CN105273754B - A kind of diesel oil ultra-deep hydrodesulfuration method - Google Patents
A kind of diesel oil ultra-deep hydrodesulfuration method Download PDFInfo
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- CN105273754B CN105273754B CN201410240178.3A CN201410240178A CN105273754B CN 105273754 B CN105273754 B CN 105273754B CN 201410240178 A CN201410240178 A CN 201410240178A CN 105273754 B CN105273754 B CN 105273754B
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Abstract
A kind of diesel oil ultra-deep hydrodesulfuration method, diesel raw material oil and hydrogen enter reactor together, hydrogenation reaction is carried out in the presence of hydrogenation catalyst I, reactor effluent is after heat exchange, into high pressure hot separator, filling hydrogenation catalyst II, the isolated liquid phase stream of high pressure hot separator obtain hydrogasoline and hydrogenated diesel oil after cooling down, being fractionated in the middle part of high pressure hot separator.The present invention can handle straight-run diesel oil or secondary processing diesel oil inferior, produce the ultra-low-sulphur diesel that sulfur content is less than 10ppm, it is not necessary to independent hydrogenation decoloring reaction device, it becomes possible to complete hydrogenation decoloring reaction, product ASTMD1500 colourities is less than 1.0.
Description
Technical field
The invention belongs to the method for the hydrocarbon oil refining under conditions of it hydrogen be present, is that a kind of diesel oil is ultra-deep more specifically
Hydrodesulfurization and discoloration method.
Background technology
With the quickening of diesel oil of vehicle trend in world wide, the demand of future diesel will be further increased.However,
Contain oxysulfide (SO in the waste gas discharged after diesel combustionX), nitrogen oxides (NOX) and particulate matter (PM) etc. it is substantial amounts of harmful
Material.These materials not only form the acid rain in city and surrounding area, destroy the ozone layer of the earth, it is also possible to cause human body to cause
Cancer.Reduce the SO in vehicle exhaustX、NOXWith the discharge capacity of the pollutant such as PM, the sulfur content in diesel oil is not only reduced, is also needed
Reduce the arene content in diesel oil.
Therefore, diesel oil standard is increasingly strict in world wide, the friendly low-sulfur of production environment or ultra-low-sulphur diesel have turned into
The problem of countries in the world government and oil refining enterprise's most attention.The diesel oil of Europe IV discharge standards, it is specified that sulfur content is less than 50 μ g/g,
Polycyclic aromatic hydrocarbon (double ring arene and bicyclic above aromatic hydrocarbons) mass fraction is less than 11%；The diesel oil of Euro V emissions is, it is specified that sulfur content
It is further lowered into and is less than 10 μ g/g.As can be seen here, the development trend of diesel quality is in world wide：Constantly reduce diesel oil
Sulfur content, while arene content and density are further reduced, Cetane number is improved, to meet more strict Abgasgesetz.
Hydrofinishing be removing raw material in sulphur, the Main Means of nitrogen heteroatom, under certain temperature, pressure, hydrogen and
Raw material reacts on a catalyst, and sulfide and nitride are separately converted to hydrogen sulfide and ammonia.Production sulfur content is less than 50 μ g/g, very
To 10 μ g/g ultra-low-sulphur diesel, generally require to improve the severity of operating condition, such as improve reaction temperature, make the sulphur in product
Content touches the mark requirement, but this will cause oil product form and aspect problem.General diesel oil distillate can because be in containing nitride it is faint yellow,
As hydrogenation reaction must occur, these hetero atoms can be removed, and diesel product color is thin out or even becomes colourless.But ultra-deep
During hydrodesulfurization, high reaction temperature can cause product to present with fluorescent yellow green, and this is primarily due to send out at high temperature
The reaction such as condensation, dehydrogenation has been given birth to, has generated free radical that is unstable, easily polymerizeing, has formed that color is relatively deep and the composition of difficult removing.
