阅读说明：本技术 提高丙烯和汽油中芳烃含量的方法及装置 (Method and device for increasing aromatic hydrocarbon content in propylene and gasoline ) 是由 谢恪谦 张星 王佳琨 许步建 刘春阳 刘缓 于 2020-06-24 设计创作，主要内容包括：本申请公开了提高丙烯和汽油中芳烃含量的方法及装置,属于石油化工技术领域。所述方法包括重油进料在重油提升管内与催化剂混合并进行催化反应；轻烃进料在轻烃提升管内与催化剂混合并进行催化反应,得到轻烃反应物；轻烃反应物与正在进行催化反应的重油进料混合并继续进行催化反应,且反应后进行气固分离和分馏,其中气固分离用于将催化剂和油气进行分离,分馏用于将油气进行分馏以得到丙烯和芳烃；分离出的催化剂经过汽提后进行烧焦再生,再生催化剂分别返回重油提升管和轻烃提升管。如此,重油进料和轻烃进料可以均处于最佳反应条件,且由于轻烃反应物中的催化剂继续用于催化重油反应,进而可以提高丙烯和汽油中芳烃等的收率。(The application discloses a method and a device for improving the content of aromatic hydrocarbon in propylene and gasoline, belonging to the technical field of petrochemical industry. The method comprises mixing heavy oil feed with a catalyst in a heavy oil riser and carrying out a catalytic reaction; mixing the light hydrocarbon feed with a catalyst in a light hydrocarbon lifting pipe and carrying out catalytic reaction to obtain a light hydrocarbon reactant; mixing a light hydrocarbon reactant with a heavy oil feed undergoing catalytic reaction, continuing catalytic reaction, and performing gas-solid separation and fractionation after the reaction, wherein the gas-solid separation is used for separating a catalyst and oil gas, and the fractionation is used for fractionating the oil gas to obtain propylene and aromatic hydrocarbon; the separated catalyst is subjected to steam stripping and then is subjected to scorching regeneration, and the regenerated catalyst returns to the heavy oil riser and the light hydrocarbon riser respectively. Therefore, the heavy oil feeding and the light hydrocarbon feeding can be both in the optimal reaction condition, and the catalyst in the light hydrocarbon reactant is continuously used for catalyzing the heavy oil reaction, so that the yield of the aromatic hydrocarbon and the like in the propylene and the gasoline can be improved.)

1. A method for increasing the aromatic content of propylene and gasoline, comprising: the heavy oil feed is contacted and mixed with a catalyst in a heavy oil lifting pipe and is subjected to catalytic reaction; the method is characterized in that the light hydrocarbon reactant is mixed with the heavy oil feed which is undergoing catalytic reaction and is subjected to catalytic reaction continuously, and gas-solid separation and fractionation are carried out after the reaction, wherein the gas-solid separation is used for separating the catalyst and oil gas, and the fractionation is used for fractionating the oil gas to obtain a target product,

optionally, the separated catalyst is subjected to scorching regeneration after being stripped, and preferably, the regenerated catalyst is respectively returned to the heavy oil riser and the light hydrocarbon riser for recycling.

2. The process of claim 1, wherein the light hydrocarbon reactants are mixed after the heavy oil feed contacts and catalytically reacts with the catalyst in the first reaction section of the heavy oil riser.

3. The method of claim 2, wherein the heavy oil feed contacts the catalyst in the first reaction section of the heavy oil riser and undergoes a catalytic reaction to produce a first reaction oil gas;

the light hydrocarbon feed is contacted with the catalyst in the light hydrocarbon lifting pipe and is subjected to catalytic reaction to obtain the light hydrocarbon reactant;

the light hydrocarbon reactant enters a second reaction section of the heavy oil lifting pipe to be mixed with the first reaction oil gas and undergo catalytic reaction to obtain second reaction oil gas;

the second reaction oil gas is further subjected to catalytic reaction in a third reaction section of the heavy oil riser to obtain third reaction oil gas;

the third reaction oil gas enters a settler through an outlet of the heavy oil riser and is separated in the settler to obtain oil gas and the catalyst;

and sending the catalyst to the heavy oil riser and the light hydrocarbon riser for recycling, and sending the oil gas serving as target gas to a separation system.

4. The method of claim 3, wherein the heavy oil feedstock contacts a catalyst and undergoes a catalytic reaction in the first reaction section of the heavy oil riser to produce a first reaction oil gas, and further comprising:

injecting pre-lift gas into the first reaction section of the heavy oil riser; and/or

The light hydrocarbon feed contacts the catalyst in the light hydrocarbon riser and undergoes catalytic reaction, before a second light hydrocarbon reactant is obtained, the method further comprising:

and injecting pre-lifting gas into the light hydrocarbon lifting pipe.

5. The method of claim 3, wherein the heavy oil feed is contacted with a catalyst and catalytically reacted in the first reaction section of the heavy oil riser, comprising catalyzing under the following operating conditions:

the mass ratio of the catalyst to the heavy oil feed is 2-10.

6. The process of claim 3, wherein the light hydrocarbon feed is contacted with the catalyst and catalytically reacted within the light hydrocarbon riser, comprising catalyzing at operating conditions comprising:

the mass ratio of the catalyst to the light hydrocarbon feed is 2-20.

7. An apparatus for increasing the aromatics content of propylene and gasoline, said apparatus comprising: a heavy oil lifting pipe (1), a light hydrocarbon lifting pipe (2), a settler (3) and a regenerator (4);

the heavy oil riser (1) comprises a first reaction section (11), a second reaction section (12) and a third reaction section (13) which are communicated from bottom to top in sequence;

the outlet of the light hydrocarbon riser (2) is communicated with the bottom end of the second reaction section (12), and the outlet (131) of the third reaction section (13) is communicated with the settler (3);

the bottom (31) of the settler (3) is connected with the regenerator (4), and the bottom (41) of the regenerator (4) is respectively communicated with the side wall of the first reaction section (11) and the side wall of the light hydrocarbon riser (2).

8. The apparatus according to claim 7, characterized in that it further comprises a first regeneration chute (5);

the first end (51) of the first regeneration chute (5) communicates with the side wall of the first reaction section (11), and the second end (52) of the first regeneration chute (5) communicates with the bottom (41) of the regenerator (4).

