CN110114445A - Method for producing middle distillate - Google Patents
Method for producing middle distillate Download PDFInfo
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- CN110114445A CN110114445A CN201780078935.3A CN201780078935A CN110114445A CN 110114445 A CN110114445 A CN 110114445A CN 201780078935 A CN201780078935 A CN 201780078935A CN 110114445 A CN110114445 A CN 110114445A
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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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
-
- 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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
-
- 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
- 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
- C10G67/04—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 solvent extraction as the refining step in the absence of hydrogen
- C10G67/0454—Solvent desasphalting
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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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
-
- 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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
- C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1077—Vacuum residues
-
- 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
- C10G2400/06—Gasoil
-
- 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
- C10G2400/08—Jet fuel
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of methods for by remaining hydrocarbon-containing feedstock production middle distillate, the described method comprises the following steps: (a) in the first thermal cracking unit by the remaining hydrocarbon-containing feedstock thermal cracking with obtain include thermal cracking residual oil thermal cracking products；(b) at least make the thermal cracking residual oil depitching to obtain thermal cracking deasphalted oil and bitumen product；(c) in the second thermal cracking unit by least part thermal cracking of the thermal cracking deasphalted oil to obtain the deasphalted oil of thermal cracking twice；(d) by least part hydrocracking such as the deasphalted oil of the thermal cracking twice obtained in step (c) to obtain hydrocrackates；And at least part such as the hydrocrackates obtained in step (d) is set to be subjected to separating treatment (e) to obtain at least one middle distillate fraction.The present invention also provides a kind of for producing super-low sulfur fuel oil and middle distillate and sulfur content in 0.03wt.% to the Low Sulfur Fuel Oil being less than within the scope of 0.5wt.% or the method for fuel oil blend components.
Description
Technical field
The present invention relates to the methods for producing middle distillate.The invention further relates to a kind of for producing the side of fuel oil
Method, the fuel oil meet maximum sulfur specification January 1 to come into force as defined in International Maritime Organization in the year two thousand twenty.The present invention
Further relate to a kind of Low Sulfur Fuel Oil or fuel oil blend components.
Background technique
According to New emission standard, nowadays numerous studies and exploitation is related to producing so-called super-low sulfur middle distillate for example ultralow
Sulfur diesel fuel.
Become known for producing many multistep methods of super-low sulfur middle distillate.Oil plant be faced with a variety of crude oil of processing and
Difference composition crude oil blends challenge and be processed into the challenge for having to comply with the product more strictly regulated.
As the maximum sulfur specification that January 1 came into force as defined in International Maritime Organization in the year two thousand twenty recently is into one
Step is stringent, and the oil plant for producing the fuel oil for not meeting sulphur specification is faced with that be effectively converted into its refinery operations can be with high yield
Rate produces super-low sulfur middle distillate and/or meets the challenge of the operation of the fuel oil of required sulphur specification.
WO2015/097199 describes a kind of be used for using hydrodemetallization unit to evaporate among high yield production super-low sulfur
The method of object out.But not many oil plants possess a large amount of hydrodemetallization unit, and throw in no significant amount fund
It the use of hydrodemetallization unit is not a practical solution for those oil plants in the case where entering.
EP0372652 describes a kind of in the thermal cracking of decompression residuum and two step of solvent deasphalting of thermal cracking residual oil
Method of the heavy hydrocarbon-containing feedstock to prepare deasphalted oil is converted in the process.EP0372652 does not refer to sulfur content or tenor, and
And the method for not describing production super-low sulfur middle distillate or super-low sulfur fuel oil.The 25-26 row of page 4 describes deasphalted oil can
For use as hydrotreating or the charging of hydrocracking processes, catalytic pyrolysis process or thermal cracking processes, but the not yet description present invention
Specific multistep method.
Summary of the invention
The object of the present invention is to provide a kind of in the method for high yield production super-low sulfur middle distillate.Of the invention
Another object is to provide a kind of method for producing fuel oil, and the fuel oil meets as defined in International Maritime Organization in the year two thousand twenty
The maximum sulfur specification that January 1 came into force.It is a further object of the present invention to provide a kind of Low Sulfur Fuel Oil or fuel oil blend components.
In one aspect, the present invention provides a kind of method for by remaining hydrocarbon-containing feedstock production middle distillate, institutes
State method the following steps are included:
(a) in the first thermal cracking unit by the remaining hydrocarbon-containing feedstock thermal cracking with obtain include thermal cracking residual oil heat
Pyrolysis product；
(b) at least make the thermal cracking residual oil depitching to obtain thermal cracking deasphalted oil and bitumen product；
(c) in the second thermal cracking unit by least part thermal cracking of the thermal cracking deasphalted oil to obtain hot tearing
The deasphalted oil of solution twice；
It (d) will be such as at least part hydrocracking of the deasphalted oil of the thermal cracking twice obtained in step (c)
To obtain hydrocrackates；And
(e) at least part such as the hydrocrackates obtained in step (d) is made to be subjected to separating treatment to obtain
To at least one middle distillate fraction.
According to the present invention it is possible to advantageously produced by remaining hydrocarbon-containing feedstock high yield containing a small amount of sulphur, preferably less than
The middle distillate of 10ppmw sulphur.
