CN108179028A - A kind of processing of heavy oil method and system - Google Patents

A kind of processing of heavy oil method and system Download PDF

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Publication number
CN108179028A
CN108179028A CN201711419863.2A CN201711419863A CN108179028A CN 108179028 A CN108179028 A CN 108179028A CN 201711419863 A CN201711419863 A CN 201711419863A CN 108179028 A CN108179028 A CN 108179028A
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heavy oil
product
low
plasma reactor
gas
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CN108179028B (en
Inventor
王洪彬
郑应绪
黄新龙
张婧帆
庞晓飞
亚飞
冯凌
周文琳
张国库
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Sinopec Engineering Group Co Ltd
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Sinopec Engineering Group Co Ltd
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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
    • 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
    • C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking 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
    • 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
    • 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
    • C10G2400/26—Fuel gas

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (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 present invention provides a kind of processing of heavy oil method and system.A kind of processing of heavy oil method, includes the following steps：Step A：Hydrogen-rich gas is made to react in low-temperature cold plasma reactor with heavy oil feedstock, generates the first product；The weight ratio of the hydrogen-rich gas and the heavy oil feedstock is 0.001~0.2:1, preferably 0.005~0.15:1；Step B：First product is made to carry out delayed coking, generates the second product；Step C：Gas-liquid phase component in second product is fractionated, obtains the product of different fractions.The present invention is based on the unique activity of plasma, strengthens conventional delayed coking reaction process with it, to activate feedstock oil, and then improve liquid oil yield, coking heater of the present invention need not inject vapor simultaneously, and technique waste water discharge capacity significantly reduces, more environmentally-friendly.

Description

A kind of processing of heavy oil method and system
Technical field
The present invention relates to chemical technology field, more particularly, to a kind of processing of heavy oil method and system.
Background technology
With the increasingly reduction of world petroleum resource, crude oil shows heaviness, in poor quality trend, what process generated Heavy oil (reduced crude and decompression residuum) ratio is higher and higher.How the comprehensive utilization ratio of existing resource especially heavy oil is improved Have become petroleum refining industry and be badly in need of the significant problem solved.
Conventional heavy oils processing technology mainly has plus two class technique of hydrogen and decarburization.
Heavy oil hydrogenation process mainly includes three kinds of fixed bed hydrogenation, boiling bed hydrogenation and floating bed hydrogenation technologies.It is wherein solid The technological process of fixed bed hydrogen addition technology and the relatively simple maturation of device structure, device is easy to operate, and product yield is high, technological deficiency master If the easy coking of catalyst, poisoning, the cycle of operation is short (generally 12 months), to the bad adaptability of inferior raw material；Ebullated bed adds Hydrogen technology can realize the online supplement of catalyst and outer row, the greater activity of catalyst reactor can be kept, with fixation Bed hydroprocessing technology compare can process high-sulfur, high carbon residue, high metal inferior heavy oil, there is higher conversion ratio, but the skill The deficiencies of art is big there are plant investment, and device structure is complicated, and catalyst attrition is big, and operating cost is high；Floating bed hydrogenation technology is The research hotspot in processing of heavy oil field in recent years is suitable for processing high metal, high carbon residue, high-sulfur, high acid value, highly viscous bad Reduced fuel oil, with high conversion rate, light oil yield is high, structure of reactor is relatively easy, the more low advantage of device operating cost, but should Sulfur content is higher in technical products, needs to carry out post-processing, in addition metal is higher with carbon residue in tail oil and contains catalyst powder End, tail oil can rationally using as limit the technique application an important technology difficult point.
Heavy oil decarbonization process mainly has delayed coking, visbreaking, solvent deasphalting and heavy oil catalytic cracking etc..Mesh Before, petroleum refining industry is still delay coking process technology using most heavy oil decarbonization process.Delayed Coking Technology has technique Simply, technology maturation, the advantages that equipment investment and operating cost are low, adaptability to raw material is strong, occupy in processing of heavy oil technique to Close consequence, however delayed coking there is also coke yield it is high the problems such as.
