CN116355652A - Processing method and system for inferior heavy oil - Google Patents
Processing method and system for inferior heavy oil Download PDFInfo
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- CN116355652A CN116355652A CN202111622969.9A CN202111622969A CN116355652A CN 116355652 A CN116355652 A CN 116355652A CN 202111622969 A CN202111622969 A CN 202111622969A CN 116355652 A CN116355652 A CN 116355652A
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Images
Classifications
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
-
- 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
-
- 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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
-
- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- 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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a method and a system for processing inferior heavy oil, wherein the method comprises the following steps: fully mixing inferior heavy oil, a catalyst and hydrogen, then carrying out shallow hydrocracking reaction, and carrying out gas-liquid separation on a product obtained by the reaction to obtain a liquid-phase product; mixing the liquid phase product with a composite flocculant, and then continuously depositing to separate and obtain overflow materials and underflow materials; fractionating the overflow material to obtain unconverted oil; and fully mixing the rest part of unconverted oil from which tail oil is thrown out, the catalyst and hydrogen, and then carrying out deep hydrocracking reaction, carrying out gas-liquid separation on the product obtained by the reaction to obtain a liquid-phase product, and then carrying out fractionation on the liquid-phase product alone or together with the overflow material to obtain a light oil product. The method and the system can ensure the product yield, simultaneously greatly reduce the risk of coking and blocking of equipment such as a slurry bed hydrogenation reactor, a follow-up fractionating tower and the like, and prolong the operation stability and the operation period of the device.
Description
Technical Field
The invention relates to a processing method and a system of inferior heavy oil, in particular to a method and a system for producing light oil products or chemical raw materials by hydrocracking an inferior heavy oil slurry bed, belonging to the technical field of hydrocarbon oil processing.
Background
With the increasing decrease of conventional petroleum resources and the increasing maturity of heavy oil exploitation technologies, the production of crude oil has a trend of heavy quality and poor quality. At present, the conventional petroleum resource which is ascertained in the world is about 3 trillion barrels, so far about 1 trillion barrels are mined, and the dominant oil fields of the world main oil producing countries enter the middle and later stages of development, so that the heavy crude oil mining proportion is continuously improved. Also, for our country, heavy oil resources will become the most important strategic alternative energy source. Therefore, the lightening of the inferior heavy oil becomes an important problem which is faced by the oil refining industry in China, the high-efficiency utilization of heavy oil resources is realized, the distillate oil and the chemical raw materials are produced more, the national energy requirements are guaranteed, and the economic benefit and the social benefit are better.
The slurry bed hydrocracking technology is an excellent technology which can process high-metal, high-carbon residue and high-sulfur raw materials, has high conversion rate and high light oil yield, and accords with the development trend of improving the resource utilization rate. Residuum is a very complex mixture containing, in addition to a large amount of S, N, heavy metals and other impurities, gum and asphaltenes. Wherein asphaltenes are high polar, high molecular weight compounds containing heteroatoms. The Pfeiffer & Sal model describes asphaltenes as: a colloidal layer or high boiling polar aromatic hydrocarbon surrounds the asphaltenes and stabilizes the asphaltenes in a colloidal suspension. In the absence of gum or dilution of gum by paraffinic molecules, these asphaltenes coalesce or flocculate themselves to form macromolecules which precipitate out of solution, the first step in the coking process. Asphaltenes have a tendency to be converted to light alkanes and aromatics in a hydrogen-critical environment; polar aromatics are also converted to lighter components but at a faster rate than asphaltenes. As a result, as the reaction proceeds, the polar aromatics to asphaltenes ratio decreases and the paraffins to aromatics ratio increases, eventually causing asphaltenes to flocculate, mesophase formation, precipitation and eventually coking. Thus, for the hydrogenation of slurry bed residuum in which the hydro-thermal cracking reaction occurs, the residuum is easily coked. In addition, the coking rate of the residual oil in the slurry bed residual oil hydrogenation device is increased along with the improvement of the residual oil conversion rate, and the cost of obtaining the high conversion rate of the residual oil is that a large amount of coke is generated, so that a reactor and a subsequent separation unit of the slurry bed residual oil hydrogenation device are blocked by the coke, the operation period of the device is shortened, and the requirement of industrial long-period operation cannot be met.
At present, there are many reports in the prior art about heavy crude oil and residuum processing, for example, chinese patent No. cn00110716.X discloses a heavy and residuum hydroconversion process comprising: the raw materials of the mixed catalyst and hydrogen enter a first section of low-temperature long-residence-time suspension bed hydrogenation device (a first slurry bed) for pretreatment, the hydrogen-carbon ratio and colloid stability of residual oil are improved, and reaction effluent directly enters a second section of high-temperature short-residence-time suspension bed hydrogenation device (a second reaction) for high-conversion-rate hydrogenation reaction, so that the coke generation amount of the reaction is reduced, and the operation period of the device is prolonged to a certain extent. However, because the process does not carry out post-treatment on solid particles such as coke, catalyst and the like in reaction products, the device has hidden danger of blocking subsequent equipment and pipelines during long-term operation, and raw materials entering the second reaction in the process are full-fraction generated oil of the first reaction, and contain a certain amount of light components, so that the reaction materials are diluted, the consumption of the second reaction hydrogen is increased, and meanwhile, the light components are excessively cracked, so that the yield of the light components is reduced.