9. The device according to claim 7, characterized in that it further comprises a second regeneration chute (6);

the first end (61) of the second regeneration inclined tube (6) is communicated with the side wall of the light hydrocarbon riser (2), and the second end (62) of the second regeneration inclined tube (6) is communicated with the bottom (41) of the regenerator (4).

10. The apparatus according to claim 7, characterized in that it further comprises a tube to be grown (7);

the first end (71) of the inclined tube to be regenerated (7) is communicated with the bottom (31) of the settler (3), and the second end (72) of the inclined tube to be regenerated (7) is communicated with the regenerator (4).

11. The apparatus according to claim 7, characterized in that the settler (3) comprises a first cyclone (32) and a second cyclone (33);

the inlet (321) of the first cyclone separator (32) is connected with the outlet (131) of the third reaction section (13), and the outlet (322) of the first cyclone separator (32) is opposite to or directly communicated with the inlet (331) of the second cyclone separator (33);

the bottom (332) of the second cyclone separator (33) is used for outputting catalyst, and the top (333) of the second cyclone separator (33) is used for outputting oil gas.

Technical Field

The application relates to the technical field of petrochemical industry, in particular to a method and a device for improving the content of aromatic hydrocarbon in propylene and gasoline.

Background

With the rapid development of economy, the catalytic cracking unit has become one of the core units in oil refining enterprises, and the catalytic gasoline and the catalytic diesel oil generated by the catalytic cracking unit also become the main components of commercial gasoline and diesel oil. However, as the economy of China enters a high-quality development stage, particularly as the structural reform of the supply side and the deep advance of the adjustment of the industrial structure are carried out, the demand of the domestic market on gasoline and diesel oil is gradually relieved. Meanwhile, under the double driving of the rise of new energy industry and environmental protection pressure, the traditional energy structure is being changed, and the surplus of gasoline and diesel oil becomes a new normal state, so that the oil refining enterprise is urgently needed to complete the transformation from oil refining to chemical industry as soon as possible, and the integration of oil refining and chemical industry is realized. The catalytic cracking unit is an important heavy oil processing unit in oil refining enterprises, and the structure of a target product generated by the catalytic cracking unit can be adjusted in the process of transformation of the oil refining enterprises to chemical engineering, so that ethylene, propylene and aromatic hydrocarbon are produced as much as possible, and the requirements of domestic markets are met.

The related technology provides a method for producing propylene and aromatic hydrocarbon by double-riser catalytic cracking. In the method, heavy oil feed is contacted and mixed with a catalyst in a heavy oil riser and is subjected to catalytic cracking reaction, and light hydrocarbon feed is contacted and mixed with the catalyst in a light hydrocarbon riser and is subjected to catalytic upgrading reaction. Then the heavy oil reaction material flow and the light hydrocarbon reaction material flow respectively enter into respective special cyclone separators from the heavy oil lift pipe outlet and the light hydrocarbon lift pipe outlet through closed pipelines for gas-solid separation, and the separated heavy oil reaction oil gas and light hydrocarbon reaction oil gas respectively enter into respective special fractionating towers for fractionation to obtain propylene and aromatic hydrocarbon. Then the heavy oil spent catalyst and the light hydrocarbon spent catalyst are subjected to turbulent bed regeneration after steam stripping, and the regenerated catalyst returns to the heavy oil riser and the light hydrocarbon riser respectively for recycling.

However, the higher coke rate of the heavy oil feed results in a lower average activity of the catalyst within the heavy oil riser, which in turn results in a lower yield of propylene and aromatics ultimately obtained.

Disclosure of Invention

The application provides a method and a device for improving the content of aromatic hydrocarbon in propylene and gasoline, which can improve the yield of the aromatic hydrocarbon in the finally obtained propylene and gasoline. The technical scheme is as follows:

in one aspect, a method for increasing the aromatic content of propylene and gasoline is provided, the method comprising: the heavy oil feed is contacted and mixed with a catalyst in a heavy oil lifting pipe and is subjected to catalytic reaction; the light hydrocarbon is fed into the light hydrocarbon lifting pipe to contact and mix with the catalyst and carry out catalytic reaction to obtain a light hydrocarbon reactant; the light hydrocarbon reactant is mixed with the heavy oil feed which is undergoing catalytic reaction and continues to undergo catalytic reaction, and gas-solid separation and fractionation are carried out after the reaction, wherein the gas-solid separation is used for separating the catalyst and oil gas, and the fractionation is used for fractionating the oil gas to obtain a target product,

optionally, the separated catalyst is subjected to scorching regeneration after being stripped, and preferably, the regenerated catalyst is respectively returned to the heavy oil riser and the light hydrocarbon riser for recycling.

Optionally, wherein the light hydrocarbon reactants are mixed after the heavy oil feed contacts and catalytically reacts with the catalyst in the first reaction section of the heavy oil riser.

Optionally, the heavy oil feed is contacted with the catalyst in a first reaction section of the heavy oil riser and is subjected to catalytic reaction to obtain a first reaction oil gas;

the light hydrocarbon feed is contacted with the catalyst in the light hydrocarbon lifting pipe and is subjected to catalytic reaction to obtain the light hydrocarbon reactant;

the light hydrocarbon reactant enters a second reaction section of the heavy oil lifting pipe to be mixed with the first reaction oil gas and undergo catalytic reaction to obtain second reaction oil gas;

the second reaction oil gas is further subjected to catalytic reaction in a third reaction section of the heavy oil riser to obtain third reaction oil gas;

the third reaction oil gas enters a settler through an outlet of the heavy oil riser and is separated in the settler to obtain oil gas and the catalyst;

and sending the catalyst to the heavy oil riser and the light hydrocarbon riser for recycling, and sending the oil gas serving as target gas to a separation system.

Optionally, before the heavy oil feedstock contacts with a catalyst and undergoes a catalytic reaction in the first reaction section of the heavy oil riser to obtain a first reaction oil gas, the method further comprises:

injecting pre-lift gas into the first reaction section of the heavy oil riser; and/or

The light hydrocarbon feed contacts the catalyst in the light hydrocarbon riser and undergoes catalytic reaction, before a second light hydrocarbon reactant is obtained, the method further comprising:

and injecting pre-lifting gas into the light hydrocarbon lifting pipe.

