for the production of propylene according to the present invention; The said light hydrocarbon is introduced into the second lifter reactor after the fractionated heavy oil is introduced and contacted with the hydrocarbon stream mixture which is characterized by a temperature ranging between 00-86 ca, for example 8545- 0 1790-0 mu, To = TY m » such as about 0 090 about YL m »about 148 m; about 100 m; or about 175 m; It is derived from the cracked heavy oil and catalytic cracking catalyst for the second reaction. The catalyst/oil ratio for the light hydrocarbon reaction in the second upper reactor (the weight ratio of the second catalytic cracking catalyst introduced into the second upper reactor to the light hydrocarbon introduced into the second upper reactor) Jie ct emo is about 111 about ATA Vo is about 7/a7; and about FT, the temperature of the second upper reactor (which denotes Sha degree at the outlet of the second upper reactor) is 240-571 °C; as about cp oY about 270 m; about 546 AD” or about OVE .m. in this document; A light hydrocarbon refers to a hydrocarbon with a final boiling point higher than 7501 C or 771 C. The light hydrocarbon comprises a gasoline fraction and/or hydrocarbon 04. In a specified embodiment; 0 light hydrocarbon is a gasoline fraction and/or hydrocarbon 04. Where said light hydrocarbon includes a gasoline fraction” reaction operating conditions for the gasoline fraction in the second upper reactor include the following: The catalyst/oil ratio of the gasoline fraction to be operated is In the second upper reactor (the ratio by weight of the catalyst introduced into the second upper reactor to the gasoline fraction) 78-11 0-01 for example or 70-115 y about 11.1 Yo about IT about 05.4 and about 77.7 with a reaction time of 0.5-1.1 seconds; on

eg 6.7 -0.1 seconds or ALY seconds; such as about 1.76 seconds; 1.7 seconds; about +LA sec; about 100 seconds; The vapor atomized is used for gasoline in an amount of -0 AR eg ZY 0-01 as about VAR about m and about AR by weight of the gasoline feedstock. © when said light hydrocarbon includes hydrocarbon 04; The reaction operating conditions for the CA hydrocarbon in the second upper reactor include the following: The catalyst/oil ratio of C4 hydrocarbon running in the second upper reactor (weight ratio of catalyst introduced into the second upper reactor to hydrocarbons is 0-11 (C4 ; eg 711-30; about the same as any burglar) The reaction time of the C4 hydrocarbon in the second upper reactor is 0 al Yoe—2, 0 eg 0.5-0.5 seconds; Jie ~ + sec; aerosolized vapor is applied to hydrocarbon 04 in an amount of 24-1 ie ZF as ~ 5 wt. of hydrocarbon feedstock Cd is a percentage by weight of light hydrocarbon introduced to the upper reactor The second to heavy raw materials: 5.00 d eg Jia ce.

ViY—ee0 about cro) about Yo 217:1. 0 about 21 and about ce Ye in the catalytic cracking process to produce propylene according to the present invention; The hydrocarbon stream and catalyst after the reaction in the second upper reactor is introduced into the fluidized bed reactor for another reaction. The operating conditions of the fluidized bed reactor are as follows: The reaction temperature is 580-800 ‘a ie 51-50 se o¥.”—2\). JU m is about yo m and about A is 0 m and about 070 m; about 0 08 m” or about 070 m” and the gravimetric velocity per hour of reaction (relative to Mea the hydrocarbon feedstock of the fluidized bed reactor) is 1-75/h; ex = F JE 7/h ; like about 1/hour; about 7/hour; about 10/hr; about 1/hr; and about 11/hr; and the reaction pressure is 0-015 - 7 MPa (absolute); eg Yom ou . + MPa (absolute); Jie is about 071 MPa (absolute).

veo in the catalytic cracking process to produce propylene according to the present invention; The light hydrocarbon to the second upper reactor comprises or is a fraction of gasoline and/or allay hydrocarbon that is made into olefin-rich gasoline and/or olefin-rich hydrocarbon 4©. sha 4; For example, the gasoline fraction includes the gasoline fraction produced by the current equipment (obtained from said product separation system) and the gasoline fraction produced by another equipment. The gasoline fraction 0 produced by another device may be selected from one or more fractionally fractionated crude gasoline; catalytically cracked stabilized gasoline and shuttle gasoline; viscosity-reduced gasoline and gasoline fractions resulting from petroleum refining processes or other chemical engineering. The olefin content of the gasoline feedstock is by weight or 7 5 0 by weight; eg 705-79 wt; Preferably 7 90-71 olefin-rich full-range gasoline has a point on more. The aforementioned gasoline feedstock may be 0 final boiling not exceeding more than 704 m; For example, the gasoline fraction is distinguished by the range of distillation of the gasoline fraction, which is distinguished (JE, for example, cag. m) and also it can be a narrower cut 004 oT and then or a narrower cut in it. 71-85 m; preferably 150 71- With the extent of distillation, the weight ratio of the gasoline part that is introduced to the second upper reactor to the feedstock —vor Ah to the first upper reactor is 0070:1-08.55; the mentioned heavy allay is preferred, which is Ye, and the ratio is The weight of the gasoline fraction that is introduced to the second upper reactor into crude 0.0111.

