CN112538371A - Heavy oil lightening coupling reaction device - Google Patents
Heavy oil lightening coupling reaction device Download PDFInfo
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- CN112538371A CN112538371A CN201910900586.XA CN201910900586A CN112538371A CN 112538371 A CN112538371 A CN 112538371A CN 201910900586 A CN201910900586 A CN 201910900586A CN 112538371 A CN112538371 A CN 112538371A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
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Abstract
The invention provides a heavy oil lightening coupling reaction device, which comprises a reactor and a synthesis gas-solid separator; the reactor comprises a cracking section and a gasification section which are communicated with each other through a material pipeline; the input end of the material pipeline is communicated with the bottom of the gasification section, and the output end of the material pipeline is communicated with the top of the cracking section; the cracking section is provided with a heavy oil raw material inlet, a solid particle outlet, a synthesis gas inlet and an oil gas outlet; the gasification section is provided with a gasification agent inlet, a solid particle inlet and a synthesis gas outlet; the synthesis gas outlet is communicated with the inlet of the synthesis gas-solid separator, and the gas phase outlet of the synthesis gas-solid separator is communicated with the synthesis gas inlet through an external synthesis gas conveying pipeline; the solid particle outlet is communicated with the solid particle inlet through an external riser. The device can realize the cooperation of two reaction processes of heavy oil cracking and gasification to obtain high-yield high-quality oil gas and synthetic gas, reduced the energy consumption of cracking reaction.
Description
Technical Field
The invention relates to a heavy oil lightening coupling reaction device, and belongs to the technical field of petroleum processing.
Background
With the heavy and inferior crude oil, the yield of inferior heavy oil (heavy oil, super heavy oil, oil sand asphalt, vacuum residue oil, oil slurry, deoiled asphalt, etc.) is increased dramatically. The inferior heavy oil generally has the characteristics of low H/C ratio, high contents of sulfur, nitrogen and heavy metals, large carbon residue value and the like, and the coking tendency of the heavy oil in the processing process is serious due to the carbon residue and asphaltene components enriched inside. Due to the problems of catalyst deactivation, high hydrogen consumption, long-period operation and the like, the direct processing and treatment requirements of a large amount of inferior heavy oil are difficult to meet by directly adopting means such as catalytic cracking or catalytic hydrogenation. The inferior heavy oil is processed by adopting the coupling mode of technologies such as solvent deasphalting, visbreaking, catalytic cracking, hydrotreating and delayed coking, and the like, and compared with a one-step heavy oil processing technology, the method has the advantages of longer overall process flow and higher investment cost.
The delayed coking process is used as an inferior heavy oil processing technology widely applied at present, and has the problems of furnace tube coking, large environmental protection pressure in a decoking process, low liquid yield and the like. In addition, a large amount of solid coke is produced as a byproduct in the delayed coking process, particularly high-sulfur coke has low value, and the latest environment-friendly requirement is to take factory-limiting measures on the high-sulfur coke with the sulfur content of more than 3%. In some domestic refineries, petroleum coke generated by delayed coking is used for a circulating fluidized bed combustion power generation or gasification poly-generation process, so that the conversion and utilization of coke are realized. Heavy oil is firstly converted into low-activity petroleum coke, and then the petroleum coke is converted by cooling, grinding and reheating, but the overall process flow is complex and the efficiency is low.
In addition, because the poor heavy oil raw material has a low H/C atomic ratio, the light oil product can be produced to the maximum extent only through the hydrogenation process, and the quality requirement of clean oil products is met, so that the problem of hydrogen source shortage in the process of processing the poor heavy oil in a refinery is more prominent, and hydrogen generated in the technical processes of catalytic reforming and the like is not enough to meet the hydrogen requirement of clean oil product production. Although the direct gasification of inferior heavy oil can directly convert heavy oil into small molecules such as synthesis gas, the oil gas molecules and hydrogen elements existing in the heavy oil are not fully utilized, and the resource waste of the heavy oil is also caused to a certain extent.
In response to the above problems, many researchers have proposed a corresponding short-flow technical solution for conversion of inferior heavy oil processing. One of the processes developed by Exxon is the flexicoking series using fluidized coke powder as the bed material for heavy oil cracking reaction.