Optionally, the heavy oil feed is contacted with a catalyst and subjected to a catalytic reaction in a first reaction section of a heavy oil riser, including catalysis under the following operating conditions:

the mass ratio of the catalyst to the heavy oil feed is 2-10.

Optionally, the light hydrocarbon feed is contacted with the catalyst and catalytically reacted within the light hydrocarbon riser, including catalysis under the following operating conditions:

the mass ratio of the catalyst to the light hydrocarbon feed is 2-20.

In one aspect, an apparatus for increasing the content of aromatics in propylene and gasoline is provided, the apparatus comprising: heavy oil riser, light hydrocarbon riser, settler and regenerator;

the heavy oil riser comprises a first reaction section, a second reaction section and a third reaction section which are sequentially communicated from bottom to top;

the outlet of the light hydrocarbon riser is communicated with the bottom end of the second reaction section, and the outlet of the third reaction section is communicated with the settler;

the bottom of the settler is connected with the regenerator, and the bottom of the regenerator is respectively communicated with the side wall of the first reaction section and the side wall of the light hydrocarbon riser.

Optionally, the apparatus further comprises a first regeneration chute;

a first end of the first regeneration chute is in communication with the sidewall of the first reaction section and a second end of the first regeneration chute is in communication with the bottom of the regenerator.

Optionally, the apparatus further comprises a second regeneration chute;

the first end of the second regeneration inclined tube is communicated with the side wall of the light hydrocarbon riser, and the second end of the second regeneration inclined tube is communicated with the bottom of the regenerator.

Optionally, the device further comprises a to-be-grown inclined tube;

the first end of the inclined tube to be grown is communicated with the bottom of the settler, and the second end of the inclined tube to be grown is communicated with the regenerator.

Optionally, the settler comprises a first cyclone and a second cyclone;

the inlet of the first cyclone separator is connected with the outlet of the third reaction section, and the outlet of the first cyclone separator is opposite to or directly communicated with the inlet of the second cyclone separator;

the bottom of the second cyclone separator is used for outputting the catalyst, and the top of the second cyclone separator is used for outputting oil gas.

The technical scheme provided by the application can at least bring the following beneficial effects:

heavy oil feeding carries out catalytic reaction with catalyst contact in the heavy oil riser, and light hydrocarbon feeding carries out catalytic reaction with catalyst contact in the light hydrocarbon riser, because heavy oil feeding and light hydrocarbon feeding separately react, consequently can make the two all be in optimum reaction condition to can be when satisfying the production demand, reduction production energy consumption, and then reduction in production cost. And because the light hydrocarbon reactant is mixed with the heavy oil feed which is undergoing catalytic reaction, the catalyst with activity in the light hydrocarbon reactant can continuously catalyze the heavy oil feed, so that the catalytic cracking reaction capability of the heavy oil feed can be improved, and the yield of the target products such as the aromatic hydrocarbon in propylene and gasoline can also be improved.

Drawings

FIG. 1 is a schematic flow chart of a method for increasing the propylene and aromatics content in gasoline provided by an embodiment of the present application;

FIG. 2 is a schematic structural diagram of a first apparatus for increasing the aromatic hydrocarbon content in propylene and gasoline provided in the examples of the present application;

FIG. 3 is a schematic diagram of a second apparatus for increasing the aromatics content in propylene and gasoline provided in the examples herein;

FIG. 4 is a schematic structural diagram of a third apparatus for increasing the aromatic hydrocarbon content in propylene and gasoline provided in the examples of the present application.

Reference numerals:

1: a heavy oil riser; 11: a first reaction section; 12: a second reaction section; 13: a third reaction section; 131: an outlet of the third reaction zone; 2: a light hydrocarbon riser; 3: a settler; 31: the bottom of the settler; 32: a first cyclone separator; 321: an inlet of a first cyclone; 322: an outlet of the first cyclone; 33: a second cyclone separator; 331: an inlet to the second cyclone; 332: a bottom of the second cyclone; 333: a top of the second cyclone; 4: a regenerator; 41: the bottom of the regenerator; 5: a first regeneration chute; 51: a first end of a first regeneration chute; 52: a second end of the first regeneration chute; 6: a second regenerative chute; 61: a first end of a second regenerative chute; 62: a second end of a second regeneration chute; 7: a pipe chute to be grown; 71: a first end of a to-be-grown inclined tube; 72: a second end of the inclined tube to be grown; 8: a pressure controller; 9: a temperature sensor; 10: a flow controller.

Detailed Description

To make the objects, technical solutions and advantages of the present application more clear, embodiments of the present application will be described in further detail below with reference to the accompanying drawings.

FIG. 1 is a schematic flow chart of a method for increasing the content of aromatic hydrocarbons in propylene and gasoline provided by an embodiment of the application. Referring to fig. 1, the method includes:

step 101: the heavy oil feed is contacted and mixed with the catalyst in the heavy oil lifting pipe and is subjected to catalytic reaction.

The heavy oil feedstock refers to the residual heavy oil after gasoline and diesel oil are extracted from crude oil. Heavy oil feeds are characterized by high molecular weight and high viscosity.

In addition, the heavy oil riser is a means for contacting the heavy oil feed with the catalyst sufficiently to catalyze the heavy oil feed.

Moreover, the catalyst is used for catalyzing the heavy oil feed so that macromolecular hydrocarbons in the heavy oil feed are converted into micromolecular hydrocarbons. The type of the catalyst can be selected according to the use requirement, for example, the catalyst can be a rare earth Y-type molecular sieve cracking catalyst, an ultrastable Y-type molecular sieve cracking catalyst or a rare earth hydrogen Y-type molecular sieve cracking catalyst, and the like.

It is worth noting that the heavy oil feed may be preheated prior to entering the heavy oil riser. So, can make the heavy oil feeding that gets into in the heavy oil riser distribute in the heavy oil riser better to can make the heavy oil feeding contact the mixture with the catalyst better, and then can make catalytic reaction more abundant.

The preheating temperature can be selected according to the use requirement, for example, the preheating temperature can be 150-300 ℃. Illustratively, the preheating temperature may be 150 ℃, 200 ℃, 250 ℃, or 300 ℃, etc.

