WO2019015580A1

WO2019015580A1 - Productive catalytic conversion method for producing propylene

Info

Publication number: WO2019015580A1
Application number: PCT/CN2018/095952
Authority: WO
Inventors: 石宝珍
Original assignee: 石宝珍
Priority date: 2017-07-21
Filing date: 2018-07-17
Publication date: 2019-01-24
Also published as: CN108794292B; CN108794292A

Abstract

The present invention relates to the technical field of catalytic conversion of petroleum hydrocarbons and specifically relates to a productive fluid catalytic conversion method for producing propylene. Catalytic raw oil and a light hydrocarbon respectively undergo reactions in a raw oil reactor and a light hydrocarbon reactor; the light hydrocarbon reaction process consists of gasification using a catalyst or a spent catalyst after a low-temperature light hydrocarbon reaction, and a high-temperature catalytic cracking reaction; the heat needed by the light hydrocarbon reactor is provided by a catalytic cracking reaction zone in the middle; the catalyst or the spent catalyst after the low-temperature light hydrocarbon reaction is used for gasifying light hydrocarbon; the gasified light hydrocarbon enters the catalytic cracking reaction zone and contact the catalyst from a regenerator to implement the catalytic cracking reaction of the light hydrocarbon; the catalytic cracking reaction of the light hydrocarbon is carried out in a fluidized bed or a circulating fluidized bed. The method in the present invention is able to implement low-temperature spent catalyst gasification and a pre-reaction, achieves an independent high-temperature cracking reaction of light hydrocarbons in a catalytic cracking reaction zone, improves propylene selectivity, and significantly reduces yields of byproducts such as dry gas and coke.

Description

Catalytic conversion method for producing propylene

Technical field

The invention belongs to the technical field of catalytic conversion of petroleum hydrocarbons, and particularly relates to a catalytic conversion method for producing propylene, which can improve the yield of propylene.

Background technique

Propylene is one of the most important petrochemical raw materials. 70% of propylene is produced by a tubular furnace cracking process for petroleum hydrocarbons, and another 30% of propylene is supplied by a catalytic cracking process. Drawing on the operation and design experience of conventional heavy oil catalytic cracking reaction-regeneration system, researchers at home and abroad have developed a series of process technologies for heavy oil catalytic cracking to produce propylene.

KBR and Mobil Technology have jointly developed Maxofin technology for the production of propylene from heavy oil. The technology uses a double riser reactor. The first riser cracks the conventional FCC feedstock, and the reaction produces naphtha into the second. The root riser cracking increases propylene production, and the two risers share a settler and regenerator.

UOP has developed the RxPro technology for the production of propylene from carbon tetra- or higher-carbon olefins. The technology also uses a double riser reactor structure. The first riser reactor is used for the cracking of heavy feedstocks, and the second riser reactor is used. The C4 component and naphtha produced in the first reactor are recirculated, and the two reaction products are separately fed into separate fractionation systems.

China University of Petroleum (East China) has developed TMP technology based on two-stage riser catalytic cracking technology. This technology uses heavy oil as raw material and utilizes two-stage riser catalytic cracking process for segmentation reaction, catalyst relay and large oil-to-oil ratio. Process characteristics, optimized mixing of feed materials for different reactive materials, control of suitable reaction conditions of different materials, in order to achieve the purpose of improving propylene yield.

The Sinopec Research Institute of Petroleum and Petrochemicals (Shike Institute) has developed DCC technology with heavy oil as raw material and propylene as the target product. The reactor of this technology is a riser-flow fluidized bed series reactor. Based on the DCC process, the Institute of Science and Technology has developed an enhanced catalytic cracking technology (DCC-PLUS) using a new combined reactor system. This technology is identical to the DCC process in that it uses a riser reactor plus a fluidized bed reactor. The form differs in that the DCC-PLUS process introduces another regenerated catalyst from the regenerator into the fluidized bed reactor. Regardless of DCC or DCC-PLUS, one reactor is divided into two series of cracking reaction zones, that is, both the riser and the fluidized bed are subjected to catalytic cracking reaction, the riser part is subjected to the cracking reaction of the feedstock, and the fluidized bed is partially made of the riser. The intermediate product in the reaction zone is further subjected to a secondary cracking reaction for increasing propylene production, and the whole fraction of the feedstock reaction product, including the slurry, the refinery oil, the diesel oil and the catalyst, enters the fluidized bed reaction zone to continue the secondary in the fluidized bed. The reaction, while the oil slurry, the refining oil, and the diesel oil are partially rich in aromatic hydrocarbons, contribute little to the propylene yield, and the excessive reaction causes an increase in the yield of coke and dry gas. Since the catalyst in the fluidized bed reaction zone is the raw material for the reaction of the feedstock oil, the catalytic cracking performance of the small molecule in the fluidized bed reaction zone is lowered, and the reaction temperature is further increased to increase the propylene yield, thereby further reducing the selectivity of propylene. Both DCC and DCC-PLUS use regenerant cycle. The space velocity of the fluidized bed reaction zone of fixed feedstock can only be controlled by the catalyst inventory in the reactor. Therefore, the reaction part itself needs to be set up for catalyst storage and stripping. And adjustment measures increase the complexity of the reactor. In addition, the catalysts in the DCC and DCC-PLUS fluidized bed cracking reaction zone are the carbon deposition catalysts after the reaction of the feedstock oil. In order to increase the propylene yield, it is necessary to further increase the reaction temperature in the fluidized bed reaction zone, which inevitably leads to the limitation of the catalytic cracking reaction. The increase in reaction greatly reduces the selectivity of propylene, resulting in a high yield of dry gas and coke. Furthermore, in the existing riser and fluidized bed series reactor, the bottom of the riser, that is, the pre-lift section, has the highest temperature throughout the reaction process, and the riser reaction zone is the high temperature zone which is second only to the pre-lift section of the bottom of the riser; The bed reaction zone and the gas-solid separator are all dilute phase space, and the oil and gas still carry a large amount of catalyst when leaving the fluidized bed, and the residence time of the oil and gas leaving the fluidized bed to the gas-solid separator is more than 20 seconds, causing the reaction to be timely. Upon termination, propylene is further thermally cracked, affecting product distribution and propylene selectivity.

The above prior art focuses on the production of propylene, which is divided into two categories. The first type is a riser-type fluidized bed series reaction, and the second type is a double riser parallel reaction. The researchers believe that the propylene in the heavy oil catalytic cracking reaction is indirectly formed by secondary cracking of the gasoline fraction produced by primary cracking of heavy hydrocarbons. The C5-C8 olefin in the gasoline fraction is the main precursor of propylene. The prior art has a number of features in common, and employs higher reaction temperatures, ratios of agent to oil, and steam injection than conventional FCC processes to increase the depth of the cracking reaction and the selectivity of propylene.

In the prior art, all or most of the heat required by the reactor is supplied from the bottom of the reactor, and the catalyst from the regenerator also enters the reactor mainly from the bottom of the reactor, and the bottom of the reactor is the highest temperature in the reactor; Contact with the highest temperature catalyst. The present application creatively alters the original regenerant distribution pattern and heating mode to provide better microscopic reaction conditions and reactive gas-solid contact forms for light hydrocarbon reactions.

Summary of the invention

One of the objects of the present invention is to provide a catalytic conversion process for producing propylene which increases the yield of propylene and significantly reduces the yield of by-products such as dry gas and coke.

Another object of the present invention is to provide an apparatus for carrying out the above-described catalytic conversion method for producing propylene.

The technical scheme of the present invention is as follows:

A catalytic conversion method for producing propylene, the method comprising:

Setting a feedstock oil reactor and a light hydrocarbon reactor;

The catalytic feedstock oil (fresh feedstock oil) is atomized by steam into the feedstock oil reactor, contacted with a regenerant (regenerated catalyst) from the regenerator, or a mixed catalyst of the regenerant and the light hydrocarbon biocide, and then gasified and carried out. Catalytic cracking reaction, the feedstock oil reaction product (reacted oil and gas) is separated from the entrained catalyst by a cyclone in a settler and then exits the settler;

The light hydrocarbon reactor is provided with a catalytic cracking reaction zone for transporting the distribution zone and increasing temperature from bottom to top, and light hydrocarbons (light hydrocarbon feedstock, liquid or gaseous) enters the light hydrocarbon reactor in the transport distribution zone; the light hydrocarbon gas is in the catalytic cracking reaction The zone undergoes a catalytic cracking reaction, wherein the catalytic cracking reaction zone adopts a fluidized bed or a circulating fluidized bed condition; the catalyst from the regenerator enters the catalytic cracking reaction zone, provides heat required for the light hydrocarbon reactor, and improves the logistics in the catalytic cracking reaction zone. After the temperature, the light hydrocarbon is subjected to catalytic cracking reaction, and the reaction temperature is controlled by the amount of the catalyst from the regenerator; the catalyst after the light hydrocarbon reaction or the light hydrocarbon biocide is distributed from the catalytic cracking reaction zone or the bottom of the light hydrocarbon reactor. The zone returns to the light hydrocarbon reactor.