In view of this, it is special to propose the present invention.
Invention content
The first object of the present invention is to provide a kind of processing of heavy oil method, and the processing of heavy oil method is burnt compared to traditional delay Change method, coke production rate is low, and liquid yield significantly improves.
The second object of the present invention is a kind of heavy oil precessing system, change of the system to existing heavy oil precessing system It is small, reduce update difficulty.
In order to achieve the goal above, the present invention provides following technical schemes：
A kind of processing of heavy oil method, includes the following steps：
Step A：Hydrogen-rich gas is made to react in low-temperature cold plasma reactor with heavy oil feedstock, the first production of generation Object；The weight ratio of the hydrogen-rich gas and the heavy oil feedstock is 0.001~0.2:1, preferably 0.005~0.15:1；
Step B：First product is made to carry out delayed coking, generates the second product；
Step C：Gas-liquid phase component in second product is fractionated, obtains the product of different fractions.
Plasma is the 4th state substance in addition to gas-liquid-solid three-state tri-state substance.Plasma is by several Typical particle groups Into i.e. electronics, cation, anion, the atom of excitation state or molecule, the atom of ground state or molecule etc..Due to negative electricity therein Lotus sum is equal to positive charge sum, and macroscopic view is referred to as plasma in electroneutral.In plasma containing a large amount of ions, High energy electron, the atom of excitation state or molecule etc. can provide a large amount of active groups for being prone to chemical reaction.According to temperature Difference, plasma can be divided into two classes：High-temperature plasma (such as sun, nuclear fusion plasma) and low-temperature plasma Body.And low temperature plasma can be divided into hot plasma (such as electric arc electric discharge and burning generate plasma) and it is cold from Daughter (such as plasma of glow discharge, corona discharge, dielectric barrier discharge generation).Plasma is as novel point a kind of Sub- activation method, it is considered to be new cleaning fuel technology.With the development of plasma technique, in the application of chemical field Also it is more and more.
The present invention is based on the unique activity of plasma, strengthens conventional delayed coking reaction process with it, to activate Feedstock oil, and then improve liquid oil yield.
In the present invention, first in step, hydrogen-rich gas generation plasma is converted into excited state particle or free radical, together When, part material heavy oil molecules carry out cracking reaction, be cracked into more than two short chain free radicals, using hydrogen-rich gas grade from Sub- state protects these short chain free radicals, avoids short chain free radical secondary coupling again, while excitation state hydrogen-rich gas particle can also be with portion Divide the heavy oil molecules of activated state that hydrogenation reaction occurs.It can be seen that on the one hand the low-temperature cold plasma reaction of the present invention activates Heavy oil feedstock, and then improve the reaction rate of subsequent delay coking and reduce energy consumption of reaction；On the other hand part has occurred to add Hydrogen reacts, and then reduces the reacting dose of subsequent delay coking, also improves liquid yield.
Later, delayed coking reaction occurs in stepb for the present invention, and the raw material heavy oil that will be activated is by heating stove heat It is brought rapidly up to pyrogenetic reaction temperature, pyrogenetic reaction is carried out into coke drum.
Last fractionation is according to product it needs to be determined that fraction section, common are the product of value has gasoline, diesel oil, wax Oil, wax slop, gas etc..
In the present invention, the weight ratio of the hydrogen-rich gas and the heavy oil feedstock is 0.001~0.2:1, such as 0.001: 1、0.003:1、0.005:1、0.007:1、0.01:1、0.05:1、0.1:1、0.15:1、0.17:1、0.2:1 etc., preferably 0.005 ~0.15:1.
The above processing method of the present invention at least improves 4 percentage points compared to traditional delayed coking method, liquid yield, Correspondingly, coke rate at least reduces by 5 percentage points.