The flexible coking process takes coke powder as a heat carrier for heavy oil cracking reaction, the generated coke is attached to the surface of the coke powder and is conveyed to a gasification/combustion reactor for removal, so that the coke material in the reaction needs to be recycled among reactors such as coking, combustion and gasification, the difficulty in recycling the coke powder material among a plurality of reactors is caused, direct material flow or heat exchange between coke gasification and heavy oil coking reaction is difficult to realize, and the energy consumption of the cracking reaction is increased.
Disclosure of Invention
The invention provides a heavy oil lightening coupling reaction device which can realize the cooperation of heavy oil cracking and gasification reaction processes, thereby obtaining high-yield and high-quality oil gas and synthesis gas and reducing the energy consumption of cracking reaction.
The invention provides a heavy oil lightening coupling reaction device, which comprises a reactor and a synthesis gas-solid separator;
the reactor comprises a cracking section and a gasification section which are communicated with each other through a material pipeline;
the input end of the material pipeline is communicated with the bottom of the gasification section, the output end of the material pipeline is communicated with the top of the cracking section, and the output end of the material pipeline is provided with a one-way plug valve;
the cracking section is provided with a heavy oil raw material inlet, a solid particle outlet and a synthesis gas inlet, and the upper part of the cracking section is provided with an oil gas outlet;
the gasification section is provided with a gasification agent inlet, a solid particle inlet and a synthesis gas outlet;
the synthesis gas outlet is communicated with the inlet of the synthesis gas-solid separator, and the gas phase outlet of the synthesis gas-solid separator is communicated with the synthesis gas inlet through an external synthesis gas conveying pipeline;
the solid particle outlet is communicated with the solid particle inlet through an external riser.
The coupled reaction device, wherein the reactor interior further comprises a steam stripping section and a grain size refining section which are communicated with each other;
the steam stripping section and the particle size refining section are arranged at the lower part of the cracking section, and the top of the steam stripping section is communicated with the bottom of the cracking section;
the steam stripping section is positioned at the upper part of the grain size refining section;
the steam stripping section is provided with a stripping steam inlet, and the grain size refining section is provided with a grinding steam inlet.
The coupling reaction device comprises a reactor, wherein the reactor further comprises a cooling washing section, and the cooling washing section is located between the cracking section and the gasification section and used for cooling and washing the light oil gas in the cracking section.
The coupling reaction device as described above, wherein the reactor further includes an atomizing unit inside, and the atomizing unit is communicated with the heavy oil feedstock inlet and is used for performing an atomizing treatment on the heavy oil feedstock.
The coupling reaction device further comprises an oil-gas-solid separator outside the reactor, wherein an inlet of the oil-gas-solid separator is communicated with the oil-gas outlet, and a solid phase outlet of the oil-gas-solid separator is communicated with the cracking section.
The coupled reaction device as described above, wherein the cracking section is a cracking reactor, and the gasification section is a gasification reactor.
The coupling reaction device as described above, wherein the cracking reactor and the gasification reactor are coaxially communicated through the material pipeline.
The coupled reaction apparatus as described above, wherein the gasification reactor has a diameter greater than a diameter of the cracking reactor.
The coupled reaction device as described above, wherein the ratio of the diameter of the cracking reactor to the diameter of the gasification reactor is 1: (1.5-4).
The coupling reaction device as described above, wherein the operating pressure inside the coupling reaction device is 0.1-6 Mpa.
The implementation of the invention has at least the following advantages:
1) according to the heavy oil lightening coupling reaction device, the cracking section is coupled with the gasification section through the material conveying pipeline inside the reactor, the external lifting pipe and the external synthesis gas conveying pipeline, compared with processes such as flexible coking, the problems that materials are difficult to operate circularly among a plurality of reactors, the process is complex, the occupied area is large, the investment is high and the like are solved, and the technical economy of the method is improved.
2) The heavy oil lightening coupling reaction device fully plays a synergistic role in reactions such as heavy oil cracking, coke gasification and the like. On one hand, the cracked green coke is used as a reaction raw material of the gasification section and reacts in the gasification section to generate high-quality synthesis gas, so that a large amount of low-value petroleum coke is avoided, and the hydrogen source of a refinery is enriched; on the other hand, the synthesis gas in the gasification section can provide heat for the cracking reaction, and can be used as the hydrogen atmosphere of the heavy oil cracking reaction to improve the quality of the light oil gas. Through the processes, the technical advantages of mutual material supply, energy complementation, synergistic reaction, oil-gas co-production and the like among the reactions are realized.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of a heavy oil lightening coupling reaction apparatus according to the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages 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 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.