Chinese patent CN 111434755a discloses a method for processing heavy oil, which comprises first feeding heavy oil raw material into slurry bed hydrogenation unit, then separating light product and tail oil, feeding tail oil into solvent deasphalting unit, feeding the obtained deasphalted oil into catalytic cracking unit, and recycling part of deasphalted asphalt into slurry bed hydrogenation unit. The method can improve the yield of high added value products and the overall yield of heavy oil processing. However, the solvent deasphalting device needs distillation and extraction, has high energy consumption, and the deasphalted asphalt contains a large amount of asphaltenes, and the recycling under severe slurry bed operation conditions (high temperature) can cause the increase of coke generation amount of the device, and influence the operation period of the device.
Chinese patent CN106147848A discloses a two-stage heavy oil slurry bed hydrogenation apparatus and method, which realizes efficient lightening of hydrocarbons with different components and different structures in a heavy oil system by strengthening different reactions in different reactors, has high heavy oil conversion rate, reduces the external throwing amount of unconverted tail oil, reduces environmental pollution, and prolongs the operation period. However, the method does not consider the influence of generated oil on the coking of a follow-up separator and a fractionation system, and has a specific reactor structure, is more complex than a normal cylindrical reactor structure, is easy to generate dead zone, causes local coking, and can easily cause faults in the actual operation process to influence the operation stability.
Therefore, providing a novel method and system for processing inferior heavy oil has become a technical problem to be solved in the art.
Disclosure of Invention
In order to solve the above-mentioned drawbacks and disadvantages, an object of the present invention is to provide a method for processing inferior heavy oil.
Another object of the present invention is to provide a system for processing inferior heavy oil. The processing method and the processing system of the inferior heavy oil provided by the invention utilize the characteristic of unstable colloid system of shallow thermal cracking residual oil, so that coking precursors such as asphaltene are separated before entering deep cracking, the product yield is ensured, the risk of coking blockage of equipment such as a slurry bed reactor and a subsequent fractionating tower is greatly reduced, and the operation stability and the operation period of the device are prolonged.
In order to achieve the above object, in one aspect, the present invention provides a method for processing inferior heavy oil, wherein the method for processing inferior heavy oil comprises:
s1: fully mixing inferior heavy oil, a catalyst and hydrogen, then carrying out shallow hydrocracking reaction, and carrying out gas-liquid separation on a product obtained by the reaction to obtain a liquid-phase product;
s2: mixing the liquid phase product with a composite flocculant, and then continuously depositing to separate and obtain overflow materials and underflow materials;
s3: fractionating the overflow material to obtain unconverted oil;
s4: and fully mixing the rest part of unconverted oil from which tail oil is thrown out, the catalyst and hydrogen, and then carrying out deep hydrocracking reaction, carrying out gas-liquid separation on the product obtained by the reaction to obtain a liquid-phase product, and then carrying out fractionation on the liquid-phase product alone or together with the overflow material to obtain a light oil product.
In the above processing method of inferior heavy oil provided by the invention, the light oil product refers to oil products from a fractionation device, including gasoline, diesel oil and wax oil.
As a specific embodiment of the method for processing inferior heavy oil according to the present invention, the method further comprises: and mixing the underflow material with inferior heavy oil and a catalyst, and then fully mixing the obtained mixture with hydrogen.
In a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S1, the inferior heavy oil includes one or a combination of several of atmospheric residue, vacuum residue, deasphalted oil, oil sand pitch, high-viscosity crude oil, coal tar and coal liquefied heavy oil.
As a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S1, the metal content in the inferior heavy oil is greater than 200 μg/g based on the total weight of Ni and V, and the total content of gum and asphaltene is greater than 30wt%.
As a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S1, the catalyst used in the shallow hydrocracking reaction is a solid powder catalyst, a water-soluble catalyst or an oil-soluble catalyst, wherein the particle size of the catalyst is 0.01-100 μm.
As a specific embodiment of the above method for processing inferior heavy oil according to the present invention, in S1, the process operating conditions of the shallow hydrocracking reaction are as follows:
the reaction temperature is 350-420 ℃, the reaction pressure is 4-14MPa, the volume ratio of hydrogen to oil at the inlet of the reactor is 600-2000, the catalyst dosage corresponding to each gram of inferior heavy oil is 100-10000 mug based on the metal content, and the volume space velocity is 0.5-2h -1 The per pass conversion is 30-60wt%.
As a specific embodiment of the above method for processing inferior heavy oil according to the present invention, in S1, the process operating conditions of the shallow hydrocracking reaction are as follows:
the reaction temperature is 400-420 ℃, the reaction pressure is 10-12MPa, the volume ratio of hydrogen to oil at the inlet of the reactor is 1000-1500, the catalyst dosage corresponding to each gram of inferior heavy oil is 100-5000 mug based on the metal content, and the volume space velocity is 1-1.5h -1 The per pass conversion is 40-50wt%.
As a specific embodiment of the method for processing inferior heavy oil, in the invention, in S2, the adding amount of the composite flocculant is 0.01-0.2% of the weight of the liquid phase product.
As a specific embodiment of the method for processing inferior heavy oil, in the invention, in S2, the adding amount of the composite flocculant is 0.05-0.1% of the weight of the liquid phase product.
As a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S2, the composite flocculant comprises a quaternary ammonium salt surfactant, an organic polymeric flocculant, an inorganic polymeric flocculant and a reverse oil-soluble demulsifier, wherein the weight ratio of the four is 5-10:1-3:50-100:10-50.
As a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S2, the quaternary ammonium salt surfactant includes one or a combination of several of dicetyl dimethyl ammonium bromide, dodecyl trimethyl ammonium bromide, alkyl dimethyl ammonium chloride, octadecyl trimethyl ammonium bromide, and the like.