On the other hand, the present invention provides one kind for being evaporated by remaining hydrocarbon-containing feedstock production super-low sulfur fuel oil and centre
The method of object out, the described method comprises the following steps:
(a) in the first thermal cracking unit by the remaining hydrocarbon-containing feedstock thermal cracking with obtain include thermal cracking residual oil heat
Pyrolysis product；
(b) at least make the thermal cracking residual oil depitching to obtain thermal cracking deasphalted oil and bitumen product；
(c) in the second thermal cracking unit by least part thermal cracking of the thermal cracking deasphalted oil to obtain hot tearing
The deasphalted oil of solution twice；
It (d) will be such as at least part hydrocracking of the deasphalted oil of the thermal cracking twice obtained in step (c)
To obtain hydrocrackates；
(e) at least part such as the hydrocrackates obtained in step (d) is made to be subjected to separating treatment with obtain to
The fraction of a kind of few middle distillate fraction and boiling point within the scope of fuel oil；
(f) at least part of the fraction of the boiling point within the scope of the fuel oil is optionally made to be subjected to further adding hydrogen
Cleavage step is to generate hydrocrackates (f)；And
(g) at least part such as the hydrocrackates obtained in step (f) is made to be subjected to separating treatment with obtain to
The fraction of a kind of few middle distillate fraction and boiling point within the scope of fuel oil.
It yet still another aspect, the present invention provides a kind of sulfur content in 0.03wt.% to less than low within the scope of 0.5wt.%
Sulphur fuel oil or fuel oil blend components comprising 50wt.% to 95wt.% can be from method as described above the step of (e) or
(g) sulfur content of fraction and 5wt.% to 50wt.% of the boiling point obtained within the scope of fuel oil is greater than the boiling point of 0.5wt.%
Fraction within the scope of fuel oil.
Detailed description of the invention
Attached drawing depicts one or more embodiments of content according to this teaching, only by way of example, and without
Limitation.In the accompanying drawings, similar appended drawing reference refers to same or similar element.
Fig. 1 depicts the preferred embodiment of the method for production middle distillate according to the present invention.
Specific embodiment
Remaining hydrocarbon-containing feedstock used according to the invention can be residual hydrocarbon oil, such as under normal or reduced pressure in the steaming of crude oil
It evaporates middle as residual oil and those of obtains residual hydrocarbon oil, commonly referred to as normal pressure (atmospheric/long) residual oil and decompression
(vacuum/short) residual oil.Preferably, remaining hydrocarbon-containing feedstock is decompression residuum.In general, at least 55wt%, preferably at least
75wt%, more preferably at least 85wt%, and the remaining hydrocarbon-containing feedstock of even more preferably at least 90wt% is under atmospheric pressure
Boiling point be higher than 550 DEG C.
It includes thermal cracking that step (a), which is included in the remaining hydrocarbon-containing feedstock thermal cracking in the first thermal cracking unit to obtain,
The thermal cracking products of residual oil.
In general, remaining hydrocarbon-containing feedstock to be usually provided in one or more to the heating furnace or heating furnace of heat-exchange tube or circle
It is preheated in part, raw material passes through the heat-exchange tube or circle.Temperature raw material being preferably preheating within the scope of 350 DEG C to 600 DEG C
It spends and is fed to thermal cracking area.
Thermal cracking occurs in thermal cracking area.Raw material can be along upwardly or downwardly passing through cracking zone.Preferably, it flows
It moves upward.Raw material can be by being configured to the cracking zone of empty container, such as such as US-A 1, described in 899,889.
Preferably, thermal cracking area is located in the soaking container comprising internal component.Internal component is preferably in perforated plate
Form.In such soaking container, internal component provides compartment, and the generation of back-mixing is reduced by the compartment.Soaking container
An example be described in EP-A 7656.
In one embodiment of the invention, it is preferable that effluent is flashed or is fractionated to generate the distillate of thermal cracking
Fraction or a variety of fractions and thermal cracking residual oil.
Thermal cracking products are separated into thermal cracking residual oil in cracking step (a) in a preferred aspect of the invention
And one or more thermal cracking distillates.
Preferably, cracking step (a) is in 25wt% to 55wt% range, more preferably 30wt% to 50wt% range
It is operated under interior conversion ratio.
Thermal cracking is usually carried out in the case where reducibility gas such as hydrogen is not present.Cracking can be there are the feelings of steam
It is carried out under condition.It can change the condition that can carry out thermal cracking.People can arbitrarily adjust temperature, pressure and residence time, with
So that desired conversion ratio occurs.It will be apparent to those skilled in the art that on the one hand in high temperature and short can stop
It stays under the time, identical conversion ratio is on the other hand obtained under lower temperature but longer dwell time.In addition, cracking reaction is to inhale
Heat, therefore in the case where soaking pit cracking, the temperature on entire cracking zone often reduces.Therefore, those skilled in the art
The condition in cracking zone will be selected, so that desired level of conversion will be obtained.Suitable cracking condition includes 350 DEG C and arrives
600 DEG C of temperature, 1 bar to 100 bars of absolute pressure and 0.5 minute to 60 minutes residence time.Residence time and cold original
Expect related.
In step (b), by the residual oil depitching of at least thermal cracking, the deasphalted oil and bitumen product of thermal cracking are obtained,
And at least 45wt%, preferably at least 65wt%, more preferably at least 80wt%, and even more preferably at least 85wt%
The deasphalted oil have higher than 550 DEG C of boiling point.
Depitching in step (b) can carry out in any usual manner.Known and suitable de-asphalting method is solvent
Depitching.According to the present invention, the depitching in step (b) is preferably handled by solvent deasphalting and is carried out.It is highly preferred that step
(b) it is handled by solvent deasphalting and carries out and operated under the extraction depth in 25wt.% to 65wt.% range.