Step 102: the light hydrocarbon feed is contacted and mixed with the catalyst in the light hydrocarbon lifting pipe and is subjected to catalytic reaction to obtain a light hydrocarbon reactant.

It should be noted that light hydrocarbon feedstock refers to a substance composed of two elements, i.e., hydrocarbon, such as mixed carbon four, light gasoline or diesel, which belong to light hydrocarbon feedstock.

In addition, the light hydrocarbon riser is a component for fully contacting light hydrocarbon feeding with the catalyst to catalyze the light hydrocarbon feeding.

Moreover, the catalyst is used for catalyzing light hydrocarbon feeding, so that the light hydrocarbon feeding is converted into target products such as liquefied gas, aromatic hydrocarbon and the like. The type of the catalyst can be selected according to the use requirement, for example, the catalyst can be a rare earth Y-type molecular sieve cracking catalyst, an ultrastable Y-type molecular sieve cracking catalyst or a rare earth hydrogen Y-type molecular sieve cracking catalyst, ZSM-5, and the like.

It is noted that the catalyst in contact with the light hydrocarbon feed and the catalyst in contact with the heavy oil feed are the same type of catalyst, i.e., the catalyst catalyzing the heavy oil feed and the catalyst catalyzing the light hydrocarbon feed are the same catalyst. Therefore, the catalyst is convenient to recycle in the later period.

The values indicate that the light hydrocarbon feed may be preheated prior to entering the light hydrocarbon riser. So, can make the lighter hydrocarbons feeding that gets into in the lighter hydrocarbons riser distribute better in the lighter hydrocarbons riser to can make the lighter hydrocarbons feeding contact with the catalyst better, and then can make catalytic reaction more abundant.

The preheating temperature can be selected according to the use requirement, for example, the preheating temperature can be 40-500 ℃. Illustratively, the preheating temperature may be 40 ℃, 100 ℃, 200 ℃, 250 ℃, 300 ℃, 400 ℃, or 500 ℃, etc.

Step 103: the light hydrocarbon reactant is mixed with the heavy oil feed undergoing catalytic reaction and continues to undergo catalytic reaction, and gas-solid separation and fractionation are carried out after the reaction.

It should be noted that the light hydrocarbon reactant refers to a product generated after a catalytic reaction of a light hydrocarbon feed. Wherein, because the reaction coke rate of light hydrocarbon feeding is low, because of catalyst and light hydrocarbon feeding take place the reaction back, the surface of catalyst can not be all attached to by the produced coke of light hydrocarbon feeding, and the catalyst still has certain catalytic activity this moment.

In addition, after the light hydrocarbon reactant is mixed with the heavy oil feed, the light hydrocarbon reactant carries the catalyst still having activity, so that the catalyst can be mixed and contacted with the heavy oil feed, and the heavy oil feed can be continuously catalyzed.

Further, the gas-solid separation is an operation for separating the catalyst and the oil gas. Wherein, the oil gas refers to a mixture of a product generated after the heavy oil feeding material is subjected to catalytic reaction and a product generated after the light hydrocarbon feeding material is subjected to catalytic reaction.

Wherein, the separated catalyst can be regenerated by burning coke after steam stripping, namely, the coke attached to the catalyst is burnt out by adopting a combustion method, thereby the activity of the catalyst is recovered. Preferably, the regenerated catalyst can be respectively returned to the heavy oil riser and the light hydrocarbon riser for recycling. Thus, resources can be repeatedly used, and the production cost can be reduced.

Fractionation is then the operation used to fractionate the hydrocarbons to obtain the target product. The target products refer to propylene and aromatic hydrocarbon generated after catalytic reaction of heavy oil feed and light hydrocarbon feed. Therefore, the required gasoline can be quickly and conveniently obtained by fractionating the oil gas.

Wherein, the mixing of the light hydrocarbon reactant and the heavy oil feedstock undergoing the catalytic reaction in step 103 and the continuing of the catalytic reaction may be: the light hydrocarbon reactant is contacted with the catalyst in the first reaction section of the heavy oil riser in the heavy oil feeding pipe, and is mixed after the catalytic reaction.

It should be noted that, after the heavy oil feedstock contacts the catalyst and undergoes the catalytic reaction in the first reaction section of the heavy oil riser, it indicates that the heavy oil feedstock has undergone the catalytic reaction with the catalyst in the first reaction section of the heavy oil riser. That is, the light hydrocarbon reactant may be mixed with the heavy oil feedstock undergoing the catalytic reaction at the end of the first reaction section of the heavy oil riser and continue the catalytic reaction, or the light hydrocarbon reactant may be mixed with the heavy oil feedstock undergoing the catalytic reaction after the first reaction section of the heavy oil riser and continue the catalytic reaction.

In addition, since the reaction coking rate of the heavy oil feedstock is high, the catalyst after catalytic reaction with the heavy oil feedstock in the first reaction stage of the heavy oil riser may lose activity due to excessive coke adhered to the surface, and thus, the heavy oil feedstock cannot be continuously catalyzed.

The values indicate that the catalyst after the catalytic reaction with the light hydrocarbon feed in the light hydrocarbon riser can continuously catalyze the heavy oil feed for catalytic reaction, so that the reaction capacity of the catalytic cracking of the heavy oil feed can be improved.

Specifically, step 103 may be: heavy oil feeding is contacted with a catalyst in a first reaction section of a heavy oil lifting pipe and is subjected to catalytic reaction to obtain first reaction oil gas; the light hydrocarbon is fed into the light hydrocarbon lifting pipe to contact with the catalyst and carry out catalytic reaction to obtain a light hydrocarbon reactant; the light hydrocarbon reactant enters a second reaction section of the heavy oil riser to be mixed with the first reaction oil gas and undergo catalytic reaction to obtain second reaction oil gas; the second reaction oil gas is further subjected to catalytic reaction in a third reaction section of the heavy oil riser to obtain third reaction oil gas; the third reaction oil gas enters the settler through the outlet of the heavy oil riser and is separated in the settler to obtain oil gas and a catalyst; the catalyst is sent to a heavy oil riser and a light hydrocarbon riser for recycling, and the oil gas is taken as target gas and sent to a separation system.