In the present invention, the catalyst from the regenerator is either a fully regenerated regenerant (regenerated catalyst) or a semi-regenerant which is not completely regenerated, and the difference is that the amount of carbon deposition is different, but the activity of the semi-regenerant can also be normal. In the present invention, when the regenerator uses a countercurrent two-stage regeneration method for catalyst regeneration, the semi-regenerant is a semi-regenerant having a carbon content of less than 0.4%. Specifically, the regenerator uses a countercurrent regeneration form, a semi-regeneration zone. And the regeneration zone is arranged up and down, the semi-regeneration zone is above, the regeneration zone is below, and the semi-regeneration zone where the green agent enters above is also called a regeneration zone. After partial regeneration reaction, the catalyst enters the regeneration zone through the circulation pipe, also called the second regeneration. The zone continues to regenerate and the regenerant enters the feedstock reactor; the flue gas from the regeneration zone continues to enter the semi-regeneration zone and the carbon content of the semi-regenerant is controlled by the residence time of the semi-regeneration zone catalyst. Regarding countercurrent regeneration, two-stage regeneration, and semi-regeneration, all of them are well known in the art and will not be described in detail herein.

In the present invention, after the light hydrocarbon reaction, the stripped catalyst is referred to as "light hydrocarbon waiter (light hydrocarbon standby catalyst)", and the unstripped catalyst is referred to as "light hydrocarbon reaction catalyst", both The amount of carbon deposits is the same, but the catalyst after the light hydrocarbon reaction also carries a small amount of reaction product, namely oil and gas.

In the above catalytic conversion method for producing propylene, further, when the light hydrocarbon is in a liquid state (liquid state), the light hydrocarbon reaction is carried out by a catalyst double circulation method, and the light hydrocarbon is vaporized in the transport distribution zone, and the zone becomes a light hydrocarbon gasification zone. In this area, a light hydrocarbon gas is pre-contacted with the catalyst, and it takes time to gasify the light hydrocarbon. The gasification process and the transportation process are inevitably accompanied by a certain reaction, which is a passive accompanying reaction. This zone is also known as the pre-reaction zone; the catalyst for gasification of light hydrocarbons, ie the gasification catalyst, enters the transport distribution zone, the catalyst from the regenerator enters the catalytic cracking reaction zone; the light hydrocarbons are atomized by steam in the atomizing nozzle After entering the transport distribution zone or the light hydrocarbon gasification zone, the gas is contacted with the gasification catalyst, the light hydrocarbon is first gasified at a lower temperature than the catalytic cracking reaction zone, and then contacted with the catalyst from the regenerator in the catalytic cracking reaction zone to raise the temperature. And carry out catalytic cracking reaction; the conveying distribution zone or the light hydrocarbon gasification zone adopts the condition of gas-solid conveying bed or tubular gas-solid conveying bed; when the conveying distribution zone adopts tubular gas-solidification When the feed bed, the light hydrocarbon during transport in a tube in direct contact with a gasification catalyst.

In the present invention, when the light hydrocarbon enters the transport distribution zone in a gaseous state, the catalyst entering the transport distribution zone is a light hydrocarbon-reacted catalyst or a light hydrocarbon spent agent, or a light hydrocarbon-reacted catalyst or a light hydrocarbon spent agent and The regenerant enters the transport distribution zone at the same time, and the light hydrocarbon gas is heated by the catalyst to enter the catalytic cracking reaction zone for catalytic cracking reaction.

The above-mentioned catalytic conversion method for producing propylene, further, the catalyst from the regenerator directly enters the fluidized bed or the circulating fluidized bed of the catalytic cracking reaction zone, increases the temperature of the catalyst and oil and gas in the catalytic cracking reaction zone, and performs light hydrocarbon catalysis. The cracking reaction; or the catalyst from the regenerator is cooled first and then enters a fluidized bed or a circulating fluidized bed to carry out a light hydrocarbon catalytic cracking reaction.

In the above-mentioned method for producing propylene, a part of the light hydrocarbon-reacted catalyst or the light hydrocarbon spent agent is returned to the light hydrocarbon reactor, and the part of the catalyst enters the light hydrocarbon reactor from the catalytic cracking reaction zone in the middle or enters the light from the bottom transfer zone. A hydrocarbon reactor; when the catalyst after the light hydrocarbon reaction enters the light hydrocarbon reactor from the catalytic cracking reaction zone in the middle, the light hydrocarbon enters the light hydrocarbon reactor in a gaseous state.

The above-mentioned catalytic conversion method for producing propylene, further, the catalyst or gasification catalyst entering the transport distribution zone is a light hydrocarbon reaction catalyst or a light hydrocarbon green agent, or a catalyst from a regenerator, or a light hydrocarbon reaction catalyst or A mixed catalyst of a light hydrocarbon spent agent with a catalyst from a regenerator, preferably a light hydrocarbon spent.

The above-mentioned catalytic conversion method for producing propylene, further, the regenerator adopts a countercurrent two-stage regeneration mode, the catalyst from the regenerator entering the catalytic cracking reaction zone, and a semi-regeneration zone from the regenerator (also called A section of regeneration zone) is a semi-regenerant of certain carbon deposits, and its carbon content is not higher than 0.4%.

The above-mentioned catalytic conversion method for producing propylene, further, the refinery oil produced by the reaction of a part of light hydrocarbons, the refinery oil in the feedstock reaction product, and/or the hydrogenated catalytic cracked diesel oil at the outlet of the catalytic cracking reaction zone or In the light hydrocarbon reactor transport pipe (process is downstream of the catalytic cracking reaction zone) into the light hydrocarbon reactor, using the heat of the catalytic cracking reaction zone stream and the catalyst to achieve the reaction of the partial stream, while reducing the light hydrocarbons in the catalytic cracking reaction zone The degree of post reaction of the reaction product. In the present invention, after the fluidized bed or the circulating fluidized bed is behind or downstream, that is, the outlet region of the catalytic cracking reaction zone or the conveying pipe region behind the catalytic cracking reaction zone, another post-reaction medium such as refining oil and/or hydrogenation is introduced. After the catalytic cracking diesel oil, the heat of the light hydrocarbon reaction and the catalyst are used to realize the reaction of the subsequent reaction medium, and the temperature of the light hydrocarbon reaction stream is lowered, and the post reaction degree of the light hydrocarbon reaction product in the fluidized bed or the circulating fluidized bed is lowered. To achieve control of the depth of high temperature catalytic cracking reaction of light hydrocarbons.

The above-mentioned catalytic conversion method for producing propylene, further, when the light hydrocarbon is selected from the group consisting of C4 (carbon four), heavy catalytic gasoline, straight run naphtha, catalytic light gasoline, and coking gasoline, the classification is performed according to the difficulty of cracking. In the feed reaction, the order of the graded feed is C4, heavy catalytic gasoline, straight run naphtha, catalytic light gasoline, and coking gasoline from bottom to top.

In a specific implementation, the light hydrocarbon is a feedstock oil reactor self-produced gasoline (ie, crude gasoline) or light gasoline, or an external gasoline or light gasoline fraction, a naphtha, a C ₄ to C ₁₀ fraction, or a mixture of the above materials. Component; light gasoline fraction or other olefin-rich light hydrocarbons are preferred as light hydrocarbon feedstock; when C _{4 is} used as a separate light hydrocarbon reaction feedstock, it can be used as a feed for light hydrocarbon reactor feedstock or feedstock oil reactor. when the feed stock oil of the reactor, C ₄ feedstock oil into the reactor with the regenerated catalyst before contacting the feedstock under catalytic inlet pipe.

The graded feed reaction, that is, according to the difficulty of cracking, the material with high cracking difficulty is first contacted with the catalyst, and then the material with low difficulty in cracking is fed.

When C4, straight run naphtha or catalytic heavy gasoline is reacted as a light hydrocarbon in a light hydrocarbon reactor, the catalyst from the regenerator enters the transport distribution zone, first C4, catalytic heavy gasoline, straight run naphtha or Pre-reaction.

The above-mentioned catalytic conversion method for producing propylene, further, when the transport distribution zone does not enter the catalyst, the light hydrocarbon enters the transport distribution zone (26) in a gaseous state (gas state), and then enters the fluidized bed of the catalytic cracking reaction zone or The circulating fluidized bed, the light hydrocarbon spent agent enters the light hydrocarbon reactor in the fluidized bed or circulating fluidized bed zone.

In the above catalytic conversion method for producing propylene, further, the light hydrocarbon reaction product (also referred to as light hydrocarbon reaction oil and gas) flows out of the settler and then exchanges heat with the liquid light hydrocarbon to be reacted to vaporize the liquid light hydrocarbon to be reacted simultaneously. The light hydrocarbon reaction product is cooled; the heat exchange uses a vertical shell-and-tube heat exchanger, and the high-temperature light hydrocarbon reaction product flows in the tube process (ie, the heat exchange tube), and the liquid light hydrocarbon to be reacted is in the shell side (shell The side flows, which is outside the heat transfer tube; the light hydrocarbon reaction product flows from above the heat exchanger to the bottom, and the liquid light hydrocarbon to be reacted flows from the bottom to the top in the heat exchanger housing.