According to one embodiment, the thermal cracking products of step (a) are without individually distilling or (decompression) flash steps
In the case of go to step (b).
According to another embodiment, the thermal cracking products of step (a) are flashed or are fractionated, so that only gas or gas
With naphtha fraction (i.e. 160 DEG C of 95wt.% boils up till) or gas, naphtha fraction and gas oil fraction are (i.e.
350 DEG C of 95wt.% boils up till) it is removed from thermal cracking products and forms the hot tearing containing high relative contents compared with light oil constituents
Solve residual oil.
It should be appreciated that the thermal cracking products or thermal cracking residual oil when the relatively light oil constituents with high relative contents go to solvent
When depitching step, it is easier to realize higher levels of extraction depth.
According to a preferred embodiment, the amount of thermal cracking residual oil of the boiling point equal to or less than 520 DEG C is for 10wt.% or more
It is few, even more preferably less than 9wt.%, even more preferably less than 5wt.%.
It is 10wt.% or less in the amount of thermal cracking residual oil of the boiling point equal to or less than 520 DEG C, even more preferably less than
9wt.%, even more preferably less than in the embodiment of 5wt.%, extraction depth is preferably 30wt.% to 60wt.%, even
More preferably 35wt.% to 55wt.%.
In solvent deasphalting, hydrocarbon charging usually uses spe medium countercurrent treatment, and the spe medium is usually containing chain
The light hydrocarbon solvent of hydride compounds.Commonly used paraffinic compounds include C3-C8 alkane, as propane, butane, iso-butane,
The mixture of two or more in pentane, isopentane, hexane or these alkanes.For the purposes of the present invention, preferably
It is using C3-C5 alkane, most preferably or mixtures thereof butane, pentane is used as extractant.In general, extraction depth with
The increase of the carbon atom number of extractant and increase.In this regard, it should be noted that extraction depth is higher, extracts from raw material
Hydrocarbon amount it is bigger, bitumen product is smaller and viscosity is bigger, and the content of bitumen product studies on asphaltene obtained in step (b) is got over
It is high.
In solvent deasphalting processing, in general, rotating disk contactors, void column or sheet-pile can be with the raw materials that enter at top
It is matched with the extractant entered in bottom.The relatively lighter hydrocarbons and/or alkane being present in raw material are typically dissolved in extraction
In solvent, and as the thermal cracking deasphalted oil extraction at the top of equipment.Asphalitine insoluble in extractant is with bitumen product
Form from device bottom extract out.The condition that depitching occurs is well known in the art.Suitably, depitching is in 1.5wt/
At a temperature of the total extractant and residual hydrocarbon oil ratio of wt to 8wt/wt, 1 bar to 60 bars of pressure and 40 DEG C to 200 DEG C into
Row.
The bitumen product taken out from depitching step can be used for any purposes known in the art, such as fuel oil, drip
Green, gasifier feed or power station charging.It should be appreciated that bitumen product does not meet the stringent maximum sulphur rule of recently introduced fuel oil
Model, but its sulfur content is greater than 0.5wt.%, typically at least 2wt.%, such as 2.5wt.% to 7wt.%.
If desired, at least part of bitumen product may be used as boiling point within the scope of fuel oil and of the invention low
Sulfur content is greater than the fraction of 0.5wt% in sulphur fuel oil or fuel oil blend components.
As used herein, fraction of the boiling point within the scope of fuel oil is usually the residual fraction (5wt% that boiling point is higher than 370 DEG C
Point, i.e. 95wt.% boiling point are higher than 370 DEG C).
According to preferred embodiment, at least part such as the bitumen product obtained in step (b) is made to be subjected to gasification step
Suddenly (h) is to obtain hydrogen and carbon monoxide.
If should be appreciated that bitumen product is used for further process step, practical in oil plant, solvent deasphalting
The extraction depth of step may be limited by the accessible peak viscosity of following process unit being such as mounted in oil plant.
Depitching processing is typically resulted in charging and is accumulated in as a large amount of metal pollutants existing for high molecular weight complex compound
In bitumen product rather than in depitching product.Nevertheless, in the art, such as Ying Li for example in WO2015/097199
The tenor of solution, depitching product will be so that depitching product may need before being subjected to further hydrotreating upgrade step
It is subjected to hydrodemetallization step.
According to the present invention it has been found that if being the first cracking step before depitching step and being the second heat later
Cleavage step, then the tenor in the deasphalted oil of at least part thermal cracking twice is low enough to do not make hydrocracking
Catalyst allows the hydrocracking of the deasphalted oil of thermal cracking twice in the case where crossing moderate intoxication.If desired, hydrocracking list
Member include have the active guard bed of further hydrodemetallization or catalyst bed, but be not usually required in individual unit into
The individual hydrodemetallization step of row.
It therefore, will be such as the thermal cracking depitching obtained in step (b) in the second thermal cracking unit in step (c)
At least part thermal cracking of oil is to obtain the deasphalted oil of thermal cracking twice.
It preferably, will be such as the complete thermal cracking deasphalted oil thermal cracking obtained in step (b) in step (c).
According to a preferred embodiment, conversion ratio of second cracking step (c) in 25wt% to 80wt% range,
More preferably operated under the conversion ratio of 30wt% to 75wt%.
