CN113122331B - Combined process and system for processing crude oil - Google Patents
Combined process and system for processing crude oil Download PDFInfo
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- CN113122331B CN113122331B CN201911423702.XA CN201911423702A CN113122331B CN 113122331 B CN113122331 B CN 113122331B CN 201911423702 A CN201911423702 A CN 201911423702A CN 113122331 B CN113122331 B CN 113122331B
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- 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
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Abstract
The invention discloses a combined process and a system for processing crude oil, wherein the combined process comprises the steps of firstly carrying out flash evaporation treatment on the crude oil to obtain a first light fraction and a first heavy fraction, and carrying out hydrotreating on the first heavy fraction to obtain gas, first light naphtha, first heavy naphtha, a second heavy fraction and first residual oil; feeding the first residual oil into a solvent deasphalting unit for treatment to obtain an oil phase and deoiled asphalt; feeding the oil phase into the first riser reactor, and contacting the oil phase with the catalyst reacted in the second riser reactor for reaction; the second heavy fraction enters the first riser reactor through a second feed inlet to react; and the first light fraction and the first light naphtha enter a second riser reactor to react, and the oil-gas phase obtained after separation and the effluent of the first riser reactor are subjected to settling separation fractionation to obtain low-carbon olefin mixed gas, second light naphtha, second heavy naphtha, circulating oil and slurry oil. In the combined process, by means of segmented feeding and reasonable utilization of catalysts with different activities, the yield of dry gas and coke such as C1/C2 is reduced, the selectivity of a target product is improved, and the running period of the device is prolonged.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a method and a system for directly processing crude oil to produce chemical raw materials.
Background
At present, the petrochemical industry in China faces a plurality of challenges, the external dependence of petroleum rises year by year, the problem of energy safety is concerned, the oil refining capacity is obviously surplus, the consumption of the finished oil is accelerated slowly, the oil is changed from a large import country of the finished oil to a main export country in Asia-Tai regions, meanwhile, the demand of China on high-end chemical products is vigorous, the consumption demand of basic organic raw materials such as ethylene, propylene, paraxylene and the like is vigorous, and the capacity of the basic raw materials in China is always insufficient and the self-sufficiency rate is low for a long time. Based on this, the transformation of oil refining to chemical industry becomes a common consensus in the industry, and the transformation and upgrading pace of the refining and chemical enterprises is accelerated.
The key point of transformation from oil refining to chemical engineering is how to realize crude oil lightening and provide raw materials for chemical production devices. However, with the aggravation of heavy and inferior crude oil, the conventional processing methods such as atmospheric and vacuum distillation, catalytic cracking, fixed bed hydrogenation and the like are difficult to realize the high-efficiency light conversion of the crude oil, and have the problems of poor raw material adaptability, easy blockage of a device, short service life of a catalyst, low raw material conversion rate and the like, so that the device is difficult to operate stably; in addition, the processing flow of the existing refinery is complex, crude oil needs to be processed by atmospheric and vacuum distillation and a plurality of secondary processing devices, the problems of high operation cost such as energy consumption and the like exist, the direct generation of chemical raw materials from crude oil cannot be efficiently realized, and the economic benefit is not high.
CN104711015A discloses a method for using whole distillate oil as raw material of pyrolysis furnace of olefin production device, mainly processing whole distillate oil into light fraction such as condensate oil and light crude oil, and hard to process heavy crude oil. CN104093820A discloses a process directed to a steam pyrolysis zone integrated with a solvent deasphalting zone to allow direct processing of crude oil feedstock for the production of petrochemicals including olefins and aromatics, but with difficulty in further conversion of heavier hydrocarbons in crude oil, and with lower chemical yields CN108884397A discloses an integrated process for converting crude oil to petrochemicals including crude oil distillation, hydrocracking and steam cracking, whereas heavier fractions during processing have difficulty meeting the feed requirements of steam cracking, affecting the petrochemical yields, especially propylene yields.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a combined process and a system for directly processing crude oil to produce chemical raw materials, wherein the combined process can directly take the crude oil as the raw material to produce the chemical raw materials.