In the method of the invention:

1. The catalytic feedstock oil and light hydrocarbons are respectively subjected to catalytic cracking reaction in two reactors, the light hydrocarbon reactor is provided with a transport distribution zone, a catalytic cracking reaction zone, and a transport pipe is also provided; the light hydrocarbon catalytic cracking reaction adopts a specific catalytic raw material. High reaction temperature of oil.

2. The petroleum hydrocarbon catalytic cracking or cracking reaction is an endothermic reaction, and the heat required for the reaction is provided by a catalyst from the regenerator. In a specific implementation, in order to uniformly distribute the regenerant from the fluidized bed or the circulating fluidized bed, a catalyst distributor may be disposed in the catalytic cracking reaction zone to distribute the regenerant through the distribution measure in the cross section of the reactor; When the reacted catalyst or light hydrocarbon spent agent is returned to the fluidized bed or the circulating fluidized bed, a catalyst distributor is disposed in the catalytic cracking reaction zone, and the catalysts can also be distributed in the reactor cross section by distribution measures; The catalyst or light hydrocarbon reacted catalyst or light hydrocarbon spent agent enters the fluidized bed or circulating fluidized bed from the catalyst distributor to effect catalyst partitioning and mixing.

3. Light hydrocarbon gas undergoes light hydrocarbon catalytic cracking reaction in the catalytic cracking reaction zone; light hydrocarbon reaction is divided into low temperature gasification or transportation process and high temperature catalytic cracking reaction process; heat supply catalyst from regenerator is catalyzed in the middle of light hydrocarbon reactor The cracking reaction zone enters the light hydrocarbon reactor, and the light hydrocarbons achieve high temperature catalytic cracking reaction in the catalytic cracking reaction zone in the middle of the light hydrocarbon reactor.

4. When the catalytic cracking reaction zone adopts a fluidized bed, the apparent gas flow rate is 1.2 m/s or less, preferably the apparent gas velocity is 0.6 m/s to 1.2 m/s; the catalytic cracking reaction zone adopts circulating fluidization. At the bed, the apparent gas flow rate is greater than or equal to 1.2 m/s, preferably from 1.2 m/s to 3.0 m/s; preferred reaction conditions are:

When the light hydrocarbon is a fraction having a final boiling point of less than 200 ° C, the reaction temperature of the catalytic cracking reaction zone is 530 ° C to 620 ° C for the purpose of producing propylene and ethylene, and the catalytic cracking reaction zone is used for the purpose of producing propylene and ethylene. The reaction temperature is 640 to 700 ° C;

When the gasoline is the target product, the light hydrocarbon is a light cycle oil fraction of 200 ° C to 350 ° C, the reaction temperature of the light hydrocarbon catalytic cracking reaction zone is 490 to 530 ° C;

The catalyst has a weight hourly space velocity of 2 to 15 (1/h) in a fluidized bed or a circulating fluidized bed.

5. The present invention returns a portion of the light hydrocarbon-reacted catalyst or light hydrocarbon spent agent to a light hydrocarbon reactor which enters the light hydrocarbon reactor from the catalytic cracking reaction zone in the middle or enters the light hydrocarbon from the bottom distribution zone. a reactor; when the catalyst after the light hydrocarbon reaction enters the light hydrocarbon reactor from the catalytic cracking reaction zone in the middle, the light hydrocarbon enters the light hydrocarbon reactor in a gaseous state;

The light hydrocarbon reacted catalyst can be returned to the light hydrocarbon reactor from the stripping zone of the settler or from the light hydrocarbon reactor to the light hydrocarbon reactor.

6. The light hydrocarbon reactor is provided with a conveying pipe at the outlet of the fluidized bed or the circulating fluidized bed reaction zone, and the outlet of the conveying pipe, that is, the outlet of the light hydrocarbon reactor is disposed in the settler, and the gas outlet separator is arranged at the outlet of the conveying pipe to react the light hydrocarbon The product and the catalyst are rapidly subjected to gas-solid separation; in the specific implementation, the product of the light hydrocarbon reaction catalytic cracking reaction zone is cooled by injecting the liquid medium in the fluidized bed or the circulating fluidized bed outlet or the conveying pipe to realize the light hydrocarbon in the fluidized bed or The reaction after the completion of the catalytic cracking reaction in the circulating fluidized bed is rapidly terminated; the liquid medium preferably uses the refinery oil in the feedstock reaction product or the hydrogenated catalytic diesel or a part of the light hydrocarbon raw material to realize the catalyst for the light hydrocarbon catalytic cracking reaction zone. And reuse of waste heat.

7. The fluidized bed and circulating fluidized bed are technical names for gas solid fluidization, and are well defined in the art.

8. In the present invention, the feedstock oil reaction product and the light hydrocarbon reaction product are separated from the catalyst by a gas-solid separator in a settler, and the catalyst is regenerated after being stripped by the stripper;

The light hydrocarbon reactor and the feedstock oil reactor may share a settler, the two reactors being disposed outside the settler or one reactor being disposed coaxially with the settler; the light hydrocarbon reactor outlets in the settler are directly provided with independent light Hydrocarbon reactor gas-solid separator, light hydrocarbon reaction catalyst and oil and gas enter the light hydrocarbon reactor gas-solid separator to achieve separation of oil and gas and catalyst, after separation of the catalyst, light hydrocarbon reaction oil and gas outflow settler; light hydrocarbon reaction product can be The feedstock reaction products are mixed together and exit the settler, and the settler can also be discharged from a separate line; if necessary, the settler is provided with an independent light hydrocarbon reaction product outlet, and the light hydrocarbon reaction product is directly reacted from the gas-solid separator from the independent light hydrocarbon The product outlet exits the settler and is not mixed with the feedstock reactor product;

When two reactors use a settler, it is also possible to simultaneously provide a separate light hydrocarbon reactor gas-solids separator and a stripping zone, ie a second stripping zone, in the light hydrocarbon reactor outlet in the settler, light hydrocarbon reactor gas. The catalyst separated by the solid separator first enters the second stripping zone and then enters the stripper below the settler, and a part of the catalyst, that is, the light hydrocarbon standby agent, is returned from the second stripping zone to be mixed with the regenerant. Continued to catalyze the reaction of the feedstock oil

The light hydrocarbon reaction or the light hydrocarbons from the second stripping zone or the light hydrocarbons are returned to the transport distribution zone to directly contact the light hydrocarbons to achieve gasification of the liquid light hydrocarbons or to increase the temperature of the light hydrocarbons; The hydrocarbon or gasified light hydrocarbon, steam is transported upward together with the catalyst into the catalytic cracking reaction zone; or the catalyst after partial light hydrocarbon reaction is directly returned to the fluidized bed or the circulating fluidized bed; the catalyst after the reaction of the light hydrocarbon The amount of return controls the temperature of the transport distribution zone or the weight hourly space velocity of the catalytic cracking reaction zone, thereby controlling the degree of reaction and product distribution in the catalytic cracking reaction zone.

9. In the present invention, the light hydrocarbon reactor is added to the steam to reduce the partial pressure of the hydrocarbon, and the total mass flow rate of the light hydrocarbon atomized and replenished steam is greater than 15% of the mass flow rate of the light hydrocarbon entering the light hydrocarbon reactor, generally 20 to 40%; The steam enters the light hydrocarbon reactor in the transport distribution zone or in the catalytic cracking reaction zone; the steam preferentially enters the light hydrocarbon reactor in the gas transport distribution zone upstream of the catalytic cracking reaction zone.

10. When the light hydrocarbon is a gas, it enters the catalytic cracking reaction zone through the distribution plate or the distribution pipe, and enters the catalytic cracking reaction zone through the distribution plate when the light hydrocarbon gas transports the catalyst or when the catalyst is used to raise the temperature; the light hydrocarbon is the liquid feed gas After the reaction, the catalyst is passed through a distribution plate into a fluidized bed or a circulating fluidized bed catalytic cracking reaction zone.

11. When the catalyst or light hydrocarbons after the regenerant and the light hydrocarbons are reacted simultaneously into the fluidized bed or the circulating fluidized bed, the catalyst or the light hydrocarbon bioreactor after the light hydrocarbon reaction is preferentially entered into the reaction zone under the regenerant. .

The present invention also provides a catalytic converter for producing propylene, and in particular, the apparatus is a device for carrying out the catalytic conversion process for producing propylene according to the present invention.

According to a particular embodiment of the invention, the apparatus comprises: a feedstock oil reactor, a light hydrocarbon reactor and a regenerator;

The feedstock oil reactor is provided with a catalytic feedstock oil inlet, and is provided with a regenerant inlet from the regenerator, or a regenerant and a light hydrocarbon standby agent inlet; a settler is arranged above the feedstock oil reactor, and the settler is provided for separating the raw materials a cyclone separator for the catalyst entrained by the oil reaction product, the settler is further provided with an outlet of the raw material oil reaction product after separating the entrained catalyst;

The light hydrocarbon reactor is provided with a transport distribution zone and a catalytic cracking reaction zone for increasing temperature from bottom to top, and the transport distribution zone is provided with an inlet of light hydrocarbons into the light hydrocarbon reactor; the catalytic cracking reaction zone adopts a fluidized bed or a circulating fluidized bed. Condition; the catalytic cracking reaction zone is provided with a catalyst inlet from the regenerator; and the catalytic cracking reaction zone or the bottom transport distribution zone in the middle of the light hydrocarbon reactor is provided with a light hydrocarbon reaction catalyst or a light hydrocarbon standby agent to return light hydrocarbons The inlet to the reactor.