Second thermal cracking is usually carried out in the case where reducibility gas such as hydrogen is not present.Cracking can be there are steam
In the case where carry out.It can change the condition that can carry out thermal cracking.When people can arbitrarily adjust temperature, pressure and stop
Between, so that desired conversion ratio occurs.It will be apparent to those skilled in the art that on the one hand can in high temperature and
Under short residence time, identical conversion ratio is on the other hand obtained under lower temperature but longer dwell time.In addition, cracking reaction
It is heat absorption, therefore in the case where soaking pit cracking, the temperature on entire cracking zone is often reduced.Therefore, art technology
Personnel will select the condition in cracking zone, so that desired level of conversion will be obtained.Suitable cracking condition includes 350 DEG C
To 600 DEG C of temperature, 1 bar to 100 bars of absolute pressure and 0.5 minute to 60 minutes residence time.Residence time with it is cold
Raw material is related.
Since thermal cracking deasphalted oil is relatively clean, but the processing of the first thermal cracking is already subjected to, therefore have found second
Condition needed for reaching desired level of conversion in cracking step in the first cracking step usually than reaching identical turn
Condition needed for rate is tightened up.For example, if residence time and pressure are kept constant between two cracking steps, the
Two cracking steps usually can 10 DEG C to 80 DEG C higher than temperature used in the first cracking step at a temperature of carry out, with
Reach identical level of conversion.
The thermal cracking depitching product of thermal cracking is the pure depitching product of heavy again in step (c).This means that extremely
Few 45wt%, preferably at least 65wt%, more preferably at least 80wt%, and even more preferably at least 85wt% is stayed in
The boiling point of the depitching product handled in step (c) is higher than 550 DEG C.With hydrogenating conversion process (as in such as EP 1731588A1
Disclosed method) it is different, as all undiluted depitching product now can be in step (c) obtained in step (b)
Processing, and may not be needed dilution depitching product before depitching product is further processed.Of the invention one is excellent
Point is that such undiluted heavy depitching product can be further processed, to obtain distillating among the low-sulfur of such high yield
Object.
The deasphalted oil of thermal cracking twice is typically included lightweight distillate and middle distillate (naphtha, kerosene, gas
Oil) and boiling point be higher than 370 DEG C (5wt% point, i.e. 95wt.% boiling point are higher than 370 DEG C) of residual fraction.In addition, it should be understood that
Cracking step is gaseous product under environment temperature and atmospheric pressure by generating.
According to a preferred embodiment, the deasphalted oil of thermal cracking twice is separated into one or more boiling points and is lower than
370 DEG C of fraction (95wt.% point, i.e. highest 5wt.% boiling point are higher than 370 DEG C)；One or more boiling points are in vacuum gas oil (VGO) model
Fraction and residual oil in enclosing (most 5wt.% boiling points are lower than 550 DEG C).
The residual oil (that is, at most 5wt.% boiling point is lower than 550 DEG C) generated in this embodiment can be used for as is generally known in the art
Any purposes, be such as used for fuel oil, pitch, gasifier feed, including gasification step is to obtain hydrogen and carbon monoxide or power station
Charging.It should be appreciated that residual oil does not meet the stringent maximum sulphur specification of recently introduced fuel oil, but its sulfur content is greater than
0.5wt.%, typically at least 2wt.%, such as 2.5wt.% to 7wt.%.
If desired, at least part of residual oil may be used as boiling point within the scope of fuel oil and fire in low-sulfur of the invention
Sulfur content is greater than the fraction of 0.5wt% in oil or fuel oil blend components.
In step (d), at least part of the deasphalted oil such as the thermal cracking obtained in step (c) twice is added into hydrogen
Cracking, obtains hydrocrackates.It preferably, in one embodiment, will be as obtained in the step (c) in step (d)
The deasphalted oil product hydrocracking of whole thermal crackings twice.However, for the present invention, by whole thermal crackings taking off twice
Pitch oil product hydrocracking is not important.
It should be appreciated that making boiling point at one of the thermal cracking deasphalted oil twice of naphtha, kerosene and gas oil range
Lease making be may not be necessary by hydrocracking step.On the contrary, making boiling point lower than 370 DEG C of (95wt.% points, i.e. highest 5wt.%
Boiling point is higher than 370 DEG C) thermal cracking deasphalted oil twice a part be subjected to hydrotreating step may be it is enough and
It is actually preferred.
Therefore, in a preferred embodiment, by boiling point within the scope of vacuum gas oil (VGO) and higher thermal cracking twice
Deasphalted oil fraction (most 5wt.% boiling points be lower than 320 DEG C, preferably up to 5wt.% boiling point be lower than 370 DEG C) in step
(d) hydrocracking in.
Tenor in the deasphalted oil of thermal cracking of the boiling point within the scope of vacuum gas oil (VGO) twice may be sufficiently low, with
Just allow the hydrocracking of the deasphalted oil of thermal cracking twice in the case where not making hydrocracking catalyst cross moderate intoxication.It can connect
The tenor level received depends on the tenor in the charging of used hydrocracking catalyst and the method for the present invention, and
Tenor in the charging of the method for the present invention then depends on the thick charging of oil plant.If desired, hydrocracking unit packet
It includes with the active guard bed of further hydrodemetallization or catalyst bed, it is, however, preferable that not needing in individual unit
Carry out individual hydrodemetallization step.
It has now surprisingly been found that the deasphalted oil of thermal cracking of the boiling point within the scope of vacuum gas oil (VGO) twice has phase
To low tenor.Therefore, according to a highly advantageous elaboration of the invention, hot tearing of the boiling point within the scope of vacuum gas oil (VGO)
The deasphalted oil fraction of solution twice is used as the charging of hydrocracking step (d).