Fig. 1 is a schematic structural diagram of an embodiment of a heavy oil upgrading coupled reaction apparatus according to the present invention, which includes a reactor and a syngas-gas-solid separator 100; the reactor comprises a cracking section 1 and a gasification section 2 which are communicated with each other through a material pipeline a; the input end of the material pipeline 1 is communicated with the bottom of the gasification section 2, the output end of the material pipeline a is communicated with the top of the cracking section 1, and the output end of the material pipeline a is provided with a one-way plug valve b; the cracking section 1 is provided with a heavy oil raw material inlet, a solid particle outlet and a synthesis gas inlet, and the upper part of the cracking section is provided with an oil gas outlet; the gasification section 2 is provided with a gasification agent inlet, a solid particle inlet and a synthesis gas outlet; the synthesis gas outlet is communicated with the inlet of the synthesis gas-solid separator 100, and the gas phase outlet of the synthesis gas-solid separator 100 is communicated with the synthesis gas inlet through an external synthesis gas conveying pipeline c; the solid particle outlet is communicated with the solid particle inlet through an external riser d.
Cracking section 1 is used to provide a location for cracking a heavy oil feedstock. The cracking section 1 is filled with cracking carriers such as coke powder, so that the heavy oil feedstock entering the cracking section 1 through the heavy oil feedstock inlet contacts with fluidized coke powder under the action of fluidized gas to perform cracking reaction to generate light oil gas and coke particles, wherein the coke particles refer to particles formed by attaching coke in the heavy oil feedstock to the surface of the coke powder.
The coke particles descend from the cracking section 1 and are output from the reactor through a solid particle outlet to enter an external riser d, wherein the lower part of the external riser d is provided with a lifting gas inlet, so that the coke particles can ascend in the external riser d under the action of lifting gas and finally enter the gasification section 2 through a solid particle inlet.
The gasification section 2 receives the coke particles from the pyrolysis section 1 through an external riser d, and the coke particles are subjected to gasification reaction under the action of a gasification agent entering the gasification section 2 through a gasification agent inlet to generate synthesis gas, wherein the gasification agent not only can participate in the gasification reaction, but also can be used as fluidizing gas of the coke particles in the gasification section 2. With the continuous generation of the synthesis gas, the synthesis gas is output from the synthesis gas outlet of the reactor and enters the synthesis gas-solid separator 100 to carry out gas-solid separation, so that part of coke particles which are carried in the synthesis gas and do not undergo gasification reaction are removed, the removed coke particles can be output from the solid phase outlet of the synthesis gas-solid separator 100 to enter the cracking section 1 to participate in the cracking reaction again, the purified synthesis gas is output from the gas phase outlet of the synthesis gas-solid separator 100, part of the purified synthesis gas a1 enters the cracking section 1 through an external synthesis gas conveying pipeline c, and the rest of the purified synthesis gas a2 can be collected for later use. The ash in the gasification section 2 can be discharged out of the reactor through an ash discharge port, the discharged ash also comprises ash and a small amount of products such as un-gasified carbon, and the useful components in the discharged ash can be recovered after being treated or can be used as reaction bed materials again.
In addition, the coke particles which are not completely reacted in the gasification section 2 can also enter a material flow conveying pipeline a, and after the coke particles in the material flow conveying pipeline a reach a certain quality, a one-way plug valve b at the bottom end of the material flow conveying pipeline a can be opened, so that the coke particles in the material flow conveying pipeline a can enter the cracking section 1 to participate in the cracking reaction again in a descending mode, and after the coke particles in the material flow conveying pipeline a enter the cracking section 1 in a descending mode, the one-way plug valve b is automatically closed until the coke particles in the material flow conveying pipeline a at the next time reach a certain quality and then are opened again. In particular, the one-way plug valve b may be a flap valve.
