CN112538380B

CN112538380B - Method and device for integrating heavy oil contact cracking and coke gasification

Info

Publication number: CN112538380B
Application number: CN201910901510.9A
Authority: CN
Inventors: 蓝兴英; 李大鹏; 张玉明; 高金森; 高亚男; 霍鹏举; 杨会民; 黄勇; 姚晓虹; 黄传峰; 王成秀; 石孝刚; 王汝成; 任健; 蒋中山; 王武生
Original assignee: Nanjing Zhonghui Energy Technology Research And Development Center; China University of Petroleum Beijing
Current assignee: Nanjing Zhonghui Energy Technology Research And Development Center; China University of Petroleum Beijing
Priority date: 2019-09-23
Filing date: 2019-09-23
Publication date: 2022-02-22
Anticipated expiration: 2039-09-23
Also published as: CN112538380A

Abstract

The invention provides a method and a device for integrating heavy oil contact cracking and coke gasification. The method utilizes a coupling reactor and a coke burning regenerator, wherein the coupling reactor comprises an upper cracking section and a lower gasification section, and the cracking section and the gasification section are communicated with each other; the method comprises the following steps: introducing a heavy oil raw material into a cracking section, and contacting the heavy oil raw material with a contact agent to crack so as to obtain light oil gas and a carbon deposit contact agent; the carbon deposit contact agent is conveyed into a coke burning regenerator for partial coke burning treatment, then conveyed into a gasification section, and is subjected to gasification reaction with a gasification agent to be regenerated, so that a regeneration contact agent and synthesis gas are obtained; the regenerated contact agent returns to the cracking section for cyclic utilization, and the synthesis gas ascends to enter the cracking section; and (3) carrying out gas-solid separation on the light oil gas and the synthesis gas merged upwards to obtain purified oil gas. The method provided by the invention realizes mutual supply and heat complementation of materials in three reaction processes of heavy oil cracking, coke burning and coke gasification, reduces energy consumption and saves the floor area of equipment.

Description

Method and device for integrating heavy oil contact cracking and coke gasification

Technical Field

The invention relates to a heavy oil lightening processing technology, in particular to a method and a device for integrating heavy oil contact cracking and coke gasification.

Background

The heavy oil is the residue left after the crude oil is fractionated to extract gasoline, kerosene and diesel oil; in addition, the stratum is also rich in heavy oil resources. Heavy oil has the characteristics of heavy component weight, low hydrogen-carbon ratio and the like, and generally has higher contents of sulfur, nitrogen, heavy metal and high carbon residue value. With continuous exploitation of crude oil, the problems of heavy oil and poor oil are more and more serious, and environmental regulations are increasingly strict, so that how to process heavy oil into light oil and convert heavy oil into qualified clean oil products such as gasoline, diesel oil and liquefied gas is a major challenge for petroleum processing enterprises at present.

At present, the processing route of heavy oil can be roughly divided into hydrogenation and decarburization. Wherein, the hydrogenation treatment is to increase the hydrogen-carbon ratio by the reaction of heavy oil and hydrogen. Because the carbon residue value, the heavy metal content and the heteroatom content of the heavy oil are high, a hydrocracking mode is directly adopted, a large amount of hydrogen is usually needed, the hydrocracking mode is usually carried out under the conditions of high pressure and high-efficiency catalysts, and the process implementation difficulty is relatively high. And because the heavy oil has a lower hydrogen-carbon ratio, the problem of hydrogen deficiency in the heavy oil lightening process is more prominent.

The decarbonization process is generally a redistribution of the hydrocarbon resources in the feedstock into products. At present, the more common decarburization technologies at home and abroad mainly comprise catalytic cracking and delayed coking processes. The catalytic cracking means is adopted, the catalyst is usually subjected to rapid carbon deposition or poisoning inactivation, the coke formation amount in the heavy oil catalytic cracking process is large, if the catalyst is regenerated by adopting the traditional coke burning mode, a large amount of external heat extraction is often needed, and meanwhile, the carbon resource is greatly wasted to a certain extent. The delayed coking process has no catalyst involved and thus has high material adaptability. However, a large amount of solid coke is produced as a byproduct in the delayed coking process, and the latest environmental protection requirement requires that factory-limiting measures be taken for high-sulfur coke with the sulfur content of more than 3 percent, so that the application of the delayed coking process is limited.

In view of the advantages and disadvantages of hydrogenation and decarburization, cracking heavy oil into light oil, and then hydrotreating the light oil to obtain qualified products become the choice of many petroleum processing enterprises.

CN1504404A discloses a process combining oil refining and gasification. Petroleum hydrocarbon is firstly contacted with a coke transfer agent in a reactor for reaction, oil gas enters a subsequent product separation system, the coke transfer agent with carbon deposit is sent to a gasification furnace and reacts with steam, oxygen-containing gas and the like to generate synthesis gas, and the regeneration of the coke transfer agent with carbon deposit is realized. The regenerated coke transfer agent returns to the cracking section for recycling. The invention realizes the combination of two technological processes of oil refining and gasification, the technological process is close to the catalytic cracking process, and the traditional coke burning regeneration process is replaced by the coke gasification process.

CN102234534A discloses a method for processing inferior heavy oil, which comprises the steps of selecting a low-activity contact agent to carry out heavy oil cracking reaction, conveying the carbon deposit contact agent after reaction to different reaction areas of a gasification section to carry out combustion or gasification regeneration, respectively obtaining semi-regenerants and secondary regenerants with different coke contents, and increasing the operation difficulty of the process to a certain extent through multi-section regeneration reaction in a reactor.

CN102115675A discloses a heavy oil lightening processing method and device. Raw oil firstly reacts with a solid heat carrier in a thermal cracking reactor to obtain a light oil gas product. Heavy coke is attached to the surface of the solid heat carrier and enters a combustion (gasification) reactor through a material returning valve to remove the surface coke, and the regenerated high-temperature solid heat carrier returns to the thermal cracking reactor through a distribution valve part to be used as a reaction bed material.

CN102965138A discloses a pyrolysis gasification coupling process of a heavy oil double-reaction-tube semicoke circulating bed, and proposes that a descending reaction tube is used for heavy oil cracking to obtain a light oil gas product. After coking, semicoke enters a riser gasification reactor to perform gasification reaction with oxidant and steam to generate synthesis gas, and the reacted high-temperature semicoke flows into a material returning device to continue circulation to provide heat required by heavy oil reaction.