The above processing method of the present invention can also be improved from the following aspect：
Preferably, the reaction temperature in the low-temperature cold plasma reactor be 100 DEG C~400 DEG C, preferably 180 DEG C~ 350℃；
The activation degree of reaction temperature relationship raw material heavy oil in low-temperature cold plasma reactor and plus hydrogen degree, not Reaction temperature is higher, and liquid yield is higher.Reaction temperature is excessively high may to occur carbochain lengthening, be unfavorable for heavy oil modification.Through sieve Choosing, the reaction temperature of optimization are 100 DEG C~400 DEG C, for example, 100 DEG C, 120 DEG C, 140 DEG C, 150 DEG C, 200 DEG C, 250 DEG C, 300 DEG C, 330 DEG C, 350 DEG C, 370 DEG C, 400 DEG C etc., preferably 180 DEG C~350 DEG C.
Preferably, the reaction temperature of the delayed coking is 400 DEG C~550 DEG C, preferably 475 DEG C~525 DEG C.
The reaction temperature of delayed coking was both related with the quality of raw material heavy oil, also had with the plasma reaction of back Close, through screening, to obtain higher liquid yield, preferred reaction temperature is 475 DEG C, 480 DEG C, 490 DEG C, 500 DEG C, 510 DEG C, 520 DEG C or 525 DEG C of grades (please being changed according to claim range).
Preferably, after reacting in the low-temperature cold plasma reactor and before the delayed coking reaction Also carry out：
First product is fractionated, is divided into light component and heavy constituent；The heavy constituent is made to carry out the delay coke Change.
The light oil produced after plasma reaction is separated in advance at this time, and heavy constituent is only subjected to delay coke Change, production efficiency can be improved.
Preferably, the gas of the light component is made to return to the low-temperature cold plasma reactor the reaction was continued.
Containing a large amount of hydrogen-rich gases in light components, these hydrogen-rich gases are returned into low-temperature cold plasma reactor, both It can recycle, improve resource utilization, and the effect of vapor in conventional delayed coking technique can be served as, improve Fluid linear speed, slows down carbon deposition phenomenon.
The present invention is not restricted the back amount of gas in light components, such as according to feedstock oil during initial reaction and hydrogen-rich The ratio of gas, the gas and the ratio of raw material heavy oil that this part can return to also are located in the range of this, and since loss causes to compare Example may smaller.
Preferably, the hydrogen-rich gas is one or more mixing in hydrogen, methane, ethane and propane.
These hydrogen-rich gases will not introduce exogenous impurity, reduce product quality.The present invention only makees hydrogen-rich gas above-mentioned row It lifts, practical application is not limited to this.
Preferably, the heavy oil feedstock is reduced crude, decompression residuum, catalytic slurry, heavy crude, heavy crude, takes off One or more of oil asphalt and refinery's trowel used for plastering oil.
These heavy oil feedstocks are conventional inferior raw material, the present invention only make it is above-mentioned enumerate, practical application is not limited to this.
Preferably, it further includes：By the gas fractionated out in the step C return the low-temperature cold plasma reactor after Continuous reaction.
Equally, it by this portion gas reuse, can both recycle, and improve resource utilization, and biography can be served as The effect of vapor, improves fluid linear speed, slows down carbon deposition phenomenon in system delay coking process.
The present invention is not restricted the gas back amount in final fraction, such as according to feedstock oil during initial reaction and hydrogen-rich The ratio of gas, the gas and the ratio of raw material heavy oil that this part can return to also are located in the range of this, and since loss causes to compare Example may smaller.
Preferably, it is further included before the step A：
The hydrogen-rich gas is preheated to 50 DEG C~300 DEG C, preferably 120 DEG C~260 DEG C；
The heavy oil feedstock is preheated to 100 DEG C~400 DEG C, preferably 180 DEG C~350 DEG C.
The contacting efficiency of hydrogen-rich gas and heavy oil feedstock is improved by preheating, improves active rate and effect.