SU for example crn Y end =o the heavy feed introduced to the first upper reactor ... 09:1 (about 217:1 about cnn Te) as about cron =A or 1:13 more preferably cul YU and the said gasoline fraction is preferably a rich gasoline fraction the olefin-rich gasoline fraction produced from the present apparatus. Ye to a low molecular hydrocarbon; It mainly consists of 04 parts; There is in CA and indicates a hydrocarbon pressure of 1 Ji (m) at normal atmospheric pressure 0-71 gaseous form at normal temperature (atmospheric equivalent); It includes alkanes; olefins and alkenes therein; carbon atoms. The hydrocarbon can be a gaseous hydrocarbon stream rich in fraction 64 produced from the current apparatus; It is also possible that 4 produced from C4 is a gaseous hydrocarbon rich in part 04 produced from another device, preferably the yi part rich in olefin C4 of the current device. said hydrocarbon 64 shall preferably be a fraction preferably more than cil 60 # by weight; Preferably more than 50 C4 has an olefin content by weight. preferably; The light hydrocarbon includes a gasoline fraction containing or not 0-01 where the ratio by weight of hydrocarbon 4 to the gasoline fraction (C4 comprising hydrocarbon) is about 7:7. When the hydrocarbon includes Jie cA = e or VY = eg 7:1 0 which is introduced into the C4 light reactor on hydrocarbon 04; the hydrocarbon by weight is

Jie cron = r vo second upper to heavy feedstock 0.05 -0.7:1; For example....8:1 is about -©0[1 of steam; JS hydrocarbons in this document; Pre-raising medium can be chosen from one or more conventional Cd rich or conventional dry catalytic cracking gas; Preferably vapor and/or part 04 0 olefin. The pre-lift sector in this document indicates the work area; In which the pre-raising medium changes the movement of the regenerative catalyst into an accelerated movement in an upper vertical direction along the riser pipe and makes the catalyst characterized by an evenly distributed flow state in a radial direction from the upper reactor (i.e. a mass flow state). introduction of san ore into the catalytic cracking process for the production of propylene according to the present invention; V0 feeding heavy and heavy oil are cracked together to the riser piping at the position in; before; or after the pre-lift section; With respect to the direction from the inlet of the riser (lower) to the outlet of the riser (upper). In the catalytic cracking process for the production of propylene according to the present invention; A separator at the end of the second upper reactor separates the hydrocarbon stream from the spool catalyst. This ls 0 hydrocarbon stream is also separated to remove the catalyst being carried in it (as shown below) and enters the subsequent product separation system. The hydrocarbon stream after the reaction in the fluidized bed reactor is separated by a separator to remove the catalyst being carried in it; Then it enters the subsequent product separation system. in product separation system; The hydrocarbon stream is separated to produce the fractal gas; broken gasoline; The cyclic oil is the light, fractured, and the heavy, fractured oil. The product separation system is defined in Art. There are no special restrictions for the product separation system in the present invention. In the catalytic cracking process for the production of propylene according to the present invention; The shuttle catalyst may be introduced by the separator at the first upper reactor end to the stripping column for the separated Sle to be extracted; or it may be first introduced into the fluidized bed reactor and mixed with the catalyst in the oo fluidized bed reactor; Then he enters the shaft for extraction. It is preferable to enter it first into the fluidized bed reactor and then into the stripping column for recovery. The cracking catalyst leaving the fluidized bed reactor enters the separation column of two of the catalyst vapors from the first upper reactors (tal stripping) for recovery. And the second is done in the same column as the blade. The recovered catalyst is fed into the regenerator to be regenerated. The regenerated catalyst is introduced to the first upper reactor and the second upper reactor 0 for use in recycling. In the catalytic cracking process for the production of propylene according to the present invention; The extraction steam and the extracted hydrocarbon stream are preferentially introduced into the bottom of the fluidized bed reactor; and drawn through the fluidized bed reactor. Therefore; The partial pressure of the hydrocarbon stream can be reduced and the residence time of the hydrocarbon stream in the separator can be reduced so as to increase the production of VO propylene and reduce the dry gas and coke output. In the catalytic cracking process to produce propylene according to the present invention; The aforementioned upper reactor is selected from one or more risers of equal diameter, risers of equal diameter, where the first upper reactor, the spate reactor, and the second upper risers can take the same or different types of reactor. Said fluidized bed reactor is selected from 0 one or more fixed fluidized bed; a particularly fluidized bed; bubble layer; a troubled class; quick layer; In the catalyst cracking process for the production of propylene according to the present invention” said catalysts (i.e. both catalytic cracking catalyst I and catalytic cracking catalyst II) comprise a shape-selective vy A-nm zeolite. The selective morphotype zeolite has 1.7 less average pore size than ferrite; Chapasite; ZSM of one or more 1.7 nm zeolites with an average pore size less than and/or chemically thereof. lumonite; a modified zeolite A dashyardite; erionite; Zeolite 11-//25; ZSM-8 ZSM-5 mentioned from one or more ZSM zeolites selected

ZRP 250 2500-48 2500-38 250-35 2500-23 500-22 500-12H and other zeolites having similar structures. For more detailed information about 5-/251; One example or HZSM=5 is 751/-5 more than the 251/-5 modified B© zeolite and transition metal(s). and be a zeolite

ZSM-5 Modified B© and the transition metal(s) mentioned for example are ZRP-type 0 or ZRP-11 zeolites and are ZRP-modified ZRP zeolites and iron. The zeolite may be modified with element(s); For example; © The rare earth metal(s). More ZRP