In the method, different types of reactors such as a fluidized bed, a lifting pipe and a downer are adopted for heavy oil cracking reaction, but the generated heavy coke needs to be conveyed to another reactor for gasification, combustion and other regeneration reactions, so that materials need to be subjected to circulating material returning operation among a plurality of reactors, and not only is the occupied area of equipment in actual production larger, but also the energy consumption is higher.

Disclosure of Invention

Aiming at the defects, the invention provides the method for integrating the heavy oil contact cracking and the coke gasification, which can realize the mutual supply and heat complementation of materials in three reaction processes of the heavy oil cracking, the coke burning and the coke gasification, reduce the energy consumption in the heavy oil processing process and save the floor area of equipment.

The invention also provides a device for integrating heavy oil contact cracking and coke gasification, and the device is used for processing heavy oil, so that the method for integrating heavy oil contact cracking and coke gasification can be realized, the energy consumption is saved, and the occupied area of equipment is saved.

In order to achieve the above object, the present invention provides a method for integrating heavy oil contact cracking and coke gasification, which is carried out by using a coupling reactor and a coke-burning regenerator, wherein the coupling reactor is provided with a cracking section and a gasification section which are communicated with each other internally; the method comprises the following steps:

introducing a heavy oil raw material into a cracking section at the upper part of the coupling reactor, and contacting the heavy oil raw material with a contact agent to crack so as to obtain light oil gas and a carbon deposit contact agent;

conveying the carbon deposit contact agent into a coke burning regenerator for partial coke burning treatment, conveying the carbon deposit contact agent into a gasification section at the lower part of the coupling reactor, and carrying out gasification reaction with a gasification agent to regenerate the carbon deposit contact agent and the synthesis gas; the regenerated contact agent returns to the cracking section for cyclic utilization, and the synthesis gas ascends to enter the cracking section;

and (3) carrying out gas-solid separation on the light oil gas and the synthesis gas merged upwards to obtain purified oil gas.

The invention provides a method for integrating heavy oil contact cracking and coke gasification, wherein a heavy oil raw material firstly enters a cracking section at the upper part of a coupling reactor and contacts with a contact agent to be cracked, so that light oil gas and coke are obtained. The coke is attached to the surface of the contact agent, namely the carbon deposit contact agent.

The carbon deposit contact agent firstly enters a coke burning regenerator for partial coke burning treatment to convert partial coke into CO and CO₂The formed flue gas can be discharged from a flue gas outlet of the coke burning regenerator, and the temperature of the semi-regenerated carbon deposit contact agent obtained correspondingly is increased to provide heat for the subsequent gasification reaction; the semi-regenerated carbon deposit contact agent then enters the gasification section to carry out gasification reaction, so that the coke is fully regenerated, and the high-temperature regenerated contact agent and the high-temperature synthesis gas are obtained.

The high-temperature regenerated contact agent returns to the cracking section to provide partial heat and catalytic activity required by heavy oil cracking for the cracking section; the high-temperature synthesis gas returns to the cracking section, which not only provides the required heat for the cracking reaction and ensures the full fluidization of the contact agent (regenerated contact agent), but also contains rich active micromolecules such as hydrogen, carbon monoxide and the like, which can improve the yield and quality of the light oil gas to a certain extent, inhibit the coking in the heavy oil cracking process, improve the product distribution of the heavy oil cracking and improve the yield of the light oil gas.

And (3) carrying out gas-solid separation on the light oil gas and the synthesis gas (collectively referred to as high-temperature oil gas) entering from the bottom of the cracking section to obtain purified oil gas. The purified oil gas can further pass through a gas-liquid fractionating tower, an oil gas absorption stabilizing tower and other systems to respectively obtain gas products such as synthesis gas, dry gas, liquefied gas and the like and light oil products. Of course, the obtained light oil product can be further cut and separated to obtain liquid products with different distillation range components, wherein heavy oil can be mixed with heavy oil raw materials for recycling processing; the synthesis gas can be used as a refinery hydrogen source.

Therefore, in the embodiment, the cracking section and the gasification section are integrated in the same coupling reactor and are matched with the coke-burning regenerator, so that the mutual supply of materials and the complementation of raw materials in three reaction processes of heavy oil cracking, coke combustion and coke gasification are realized. Compared with the existing process method for transporting and circulating materials among a plurality of reactors in the process of catalytic cracking of heavy oil and gasification of coke, the method provided by the invention not only can obviously reduce the energy consumption in the process of processing the heavy oil and improve the yield of light oil gas, but also solves the problems of high difficulty in circulating operation of the materials, large floor area of a heavy oil processing device, high equipment investment and the like in the existing process.

The heavy oil raw material is not particularly limited, and may be one or a mixture of several of heavy oil, super heavy oil, oil sand bitumen, atmospheric heavy oil, vacuum residual oil, catalytic cracking slurry oil, solvent deoiled bitumen, and the like, or one or a mixture of several of heavy tar and residual oil generated in a coal pyrolysis or liquefaction process, heavy oil generated in an oil shale dry distillation process, and heavy oil derived from a biomass medium-low temperature pyrolysis liquid product.

The inventor researches and discovers that the method for integrating heavy oil contact cracking and coke gasification has good treatment effect on heavy oil raw materials with the Conradson carbon residue value of more than 10 wt%, even on heavy oil raw materials with the Conradson carbon residue value of more than 15 wt%, and can obtain a large amount of light oil gas.

The contact agent used in the invention can be a decarburization modification contact agent which is commonly used at present, for example, the decarburization modification contact agent can be a silicon-aluminum material such as quartz sand, kaolin, argil, alumina, silica sol, montmorillonite, illite and the like, and also can be one or more of a catalytic cracking (FCC) industrial balancing agent or a waste catalyst, red mud, steel slag, blast furnace ash, coal ash and other solid particles.

The inventor finds that it is preferable to select a contact agent with relatively low cracking activity, for example, a contact agent with a micro-reaction activity index of 5-30, so as to ensure high cracking efficiency and light oil yield in the heavy oil cracking process. In the specific implementation process of the invention, the micro-reaction activity index of the used contact agent is 10-20, such as kaolin, clay, alumina, silica sol, industrial equilibrium agent or waste catalyst in the catalytic cracking process, and the like.

Furthermore, the contact agent is preferably in a microspherical shape, and the particle size of the contact agent is preferably distributed in a range of 10-500 mu m so as to have better fluidization performance; in the specific implementation process of the invention, the particle size distribution of the used contact agent is 20-200 μm.