With the corresponding system of above-mentioned processing method of the present invention, structure is as follows：
Including passing through the sequentially connected low-temperature cold plasma reactor of pipeline, delayed coking unit and fractionating column；
The low-temperature cold plasma reactor is used for：Hydrogen-rich gas is made to be reacted with heavy oil feedstock in low-temperature cold plasma It reacts in device, generates the first product；The weight ratio of the hydrogen-rich gas and the heavy oil feedstock is 0.001~0.2:1, it is excellent Select 0.005~0.15:1；
The delayed coking unit is used for：First product is made to carry out delayed coking, generates the second product；
The fractionating column is used for：Gas-liquid phase component in second product is fractionated, obtains the production of different fractions Product.
The raw material that the system improves liquid yield is described above.
The delayed coking unit of the present invention includes heating furnace unit and coke drum unit.
Preferably, it is also associated with another fractionation between the low-temperature cold plasma reactor and the delayed coking unit Tower.
Two fractionating columns of setting be successively fractionated twice, improve reaction efficiency.
Preferably, the fractionating column and another fractionating column are equipped with gas discharge outlet, and the gas discharge outlet of the two is equal It is connect by pipeline with the low-temperature cold plasma reactor.
Such structure facilitates in the gas backstreaming to low-temperature cold plasma reactor in fraction, and it is anti-to participate in plasma It should.
Preferably, the low-temperature cold plasma reactor is dielectric barrier discharge reactor, such as parallel plate type or same Shaft type dielectric barrier discharge reactor.But the type of reactor of the present invention is not limited to that.
To sum up, compared with prior art, invention achieves following technique effects：
(1) coke rate of the invention is low；
(2) liquid yield of the invention is high；
(3) present invention need not inject vapor, and technique waste water discharge capacity significantly reduces, more environmentally-friendly；
(4) present invention recycles gas, reduces consumption of raw materials, saves the energy；
Therefore, the alternative traditional delay coking process of technique of the invention, and generate huge economic value and society Benefit.
Description of the drawings
It, below will be to specific in order to illustrate more clearly of the specific embodiment of the invention or technical solution of the prior art Embodiment or attached drawing needed to be used in the description of the prior art are briefly described, it should be apparent that, in being described below Attached drawing is some embodiments of the present invention, for those of ordinary skill in the art, before not making the creative labor It puts, can also be obtained according to these attached drawings other attached drawings.
Fig. 1 is the route map of processing of heavy oil that the embodiment of the present invention 1 provides.
Specific embodiment
Technical scheme of the present invention is clearly and completely described below in conjunction with the drawings and specific embodiments, but It is it will be understood to those of skill in the art that following described embodiment is part of the embodiment of the present invention rather than whole Embodiment is merely to illustrate the present invention, and is not construed as limiting the scope of the invention.Based on the embodiments of the present invention, ability Domain those of ordinary skill all other embodiments obtained without making creative work, belong to guarantor of the present invention The range of shield.The person that is not specified actual conditions in embodiment, the condition suggested according to normal condition or manufacturer carry out.Agents useful for same Or production firm person is not specified in instrument, is the conventional products that can be obtained by commercially available purchase.
Embodiment 1
A kind of heavy oil precessing system and method
The system of the embodiment includes：By the sequentially connected low-temperature cold plasma reactor of pipeline, the first fractionating column, Delayed coking unit and after-fractionating tower.
First fractionating column and after-fractionating tower are equipped with gas discharge outlet, the gas discharge outlet of the two by pipeline with it is low Warm cold plasma reaction device connection.
Low-temperature cold plasma reactor is dielectric barrier discharge reactor.