In order to keep the color of diesel product, it has been proposed that the reaction condition of hydrodesulfurization is controlled by routine techniques, or is introduced
For improving subsequent step of the hydrotreating as hydrodesulfurization of color, to improve the color of diesel oil.These routine techniques
It is as follows：
CN1115387C discloses a kind of process for deeply desulfurizing fractional oil of low hydrogen consumption, in the method diesel raw material and hydrogen
Gas is 2~7h in 2.0~8.0MPa of hydrogen dividing potential drop, 320~440 DEG C of temperature, liquid hourly space velocity (LHSV)-1, 200~700v/v of hydrogen-oil ratio condition
The contact of lower and Hydrobon catalyst, reaction effluent is 200~290 DEG C, 4~10h of liquid hourly space velocity (LHSV) in temperature-1Under conditions of with
Hydrobon catalyst contacts.Using this method, sulfur content can be produced and be less than 300 μ g/g diesel product, and improved
Diesel product colourity.
CN1115390C discloses a kind of medium pressure hydrogenation Porous deproteinized bone method of diesel oil distillate, in the method diesel raw material with
Hydrogen enters first reactor, in 330~390 DEG C of temperature, 6.0~9.0MPa of hydrogen dividing potential drop, 0.3~1.0h of liquid hourly space velocity (LHSV)-1, hydrogen oil
Than being contacted under conditions of 400~700v/v with Hydrobon catalyst, into aromatic hydrocarbons saturated reaction, first reactor effluent enters
Enter second reactor, in 250~290 DEG C of temperature, 6.0~9.0MPa of hydrogen dividing potential drop, 1.5~5.0h of liquid hourly space velocity (LHSV)-1, hydrogen-oil ratio 400
Contacted under conditions of~700v/v with Hydrobon catalyst, improve the color of reaction stream.
CN100443571C discloses a kind of diesel fraction deep desulfurization and the method for hydrotreating to decolourize, in the method raw material
Oil is mixed into the first hydrotreating reactor with hydrogen, and its reaction product enters high pressure hot separator, the liquid phase isolated
Logistics is mixed into the top hydroconversion reaction zone of the second hydrotreating reactor with hydrogen, carries out deep hydrodesulfurizationof reaction；Heat
The gaseous stream that high-pressure separator is isolated enters the middle part of the second hydrotreating reactor after cooling, is hydrogenated with herein with second
Enter bottom hydroconversion reaction zone after the top product mixing for the treatment of reactor, carry out hydrogenation decoloring reaction., can be with using this method
Produce sulfur content and meet Europe III, the fine-quality diesel oil of Europe IV discharge standards requirement, while its ASTM D1500 colourity is less than 1.0.
CN1824736B discloses a kind of two-step method for being used for preparing the ultra-low-sulphur diesel with improved color property,
In this method, reaction pressure is 40~80,000 grams/cm, reaction temperature is 330~380 DEG C, liquid hourly space velocity (LHSV) be 0.1~
2.0h-1, deep hydrodesulfurizationof is carried out to hydrocarbon ils under conditions of 150~1000v/v of hydrogen-oil ratio, the product of hydrodesulfurization is made；
Reaction pressure is 40~80,000 grams/cm, reaction temperature is 230~320 DEG C, liquid hourly space velocity (LHSV) is 4~10h-1, hydrogen-oil ratio
Under conditions of 150~1000v/v, hydrotreating is carried out to the product of the hydrodesulfurization, improves product colour.
However, on the one hand this above-mentioned several method can not produce the diesel product that sulfur content is less than 10 μ g/g, on the other hand
It is required for completing the hydrotreating reaction for improving colourity in independent reactor, equipment investment is larger.
The content of the invention
The technical problems to be solved by the invention are to produce the diesel product that sulfur content is less than 10 μ g/g in the prior art
When, it is impossible to while the problem of meet the chromaticity index of product.