In the invention, in the heavy oil cracking process, the surface of the carbon deposit contact agent preferably forms high-content coke, namely the carbon deposit contact agent with high coke content enters the gasification section for gasification reaction, so that the temperature rise and the temperature decrease of a large amount of contact agents in the cracking reaction and the gasification reaction process can be prevented, the energy consumed in the temperature rise process is mainly used for the gasification reaction of the coke, and the overall energy efficiency in the whole heavy oil processing process is improved. Specifically, it is desirable to maintain the contact agent surface coke mass content above 10% during the cracking process, for example, by using a smaller weight ratio of contact agent to heavy oil (i.e., the agent-to-oil ratio) to ensure that the heavy oil cracking process forms a higher coke content on the contact agent surface.

In the specific implementation process of the invention, the reaction temperature in the cracking section is usually controlled to be 450-700 ℃, the reaction pressure is 0.1-3.0 Mpa, the reaction time is 1-20 seconds, and the weight ratio (solvent-oil ratio) of the contact agent to the heavy oil raw material is 0.1-1.0: 1, the apparent gas velocity is 1-20 m/s. Preferably, the temperature of the cracking reaction is 480-580 ℃, the reaction pressure is 0.1-1.0 Mpa, such as normal pressure, the reaction time is 3-20 seconds, the agent-oil ratio is 0.2-0.6, and the apparent gas velocity is 1-20 m/s.

In the present stage, the catalyst-to-oil ratio in the heavy oil catalytic cracking process is usually greater than 1.0, and the coke content on the surface of the catalyst is usually less than 5%, so a large amount of heat is consumed in the gasification regeneration process to heat the catalyst and provide heat for the cracking reaction, resulting in low efficiency in the heavy oil processing process. Compared with the prior art, the method has the advantages that the agent-oil ratio is low and can be controlled below 1.0, so that the energy consumption in the whole heavy oil processing process is mainly concentrated in the gasification section, the temperature of the carbon deposit contact agent in the combustion process is increased in the coke burning regenerator to provide energy for the gasification reaction and regeneration of the gasification section, and the synthesis gas and the regeneration contact agent generated in the contact agent regeneration process provide heat for the cracking reaction, so that the energy consumption utilization rate in the whole heavy oil lightening processing process is very high, the required energy consumption is very low, and the production cost in the heavy oil processing process is remarkably reduced.

The gasification agent introduced into the gasification stage is not particularly limited in the present invention, and may be, for example, steam, an oxygen-containing gas, or a mixed gas of steam and an oxygen-containing gas. Wherein the oxygen-containing gas can be, for example, air, oxygen-enriched air, etc.

In the specific implementation process of the invention, the reaction temperature in the gasification section is generally controlled to be 800-1200 ℃, the reaction pressure is generally controlled to be 0.1-6.0 Mpa, the apparent gas velocity is generally controlled to be 0.1-5 m/s, and the retention time of the carbon deposit contact agent can be controlled to be 1-20 min. By carrying out the gasification reaction under the above conditions, the contact agent can be regenerated while ensuring sufficient reaction of the coke remaining on the surface of the contact agent, and high-quality synthesis gas and regenerated contact agent can be obtained.

As mentioned above, the synthesis gas generated in the gasification section moves upwards, enters the cracking section from the bottom and moves upwards in the cracking section, which not only can ensure the contact agent (or regenerated contact agent) to be fully fluidized, but also can provide the heat required by the cracking reaction, and in addition, the high-activity hydrogen-rich synthesis gas also provides the hydrogen atmosphere for the cracking of the heavy oil, thereby inhibiting the coking in the cracking process of the heavy oil and improving the yield of the light oil gas. In actual production, according to the amount of the synthesis gas required by the cracking section and the energy utilization condition, part of the synthesis gas is generally introduced into the cracking section, and the other part of the synthesis gas can be used for enriching the hydrogen source of a refinery, so that the light processing of heavy oil and the co-production of high-quality synthesis gas are realized.

As previously mentioned, the temperature of the char-forming contact agent increases during combustion in the char-combusting regenerator to provide energy for the subsequent gasification reaction. In a preferred embodiment of the invention, the carbon deposit contact agent is subjected to partial coking treatment in a coking regenerator so that the temperature of the obtained semi-regenerated contact agent reaches the temperature required by the gasification reaction, such as 800-1200 ℃, and then the semi-regenerated contact agent enters a gasification section for gasification reaction.

Specifically, oxygen gas such as oxygen, air and the like can be introduced from an oxygen-containing gas inlet at the bottom of the coke burning regenerator, so that the oxygen in the oxygen-containing gas reacts with carbon deposit on the surface of the carbon deposit contact agent to release heat, the temperature of the obtained semi-regeneration contact agent is raised to the temperature required by gasification reaction, and simultaneously flue gas mainly containing carbon monoxide and carbon dioxide is obtained and can be discharged from the top of the coke burning regenerator.

Specifically, the reaction conditions within the char regenerator may be: the scorching reaction temperature is 600-800 ℃, the scorching pressure is 0.1-6.0 Mpa, the scorching time is 20-200 s, and the gas velocity is 0.1-5.0 m/s.

In the invention, before the carbon deposit contact agent enters the coke burning regenerator, steam stripping treatment is preferably carried out firstly to fully remove a small amount of light oil gas remained in the carbon deposit contact agent, thereby being beneficial to the smooth proceeding of combustion and gasification reaction. Specifically, the carbon deposit contact agent in the cracking section descends to a steam stripping section at the lower part of the cracking section, oil gas components attached to the surface of the carbon deposit contact agent are stripped through steam, and then the carbon deposit contact agent can be transported outside the coupling reactor and enter a coke burning regenerator.

Specifically, when steam stripping is performed, the mass ratio of steam to the heavy oil raw material is generally controlled to be 0.03-0.30: 1, the temperature of the water vapor is 200-400 ℃, and the apparent gas velocity of the water vapor is 0.5-5.0 m/s.

Furthermore, before the gas-solid separation is carried out on the light oil gas and the synthesis gas, the temperature of the light oil gas and the synthesis gas can be reduced firstly, so that the temperature of the high-temperature oil gas can be reduced, and the reactions such as excessive cracking, coking and the like can be inhibited. In the specific implementation process of the invention, a cooling washing section is arranged at the upper part of the cracking section, so that high-temperature oil gas (light oil gas and synthesis gas) is subjected to heat exchange washing with other low-temperature liquid oil products such as heavy oil and the like in the cooling washing section, the temperature of the high-temperature oil gas is reduced, and a small amount of contact agent fine powder carried in the high-temperature oil gas is removed.

The high temperature oil gas after being cooled and washed still contains some carbon deposit contact agent, and in the specific implementation process of the present invention, the light oil gas and the synthetic gas from the bottom of the cracking section are led out of the coupling reactor and gas-solid separated to obtain purified oil gas, and the separated carbon deposit contact agent may be returned to the cracking section for reuse as the bed material for cracking heavy oil.