OYYYIVO US Patent No. ZRP Detailed information can be referred to 16112998. Canadian Patent No. 1211470, and Canadian Patent No. 16112998. Said catalyst can be zeolite-selective with medium V0 nm is one or more catalysts that are provided in the art 1.7 smaller than the previous art's pore size, are commercially available, or prepared by methods known in the prior art. It includes

JU said catalyst on zeolite; inorganic oxides; and optionally silt. For example, said catalyst contains 5-5 7 by weight of zeolite; 45-5 7 by weight of oxides other than by weight of silt. Said zeolite includes organic selective zeolite Fig. 7 70-1; f _ 0 nm; and optionally a large pore zeolite. The zeolite of 1.7 with an average pore size of less than wt; 7-7000 nm includes 1.7 morphology with an average pore size of less than wt of active ingredients. The aforementioned macroporous zeolite includes 7. 001-51 preferably by weight of the active ingredients. 0-7 50 by weight »preferably 2975-0 vq 0117 The macroporous zeolite is a zeolite with a porous structure characterized by a ring hole Ground Y = Jie zeolite is at least nm; It is chosen from one or more zeolites-7

Y and zeolite o(USY) ultrastable 7 zeolite ll terrestrial HY= zeolite (REY) rare zeolite-8; and Zeolite A. (REUSY) ESR 0 The said inorganic oxide is used as a binder and is selected from silica (5502) and/or alumina (81203). Said clay is used as a mould; i.e. as a carrier; It is selected from kaolin and/or halosite. In the catalytic cracking process for the production of propylene according to the invention” the shape-selective zeolite containing the catalyst having an average pore size of less than 17 nm used 0 in the second upper reactor and that used in the first upper reactor may be identical or not. preferably; The catalyst used in the first upper reactor and that used in the second upper reactor shall be identical. In the process of catalytic cracking to produce propylene according to the present invention; The catalytic cracker used includes at least an elie section, a regenerator section and a product separation system. Vo reactor section is preferably provided with a set of two risers and a fluidized bed; where one of the risers (preferably axially) is connected in series with a fluidized bed; The series connected assembly (axially) of the riser and fluidized bed shall be connected in parallel with another riser. Furthermore; The series connected assembly (axially) of one of said risers and fluidized bed (preferably axially) is coupled with a stripping column. 0 A catalytic cracker for the production of propylene according to an embodiment of the present invention is shown in Fig. 1. Said apparatus includes the following: first upper reactor o) second upper reactor oF and fluidized bed reactor o£) and separator (1); release device (0(¢) product separation system (1) ) and a regeneration device (1). The second upper reactor (7) and the fluidized bed reactor (;) are co-axially connected respectively. The fluidized bed reactor (;) is connected with the separator (7) and the release device (*). the

The first upper reactor (1) and release device (5) are not connected to each other. Release device (0) and product separation system (1) are connected to each other. The lower part of the second upper reactor (7) is provided with an inlet for cracked heavy oil and reaction section for cracked heavy oil.The inlet of the cracked heavy oil is connected to the outlet (©) of the cracked heavy oil of the product separation system (1) through a 0 pipeline (TT) an inlet for light hydrocarbon is provided between the inlet of the fractured (Jil) oil of the upper reactor the second (7) and the upper reactor outlet?; This inlet is made by the light hydrocarbon (TV) pipeline and said reaction section for the heavy oil fracture is placed between the inlet of the heavy oil fracture and the inlet of the light hydrocarbon. It is connected to the lower part of the separator (? to the sale device) of the generation (7) through the spent catalyst pipeline (8). The sale) generator (V) 0 is connected to the bottom of said reactor (1) through the regenerated catalyst pipeline (9). The sale) generator (V) is connected at the bottom of the upper reactor (7) through the regenerated catalyst pipeline (01). In the axially connected series of riser and fluidized bed assembly, the outlet of the riser is preferably provided with a low-pressure outlet distributor having a pressure drop of . 1 Less than 10 kPa Existing distributor with low pressure outlet can be used Jie Arc distributor The following detailed description of the preferred embodiments of the invention is provided with reference to the attached drawing The examples shown below are illustrative and will not be taken as limitations to the scope of the invention, which is defined only by the accompanying claims and their equivalents.Various variations and modifications to YS are evidentiary models disclosed to those skilled in the art and can be made without departing from their spirit and scope.As shown in Figure 1 a catalyst is divided Regenerated high-temperature catalytic cracking flowing into the reactor system into two streams » One of the two streams enters the bottom of the upper reactor 1 through the regenerated catalyst tube 9; And enter the other stream at the bottom of the upper reactor? Through the pipe of the regenerated catalyst .01, the catalyst current flows upwards under the influence of the initial lift medium from the Yo tubes 717 and 7?7.