Method provided by the invention, including：
(1) diesel raw material oil and hydrogen enter reactor together, and hydrogen to oil volume ratio is 100~1000Nm3/m3, urged in hydrogenation
Hydrogenation reaction is carried out in the presence of agent I,
(2) reactor effluent is after heat exchange, and into high pressure hot separator, the operating condition of high pressure hot separator is：
180~350 DEG C, 3.0~15.0MPa of pressure of temperature, high pressure hot separator middle part filling hydrogenation catalyst II, reactor effluent
By hydrogenation catalyst II bed,
(3) the isolated liquid phase stream of high pressure hot separator obtains hydrogasoline and hydrogenated diesel oil after cooling down, being fractionated,
The isolated gaseous stream of high pressure hot separator uses through being extracted out at the top of high pressure hot separator through handling Posterior circle.
The one kind of described diesel raw material oil in straight-run diesel oil, catalytic cracking diesel oil, coker gas oil, visbreaking diesel oil
Or several mixture.
The present invention will enter reactor after diesel raw material is oily and much excessive hydrogen is mixed, and in reactor and add
Hydrogen catalyst I is contacted, and carries out the reaction such as hydrodesulfurization, hydrodenitrogeneration, alkene saturation, aromatic hydrocarbons saturation and cracking, and removing is big absolutely
Most sulfur-containing compounds and nitrogen-containing compound, the sulfur content of liquid phase stream is less than 10 μ g/ in reactor effluent obtained by step (1)
g.In reactor, much excessive hydrogen and liquid phase are fully contacted, and hydrogen is sufficiently dissolved in liquid phase, in reactor outlet
Locate, the state that the hydrogen dissolved in liquid phase dissolves close to saturation.
In the reactor, hydrogen to oil volume ratio is 100~1000Nm under standard state3/m3, preferably 200~600Nm3/m3, then
It is preferred that 250~400Nm3/m3.Reactor can be one or more, can be one or more bed in reactor.
The reaction condition of reactor is：Average reaction temperature is 320~420 DEG C, preferably 340~410 DEG C, further preferably 350
~400 DEG C, preferably 3.0~15.0MPa of pressure, 5.0~12.0MPa, further preferably 6.0~10.0MPa, volume space velocity 0.5 during liquid
~6.0h-1, preferably 0.8~4.0h-1, further preferably 1.0~3.0h-1。
The hydrogenation catalyst I loaded in reactor is that the group vib being supported in unformed aluminum oxide and/or silica-alumina supports is non-
Noble metal and/or the non-noble metal catalyst of VIII, wherein group vib base metal are Mo and/or W, VIII base metal
For Ni and/or Co.
This method completes the removing of most of sulfide in the hydrogenation reactor of step (1), is reacted obtained by step (1)
The sulfur content of liquid phase stream is less than 10 μ g/g in device effluent, but some have been there remains in liquid phase stream in higher reaction
At a temperature of caused substance that show color.In step (2), reactor effluent is high into high pressure hot separator, heat after heat exchange
Pressure separator operating condition be：180~350 DEG C, 3.0~15.0MPa of pressure of temperature, high pressure hot separator middle part filling hydrogenation
Catalyst II, reactor effluent under its effect, carry out further hydrogenation reaction by hydrogenation catalyst II bed,
Improve product colourity.
Preferably 220~320 DEG C of temperature in the high pressure hot separator, further preferably 240~300 DEG C, system pressure preferably 5.0
~12.0MPa, further preferably 6.0~10.0MPa.Reactor effluent passes through hydrogenation catalyst in step (2) high pressure hot separator
Volume space velocity is 10.1~30.0h during the liquid of II beds-1, preferably 12.0~20.0h-1, further preferably 13.0~18.0h-1。
In the one of preferred embodiment of the present invention：Reactor effluent is from high pressure hot separator in step (2)
Middle and upper part enter high pressure hot separator in, reactor effluent from top to down pass through hydrogenation catalyst II bed, and set
Vapor-liquid separation tower tray in hydrogenation catalyst II lower section, the liquid phase stream outlet port of high pressure hot separator are arranged on vapor-liquid separation
The lower section of tower tray.