The invention is not limited to how to realize the gas-solid separation, and can adopt the gas-solid separation means commonly used in the heavy oil processing field, such as a cyclone separator.

The invention also provides a device for integrating heavy oil contact cracking and coke gasification, which is used for the method, and the device at least comprises a coupling reactor, a coke burning regenerator and a gas-solid separator, wherein:

the coupling reactor comprises an upper cracking section and a lower gasification section, and the cracking section and the gasification section are communicated with each other; the cracking section is provided with a heavy oil raw material inlet, a carbon deposit contact agent discharge port, an oil gas outlet, a regeneration contact agent return port and a synthesis gas inlet at the bottom; the gasification section is provided with a gasification agent inlet, a semi-regeneration contact agent inlet, a regeneration contact agent outlet and a synthesis gas outlet at the top;

the coke burning regenerator is provided with a carbon deposit contact agent inlet, an oxygen-containing gas inlet, a semi-regeneration contact agent discharge port and a flue gas discharge port;

the gas-solid separator is provided with an inlet, a solid discharge port and a gas discharge port;

the accumulated carbon contact agent discharge port of the cracking section is connected with the accumulated carbon contact agent inlet of the coke burning regenerator, the oil gas outlet of the cracking section is connected with the inlet of the gas-solid separator, the semi-regeneration contact agent discharge port of the coke burning regenerator is connected with the semi-regeneration contact agent inlet of the gasification section, and the regeneration contact agent discharge port of the gasification section is connected with the regeneration contact agent return port of the cracking section; the synthesis gas outlet of the gasification section is connected with the synthesis gas inlet of the cracking section.

Furthermore, the cracking section is also provided with a carbon deposit contact agent return port, and a solid discharge port of the gas-solid separator is connected with the carbon deposit contact agent return port of the cracking section. The carbon deposit contact agent separated by the gas-solid separator can be returned to the cracking section for recycling.

Further, a steam stripping section is arranged at the lower part in the cracking section; and/or a cooling washing section is arranged at the upper part in the cracking section. Wherein, the carbon deposit contact agent in the cracking section descends to the steam stripping section, and oil gas components attached to the surface of the carbon deposit contact agent are stripped out through steam. The light oil gas in the cracking section and the synthesis gas entering from the bottom of the cracking section go upwards to a cooling washing section, so that the high-temperature oil gas and other low-temperature liquid oil products are subjected to heat exchange washing to reduce the temperature of the high-temperature oil gas and remove a small amount of contact agent fine powder carried in the high-temperature oil gas.

The method for integrating heavy oil contact cracking and coke gasification provided by the invention realizes mutual supply and heat complementation of materials in three reaction processes of heavy oil cracking, coke burning and coke gasification by adopting the coupling reactor integrating the cracking section and the gasification section and the coke burning regenerator. Particularly, by selecting a proper contact agent and adjusting reaction conditions such as the agent-oil ratio and the like in the cracking reaction process, the maximization of the oil yield in the heavy oil cracking process and the high efficiency in the gasification process can be realized, the oil-gas co-production of heavy oil resources is realized, and greater economic benefit is obtained.

Therefore, compared with the process method for transporting and circulating materials among a plurality of reactors in the delayed coking process at the present stage, the method provided by the invention not only can obviously reduce the energy consumption in the heavy oil processing process, improve the yield of light oil gas and reduce the difficulty of material circulation operation, but also reduces the occupied area of a heavy oil processing device and reduces the equipment investment cost.

The invention provides a device for integrating heavy oil contact cracking and coke gasification, which is used for realizing the method. By adopting the device, the mutual supply and heat complementation of materials in three reaction processes of heavy oil cracking, coke burning and coke gasification are realized, the energy consumption and the material circulation operation difficulty in the heavy oil processing process are reduced, the yield of light oil gas is improved, and the economic index of the device is far higher than that of a heavy oil processing device in the prior art. In addition, the device has smaller occupied area and lower investment cost.

Drawings

FIG. 1 is a schematic diagram of an integrated apparatus for contact cracking of heavy oil and gasification of char provided in an embodiment of the present invention;

fig. 2 is a schematic diagram of an integrated apparatus for heavy oil contact cracking and coke gasification according to another embodiment of the present invention.

Description of reference numerals:

100-coupled reactor; 110-a cleavage section;

120-a gasification stage; 130-cooling washing section;

140-steam stripping section; 150-material dropping pipe;

200-a char-combusting regenerator; 300-gas-solid separator.

Detailed Description

In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

Example one

The embodiment provides a method for integrating heavy oil contact cracking and coke gasification, which is carried out by utilizing a coupling reactor and a coke-burning regenerator, wherein the coupling reactor is provided with a cracking section and a gasification section which are communicated with each other internally; the method comprises the following steps:

conveying the carbon deposit contact agent into a coke burning regenerator for partial coke burning treatment, conveying the carbon deposit contact agent into a gasification section at the lower part of the coupling reactor, and carrying out gasification reaction with a gasification agent to be regenerated to obtain a regeneration contact agent and synthesis gas; the regenerated contact agent returns to the cracking section for cyclic utilization, and the synthesis gas ascends to enter the cracking section;

Specifically, the heavy oil raw material may be heavy oil obtained by extracting crude oil, or may be a heavy oil product obtained in a processing process of an oil refinery, including one or more mixtures of heavy oils such as heavy oil, super heavy oil, oil sand bitumen, atmospheric heavy oil, vacuum residue oil, catalytic cracking slurry oil, solvent deoiled bitumen, or may also include one or more mixtures of heavy tar and residue oil obtained in a coal pyrolysis or liquefaction process, heavy oil produced by dry distillation of oil shale, and heavy oil derived from low-temperature pyrolysis liquid products in biomass.

In some examples of the invention, the heavy oil feedstock has a conradson carbon residue value of 8 wt% or greater, preferably not less than 10 wt%, and especially not less than 15 wt%.

Specifically, the contact agent may be a contact agent commonly used in the present heavy oil decarburization upgrading process, for example, selected from silica-alumina materials such as quartz sand, kaolin, clay, alumina, silica sol, montmorillonite and illite, and may also be selected from one or more of FCC industrial equilibrium agent/waste agent, red mud, steel slag, blast furnace ash and solid particles such as coal ash.

Preferably, a contact agent with relatively low cracking activity is selected, for example, a contact agent with a micro-reaction activity index of 5-30 is selected. In some examples of the present invention, the micro-reactivity index of the contact agent is 10-20, such as kaolin, clay, alumina, silica sol, industrial balancing agent or waste catalyst in the catalytic cracking process, etc.