It should be noted that the first reaction oil gas mainly comprises propylene and aromatic hydrocarbons, and unreacted heavy oil feed and catalyst.

In addition, when the heavy oil feedstock contacts the catalyst in the first reaction section of the heavy oil riser and is subjected to catalytic reaction, the reaction time can be preset according to the use requirement, and for example, the reaction time can be 0.05 to 5 seconds. Illustratively, the reaction time may be 0.05s, 0.2s, 0.35s, 0.6s, 0.8s, 1s, 2s, 3s, 4s, 5s, or the like.

In addition, when the heavy oil feedstock contacts the catalyst in the first reaction section of the heavy oil riser and performs catalytic reaction, the mass of the catalyst and the heavy oil feedstock can be pre-selected according to the use requirement, for example, the mass ratio of the catalyst to the heavy oil feedstock can be 2 to 10. Illustratively, the mass ratio may be 2, 3, 4, 5, 6, 7.5, 9, or 10, etc.

It should be noted that the light hydrocarbon reactants include primarily propylene, as well as unreacted light hydrocarbon feed and catalyst.

In addition, light hydrocarbon feeding is contacted with the catalyst in the light hydrocarbon lifting pipe and is carried out catalytic reaction, and reaction time can be preset according to the use requirement, for example, the reaction time can be 0.05-5 s. Illustratively, the reaction time may be 0.05s, 0.2s, 0.35s, 0.6s, 0.7s, 1s, 2s, 3s, 4s, 5s, or the like.

Moreover, light hydrocarbon feeding is in contact with the catalyst in the light hydrocarbon lifting pipe and is carried out catalytic reaction, the quality of catalyst and light hydrocarbon feeding all can carry out the preselection according to the user demand, for example, the mass ratio of catalyst and light hydrocarbon feeding can be 2 ~ 20. Illustratively, the mass ratio may be 2, 3, 4, 5, 6, 7.5, 9, 12, 15, 17, or 20, etc.

The values show that after the light hydrocarbon reactant enters the second reaction section of the heavy oil riser, the total volume of the oil gas is increased, so that the partial pressure of the oil gas in the first reaction can be reduced, and the yield of the small-molecule propylene can be improved.

It should be noted that the second reaction oil gas mainly comprises propylene and aromatic hydrocarbons, and unreacted heavy oil feed, light hydrocarbon feed and catalyst.

In addition, the light hydrocarbon reactant enters the second reaction section of the heavy oil riser to be mixed with the first reaction oil gas and undergo catalytic reaction, the reaction time can be preset according to the use requirement, and for example, the reaction time can be 1-10 s. The reaction time may be, for example, 1s, 2s, 3s, 4s, 5s, 6s, 7s, 8s, 9s, 10s, or the like.

It should be noted that the third reaction oil gas mainly comprises propylene and aromatic hydrocarbon, and a catalyst attached with coke.

In addition, when the second reaction oil gas is further subjected to catalytic reaction in the third reaction section of the heavy oil riser, the reaction time can be preset according to the use requirement, and for example, the reaction time can be 0.5-5 s. Illustratively, the reaction time may be 0.5s, 0.7s, 1.2s, 1.7s, 2s, 3s, 4s, 5s, or the like.

The first reaction zone, the second reaction zone and the third reaction zone are communicated in sequence.

In addition, the settler is a component for settling the third reaction oil gas to obtain oil gas and catalyst.

The explanation of the value is that the oil gas and the catalyst in the third reaction oil gas have different mass, so the centrifugal force generated when the oil gas and the catalyst rotate in the settler is different, and the third reaction oil gas can be separated by the centrifugal force to obtain the oil gas and the catalyst.

It should be noted that, because the oil gas mainly includes propylene and aromatics, after being sent to the separation system, the oil gas can be separated to obtain propylene and aromatics, so as to meet different use requirements.

Wherein, before the heavy oil feeding material contacts with a catalyst in a first reaction section of a heavy oil riser and carries out catalytic reaction to obtain first reaction oil gas, the method also comprises the following steps: injecting pre-lift gas into the first reaction section of the heavy oil riser.

Note that the pre-lift stripping is a gas for adjusting the catalyst flow state. The pre-lift gas may be selected according to the use requirements, for example, the pre-lift gas may be a dry gas.

It is noted that when the catalyst enters the first reaction zone of the heavy oil riser, the catalyst will flow downward due to its own weight. At this time, the injected pre-lift gas moves upwards in the first reaction section of the heavy oil lift pipe, so that the pre-lift gas drives the catalyst to move upwards, and the flow state of the catalyst becomes more uniform in the moving process, so that the heavy oil feeding can be better catalyzed.

Wherein, light hydrocarbon feeding contacts with catalyst and carries out catalytic reaction in the light hydrocarbon lifting tube, before obtaining light hydrocarbon reactant, this method still includes: pre-lift gas is injected into the light hydrocarbon lift pipe.

It should be noted that, the effect of injecting into in advance lifting gas to the light hydrocarbon lifting pipe is the same with the effect of injecting into in advance lifting gas in the heavy oil lifting pipe, and this application embodiment is no longer repeated here.

In this application embodiment, the heavy oil feeding carries out catalytic reaction with the catalyst contact in the heavy oil riser, and the light hydrocarbon feeding carries out catalytic reaction with the catalyst contact in the light hydrocarbon riser, because heavy oil feeding and light hydrocarbon feeding separately react, consequently can make the two all be in optimum reaction condition to can be when satisfying the production demand, reduce the production energy consumption, and then reduction in production cost. And because the light hydrocarbon reactant is mixed with the heavy oil feed which is undergoing catalytic reaction, the catalyst with activity in the light hydrocarbon reactant can continuously catalyze the heavy oil feed, so that the catalytic cracking reaction capability of the heavy oil feed can be improved, and the yield of the target products such as the aromatic hydrocarbon in propylene and gasoline can also be improved.

FIG. 2 is a schematic structural diagram of an apparatus for increasing the content of aromatic hydrocarbons in propylene and gasoline according to an embodiment of the present application. Referring to fig. 2, the apparatus includes: heavy oil riser 1, light hydrocarbon riser 2, settler 3 and regenerator 4.