It is therefore preferable that at least 20wt.%, more preferably at least 40wt.%, even more desirably at least 60wt.%, even more excellent
Select at least 80wt.%, even more desirably at least 90wt.%, even more desirably at least 95wt.%, it is even more preferably whole as
The deasphalted oil fraction of thermal cracking of the boiling point obtained in step (c) within the scope of vacuum gas oil (VGO) twice is hydrogenated cracking.
In this embodiment, the residual fraction that boiling point is higher than the deasphalted oil of the thermal cracking of vacuum gas oil (VGO) range twice can
For use as fuel oil, pitch, gasifier feed, including gasification step to obtain hydrogen and carbon monoxide or power station charging.Remaining grade
Divide the stringent maximum sulphur specification for not meeting recently introduced fuel oil usually, but its sulfur content is greater than 0.5wt%.
If desired, at least part of residual fraction may be used as boiling point within the scope of fuel oil and of the invention low
Sulfur content is greater than the fraction of 0.5wt% in sulphur fuel oil or fuel oil blend components.
Alternatively, residual fraction is used as the charging of hydrodemetallization unit, as described in WO2015/097199.
Hydrocracking in step (d) is preferably depositing the temperature in the case of hydrogen within the scope of 300 DEG C to 500 DEG C
It carries out down and under the pressure within the scope of 80 bars to 250 bars.
Hydrocracking according to the method for the present invention the step of (d) can carry out in any manner known in the art.
Hydrocracking step is usually using hydrocracking catalyst.In general, at least one of catalyst used in hydrocracking area
It is acid.In general, hydrocracking carries out at high temperature and pressure there are hydrogen and hydrocracking catalyst.It is logical
Often, hydrocracking catalyst by carrier such as aluminium oxide, silica, silica-alumina or zeolite be in element, oxygen
One or more metals from nickel, tungsten, cobalt and molybdenum of compound or sulphided form are constituted.There are many can be applied to the present invention
Commercially available hydrocracking catalyst in method.Preferably, in the catalyst used in hydrocracking area at least
One is acidity, that is, contain a part of silica-alumina and/or zeolite component as carrier.
Hydrocracking in step (d) can carry out in single-stage or multistage operations mode.In the feelings of single stage operation mode
Under condition, it is stacking bed at the top of reforming catalyst that hydrodenitrogeneration/first order hydrocracking catalyst can be preferably used.Especially
Preferred hydrodenitrogeneration/first order hydrocracking catalyst is NiMo/Al2O3 and CoMo/Al2O3, optionally uses phosphorus and/or fluorine
Promote.Preferred reforming catalyst is based on NiW/ zeolite or NiW/ zeolite/silica-alumina reforming catalyst.Step
Suddenly preferred hydrocracking conditions are 80 bars to 250 bars in (d), preferably 90 bars to 220 bars of operating pressure, and at 300 DEG C
Temperature to 500 DEG C, within the scope of more preferable 320 DEG C to 460 DEG C, even more preferably 350 DEG C to 430 DEG C.
In step (e), it is subjected at least part such as the hydrocrackates obtained in step (d) at separation
Reason, obtains at least one middle distillate fraction.Preferably, in step (e), make as obtained in the step (d) all plus
Hydrogen pyrolysis product is subjected to separating treatment.
In general, also obtaining residual fraction in the separating treatment of step (e).
According to one embodiment, it is preferable that at least part of residual fraction is recycled to step (d).
According to one embodiment, will preferably at least 20wt.%, more preferably at least 40wt.%, even more desirably at least
60wt.%, even more desirably at least 80wt.%, even more desirably at least 90wt.%, even more desirably at least 95wt.% are followed again
Ring is to step (d).
According to another embodiment, in the separating treatment carried out in step (e), residual fraction, the remnants are also obtained
At least part of fraction is subjected to further hydrocracking step (f), and as the hydrocracking obtained in step (f) produces
At least part of object is recycled to step (e).
According to another embodiment, it is subjected at least part such as the hydrocrackates obtained in step (d) point
From processing, the fraction of at least one middle distillate fraction and boiling point within the scope of fuel oil is obtained.
Separating treatment in step (e) usually can be fractionation processing, and the fractionation processing is preferably in 50 DEG C to 400 DEG C models
At a temperature of in enclosing, more preferably at a temperature in the range of 70 DEG C to 370 DEG C, and preferably within the scope of 0.03 bar to 15 bars
Pressure more preferably carries out under the pressure within the scope of 0.05 bar to 10 bars.
Preferably, at least 80wt.% as obtained in the separating treatment of step (e) according to one embodiment of present invention
Residual fraction boiling point be higher than 370 DEG C.Preferably, at least 90wt.%'s is same obtained in the separating treatment of step (e)
The boiling point of residual fraction is higher than 370 DEG C.
According to another embodiment, at least part of the equally residual fraction obtained in step (e) can be followed again
Ring is to step (a).
Alternatively, according to another embodiment of the invention, residual fraction is also used as fluid catalytic cracking
(FCC) charging of unit or the raw material as lubricating oil manufacture.Certainly, the combination of these selections is also possible.
In order to realize optimal middle distillate yield, preferably make the residual fraction obtained in step (e) extremely
Few a part is again subjected to hydrocracking to improve the yield of middle distillate.It therefore, in a preferred embodiment, will be same
At least part of sample residual fraction obtained in step (e), more preferable 5wt% to 30wt% are recycled to step (d).