Route using the system processing heavy oil is as shown in Figure 1：
Gas raw material (hydrogen) is preheating to 150 DEG C and enters low-temperature cold plasma reactor top by pipeline, and feedstock oil is pre- Heat enters low-temperature cold plasma reactor upper side to 280 DEG C by pipeline；Gas raw material and feedstock oil low temperature cold etc. from Reacted in daughter reactor, low-temperature cold plasma reactor be parallel plate type dielectric barrier discharge reactor, low temperature cold The temperature control of plasma reactor is at 280 DEG C, and the mass values of the gas raw material and feedstock oil are 0.08, after reaction Material enters fractionating system through pipeline and is detached；Double distilled lease making pipeline after separation enters delayed coking unit, after separation Light component enters delayed coking list by the gas that pipeline enters in fractionating column or part light component after pipeline is mixed with heavy constituent Member, the gas and the mass values of feedstock oil entered through pipeline in the light component of delayed coking unit is about 0.05；Delayed coking The reaction temperature of unit is 500 DEG C, and generation oil gas enters fractionating column through pipeline；Delayed coking reaction generate oil gas fractionating column into Row product detaches, and obtains the products such as gas, gasoline, diesel oil, wax oil and wax slop；The portion gas product of fractionating column separation is by pipe Line returns to low-temperature cold plasma reactor and is reacted, the gas products (recyclegas product) and raw material that thus pipeline returns The mass values of oil are about 0.04.
Raw materials used oil nature is as shown in table 1 in the present embodiment, the present embodiment and conventional delayed coking process condition It is as shown in table 2 with the comparison of product distribution.As shown in Table 2, compared with conventional delayed coking technique, process of the invention increases Add liquid product yield for 4.39 percentage points, coking water filling (vapor) amount is 0.
1 feedstock property of table is analyzed
2 operating condition of table and product distribution
Embodiment 2
Using system of processing same as Example 1, raw material heavy oil, but processing conditions is had any different：
Reaction temperature in the present embodiment low-temperature cold plasma reactor is 100 DEG C, and the reaction temperature of delayed coking is 475 DEG C, other reaction conditions are the same as embodiment 1.
The embodiment finally obtains liquid product yield as 62.51% (mass percent).
Embodiment 3
Using system of processing same as Example 1, raw material heavy oil, but processing conditions is had any different：
Reaction temperature in the present embodiment low-temperature cold plasma reactor is 400 DEG C, and the reaction temperature of delayed coking is 515 DEG C, other reaction conditions are the same as embodiment 1.
The embodiment finally obtains liquid product yield as 67.11% (mass percent).
Embodiment 4
Using system of processing same as Example 1, raw material heavy oil, but processing conditions is had any different：
Reaction temperature in the present embodiment low-temperature cold plasma reactor is 180 DEG C, and the reaction temperature of delayed coking is 500 DEG C, other reaction conditions are the same as embodiment 1.
The embodiment finally obtains liquid product yield as 65.23% (mass percent).
Embodiment 5
Using system of processing same as Example 1, raw material heavy oil, but processing conditions is had any different：
The weight ratio of the initial hydrogen of the present embodiment and raw material heavy oil is 0.001:1, other reaction conditions are the same as embodiment 1.
The embodiment finally obtains liquid product yield as 63.55% (mass percent).
Embodiment 6
Using system of processing same as Example 1, raw material heavy oil, but processing conditions is had any different：
The weight ratio of the initial hydrogen of the present embodiment and raw material heavy oil is 0.2:1, other reaction conditions are the same as embodiment 1.
The embodiment finally obtains liquid product yield as 66.46% (mass percent).
Embodiment 7
Using system of processing same as Example 1, raw material heavy oil, but processing conditions is had any different：
The weight ratio of the initial hydrogen of the present embodiment and raw material heavy oil is 0.005:1, other reaction conditions are the same as embodiment 1.
The embodiment finally obtains liquid product yield as 65.93% (mass percent).
Finally it should be noted that：The above embodiments are only used to illustrate the technical solution of the present invention., rather than its limitations；To the greatest extent Pipe is described in detail the present invention with reference to foregoing embodiments, it will be understood by those of ordinary skill in the art that：Its according to Can so modify to the technical solution recorded in foregoing embodiments either to which part or all technical features into Row equivalent replacement；And these modifications or replacement, various embodiments of the present invention technology that it does not separate the essence of the corresponding technical solution The range of scheme.