In presently preferred embodiment：Reactor effluent is from high pressure hot separator in step (2)
Bottom enters in high pressure hot separator, reactor effluent to the lower and upper bed by hydrogenation catalyst II, and be arranged on plus
The vapor-liquid separation tower tray of hydrogen catalyst II top, the liquid phase stream outlet port of high pressure hot separator are arranged on vapor-liquid separation tower tray
Lower section.
The described hydrogenation catalyst II loaded in high pressure hot separator is to be supported on unformed aluminum oxide and/or sial
Group vib base metal and/or the non-noble metal catalyst of VIII on carrier, wherein group vib base metal are Mo and/or W,
VIII base metal is Ni and/or Co.
The liquid phase stream of the reactor of the present invention improves product colourity under high air speed in high pressure hot separator.
This not only reduces the usage amount of catalyst compared with traditional hydrodesulfurization, discoloration method, it is thus also avoided that decoloring reaction device
Use, reduce equipment investment.
In step (3), the isolated liquid phase stream of high pressure hot separator obtained after cooling down, being fractionated hydrogasoline and
Hydrogenated diesel oil, the isolated gaseous stream of high pressure hot separator make through being extracted out at the top of high pressure hot separator through handling Posterior circle
With.Gaseous stream after depriving hydrogen sulphide is handled is recycled into reactor inlet.
Using method provided by the invention, can handle straight-run diesel oil or secondary processing diesel oil inferior (including coker gas oil,
Catalytic diesel oil) or above-mentioned raw materials mixed material, produce sulfur content less than 10 μ g/g, ASTM D1500 colourities less than 1.0
Ultra-low-sulphur diesel product.
The present invention is by the hydrotreating reaction of second segment in the prior art and the high pressure separation coupling of gas, liquid at one point
Carried out from equipment, reduce equipment investment.The present invention compared with Ultra-deep Desulfurization of Diesel Fuels, discoloration method compares, it is not necessary to
Independent hydrogenation decoloring reaction device, and hydrodesulfurization and decoloring reaction can be completed in high-speed, save investment and operation
Expense.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of diesel oil ultra-deep hydrodesulfuration method one of which embodiment provided by the invention.
Fig. 2 is the schematic flow sheet of diesel oil ultra-deep hydrodesulfuration method another embodiment provided by the invention.
Embodiment
Method provided by the invention is further described below by accompanying drawing, but it is not thereby limiting the invention,
Many equipment, such as pump, heat exchanger, compressor are eliminated in figure.
As shown in figure 1, feedstock oil is mixed through pipeline 1 with hydrogen partial through pipeline 2, the heated heated transportation of stove 4 to plus
In hydrogen reactor 5, ultra-deep hydrodesulfuration reaction is carried out under the conditions of existing for hydrogen and hydrogenation catalyst I.Gained reactor
Effluent is transported in high pressure hot separator 7 through pipeline 6, and reactor effluent is by heat exchanger heat exchange to conjunction in course of conveying
Suitable temperature.Reactor effluent from pipeline 6 enters from the middle and upper part of high pressure hot separator 7, flows through hydrogenation from top to down
Catalyst II beds 14 and be arranged on hydrogenation catalyst II lower section vapor-liquid separation tower tray 12.High pressure hot separator is separating obtained
Liquid phase effluent enter subsequent processing units through pipeline 8, obtain hydrogasoline and hydrogenated diesel oil.High pressure hot separator separates institute
The gas phase effluent obtained is extracted out through pipeline 11.Hydrogen partial can be entered the catalyst bed of reactor 5 as hydrogen make-up by pipeline 3
Interlayer.