The heavy oil riser 1 comprises a first reaction section 11, a second reaction section 12 and a third reaction section 13 which are communicated from bottom to top in sequence; the outlet of the light hydrocarbon riser 2 is communicated with the bottom end of the second reaction section 12, and the outlet 131 of the third reaction section 13 is communicated with the settler 3; the bottom 31 of the settler 3 is connected with the regenerator 4, and the bottom 41 of the regenerator 4 is respectively communicated with the side wall of the first reaction section 11 and the side wall of the light hydrocarbon riser 2.

The heavy oil riser 1 is a means for bringing a heavy oil feed into sufficient contact with a catalyst to catalyze the heavy oil feed. The heavy oil riser 1 comprises a first reaction section 11, a second reaction section 12 and a third reaction section 13 which are sequentially communicated from bottom to top, wherein the first reaction section 11 is used for enabling heavy oil feed to contact with a catalyst to perform catalytic reaction so as to generate first reaction oil gas; the second reaction section 12 is used for mixing a light hydrocarbon reactant generated by light hydrocarbon feeding catalysis with the first reaction oil gas and performing catalytic reaction to generate a second reaction oil gas; the third reaction section 13 is used for further performing catalytic reaction on the second reaction oil gas to generate third reaction oil gas.

The values are stated in the specification, and the diameters of the first reaction zone 11, the second reaction zone 12 and the third reaction zone 13 may be the same or different.

In addition, the reaction temperature and the reaction pressure in the heavy oil riser 1 can be set according to the use requirement, for example, the reaction temperature of the heavy oil riser 1 is 400-700 ℃, and the absolute pressure is 0.12-0.40 Mpa (megapascal). Illustratively, the reaction temperature may be 400 ℃, 500 ℃, 540 ℃, 600 ℃, 700 ℃, or the like. The absolute pressure may be 0.12MPa, 0.18MPa, 0.24MPa, 0.30MPa or 0.4 MPa.

Moreover, the light hydrocarbon riser 2 is a member for fully contacting the light hydrocarbon feeding with the catalyst to catalyze the light hydrocarbon feeding. Wherein, the reaction temperature and the reaction pressure in the light hydrocarbon riser 2 can be set according to the use requirement, for example, the reaction temperature of the light hydrocarbon riser 2 is 400-700 ℃, and the absolute pressure is 0.12-0.40 Mpa. Illustratively, the reaction temperature may be 400 ℃, 500 ℃, 560 ℃, 600 ℃, 700 ℃, or the like. The absolute pressure may be 0.12MPa, 0.18MPa, 0.24MPa, 0.30MPa or 0.4 MPa.

The settler 3 is a member for settling the third reaction oil gas to obtain oil gas and catalyst. The size and type of the settler can be selected according to the use requirements, for example, the settler 3 can be a cyclone separator, and the settler 3 can also be a mechanical centrifugal separator.

The explanation of the value is that the oil gas and the catalyst in the third reaction oil gas have different mass, so the centrifugal force generated when the oil gas and the catalyst rotate in the settler is different, and the third reaction oil gas can be separated by the centrifugal force to obtain the oil gas and the catalyst. Wherein, the separated oil gas is output from the top of the settler 3, and the separated catalyst enters the regenerator 4 from the bottom of the settler 3 for regeneration.

The regenerator 4 is a means for regenerating the catalyst separated from the third reaction oil gas. The size and type of regenerator 4 can be selected according to the application requirements, for example, regenerator 4 can be a single stage regenerator, regenerator 4 can be a two stage regenerator, and regenerator 4 can also be a fast fluidized bed regenerator.

Specifically, when the device for increasing the content of aromatic hydrocarbons in propylene and gasoline is used for treating heavy oil feed and light hydrocarbon feed, the heavy oil feed can be conveyed into the first reaction section 11 of the heavy oil riser 1, so that the heavy oil feed contacts with a catalyst in the first reaction section 11 for catalytic reaction, and first reaction oil gas is obtained. And (3) conveying the light hydrocarbon feed into the light hydrocarbon lifting pipe 2, and enabling the light hydrocarbon feed to contact with a catalyst in the light hydrocarbon lifting pipe 2 for catalytic reaction to obtain a light hydrocarbon reactant. Then, the light hydrocarbon reactant enters the second reaction section 12 to be mixed with the first reaction oil gas and continuously perform catalytic reaction to obtain second reaction oil gas, and the second reaction oil gas further performs catalytic reaction in the third reaction section 13 to obtain third reaction oil gas. And finally, the third reaction oil gas enters the settler 3 to be separated from the oil gas and the catalyst, the separated oil gas is conveyed to a separation system to be subsequently separated, and the separated catalyst is conveyed to the regenerator 4 to be scorched and regenerated. And finally, conveying the regenerated catalyst into the heavy oil riser 1 and the light hydrocarbon riser 2 for repeated cyclic utilization.

In this application embodiment, heavy oil feeding carries out catalytic reaction with catalyst contact in heavy oil riser 1, and light hydrocarbon feeding carries out catalytic reaction with catalyst contact in light hydrocarbon riser 2, because heavy oil feeding and light hydrocarbon feeding separately react, consequently can make the both be in under the optimum reaction condition to can be when satisfying the production demand, reduce the production energy consumption, and then reduction in production cost. And because the light hydrocarbon reactant is conveyed to the second reaction section 12 to be mixed with the first reaction oil gas, the catalyst with activity in the light hydrocarbon reactant can continuously catalyze the unreacted heavy oil feed in the first reaction oil gas, so that the catalytic cracking reaction capability of the heavy oil feed can be improved, and the yield of the target products such as propylene, aromatic hydrocarbon and the like can be improved. And the catalyst is regenerated in the regenerator 4, and then the regenerated catalyst is recycled, so that resources can be fully utilized, and the production cost is reduced.

Optionally, referring to fig. 2, the apparatus further comprises a first regeneration chute 5; the first end 51 of the first regeneration ramp 5 communicates with the side wall of the first reaction section 11 and the second end 52 of the first regeneration ramp 5 communicates with the bottom 41 of the regenerator 4.

The first regeneration chute 5 is a member for connecting the first reaction zone 11 and the regenerator 4. The size and material of the first regeneration chute 5 can be selected according to the use requirement, for example, the material of the first regeneration chute 5 can be alloy, stainless steel, etc.

