CN105567319B - A kind of method for handling mink cell focus - Google Patents
A kind of method for handling mink cell focus Download PDFInfo
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- CN105567319B CN105567319B CN201410535193.0A CN201410535193A CN105567319B CN 105567319 B CN105567319 B CN 105567319B CN 201410535193 A CN201410535193 A CN 201410535193A CN 105567319 B CN105567319 B CN 105567319B
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Abstract
The invention provides a kind of method for handling mink cell focus, this method comprises the following steps：(1) mink cell focus is carried out to the operation of solvent deasphalting, deasphalted oil and de-oiled asphalt is obtained；(2) de-oiled asphalt for obtaining step (1) carries out hydrotreating in the presence of a hydrogenation catalyst with coal and hydrogen supply agent, obtains hydrotreatment products；(3) hydrogenation products for obtaining step (2) are fractionated, and obtain fraction products, and the condition of fractionation causes the cut that the fraction products at least gasoline fraction, diesel oil distillate and boiling range including separating each other are 350 500 DEG C；(4) boiling range in the fraction products for obtaining step (3) carries out partial hydrogenation processing for 350 500 DEG C of cut, obtain the product after partial hydrogenation, and using the product after partial hydrogenation as using in hydrogen supply agent return to step (2).Group technology is processed by the mink cell focus of above-mentioned technical proposal, the asphalitine in mink cell focus can effectively be converted into and be worth higher light oil by the present invention.
Description
Technical field
The present invention relates to petrochemical industry, in particular it relates to a kind of method for handling mink cell focus.
Background technology
Mink cell focus includes residual oil and viscous crude, wherein, residual oil includes reduced crude and decompression residuum, and reduced crude refers to oil
Cut of the boiling point that crude oil or oil product are obtained after normal pressure is fractionated more than 350 DEG C, decompression residuum refers to petroleum crude oil
Or cut of the boiling point that is obtained after vacuum fractionation of oil product more than 500 DEG C；Viscous crude refers to the reservoir temperature that exploitation is obtained
Lower degassed crude viscosity is 1000-10000mPas high viscosity heavy crude.
More resin and asphalt (i.e. heptane insolubles) is typically contained in mink cell focus, and it is miscellaneous containing more metal
Matter, it includes the various macromolecule hydrocarbon of quantity, has also concentrated most of sulphur, nitrogen, oxygen and metallic compound in crude oil.Due to weight
Matter oil is more and combustibility is very poor containing impurity, therefore is not suitable for being directly used in internal combustion engine and boiler oil.But at present, it is right
The demand of light-weight fuel oil increases substantially, and the price of crude oil is always in run at high level；At the same time, the heavy of crude resources
Change, in poor quality but becomes clear day by day, this just proposes higher requirement to the working depth of crude oil.With the poor quality processed raw material
Change, tenor, carbon residue and the asphalt content in decompression residuum are all continuously increased.The mode of traditional processing decompression residuum is such as prolonged
Slow coking, catalytic cracking have not adapted to the process requirements of poor residuum；Hydrocracking technology such as fixed bed hydrogenation, ebullated bed adds
The service life of the processing high metal such as hydrogen content, the residual oil meeting serious curtailment processing unit of high carbon residue.
Solvent deasphalting is to be taken out the resin and asphalt in decompression residuum with the method for extraction, to produce depitching
Oil, while producing a kind of petroleum refining process of asphalitine (de-oiled asphalt).Solvent deasphalting is in terms of processing heavy oil, to obtain
For the purpose of deasphalted oil, the asphalitine that converts and fused ring compound will be difficult in heavy charge and is had to catalytic conversion process
Harmful heavy metal and sulphur, nitrogen compound are removed away, and the preferable deasphalted oil of quality is split as catalytic cracking, fixed bed hydrogenation
The raw material of the techniques such as change.But for de-oiled asphalt, due to processing relative difficulty, effectively it is translated into the work of light fuel
Skill is few.De-oiled asphalt is generally used for the building fields such as surfacing, relative to crude oil procurement price and product oil price, de-oiling
The relative low price of pitch, profit margin is big, if developing a kind of more economical effective mink cell focus processing group technology
So that the asphalitine in mink cell focus, which can be also converted into, is worth higher light-weight fuel oil, undoubtedly by with very positive meaning.