As a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S2, the organic polymeric flocculant includes one or a combination of several of cationic polyacrylamide, sodium polyacrylate, polyvinyl pyridinium, polyethylenimine, and the like.
As a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S2, the inorganic polymeric flocculant includes one or a combination of several of polyaluminosilicate, polyaluminophosphate, and the like.
As a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S2, the reverse oil-soluble demulsifier includes one or a combination of several of polyether reverse oil-soluble demulsifiers, polypropylene oxide reverse oil-soluble demulsifiers, polyamide reverse oil-soluble demulsifiers, and polytriethanolamine reverse oil-soluble demulsifiers.
In a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S2, the composite flocculant includes dicetyl dimethyl ammonium bromide, cationic polyacrylamide, polyaluminum ferric silicate and polyether reverse phase oil-soluble demulsifier.
As a specific implementation mode of the method for processing inferior heavy oil, in the invention, in S2, the continuous deposition is performed by adopting a continuous deposition device, the operation is performed in a liquid-liquid separation operation mode, the operation temperature is 100-200 ℃, wherein overflow materials are materials discharged from an overflow outlet of the continuous deposition device, and underflow materials are materials discharged from an underflow outlet of the continuous deposition device.
As a specific embodiment of the method for processing inferior heavy oil, in the invention, in S2, the weight yield of overflow materials is 70-90% based on 100% of the total weight of the feeding materials of the continuous deposition device.
As a specific embodiment of the above-mentioned method for processing inferior heavy oil according to the present invention, in S3, the unconverted oil may be a fraction greater than 360 ℃ or a fraction greater than 460 ℃ according to the requirement, where the distillation range of the unconverted oil may be modulated according to the production requirement, and preferably, the distillation range cutting point of the unconverted oil is 360-460 ℃.
As a specific embodiment of the method for processing the inferior heavy oil, in the invention, in S4, the external throwing amount of the tail oil accounts for 3-5wt% of the feeding amount of the inferior heavy oil raw material. The tail oil is a part of unconverted oil and the part with the worst quality of unconverted oil, and contains some coked catalyst, coked material and the like.
As a specific embodiment of the method for processing inferior heavy oil according to the present invention, in S4, the reaction temperature of the deep hydrocracking reaction is 30-70 ℃ higher than the reaction temperature of the shallow hydrocracking reaction in S1, the reaction pressure of the deep hydrocracking reaction is 2-8MPa higher than the reaction pressure of the shallow hydrocracking reaction in S1, and the volume air space velocity of the deep hydrocracking reaction is 0-1.8h lower than the volume air space velocity of the shallow hydrocracking reaction in S1 -1 。
As a specific embodiment of the above method for processing inferior heavy oil according to the present invention, in S4, the process operating conditions of the deep hydrocracking reaction are as follows:
the reaction temperature is 400-500 ℃, the reaction pressure is 10-20MPa, the volume ratio of hydrogen to oil at the inlet of the reactor is 1000-2500, the dosage of the catalyst corresponding to each gram of unconverted oil is 100-20000 mug, and the volume space velocity is 0.2-1h based on the metal content -1 The per pass conversion is 60-90wt%.
As a specific embodiment of the above method for processing inferior heavy oil according to the present invention, in S4, the process operating conditions of the deep hydrocracking reaction are as follows:
the reaction temperature is 430-480 ℃, the reaction pressure is 16-18MPa, the volume ratio of hydrogen to oil at the inlet of the reactor is 1500-2000, the dosage of the catalyst corresponding to each gram of unconverted oil is 200-10000 mug based on the metal content, and the volume space velocity is 0.2-0.5h -1 The single pass conversion is 70-90wt%。
The gas-liquid separation operation and the process conditions thereof and the like in the processing methods S1 and S4 of the inferior heavy oil are not particularly required, and the inferior heavy oil is separated by a thermal high score in the actual operation process.
Meanwhile, the invention does not have specific requirements on the operation of fractionation in S4, the process conditions thereof and the like, and can be processed according to atmospheric and vacuum fractionation in the actual operation process.
In addition, the catalyst used in the above processing methods S1 and S4 of the inferior heavy oil provided by the present invention is a slurry bed catalyst conventionally used in the art, and mainly includes a solid particle catalyst, a water-soluble catalyst, an oil-soluble catalyst, a microemulsion catalyst, and the like. In some embodiments of the present invention, the slurry bed catalyst used in S1 and S4 may be, for example, an oil-soluble molybdenum catalyst.
On the other hand, the invention also provides a processing system of the inferior heavy oil, wherein the processing system of the inferior heavy oil comprises: the device comprises a first section of slurry bed hydrogenation reactor, a first gas-liquid separation device, a continuous deposition device, a fractionation device, a second section of slurry bed hydrogenation reactor and a second gas-liquid separation device;
the first-stage slurry bed hydrogenation reactor and the second-stage slurry bed hydrogenation reactor are respectively provided with an inlet and an outlet, the outlet of the first-stage slurry bed hydrogenation reactor is communicated with the inlet of the first gas-liquid separation device, the liquid phase outlet of the first gas-liquid separation device is communicated with the inlet of the continuous deposition device, the overflow material outlet of the continuous deposition device is communicated with the inlet of the second-stage slurry bed hydrogenation reactor through the fractionating device, and the outlet of the second-stage slurry bed hydrogenation reactor is communicated with the fractionating device through the second gas-liquid separation device.
As a specific embodiment of the system for processing inferior heavy oil, the system further comprises a mixing device, wherein an underflow material outlet of the continuous deposition device is communicated with an inlet of the mixing device, so that the mixing of the inferior heavy oil, the catalyst and the underflow material in the mixing device is realized.