In a first aspect the present invention provides a combined process for processing crude oil, said combined process comprising the following:
(1) carrying out flash evaporation treatment on the crude oil to obtain a first light fraction and a first heavy fraction;
(2) feeding the first heavy fraction to an ebullated bed hydrotreating unit, and separating reaction effluent in the presence of hydrogen and an ebullated bed hydrogenation catalyst to obtain gas, first light naphtha, first heavy naphtha, a second heavy fraction and first residual oil;
(3) feeding the first residual oil and a solvent into a solvent deasphalting unit together, and treating to obtain an oil phase and deoiled asphalt;
(4) feeding the oil phase into a first riser reactor in a catalytic cracking device through a first feeding hole, and contacting and reacting with a catalyst reacted by a second riser reactor;
(5) feeding the second heavy fraction into the first riser reactor in the catalytic cracking device through the second feeding hole, and continuously reacting with the reacted material in the step (4);
(6) feeding the first light fraction and the first light naphtha into a second riser reactor in a catalytic cracking device for reaction, conveying a catalyst obtained after reaction of separated reaction effluent to the bottom of the first riser reactor for reaction, and carrying out sedimentation separation on oil gas phase obtained after separation and the effluent of the first riser reactor for fractionation to obtain low-carbon olefin mixed gas, second light naphtha, second heavy naphtha, circulating oil and slurry oil.
In the above combined process for processing crude oil, the second light naphtha can be discharged as a product or recycled to the second riser reactor as a feed, and can also be used as a solvent to enter a solvent deasphalting apparatus for use.
In the combined process for processing crude oil, the first heavy naphtha and the second heavy naphtha can be fed into an aromatic extraction device for subsequent treatment.
In the combined process for processing crude oil described above, the cycle oil may be recycled to the ebullated bed hydroprocessing unit as feed for processing with the first heavy fraction obtained by flashing.
In the above combined process for processing crude oil, the slurry oil may be recycled to the solvent deasphalting unit for treatment.
In the combined process for processing crude oil, more than one set of catalytic cracking device is arranged, and the catalytic cracking device comprises a first riser reactor, a second riser reactor, a settler, a regenerator and a cyclone separator; the first riser reactor is provided with two feed inlets, wherein the first feed inlet is arranged at the bottom of the first riser reactor, the second feed inlet is arranged above the first feed inlet, and the distance between the second feed inlet and the first feed inlet accounts for 1/25-1/4 of the height of the first riser reactor, preferably 1/15-1/8. The catalytic cracking device is provided with a fractionating tower, and each set of catalytic cracking device can be set respectively or can be shared.
In the above combined process for processing crude oil, the crude oil in step (1) comprises whole crude oil from conventional sources, including crude oil that has been subjected to certain pre-treatments. The pretreated crude oil typically comprises crude oil that has been subjected to oil-water separation and/or gas-oil separation and/or desalting.
In the above combined process for processing crude oil, the flash distillation in step (1) may adopt a conventional flash distillation process existing in the prior art, and the fractionation point of the first light fraction and the first heavy fraction is 160-260 ℃, preferably 160-185 ℃.
In the above-mentioned combined process for processing crude oil, at least one ebullated-bed reactor is provided in the ebullated-bed hydrotreatment unit involved in the step (2), and when two or more reactors are provided, the reactors are connected in series. The fluidized bed reactor is filled with a fluidized bed hydrogenation catalyst, and the fluidized bed hydrogenation catalyst is a single catalyst or a combined catalyst with functions of residual oil hydrodemetallization, hydrodesulfurization, hydrodenitrogenation, hydrocracking and the like. The fluidized bed hydrogenation catalyst comprises a carrier and an active metal, wherein the active metal can be one or more of nickel, cobalt, molybdenum or tungsten, and the carrier can be one or more of alumina, silica, alumina-silica or titanium oxide. The bulk density of the catalyst is 0.3-0.8 g/cm3The particle diameter (spherical diameter or strip diameter) is 0.3-1.0 mm, and the specific surface area is 80-120 m2(ii) in terms of/g. Meanwhile, the catalyst has a bimodal distribution pore structure, the pore volume of pores with the diameter of 5-50 nm accounts for 30-65% of the total pore volume, and the pore volume of pores with the diameter of more than 100nm accounts for 20-35% of the total pore volume. When a plurality of reactors are arranged in series, the catalyst loading sequence is generally that the hydrodemetallization, hydrodesulfurization and hydrodenitrogenation catalysts are sequentially arranged according to the flowing direction of the raw materials, and the catalysts can also be mixed and loaded.