As shown in Fig. 2 feedstock oil is mixed through pipeline 1 with hydrogen partial through pipeline 2, the heated heated transportation of stove 4 to plus
In hydrogen reactor 5, ultra-deep hydrodesulfuration reaction is carried out under the conditions of existing for hydrogen and hydrogenation catalyst I.Gained reactor
Effluent is transported in high pressure hot separator 7 through pipeline 9, and reactor effluent is by heat exchanger heat exchange to conjunction in course of conveying
Suitable temperature.Reactor effluent from pipeline 9 enters from the bottom of high pressure hot separator 7, to it is lower and on flow through hydrogenation and urge
Agent II beds 14 and be arranged on hydrogenation catalyst II top vapor-liquid separation tower tray 13.High pressure hot separator is separating obtained
Liquid phase effluent enters subsequent processing units through pipeline 10, obtains hydrogasoline and hydrogenated diesel oil.High pressure hot separator separates institute
The gas phase effluent obtained is extracted out through pipeline 11.Hydrogen partial can be entered the catalyst bed of reactor 5 as hydrogen make-up by pipeline 3
Interlayer.
The following examples will be further described to method provided by the invention, but therefore not limit this
Invention.
Embodiment and comparative example use a kind of Middle East high-sulfur straight(-run) diesel distillate straight as feedstock oil A, a kind of Middle East high-sulfur
The miscella for evaporating diesel oil distillate and catalytic cracking diesel oil cut is listed in table 1 as feedstock oil B, its fundamental property.
The product designation RS-2000 for the hydrogenation catalyst C that embodiment uses, hydrogenation catalyst D product designation RS-
1000, it is the production of Sinopec catalyst branch company.
Embodiment 1
Feedstock oil A and hydrogen together enter in the reactor equipped with hydrogenation catalyst C, hydrogen to oil volume ratio 300Nm3/m3,
Deep hydrodesulfurizationof reaction is carried out in the presence of hydrogenation catalyst C, reaction condition is：380 DEG C of reaction temperature, during raw material fluid
Volume space velocity 3.0h-1, reacting system pressure 6.0MPa, the sulfur content of liquid phase stream is less than 10 μ in gained reactor effluent
g/g。
Filling hydrogenation catalyst D in the middle part of high pressure hot separator, reactor effluent is by heat exchange by high pressure hot separator
Top enters in high pressure hot separator, passes through the beds being seated in high pressure hot separator, thermal high point from top to down
Temperature from device is 300 DEG C, pressure 6.0MPa, volume space velocity 12.0h during liquid-1.The isolated liquid phase of high pressure hot separator
Logistics obtains hydrogasoline and hydrogenated diesel oil after being cooled and separated.The reaction condition and hydrogenated diesel oil product property of the present embodiment
As shown in table 2.
Embodiment 2
Feedstock oil B and hydrogen together enter in the reactor equipped with hydrogenation catalyst C, hydrogen to oil volume ratio 500Nm3/m3,
Deep hydrodesulfurizationof reaction etc. is carried out in the presence of hydrogenation catalyst C, reaction condition is：390 DEG C of reaction temperature, raw material fluid
When volume space velocity 2.0h-1, reacting system pressure 8.0MPa.
Filling hydrogenation catalyst C in the middle part of high pressure hot separator, reactor effluent is by heat exchange by high pressure hot separator bottom
Portion enters in high pressure hot separator, to lower and the upper beds by being seated in high pressure hot separator, thermal high separate
The temperature of device is 270 DEG C, pressure 8.0MPa, volume space velocity 18.0h during liquid-1.The isolated liquid phase thing of high pressure hot separator
Stream obtains hydrogasoline and hydrogenated diesel oil after being cooled and separated.The reaction condition and hydrogenated diesel oil product property of the present embodiment are such as
Shown in table 3.
Comparative example 1
Feedstock oil A and hydrogen together enter in the reactor equipped with hydrogenation catalyst C, hydrogen to oil volume ratio 300Nm3/m3,
Deep hydrodesulfurizationof reaction is carried out in the presence of hydrogenation catalyst C, reaction condition is：380 DEG C of reaction temperature, during raw material fluid
Volume space velocity 2.4h-1, reacting system pressure is that the sulfur content of liquid phase stream in reactor effluent obtained by 6.0MPa is less than 10 μ g/
g。
Reactor effluent passes through high-pressure separator, and hydrogasoline and hydrogenation are obtained into fractionation apparatus after low pressure separator
Diesel oil.