The system further comprises a first enhanced hydrogen mixing device, wherein the first enhanced hydrogen mixing device is provided with a first inlet, a second inlet and an outlet, and the outlet of the first enhanced hydrogen mixing device is communicated with the inlet of the first slurry bed hydrogenation reactor.
The first inlet and the second inlet of the first enhanced hydrogen mixing device are used for introducing raw oil, a catalyst and hydrogen into the first enhanced hydrogen mixing device, when the first inlet is used for introducing the raw oil and the catalyst, the second inlet is used for introducing the hydrogen, otherwise, when the first inlet is used for introducing the hydrogen, the second inlet is used for introducing the raw oil and the catalyst.
The system further comprises a second enhanced hydrogen mixing device, wherein the second enhanced hydrogen mixing device is provided with a first inlet, a second inlet and an outlet, the first inlet or the second inlet of the second enhanced hydrogen mixing device is communicated with the outlet of the fractionation device, and the outlet of the second enhanced hydrogen mixing device is communicated with the inlet of the second slurry bed hydrogenation reactor.
The first inlet and the second inlet of the second enhanced hydrogen mixing device are used for introducing the rest part of unconverted oil which is thrown out of tail oil, the catalyst and hydrogen into the second enhanced hydrogen mixing device, when the first inlet is used for introducing the rest part of unconverted oil which is thrown out of tail oil and the catalyst, the second inlet is used for introducing hydrogen, otherwise, when the first inlet is used for introducing hydrogen, the second inlet is used for introducing the rest part of unconverted oil which is thrown out of tail oil and the catalyst.
In a specific embodiment of the system for processing inferior heavy oil according to the present invention, the first enhanced hydrogen mixing device and the second enhanced hydrogen mixing device are micro-channel devices, supergravity devices, spraying devices or ultrasonic devices.
As a specific embodiment of the system for processing inferior heavy oil according to the present invention, the continuous deposition device is a cone thickener or a high efficiency thickener.
In the invention, the first reinforced hydrogen mixing device, the second reinforced hydrogen mixing device, the first stage slurry bed hydrogenation reactor, the first gas-liquid separation device (first thermal high fraction), the continuous deposition device, the fractionation device, the second stage slurry bed hydrogenation reactor and the second gas-liquid separation device (second thermal high fraction) are all conventional equipment used in the field.
The processing method and the processing system of the inferior heavy oil provided by the invention have the beneficial technical effects that:
(1) The invention utilizes the reinforced hydrogen mixing device, increases the hydrogen mass transfer efficiency and reduces the reaction pressure; and the two sections of slurry bed hydrogenation reactors (namely a first section of slurry bed hydrogenation reactor and a second section of slurry bed hydrogenation reactor) are used for controlling the hydrocracking degree in the reactor through the technological conditions of temperature, airspeed and the like, so that the zonal conversion of difficult and easy-to-convert components in a poor heavy oil system is realized.
(2) For a typical thermal cracking reaction, as the reaction proceeds, saturated fractions and asphaltenes increase as aromatic fractions and gum are cracked and polymerized, and while each component undergoes structural changes, there is mass flow between the components, such as disproportionation of gum to convert gum to saturated fractions and asphaltenes, aromatic to asphaltenes, etc. This eventually results in a disruption of the adsorption equilibrium between asphaltenes and gum, causing asphaltenes to lose peptized state and to produce flocculated agglomerates, forming a so-called second liquid phase which deposits on the furnace tube and reactor wall surfaces and converts to char. In order to solve the problems, the low-quality heavy oil is subjected to shallow hydrocracking through the lower temperature and higher space velocity in the first-stage slurry bed hydrogenation reactor, the reaction depth is controlled, and the coking precursor (so-called second liquid phase) is prevented from further condensing to generate coke; the characteristic that the compatibility of shallow hydrocracking residual oil is poor and a colloid system is unstable is utilized, and a composite flocculant is added to further destroy the colloid stability of the shallow hydrocracking residual oil, improve the separation speed and the separation efficiency, and enable coke precursors easy to coke such as asphaltene to be aggregated and separated before deep cracking. And then the unconverted oil with asphaltene removed is subjected to deep cracking in a second-stage slurry bed hydrogenation reactor, so that the conversion rate is improved. In addition, the invention mixes the heavy components such as asphaltene deposited in the continuous deposition device with fresh raw materials, and the colloid/polar aromatic hydrocarbon in the fresh raw materials is sufficient, and the whole colloid system reaches phase stability again after the heavy components such as the deposited asphaltene are added, and returns to the first-stage slurry bed hydrogenation reactor for shallow cracking.
In summary, the method provided by the invention can ensure the product yield, greatly reduce coking and blocking of equipment such as a slurry bed hydrogenation reactor, a follow-up fractionating tower and the like, and prolong the operation stability and the operation period of the device.
(3) The composite flocculant used in the invention comprises the bi-hexadecyl dimethyl ammonium bromide, the cationic polyacrylamide, the polymeric aluminum ferric silicate and the polyether reverse phase oil-soluble demulsifier, wherein the bi-hexadecyl dimethyl ammonium bromide can curl long chains of asphaltene polymers or agglomerate and reduce viscosity, and the polyether reverse phase oil-soluble demulsifier is cooperated to demulsifie asphaltene wrapped by colloid, so that the flocculation effect of the polymeric aluminum ferric silicate and the cationic polyacrylamide is enhanced, and the flocculation sedimentation of the agglomerated asphaltene is caused, and finally the purpose of phase separation is achieved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for the description of the embodiments will be briefly described, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings may be obtained according to the drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of a system for processing inferior heavy oil according to embodiment 1 of the present invention.