Further, the contact agent is preferably in the form of microspheres, and the particle size is preferably in the range of 10 to 500 μm, and further more preferablyThe first step is 20 to 200 μm. In the practice of this example, the contact agent used has a particle size distribution of mainly 20 to 100 μm and a bulk density of 0.78 to 1.03 g/cm^-3The micro-inverse activity index is about 10-20.

It will be appreciated that in the cracking zone, the heavy oil feedstock is preferably in an atomized state and the contact agent is preferably in a fluidized state to ensure sufficient contact between the two and sufficient progress of the cracking reaction.

During the cracking reaction, the coke content on the surface of the contact agent is preferably maintained to be more than 10 percent by mass. In some embodiments of the invention, the reaction conditions within the cleavage section are: the reaction temperature is 450-700 ℃, the reaction pressure is 0.1-3.0 Mpa, the reaction time is 1-20 seconds, the weight ratio of the contact agent to the heavy oil (namely the agent-oil ratio) is 0.1-1.0, and the apparent gas velocity is 1-20 m/s. Preferably, the temperature of the cracking reaction is 480-580 ℃, the reaction pressure is 0.1-1.0 Mpa, such as normal pressure, the reaction time is 3-20 seconds, the agent-oil ratio is 0.2-0.6, and the apparent gas velocity is 1-20 m/s.

Furthermore, before the gas-solid separation, the light oil gas obtained from the cracking section and the synthesis gas merged from the bottom of the cracking section are preferably subjected to a temperature reduction treatment to reduce the temperature of the high-temperature oil gas and inhibit the reactions such as excessive cracking and coking. The light oil gas and the synthesis gas after temperature reduction treatment inevitably carry a small amount of carbon deposit contact agent particles, and the carbon deposit contact agent can be removed and collected in the subsequent gas-solid separation process and then returns to the cracking section to be used as a reaction bed material.

Furthermore, the carbon deposit contact agent in the cracking section is preferably subjected to steam stripping firstly before entering the coke burning regenerator so as to remove a small amount of light oil gas remained on the surface and in pores of the carbon deposit contact agent, thereby facilitating the subsequent regeneration. Specifically, when steam stripping is performed, the mass ratio of steam to the heavy oil raw material is generally controlled to be 0.03-0.3: 1, the temperature of the water vapor is 200-400 ℃, and the apparent gas velocity of the water vapor is 0.5-5.0 m/s.

Specifically, the coke contact agent from the cracking section is combusted in a char-combusting regenerator, effecting partial regeneration of the coke contact agent, otherwise known as semi-regeneration. Generally, oxygen-containing gas, such as air, oxygen-enriched air and the like, is introduced from the bottom of the coking regenerator, and the carbon deposit contact agent is conveyed into the coking regenerator, so that part of coke on the surface of the contact agent reacts with the oxygen to generate carbon monoxide and carbon dioxide, and a semi-regeneration contact agent with higher temperature and flue gas are obtained. Preferably, the temperature of the semi-regenerated contact agent reaches the temperature required by the gasification reaction, such as 800-1200 ℃, and then enters the gasification section; the obtained flue gas is discharged from the top of the coke-burning regenerator. Specifically, the reaction conditions within the char regenerator may be: the reaction temperature is 600-800 ℃, the pressure is 0.1-6.0 Mpa, the time is 20-200 s, and the gas velocity is 0.1-5.0 m/s.

In the gasification section, the semi-regeneration contact agent from the coke burning regenerator and the gasification agent are subjected to gasification reaction to obtain synthesis gas and realize the regeneration of the contact agent. Specifically, the semi-regeneration contact agent and a gasification agent introduced from the bottom of the gasification section can be subjected to gasification reaction at the temperature of 800-1200 ℃, the reaction pressure of 0.1-6.0 Mpa, the apparent gas velocity of 0.1-5 m/s and the retention time of the carbon deposition contact agent of 1-20 min, so as to obtain the regeneration contact agent and the synthesis gas.

In the present embodiment, the gasifying agent is not particularly limited, and may be, for example, steam, an oxygen-containing gas, or a mixed gas of steam and an oxygen-containing gas. Wherein the oxygen-containing gas may be, for example, air, oxygen-enriched air, oxygen, or the like.

Example two

As shown in fig. 1 and 2, the present embodiment provides an apparatus for heavy oil contact cracking and coke gasification integration, for implementing the method described in the first embodiment, the apparatus at least comprises a coupling reactor 100, a coke burning regenerator 200 and a gas-solid separator 300, wherein:

the coupling reactor 100 comprises an upper cracking section 110 and a lower gasification section 120, and the cracking section 110 and the gasification section 120 are communicated with each other; the cracking section 110 is provided with a heavy oil raw material inlet, a carbon deposit contact agent discharge port, an oil gas outlet, a regeneration contact agent return port and a synthesis gas inlet at the bottom; the gasification section 120 is provided with a gasification agent inlet, a semi-regeneration contact agent inlet, a regeneration contact agent outlet and a synthesis gas outlet at the top;

the coke burning regenerator 200 is provided with a carbon deposit contact agent inlet, an oxygen-containing gas inlet, a semi-regeneration contact agent discharge port and a flue gas discharge port;

the gas-solid separator 300 has an inlet, a solid discharge port, and a gas discharge port;

the accumulated carbon contact agent discharge port of the cracking section 110 is connected with the accumulated carbon contact agent inlet of the coke burning regenerator 200, the oil gas outlet of the cracking section 110 is connected with the inlet of the gas-solid separator 300, the semi-regeneration contact agent discharge port of the coke burning regenerator 200 is connected with the semi-regeneration contact agent inlet of the gasification section 120, and the regeneration contact agent discharge port of the gasification section 120 is connected with the regeneration contact agent return port of the cracking section 110; the syngas discharge of the gasification stage 120 is connected to the syngas inlet of the cracking stage 110.

Specifically, the coupling reactor 100 may be a cracking reactor and a gasification reactor commonly used in the art, which may be a fluidized bed reactor, for example, through appropriate modification and assembly. As shown in fig. 1 and fig. 2, the bottom of the cracking section 110 and the top of the gasification section 120 may be communicated with each other, for example, coaxially disposed, so that the syngas generated by the gasification section 120 may flow upward in the coupling reactor 100 to enter the cracking section 110, thereby reducing the transportation difficulty of the syngas and avoiding the energy loss of the syngas.

The char regenerator 200 may be a conventional char regeneration device used in the heavy oil processing field, and has an oxygen-containing gas inlet at the bottom, a flue gas discharge outlet at the top, a char contact agent inlet at the upper or middle part, and a semi-regeneration contact agent discharge outlet at the lower part.