And “preheated heavy feedstock (heavy hydrocarbons or hydrocarbon-rich animal or vegetable oils) is mixed through tube 01 and steam atomized from tube YY at a certain ratio and presented to the upper reactor 1. A mixture is separated from the stream hydrocarbon and catalyst by means of a quick separator (not shown) at the upper end of the reactor 1 to obtain the hydrocarbon stream 0 and the charred catalyst.Heavy oil fraction from product separation system 76 from the present equipment is mixed through the FT pipe and steam aerosolized through the pipe TA and introduced to the bottom of the upper reactor?. The mixture is connected with the high temperature recycled catalyst provided through tube 01 to react. The mixture of the hydrocarbon stream and the catalyst flows upwards along the upper reactor?. Thereafter i.e. at a location between the inlet of the 0 Crucified heavy oil and the upper reactor outlet oF The mixture is connected with a light hydrocarbon mixture through the pipe ?and vapor converted to mist through the pipe Yo to react and continue to flow along the upper reactor LY The mixture of all hydrocarbon streams and catalyst enters into Fluidized bed reactor ; via a distributor outlet (not shown) from upper reactor 7 to complete the reaction; Finally entering separator 0 to separate the hydrocarbon stream from the catalyst. 1 All hydrocarbon streams are collected; Including the hydrocarbon stream from the upper reactor 1 and the hydrocarbon stream from the fluidized bed reactor ─ by the vortex separation system on the upper part of the separator and drawn through the pipe Te to enter the subsequent product separation system 6. In the product separation system 6; The catalytic cracking product is separated into cracked gas (drawn through pipe 1?); cracked gasoline (drawn through pipe (VY) light cycle oil pe (drawn Yo through pipe (TY) heavy oil sue ( Through-tube drawn (VE) and an oil slurry ae (Vo-tube) The through-tube pulverized gas 71 was separated and filtered again to produce olefin-rich sins grade propylene (C4) where The said olefin-rich fraction C4 can be recycled back to the second upper reactor for conversion to propylene production.

Ad \ —_ _ part or all of the fractionated gasoline drawn through the YY pipe can be regenerated back to the second upper reactor 7 for further transformation. Further, fractionated gasoline can be separated into a light gasoline part and a heavy gasoline part; Can part or all of the light gasoline be recycled back to the second upper reactor? for additional shift. © Part or all of the fractionated heavy oil is circulated back through pipe 37 to the bottom of the upper reactor ¥ for further transformation. The charred catalyst separated by the quick separator at the upper end of the reactor 1 is introduced to the fluidized bed reactor; and mixing it with the catalyst from the upper reactor 7. After the reaction in the fluidized bed reactor of the mixed charred catalyst is introduced to the separator LF the separating steam is introduced through the pipe and is connected upstream using the mixed charred catalyst to separate the separated hydrocarbon stream after that to the separator© through the fluidized bed reactor; and withdrawn in conjunction with other hydrocarbon streams through pipe 70 out of separator 5. The separated catalyst is sent via spent catalyst pipe A to generation device sale 1 to burn Vo coke for regeneration. Oxygen-containing air Jie is introduced to the regeneration device 1 through the YT pipe The flue gas sale (sale) is withdrawn through the YY pipe The regenerated catalysts are circulated to the upper reactors 1 and 1 by Regenerated catalyst piping route 4 and 10 respectively for regeneration use. In the form represented above; The initial rise medium is supplied to upper reactors 1 and 0 via tubes 77 and 77 respectively. The following examples will illustrate the present invention. The feedstock 8 used in the ARN and comparative examples is atmospheric heavy oil; Its properties are listed in Table A

Except _ the catalyst used is a catalyst 1/1/46-2 produced by NO© SINOPEC CATALYST (BRANCH COMPANY) whose properties are listed in Table LY The said catalyst contains zeolite in the selected form with an average hole size of less than 107 nm Example 1 5 1 JU is implemented in experimental equipment In that experimental equipment the first upper reactor has a diameter of

11 mm internal and 7800 mm long; The second upper reactor has an inner diameter of 11 mm and a length of 3700 mm. The outlet of the second upper reactor is connected with the fluidized bed reactor having an inner diameter of TE mm and a height of 100 mm. The router has the same design as shown in Figure 1. Example 1 was run with a rotating system as discussed later in this document.

A high temperature regenerated catalyst is introduced to the bottom of the upper reactor 1 via the regenerated catalyst pipe 9 of the regenerator ov and flows upwards under the action of steam as the initial lift medium. Feedstock 8 was preheated and mixed with aerosolized steam. The mixture was introduced into the upper reactor 1 via the feed nozzle; And connect it with the hot regenerated catalyst to deliver the catalyst cracking reaction. The mixture of the hydrocarbon stream and the moving catalyst is introduced up the entire length of the reactor

1 upper 1 to the quick separator at the upper end of the reactor 1 to perform the gas-solid separation. after dismissal; The hydrocarbon stream is introduced into product separation system 1 to separate into gas and liquid products. The catalyst is located inside the fluidized bed reactor; under the influence of Earth's gravity. The other high-temperature recycled catalyst was transported via the regenerated catalyst pipe 0 to the bottom of the upper reactor 1 and moved upwards under the action of steam as the initial raising medium. is connected