The light oil gas generated in the cracking section 1 and the purified synthesis gas a2 from the gasification section 2 are output through an oil gas outlet of the cracking section 1, and the output light oil gas and the purified synthesis gas further pass through a gas-liquid fractionating tower, an oil gas absorption stabilizing tower and other systems to respectively obtain synthesis gas products, dry gas, liquefied gas and other gas products and light oil products. Of course, the resulting oil can be further cut and separated to obtain liquid products of different boiling range components, wherein the heavy oil (possibly including a portion of the contact agent solid particles) can be mixed with the heavy oil feedstock for recycling processing. The cracking section 1 may also include a carrier replenishment inlet for replenishing coke powder therein.
The coupling reaction device disclosed by the invention couples and communicates the cracking section 1 and the gasification section 2 through the internal material flow conveying pipeline a, the external lifting pipe d and the synthesis gas output pipeline c, so that not only is the coke particles in the cracking section 1 favorably fed into the gasification section 2 for gasification reaction, but also the synthesis gas generated in the gasification section 2 can be fed into the cracking section 1 to participate in the cracking reaction, on one hand, the synthesis gas carrying heat can provide the heat required by the cracking reaction, the heat of the cracking section 1 and the gasification section 2 is matched and utilized, the overall energy efficiency is improved, on the other hand, the hydrogen in the synthesis gas can inhibit the coking reaction of the heavy oil cracking reaction to a certain extent, the product distribution of heavy oil cracking is improved, the quality and the yield of light oil gas are improved, and the synthesis gas can also enable the coke particles in the cracking section 1 to be fully fluidized. In addition, inside commodity circulation pipeline a can also make the coke granule of incomplete reaction in the gasification section 2 down to pyrolysis section 1, not only provides the reaction bed material for pyrolysis section 1, and the heat that the coke granule carried also can the pyrolysis reaction provide the required heat of pyrolysis reaction, has further reduced the reaction energy consumption. In the coupling reaction device of the present invention, the cracking section 1 may use a cracking reactor, the gasification section 2 may use a gasification reactor, and in order to ensure smooth circulation of the material flow, the cracking reactor and the gasification reactor may be coaxially communicated through an internal transfer line a. Further, both the cracking reactor and the gasification reactor include fluidized bed reactors.
To reduce the operating gas velocity in the gasification reactor, increase the residence time of the coke particles in the gasification reactor and the bed density, the diameter of the cracking reactor can be made larger than the diameter of the gasification reactor.
In one embodiment, the ratio of the diameter of the cracking reactor to the gasification reactor is 1: (1.5-4), further, the ratio of the diameter of the cracking reactor to the gasification reactor may be made to be 1: (2-3).
In order to ensure the processing capacity of the coupling reaction device to heavy oil and strengthen the assisting effect of synthesis gas to cracking reaction, the internal operating pressure of the coupling reaction device can be 0.1-6MPa, and further 2-4 MPa.
In addition, in order to ensure that the heavy oil raw material is fully contacted with the fluidized coke powder in the cracking section 1, an atomization unit 3 can be arranged at a position corresponding to an inlet of the heavy oil raw material in the cracking section 1, so that the heavy oil raw material can be atomized, and the atomized heavy oil raw material is contacted with the fluidized coke powder under the lifting action of the fluidized gas and is subjected to cracking reaction.
The atomizing unit 3 may include a raw material input pipe and a plurality of atomizing nozzles 31 disposed on the raw material input pipe, an input port of the raw material input pipe is communicated with the heavy oil raw material inlet and is disposed in a single-layer or multi-layer ring shape, the nozzles 31 are designed in a radial opposition manner or a tangential rotational flow manner, and the selection criteria of the specific nozzles 31 are based on the criteria of enhancing the heavy oil raw material atomization and the gas-solid contact effect.
Further, a steam stripping section 4 and a particle size refining section 5 which are communicated with each other may be provided inside the reactor.
The steam stripping section 4 and the particle size refining section 5 are arranged at the lower part of the cracking section 1, and the top of the steam stripping section 4 is communicated with the bottom of the cracking section 1.
During the downward movement of the coke particles in the cracking section 1, steam stripping treatment is firstly carried out in the steam stripping section 4, so that light oil gas carried on the surfaces of the coke particles is removed. Subsequently, the coke particles passing through the steam stripping section 4 pass through the size reduction section 5. The grain diameter thinning section 5 can crush and screen coke grains to prevent the coke grains from agglomerating and growing to be difficult to generate gasification reaction. Specifically, the crushing and screening of the coke particles can be carried out by the action of high-speed grinding water vapor. After coke particles from the cracking section 1 are sequentially treated by the steam stripping section 4 and the particle size refining section 5, the coke particles enter the external riser d through the solid particle outlet and enter the gasification section 2 through the solid particle inlet to perform gasification reaction.