In addition, the inclination angle of the first regeneration pipe chute 5 can be set according to the use requirements, as long as it is ensured that the first end 51 of the first regeneration pipe chute 5 is lower than the second end 52 of the first regeneration pipe chute 5. In this way, the flow force of the regenerated catalyst can be increased, and the regenerated catalyst can enter the first reaction section 11 more smoothly.

Illustratively, after the catalyst is regenerated by burning in 14, the regenerated catalyst flows from the bottom 41 of the regenerator 4 through the side wall of the first reaction zone 11 into the first reaction zone 11 through the first regeneration chute 5. In this way, the regenerated catalyst can be quickly utilized.

Optionally, referring to fig. 2, the apparatus further comprises a second regeneration chute 6; the first end 61 of the second regeneration chute 6 is in communication with the side wall of the light hydrocarbon riser 2 and the second end 62 of the second regeneration chute 6 is in communication with the bottom 41 of the regenerator 4.

The second inclined regeneration pipe 6 is a member for connecting the light hydrocarbon riser 2 and the regenerator 4. The size and material of the second recycling inclined tube 6 can be selected according to the use requirement, for example, the material of the second recycling inclined tube 6 can be alloy, stainless steel, etc.

In addition, the inclination angle of the second regeneration chute 6 can be set according to the use requirement as long as the first end 61 of the second regeneration chute 6 is lower than the second end 62 of the second regeneration chute 6. Thus, the flow force of the regenerated catalyst can be increased, and the regenerated catalyst can enter the light hydrocarbon riser 2 more smoothly.

Illustratively, after the catalyst is coked and regenerated in the regenerator 4, the regenerated catalyst flows from the bottom 41 of the regenerator 4 through the side wall of the light hydrocarbon riser 2 into the light hydrocarbon riser 2 through the second regeneration inclined tube 6. In this way, the regenerated catalyst can be quickly utilized.

Optionally, referring to fig. 2, the apparatus further comprises a to-be-grown inclined tube 7; a first end 71 of the spent chute 7 communicates with the bottom 31 of the settler 3 and a second end 72 of the spent chute 7 communicates with the regenerator 4.

Note that the spent inclined tube 7 is a member for connecting the settler 3 and the regenerator 4. The catalyst separated in the settler 3 can enter the regenerator 4 through the spent inclined tube 7. The size and material of the inclined tube to be grown 7 can be selected according to the use requirement, for example, the material of the inclined tube to be grown 7 can be alloy, stainless steel, and the like.

In addition, the inclination angle of the inclined tube to be generated 7 can be set according to the use requirement, as long as the first end 71 of the inclined tube to be generated 7 is higher than the second end 72 of the inclined tube to be generated 7. In this way, the flow force of the separated catalyst can be increased, and the separated catalyst can be introduced into the regenerator 4 more smoothly.

For example, after the fourth reaction oil gas is separated in the settler 3, the separated catalyst flows into the regenerator 4 through the spent inclined tube 7. Thus, the catalyst can be quickly burnt and regenerated.

Alternatively, referring to fig. 3, the settler 3 comprises a first cyclone 32 and a second cyclone 33; the inlet 321 of the first cyclone separator 32 is connected with the outlet 131 of the third reaction section 13, and the outlet 322 of the first cyclone separator 32 is opposite to or directly communicated with the inlet 331 of the second cyclone separator 33; the bottom 332 of the second cyclone 33 is used for outputting catalyst, and the top 333 of the second cyclone 33 is used for outputting oil gas.

The first cyclone 32 and the second cyclone 33 are both members for separating the third reaction oil gas. The size and material of the first cyclone separator 32 and the second cyclone separator 33 can be set according to the use requirement, as long as it is ensured that the first cyclone separator 32 and the second cyclone separator 33 can sufficiently separate the third reaction oil gas into the catalyst and the oil gas.

In addition, after the third reaction oil gas enters the first cyclone separator 32 and the second cyclone separator 33, the third reaction oil gas can rotate in the first cyclone separator 32 and the second cyclone separator 33, so that the third reaction oil gas has large inertial centrifugal force, and the catalyst in the third reaction oil gas can be separated from the oil gas through the inertial centrifugal force.

Specifically, when the third reaction oil gas is separated by the regenerator 3, the third reaction oil gas comes out from the outlet 131 of the third reaction section 13 and then enters the first cyclone 32 to be separated for the first time, and then the separated oil gas and the separated catalyst enter the second cyclone 33 through the outlet 322 of the first cyclone 32 to be separated for the second time. The oil and gas separated for the second time will be output through the top 333 of the second cyclone 33, and the catalyst separated for the second time will be output through the bottom 332 of the second cyclone 33. Therefore, through twice separation, the purity of the separated catalyst and oil gas is high, and subsequent utilization is facilitated.

Optionally, referring to fig. 4, the apparatus further comprises a pressure controller 8; the top of the settler 3 is provided with a pressure controller 8.

It should be noted that the pressure controller 8 can control and measure the pressure in the settler 3, and from this pressure, the pressure of the heavy oil riser 1 and the light hydrocarbon riser 2 during the catalytic reaction can be determined.

Exemplarily, the pressure controller 8 is arranged at the top of the settler 3, and can control and measure the pressure of the third reaction oil gas in the settler 3, so that the pressure in the heavy oil riser 1 and the pressure in the light hydrocarbon riser 2 can be analyzed and determined by the material balance principle, and then the heavy oil feeding can be ensured to be sufficiently catalytically reacted in the heavy oil riser 1, and the light hydrocarbon feeding can be sufficiently catalytically reacted in the light hydrocarbon riser 1.

Optionally, referring to fig. 4, the device further comprises a temperature sensor 9; temperature sensors 9 are arranged on the heavy oil lifting pipe 1 and the light hydrocarbon lifting pipe 2.

It should be noted that the temperature sensor 9 can control the temperature in the heavy oil riser 1 and the light hydrocarbon riser 2 to ensure that the heavy oil feed and the light hydrocarbon feed are sufficiently reacted catalytically.

In addition, the setting position of the temperature sensor 9 can be set according to the use requirement, and the setting position of the temperature sensor 9 in the embodiment of the present application is not limited thereto.