The beneficial effects of the invention:

1. The light hydrocarbon of the invention is first contacted with a low temperature moderate carbon deposition catalyst to achieve low temperature gasification and pre-reaction, and an independent high temperature cracking reaction of light hydrocarbon in the catalytic cracking reaction zone can be achieved, and propylene selectivity can be improved;

2. The light hydrocarbon of the invention adopts a catalyst from a regenerator to enter a light hydrocarbon reactor in a fluidized bed or a circulating fluidized bed to realize an independent high temperature cracking reaction, and the heat of the catalytic cracking reaction does not need to be provided in the transport distribution zone to realize light hydrocarbons. Optimization of catalyst conditions in the reactor;

3. The invention realizes the rapid termination of the fluidized bed reaction, reduces the thermal reaction, alleviates the contradiction between increasing the production of propylene and reducing the dry gas, and significantly reduces the yield of by-products such as dry gas and coke while increasing the yield of propylene. .

DRAWINGS

1 is a schematic view showing a first embodiment of a method for catalytic conversion of propylene produced by the present invention;

2 is a schematic view showing the second embodiment of the method for catalytic conversion of propylene produced by the present invention;

3 is a schematic view showing the third embodiment of the method for catalytic conversion of propylene produced by the present invention;

4 is a schematic view showing the fourth embodiment of the method for catalytic conversion of prolific propylene according to the present invention;

Figure 5 is a partial schematic view of gas delivery distribution using a distribution tube in the method of the present invention.

The numbered contents in the figure are as follows:

1 feedstock oil reactor, 11 feedstock oil reaction regeneration inclined pipe, 12 standby raw pipe, 12A green agent, 13 catalytic feedstock oil, 14 catalytic feedstock oil inlet pipe, 15 light hydrocarbon waste agent inlet pipe;

2 light hydrocarbon reactor, 21 light hydrocarbon reaction regeneration inclined tube, 22 light hydrocarbon reaction catalyst outlet, 22A light hydrocarbon reaction catalyst, 23 light hydrocarbon reaction catalyst inlet tube, 23B light hydrocarbon standby agent inlet tube, 24 light hydrocarbons, 24A gaseous light hydrocarbons, 25 light hydrocarbon inlet tubes, 26 transport distribution zones, 26A catalytic cracking reaction zone, 26B distribution plates, 26C distribution pipes, 27 transfer pipes (ie light hydrocarbon reactors and settler connecting pipes), 28 transport distribution zone (tubular gas-solid transport bed) regenerant inlet pipe, 29 post-reaction medium;

3 settler, 31 feedstock reaction product outlet pipe, 31A feedstock oil reaction product, 32 light hydrocarbon reaction product outlet pipe, 32A light hydrocarbon reaction product, 33 light hydrocarbon reactor gas-solid cyclone separator, 34 feedstock oil reactor gas-solid Cyclone separator

4 stripper, 41 first stripping zone, 42 second stripping zone, 43 second stripping zone outlet pipe; 43A light hydrocarbon waiting agent;

5 regenerator, 51 regenerator inlet agent inlet tube, 52 regenerant to feedstock oil reactor outlet tube, 52A feedstock oil reactor regenerant, 53 regenerant to light hydrocarbon reactor outlet tube, 53A light hydrocarbon reactor regenerant , 53B regenerant to light hydrocarbon reactor second outlet pipe, 54 regeneration zone (or second regeneration zone), 55 semi-regeneration zone (or a regeneration zone), 55A semi-regenerant to light hydrocarbon reactor outlet pipe, 55B light Hydrocarbon reactor semi-regenerant, 56 regenerator catalyst reflux tube;

7 first fractionation system, 8 second fractionation system, 71 rich gas, 72 crude gasoline, 73 light diesel oil, 74 heavy diesel oil, 75 refinery oil produced by reaction of raw material oil, 76 oil slurry; 81 rich gas, 82 crude gasoline, 83 Diesel, 84 refinery oil produced by light hydrocarbon reaction;

AR air; GAS dry gas; VA regenerative flue gas; LS steam; TC temperature control; WC storage control.

Detailed ways

The technical solutions of the present invention are described in detail below with reference to the accompanying drawings and embodiments, but the scope of the present invention is not limited thereto.

Embodiment 1:

As shown in Fig. 1, after the catalytic feedstock oil 13 (fresh feedstock oil) is atomized by the steam LS, it enters the feedstock oil reactor 1 through the catalytic feedstock oil inlet pipe 14, that is, the riser reactor, and the regenerant from the regenerator 5 The feedstock oil reactor outlet pipe 52 is vaporized by contact with the feedstock oil reactor regenerant 52A sent from the feedstock oil regeneration regeneration inclined pipe 11, and flows upward along the riser reactor under the promotion of steam LS or dry gas GAS. After the catalytic cracking reaction is completed, the feedstock oil reaction product 31A, that is, the reaction oil and gas, is separated from the entrained catalyst in the settler 3 via the feedstock oil gas-solid cyclone separator 34, and then flows out of the settler 3 along the feedstock reaction product outlet pipe 31, and the catalyst enters the first stage. stripping zone 41; the specific embodiments, oil as a raw material in the reactor feed, C ₄ feedstock in the catalytic oil inlet pipe 14 enters the bottom of reactor 1 oil feed is contacted with the feedstock oil regenerated catalyst reactor 52A;

The light hydrocarbon reactor 2 is provided with a transport distribution zone 26 and a temperature-increasing catalytic cracking reaction zone 26A from bottom to top, and is also provided with a transport pipe (ie, a light hydrocarbon reactor and a settler connection pipe) 27, and a transport distribution zone 26 is provided with a pipe. a gas-solid transport bed, the catalytic cracking reaction zone 26A adopts a fluidized bed condition;

The light hydrocarbon reactor 2 and the feedstock oil reactor 1 share a settler 3, and a separate light hydrocarbon reaction product outlet pipe 32 and a separate light hydrocarbon reactor gas-solid cyclone separator 33 are disposed in the settler 3;

The feedstock oil reactor produces gasoline, or exotic gasoline, naphtha such as coker naphtha as liquid light hydrocarbon feedstock (light hydrocarbon 24), which is atomized by steam LS and then enters the transport distribution zone 26 by the light hydrocarbon inlet pipe 25. Light hydrocarbon reactor 2; the catalyst 22A after the light hydrocarbon reaction is returned from the catalytic cracking reaction zone 26A in the middle to the catalyst outlet 22 of the light hydrocarbon reaction from the catalyst inlet 22 of the light hydrocarbon reaction to the transport distribution zone 26, and the tubular transport The light hydrocarbons 24 in the process are contacted to achieve gasification and upward flow into the catalytic cracking reaction zone 26A, and the regenerator from the regenerator 5 is removed from the light hydrocarbon reactor outlet pipe 53 by the light hydrocarbon reaction to regenerate the light hydrocarbons sent from the inclined pipe 21. The reactor regenerant 53A is contacted to realize the heat required for the light hydrocarbon reactor, increase the temperature of the stream in the catalytic cracking reaction zone, and carry out the catalytic cracking reaction of the light hydrocarbon gas in the catalytic cracking reaction zone 26A, and the reaction temperature is determined by the light hydrocarbon reactor regenerant Volume control of 53A;

The light hydrocarbon reaction product 32A entrains the catalyst and enters the settler 3 through the transfer pipe 27, and separates the entrained catalyst through the light hydrocarbon reactor gas-solid cyclone 33, and then flows out of the settler 3 from the light hydrocarbon reaction product outlet pipe 32. The feedstock oil reaction product 31A is mixed;

The spent catalysts reacted in the feedstock oil reactor 1 and the light hydrocarbon reactor 2 are separated from the oil and gas by the feedstock oil gas-solid cyclone separator 34 and the light hydrocarbon reactor gas-solid cyclone separator 33, respectively. The stripper 4 below the settler 3 is stripped in the first stripping zone 41; the stripped by-carrying agent 12A enters the regenerator 5 via the standby tube 12 and the regenerator inlet inlet tube 51. regeneration.

The regenerator 5 is provided with an air AR inlet at the bottom and a regenerative flue gas VA outlet at the top.