It will be appreciated that it is desirable to provide a stripping steam inlet in the steam stripping section 4 and a milling steam inlet in the size reduction section 5.
The steam stripping section 4 and the particle size refining section 5 are arranged in the reactor, so that coke particles can be effectively prevented from agglomerating, and the safety and the operation stability of deep lightening of the heavy oil raw material are improved.
In particular implementations, the steam stripping section 4 may include a multi-layer stripping configuration to remove light oil and gas from the surface of the coke particles by the action of stripping steam entering through a stripping steam inlet. In detail, the multi-layer stripping structure can adopt one or more combinations of herringbone baffles, annular baffles, conical baffles, grid baffles, bulk packing or structured packing and the like.
The particle size refining section 5 can comprise structures of herringbone baffles, annular baffles, conical baffles and the like which are staggered in a labyrinth manner, so that steam entering through a grinding steam inlet collides coke particles treated by a steam stripping section 4 to realize crushing and screening, and the coke particles entering a gasification section 2 can have a larger contact area with a gasification agent, so that the gasification reaction is carried out efficiently.
In order to inhibit the light oil gas in the cracking section 1 from continuously producing coke in a high-temperature state, a cooling washing section 6 can be arranged between the cracking section 1 and the gasification section 2. The cooling washing section 6 can receive the mixture flow of the light oil gas and the purified synthesis gas a1 in the cracking section 1, and further carry out further cooling washing treatment on the mixture flow to enable the mixture flow to become a low-temperature mixture flow, and then the mixture flow is discharged out of the reactor through an oil gas outlet. Wherein, the temperature-reducing washing treatment refers to contacting the mixture flow with a low-temperature liquid (such as washing oil) entering the temperature-reducing washing section 6, so as to reduce the temperature of the mixture flow and remove part of solid particles with finer particle sizes possibly carried in the mixture flow.
Specifically, the cooling washing section 6 may adopt a built-in packing structure to enhance the contact between the mixture flow and the cryogenic liquid, or adopt a tower plate structure to enhance the contact between the mixture flow and the cryogenic liquid.
The built-in packing structure can comprise loose packing such as Raschig rings, pall rings, step rings, arc saddle packing, intalox saddle packing, metal ring intalox saddle, spherical packing and the like, or a combination of more than one of regular packing such as grid packing, corrugated packing, pulse packing and the like.
The tower plate structure comprises one or more of bubble cap tower plate, sieve pore tower plate, floating valve tower plate, jet tower plate and flow-through tower plate.
In a specific implementation, the wash oil may be heavy oil feedstock a 2. Specifically, the heavy oil raw material can enter the cracking section 1 in two paths, one path of the heavy oil raw material a1 directly contacts coke powder through a heavy oil raw material inlet to perform cracking reaction, the other path of the heavy oil raw material a2 is used as washing oil and firstly enters the cooling washing section 6 to exchange heat, then carries heat to descend, outputs the heat to the reactor and then enters the cracking section 11 through the heavy oil raw material inlet to perform cracking reaction, and therefore energy consumption required by cracking reaction is effectively reduced. In the present invention, the heavy oil feedstock a2 as the wash oil is 5 to 10% by mass of the total heavy oil feedstock.
Further, the reactor can also comprise an oil gas-gas solid separator 200 outside, wherein the inlet of the oil gas-gas solid separator 200 is communicated with the oil gas outlet and is used for carrying out gas-solid separation treatment on the low-temperature mixture flow.
The cracking section 1 is provided with light oil gas generated by cracking reaction of heavy oil raw materials and purified synthesis gas a1 entering through an external synthesis gas conveying pipeline c, after the temperature reduction washing treatment of the mixture flow of the light oil gas and the purified synthesis gas a1 is completed, the low-temperature mixture flow can be output out of the reactor through an oil gas outlet and enter the oil gas-solid separator 200 through an inlet of the oil gas-solid separator 200 for gas-solid separation, on one hand, solid particles (such as coke powder and coke particles) carried in the low-temperature mixture flow can be removed, so that the removed solid particles fall back to the cracking section 1 to continue to serve as a cracking carrier, on the other hand, the low-temperature mixture flow can be cooled again, further, the low-temperature mixture flow is prevented from continuing to generate coke in a high-temperature state, and the quality of the light oil gas.