The content of the invention
The asphalitine that the purpose of the present invention is so that in mink cell focus can also be converted into be worth higher light-weight fuel oil there is provided
A kind of more economical effective mink cell focus processing group technology.
To achieve these goals, the invention provides a kind of method for handling mink cell focus, the mink cell focus includes normal pressure
At least one of residual oil, decompression residuum and viscous crude, this method comprises the following steps：(1) mink cell focus is subjected to solvent deasphalting
Operation, obtain deasphalted oil and de-oiled asphalt；(2) de-oiled asphalt for obtaining step (1) is urged with coal and hydrogen supply agent in hydrogenation
Hydrotreating is carried out in the presence of agent, hydrotreatment products are obtained；Wherein, the weight ratio of de-oiled asphalt and coal is (0.1-10)：
1；The weight ratio of the gross weight and hydrogen supply agent of de-oiled asphalt and coal is (0.2-2)：1；The hydrogen supply agent contains hydrogen-to-carbon ratio
For 1.1-1.6 hydrocarbon；(3) hydrogenation products for obtaining step (2) are fractionated, and obtain fraction products, and the condition of fractionation causes
The fraction products at least gasoline fraction, diesel oil distillate and boiling range including separating each other are 350-500 DEG C of cut；(4) will
Boiling range in the fraction products that step (3) is obtained carries out partial hydrogenation processing for 350-500 DEG C of cut, obtains after partial hydrogenation
Product, and using the product after partial hydrogenation as using in hydrogen supply agent return to step (2)；Wherein, partial hydrogenation is handled
Condition causes the hydrogen-to-carbon ratio of the product after partial hydrogenation to be 1.1-1.6.
Group technology is processed by the mink cell focus of above-mentioned technical proposal, the present invention can be effectively by the pitch in mink cell focus
Matter, which is converted into, is worth higher light oil, while by the way that de-oiled asphalt is refined altogether with coal, on the one hand can improve turning for asphalitine
Rate, obtains higher yield of light oil, on the other hand also opens a new coal utilization technique.
Other features and advantages of the present invention will be described in detail in subsequent embodiment part.
Brief description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute a part for specification, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is a kind of process chart of embodiment specifically preferred according to the invention.
Description of reference numerals
The pipeline of 1 pipeline 2
The evaporating column of 3 extraction tower 4
The pipeline of 5 stripper 6
The heating furnace of 7 pipeline 8
The stripper of 9 evaporating column 10
The pipeline of 11 pipeline 12
The pipeline of 13 pipeline 14
The coal storage tank of 15 pipeline 16
The reactor of 17 booster pump 18
The fractionating column of 19 separator 20
The pipeline of 21 pipeline 22
The hydrogenation unit of 23 pipeline 24
The recycle hydrogen processing unit of 25 pipeline 26
27 pipelines
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
In the present invention, in the case where not making opposite explanation, the gas and the volumetric quantities of liquid used is 25 DEG C
With the numerical value of 1 normal atmosphere pressure.
The invention provides a kind of method for handling mink cell focus, the mink cell focus includes coal tar pitch, straight asphalt, natural
At least one of pitch, reduced crude, decompression residuum and viscous crude, this method comprises the following steps：(1) mink cell focus is carried out molten
The deasphalting operation of agent, obtains deasphalted oil and de-oiled asphalt；(2) de-oiled asphalt for obtaining step (1) and coal and hydrogen supply agent
Hydrotreating is carried out in the presence of a hydrogenation catalyst, obtains hydrogenation products；Wherein, the weight ratio of de-oiled asphalt and coal is (0.1-
10)：1；The hydrogen supply agent contains the hydrocarbon that hydrogen-to-carbon ratio is 1.1-1.6；(3) hydrogenation products for obtaining step (2) are divided
Evaporate, obtain fraction products, the condition of fractionation make it that the fraction products are at least including gasoline fraction, diesel oil distillate and boiling range
350-500 DEG C of cut；(4) boiling range in the fraction products for obtaining step (3) for 350-500 DEG C of cut partly add
Hydrogen processing, obtains the product after partial hydrogenation, and using the product after partial hydrogenation as making in hydrogen supply agent return to step (2)
With；Wherein, the condition of partial hydrogenation processing causes the hydrogen-to-carbon ratio of the product after partial hydrogenation to be 1.1-1.6.