With further reference to fig. 2, the char regenerator 200 and the coupling reactor 100 may be coaxially disposed; such as the char regenerator 200, is installed on top of the coupling reactor 100, which can further reduce the footprint of the overall plant. Of course, the specific installation position of the coke-burning regenerator 200 can be designed reasonably according to the actual production plant conditions, and the embodiment is not particularly limited.

Further, the aforementioned apparatus may further include an atomizer (not shown). The atomizer may be disposed in the coupling reactor 100, specifically, in the cracking section 110 and corresponding to the inlet of the heavy oil feedstock, so that after the preheated heavy oil feedstock enters the cracking section 110 through the inlet of the heavy oil feedstock, the atomizer atomizes the heavy oil feedstock first, and then the cracking reaction is performed. Alternatively, the atomizer may be disposed outside the coupling reactor 100 and connected to the cracking section 110 through the heavy oil feedstock inlet. After preheating the heavy oil feedstock, it is first atomized in an atomizer and then introduced into cracking section 110.

Referring further to fig. 1, the coupling reactor 100 may further include a temperature-reducing washing section 130. The reduced temperature washing stage 130 may be specifically disposed within the cracking stage 110 at an upper portion thereof.

Specifically, the cooling washing section 130 may adopt a structure of a washing section (or a desuperheating section) in a conventional coking fractionating tower or a catalytic fractionating tower at present, and generally eight or ten layers of herringbone baffles or tongue-shaped tower plates are used, so that upstream high-temperature oil gas and downstream low-temperature liquid are subjected to countercurrent contact in the cooling washing section 130 to exchange heat, so as to inhibit excessive cracking and coking, and remove a small amount of carbon deposit contact agent small particles carried in the high-temperature oil gas.

The low-temperature liquid may be, for example, a heavy oil raw material, and since the amount of the heavy oil raw material after heat exchange is not large and the heavy oil raw material is sufficiently dispersed in the heat exchange process with the high-temperature oil gas, the heavy oil raw material generally used as the low-temperature liquid can be directly subjected to cracking reaction in the cracking section 110 after heat exchange and temperature rise.

With further reference to FIG. 1, a steam stripping section 140 may also be provided in a lower portion of the cracking section 110. In particular, the steam stripping section 140 can include a multi-layer stripping structure that can be formed using a combination of one or more of chevron baffles, annular baffles, conical baffles, grated baffles, loose fill, or structured fill, among other stripping structures. The carbon deposit contact agent generated in the cracking section 110 descends and is subjected to steam stripping in the steam stripping section 140 to remove the light oil gas products remained on the surface or in the pores of the carbon deposit contact agent, thereby facilitating the regeneration.

In addition, by arranging the steam stripping section 140, the problems of coking and blockage of large-size contact agent particles can be avoided, and the cracking section 110 and the gasification section 120 are isolated to a certain extent, so that the cracking reaction and the gasification reaction can be carried out relatively independently, and the safety and the operation stability of the whole coupling reactor 100 are improved.

Correspondingly, the aforementioned apparatus may further comprise a steam supply device (not shown) for supplying steam at a suitable temperature and flow rate into the cracking section 110, thereby forming a steam stripping section 140 at a lower portion of the cracking section 110.

As shown in fig. 1 and 2, a material conveying device (not shown) may be provided between the cracking section 110 and the char regenerator 200 to enable the char contact agent discharged from the char contact agent discharge port of the cracking section 110 to enter the char regenerator 200 from the char contact agent inlet via the material conveying device; similarly, a material transport device may be provided between the char regenerator 200 and the gasification stage 120 to allow semi-regenerated contact agent discharged from the semi-regenerated contact agent discharge outlet of the char regenerator 200 to enter the gasification stage 120 through the semi-regenerated contact agent inlet by means of the material transport device. The material conveying device is preferably disposed outside the coupling reactor 100 to facilitate adjustment and control of the flow rate of the material.

Referring to fig. 1, a descending tube 150 may be further disposed in the cracking section 110, and the descending tube 150 may be generally installed at the top of the cracking section 110 and corresponds to the regenerated contact agent return port, so that the regenerated contact agent from the gasification section 120 enters the cracking section 110 through the regenerated contact agent return port, and then descends through the descending tube 150 to return to the reaction zone in the middle of the cracking section 110.

As previously described, a gasification reaction of the semi-regenerated char-forming contact agent occurs in the gasification stage 120 to yield a regenerated contact agent and syngas. Due to the high heavy metal content and high ash content of the inferior heavy oil, part of the contact agent is easy to be permanently inactivated in the heavy oil processing process. In addition, the higher metals and ash content of the heavy oil feedstock also tends to accumulate on the contact agent, forming ash components that are difficult to convert, and therefore an ash discharge port (not shown) is provided at the lower portion of the gasification stage 120. The discharged ash contains high heavy metal content, and heavy metals such as Ni, V and the like in the discharged ash can be recovered through a subsequent treatment device.

Further, the apparatus may further include a gasifying agent supply device (not shown). The gasifying agent supply device is connected to the gasifying section 120 and is used for supplying a gasifying agent, so that the gasifying agent is introduced into the gasifying section 120 from a gasifying agent inlet at the bottom.

In this embodiment, the gas-solid separator 300 may be a gas-solid separator commonly used in the petroleum processing field. In some examples of the invention, the gas-solid separator 300 used is a cyclone separator. In practical use, the light oil gas and the synthesis gas carrying the carbon deposit contact agent are introduced into the cyclone separator from the upper inlet, the carbon deposit contact agent is separated from the airflow of the light oil gas and the synthesis gas by utilizing the centrifugal force generated when the gas-solid mixture rotates at high speed and can be collected at the solid discharge port at the bottom of the cyclone separator, and the purified oil gas is discharged from the gas discharge port at the top of the cyclone separator and then is further processed and utilized.

As shown in fig. 1, the gas-solid separator 300 may be disposed in the coupling reactor 100, and particularly may be disposed on the upper portion of the cracking section 110, especially above the cooling washing section 130, so that the purification and separation of high-temperature oil gas occurs in the coupling reactor 100, which is not easy to generate a large amount of heat to dissipate, thereby ensuring that the temperature of the oil gas components in the gas-solid separator 300 does not decrease, and avoiding the problems of condensation, coking and the like affecting the operation. Of course, the gas-solid separator 300 may be disposed outside the coupling reactor 100, and the heat preservation may be achieved by disposing an inner liner and/or an outer heat preservation layer, so as to avoid the temperature of the high-temperature oil gas from being significantly reduced.