Illustratively, the temperature sensor 9 is disposed on the heavy oil riser 1, so that the reaction temperature in the heavy oil riser 1 can be controlled when the heavy oil feedstock is catalytically reacted in the heavy oil riser 1, so as to ensure that the heavy oil feedstock can be sufficiently catalytically reacted in the heavy oil riser 1. The temperature sensor 9 is arranged on the light hydrocarbon lifting pipe 2, and can control the reaction temperature in the light hydrocarbon lifting pipe 2 when the light hydrocarbon feeding is carried out catalytic reaction in the light hydrocarbon lifting pipe 2, so as to ensure that the light hydrocarbon feeding can be carried out catalytic reaction in the light hydrocarbon lifting pipe 1 fully.

Optionally, referring to fig. 4, the apparatus further comprises a flow controller 10, and the flow controller 10 is connected to the inlet of the heavy oil riser 1 and the inlet of the light hydrocarbon riser 2, respectively.

It should be noted that the flow controller 10 can control the flow of the heavy oil feed entering the heavy oil riser 1 and the flow of the light hydrocarbon feed entering the light hydrocarbon riser 2 during the catalytic reaction operation.

In addition, the setting position of the flow controller 10 may be preset according to the use requirement, and the specific setting position of the flow controller 10 in the embodiment of the present application is not limited thereto.

Illustratively, by connecting the flow controller 10 to the inlet of the heavy oil riser 1, the flow rate of the heavy oil feedstock entering the first reaction section 11 of the heavy oil riser 1 can be controlled to ensure that the mass ratio between the heavy oil feedstock entering the first reaction section 11 and the catalyst is sufficient, so as to ensure that the catalytic reaction of the heavy oil feedstock is sufficiently performed. With the access connection of flow controller 10 and light hydrocarbon riser 2, the flow when light hydrocarbon feeding enters into light hydrocarbon riser 2 to ensure that the quality ratio between the light hydrocarbon feeding that gets into light hydrocarbon riser 2 and the catalyst satisfies the needs, thereby can ensure that the catalytic reaction of light hydrocarbon feeding fully goes on.

In order to make the technical solutions and advantages of the present application more clear, the following detailed description will be given by means of alternative embodiments.

Examples

The device for improving the aromatic hydrocarbon content in propylene and gasoline provided by the embodiment of the application is used for catalyzing heavy oil feed and light hydrocarbon feed, wherein the composition of the heavy oil feed entering the device is shown in table 1, and the light hydrocarbon feed entering the device is carbon four and light gasoline generated after the heavy oil feed is subjected to catalytic reaction. Wherein, the process conditions are shown in Table 2, and the test results are shown in Table 3.

TABLE 1

TABLE 2

Parameter(s)	Numerical value
		Reaction temperature of heavy oil riser, deg.C	540
Reaction temperature of light hydrocarbon riser, DEG C	560
		Reaction pressure, MPa (a)	0.24
Reaction time s of first reaction section of heavy oil lifting pipe	0.8
		Reaction time of second reaction section of heavy oil lifting pipe, s	4
Reaction time s of the third reaction section of the heavy oil lifting pipe	1.2
		Total reaction time of light hydrocarbon riser, s	0.7
Regenerator catalyst temperature,. deg.C	700
		Agent-oil ratio of heavy oil riser	7.5
Agent-oil ratio of light hydrocarbon lift pipe	15

TABLE 3

Product of	Numerical value
		Dry gas wt%	4.5
Liquefied gas wt%	49.5
		Wherein the propylene yield is wt%	20.8
Gasoline wt%	15.4
		Wt% of diesel oil	16.8
Oil slurry wt%	4.8
		Wt% of coke	9
Gasoline properties
		The olefin content v%	～10
Aromatic content v%	～62
		Octane RON	96

From the results in table 3 it can be seen that with the apparatus provided herein, a desirable product distribution can be obtained, especially a propylene yield in the product of 20.8 wt%. And the aromatic hydrocarbon content is 62 v%, the octane number is 96, and the gasoline is a better gasoline blending component and can also be sold as a single product.

Comparative example

The heavy oil feed and the light hydrocarbon feed are catalyzed by the method for producing propylene and aromatic hydrocarbon by double-riser catalytic cracking provided by the related technology, wherein the composition of the heavy oil feed entering the heavy oil riser is shown in table 4, and the light hydrocarbon feed entering the light hydrocarbon riser is carbon four and light gasoline generated after the heavy oil feed is subjected to catalytic reaction. Wherein, the process conditions are shown in Table 5, and the test results are shown in Table 6.

TABLE 4

Raw oil	Numerical value
		Density, kg/m3	899
Carbon residue in wt%	4.58
		Sulfur content, wt.%	0.27
Nitrogen content, wt%	0.23
		Group composition wt%
Saturation fraction	64.95
		Aromatic component	23.35
Glue	11.09
		Asphaltenes	0.61

TABLE 5

Parameter(s)	Numerical value
		Reaction temperature of heavy oil riser, deg.C	540
Reaction temperature of light hydrocarbon riser, DEG C	560
		Reaction pressure, MPa (a)	0.24
Reaction time s of first reaction section of heavy oil lifting pipe	0.8
		Reaction time of second reaction section of heavy oil lifting pipe, s	4
Reaction time s of the third reaction section of the heavy oil lifting pipe	1.2
		Total reaction time of light hydrocarbon riser, s	0.7
Regenerator catalyst temperature,. deg.C	700
		Agent-oil ratio of heavy oil riser	7.5
Agent-oil ratio of light hydrocarbon lift pipe	15

TABLE 6

As can be seen from the results of Table 6, the propylene yield in the product obtained by the method and apparatus provided in the related art can be 19 wt%, and the aromatic hydrocarbon content is only 55 v% and the octane number is 95.5.

Therefore, by comparing the examples and the comparative examples, the yield of propylene and aromatic hydrocarbon in the product can be improved by adopting the device provided by the examples, thereby improving the energy utilization rate.

The above description is only exemplary of the present application and should not be taken as limiting the present application, as any modification, equivalent replacement, or improvement made within the spirit and principle of the present application should be included in the protection scope of the present application.