Embodiment 2:

As shown in FIG. 2, after the catalytic feedstock oil 13 is atomized by the steam LS, it enters the feedstock oil reactor 1 through the catalytic feedstock oil inlet pipe 14, and reacts with the feedstock oil to regenerate the feedstock oil from the regenerator 5. After the reactor regenerant 52A is contacted, it is vaporized, and under the lifting of the steam LS or the dry gas GAS, the catalytic cracking reaction is completed by flowing upward along the riser reactor, and the feedstock oil reaction product 31A, that is, the reaction oil and gas, is passed through the feedstock in the settler 3. The reactor gas-solid cyclone separator 34 separates the entrained catalyst and then flows out of the settler 3 along the feedstock oil reaction product outlet pipe 31, and the catalyst enters the first stripping zone 41;

The light hydrocarbon reactor 2 and the feedstock oil reactor 1 share a settler 3, and a separate light hydrocarbon reaction product outlet pipe 32, a light hydrocarbon reactor gas-solid cyclone separator 33 and a second stripping zone 42 are disposed in the settler 3;

The feedstock oil reactor self-produced gasoline or crude gasoline 72 is used as a liquid light hydrocarbon feedstock (light hydrocarbon 24), which is atomized by steam LS and then enters the light hydrocarbon reactor 2 from the light hydrocarbon inlet pipe 25 in the transport distribution zone 26; The reacted catalyst 22A is returned from the catalytic cracking reaction zone 26A in the middle to the catalyst outlet 22 of the light hydrocarbon reaction from the catalyst outlet 22 of the light hydrocarbon reaction to the transport distribution zone 26 for contact with the light hydrocarbons 24 during the tubular transport. Achieving gasification and upward flow into the catalytic cracking reaction zone 26A, and contacting the regenerant de-lighting reactor outlet pipe 53 from the regenerator 5 via the light hydrocarbon reaction regeneration inclined pipe 21 to the light hydrocarbon reactor regenerant 53A The heat required by the light hydrocarbon reactor, the temperature of the stream in the catalytic cracking reaction zone, the catalytic cracking reaction of the light hydrocarbon gas in the catalytic cracking reaction zone 26A, and the reaction temperature is controlled by the amount of the light hydrocarbon reactor regenerant 53A;

The feedstock oil reaction product 31A and the light hydrocarbon reaction product 32A are separately introduced into separate fractionation systems (first fractionation system 7 and second fractionation system 8) to carry out reaction oil and gas separation, and the feedstock oil reaction product 31A is separated into rich gas 71 and coarse. Gasoline 72, light diesel oil 73, heavy diesel oil 74, refining oil 75 and slurry 76 produced by reaction of feedstock oil; separation of light hydrocarbon reaction product 32A into refined oil 81, crude gasoline 82, diesel 83 and light hydrocarbons 84, the raw gasoline reaction product 31A separated crude gasoline 72 is returned to the light hydrocarbon reactor 2, as a liquid light hydrocarbon feedstock for the reaction of the light hydrocarbon reactor; the refinery oil 75 produced by the reaction of the feedstock oil and the light refinery produced by the reaction of light hydrocarbons 84 as the post-reaction medium 29, returning to the transport tube 27 of the light hydrocarbon reactor 2, using the heat of the light hydrocarbon reaction and the catalyst to achieve the reaction of the post-reaction medium, while reducing the temperature of the light hydrocarbon reactant stream, reducing the fluidized bed or circulation The degree of post reaction of the light hydrocarbon reaction product in the fluidized bed;

The spent catalysts reacted in the feedstock oil reactor 1 and the light hydrocarbon reactor 2 are separated from the oil and gas by the feedstock oil gas-solid cyclone separator 34 and the light hydrocarbon reactor gas-solid cyclone separator 33, respectively. The stripper 4 below the settler 3. The catalyst separated by the feedstock oil gas-solid cyclone separator 34 is stripped in the first stripping zone 41. The catalyst separated by the partial light hydrocarbon reactor gas-solid separator 33 first enters the second stripping zone 42, and the second stripping zone 42 is taken out from the second stripping zone outlet pipe 43 to extract the catalyst, namely the light hydrocarbon waiting agent 43A. Returning from the light hydrocarbon spent agent inlet pipe 15 to the feedstock oil reactor 1 and mixing with the feedstock oil reactor regenerant 52A for catalyzing the reaction of the feedstock oil; the remaining part of the light hydrocarbon reactor gas-solids separator 33 is separated from the catalyst The first stripping zone 41 of the stripper 4 is introduced, stripped, and the stripped by-state agent 12A is regenerated by the freshener 12 and the regenerator inlet inlet tube 51 into the regenerator 5.

In the figure, TC represents temperature control.

Embodiment 3:

As shown in FIG. 3, after the catalytic feedstock oil 13 is atomized by the steam LS, it enters the feedstock oil reactor 1 through the catalytic feedstock oil inlet pipe 14, and reacts with the feedstock oil to regenerate the feedstock oil from the regenerator 5 which is sent from the inclined pipe 11. After the reactor regenerant 52A is contacted, it is vaporized, and under the lifting of the steam LS or the dry gas GAS, the catalytic cracking reaction is completed by flowing upward along the riser reactor, and the feedstock oil reaction product 31A, that is, the reaction oil and gas, is passed through the feedstock in the settler 3. The reactor gas-solid cyclone separator 34 separates the entrained catalyst and then flows out of the settler 3 along the feedstock reaction product outlet pipe 31, and the catalyst enters the first stripping zone 41; in specific implementation, as a feedstock reactor feed, C ₄ entering the feedstock oil reactor 1 below the catalytic feedstock oil inlet pipe 14 and first contacting the feedstock oil reactor regenerant 52A;

The light hydrocarbon reactor 2 and the feedstock oil reactor 1 share a settler 3, and a separate light hydrocarbon reactor gas-solid cyclone separator 33 and a second stripping zone 42 are disposed in the settler 3;

The feedstock oil reactor self-produces gasoline as a liquid light hydrocarbon feedstock (light hydrocarbon 24), which is atomized by steam LS and then enters the light hydrocarbon reactor 2 from the light hydrocarbon inlet pipe 25 in the transport distribution zone 26; the catalyst 22A after the light hydrocarbon reaction From the catalytic cracking reaction zone 26A in the middle, from the catalyst outlet 22 after the light hydrocarbon reaction, the catalyst inlet pipe 23 after the light hydrocarbon reaction is returned to the transport distribution zone 26, and at the same time, the regenerator is removed from the light hydrocarbon reactor second outlet pipe 53B. The unit 5 takes out part of the regenerant, which is introduced into the transport distribution zone 26 by the regenerator inlet pipe 28 of the transport distribution zone (tubular gas-solid transport bed), and is mixed with the catalyst 22A after the reaction of the light hydrocarbon to obtain a mixed catalyst, and is in contact with the tubular transport process. The light hydrocarbon 24 contacts, gasification and upward flow into the catalytic cracking reaction zone 26A, and the light hydrocarbon reactor from the regenerant from the regenerator 5 to the light hydrocarbon reactor outlet pipe 53 via the light hydrocarbon reaction regeneration ramp 21 The regenerant 53A is contacted to realize the heat required for the light hydrocarbon reactor, increase the temperature of the stream in the catalytic cracking reaction zone, and carry out the catalytic cracking reaction of the light hydrocarbon gas in the catalytic cracking reaction zone 26A, and the reaction temperature is further determined by the light hydrocarbon reactor. The amount of raw agent 53A is controlled;

The light hydrocarbon reaction product entrains the catalyst and enters the settler 3 through the transfer pipe 27, and the entrained catalyst is separated by the light hydrocarbon reactor gas-solid cyclone 33, mixed with the feedstock reaction product 31A, and flows out along the feedstock reaction product outlet pipe 31. Setter 3;

Embodiment 4:

As shown in FIG. 4, after the catalytic feedstock oil 13 is atomized by the steam LS, it enters the feedstock oil reactor 1 through the catalytic feedstock oil inlet pipe 14, and reacts with the feedstock oil to regenerate the feedstock oil from the regenerator 5. After the reactor regenerant 52A is contacted, it is vaporized, and under the lifting of the steam LS or the dry gas GAS, the catalytic cracking reaction is completed by flowing upward along the riser reactor, and the feedstock oil reaction product 31A, that is, the reaction oil and gas, is passed through the feedstock in the settler 3. after the reactor gas-solid separating entrained catalyst cyclone 34 along the feed oil reaction product effluent outlet tube settler 31 3, into the first catalyst stripping zone 41; C ₄ feedstock oil into the reactor below the catalyst feed oil inlet pipe 14 The device 1 is first contacted with the feedstock oil reactor regenerant 52A;

The light hydrocarbon reactor 2 and the feedstock oil reactor 1 share a settler 3, and a separate light hydrocarbon reaction product outlet pipe 32, a light hydrocarbon reactor gas-solid cyclone separator 33 and a second stripping zone 42 are disposed in the settler 3; The reactor 5 adopts a countercurrent two-stage regeneration mode, and the semi-regeneration zone (or a section of regeneration zone) 55 and the regeneration zone (or the two-stage regeneration zone) 54 are arranged up and down, and the semi-regeneration zone (or a section of regeneration zone) 55 is above, and the regeneration zone (or a second regeneration zone 54 is located below; a semi-regeneration zone (or a regeneration zone) 55 and a regeneration zone (or two regeneration zones) 54 between the regenerator catalyst return pipe 56;