In the above combined process for processing crude oil, the reaction conditions of the ebullated-bed hydroprocessing unit in step (2) are typically: the reaction temperature is 350-450 ℃, the preferable temperature is 380-440 ℃, the reaction pressure is 5.0-18.0 MPa, the preferable pressure is 10.0-18.0 MPa, the volume ratio of hydrogen to oil is 500-2000, the preferable pressure is 600-1500, and the liquid hourly space velocity is 0.1-5.0 h-1Preferably 0.2 to 2.0 hours-1。
In the combined process for processing crude oil, the fractionation point of the second heavy fraction and the first residual oil is 450-550 ℃, and preferably 480-550 ℃.
In the above-described integrated process for processing crude oil, the solvent deasphalting can be carried out by the conventional techniques in the art, and the solvent used comprises at least one of alkane of C3-C7 or naphtha fraction, and the operating conditions are as follows: the temperature is 80-200 ℃, preferably 100-160 ℃, the pressure is 2.0-6.0 MPa, preferably 3.0-5.0 MPa, and the volume ratio of the solvent is 1.0-10.0, preferably 3.0-8.0. The weight yield of the oil phase is controlled to be 40-80 percent, and the content of metal in the oil phase is not more than 120 mu g/g.
In the combined process for processing crude oil, the catalytic cracking catalyst used in the catalytic cracking device comprises zeolite, inorganic oxide and optional clay, wherein the content of zeolite is 10-50 wt%, the content of inorganic oxide is 5-90 wt% and the content of clay is 0-70 wt% based on the total weight of the catalytic cracking catalyst. The active component in the catalytic cracking catalyst is at least one of Y-type or HY-type zeolite containing or not containing rare earth, ultrastable Y-type zeolite containing or not containing rare earth and zeolite with MFI structure.
In the combined process for processing crude oil, the reaction temperature of the first riser reactor is 500-780 ℃, and preferably 580-700 ℃; the mass ratio of the water vapor to the feed is 0.05: 1-1: 1, preferably 0.15: 1-0.5: 1, the reaction pressure is 0.10-1.0 MPa, preferably 0.10-0.5 MPa, and the contact time with the catalyst is 0.1-15.0 seconds, preferably 0.5-5.0 seconds.
In the combined process for processing crude oil, the reaction temperature of the second riser reactor is 10-50 ℃, preferably 30-50 ℃ higher than that of the first riser reactor, the mass ratio of the water vapor to the feed is 0.05: 1-1: 1, preferably 0.15: 1-0.5: 1, the reaction pressure is 0.10-1.0 MPa, preferably 0.10-0.5 MPa, and the contact time with the catalyst is 0.1-15.0 seconds, preferably 0.3-5.0 seconds.