The main reference numerals illustrate:
1. a first enhanced hydrogen mixing device;
2. a first stage slurry bed hydrogenation reactor;
3. a first gas-liquid separation device;
4. a continuous deposition device;
5. a fractionation device;
6. a second enhanced hydrogen mixing device;
7. a second stage slurry bed hydrogenation reactor;
8. a second gas-liquid separation device;
9. raw oil and catalyst;
10. hydrogen gas;
11. a composite flocculant;
12. tail oil.
Detailed Description
It should be noted that the term "comprising" in the description of the invention and the claims and any variations thereof in the above-described figures is intended to cover a non-exclusive inclusion, such as a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements that are expressly listed or inherent to such process, method, article, or apparatus.
In the present invention, the terms "disposed," "connected/in communication" and "connected/in communication" should be construed broadly. For example, "connected/connected" may be in a fixed connection, a removable connection, or a unitary construction; may be a mechanical connection, or an electrical connection; may be directly connected, or indirectly connected through intervening media, or may be in internal communication between two devices, elements, or components. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
The "range" disclosed herein is given in the form of a lower limit and an upper limit. There may be one or more lower limits and one or more upper limits, respectively. The given range is defined by selecting a lower limit and an upper limit. The selected lower and upper limits define the boundaries of the particular ranges. All ranges defined in this way are combinable, i.e. any lower limit can be combined with any upper limit to form a range. For example, ranges of 60-120 and 80-110 are listed for specific parameters, with the understanding that ranges of 60-110 and 80-120 are also contemplated. Furthermore, if the minimum range values listed are 1 and 2 and the maximum range values listed are 3,4 and 5, then the following ranges are all contemplated: 1-3, 1-4, 1-5, 2-3, 2-4 and 2-5.
In the present invention, unless otherwise indicated, the numerical range "a-b" represents a shorthand representation of any combination of real numbers between a and b, where a and b are both real numbers. For example, the numerical range "0-5" means that all real numbers between "0-5" have been listed throughout this disclosure, and "0-5" is only a shorthand representation of a combination of these values.
In the present invention, all the embodiments and preferred embodiments mentioned in the present invention may be combined with each other to form new technical solutions, unless otherwise specified.
In the present invention, all technical features mentioned in the present invention and preferred features may be combined with each other to form a new technical solution unless specifically stated otherwise.
The present invention will be further described in detail with reference to the accompanying drawings, figures and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. The following described embodiments are some, but not all, examples of the present invention and are merely illustrative of the present invention and should not be construed as limiting the scope of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products commercially available without the manufacturer's attention.
Example 1
The embodiment provides a system for processing inferior heavy oil, the schematic structural diagram of which is shown in fig. 1, and as can be seen from fig. 1, the system comprises:
the device comprises a first reinforced hydrogen mixing device 1, a second reinforced hydrogen mixing device 6, a first stage slurry bed hydrogenation reactor 2, a first gas-liquid separation device 3, a continuous deposition device 4, a fractionation device 5, a second stage slurry bed hydrogenation reactor 7, a second gas-liquid separation device 8 and a mixing device (not shown in the figure);
the first reinforced hydrogen mixing device 1 and the second reinforced hydrogen mixing device 6 are respectively provided with a first inlet, a second inlet and an outlet, the outlet of the first reinforced hydrogen mixing device 1 is communicated with the inlet of the first-stage slurry bed hydrogenation reactor 2, the outlet of the first-stage slurry bed hydrogenation reactor 2 is communicated with the inlet of the first gas-liquid separation device 3, the liquid phase outlet of the first gas-liquid separation device 3 is communicated with the inlet of the continuous deposition device 4, the overflow material outlet of the continuous deposition device 4 is communicated with the first inlet of the second reinforced hydrogen mixing device 6 through the fractionation device 5, the outlet of the second reinforced hydrogen mixing device 6 is communicated with the inlet of the second-stage slurry bed hydrogenation reactor 7, and the outlet of the second-stage slurry bed hydrogenation reactor 7 is communicated with the fractionation device 5 through the second gas-liquid separation device 8;
the underflow material outlet of the continuous deposition device 4 is communicated with the inlet of the mixing device, so that poor heavy oil, catalyst and underflow materials are uniformly mixed in the mixing device.
In this embodiment, the enhanced hydrogen mixing device may be any one of a micro-channel device, a hypergravity device, a spraying device, or an ultrasonic device.
In this embodiment, the continuous deposition device may be a cone thickener or a high efficiency thickener.
Example 2
The embodiment provides a method for processing inferior heavy oil, which is implemented by using the processing system of inferior heavy oil provided in embodiment 1, and specifically includes:
s1: the vacuum residuum raw material and oil-soluble molybdenum catalyst (conventional catalyst used in the field), namely raw oil and catalyst 9 enter a first enhanced hydrogen mixing device 1 and are fully mixed with hydrogen 10 in the first enhanced hydrogen mixing device 1, the obtained mixed material enters a first stage slurry bed hydrogenation reactor 2 for shallow hydrocracking reaction, and a product obtained by the reaction is subjected to high-pressure gas-liquid separation in a first gas-liquid separation device 3 to obtain a first liquid phase product;
wherein the properties of the vacuum residuum feedstock are shown in table 1.
TABLE 1 Properties of vacuum residuum feedstock
As can be seen from Table 1 above, the vacuum residuum feedstock used in this example is very high in viscosity, char, metal content and is a poor quality feedstock that is difficult to process with conventional residuum hydrogenation equipment (e.g., ebullated bed/fixed bed, etc.).