The feedstock oil reactor produces gasoline as a liquid light hydrocarbon feedstock (light hydrocarbon 24), which is atomized by steam LS and then enters the light hydrocarbon reactor 2 from the light hydrocarbon inlet pipe 25 in the transport distribution zone 26; from the second stripping zone 42 The extracted light hydrocarbon spent agent 43A enters the transport distribution zone 26 from the light hydrocarbon spent agent inlet tube 23B, contacts the light hydrocarbons 24 during the tubular transport process, achieves gasification and upward flow into the catalytic cracking reaction zone 26A, and The semi-regenerant of the regenerator 5 is contacted with the light hydrocarbon reactor semi-regenerant 55B sent from the light hydrocarbon reaction regeneration tube 55A by the light hydrocarbon reaction regeneration inclined tube 21 to realize the heat required for the light hydrocarbon reactor and to increase the catalytic cracking reaction zone. The temperature of the internal stream causes the light hydrocarbon gas to undergo a catalytic cracking reaction in the catalytic cracking reaction zone 26A;

The spent catalysts reacted in the feedstock oil reactor 1 and the light hydrocarbon reactor 2 are separated from the oil and gas by the feedstock oil gas-solid cyclone separator 34 and the light hydrocarbon reactor gas-solid cyclone separator 33, respectively. The stripper 4 below the settler 3. The catalyst separated by the feedstock oil gas-solid cyclone separator 34 is stripped in the first stripping zone 41. The catalyst separated by the partial light hydrocarbon reactor gas-solid separator 33 first enters the second stripping zone 42, and the second stripping zone 42 is taken out from the second stripping zone outlet pipe 43 to extract the catalyst, namely the light hydrocarbon waiting agent 43A. Returning from the light hydrocarbon spent agent inlet pipe 23B to the light hydrocarbon reactor 2 for gasifying the raw light hydrocarbons 24; the remaining part of the light hydrocarbon reactor gas-solids separator 33 is separated into the first of the stripper 4 The stripping zone 41, stripping, the stripped by-carrying agent 12A is regenerated by the regeneration tube 12 and the regenerator waiting agent inlet tube 51 into the regenerator 5.

In the method of the present invention, when the light hydrocarbon is in a gaseous state, that is, a light hydrocarbon gas is fed, and the catalyst or the living agent after the light hydrocarbon reaction does not return to the transport distribution zone (ie, the light hydrocarbon gas does not transport the catalyst), it can be convenient. The distribution of light hydrocarbon gas is realized by using a distribution pipe (ie, a tubular distributor). The gas distribution is as shown in FIG. 5. The distribution pipe 26C is a commonly used distributor in a gas-solid reactor, and the gaseous light hydrocarbon 24A is transported under steam LS. Along the transport distribution zone 26, it enters the distribution pipe 26C to be distributed into the catalytic cracking reaction zone 26A, and is reacted with the light hydrocarbon-reacted catalyst 22A and the light hydrocarbon reactor regenerant 53A to react with the reaction temperature by the light hydrocarbon reactor regenerant. The amount of catalyst is controlled by the amount of catalyst after the light hydrocarbon reaction. In Figure 5, TC represents temperature control; WC represents storage control. In the method of the present invention, it should be noted that when there is a catalyst in the transport distribution zone, that is, when the light hydrocarbon gas transport catalyst enters the catalytic cracking reaction zone together, the distribution pipe is generally not used due to the problem of wear and distribution uniformity, but Gas distribution is performed using a distribution plate 26B (as shown in Figures 1 and 3).

Example:

The device used in this embodiment is shown in Figure 2;

Feedstock oil reaction:

The catalytic feedstock oil is: 150t/h heavy oil, the properties are shown in Table 1; the heavy oil is preheated at 280 °C; the feedstock oil reactor is in the form of a riser, the 680 °C regenerant from the regenerator and the hydrocarbon hydrocarbons from the second stripping zone are awaiting The agent is mixed with the catalytic feedstock oil after mixing at the bottom of the transport distribution zone (ie, the pre-lift zone), the mixing temperature of the catalyst is 640 ° C, the outlet temperature of the feedstock oil reactor is 510 ° C, and the reaction time is 1.4 s;

Light hydrocarbon reaction:

The gasoline is the light hydrocarbon raw material, the light hydrocarbon reactor is the gasoline reactor, the catalytic cracking reaction zone of the gasoline reactor is in the form of a circulating fluidized bed, and the reaction raw material is the raw material oil reaction self-produced gasoline, 50t/h, the gasoline liquid phase feed . The gasoline reactor is gasified by a gasoline reaction at 560 ° C, the gasification temperature is 350 ° C, and the 680 ° C regenerant from the regenerator enters the circulating fluidized bed of the catalytic cracking reaction zone, and the circulating fluidized bed temperature is 560 ° C. The space-time velocity is 4 (1/h), the oil and gas velocity is 1.3m/s, and the residence time is 3.5s. The raw oil reacts the oil obtained by fractional distillation into the conveying pipe at the outlet of the catalytic cracking reaction zone to continue the reaction, and at the same time reduces the reaction rate of the light hydrocarbon, and the outlet temperature of the conveying pipe is 500 °C. Regenerator regeneration temperature 680 ° C;

The two reactors share a settler, and the gasoline reaction product and the feedstock reaction product are separately fed from separate lines to the gasoline product fractionation column and the feedstock oil product fractionation column.

The reaction conditions and product distribution of the examples are shown in Table 2.

Comparative example:

Using a conventional catalytic cracking process, that is, using a feedstock oil reactor for catalytic feedstock oil cracking, the properties of the feedstock oil are the same as in Table 1;

The comparative reaction conditions and product distribution are shown in Table 2.

Table 1 Catalytic properties of feedstock oil

项目project	数据data
密度g/cm ³(20℃) Density g/cm ³ (20 ° C)	0.90350.9035
残碳，w％Carbon residue, w%	0.620.62
氢含量，w％Hydrogen content, w%	12.5612.56
硫含量，w％Sulfur content, w%	0.310.31
氮含量，w％Nitrogen content, w%	0.160.16
馏程，℃Distillation range, °C	256～545256~545

Table 2 embodiment compared with the prior art

项目project	实施例Example	对比例Comparative example
原料油提升管出口温度Feedstock riser outlet temperature	510510	520520
轻烃流化床反应温度Light hydrocarbon fluidized bed reaction temperature	560560
再生温度Regeneration temperature	680680	680680
产物分布％Product distribution %
干气(H ₂～C2) Dry gas (H ₂ ~ C2)	2.12.1	4.454.45
液化气(C3～C4)Liquefied gas (C3～C4)	33.833.8	18.3418.34
汽油gasoline	29.229.2	40.8440.84
柴油Diesel	26.526.5	26.0426.04
焦炭 Coke	88	9.739.73
损失loss	0.40.4	0.60.6
转化率Conversion rate	89.589.5	85.2285.22
总烯烃产率Total olefin yield	28.628.6	14.6514.65

As can be seen from the comparison results of Table 2, the present invention is compared with the conventional catalytic process: the conversion rate is increased by 4.28 percentage points, the low-value products such as dry gas and coke yield are significantly decreased, and high-value products such as olefins, liquefied gases and gasoline are high. The yield was significantly improved, in which the dry gas yield decreased by 1.35 percentage points, the coke yield decreased by 1.73 percentage points, the total olefin yield increased by 13.95 percentage points, and the propylene yield increased by 6.89 percentage points. It can be seen that the present invention substantially increases the yield of propylene, the dry gas and coke yields are greatly reduced, and the propylene selectivity is improved.

Claims

A catalytic conversion method for producing propylene, the method comprising:

Providing a feedstock oil reactor (1) and a light hydrocarbon reactor (2);

The catalytic feedstock oil (13) is atomized by steam into the feedstock oil reactor (1), contacted with a regenerant from the regenerator (5), or a mixed catalyst of a regenerant and a light hydrocarbon biocide, and then gasified and carried out. Catalytic cracking reaction, the feedstock oil reaction product (31A) is separated into the entrained catalyst by a cyclone in the settler (3) and then exits the settler (3);