In a second aspect the present invention provides a combined system for processing crude oil, the combined system comprising:
the flash evaporation unit is used for receiving and processing crude oil to obtain a first light fraction and a first heavy fraction;
the ebullated bed hydrotreating unit is used for receiving the first heavy fraction and hydrogen from the flash evaporation unit and reacting under the action of an ebullated bed hydrogenation catalyst;
the first fractionation unit is used for receiving and processing reaction effluent from the ebullated bed hydrotreating unit, and obtaining gas, first light naphtha, first heavy naphtha, second heavy fraction and first residual oil after separation;
a solvent deasphalting unit for receiving the solvent and the first residuum from the first fractionation unit and treating to obtain an oil phase and a deasphalted asphalt;
a catalytic cracking unit comprising a first riser reactor, a second riser reactor, a settler, a regenerator, and a cyclone; the first riser reactor is provided with two feed inlets, wherein the first feed inlet is arranged at the bottom of the first riser reactor, and the second feed inlet is arranged above the first feed inlet;
wherein, the oil phase from the solvent deasphalting unit is fed into the first riser reactor through a first feed inlet and contacts with the catalyst reacted in the second riser reactor for reaction, and the second heavy fraction is fed into the first riser reactor through a second feed inlet and continuously reacts with the reacted material of the oil phase; mixing the first light fraction from the flash unit and the first light naphtha from the first fractionation unit, feeding the mixture into a second riser reactor for reaction, separating the reaction effluent in a cyclone separator, feeding the separated catalyst obtained after the reaction into the bottom of the first riser reactor through a pipeline, and feeding the separated oil phase into a settler at the upper part of the first riser reactor;
and the second fractionating unit is used for receiving the oil gas material from the settler and separating the oil gas material to obtain low-carbon olefin mixed gas, second light naphtha, second heavy naphtha, circulating oil and oil slurry.
And the regenerator is used for receiving the material containing the catalyst to be regenerated from the bottom of the settler, and conveying the regenerated catalyst obtained after treatment to the first riser reactor and the second riser reactor through pipelines.
In the combined system for processing crude oil, the distance between the second feeding hole and the first feeding hole of the first riser reactor accounts for 1/25-1/4 of the height of the first riser reactor, and preferably 1/15-1/8.
Compared with the prior art, the combined process and system for processing crude oil provided by the invention have the following advantages:
1. in the combined process, the first riser reactor in the catalytic cracking device is provided with two feed inlets, wherein the oil phase from the solvent deasphalting unit and the reacted catalyst (with partial coke and lower activity) from the second riser reactor are subjected to cracking reaction at the inlet of the first riser reactor under relatively mild conditions, so that larger hydrocarbon molecules are cracked into relatively smaller hydrocarbons, and the rapid inactivation of the catalyst caused by the direct adsorption of macromolecular condensed ring aromatic hydrocarbons in the oil phase onto the catalyst is avoided. And the second heavy fraction and the regenerated catalyst with higher activity enter the first riser reactor from the second feed inlet, are mixed with the oil agent reacted from the lower part of the first riser reactor, and are subjected to cracking reaction under the action of the high-activity catalyst. In the combined process, by means of segmented feeding and reasonable utilization of catalysts with different activities, the yield of dry gas and coke such as C1/C2 is reduced, the selectivity of a target product is improved, and the running period of the device is prolonged.
2. In the combined process, the first light naphtha and the flash evaporation light fraction are subjected to catalytic cracking treatment by arranging the separate second riser reactor, reaction conditions can be set according to hydrocarbon composition difference in a targeted manner, naphtha is directionally converted into olefin chemical raw materials, the activity of the catalyst after reaction is slightly reduced, and the catalyst is relatively suitable for mild cracking with a heavier deasphalted oil phase at the inlet section of the first riser reactor, so that the graded utilization of catalysts with different activities is realized.
3. In the combined process, the circulating oil and the catalytic slurry oil obtained by the catalytic cracking device are respectively circulated to the boiling hydrotreatment unit and the solvent deasphalting device, so that the mass transfer efficiency in the reaction process is increased, the complete conversion of all components in the crude oil is realized, the conversion rate is improved, and the crude oil is converted into high-value chemical products as much as possible.
4. Compared with the traditional refinery crude oil processing flow, namely the series of processing flows of atmospheric and vacuum distillation, fixed bed hydrocracking, catalytic cracking and the like, the process flow of the invention can greatly improve the conversion rate of the crude oil directly producing chemical products and obviously improve the economic benefit of the refinery.
Drawings
FIG. 1 is a schematic diagram of a combined process and system for processing crude oil.