Yo with a mixture of Vow 00 degree sie distillation range fraction heavy oil fraction of product separation system 1 and vapor aerosolized to react. The batter continued to move up; It was then connected with the recycled light gasoline fraction al (distillation range 85-708°C) provided by a nozzle at a level above the entry point of the heavy oil fractionated by ae 0010 and reacted; and moves up; and then it enters into the fluidized bed reactor; to complete the interaction. after the reaction; It was completed

the

Ad ¢ —_ _ separate the hydrocarbon stream from the catalyst carried on it in the separator; Then it is presented to the product separation system 6. Then the charred catalyst (i.e. the spent catalyst » including catalysts from the first upper reactor and the second upper reactor) is presented to the separator connected with the fluidized bed reactor from the bottom of the fluidized bed reactor. after dismissal; The spent catalyst was introduced to the generator (sale) 1 to come into contact with air and burn the coke at a high temperature to regenerate the catalyst. The regenerated catalyst was introduced to the two upper reactors via the regenerated catalyst piping for regeneration use. After separating the hydrocarbon stream adsorbed on the spent catalyst by the separated steam; The separated hydrocarbon stream was introduced into the separator for gas-solid separation. The conditions and results of the basic operation of Example 1 are listed in Table 7. Comparative Example 1 Comparative JU 1 was performed on experimental equipment. in that experimental stomach; Two upper reactors were used. The first upper reactor has an inner diameter of 16 mm and a length of can PAV and the second upper reactor has an inner diameter of VE mm and a length of 780860 mm. The difference from Example 1 was that no fluidized bed reactor 1 was connected to the outlet of the second upper reactor. The basic design for comparative example 1 in Figure 1 can be obtained from 01001747347 CN 8 (/010101074392). The shal of Comparative Example 1 is also performed using a rotation system substantially similar to that of Example 1. The basic operating conditions and results of Comparative Example 1 are listed in Table 7. Example Y 0 is performed JE ¥ in the same manner as Jie (example Lado) except that part 64 of the product separation system 1 cycled into the second upper reactor; And the operating conditions have been appropriately adjusted. Basic operating conditions and results for Example BY are listed in Table 7. Example?

And the methal was executed? in experimental equipment; As shown in Figure 1. In that experimental equipment which is in a continuous reaction regeneration system; The upper reactor has 1 inner diameter VT mm and a length of can 05 and the upper reactor has ? 11 mm inner diameter and YY ov mm long. The upper reactor outlet Y is connected to fluidized bed 9 which has an inner diameter of 14 mm and a height of 100 mm. The feedstock was Jill Air 8; The catalyst is MMC-2 The first high-temperature regenerated catalyst is introduced to the bottom of the upper reactor 1 from the Gob of the regenerated catalyst pipe 9 of the generator sale oF and LY flows under vapor effect as the primary lifting medium; It connects with the feedstock 8 supplied to the upper reactor 1 through the Yo pipe to react. after the reaction; The hydrocarbon stream and the catalyst are introduced to the separator © to separate from each other. The separated hydrocarbon stream was submitted to product separation system 6; The separated catalyst was introduced to fluidized bed reactor 4. The second high-temperature regenerated catalyst was transported through the regenerated catalyst tube 01 to the bottom of the upper reactor 1 and agitated upwards under the action of steam as the initial raising medium. delivered with a mixture of fractionated heavy oil fraction of distillation range 0-7000 05°C supplied to upper reactor 1 ? Through the pipe YT of the product separation system 1 and the vapor converted to aerosol through the pipe VA to react. Fractionated light gasoline (al) (distillation range 85-77 °C) was introduced into the upper reactor 1 at a level above the entry point of the heavy fractionated oil by 00 mm to participate in the reaction. The reaction mixture moves up along the upper reactor and into the fluidized bed reactor which is connected to the upper reactor by the upper reactor outlet. After reaction in Yo fluidized bed reactor; The hydrocarbon stream carried with a portion of the catalyst to enter the separator. after that; Gas-solid separation is connected by vortex separation system on the upper part of the separator. The hydrocarbon stream is introduced via pipe 1 into product separation system 1 to separate into gas and liquid products. After the reaction in the Jolie fluidized bed; The coke-containing catalyst (spent catalyst) falls inside the separator under the action of gravity. After separating the © hydrocarbon stream adsorbed on the spent catalyst by the separated steam; The stream is entered

©"

The separated hydrocarbon in the gas-solid separator. The separated spent catalyst was fed into the regenerator via the spent catalyst pipe A to come into contact with air and burn the coke at a high temperature to regenerate the catalyst. The regenerated catalyst was prepared for recycling use.

The basic operating conditions and results for Example © are listed in Table 4. Example 5-4 According to 1 JU The reaction conditions of Examples 5-4 are appropriately modified. Examples 5 Basic operating conditions and results are listed in Table 4. Comparative example?

0 Comparative example done? According to Led oF JE except that cracked light gasoline oil is inserted into the bottom of the upper reactor oF and heavy cracked oil is inserted in the bottom of fluidized bed 4. The part 64 cyclone of the product separation system 6 is inserted into the primary lifting section of the upper reactor 7. The basic operating conditions and results for the comparative example are listed in Table BY. Comparative example?

0 The comparative example ¥ was performed according to JU 1, except that light hydrocarbon was introduced at the bottom of the upper reactor 7; The inlet of the crushed heavy oil is mid-length from the light hydrocarbon inlet to the outlet of the upper reactor 7. The regenerated catalyst transported through the catalyst pipe to the upper reactor YY is connected to the light hydrocarbon for brief contact; Then contact with the crushed heavy oil that was introduced into the upper reactor? to interact; Then it enters the reactor

0 fluidized bed; to react. tables can? And the; Seeing that the process according to the present invention is capable of improving the yield of propylene and butylene; And also it can greatly reduce the output of coke and dry gas. Complete

the

Dry gas selectivity reduction system (i.e. dry yield /100 X conversion rate). The process according to the present invention has an increased ability to convert heavy oil and distribute a desirable product. Jabbul 1 geoe).