Wherein, the mink cell focus includes at least one of reduced crude, decompression residuum and viscous crude.Reduced crude refers to stone
The initial boiling point that oily crude oil is obtained after normal pressure is fractionated is more than 350 DEG C of cut.Decompression residuum refers to petroleum crude oil by decompression
The initial boiling point obtained after fractionation is more than 500 DEG C of cut.Viscous crude refers to that ground surface density is more than 0.943 and underground viscosity is more than 50 lis
The petroleum crude oil of pool.
Wherein, the operation of solvent deasphalting refers to, using mink cell focus as raw material, be extracted as solvent using C3-C5 hydrocarbon
With the process of solvent recovery.Extraction in solvent deasphalting can be carried out by conventional extraction equipment, such as spray column, filler
Extraction tower, perforated-plate extraction tower, pulsed perforated-plate tower, reciprocal perforated-plate extraction tower or turntable extracting tower.Solvent in solvent deasphalting is returned
Receipts are to utilize C3-C5 hydrocarbon is essentially insoluble under critical conditions to solve oily characteristic, make oil all precipitations in extract, so that
Realize the process that solvent is separated with oil.
The method according to the invention, wherein, in step (1), in the operation of solvent deasphalting, the volume of solvent and mink cell focus
Than that can be conventional selection, for example, can be (5-13)：1, be preferably (6-8)：1.
The method according to the invention, wherein, in step (1), solvent deasphalting is carried out in extraction tower, extracts column overhead pressure
Power and temperature can be the selection of routine, and such as extraction tower tower top pressure can be 2-4.5MPa, preferably 2.8-3.9MPa, tower
Top temperature is 50-90, preferably 54-82 DEG C.
Wherein, the feeding temperature of solvent can be 30-80 DEG C, and the feeding temperature of mink cell focus can be 120-150 DEG C.
The method according to the invention, wherein, in step (1), solvent used in solvent deasphalting include propane, normal butane,
At least one of iso-butane, pentane, isopentane and neopentane, solvent preferably used include propane and/or normal butane.
The method according to the invention, as a kind of particularly preferred embodiment, wherein, in step (2), de-oiled asphalt and
The weight ratio of coal is (0.5-5)：1.Under the preferable case, the method that can further improve the present invention handles the vapour of mink cell focus
Diesel oil mass output rate.
Wherein, the hydrogen supply agent contains the hydrocarbon that hydrogen-to-carbon ratio is 1.1-1.6；In going into operation the stage for method of the invention,
The source of hydrogen supply agent can be catalytic thermal solution recycle oil.
The method according to the invention, wherein, the weight ratio of the gross weight and hydrogen supply agent of de-oiled asphalt and coal is preferably
(0.5-0.8)：1.
The method according to the invention, wherein, in step (2), the weight of the gross weight and hydrogenation catalyst of de-oiled asphalt and coal
It can be 1 to measure ratio：(0.01-0.1), preferably 1：(0.02-0.06), more preferably 1：(0.03-0.05).
The method according to the invention, wherein, in step (2), hydrotreating can be carried out in paste state bed reactor, slurry
Hydrogen partial pressure in bed reactor can be 15-25MPa, and bed temperature can be 380-480 DEG C, and liquid hourly space velocity (LHSV) can be 0.2-
2h-1, hydrogen-oil ratio can be 500-3000Nm3/t。
Wherein, the definition of liquid hourly space velocity (LHSV) is the ratio between slurries volume flow hourly and reactor effective volume.Wherein, hydrogen
The definition of oily ratio is the ratio between mass velocity of fresh hydrogen volume flow and slurry oil.
The method according to the invention, wherein, in step (2), hydrogenation catalyst can include at least one in iron, molybdenum and nickel
Kind.
The method according to the invention, wherein, in step (3), the condition of fractionation can cause fraction products at least to include that
Gasoline fraction, diesel oil distillate and the boiling range of this separation are 350-500 DEG C of cut.
The method according to the invention, wherein, in step (4), partial hydrogenation processing can hydrotreating conventional equipment
It is middle to carry out, it can for example be carried out in expanded bed, ebullated bed, suspension bed or fixed bed.