Wherein 1-crude oil, 2-flash unit, 3-first light fraction, 4-first heavy fraction, 5-ebullated bed hydrotreating unit, 6-first fractionating unit, 7-gas, 8-first light naphtha, 9-first heavy naphtha, 10-second heavy fraction, 11-first residual oil, 12-solvent deasphalting unit, 13-oil phase, 14-deasphalting asphalt, 15-first riser reactor lower reaction zone, 16-first riser reactor upper reaction zone, 17-settler, 18-regenerator, 19-mixed light naphtha, 20-second riser reactor, 21-cyclone separator, 22-second fractionating unit, 23-low carbon olefin mixed gas, 24-second light naphtha, 25-second heavy naphtha, 26-cycle oil, 27-catalytic slurry oil.
FIG. 2 is a schematic diagram of the combined process and system for processing crude oil of comparative example 1.
FIG. 3 is a schematic diagram of a combined process and system for processing crude oil according to comparative example 2.
Detailed Description
The technical features of the present invention will be further described by way of examples in conjunction with the accompanying drawings, but the present invention is not limited to these examples.
As shown in fig. 1, the present invention provides a combined process for processing crude oil, the combined process comprising: the crude oil 1 enters a flash evaporation unit 2 for flash evaporation treatment to obtain a first light fraction 3 and a first heavy fraction 4; feeding the first heavy fraction 4 to an ebullated bed hydrotreating unit 5, and in the presence of hydrogen and an ebullated bed hydrogenation catalyst, obtaining a gas 7, a first light naphtha 8, a first heavy naphtha 9, a second heavy fraction 10 and a first residual oil 11 after the reaction effluent passes through a first fractionation unit 6; feeding the first residual oil 11 and a solvent into a solvent deasphalting unit 12, and processing to obtain an oil phase 13 and deasphalted asphalt 14; feeding the oil phase into a lower reaction zone 15 of a first riser reactor in the catalytic cracking device through a first feed inlet, and contacting and reacting with a catalyst reacted in a second riser reactor 20; feeding the second heavy fraction 10 into the first riser reactor of the catalytic cracking device through the second feeding hole, and continuously reacting with the reacted material in the upper reaction zone 16 of the first riser reactor; the first light fraction 3, the first light naphtha 8 and the second light naphtha 24 are mixed into a material flow 19, the material flow 19 is sent to a second riser reactor 20 in a catalytic cracking device for reaction, a catalyst obtained after reaction is separated by a cyclone separator 21 is conveyed to the bottom of the first riser reactor for reaction, oil gas obtained after separation and effluent of the first riser reactor are separated by a settler 17 and then enter a second fractionating unit 22 for fractionation, so that low-carbon olefin mixed gas 23, second light naphtha 24, second heavy naphtha 25, circulating oil 26 and oil slurry 27 are obtained, the circulating oil 26 is circulated back to a boiling bed hydrogenation reaction unit, and the oil slurry 27 is circulated back to a solvent deasphalting unit 12.
The basic properties of the crude oils used in the inventive examples and comparative examples are shown in Table 1.
TABLE 1 basic Properties of crude oils
Example 1
This example was carried out using the process flow diagram shown in FIG. 1, wherein the crude oil passed through the flash unit, the first heavy fraction had an initial boiling point of 210 ℃; the fluidized bed hydrogenation unit is provided with two fluidized bed reactors which are connected in series, the reaction pressure is 16MPa, the volume ratio of hydrogen to oil is 800, the reaction temperature of the first reactor is 410 ℃, and the liquid hourly volume space velocity is 0.35 h-1The reaction temperature of the second reactor is 420 ℃, and the liquid hourly space velocity is 0.4h-1. The catalysts filled in the two reactors are the same and are both FES-30 catalysts developed by the comforting petrochemical research institute; the solvent deasphalting unit selects a normal butane solvent, the extraction temperature is 135 ℃, the pressure is 4.0Mpa, and the solvent-oil volume ratio is 5.0; the reaction temperature of the lower reaction zone 15 of the first riser reactor of the catalytic cracking unit is 560 ℃, and the weight hourly space velocity is 160h-1The mass ratio of the water vapor to the feeding material is 0.2:1, the reaction pressure is 0.2MPa, the reaction temperature of the upper reaction zone of the first riser reactor is 600 ℃, the reaction temperature of the second riser reactor is 650 ℃, and the weight hourly space velocity is 4.0h-1The catalyst-oil ratio is 40, the catalytic cracking catalyst is MMC-2 catalyst, and the reaction result is shown in Table 1.