M. Note: / do not refer to the weight in the tables AY Table ? chemical composition / wt. 9 lbs.Y A203

AA Na20 1) RE203

4+ Physical properties Total hole size; [de g Na microhole size; [de g AE: specific surface; [Vo g Veo Specific Surface of Zeolite» m1/g 0 .5 Specific Surface of Mold; [Ya g Yao mass density; g/mL A Volume Distribution » 0-70 00 µm 0-46 1 µm 0-80 7 0-1101 µm 0-1101 21 0-19 µm VY. 8m" Table? JE Numbers Example 1 Example Y Comparator 1 Comparator Y

=” _ Example Example Numbers Example 1 Example 1 Comparator 1 Comparator Y Reaction pressure” Mega NAR NAR NAR NAR Pa (Absolute) Regeneration temperature; “oe 7” a 7 b 7 b 7 degrees YEP Reactor outlet temperature Oo ov. ov. upper; YEP grade Y.o stream reaction time 7 7 7 Hydrocarbon; Al is the catalyst/oil ratio; wt./Yauv kh yy.¢ Wt Ratio of Mist Stream (for new feedstock | yo A A A A)” 7 wt upper reactor combination second upper reactor and second fluidized bed temperature of catalyst inlet in upper reactor the second; | 140 140 5 E degree YEP

Example Example Judi numbers Example 1 Example ? Comparator 1 Comparator Y is the reactor outlet temperature

OT lo) $ 0 - d 0 - d 0 upper second; °C layer temperature» 25 degrees. / ov. Centigrade Layer Weight Vacuum Velocity 1 / 10 1- Instantaneous Ease; Heavy Oil Reaction Conditions

Ja Percentage of recycled heavy clumped oil 1 (relative to the new feedstock) » 7 by weight Heavy oil input location Reactor bottom Reactor bottom to reactor bottoms | The bottom of the broken layer The upper second The upper second The upper second | The liquefied is the total oil reaction time

RE 8 0.30 | The cracked in the upper Jaa reactor in seconds The reaction time of the broken heavy oil before contact with the 'light hydrocarbon' in seconds

Example Example Numbers Example 1 Example 1 Comparator 1 Comparator Y ian The reaction heat of heavy zyrite broken before this contact “5e TY.

with light hydrocarbon; YEP grade Ratio of stream transferred to atomizer (for fractionated Ve 10 A 10 heavy oil) –; A by weight ratio of catalyst/oil in cracked heavy zyrite; 1.? YY.y 7.0 w/w Amount of coke on catalyst during initial contact with

A YY YY 0 light hydrocarbon; 7 By weight Reaction conditions for light gasoline and the C4 fraction Ratio of the recycled C4 fraction (in relation to the new A / A feedstock) » 7 By weight

Ad — ¢ — Example Example Numbers Example 1 Example Y Comparator 1 Comparator Y You mm The lift segment is insertion site A for the primary Ca segment insertion site / / heavy oil clad For upper alll catalyst/oil ratio in A 1 / / 1 part «C4 w/ weight reaction time of part 4 in / / 1 no upper reactor; sec Ratio of stream converted to atomizer (for fraction 001 / / | “(C4 7 wt.) Percentage of light recycled gasoline (for raw | Yo VY VY VY fresh feed)” 7 wt m) “ final ol NE I - For light recycled gasoline; | Ao Ao Ao AO grade YEP

Example Example Numbers Example 1 Example ? Comparator 1 Comparator Y Yeo mm count .7 mm Yeo count mm After gasoline insertion site Insertion site Insertion site Bottom insertion site Jc lad Crushed Crushed Crushed Catalyst / oil ratio in light gasoline; Weight / 7. YY 1.4 1. The weight of the reaction time of light gasoline in the reactor | volume 0. 0.01 upper; mc-2| 10062 Supporting the supplication of the

C _ Example Example Numbers Jud) Example 1 Example ? Comparator 1 Comparator Y Dry (gas selectivity on) A . g oY dry) YT AVY AYA 4 coke (selective coke) dh as light hydrocarbon (for new feedstock)” 7 by weight a clear we table; example numbers example example? Jud ¢ example o comparative?

example numbers example example? Jud ¢ example o comparative?

RUN RT I I

The name of the raw material Nutrition 8 | Nutrition 8 | Nutrition 8 | Feed 8 Reaction pressure - MPa

AR AR AR YY

(a) The call temperature is the return temperature

You Yoo Yoo Yoo Celsius Reactor exit temperature ian ov. dah ovo upper; YEP score hydrocarbon stream reaction time” 10. 0. 0. 2 seconds, we pay 1 percent of the catalyst / zyrite ' weight / 11 Ve Ve 7 weight of the proportion of the stream converted to atomizer (for the new feedstock); 10 10 10 # wt combination of the second upper reactor and fluidized bed L

example numbers example example? Jud ¢ example o comparative? the temperature of the catalyst entering the second upper reactor; degree | 190 140 140 140 A she ian The reactor outlet temperature ovo ov. ov. ov. upper second; °C Layer Weight Vacuum Velocity AR 11 YY 7 Instantaneous; hr-1 yds 3 p oil reaction | |g sd Recycled Recycled Heavy Oil Percentage (for new feedstock 1.0 10 10 10 90)” #7 by weight