S2: adding a composite flocculant 11 into the first liquid-phase product, wherein the adding amount of the composite flocculant 11 is 0.05% of the weight of the first liquid-phase product, the composite flocculant 11 is formed by mixing dicetyl dimethyl ammonium bromide, cationic polyacrylamide, polyaluminum ferric silicate and polyether reverse phase oil-soluble demulsifier, the weight ratio of the four is 6:1:50:40, the obtained mixture is subjected to continuous deposition separation operation in a continuous deposition device 4, the operation temperature is 150 ℃, overflow materials are obtained at an overflow outlet of the continuous deposition device 4 after the operation is finished, the weight yield of the overflow materials is 80%, and underflow materials (which are oil rich in asphaltenes) are obtained at an underflow outlet of the continuous deposition device 4.
S3: fractionating the overflow material in a fractionating device 5 to obtain unconverted oil, wherein the distillation range cutting point of the unconverted oil is 460 ℃; and (2) sending the underflow material to a mixing device, mixing the underflow material with a vacuum residue raw material and an oil-soluble molybdenum catalyst, recycling the obtained mixed material to the S1, fully mixing the mixed material with hydrogen in a first enhanced hydrogen mixing device 1, and continuously treating according to the flow of the S1.
S4: the rest part of unconverted oil which is 5wt% of tail oil 12 and oil-soluble molybdenum catalyst (conventional catalyst used in the field) which are obtained by throwing out the tail oil 12 from the feed amount of vacuum residue raw material are led into a second enhanced hydrogen mixing device 6 from a first inlet of the second enhanced hydrogen mixing device 6, hydrogen 10 is led into the second enhanced hydrogen mixing device 6 from a second inlet of the second enhanced hydrogen mixing device 6, the rest part of unconverted oil which is thrown out of the tail oil 12 and the oil-soluble molybdenum catalyst are fully mixed in the second enhanced hydrogen mixing device 6, the obtained mixed material is led into a second-stage slurry bed hydrogenation reactor 7, deep hydrocracking reaction is carried out in the second-stage slurry bed hydrogenation reactor 7 under the existence of the oil-soluble molybdenum catalyst and the hydrogen, the product obtained by the reaction is subjected to high-pressure gas-liquid separation in a second gas-liquid separation device 8, and then the second liquid-phase product is led into a fractional distillation device 5 together with overflow material, and finally the light oil product is obtained.
Wherein, the technological operation conditions and test results of the shallow hydrocracking reaction and the deep hydrocracking reaction are shown in table 2; the parameters of the first liquid phase product are shown in table 3.
Example 3
The embodiment provides a method for processing inferior heavy oil, which is implemented by using the processing system of inferior heavy oil provided in embodiment 1, and is different from embodiment 2 only in that the weight ratio of the bi-hexadecyl dimethyl ammonium bromide, the cationic polyacrylamide, the polyaluminum ferric silicate and the polyether reverse phase oil-soluble demulsifier in the composite flocculant is 3:1:25:20.
Example 4
The embodiment provides a method for processing inferior heavy oil, which is implemented by using the processing system of inferior heavy oil provided in embodiment 1, and is different from embodiment 2 only in that the weight ratio of the bi-hexadecyl dimethyl ammonium bromide, the cationic polyacrylamide, the polyaluminum ferric silicate and the polyether reverse phase oil-soluble demulsifier in the composite flocculant is 10:1:50:50.
Example 5
The present embodiment provides a method for processing inferior heavy oil, which is implemented by using the processing system of inferior heavy oil provided in embodiment 1, and differs from embodiment 2 only in that the adding amount of the composite flocculant is 0.01% of the weight of the first liquid phase product.
Example 6
The present embodiment provides a method for processing inferior heavy oil, which is implemented by using the processing system of inferior heavy oil provided in embodiment 1, and differs from embodiment 2 only in that the adding amount of the composite flocculant is 0.2% of the weight of the first liquid phase product.
Example 7
The present embodiment provides a method for processing inferior heavy oil, which is implemented by using the processing system for inferior heavy oil provided in embodiment 1, and differs from embodiment 2 only in that the operating conditions of the first slurry bed reactor are changed, the specific operating conditions are shown in table 2, and the property parameters of the first liquid phase product obtained in this embodiment are shown in table 3.
Example 8
The present embodiment provides a method for processing inferior heavy oil, which is implemented by using the processing system for inferior heavy oil provided in embodiment 1, and differs from embodiment 2 only in that the operating conditions of the second slurry bed reactor are changed, the specific operating conditions are shown in table 2, and the coke formation condition in this embodiment is shown in table 4.
Comparative example 1
The comparative example provides a method for processing inferior heavy oil, which is realized by using the processing system of inferior heavy oil provided in embodiment 1, and the difference from embodiment 2 is that the added composite flocculant only comprises cationic polyacrylamide and polyaluminum ferric silicate, and the weight ratio of the cationic polyacrylamide to the polyaluminum ferric silicate is 1:50.
Comparative example 2
The present comparative example provides a process for the processing of inferior heavy oil by processing the vacuum residuum feedstock used in example 2 using a conventional two-stage serial slurry bed residuum hydrocracking unit.
In this comparative example, the process conditions and test results of the reaction are shown in Table 2.
TABLE 2 shallow hydrocracking reaction and process operating conditions and test results for the deep hydrocracking reaction
* Different overflow components have different conversion rates
TABLE 3 Property parameters of the first liquid phase products obtained in example 2 and example 7
The parameters of the overflow materials described in examples 2 to 6 and comparative example 1 according to the present invention and the scorch conditions of the products in examples 2 to 6 and comparative example 1 to comparative example 2 are shown in Table 4 below.