After the low-temperature mixture flow enters the oil-gas-solid separator 200, the separated solid particles are output from the solid phase outlet of the oil-gas-solid separator 200 and return to the cracking section 1, and the purified mixture flow after the solid removal can be directly subjected to the next flow such as fractionation after being output from the gas phase outlet of the oil-gas-solid separator 200.
The oil gas-gas solid separator 200 may include an oil gas fast extraction device and a connection device thereof, and a gas-solid separation device, wherein the gas-solid separation device includes one or more combinations of axial flow or cyclone centrifugal separators commonly used in the art, and when the gas-solid separation device is a combination of a plurality of separators, the invention does not limit the specific connection relationship thereof, and the oil gas-gas solid separator may be connected in series or in parallel.
Hereinafter, the actual effect of treating the heavy oil feedstock will be described in detail by using the heavy oil lightening coupled reactor shown in fig. 1.
Inside this heavy oil weight coupling reaction unit's reactor, include from top to bottom:
the gasification section 1 is provided with a gasification agent inlet, a synthesis gas outlet, a solid particle inlet and an ash residue outlet;
specifically, the gasification section 1 is a gasification reactor and further comprises a fluidized bed reactor, and under the action of a gasification agent entering the gasification reactor through a gasification agent inlet, coke particles are in a fluidized state and contact with the gasification agent to carry out gasification reaction;
the cooling washing section 6 is used for receiving the mixed material flow of the light oil gas and the purified synthesis gas a1 in the cracking section 1, cooling and washing the mixed material flow, and outputting the low-temperature mixed material flow generated by cooling and washing to the reactor from an oil gas outlet;
a cracking section 1 including a heavy oil feedstock inlet, a fluidizing gas inlet (not shown), and a solid particle outlet;
specifically, the cracking section 1 is a cracking reactor and further comprises a fluidized bed reactor, and under the action of fluidizing gas entering through a fluidizing gas inlet, the fluidized bed reactor enables coke powder to be in a fluidized state and serve as a carrier of cracking reaction;
the atomization unit 3 is communicated with the heavy oil raw material inlet and is used for carrying out atomization treatment on the heavy oil raw material entering the cracking section 1 through the heavy oil raw material inlet;
the steam stripping section 4 is positioned at the lower part of the cracking section 1, comprises a stripping steam inlet and is used for carrying out steam stripping treatment on coke particles descending through the cracking section 1 by utilizing stripping steam entering through the stripping steam inlet;
the particle size refining section 5 is positioned at the lower part of the steam stripping section 4, comprises a grinding steam inlet and is used for carrying out particle size refining treatment on the coke particles treated by the steam stripping section 4 by using grinding steam entering from the grinding steam inlet;
the reactor outside of the heavy oil lightening coupling reaction device comprises:
the oil gas-gas solid separator 200 is used for performing gas-solid separation on the low-temperature mixture flow subjected to the temperature reduction washing treatment by the temperature reduction washing section 6 of the reactor, the inlet of the oil gas-gas solid separator 200 is communicated with the oil gas outlet, the solid phase outlet of the oil gas-gas solid separator 200 is communicated with the cracking section 1, and the gas phase outlet of the oil gas-gas solid separator 200 is used for outputting the purified mixture flow, so that the next step of fractionation treatment is facilitated;
the synthesis gas-solid separator 100 is used for carrying out gas-solid separation on synthesis gas output from the synthesis gas outlet of the gasification section 2, the inlet of the synthesis gas-solid separator 100 is communicated with the synthesis gas outlet, the gas phase outlet of the synthesis gas-solid separator 100 is communicated with the cracking section 1 through an external synthesis gas conveying pipeline c, and the solid phase outlet of the synthesis gas-solid separator 100 is communicated with the cracking section 1.
In addition, the gasification section 2 is coaxially communicated with the cracking section 1 through a material flow conveying pipeline a to facilitate the transportation and circulation of materials, and the output end of the material flow conveying pipeline a is provided with a one-way plug valve b; the solid particle outlet is communicated with the solid particle input port through an external lifting pipe d.