Ja) o Example numbers example? Example ¢ Comparative example? reactor | reactor | gasoline | upper cracked reactor | upper | light | to the upper exit to the exit | second | Ast] asl second reactor [YAY vo +90 cA] fracturing in the upper reactor; seconds is the reaction time of zerite to trust me

AL / Yo AI pre-contact fractionated with light hydrocarbon; Second, the reaction temperature of the refined heavy oil before contact with

Tye/1¢o odo light hydrocarbon; Celsius degree

q — ¢ — example numbers example 1 Jud example; Metal 5 comparison? Ratio of stream converted to mist (for heavy fractionated oil); 01 A A # by weight ratio of catalyst / oil in oil AY 1

broken heavy The weight/weight of the amount of catalyst coke during the exit of the crushed heavy oil from the | area YY / CY 0111 Reaction » 7 Hydrocarbon Reaction Conditions 1 3 5.4 Percentage of Recycled Light Gasoline (for new feedstock); | 71 VY Vo Vo # by weight is the final boiling point of gasoline

‎Ao Ao AO AO Light Round; degree of

Qo = _ Example JE Numbers Example 1 Example ¢ Comparative Example o ?

Yo 0 mm Yoo mm 0 mm

after site | After the location of the bottom | post site

Input Jaa Reactor 1 Input Light gasoline input site

Jal heavy a second Qaysl

Cracker (Sal) The catalyst/oil ratio in

7.3 1101 1101 YV.v “light gasoline”; The weight/weight of the reaction time of light gasoline

LY AA in the upper reactor; sec transform current ratio to 33 (for light gasoline); 7 | yo yo yo 01 by weight

MMC- MMC-2 1 MMC-2 | MMC-2 Catalyst 2l

_— \g Example numbers Example Juv ; Comparative analogy o? The gas yield/gas transformation rate OY “Le ¢YA is given to QAS . Dry (dry gas selectivity) coke yield/conversion rate 4 ounces per throat. Claclenet (selective coke) has a light hydrocarbon yield (for the new feedstock); # by weight we Note: in Tables 7 5 of new feedstock refers to heavy feedstock; any; feedstock 8 in the examples of the present invention. 1 indicates weight. The reaction pressure refers to the pressure of the separator.

Claims (1)