The method according to the invention, wherein, in step (4), the condition of partial hydrogenation processing is enabled to after partial hydrogenation
Product hydrogen-to-carbon ratio be 1.1-1.6, for example partial hydrogenation processing condition include：Hydrogen partial pressure can be 5-20MPa,
Bed temperature can be 300-420 DEG C, and liquid hourly space velocity (LHSV) can be 0.2-1.2h-1, hydrogen-oil ratio can be 500-2000Nm3/t。
The method according to the invention, wherein, in step (4), the catalyst of partial hydrogenation processing can include the VIth race gold
At least one of metal catalyst and the VIIIth group 4 transition metal catalyst.
The method according to the invention, wherein, the VIth race's metallic catalyst includes W and Mo, the VIIIth race transition gold
Metal catalyst includes Co and Ni.
Wherein it is preferred to, in the catalyst of partial hydrogenation processing, W content is 5-40 weight %, more preferably 10-30
Weight %；Mo, Ni, Co content are 1-15 weight %, more preferably 2-10 weight %.
The method according to the invention, wherein, the phosphorus content of the mink cell focus can be 80-90 weight %, and hydrogen content can be with
For 8-10 weight %.Wherein, the phosphorus content and hydrogen content of the mink cell focus refer to the number being measured according to standard SH/T 0656
Value.
The method according to the invention, wherein, the phosphorus content of the coal can be 70-90 weight %, and hydrogen content can be
4.1-6.0 weight %.Wherein, the phosphorus content and hydrogen content of the coal refer to the numerical value being measured according to standard GB/T212.Its
In, the coal can be used by crushing for coal dust, and the particle diameter of coal dust can be 5-100 μm.
The method according to the invention, wherein, the phosphorus content of the hydrogen supply agent can be 75-90 weight %, and hydrogen content can be with
For 6.8-12 weight %.Wherein, the phosphorus content and hydrogen content of the hydrogen supply agent refer to what is be measured according to standard SH/T 0656
Numerical value.
The method according to the invention, wherein, the condition of fractionation can cause solid in material derived from the bottom of fractionating column
Ratio in below 55 weight %, preferably in below 45 weight %.
The method according to the invention, wherein, the coal can include in lignite, bituminous coal, ub-bituminous coal and fat coal
It is at least one.
The method according to the invention, wherein, in step (2), the hydrogen supply agent remove the partial hydrogenation after product with
Outer insufficient section is provided by decompressed wax oil and/or catalytic cracking recycle oil.The decompressed wax oil refers to the decompression point in oil
The boiling range produced during evaporating is 350-500 DEG C of distillate.The catalytic cracking recycle oil refers in the product of catalytic cracking
Boiling range is 360-500 DEG C of distillate.
The present invention is further described by the following examples.
In following examples, the mink cell focus used is decompression residuum, and the property of the decompression residuum is as shown in table 1.Following reality
The coal dust of coal crushing used in example for 75 μm of average grain diameter is applied, the Industrial Analysis and elementary analysis of coal dust are as shown in table 2, coal dust
Analysis be according to standard GB/T212 carry out.
Table 1
Table 2
Embodiment 1
With reference to Fig. 1, mink cell focus is imported in extraction tower 3 (rotating disc column) through pipeline 1, solvent (propane) is imported through pipeline 2
In extraction tower 3 (rotating disc column), the feeding temperature of mink cell focus is 140 DEG C, and the feeding temperature of solvent is 60 DEG C, carries out solvent deasphalting
Operation, wherein, the volume ratio of solvent and mink cell focus is 10：1, extraction tower top pressure is 3.2MPa, 70 DEG C of tower top temperature.
Extract is exported from extraction tower 3 into evaporating column 4, evaporation of solvent (propane) simultaneously separates out thick deasphalted oil,
The solvent (propane) that evaporation is removed is returned to be continuing with extraction tower 3, and thick deasphalted oil is imported in stripper 5, from pipeline 11 to
Steam is passed through in stripper 5 to be stripped, and is exported with removing the deasphalted oil obtained after the solvent of residual, stripping through pipeline 6, vapour
Rear remaining steam is carried to export by pipeline 12.