In yet another preferred embodiment, at least part of the equally residual fraction obtained in step (e) is passed through
By further hydrocracking step (f), and will be such as at least one of the hydrocrackates obtained in such step (f)
Divide and is recycled to step (e).
Preferably, the hydrocracking in step (d) and/or step (f) carries out in two or more reaction zones.It is preferred that
Ground, two or more reaction zones press stacked bed deployment arrangements.
According to another preferred embodiment, at least part of residual fraction is made to be subjected to further hydrocracking step
To generate hydrocrackates (f)；And preferably make at least part such as the hydrocrackates obtained in step (f)
It is subjected to separating treatment.Separation can individually carry out or with for the method for the present invention the step of in (e) identical unit into
Row.Preferably, separating step is carried out to obtain at least fraction of middle distillate fraction and boiling point within the scope of fuel oil.
As the bitumen product obtained in step (b) can use in many ways.For example, it can burn for electricity
The steam-electric accreting of power and steam.Alternatively, it can partly burn with the vapour for the production of clean fuel gas, electric power and steam
Electric symbiosis, hydrogen manufacture or hydrocarbon synthesis.Alternatively by being granulated answering in pitch, emulsion fuel or solid fuel
With.
Preferably, at least part such as the bitumen product obtained in step (b) is made to be subjected to gasification step (h) to obtain
Hydrogen and carbon monoxide.Preferably, such gasification step (h) is partial combustion step.
In a preferred embodiment, such as at least part of the hydrogen obtained in step (h) is recycled to step (d)
At least one of (f).
As the middle distillate obtained in step (e) generally contains less than the sulphur of 10ppmwt.Preferably, centre distillates
Object contains the sulphur less than 8ppmwt, the more preferably less than sulphur of 6ppmwt, and the sulphur of most preferably in less than 5ppmwt.
Method of the invention can produce super-low sulfur fuel oil by remaining hydrocarbon-containing feedstock in one embodiment and centre distillates
Object the described method comprises the following steps:
(a) in the first thermal cracking unit by the remaining hydrocarbon-containing feedstock thermal cracking with obtain include thermal cracking residual oil heat
Pyrolysis product；
(b) at least make the thermal cracking residual oil depitching to obtain thermal cracking deasphalted oil and bitumen product；
(c) in the second thermal cracking unit by least part thermal cracking of the thermal cracking deasphalted oil to obtain hot tearing
The product of solution twice, the product include the deasphalted oil of thermal cracking twice；
It (d) will be such as at least part hydrocracking of the deasphalted oil of the thermal cracking twice obtained in step (c)
To obtain hydrocrackates；
(e) optionally make at least part such as the hydrocrackates obtained in step (d) be subjected to separating treatment with
Obtain the fraction of at least one middle distillate fraction and boiling point within the scope of fuel oil；
(f) at least part of fraction of the boiling point within the scope of fuel oil is made to be subjected to further hydrocracking step to generate
Hydrocrackates (f)；And
(g) at least part such as the hydrocrackates obtained in step (f) is made to be subjected to separating treatment with obtain to
The fraction of a kind of few middle distillate fraction and boiling point within the scope of fuel oil.
It should be appreciated that whether isolating super-low sulfur fuel oil in the method for the invention is a kind of warp for conche
Selection in Ji.The shortcomings that super-low sulfur middle distillate is engine, especially through designing by peculiar to vessel the starting of fuel oil driving
Machine may need to adapt to be capable of handling super-low sulfur middle distillate such as diesel oil.
Therefore, according to another aspect, the present invention provides a kind of sulfur content 0.03wt.% to be less than 0.5wt.% range
Interior Low Sulfur Fuel Oil or fuel oil blend components comprising 50wt.% to 95wt.%'s can be required from such as claim 10
The step of method of protection (e) or the boiling point (g) obtained, the sulphur of the fraction and 5wt.% to 50wt.% within the scope of fuel oil contained
Fraction of boiling point of the amount greater than 0.5wt.% within the scope of fuel oil.
In the embodiment of the method for the present invention shown in Fig. 1, crude oil or blends of crudes 1 are divided in air-distillation unit 20
Evaporate into a variety of distillate products 14 (usually LPG, naphtha and gas oil) and reduced crude 2.Reduced crude 2 is being evaporated under reduced pressure
One or more vacuum distillation products 15 (usually vacuum gas oil (VGO)) and decompression residuum 3 are fractionated into unit 30.
Decompression residuum 3 is fed in thermal cracking unit 40 to (usually thermal cracking subtracts to generate a variety of thermal cracking products 16
Press gas oil and thermal cracking gas oil and compared with light product) and thermal cracking residual oil 4.
At least part of thermal cracking residual oil 4 passes to Solvent deasphalting unit 50 via pipeline 6.Optionally, thermal cracking slag
A part of oil 4 passes to storage device via pipeline 5 and is used as fuel oil, pitch, gasifier feed, comprising gasification step to obtain
Hydrogen and carbon monoxide or power station feed (not shown).
In Solvent deasphalting unit 50, makes thermal cracking residual oil and propane, iso-butane, butane, pentane, isopentane or it is mixed
Object is closed to contact as solvent.Solvent is fed in Solvent deasphalting unit 50 via pipeline 19.The deasphalted oil of thermal cracking via
Pipeline 8 leaves unit 50 and bitumen product is left via pipeline 7.