They are the elements of protection 1- A catalytic cracking process for the production of propylene, which includes: (1) Introduce the feedstock JB and a first catalytic cracking catalyst into a first upper reactor to perform a cracking reaction catalytic Separation of the resulting hydrocarbon stream and resulting shuttle catalyst by means of a separator at the reactor end first upper introduction of a hydrocarbon stream into a separation system for a subsequent product to be separated; Either directly enter 5 The SA catalyst is in a separator to be separated; or first inserting the shuttle catalyst into a Jolie fluidized bed; and then by inserting it into a separator to be separated; Introduce the separated catalyst into the regenerator to take place regenerate The first mentioned catalytic cracking catalyst contains a form-selective zeolite having an intermediate pore size less than 1.7 nm; (vii) introducing fractionated heavy oil into a second upper reactor; contact with a second catalytic cracking catalyst 0 introduced into the second upper reactor to react; The mentioned second catalytic cracking catalyst contains a zeolite Amorphous has an average pore size of less than 0.7 nm; (TV) introduction of a light hydrocarbon into the GB upper reactor at site after the introduction of the fractionated heavy oil; Mixing the light hydrocarbon with a mixture consisting of the contact and reaction of the fractured heavy oil and a catalyst second catalytic cracking; interaction; Vo said light hydrocarbon includes hydrocarbon 4© and/or a gasoline fraction obtained of said product separation system; (?) Introduction of a hydrocarbon stream and a catalyst obtained after the reaction into the second upper reactor at The fluidized bed reactor is connected in series with the second upper reactor for them to react; (0) After the reaction in the fluidized bed reactor, introduce the resulting hydrocarbon stream into the product separation system Yo to be separated; Introduce the resulting shuttle catalyst into a separator to be separated; And then Introducing the separated catalyst into the sale generating device for sale to be generated. “- The process according to Claim 1; where for the reaction of the heavy feedstock in the first upper reactor; Yo the reaction temperature ranges between 600-4860 m; the catalyst / oil ratio is 0 = oY the time ranges Ad —_ g reaction from cS) emo vapor to aerosol for the heavy feedstock is used with a weight-to-heavy feedstock ratio of 00 h m by weight and a reaction pressure of 1 d MPa (absolute). 5 7- The process according to claim 1, where for the reaction of the heavy feedstock in the first upper reactor; The reaction temperature ranges from 070-80 ca The catalyst/oil ratio is 05-17 The reaction time ranges from 1-?; seconds; Steam-to-aerosol for heavy feedstock is used with a weight-to-heavy feedstock ratio of 0—+ A 1 wt ¢ and a reaction pressure of ve. YO—nw. Y is MPa (absolute). 11, where before contact with the light hydrocarbon; The time of 11 lead); The catalyst/oil ratio for the heavy oil fractionated reaction is *e-.*: 0-101 7159-5 to a heavy oil fractionated aerosol used in a weight ratio to the heavy oil fractionated by weight; The temperature of the second catalytic cracking catalyst introduced into the second upper reactor is Vo from VY =e 2 —o operation according to claim ;; Where before contact with the light hydrocarbon; The contact reaction time for the cracked heavy oil and the second catalytic cracking catalyst in the second upstream (A) reactor is between a second. 7- The process according to the protection element, of where the temperature of the second catalytic cracking catalyst that was allay in the second upper reactor is from 0-786 eV YO #- The process according to the protection element of where in the second upper reactor ; The catalyst/oil ratio for the EASY fractionated heavy oil reaction is L _ g 4 - process according to claim (0) where in the second upper reactor; Before contact with the light hydrocarbon, the reaction temperature of the heavy oil, which is fractured, ranges from 100-880 °C. 4- Claim process (A where prior to contact with the light hydrocarbon; the reaction temperature of the fractured heavy oil is from 175-845 °C. -0 Claim process Gua) catalyst/oil ratio for the light hydrocarbon reaction In the second upper reactor 40-0. -11 0 the process according to claim 1, wherein said light hydrocarbon is a gasoline fraction and/or hydrocarbon 04; when said light hydrocarbon includes a gasoline portion; The reaction process conditions for the gasoline fraction in the second upper reactor include: catalyst/oil ratio (Fe) the reaction time is 0.5-0.1 s; vapor to aerosol for the gasoline fraction to be applied at a weight-to-gasoline fraction ratio of 0-8 727 wt; YO when said light hydrocarbon includes a hydrocarbon (C4) The reaction process conditions for C4 hydrocarbon in the second upper reactor include: catalyst/oil ratio ef em VY and the reaction time is 1-6 seconds. -1 The process according to Claim 0) where the weight ratio of the aforementioned cracked heavy oil to crude 0 said heavy feed shall be 0.01 sel FOm 1; and the weight ratio of said light hydrocarbon to said heavy feedstock shall be 00 SS A Dd VY process according to claim 0 where the weight ratio of said heavy fractured oil to Said heavy feedstock is: 0.90-0.09) and the weight ratio of said light hydrocarbon to AEE ERE The aforementioned lean feedstock is Yo £€¢ 64- Process under claim o) where for a fluidized bed reactor; Sha The reaction is from ca 080-50 0 and the gravimetric velocity per hour is from 1-50 ?/h. -1 The process according to claim 0 whereby the sintered catalyst obtained from ©1 upper reactor is introduced into the fluidized bed reactor. 7- The process according to claim 1, where the aforementioned feedstock JE is ALE hydrocarbons or animal or vegetable oils rich in hydrocarbons. -1#0 process under claim 1 wherein said fractionated heavy oil is a fraction having a distillation range of 0-"010©m or narrower fraction thereof obtained from separation in a product separation system. -08 Process according to claim 1 where said catalyst contains *-. 75 wt. Vo zeolite; 7495-5 Wt Inorganic Oxides; ZY em as by weight of opal) where The aforementioned zeolite contains from 78-7000 by weight of morph-selective zeolites with an average size Pores less than 1.7 nm and zero-7779 by weight of large pore zeolites. NA catalytic cracker for the production of propylene; Includes: (7) a fluidized bed reactor (;); separator oY) OB first upper reactor (1); upper reactor 0 launcher (5); A product separation system (1) and a regeneration device (7); in which the second upper reactor (7) and the fluidized bed reactor (;) are co-axially connected respectively; the fluidized bed reactor (;) is connected to the separator ( ?) and launcher (0) Upper reactor and launcher (0) connected to each other; launcher (5) and first (1) separation system connected Yo product (1) are connected to each other; the bottom of the second upper reactor (7) is provided with a heavy oil cracked inlet and a heavy oil cracked reaction section; the heavy oil inlet is connected the h —_ g The fractured heavy oil outlet (V8) of the product separation system (1) through the pipeline (V1) to deliver the fractured heavy oil to the product separation system (6); the regeneration device (V) is connected to the separation device oY) first upper reactor (1) and second upper reactor (7) respectively through spent catalyst pipeline (A) catalyst pipeline (9) to first upper reactor (1); catalyst pipeline 0 (01) to the second upper reactor (7); a light hydrocarbon inlet is provided between the fractured Jul oil inlet of the second upper reactor (7) and the upper reactor outlet “; the reaction section is located The aforementioned is for the heavy oil that is broken between the inlet of the heavy oil and the inlet of the light hydrocarbon. _ 7 g except b 1 ) 1 1 aha Fal 1 0| ope me To 1 0 Po = | a and NN NE Nog 1 * a 3 i 5 + - i ) ! A tad Co i EAE i ey 4 EE "p: ben I md i i ah a a T i ow i i Ea 4 . i e ja C I Ba | That Matt The | th vs Fe . By yi C A B MERE A May wR to Sunjin | } **-Lt vo | Fo , A ¥ for Ty 1 The validity period of this patent is twenty years from the date of filing the application, provided that the annual financial fee is paid for the patent and that it is not invalid or forfeited for violating any of the provisions of the patent system, layout designs of integrated circuits, plant varieties, and industrial designs, or its executive regulations issued by King Abdulaziz City for Science and Technology; Saudi Patent Office P.O. Box TAT Riyadh 57??11 ¢ Kingdom of Saudi Arabia Email: Patents @kacst.edu.sa