Claims (10)

  1. A kind of 1. processing of heavy oil method, which is characterized in that include the following steps：
    Step A：Hydrogen-rich gas is made to react in low-temperature cold plasma reactor with heavy oil feedstock, generates the first product； The weight ratio of the hydrogen-rich gas and the heavy oil feedstock is 0.001~0.2:1, preferably 0.005~0.15:1；
    Step B：First product is made to carry out delayed coking, generates the second product；
    Step C：Gas-liquid phase component in second product is fractionated, obtains the product of different fractions.
  2. 2. processing of heavy oil method according to claim 1, which is characterized in that in the low-temperature cold plasma reactor Reaction temperature is 100 DEG C~400 DEG C, preferably 180 DEG C~350 DEG C；
    Preferably, the reaction temperature of the delayed coking is 400 DEG C~550 DEG C, preferably 475 DEG C~525 DEG C.
  3. 3. processing of heavy oil method according to claim 1, which is characterized in that in the low-temperature cold plasma reactor It is also carried out after reacting and before the delayed coking reaction：
    First product is fractionated, is divided into light component and heavy constituent；The heavy constituent is made to carry out the delayed coking；
    Preferably, the gas of the light component is made to return to the low-temperature cold plasma reactor the reaction was continued.
  4. 4. processing of heavy oil method according to claim 1, which is characterized in that the hydrogen-rich gas is hydrogen, methane, ethane With one or more mixing in propane；
    Preferably, the heavy oil feedstock is reduced crude, decompression residuum, catalytic slurry, heavy crude, heavy crude, de-oiling drip One or more of green and refinery's trowel used for plastering oil.
  5. 5. the processing of heavy oil method according to claim 1 or 3, which is characterized in that further include：It will be fractionated in the step C The gas gone out returns to the low-temperature cold plasma reactor, and the reaction was continued.
  6. 6. processing of heavy oil method according to claim 1, which is characterized in that further included before the step A：
    The hydrogen-rich gas is preheated to 50 DEG C~300 DEG C, preferably 120 DEG C~260 DEG C；
    The heavy oil feedstock is preheated to 100 DEG C~400 DEG C, preferably 180 DEG C~350 DEG C.
  7. 7. a kind of system for claim 1-6 any one of them processing of heavy oil methods, which is characterized in that including passing through pipe The sequentially connected low-temperature cold plasma reactor of line, delayed coking unit and fractionating column；
    The low-temperature cold plasma reactor is used for：Make hydrogen-rich gas with heavy oil feedstock in low-temperature cold plasma reactor It reacts, generates the first product；The weight ratio of the hydrogen-rich gas and the heavy oil feedstock is 0.001~0.2:1, preferably 0.005~0.15:1；
    The delayed coking unit is used for：First product is made to carry out delayed coking, generates the second product；
    The fractionating column is used for：Gas-liquid phase component in second product is fractionated, obtains the product of different fractions.
  8. 8. system according to claim 7, which is characterized in that the low-temperature cold plasma reactor and the delay coke Another fractionating column is also associated between change unit.
  9. 9. system according to claim 8, which is characterized in that the fractionating column and another fractionating column are equipped with gas Outlet, the gas discharge outlet of the two are connect by pipeline with the low-temperature cold plasma reactor.
  10. 10. system according to claim 7, which is characterized in that the low-temperature cold plasma reactor is dielectric impedance Discharge reactor.
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CN103305271A (en) * 2013-06-25 2013-09-18 中石化南京工程有限公司 Combined process method of lightening residual oil/ medium and low temperature coal tar
CN103773477A (en) * 2012-10-24 2014-05-07 中国石油化工股份有限公司 Coal tar and residuum hydrocracking-delayed coking combination processing method

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