In unit 50, solvent is mixed with thermal cracking residual oil, and extracts hot tearing from residual oil using solvent and free drip
Green oil.In the unit, solvent is removed from extract via unshowned device, and via pipeline 21 and unshowned another
Outer device is recycled to pipeline 19 to be re-introduced into device 50.
At least part of thermal cracking deasphalted oil in pipeline 8 passes to the second thermal cracking unit 60 via pipeline 9 to produce
One or more fractions of the deasphalted oil of heat cracking twice.Residual fraction (95wt.% boiling point is higher than 550 DEG C) is via pipeline
11 pass to storage device and are used as fuel oil, pitch, gasifier feed, comprising gasification step to obtain hydrogen and carbon monoxide, or
Power station feeds (not shown).
Optionally, a part of thermal cracking deasphalted oil is recycled to vacuum distillation unit 30 via pipeline 10.At one
In alternate embodiment, a part of thermal cracking deasphalted oil is optionally recycled to 40 (not shown) of thermal cracking unit.Root
According to a preferred embodiment, will at least 90 weight %, the thermal cracking deasphalted oil of more preferably at least 95wt% passes to the second heat
Crack unit 60.According to a particularly preferred embodiment, do not use thermal cracking deasphalted oil via the circulation of pipeline 10.
The deasphalted oil of thermal cracking twice is usually fractionated into pressure reduction gas oil product, residual fraction and one or more
Compared with light product.At least the deasphalted oil of thermal cracking of the boiling point within the scope of vacuum gas oil (VGO) twice is fed to via pipeline 12 adds hydrogen
It cracks in unit 70 to generate hydrocrackates 17.
Optionally, a part of the relatively light product from unit 60, product of the normally boiling in gas oil range can be with
Hydrotreating unit 80 is fed to via pipeline 12 and is fed to the hydrotreating unit via pipeline 13 compared with light product, is produced
Raw hydrotreatment products 18.
Certain terms used herein are defined as follows:
Conversion ratio is defined as net " 520 DEG C subtract " conversion per pass, be calculated as 100%* [(charging mid-boiling point be equal to or
Wt% higher than 520 DEG C)-(product mid-boiling point is equal to or higher than 520 DEG C of wt%)]/(charging mid-boiling point is equal to or higher than 520
DEG C wt%).The wt% of charging or product mid-boiling point equal to or higher than 520 DEG C is measured according to ASTM D2887.
Extraction depth is defined as the yield of " 520 DEG C add " material of extraction, is calculated as 100%* and (boils in extraction product
Point equal to or higher than 520 DEG C wt%* extract flow velocity [kg/ second])/(charging mid-boiling point be equal to or higher than 520 DEG C wt%* into
Stream speed [kg/ seconds]), and measured according to ASTM D2887.
Vacuum gas oil (VGO) range be defined as most 5wt% boiling points at 320 DEG C hereinafter, and at least 90wt% boiling point exist
550 DEG C according to ASTM D2887 hereinafter, and measure.
Fuel oil range is defined as fraction of the boiling point higher than 370 DEG C (5wt% point, i.e. 95wt.% boiling point are higher than 370 DEG C),
And it is measured according to ASTM D2887.Therefore, fuel oil range generally includes fraction and/or boiling of the boiling point within the scope of vacuum gas oil (VGO)
Select the fraction higher than vacuum gas oil (VGO) range.
The present disclosure is not limited to embodiment as described above and the appended claims.It is contemplated that many modifications and can be with
Combine the feature of each embodiment.
Claims (12)
1. a kind of method for by remaining hydrocarbon-containing feedstock production middle distillate, the described method comprises the following steps:
(a) in the first thermal cracking unit by the remaining hydrocarbon-containing feedstock thermal cracking with obtain include thermal cracking residual oil thermal cracking
Product；
(b) at least make the thermal cracking residual oil depitching to obtain thermal cracking deasphalted oil and bitumen product；
(c) in the second thermal cracking unit by least part thermal cracking of the thermal cracking deasphalted oil to obtain thermal cracking two
Secondary deasphalted oil；
It (d) will be if at least part hydrocracking of the deasphalted oil of the thermal cracking twice obtained in step (c) is to obtain
To hydrocrackates；And
(e) at least part such as the hydrocrackates obtained in step (d) is made to be subjected to separating treatment with obtain to
A kind of few middle distillate fraction.
2. according to the method described in claim 1, the thermal cracking products are separated into heat by the wherein cracking step (a)
Pyrolysis residue and one or more thermal cracking distillates.
3. method according to claim 1 or 2, wherein the cracking step (a) is in 25wt.% to 45wt.% range
It is operated under interior conversion ratio.
4. method according to any of the preceding claims, wherein step (b) is handled by means of solvent deasphalting and is carried out
And it is operated under the extraction depth in 25wt.% to 65wt.% range.
5. method according to any of the preceding claims, wherein second cracking step (c) is arrived in 25wt.%
It is operated under conversion ratio within the scope of 80wt.%.
6. the method according to any one of claims 1 to 5, wherein the hydrocracking in step (d) is there are hydrogen
It is carried out in the case where gas at a temperature in the range of 300 DEG C to 500 DEG C and under the pressure within the scope of 80 bars to 250 bars.
7. method according to any one of claim 1 to 6, the hot tearing of the mid-boiling point within the scope of vacuum gas oil (VGO)
The deasphalted oil fraction of solution twice is used as the charging of hydrocracking step (d).