The light hydrocarbon reactor (2) is provided with a transport distribution zone (26) and a temperature-enhanced catalytic cracking reaction zone (26A) from the bottom up, and a light hydrocarbon (24) enters the light hydrocarbon reactor in the transport distribution zone (26) (2) The light hydrocarbon gas undergoes a catalytic cracking reaction in the catalytic cracking reaction zone (26A), the catalytic cracking reaction zone (26A) adopts a fluidized bed or a circulating fluidized bed condition; the catalyst from the regenerator enters the catalytic cracking reaction zone (26A) Providing heat required for the light hydrocarbon reactor (2), increasing the temperature of the stream in the catalytic cracking reaction zone (26A), and subjecting the light hydrocarbons to catalytic cracking reaction, the reaction temperature is controlled by the amount of catalyst from the regenerator; after the light hydrocarbon reaction The catalyst or light hydrocarbon spent agent is returned to the light hydrocarbon reactor (2) from the catalytic cracking reaction zone (26A) in the middle of the light hydrocarbon reactor (2) or to the transport distribution zone (26) in the bottom.
The method for catalytically converting propylene produced according to claim 1, wherein when the light hydrocarbon is in a liquid state, the light hydrocarbon reaction is carried out by a catalyst two-cycle method, and the light hydrocarbon (24) is gasified in the transport distribution zone (26). As a light hydrocarbon gasification zone, a catalyst for gasification of light hydrocarbons, that is, a gasification catalyst, enters a transport distribution zone (26), a catalyst from the regenerator enters a catalytic cracking reaction zone (26A); a light hydrocarbon (24) is fogged. The nozzle is vaporized and then enters the transport distribution zone (26) to contact the gasification catalyst. The light hydrocarbon (24) is first vaporized at a lower temperature than the catalytic cracking reaction zone (26), and then in the catalytic cracking reaction zone. (26A) contact with the catalyst from the regenerator to increase the temperature and carry out the catalytic cracking reaction; the transport distribution zone (26) adopts a gas-solid transport bed or a tubular gas-solid transport bed condition; when the transport distribution zone (26) adopts a tubular gas In the solid transport bed, the light hydrocarbon (24) is vaporized directly in contact with the catalyst during the tubular transport.
The method for catalytically converting propylene produced according to claim 1 or 2, wherein the catalyst from the regenerator directly enters the fluidized bed or the circulating fluidized bed of the catalytic cracking reaction zone (26A) to increase the catalytic cracking reaction zone (26A). The catalyst and the temperature of the oil and gas are subjected to a light hydrocarbon catalytic cracking reaction; or the catalyst from the regenerator is cooled first and then enters a fluidized bed or a circulating fluidized bed of the catalytic cracking reaction zone (26A) to carry out a light hydrocarbon catalytic cracking reaction.
The method for catalytically converting propylene produced according to claim 1 or 2, wherein the catalyst or gasification catalyst entering the transport distribution zone (26) is a light hydrocarbon-reacted catalyst or a light hydrocarbon spent agent, or from a regenerator a catalyst, or a light hydrocarbon reaction catalyst or a mixed catalyst of a light hydrocarbon spent agent and a catalyst from a regenerator.
A method of catalytically converting propylene produced according to claim 4, wherein the catalyst entering the transport distribution zone (26) is a light hydrocarbon spent.
The method for catalytically converting propylene produced according to claim 1, wherein said regenerator (5) adopts a countercurrent two-stage regeneration mode to enter said catalyst from said regenerator of said catalytic cracking reaction zone (26A), The semi-regeneration zone from the regenerator (5) is a semi-regenerant.
The method for catalytically converting propylene produced according to claim 1, wherein the refinery oil produced by the reaction of a part of light hydrocarbons, the refinery oil in the feedstock reaction product, and/or the hydrogenated catalytic cracked diesel oil are subjected to the catalytic cracking. The reaction zone (26A) outlet or the light pipe (27) of the light hydrocarbon reactor (2) enters the light hydrocarbon reactor (2), and the reaction of the partial stream is realized by the heat of the catalytic cracking reaction zone (26A) and the catalyst. At the same time, the degree of post-reaction of the light hydrocarbon reaction product in the catalytic cracking reaction zone (26A) is reduced.
The method for catalytically converting propylene produced according to claim 1, wherein the light hydrocarbon (24) is selected from the group consisting of C4, heavy catalytic gasoline, straight run naphtha, catalytic light gasoline, coking gasoline, and fractionated feed. The reaction and the stepwise feeding sequence are C4, heavy catalytic gasoline, straight run naphtha, catalytic light gasoline, and coking gasoline from bottom to top.
The method for catalytically converting propylene produced according to claim 1, wherein when the transport distribution zone (26) does not enter the catalyst, the light hydrocarbon (24) enters the transport distribution zone (26) in a gaseous state and then enters the catalytic cracking reaction. In the fluidized bed or circulating fluidized bed of zone (26A), the catalyst or spent agent after the light hydrocarbon reaction enters the light hydrocarbon reactor (2) in the fluidized bed or circulating fluidized bed zone.
The method for catalytically converting propylene produced according to claim 1 or 2, wherein the light hydrocarbon reaction product (32A) flows out of the settler (3) and then exchanges heat with the liquid light hydrocarbon to be reacted, so that the liquid to be reacted is light. The hydrocarbon gasification simultaneously lowers the light hydrocarbon reaction product (32A); the heat exchange uses a vertical shell-and-tube heat exchanger, and the high-temperature light hydrocarbon reaction product (32A) flows in the tube, and the liquid light hydrocarbon to be reacted is in the shell. In-process flow; the light hydrocarbon reaction product (32A) flows from above the heat exchanger to flow from below, and the liquid light hydrocarbon to be reacted flows from bottom to top in the heat exchanger housing.
A catalytic converter for producing propylene, the device comprising: a feedstock oil reactor (1), a light hydrocarbon reactor (2) and a regenerator (5);

The feedstock oil reactor (1) is provided with a catalytic feedstock oil (13) inlet, and is provided with a regenerant inlet from the regenerator (5), or a regenerant and a light hydrocarbon waiter inlet; a feedstock oil reactor (1) above A settler (3) is provided, and a cyclone separator for separating the catalyst entrained in the feedstock reaction product (31A) is disposed in the settler (3), and the settler (3) is further provided with a feedstock oil reaction product (31A) separated and entrained. a flow outlet after the catalyst;

The light hydrocarbon reactor (2) is provided with a transport distribution zone (26) and a temperature-increasing catalytic cracking reaction zone (26A) from the bottom up, and the transport distribution zone (26) is provided with a light hydrocarbon (24) entering the light hydrocarbon reactor ( 2) inlet; catalytic cracking reaction zone (26A) using fluidized bed or circulating fluidized bed conditions; catalytic cracking reaction zone (26A) provided with a catalyst inlet from the regenerator; and, in the middle of the light hydrocarbon reactor (2) The catalytic cracking reaction zone (26A) or the bottom transport distribution zone (26) is provided with a light hydrocarbon reacted catalyst or a light hydrocarbon spent agent returning to the inlet of the light hydrocarbon reactor (2).
The apparatus according to claim 11, which is an apparatus for carrying out the catalytic conversion method for producing propylene according to any one of claims 1 to 10.
A device according to claim 11 or 12, wherein:

The feedstock oil reactor (1) is a riser reactor, and is provided with a catalytic feedstock oil inlet pipe (14) for reacting the catalytic feedstock oil (13) by steam atomization into the feedstock oil through the catalytic feedstock inlet pipe (14). Device (1);

A feedstock oil gas-solid cyclone (34) for separating the catalyst entrained in the feedstock reaction product (31A) is disposed in the settler (3) above the feedstock oil reactor (1), and a feedstock oil reaction product is also provided. (31A) an outlet for separating the entrained catalyst; a stripper (4) disposed below the feedstock reactor gas-solid cyclone (34) having a first stripping zone (41); a first stripping zone ( 41) setting the outlet of the stripped spent agent (12A), connecting the regenerator (5) through the standby riser (12), the regenerator waiter inlet tube (51);

The light hydrocarbon reactor (2) is provided with a transport distribution zone (26), a catalytic cracking reaction zone (26A) for increasing temperature, and a transport pipe (27) from bottom to top; and a tubular gas-solid transport bed for the transport distribution zone (26). The catalytic cracking reaction zone (26A) adopts fluidized bed conditions, the conveying pipe (27) is a light hydrocarbon reactor and a settler connecting pipe; the central catalytic cracking reaction zone (26A) is provided with a catalyst outlet after light hydrocarbon reaction (22) ), connecting the catalyst (22A) after reacting the light hydrocarbons to the catalyst inlet tube (23) after the light hydrocarbon reaction in the distribution zone (26);

The light hydrocarbon reactor (2) and the feedstock oil reactor (1) share a settler (3), and an independent light hydrocarbon reaction product outlet pipe (32) and a separate light hydrocarbon reactor gas-solid cyclone are disposed in the settler (3). Separator (33);

The regenerator (5) is provided with a regenerant to the feedstock reactor outlet pipe (52), and is connected to the feedstock oil for regenerating the inclined oil pipe for feeding the feedstock oil reactor regenerant (52A) to the feedstock oil reactor (1) ( 11) The regenerator (5) is further provided with a regenerant to the light hydrocarbon reactor outlet pipe (53) for connecting the light hydrocarbon reaction for sending the light hydrocarbon reactor regenerant (53A) to the catalytic cracking reaction zone (26A). Regeneration inclined tube (21);

Preferably, the inlet of feed C4 of the feedstock oil reactor is disposed below the catalytic feedstock inlet pipe (14).
The apparatus according to claim 11 or 12, further comprising a first fractionation system (7) and a second fractionation system (8), wherein:

The feedstock oil reactor (1) is a riser reactor, and is provided with a catalytic feedstock oil inlet pipe (14) for reacting the catalytic feedstock oil (13) by steam atomization into the feedstock oil through the catalytic feedstock inlet pipe (14). Device (1);