In order to illustrate the practical effects of the present invention, the following embodiments will be further described with reference to specific application examples:

application example 1

As shown in fig. 1, the low-quality heavy oil feedstock is preheated and then atomized through the heavy oil feedstock inlet into the cracking section 110 of the coupling reactor 100, and the atomized heavy oil droplets contact with the fluidized contact agent to undergo a cracking reaction to obtain light oil gas and coke. The coke is attached to the surface of the contact agent, namely the carbon deposit contact agent.

The carbon deposit contact agent falls under the action of gravity and passes through the steam stripping section 140 to remove the residual light oil gas product on the surface of the carbon deposit contact agent, wherein the steam supply device introduces necessary steam into the cracking section 110, and then the carbon deposit contact agent is discharged from the carbon deposit contact agent discharge port at the lower part of the cracking section 110 and enters the coke burning regenerator 200.

The carbon deposit contact agent is partially burnt in the burning regenerator 200, and after the temperature is raised to a temperature suitable for the gasification reaction, the obtained semi-regeneration contact agent is discharged from a semi-regeneration contact agent discharge port at the lower part of the burning regenerator 200 and enters the gasification section 120 from a semi-regeneration contact agent inlet for the gasification reaction.

In the gasification section 120, the semi-regenerated contact agent and the gasifying agent such as steam, oxygen/air and the like introduced from the gasifying agent inlet at the bottom of the gasification section 120 through the gasifying agent supply device are subjected to high-temperature gasification reaction to obtain high-quality synthetic gas, and the regeneration of the contact agent is realized.

The regenerated contact agent travels up the exterior of the coupled reactor 100 into the cracking section 110, providing the heat and catalytic activity required for the heavy oil cracking reaction. The synthesis gas ascends to enter the cracking section 110, and the synthesis gas is rich in hydrogen, CO and other active small molecules, so that the yield and the quality of the light oil gas can be improved to a certain degree, the yield of coke is reduced, and the product distribution of heavy oil cracking is improved. In addition, the heat required by the heavy oil cracking reaction can be provided, and the sufficient fluidization of the contact agent is ensured.

The gas flow of the ascending synthesis gas and the amount of the regeneration contact agent carried by the ascending synthesis gas can regulate and control the gas velocity in the bed through modes of gasifying agent type, flow, reactor size and the like, so that the matching of the material flow and the energy flow of the coupling reactor 100 is ensured, and the stable operation of a process system is ensured.

The synthesis gas and the light oil gas go upward and are cooled in the cooling washing section 130, so that the occurrence of reactions such as excessive cracking, coking and the like is inhibited, and meanwhile, part of carbon deposit contact agent fine powder in the synthesis gas and the light oil gas is removed. The light oil gas and the synthesis gas passing through the cooling washing section 130 then enter a gas-solid separator 200, such as a cyclone separator, for gas-solid separation, and carbon deposit contact agent particles entrained therein are removed. The small amount of collected carbon deposit contact agent fine particles can be returned to the cracking section 110 to be used as reaction bed materials, so that 100 carbon deposit contact agent particle circulation of the cracking section is formed, and partial heat required by the cracking process and a gas-solid catalytic cracking reaction site are provided.

The oil gas components purified by the gas-solid separator 300 pass through a gas-liquid fractionating tower, an oil gas absorption stabilizing tower and other systems to respectively obtain gas products such as dry gas, liquefied gas and the like and oil products at the bottom of the tower. Of course, the oil product can be further cut and separated to obtain liquid products with different distillation range components, wherein the heavy oil at the bottom of the tower can be mixed with the heavy oil raw material for recycling processing.

In the embodiment of the application, the cracking section 110 and the gasification section 120 are effectively isolated through the steam stripping section 140, so that the cracking reaction of the heavy oil raw material and the gasification reaction of the carbon deposit contact agent can be kept independent to a certain extent, and the safety and the operation stability of the whole heavy oil processing device are improved; in addition, the arrangement of the steam stripping section 140 can also improve the oil gas yield, and effectively solves the problems of coking, blockage and the like of large-size coke particles.

The process flow of the application example 1 is used for processing domestic vacuum residue of a certain refinery, and the properties of the raw oil are shown in Table 1.

As can be seen from Table 1, the feedstock oil has high density, high carbon residue value, and high asphaltene content, and contains high sulfur, nitrogen, and heavy metal components. The coke formation tendency is serious by adopting the traditional catalytic cracking process, and the rapid carbon deposition inactivation or heavy metal poisoning inactivation of the catalyst is easily caused.

TABLE 1

Item	Data of
		Density (20 ℃), kg m^-3	993.8
Viscosity (80 ℃ C.), mm²·s^-1	5357.85
		Kang's carbon residue, wt.%	17.82
Group composition, wt%
		Saturated hydrocarbons	21.13
Aromatic hydrocarbons	35.33
		Glue	37.51
Asphaltenes	6.03
		Sulfur, wt.%	1.10
Nitrogen, wt%	1.03
		Ni，μg·g^-1	79.4
V，μg·g^-1	88.1

In the process, a self-made decarbonization modification contact agent with certain micro-reverse activity is adopted, and a cheap kaolin material is adopted for modification to obtain a macroporous structure with a high proportion, a large specific surface area and low acidity. The particle size distribution range of the contact agent is mainly 20 to 100 μm, and the bulk density is 0.78 to 1.03 g/cm^-3Abrasion index<1 wt%, and a microreflective index of about 20.

The cracking reaction conditions are as follows: the reaction temperature is 491 ℃, the pressure is 0.1Mpa, the mass ratio of the catalyst to the oil is 0.4, the reaction time is about 20 seconds, and the apparent gas velocity is about 3.5 m/s.

The gasification reaction conditions are as follows: the gasifying agent is water vapor and oxygen according to the volume ratio of 1: 1, the reaction temperature is 820 ℃, the reaction pressure is 0.1Mpa, the apparent gas velocity is about 0.6m/s, and the retention time of the carbon deposition contact agent is about 15 min.

The steam stripping conditions were: the mass ratio of the steam to the heavy oil raw material was 0.20, the temperature of the steam was 350 ℃, and the superficial gas velocity of the stripping steam was 2.5 m/s.

The reaction conditions in the char regenerator 200 are: the reaction scorching temperature is 670 ℃, the scorching pressure is 0.1Mpa, the scorching time is 140s, and the gas velocity is 1.5 m/s.

The light oil gas obtained by the cracking reaction and the synthesis gas from the gasification section are purified by gas-solid separation to obtain the final oil gas product, and the product distribution is shown in table 2. Table 3 gives the composition of the synthesis gas obtained by carrying out the gasification reaction under the above conditions.