Example 2
The same procedure is adopted as in example 1, except that the reaction conditions are different, the reaction pressure of the fluidized bed hydrogenation unit is 18MPa, the volume ratio of hydrogen to oil is 1000, the reaction temperature of the first reactor is 410 ℃, and the liquid hourly space velocity is 0.35 h-1The reaction temperature of the second reactor is 430 ℃, and the liquid hourly space velocity is 0.4h-1. The solvent deasphalting unit selects a normal butane solvent, the extraction temperature is 130 ℃, the pressure is 4.0Mpa, and the solvent-oil volume ratio is 6.0; the reaction temperature of the lower reaction zone 15 of the first riser reactor of the catalytic cracking unit is 580 ℃, and the weight hourly space velocity is 160h-1The mass ratio of the water vapor to the feeding material is 0.2:1, the reaction pressure is 0.2MPa, the reaction temperature of the upper reaction zone of the first riser reactor is 620 ℃, and the reaction temperature of the second riser reactor isThe temperature is 650 ℃, and the weight hourly space velocity is 4.0h-1The catalyst-oil ratio is 40, the catalytic cracking catalyst is MMC-2 catalyst, and the reaction result is shown in Table 1.
Comparative example 1
The comparative example is carried out by adopting the process flow diagram shown in FIG. 2, the differences between the comparative example 1 and the example 1 are mainly that the first riser of the catalytic cracking device is not provided with a second feeding hole, the second heavy fraction 10 and the oil phase 13 treated by the solvent deasphalting unit 12 are directly fed into the first riser of the catalytic cracking device, other process flows are the same as the example 1, and the reaction results are shown in Table 2.
Comparative example 2
The comparative example is carried out by adopting a process flow diagram shown in fig. 3, the difference between the comparative example 2 and the example 1 is that a solvent deasphalting unit is not arranged, the oil generated by the hydrogenation of an ebullated bed passes through a first fractionating unit 6 to obtain dry gas 7, first light naphtha 8, first heavy naphtha 9 and second heavy fraction 11, a second feeding hole is not arranged in a first riser of a catalytic cracking device, the second heavy fraction 11 directly enters the first riser of the catalytic cracking device, other process flows are the same as the example 1, and the reaction results are shown in table 2.
TABLE 2 results of the reaction
Claims (22)
1. A combined process for processing crude oil, the combined process comprising:
(1) carrying out flash evaporation treatment on the crude oil to obtain a first light fraction and a first heavy fraction;
(2) feeding the first heavy fraction to an ebullated bed hydrotreating unit, and separating reaction effluent in the presence of hydrogen and an ebullated bed hydrogenation catalyst to obtain gas, first light naphtha, first heavy naphtha, a second heavy fraction and first residual oil;
(3) feeding the first residual oil and a solvent into a solvent deasphalting unit together, and treating to obtain an oil phase and deoiled asphalt;
(4) feeding the oil phase into a first riser reactor in a catalytic cracking device through a first feeding hole, and contacting and reacting with a catalyst reacted by a second riser reactor;
(5) feeding the second heavy fraction into the first riser reactor in the catalytic cracking device through the second feeding hole, and continuously reacting with the reacted material in the step (4);
(6) feeding the first light fraction and the first light naphtha into a second riser reactor in a catalytic cracking device for reaction, conveying a catalyst obtained after reaction of separated reaction effluent to the bottom of the first riser reactor for reaction, and carrying out sedimentation separation on oil gas phase obtained after separation and the effluent of the first riser reactor for fractionation to obtain low-carbon olefin mixed gas, second light naphtha, second heavy naphtha, circulating oil and slurry oil.
2. The integrated process for processing crude oil according to claim 1, wherein: and the second light naphtha is discharged as a product or recycled to the second riser reactor as a feed, and then enters a solvent deasphalting device as a solvent for use.