Table 4 the parameters of the nature of the overflow materials in examples 2-6 and comparative example 1 and the scorch of the products in examples 2-6 and comparative example 1-2
As can be seen from comparison of experimental data of example 1 and comparative example 1 shown in table 4 above, the complex modified flocculant used in example 1 of the present invention enhances flocculation effect of the cationic flocculant compared with the industrially conventionally used cationic example metal flocculant used in comparative example 1, causes flocculation sedimentation of flocculated aggregates of agglomerated asphaltenes, and reduces the content of asphaltenes in overflow components.
As can be seen from the experimental data of example 1 and comparative example 2 shown in Table 4 above, compared with the conventional two-stage series slurry bed process, the continuous deposition device in the processing method of inferior heavy oil provided by the embodiment of the invention separates asphaltene and coke precursor from the feed, so that the second-stage slurry bed hydrogenation reactor can still maintain very low coke formation rate under the premise of greatly increasing the temperature, the blocking condition of equipment and subsequent separation equipment is reduced, the operation period of the slurry bed device is greatly increased, the conversion rate of the device can also be increased under high temperature, and the problem of contradiction between the conversion rate and the operation period is solved.
The foregoing description of the embodiments of the invention is not intended to limit the scope of the invention, so that the substitution of equivalent elements or equivalent variations and modifications within the scope of the invention shall fall within the scope of the patent. In addition, the technical features and the technical features, the technical features and the technical invention can be freely combined for use.
Claims (22)
1. The processing method of the inferior heavy oil is characterized by comprising the following steps of:
s1: fully mixing inferior heavy oil, a catalyst and hydrogen, then carrying out shallow hydrocracking reaction, and carrying out gas-liquid separation on a product obtained by the reaction to obtain a liquid-phase product;
s2: mixing the liquid phase product with a composite flocculant, and then continuously depositing to separate and obtain overflow materials and underflow materials;
s3: fractionating the overflow material to obtain unconverted oil;
s4: and fully mixing the rest part of unconverted oil from which tail oil is thrown out, the catalyst and hydrogen, and then carrying out deep hydrocracking reaction, carrying out gas-liquid separation on the product obtained by the reaction to obtain a liquid-phase product, and then carrying out fractionation on the liquid-phase product alone or together with the overflow material to obtain a light oil product.
2. The method for processing inferior heavy oil according to claim 1, wherein the method further comprises: and mixing the underflow material with inferior heavy oil and a catalyst, and then fully mixing the obtained mixture with hydrogen.
3. The method for processing inferior heavy oil according to claim 1 or 2, wherein in S1, the inferior heavy oil comprises one or a combination of several of atmospheric residuum, vacuum residuum, deasphalted oil, oil sand pitch, high-viscosity crude oil, coal tar and coal liquefied heavy oil.
4. The method for processing inferior heavy oil according to claim 1 or 2, wherein in S1, the metal content in the inferior heavy oil is more than 200 μg/g based on the total weight of Ni and V, and the total content of gum and asphaltene is more than 30wt%.
5. The method for processing inferior heavy oil according to claim 1 or 2, wherein in S1, the catalyst used in the shallow hydrocracking reaction is a solid powder catalyst, a water-soluble catalyst or an oil-soluble catalyst, wherein the catalyst has a particle size of 0.01 to 100 μm.
6. The method for processing inferior heavy oil according to claim 1 or 2, wherein in S1, the process operation conditions of the shallow hydrocracking reaction are:
the reaction temperature is 350-420 ℃, the reaction pressure is 4-14MPa, the volume ratio of hydrogen to oil at the inlet of the reactor is 600-2000, the catalyst dosage corresponding to each gram of inferior heavy oil is 100-10000 mug based on the metal content, and the volume space velocity is 0.5-2h -1 The per pass conversion is 30-60wt%.
7. The method for processing inferior heavy oil according to claim 6, wherein in S1, the process operation conditions of the shallow hydrocracking reaction are:
the reaction temperature is 400-420 ℃, the reaction pressure is 10-12MPa, the volume ratio of hydrogen to oil at the inlet of the reactor is 1000-1500, the catalyst dosage corresponding to each gram of inferior heavy oil is 100-5000 mug based on the metal content, and the volume space velocity is 1-1.5h -1 The per pass conversion is 40-50wt%.
8. The method for processing inferior heavy oil according to claim 1, wherein in S2, the amount of the composite flocculant added is 0.01 to 0.2% by weight of the liquid phase product.
9. The method for processing inferior heavy oil according to claim 8, wherein in S2, the amount of the composite flocculant added is 0.05 to 0.1% by weight of the liquid phase product.
10. The method for processing inferior heavy oil according to any one of claims 1,8 to 9, wherein in S2, the composite flocculant comprises a quaternary ammonium salt surfactant, an organic polymeric flocculant, an inorganic polymeric flocculant and a reverse oil-soluble demulsifier in a weight ratio of 5 to 10:1 to 3:50 to 100:10 to 50;
preferably, the quaternary ammonium salt surfactant comprises one or a combination of a plurality of bi-hexadecyl dimethyl ammonium bromide, dodecyl trimethyl ammonium bromide, alkyl dimethyl ammonium chloride and octadecyl trimethyl ammonium bromide;
still preferably, the organic polymeric flocculant comprises one or a combination of several of cationic polyacrylamide, sodium polyacrylate, polyvinyl pyridinium and polyethyleneimine;
still preferably, the inorganic polymeric flocculant comprises one or a combination of several of polymeric aluminum ferric silicate, polymeric aluminum ferric sulfate, polymeric aluminum silicate and polymeric aluminum ferric phosphate;
still preferably, the reverse oil-soluble demulsifier comprises one or a combination of several of polyether reverse oil-soluble demulsifier, polypropylene oxide reverse oil-soluble demulsifier, polyamide reverse oil-soluble demulsifier and polytriethanolamine reverse oil-soluble demulsifier;
more preferably, the composite flocculant comprises a dicetyl dimethyl ammonium bromide, a cationic polyacrylamide, a polymeric aluminum ferric silicate and a polyether reverse phase oil soluble demulsifier.