TABLE 2

Product distribution, wt%	Numerical value
		Dry gas	2.04
Liquefied gas	2.44
		Gasoline (gasoline)	13.95
Diesel oil	19.84
		Wax oil	31.85
＞500℃	14.21
		C₃～500℃	68.08
C₅～500℃	70.04
		Total liquid yield	79.85
Coke	15.67

As can be seen from table 2, compared with the initial carbon residue value of the raw material, the ratio of the coke yield to the carbon residue is about 0.8 to 0.9, which is much smaller than the ratio of coke/carbon residue 1.4 to 1.6 in the delayed coking, which indicates that the economic index of the device of the present embodiment is much higher than that of the heavy oil processing device in the prior art; the total liquid yield is close to 80 percent, and most of the total liquid yield is light oil fraction of less than 500 ℃, which shows that the process of the embodiment can realize the lightening of heavy oil and obtain a large amount of oil products with higher added value and has very high processing efficiency; in addition, heavy oil components greater than 500 ℃ can be further processed by means of recycling.

TABLE 3

Synthesis gas Components	H₂	CO	CO₂	CH₄Etc. other components
					Volume content (vol%)	42.7	35.6	20.1	1.6

As can be seen from Table 3, in the synthesis gas obtained by gasifying coke, H is₂The sum of the volume fraction of the CO and the CO is close to 80 percent, and the high-quality synthetic gas can be used for subsequent hydrogen production by reforming to supplement a refinery hydrogen source.

Application example 2

As an alternative to application example 1, the specific process of this application example is substantially the same as application example 1 except that the char-combusting regenerator 200 is installed at the top of the coupling reactor 100, coaxially with the cracking section 110 and the gasifying section 120.

Processing the inferior heavy oil processing raw material completely consistent with the application example 1 by adopting the process conditions completely consistent with the application example 1, wherein the distribution of the obtained product and the composition of the synthesis gas are basically consistent with the application example 1, the total liquid yield is about 80 percent, and the majority of the obtained product is light oil fraction of less than 500 ℃; the ratio of the coke yield to the carbon residue is about 0.8-0.9.

Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A method for integrating heavy oil contact cracking and coke gasification is characterized in that the method is carried out by utilizing a coupling reactor and a coke burning regenerator, wherein the coupling reactor is provided with a cracking section and a gasification section which are communicated with each other internally; a steam stripping section is arranged at the lower part in the cracking section, and a cooling washing section is arranged at the upper part in the cracking section; the method comprises the following steps:

introducing a heavy oil raw material into the cracking section at the upper part of the coupling reactor, and contacting with a contact agent to crack to obtain light oil gas and a carbon deposit contact agent;

the carbon deposit contact agent descends in a cracking section, is subjected to steam stripping in a steam stripping section, is conveyed to a coke burning regenerator for partial coke burning treatment, is conveyed to a gasification section at the lower part of the coupling reactor, and is subjected to gasification reaction with a gasification agent to be regenerated, so that a regenerated contact agent and synthesis gas are obtained; the regenerated contact agent returns to the cracking section for cyclic utilization, and the synthesis gas ascends to enter the cracking section;

and the light oil gas and the synthesis gas merged in the upward flow go upward, are subjected to temperature reduction treatment through a temperature reduction washing section, are discharged out of a cracking section, and are subjected to gas-solid separation to obtain purified oil gas.

2. The method according to claim 1, wherein the particle size distribution of the contact agent is 10 to 500 μm; and/or the micro-inverse activity index of the contact agent is 5-30.

3. The method of claim 1 wherein the coke mass content of the coke-depositing contact agent is above 10%.

4. The method according to claim 1 or 3, wherein the reaction temperature in the cracking section is 450-700 ℃, the reaction pressure is 0.1-3.0 MPa, the reaction time is 1-20 seconds, the apparent gas velocity is 1-20 m/s, and the weight ratio of the contact agent to the heavy oil raw material is 0.1-1.0: 1.

5. the method according to claim 1 or 3, wherein the reaction temperature in the gasification section is 800-1200 ℃, the reaction pressure is 0.1-6.0 Mpa, the apparent gas velocity is 0.1-5 m/s, and the residence time of the carbon deposit contact agent is 1-20 min; the gasifying agent is water vapor and/or oxygen-containing gas.

6. The method of claim 1, wherein the char-forming contact agent is transported to a char-burning regenerator for partial char-burning treatment to bring the temperature of the resulting semi-regenerated contact agent to a temperature required for the gasification reaction, and then the semi-regenerated contact agent is transported to a gasification zone for the gasification reaction.

7. The method of claim 5, wherein the deposited carbon contact agent is transported into a coke burning regenerator for partial coke burning treatment, so that the temperature of the obtained semi-regeneration contact agent reaches the temperature required by the gasification reaction, and then the semi-regeneration contact agent is transported into a gasification section for the gasification reaction.

8. The method according to claim 1, wherein the steam stripping is performed while controlling the mass ratio of steam to the heavy oil feedstock to be 0.03 to 0.3: 1, the temperature of the water vapor is 200-400 ℃, and the apparent gas velocity of the water vapor is 0.5-5.0 m/s.

9. An apparatus for the integrated catalytic cracking of heavy oil and gasification of coke for carrying out the process according to any one of claims 1 to 8, characterized in that it comprises at least a coupling reactor, a coke-burning regenerator and a gas-solid separator, wherein:

the coupling reactor is provided with an upper cracking section and a lower gasification section, the cracking section and the gasification section are communicated with each other, and the cracking section is provided with a heavy oil raw material inlet, a carbon deposit contact agent outlet, an oil gas outlet, a regeneration contact agent return port and a synthesis gas inlet at the bottom; the gasification section is provided with a gasification agent inlet, a semi-regeneration contact agent inlet, a regeneration contact agent outlet and a synthesis gas outlet at the top;

the gas-solid separator has an inlet, a solids discharge outlet, and a gas discharge outlet;

the accumulated carbon contact agent discharge port of the cracking section is connected with the accumulated carbon contact agent inlet of the coke burning regenerator, the oil gas outlet of the cracking section is connected with the inlet of the gas-solid separator, the semi-regeneration contact agent discharge port of the coke burning regenerator is connected with the semi-regeneration contact agent inlet of the gasification section, and the regeneration contact agent discharge port of the gasification section is connected with the regeneration contact agent return port of the cracking section; the synthesis gas outlet of the gasification section is connected with the synthesis gas inlet of the cracking section; the lower part in the cracking section is provided with a steam stripping section, and the upper part in the cracking section is provided with a cooling washing section.