Thick de-oiled asphalt is exported from extraction tower 3 150 DEG C are heated into heating furnace 8, be then introduced into evaporating column 9 and carry out
Evaporate to remove remnants solvent, the remaining solvent of abjection returns to reclaim in extraction tower 3 through pipeline 7 to be used, remaining after evaporation
Material import stripper 10, be passed through steam into stripper 10 from pipeline 11 and stripped, the de-oiled asphalt after stripping is through pipe
Road 13 is exported, and remaining steam is exported by pipeline 12 after stripping.
The coal dust being passed through through de-oiled asphalt derived from pipeline 13, through pipeline 14 and the catalyst being passed through through pipeline 15 import oil
Coal paste storage tank 16, hydrogen supply agent is added into coal storage tank 16 also through pipeline 25, and (in the stage of going into operation, the source of hydrogen supply agent is decompression
Wax oil), de-oiled asphalt, coal dust, the weight ratio of hydrogen supply agent and hydrogenation catalyst are 1：1：3.3：0.04, in coal storage tank 16
The material of addition is well mixed, the material after being well mixed is pressurized and heated through booster pump 17, temperature is reached 450 DEG C, pressure
Power reaches 20MPa, imports in reactor 18 (paste state bed reactor) liquid hourly space velocity (LHSV) carried out in hydrogenation reaction, reactor 18 and is
1h-1, hydrogen-oil ratio is 1500Nm3/ t, material derived from reactor 18 is separated into hydrogen and the material after hydrogenation through separator 19, plus
Material after hydrogen is imported to be fractionated in fractionating column 20, and petrol and diesel oil cut is exported through pipeline 21, and boiling range is 350-450 DEG C of cut
Exported through pipeline 22, tailings is exported through pipeline 23.Hydrogen derived from separator 19 enters to be followed in recycle hydrogen processing unit 26
Ring hydrogen processing, the hydrogen after processing is exported through pipeline 27, is recycled.
It is directed into through the cut that boiling range derived from pipeline 22 is 350-450 DEG C in hydrogenation unit 24 and carries out partial hydrogenation, portion
Dividing the condition of hydrotreating includes：Hydrogen partial pressure is 10MPa, and bed temperature is 380 DEG C, and liquid hourly space velocity (LHSV) is 1h- 1, hydrogen-oil ratio is
1000Nm3/ t, the condition of partial hydrogenation processing causes the hydrogen-to-carbon ratio of the product after partial hydrogenation to be 1.3-1.4.Part adds
Product after hydrogen is exported into coal storage tank 16 as hydrogen supply agent through pipeline 25 to be used.
According to the method for the present embodiment, after stable operation, when the de-oiled asphalt and coal (deduct coal in inanimate matter) of input
When gross weight is 100kg, obtained C1-C4 alkane is 10.36kg, and gasoline is 16.06kg, and diesel oil is 24.25kg, and wax oil is
25.41kg, tailings is 23.92kg.
Embodiment 2
Method according to embodiment 1 is handled, unlike, de-oiled asphalt, coal dust, hydrogen supply agent and hydrogenation catalyst
Weight ratio is 1：0.5：3：0.024.
According to the method for the present embodiment, after stable operation, when input de-oiled asphalt and coal gross weight be 100kg when,
Obtained C1-C4 alkane is 8.73kg, and gasoline is 14.64kg, and diesel oil is 23.66kg, and wax oil is 27.39kg, and tailings is
25.57kg。
Embodiment 3
Method according to embodiment 1 is handled, unlike, de-oiled asphalt, coal dust (deducting inanimate matter in coal), hydrogen supply
The weight ratio of agent and hydrogenation catalyst is 5：1：6.25：0.6.
According to the method for the present embodiment, after stable operation, when the de-oiled asphalt and coal (deduct coal in inanimate matter) of input
When gross weight is 100kg, obtained C1-C4 alkane is 10.18kg, and gasoline is 13.59kg, and diesel oil is 24.68kg, and wax oil is
26.84kg, tailings is 24.72kg.
Embodiment 4
Method according to embodiment 1 is handled, unlike, de-oiled asphalt, coal dust (deducting inanimate matter in coal), hydrogen supply
The weight ratio of agent and hydrogenation catalyst is 1：0.1：5.5：0.022.