11. The process for producing low-grade heavy oil according to any one of claims 1,8 to 9, wherein in S2, the continuous deposition is performed by a continuous deposition apparatus, operated in a liquid-liquid separation mode, at an operation temperature of 100 to 200 ℃, wherein overflow material is discharged from an overflow outlet of the continuous deposition apparatus, and underflow material is discharged from an underflow outlet of the continuous deposition apparatus.
12. The method for processing inferior heavy oil according to claim 11, wherein in S2, the weight yield of overflow material is 70 to 90% based on 100% of the total weight of the feed to the continuous deposition apparatus.
13. The method for processing inferior heavy oil according to claim 1 or 2, wherein in S3, the cut point of the distillation range of the unconverted oil is 360 to 460 ℃.
14. The method for processing inferior heavy oil according to claim 1 or 2, wherein in S4, the external throwing amount of the tail oil is 3-5wt% of the feeding amount of the inferior heavy oil raw material.
15. The method for processing inferior heavy oil according to claim 1, wherein in S4, the reaction temperature of the deep hydrocracking reaction is 30-70 ℃ higher than the reaction temperature of the shallow hydrocracking reaction in S1, the reaction pressure of the deep hydrocracking reaction is 2-8MPa higher than the reaction pressure of the shallow hydrocracking reaction in S1, and the volume air space velocity of the deep hydrocracking reaction is 0-1.8h lower than the volume air space velocity of the shallow hydrocracking reaction in S1 -1 。
16. The method for processing inferior heavy oil according to claim 1 or 15, wherein in S4, the process operation conditions of the deep hydrocracking reaction are:
the reaction temperature is 400-500 ℃, the reaction pressure is 10-20MPa, the volume ratio of hydrogen to oil at the inlet of the reactor is 1000-2500, the dosage of the catalyst corresponding to each gram of unconverted oil is 100-20000 mug, and the volume space velocity is 0.2-1h based on the metal content -1 The single pass conversion is 60-90wt%.
17. The method for processing inferior heavy oil according to claim 16, wherein in S4, the process operation conditions of the deep hydrocracking reaction are:
the reaction temperature is 430-480 ℃, the reaction pressure is 16-18MPa, the volume ratio of hydrogen to oil at the inlet of the reactor is 1500-2000, the dosage of the catalyst corresponding to each gram of unconverted oil is 200-10000 mug based on the metal content, and the volume space velocity is 0.2-0.5h -1 The per pass conversion is 70-90wt%.
18. The utility model provides a processing system of heavy oil of inferior quality, its characterized in that, the processing system of heavy oil of inferior quality includes: the device comprises a first section of slurry bed hydrogenation reactor, a first gas-liquid separation device, a continuous deposition device, a fractionation device, a second section of slurry bed hydrogenation reactor and a second gas-liquid separation device;
the first-stage slurry bed hydrogenation reactor and the second-stage slurry bed hydrogenation reactor are respectively provided with an inlet and an outlet, the outlet of the first-stage slurry bed hydrogenation reactor is communicated with the inlet of the first gas-liquid separation device, the liquid phase outlet of the first gas-liquid separation device is communicated with the inlet of the continuous deposition device, the overflow material outlet of the continuous deposition device is communicated with the inlet of the second-stage slurry bed hydrogenation reactor through the fractionating device, and the outlet of the second-stage slurry bed hydrogenation reactor is communicated with the fractionating device through the second gas-liquid separation device.
19. The system for processing inferior heavy oil of claim 18, further comprising a blending device, wherein the underflow outlet of the continuous deposition device is in communication with the inlet of the blending device to achieve uniform blending of the inferior heavy oil, catalyst and underflow in the blending device.
20. The system for processing inferior heavy oil according to claim 18 or 19, further comprising a first enhanced hydrogen mixing device, the first enhanced hydrogen mixing device being provided with a first inlet, a second inlet and an outlet, the outlet of the first enhanced hydrogen mixing device being in communication with the inlet of the first stage slurry bed hydrogenation reactor;
preferably, the system further comprises a second enhanced hydrogen mixing device, wherein the second enhanced hydrogen mixing device is provided with a first inlet, a second inlet and an outlet, the first inlet or the second inlet of the second enhanced hydrogen mixing device is communicated with the outlet of the fractionation device, and the outlet of the second enhanced hydrogen mixing device is communicated with the inlet of the second-stage slurry bed hydrogenation reactor.
21. The system for processing inferior heavy oil according to claim 20, wherein the first and second enhanced hydrogen mixing devices are micro-channel devices, supergravity devices, spraying devices or ultrasonic devices.
22. The system for processing low-grade heavy oil according to claim 18 or 19, wherein the continuous deposition device is a cone thickener or a high efficiency thickener.
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| CN202111622969.9A CN116355652A (en) | 2021-12-28 | 2021-12-28 | Processing method and system for inferior heavy oil |
| PCT/CN2022/136128 WO2023124769A1 (en) | 2021-12-28 | 2022-12-02 | Inferior heavy oil processing method and system |
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