3. The integrated process for processing crude oil according to claim 1, wherein: and (4) recycling the circulating oil obtained in the step (6) to the ebullated bed hydrotreating unit as a feed to be treated together with the first heavy fraction obtained by flashing.
4. The integrated process for processing crude oil according to claim 1, wherein: and (4) circulating the oil slurry obtained in the step (6) to a solvent deasphalting device for treatment.
5. The integrated process for processing crude oil according to claim 1, wherein: the catalytic cracking device is provided with more than one set, and comprises a first riser reactor, a second riser reactor, a settler, a regenerator and a cyclone separator; the first riser reactor is provided with two feed inlets, wherein the first feed inlet is arranged at the bottom of the first riser reactor, the second feed inlet is arranged above the first feed inlet, and the distance between the second feed inlet and the first feed inlet accounts for 1/25-1/4 of the height of the first riser reactor.
6. The integrated process for processing crude oil according to claim 1, wherein: the catalytic cracking device is provided with more than one set, and comprises a first riser reactor, a second riser reactor, a settler, a regenerator and a cyclone separator; the first riser reactor is provided with two feed inlets, wherein, first feed inlet is established in the bottom of first riser reactor, and the second feed inlet is established in the top of first feed inlet, and the distance between second feed inlet and the first feed inlet accounts for 1/15 ~ 1/8 of first riser reactor height.
7. The integrated process for processing crude oil according to claim 1, wherein: the fractionation point of the first light fraction and the first heavy fraction in the step (1) is 160-260 ℃.
8. The integrated process for processing crude oil according to claim 1, wherein: the fractionation point of the first light fraction and the first heavy fraction in the step (1) is 160-185 ℃.
9. The integrated process for processing crude oil according to claim 1, wherein: the reaction conditions of the ebullated bed hydrotreating unit in step (2) are as follows: the reaction temperature is 350-450 ℃, the reaction pressure is 5.0-18.0 MPa, the volume ratio of hydrogen to oil is 500-2000, and the liquid hourly space velocity is 0.1-5.0 h-1。
10. The integrated process for processing crude oil according to claim 1, wherein: step (2)The reaction conditions of the medium boiling bed hydrotreating unit are as follows: the reaction temperature is 380-440 ℃, the reaction pressure is 10.0-18.0 MPa, the hydrogen-oil volume ratio is 600-1500, and the liquid hourly space velocity is 0.2-2.0 h-1。
11. The integrated process for processing crude oil according to claim 1, wherein: the second heavy fraction and the first residual oil have a fractionation point of 450-550 ℃.
12. The integrated process for processing crude oil according to claim 1, wherein: the second heavy fraction and the first residual oil have a fractionation point of 480-550 ℃.
13. The integrated process for processing crude oil according to claim 1, wherein: the solvent used for solvent deasphalting comprises at least one of alkane of C3-C7 or naphtha fraction, and the operating conditions are as follows: the temperature is 80-200 ℃, the pressure is 2.0-6.0 MPa, and the volume ratio of the solvent is 1.0-10.0.
14. The integrated process for processing crude oil according to claim 1, wherein: the solvent used for solvent deasphalting comprises at least one of alkane of C3-C7 or naphtha fraction, and the operating conditions are as follows: the temperature is 100-160 ℃, the pressure is 3.0-5.0 MPa, and the volume ratio of the solvent is 3.0-8.0.
15. The integrated process for processing crude oil according to claim 1, wherein: the weight yield of the oil phase of the solvent deasphalting unit is controlled to be 40-80%, and the content of metal in the oil phase is not more than 120 mu g/g.
16. Combined process for processing crude oil according to claim 5, characterized in that: the reaction temperature of the first riser reactor is 500-780 ℃, the mass ratio of the water vapor to the feeding material is 0.05: 1-1: 1, the reaction pressure is 0.10-1.0 MPa, and the contact time with the catalyst is 0.1-15.0 seconds.
17. The integrated process for processing crude oil according to claim 1, wherein: the reaction temperature of the first riser reactor is 580-700 ℃; the mass ratio of the water vapor to the feed is 0.15: 1-0.5: 1, the reaction pressure is 0.10-0.5 MPa, and the contact time with the catalyst is 0.5-5.0 seconds.