The method for lightening heavy oil using the apparatus provided in fig. 1 is briefly described as follows:
the heavy oil raw material enters the cracking section 1 in two paths, specifically, one path of heavy oil raw material a1 directly enters the cracking section 1 through a heavy oil raw material inlet, the other path of heavy oil raw material a2 is used as low-temperature liquid and firstly enters the cooling washing section 6 for heat exchange, and then descends and is output out of the reactor and then enters the cracking section 1 again through the heavy oil raw material inlet. Heavy oil raw materials (a1, a2) entering the cracking section 1 are treated by the atomization unit 3 and then contact with fluidized coke powder in an atomized state to carry out cracking reaction to generate coke particles and light oil gas.
Coke particles descend under the action of gravity, are sequentially treated by the steam stripping section 4 and the particle size refining section 5 and then enter the external lifting pipe d through the solid phase outlet, ascend in the external lifting pipe d under the action of lifting gas and enter the gasification section 2 through the solid phase inlet. The coke particles entering the gasification section 2 and the gasification agent are subjected to gasification reaction to generate synthesis gas.
With the continuous generation of the synthesis gas, the synthesis gas is output from the synthesis gas outlet of the reactor 2, enters the synthesis gas-solid separator 100 through the inlet of the synthesis gas-solid separator 100 to perform gas-solid separation, finally, coke particles output from the solid phase outlet of the synthesis gas-solid separator 100 enter the cracking section 1 to participate in cracking reaction, purified synthesis gas is output from the gas phase outlet of the synthesis gas-solid separator 100, a part of the purified synthesis gas a2 is collected and processed, and the other part of the purified synthesis gas a1 enters the cracking section 1 through an external synthesis gas conveying pipeline c, so that reaction energy is provided for the cracking reaction, the hydrogen in the purified synthesis gas a1 can also inhibit the coking reaction of the heavy oil cracking reaction, the product distribution of the heavy oil cracking is improved, and the quality and yield of light oil gas are improved. And the purified syngas a1 also provides for the adequate fluidization of the coke particles in cracking section 1. The coke particles which are not completely reacted in the gasification section 2 can move downwards to enter a material flow conveying pipeline a, after the coke particles in the material flow conveying pipeline a reach a certain mass, a one-way plug valve b at the bottom end of the material flow conveying pipeline a can be opened, so that the coke particles in the material flow conveying pipeline a can move downwards to enter the cracking section 1 to participate in the cracking reaction again, and after the coke particles in the material flow conveying pipeline a move downwards to enter the cracking section 1, the one-way plug valve b is automatically closed until the coke particles in the material flow conveying pipeline a at the next time reach a certain mass and then are opened again.
The purified synthesis gas a1 is mixed with light oil gas in the cracking section 1 to form a mixture flow, the mixture flow ascends to enter the cooling washing section 6 to exchange heat with the heavy oil raw material a2, the generated low-temperature mixture flow is output from an oil gas outlet to a reactor and enters the oil gas-solid separator 200 through an outlet of the oil gas-solid separator 200 to carry out gas-solid separation, finally, coke particles output from a solid phase outlet of the oil gas-solid separator 200 enter the cracking section 1 to participate in cracking reaction, and the purified mixture flow output from a gas phase outlet of the oil gas-solid separator 200 can be subjected to next fractionation treatment, so that light oil, cracking gas (dry gas, liquefied gas and the like) and synthesis gas products are obtained.
The device is adopted to treat the domestic vacuum residue oil of a certain refinery, and the table 1 shows the property of the domestic vacuum residue oil of a certain refinery to be treated.
TABLE 1
| Density (20 ℃ C.), g.cm-3 | 0.942 |
| Carbon residue value (wt.%) | 16.57 |
| n (H)/n (C) (molar ratio) | 1.58 |
| Relative molecular weight | 838 |
| C(wt％) | 87.63 |
| H(wt％) | 11.38 |
| S(wt％) | 0.24 |
| N(wt％) | 0.65 |
As can be seen from Table 1: the raw oil has high density and high carbon residue value. And the initial boiling point of the raw oil is about 485 ℃, and the raw oil belongs to heavy raw oil which is difficult to convert.