A feedstock oil gas-solid cyclone (34) for separating the catalyst entrained in the feedstock reaction product (31A) is disposed in the settler (3) above the feedstock oil reactor (1), and a feedstock oil reaction product is also provided. (31A) an outlet for separating the entrained catalyst; a stripper (4) disposed below the feedstock reactor gas-solid cyclone (34) having a first stripping zone (41); a first stripping zone ( 41) setting the outlet of the stripped spent agent (12A), connecting the regenerator (5) through the standby riser (12), the regenerator waiter inlet tube (51);

The light hydrocarbon reactor (2) is provided with a transport distribution zone (26), a catalytic cracking reaction zone (26A) for increasing temperature, and a transport pipe (27) from bottom to top; and a tubular gas-solid transport bed for the transport distribution zone (26). The catalytic cracking reaction zone (26A) adopts fluidized bed conditions, the conveying pipe (27) is a light hydrocarbon reactor and a settler connecting pipe; the central catalytic cracking reaction zone (26A) is provided with a catalyst outlet after light hydrocarbon reaction (22) ), connecting the catalyst (22A) after reacting the light hydrocarbons to the catalyst inlet tube (23) after the light hydrocarbon reaction in the distribution zone (26);

The light hydrocarbon reactor (2) and the feedstock oil reactor (1) share a settler (3), and a separate light hydrocarbon reaction product outlet pipe (32) and a light hydrocarbon reactor gas-solid cyclone separator are disposed in the settler (3). (33) and a second stripping zone (42); the second stripping zone (42) is provided with a second stripping zone outlet pipe (43) connected to the light hydrocarbon green agent inlet pipe (15) for The light hydrocarbon waiting agent (43A) in the second stripping zone (42) is taken out of the second stripping zone and returned to the feedstock oil reactor (1);

The regenerator (5) is provided with a regenerant to the feedstock reactor outlet pipe (52), and is connected to the feedstock oil for regenerating the inclined oil pipe for feeding the feedstock oil reactor regenerant (52A) to the feedstock oil reactor (1) ( 11) The regenerator (5) is further provided with a regenerant to the light hydrocarbon reactor outlet pipe (53) for connecting the light hydrocarbon reaction for sending the light hydrocarbon reactor regenerant (53A) to the catalytic cracking reaction zone (26A). Regeneration inclined tube (21);

The first fractionation system (7) is used for reacting the feedstock oil reaction product (31A) for oil and gas separation, and separating the feedstock oil reaction product (31A) into rich gas (71), crude gasoline (72), and light diesel oil (73). Heavy diesel oil (74), refinery oil (75) and oil slurry (76) produced by reaction of feedstock oil; second fractionation system (8) is used for reaction of light hydrocarbon reaction product (32A) for oil and gas separation, light hydrocarbon The reaction product (32A) is separated into a refinery oil (84) produced by the reaction of rich gas (81), crude gasoline (82), diesel (83) and light hydrocarbons; a first fractionation system (7) and a light hydrocarbon reactor (2) Between the crude gasoline (72) separating the feedstock reaction product (31A) is returned to the light hydrocarbon reactor (2) as a liquid light hydrocarbon feedstock for the reaction of the light hydrocarbon reactor; the first fractionation system (7), The second fractionation system (8) and the light hydrocarbon reactor (2) are provided with a refinery oil (75) produced by reacting the feedstock oil and/or a refinery oil (84) produced by the reaction of light hydrocarbons as a post reaction medium (29). The line of the delivery tube (27) of the light hydrocarbon reactor (2).
A device according to claim 11 or 12, wherein:

The feedstock oil reactor (1) is a riser reactor, and is provided with a catalytic feedstock oil inlet pipe (14) for reacting the catalytic feedstock oil (13) by steam atomization into the feedstock oil through the catalytic feedstock inlet pipe (14). Device (1);

A feedstock oil gas-solid cyclone (34) for separating the catalyst entrained in the feedstock reaction product (31A) is disposed in the settler (3) above the feedstock oil reactor (1), and a feedstock oil reaction product is also provided. (31A) an outlet for separating the entrained catalyst; a stripper (4) disposed below the feedstock reactor gas-solid cyclone (34) having a first stripping zone (41); a first stripping zone ( 41) setting the outlet of the stripped spent agent (12A), connecting the regenerator (5) through the standby riser (12), the regenerator waiter inlet tube (51);

The light hydrocarbon reactor (2) is provided with a transport distribution zone (26), a catalytic cracking reaction zone (26A) for increasing temperature, and a transport pipe (27) from bottom to top; and a tubular gas-solid transport bed for the transport distribution zone (26). The catalytic cracking reaction zone (26A) adopts fluidized bed conditions, the conveying pipe (27) is a light hydrocarbon reactor and a settler connecting pipe; the central catalytic cracking reaction zone (26A) is provided with a catalyst outlet after light hydrocarbon reaction (22) ), connecting the catalyst (22A) after reacting the light hydrocarbons to the catalyst inlet tube (23) after the light hydrocarbon reaction in the distribution zone (26);

The light hydrocarbon reactor (2) and the feedstock oil reactor (1) share a settler (3), and a separate light hydrocarbon reaction product outlet pipe (32) and a light hydrocarbon reactor gas-solid cyclone separator are disposed in the settler (3). (33) and a second stripping zone (42); the second stripping zone (42) is provided with a second stripping zone outlet pipe (43) connected to the light hydrocarbon green agent inlet pipe (15) for The light hydrocarbon waiting agent (43A) in the second stripping zone (42) is taken out of the second stripping zone and returned to the feedstock oil reactor (1);

The regenerator (5) is provided with a regenerant to the feedstock reactor outlet pipe (52), and is connected to the feedstock oil for regenerating the inclined oil pipe for feeding the feedstock oil reactor regenerant (52A) to the feedstock oil reactor (1) ( 11) The regenerator (5) is further provided with a regenerant to the light hydrocarbon reactor outlet pipe (53) for connecting the light hydrocarbon reaction for sending the light hydrocarbon reactor regenerant (53A) to the catalytic cracking reaction zone (26A). a regenerative inclined pipe (21); the regenerator (5) is further provided with a regenerant to the light hydrocarbon reactor second outlet pipe (53B), and is connected to introduce a part of the regenerant of the regenerator (5) into the transport distribution zone (26) Transport distribution zone regenerant inlet tube (28);

Preferably, the inlet of feed C4 of the feedstock oil reactor is disposed below the catalytic feedstock inlet pipe (14).
A device according to claim 11 or 12, wherein:

The feedstock oil reactor (1) is a riser reactor, and is provided with a catalytic feedstock oil inlet pipe (14) for reacting the catalytic feedstock oil (13) by steam atomization into the feedstock oil through the catalytic feedstock inlet pipe (14). Device (1);

A feedstock oil gas-solid cyclone (34) for separating the catalyst entrained in the feedstock reaction product (31A) is disposed in the settler (3) above the feedstock oil reactor (1), and a feedstock oil reaction product is also provided. (31A) an outlet for separating the entrained catalyst; a stripper (4) disposed below the feedstock reactor gas-solid cyclone (34) having a first stripping zone (41); a first stripping zone ( 41) setting the outlet of the stripped spent agent (12A), connecting the regenerator (5) through the standby riser (12), the regenerator waiter inlet tube (51);

The light hydrocarbon reactor (2) is provided with a transport distribution zone (26), a catalytic cracking reaction zone (26A) for increasing temperature, and a transport pipe (27) from bottom to top; and a tubular gas-solid transport bed for the transport distribution zone (26). The catalytic cracking reaction zone (26A) adopts a fluidized bed condition, and the conveying pipe (27) is a light hydrocarbon reactor and a settler connecting pipe;

The light hydrocarbon reactor (2) and the feedstock oil reactor (1) share a settler (3), and a separate light hydrocarbon reaction product outlet pipe (32) and a light hydrocarbon reactor gas-solid cyclone separator are disposed in the settler (3). (33) and a second stripping zone (42); the second stripping zone (42) is provided with a second stripping zone outlet pipe (43) connected to the light hydrocarbon green agent inlet pipe (23B) for lightening The hydrocarbon spent agent (43A) is taken out of the second stripping zone and enters the transport distribution zone (26);

The catalytic cracking reaction zone (26A) in the middle portion is provided with a catalyst outlet (22) after light hydrocarbon reaction, and is connected to the catalyst inlet pipe after returning the light hydrocarbon reaction catalyst (22A) to the light hydrocarbon reaction in the distribution zone (26) ( twenty three);

The regenerator (5) adopts a countercurrent two-stage regeneration mode, and has a semi-regeneration zone (55) and a regeneration zone (54) arranged above and below, a semi-regeneration zone (55) at the top, a regeneration zone (54) at the bottom, and a semi-regeneration zone. (55) a regenerator catalyst return pipe (56) is disposed between the regeneration zone (54); the regenerator (5) is provided with a semi-regenerant to the light hydrocarbon reactor outlet pipe (55A) for connection to the light hydrocarbon reactor a semi-regenerant (55B) is sent to the catalytic cracking reaction zone (26A) of the light hydrocarbon reaction regeneration inclined pipe (21);

Preferably below, the catalytic feed oil inlet pipe (14) is provided with an oil feed reactor inlet feed C 4.