18. The integrated process for processing crude oil according to claim 1, wherein: the reaction temperature of the second riser reactor is 10-50 ℃ higher than that of the first riser reactor, the mass ratio of the water vapor to the feeding material is 0.05: 1-1: 1, the reaction pressure is 0.10-1.0 MPa, and the contact time with the catalyst is 0.1-15.0 seconds.
19. The integrated process for processing crude oil according to claim 1, wherein: the reaction temperature of the second riser reactor is 30-50 ℃ higher than that of the first riser reactor, the mass ratio of the water vapor to the feed is 0.15: 1-0.5: 1, the reaction pressure is 0.10-0.5 MPa, and the contact time of the second riser reactor with the catalyst is 0.3-5.0 seconds.
20. A combined system for processing crude oil, the combined system comprising:
the flash evaporation unit is used for receiving and processing crude oil to obtain a first light fraction and a first heavy fraction;
the ebullated bed hydrotreating unit is used for receiving the first heavy fraction and the hydrogen from the flash evaporation unit, and reacting under the action of an ebullated bed hydrogenation catalyst;
the first fractionating unit is used for receiving and processing reaction effluent from the ebullated bed hydrotreating unit, and obtaining gas, first light naphtha, first heavy naphtha, second heavy fraction and first residual oil after separation;
a solvent deasphalting unit for receiving the solvent and the first residuum from the first fractionation unit and treating to obtain an oil phase and a deasphalted asphalt;
a catalytic cracking unit comprising a first riser reactor, a second riser reactor, a settler, a regenerator, and a cyclone; the first riser reactor is provided with two feed inlets, wherein the first feed inlet is arranged at the bottom of the first riser reactor, and the second feed inlet is arranged above the first feed inlet; wherein, the oil phase from the solvent deasphalting unit is fed into the first riser reactor through a first feed inlet and contacts with the catalyst reacted in the second riser reactor for reaction, and the second heavy fraction is fed into the first riser reactor through a second feed inlet and continuously reacts with the reacted material of the oil phase; mixing the first light fraction from the flash unit and the first light naphtha from the first fractionation unit, feeding the mixture into a second riser reactor for reaction, separating the reaction effluent in a cyclone separator, feeding the separated catalyst obtained after the reaction into the bottom of the first riser reactor through a pipeline, and feeding the separated oil phase into a settler at the upper part of the first riser reactor;
the second fractionation unit is used for receiving the oil gas material from the settler and separating the oil gas material to obtain low-carbon olefin mixed gas, second light naphtha, second heavy naphtha, circulating oil and oil slurry;
and the regenerator is used for receiving the material containing the catalyst to be regenerated from the bottom of the settler, and conveying the regenerated catalyst obtained after treatment to the first riser reactor and the second riser reactor through pipelines.
21. The combination for processing crude oil as claimed in claim 20, wherein: the distance between the second feed opening and the first feed opening of the first riser reactor accounts for 1/25-1/4 of the height of the first riser reactor.
22. The combination for processing crude oil as claimed in claim 20, wherein: the distance between the second feed opening and the first feed opening of the first riser reactor accounts for 1/15-1/8 of the height of the first riser reactor.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101418222A (en) * | 2007-10-26 | 2009-04-29 | 中国石油化工股份有限公司 | Composite process for treatment of inferior residual oil |
| CN102311799A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Residual oil treatment combined process method |
| CN107286990A (en) * | 2016-04-12 | 2017-10-24 | 中国石油化工股份有限公司 | A kind of heavy-oil hydrogenation processing and catalytic cracking combined technique |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101418222A (en) * | 2007-10-26 | 2009-04-29 | 中国石油化工股份有限公司 | Composite process for treatment of inferior residual oil |
| CN102311799A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Residual oil treatment combined process method |
| CN107286990A (en) * | 2016-04-12 | 2017-10-24 | 中国石油化工股份有限公司 | A kind of heavy-oil hydrogenation processing and catalytic cracking combined technique |
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