8. method according to any one of claim 1 to 6, wherein in the separating treatment carried out in step (e),
Residual fraction is also obtained, at least part of the residual fraction is recycled to step (d).
9. method according to any one of claim 1 to 6, wherein in the separating treatment carried out in step (e),
Residual fraction is also obtained, at least part of the residual fraction is subjected to further hydrocracking step (f), and such as in step
Suddenly at least part of the hydrocrackates obtained in (f) is recycled to step (e).
10. method according to any one of claim 1 to 9, wherein making such as the Asphalt Production obtained in step (b)
At least part of object is subjected to gasification step (h) to obtain hydrogen and carbon monoxide.
11. it is a kind of for by remaining hydrocarbon-containing feedstock production super-low sulfur fuel oil and middle distillate method, the method includes with
Lower step:
(a) in the first thermal cracking unit by the remaining hydrocarbon-containing feedstock thermal cracking with obtain include thermal cracking residual oil thermal cracking
Product；
(b) at least make the thermal cracking residual oil depitching to obtain thermal cracking deasphalted oil and bitumen product；
(c) in the second thermal cracking unit by least part thermal cracking of the thermal cracking deasphalted oil to obtain thermal cracking two
Secondary product, the product include the deasphalted oil of thermal cracking twice；
(d) by at least partly hydrocracking such as the deasphalted oil of the thermal cracking twice obtained in step (c) to obtain
Hydrocrackates；
(e) at least part such as the hydrocrackates obtained in step (d) is made to be subjected to separating treatment with obtain to
The fraction of a kind of few middle distillate fraction and boiling point within the scope of fuel oil；
(f) at least part of the fraction of the boiling point within the scope of the fuel oil is optionally made to be subjected to further hydrocracking
Step is to generate hydrocrackates (f)；And
(g) at least part such as the hydrocrackates obtained in step (f) is made to be subjected to separating treatment with obtain to
The fraction of a kind of few middle distillate fraction and boiling point within the scope of the fuel oil.
12. a kind of sulfur content is in 0.03wt.% to the Low Sulfur Fuel Oil or fuel oil blend components being less than within the scope of 0.5wt.%, packet
Include 50wt.% to 95wt.% can be from the method according to claim 11 the step of (e) or the boiling point that (g) obtains exist
Boiling point of the sulfur content of fraction and 5wt.% to 50wt.% within the scope of fuel oil greater than 0.5wt.% is within the scope of the fuel oil
Fraction.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP16207042 | 2016-12-28 | ||
| EP16207042.9 | 2016-12-28 | ||
| PCT/EP2017/084668 WO2018122274A1 (en) | 2016-12-28 | 2017-12-27 | Process for producing middle distillates |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110114445A true CN110114445A (en) | 2019-08-09 |
Family
ID=57614261
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780078935.3A Pending CN110114445A (en) | 2016-12-28 | 2017-12-27 | Method for producing middle distillate |
Country Status (3)
| Country | Link |
|---|---|
| EP (1) | EP3562916A1 (en) |
| CN (1) | CN110114445A (en) |
| WO (1) | WO2018122274A1 (en) |
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| US10696906B2 (en) | 2017-09-29 | 2020-06-30 | Marathon Petroleum Company Lp | Tower bottoms coke catching device |
| US12000720B2 (en) | 2018-09-10 | 2024-06-04 | Marathon Petroleum Company Lp | Product inventory monitoring |
| CN113544239A (en) | 2018-12-04 | 2021-10-22 | 沙特基础全球技术有限公司 | Optimizing the simultaneous production of high value chemicals and fuels from heavy hydrocarbons |
| EP3921389A1 (en) * | 2019-02-05 | 2021-12-15 | Shell Internationale Research Maatschappij B.V. | Residue conversion |
| US11975316B2 (en) | 2019-05-09 | 2024-05-07 | Marathon Petroleum Company Lp | Methods and reforming systems for re-dispersing platinum on reforming catalyst |
| CA3109606C (en) | 2020-02-19 | 2022-12-06 | Marathon Petroleum Company Lp | Low sulfur fuel oil blends for paraffinic resid stability and associated methods |
| US11905468B2 (en) | 2021-02-25 | 2024-02-20 | Marathon Petroleum Company Lp | Assemblies and methods for enhancing control of fluid catalytic cracking (FCC) processes using spectroscopic analyzers |
| US11898109B2 (en) | 2021-02-25 | 2024-02-13 | Marathon Petroleum Company Lp | Assemblies and methods for enhancing control of hydrotreating and fluid catalytic cracking (FCC) processes using spectroscopic analyzers |
| US20220268694A1 (en) | 2021-02-25 | 2022-08-25 | Marathon Petroleum Company Lp | Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers |
| US11692141B2 (en) | 2021-10-10 | 2023-07-04 | Marathon Petroleum Company Lp | Methods and systems for enhancing processing of hydrocarbons in a fluid catalytic cracking unit using a renewable additive |
| CA3188122A1 (en) | 2022-01-31 | 2023-07-31 | Marathon Petroleum Company Lp | Systems and methods for reducing rendered fats pour point |
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| CN1044116A (en) * | 1988-12-05 | 1990-07-25 | 国际壳牌研究有限公司 | The method of conversion of heavy hydrocar-bonaccous feedstock |
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| Publication number | Publication date |
|---|---|
| EP3562916A1 (en) | 2019-11-06 |
| WO2018122274A1 (en) | 2018-07-05 |
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