The method is characterized in that the vacuum residue oil in the table 1 is used as a raw material, the cracking reaction conditions shown in the figure 1 are selected to carry out heavy oil cracking conversion, fluidized coke powder is used as a fluidized reaction bed material of a cracking section under the cracking reaction conditions of 3Mpa and 500 ℃, and mixed gas consisting of steam and synthesis gas is used as fluidization and reaction atmosphere of the heavy oil cracking conversion. The resulting heavy oil pyrolysis product distribution is shown in table 2 and compared to the product distribution in a conventional delayed coking reactor.
TABLE 2
As can be seen from Table 2: compared with the traditional delayed coking reactor, in the heavy oil lightening coupling reaction device, due to the high-efficiency coupling among a plurality of reaction sections and the strengthening effect of the synthetic gas on the heavy oil cracking reaction process, the liquid yield (quality) of the cracking process is improved by nearly 10 percentage points, the yield of coke in the delayed coking reactor is about 1.5 times of the residual carbon value of raw oil, the yield of coke in the cracking lightening coupling reaction device is less than the coke value of the raw material, and the yield of coke is greatly reduced. And the cracking section is coupled with the gasification section through an internal material flow conveying pipeline, an external lifting pipe and an external synthesis gas conveying pipeline, so that the direct gasification reaction of the thermal coke can be realized inside to prepare the hydrogen-rich synthesis gas, and the generation of low-value petroleum coke products is avoided.
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 (10)
1. A heavy oil lightening coupling reaction device is characterized by comprising a reactor and a synthesis gas-solid separator;
the reactor comprises a cracking section and a gasification section which are communicated with each other through a material pipeline;
the input end of the material pipeline is communicated with the bottom of the gasification section, the output end of the material pipeline is communicated with the top of the cracking section, and the output end of the material pipeline is provided with a one-way plug valve;
the cracking section is provided with a heavy oil raw material inlet, a solid particle outlet and a synthesis gas inlet, and the upper part of the cracking section is provided with an oil gas outlet;
the gasification section is provided with a gasification agent inlet, a solid particle inlet and a synthesis gas outlet;
the synthesis gas outlet is communicated with the inlet of the synthesis gas-solid separator, and the gas phase outlet of the synthesis gas-solid separator is communicated with the synthesis gas inlet through an external synthesis gas conveying pipeline;
the solid particle outlet is communicated with the solid particle inlet through an external riser.
2. The coupled reaction device as claimed in claim 1, wherein the reactor interior further comprises a steam stripping section and a grain size refining section which are communicated with each other;
the steam stripping section and the particle size refining section are arranged at the lower part of the cracking section, and the top of the steam stripping section is communicated with the bottom of the cracking section;
the steam stripping section is positioned at the upper part of the grain size refining section;
the steam stripping section is provided with a stripping steam inlet, and the grain size refining section is provided with a grinding steam inlet.
3. The coupling reaction device according to claim 1 or 2, wherein the reactor further comprises a cooling washing section inside, and the cooling washing section is located between the cracking section and the gasification section and used for cooling and washing the light oil gas in the cracking section.
4. The coupling reaction device according to any one of claims 1 to 3, wherein the reactor further comprises an atomization unit inside, and the atomization unit is communicated with the heavy oil feedstock inlet and is used for carrying out atomization treatment on the heavy oil feedstock.
5. The coupling reaction device according to claim 1, further comprising a gas-oil-gas-solid separator outside the reactor, wherein an inlet of the gas-oil-gas-solid separator is communicated with the gas-oil outlet, and a solid phase outlet of the gas-oil-gas-solid separator is communicated with the cracking section.
6. The coupled reaction device of claim 1, wherein the cracking section is a cracking reactor and the gasification section is a gasification reactor.
7. The coupled reaction device of claim 6, wherein the cracking reactor and the gasification reactor are in coaxial communication through the feed line.
8. The coupled reaction device of claim 7, wherein a diameter of the gasification reactor is larger than a diameter of the cracking reactor.
9. The coupled reaction device of claim 8, wherein a diameter ratio of the cracking reactor to the gasification reactor is 1: (1.5-4).
10. The coupling reaction device according to any one of claims 1 to 9, wherein the operating pressure inside the coupling reaction device is 0.1 to 6 Mpa.
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