According to the method for the present embodiment, after stable operation, when the de-oiled asphalt and coal (deduct coal in inanimate matter) of input
When gross weight is 100kg, obtained C1-C4 alkane is 8.19kg, and gasoline is 13.49kg, and diesel oil is 24.67kg, and wax oil is
26.78kg, tailings is 26.87kg.
Embodiment 5
Method according to embodiment 1 is handled, unlike, de-oiled asphalt, coal dust (deducting inanimate matter in coal), hydrogen supply
The weight ratio of agent and hydrogenation catalyst is 0.1：1：0.55：0.022.
According to the method for the present embodiment, after stable operation, when the de-oiled asphalt and coal (deduct coal in inanimate matter) of input
When gross weight is 100kg, obtained C1-C4 alkane is 10.82kg, and gasoline is 15.05kg, and diesel oil is 23.05kg, and wax oil is
24.74kg, tailings is 26.34kg.
Comparative example 1
Method according to embodiment 1 is handled, unlike, de-oiled asphalt, coal dust (deducting inanimate matter in coal), hydrogen supply
The weight ratio of agent and hydrogenation catalyst is 1：0.05：1：0.02.
According to the method for the present embodiment, after stable operation, when the de-oiled asphalt and coal (deduct coal in inanimate matter) of input
When gross weight is 100kg, obtained C1-C4 alkane is 9.99kg, and gasoline is 10.84kg, and diesel oil is 20.45kg, and wax oil is
23.17kg, tailings is 35.54kg.
Comparative example 2
Method according to embodiment 1 is handled, unlike, de-oiled asphalt, coal dust (deducting inanimate matter in coal), hydrogen supply
The weight ratio of agent and hydrogenation catalyst is 0.05：1：1：0.02.
According to the method for the present embodiment, after stable operation, when the de-oiled asphalt and coal (deduct coal in inanimate matter) of input
When gross weight is 100kg, obtained C1-C4 alkane is 9.75kg, and gasoline is 9.44kg, and diesel oil is 21.03kg, and wax oil is
22.12kg, tailings is 38.54kg.
Visible according to embodiment 1-5 and comparative example 1 and 2 data, the present invention can be effectively by the pitch in mink cell focus
Matter, which is converted into, is worth higher light oil, while by the way that de-oiled asphalt is refined altogether with coal, on the one hand can improve turning for asphalitine
Rate, obtains higher yield of light oil, on the other hand a new coal utilization technique is also opened, while the present invention can be big
Amplitude improves the petrol and diesel oil mass output rate of heavy oil processing, also, is (0.5-5) in the weight ratio of de-oiled asphalt and coal：1 and described
The weight ratio of the gross weight of de-oiled asphalt and the coal and the hydrogen supply agent is (0.5-0.8)：In the case of 1, one can be entered
Step improves the petrol and diesel oil mass output rate of heavy oil processing.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the present invention, a variety of letters can be carried out to technical scheme
Monotropic type, these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (15)
1. a kind of method for handling mink cell focus, the mink cell focus includes at least one of reduced crude, decompression residuum and viscous crude,
It is characterized in that：This method comprises the following steps：
(1) mink cell focus is carried out to the operation of solvent deasphalting, deasphalted oil and de-oiled asphalt is obtained；
(2) de-oiled asphalt for obtaining step (1) carries out hydrotreating in the presence of a hydrogenation catalyst with coal and hydrogen supply agent, obtains
Hydrotreatment products；Wherein, the weight ratio of the de-oiled asphalt and the coal is (0.1-10)：1；The de-oiled asphalt and described
The weight ratio of the gross weight of coal and the hydrogen supply agent is (0.2-2)：1；The hydrogen supply agent contains hydrogen-to-carbon ratio for 1.1-1.6
Hydrocarbon；
(3) hydrotreatment products for obtaining step (2) are fractionated, and obtain fraction products, and the condition of fractionation causes institute
State the cut that fraction products at least gasoline fraction, diesel oil distillate and boiling range including separating each other are 350-500 DEG C；
(4) boiling range in the fraction products for obtaining step (3) carries out partial hydrogenation processing for 350-500 DEG C of cut, obtains
Product after partial hydrogenation, and using the product after the partial hydrogenation as using in hydrogen supply agent return to step (2)；Wherein,
The condition of partial hydrogenation processing causes the hydrogen-to-carbon ratio of the product after the partial hydrogenation to be 1.1-1.6.
2. according to the method described in claim 1, it is characterised in that：It is described molten in the operation of solvent deasphalting in step (1)
The volume ratio of agent and the mink cell focus is (5-13)：1；Solvent deasphalting is carried out in extraction tower, the tower top pressure of the extraction tower
Power is 2.8-3.9MPa, and tower top temperature is 54-82 DEG C；Solvent used in solvent deasphalting include propane, normal butane, iso-butane,
At least one of pentane, isopentane and neopentane.
3. according to the method described in claim 1, it is characterised in that：In step (2), the weight of the de-oiled asphalt and the coal
Than for (0.5-5)：1.
4. the method according to claim 1 or 3, it is characterised in that：In step (2), the de-oiled asphalt and the coal
The weight ratio of gross weight and the hydrogen supply agent is (0.5-0.8)：1.
5. the method according to claim 1 or 3, it is characterised in that：In step (2), hydrotreating is in paste state bed reactor
Middle to carry out, the hydrogen partial pressure in the paste state bed reactor is 15-25MPa, and bed temperature is 380-480 DEG C, and liquid hourly space velocity (LHSV) is
0.2-2h-1, hydrogen-oil ratio is 500-3000Nm3/t；The gross weight of the de-oiled asphalt and the coal and the hydrogenation catalyst
Weight ratio is 1：(0.01-0.1).
6. according to the method described in claim 1, it is characterised in that：In step (2), the hydrogenation catalyst include iron, molybdenum and
At least one of nickel.
7. according to the method described in claim 1, it is characterised in that：In step (4), partial hydrogenation processing is in expanded bed, boiling
Carried out in bed, suspension bed or fixed bed.
8. the method according to claim 1 or 7, it is characterised in that：In step (4), the condition of partial hydrogenation processing includes：
Hydrogen partial pressure is 5-20MPa, and bed temperature is 300-420 DEG C, and liquid hourly space velocity (LHSV) is 0.2-1.2h-1, hydrogen-oil ratio is 500-
2000Nm3/t。
9. the method according to claim 1 or 7, it is characterised in that：In step (4), the catalyst bag of partial hydrogenation processing
Include at least one of the VIth race's metallic catalyst and the VIIIth group 4 transition metal catalyst.
10. method according to claim 9, it is characterised in that：VIth race's metallic catalyst includes W and Mo, described
VIIIth group 4 transition metal catalyst includes Co and Ni.
11. method according to claim 10, it is characterised in that：In the catalyst of partial hydrogenation processing, W content is 5-
40 weight %, Mo, Ni and Co total content is 1-15 weight %.
12. according to the method described in claim 1, it is characterised in that：In step (3), the condition of fractionation causes the kettle of fractionating column
The ratio of solid is in below 55 weight % in material derived from bottom.
13. according to the method described in claim 1, it is characterised in that：The coal is included in lignite, bituminous coal and ub-bituminous coal at least
It is a kind of.
14. according to the method described in claim 1, it is characterised in that：The coal includes fat coal.
15. according to the method described in claim 1, it is characterised in that：The product removed after the partial hydrogenation of the hydrogen supply agent
Insufficient section in addition is provided by decompressed wax oil and/or catalytic cracking recycle oil.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410535193.0A CN105567319B (en) | 2014-10-11 | 2014-10-11 | A kind of method for handling mink cell focus |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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| CN110396424A (en) * | 2019-07-16 | 2019-11-01 | 中国启源工程设计研究院有限公司 | A kind of waste mineral oil decompression residuum processing unit and method |
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| CN1654603A (en) * | 2004-02-13 | 2005-08-17 | 中国石油化工股份有限公司 | Conversion method for low-grade heavy and residual oil |
| CN102041018A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | Processing method of coal and oil co-refining |
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| CN1654603A (en) * | 2004-02-13 | 2005-08-17 | 中国石油化工股份有限公司 | Conversion method for low-grade heavy and residual oil |
| CN102041018A (en) * | 2009-10-16 | 2011-05-04 | 中国石油化工股份有限公司 | Processing method of coal and oil co-refining |
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