Reaction condition and hydrogenated diesel oil product main character are as shown in table 2.
Comparative example 2
Feedstock oil B and hydrogen together enter in the reactor equipped with hydrogenation catalyst C, hydrogen to oil volume ratio 500Nm3/m3,
Deep hydrodesulfurizationof reaction is carried out in the presence of hydrogenation catalyst C, reaction condition is：390 DEG C of reaction temperature, during raw material fluid
Volume space velocity 1.8h-1, reacting system pressure 8.0MPa.The sulfur content of liquid phase stream is less than 10 μ in gained reactor effluent
g/g。
Reactor effluent passes through high-pressure separator, and hydrogasoline and hydrogenation are obtained into fractionation apparatus after low pressure separator
Diesel oil.
Reaction condition and hydrogenated diesel oil product main character are as shown in table 3.
The raw material oil nature of table 1
| Embodiment 1 | Embodiment 2 | |
| Feedstock oil | A | B |
| Density (20 DEG C), g/cm3 | 0.8462 | 0.8801 |
| Sulfur content, μ g/g | 12000 | 9200 |
| Nitrogen content, μ g/g | 200 | 429 |
| Boiling range ASTM D-86, DEG C | ||
| IBP | 206 | 195 |
| 10% | 249 | 237 |
| 50% | 272 | 282 |
| 90% | 335 | 345 |
| FBP | 358 | 371 |
Table 2
| Process conditions | Embodiment 1 | Comparative example 1 |
| Reacting system pressure, MPa | 6.0 | 6.0 |
| Hydrogen dividing potential drop, MPa | 4.8 | 4.8 |
| Reactor reaction temperature, DEG C | 380 | 380 |
| High pressure hot separator temperature, DEG C | 320 | 320 |
| Volume space velocity during reactor liquid, h-1 | 3.0 | 2.4 |
| Volume space velocity during high pressure hot separator liquid, h-1 | 12.0 | Nothing |
| Cumulative volume air speed, h-1 | 2.4 | 2.4 |
| Hydrogenated diesel oil product property | ||
| Product sulfur content, μ g/g | 8 | 8 |
| Product nitrogen content, μ g/g | <0.2 | <0.2 |
| Colourity (ASTM D1500) | 0.3 | 1.6 |
| Colourity (ASTM D1500) after placing 10 days | 0.4 | 2.4 |
As it can be seen from table 1 the feedstock oil A of embodiment 1 is a kind of high-sulfur straight(-run) diesel distillate, sulfur content is 12000 μ g/
G, nitrogen content are 200 μ g/g.From table 2 it can be seen that using the method for hydrotreating of embodiment 1, the sulfur content of product is 8 μ g/g, color
Degree is only 0.3.The method provided using comparative example 1, because no process improves the processing of colourity, although hydrogenated diesel oil product
Sulfur content is 8 μ g/g, but colourity is up to 1.6.And the product after processing of changing colour has more preferable stability, places 10
After it, the product colourity of embodiment 1 is 0.4, increase only 0.1, and the product colourity of comparative example 1 is 2.4, adds 0.8.Can
The product seen after the method provided by the present invention is handled can not only greatly improve product colourity, moreover it is possible to which the color for strengthening product is steady
It is qualitative.
Table 3
| Process conditions | Embodiment 2 | Comparative example 2 |
| Reacting system pressure, MPa | 8.0 | 8.0 |
| Hydrogen dividing potential drop, MPa | 6.4 | 6.4 |
| Reactor reaction temperature, DEG C | 390 | 390 |
| High pressure hot separator temperature, DEG C | 270 | 270 |
| Volume space velocity during reactor liquid, h-1 | 2.0 | 1.8 |
| Volume space velocity during high pressure hot separator liquid, h-1 | 18.0 | Nothing |
| Cumulative volume air speed, h-1 | 1.8 | 1.8 |
| Hydrogenated diesel oil product property | ||
| Product sulfur content, μ g/g | 7 | 7 |
| Product nitrogen content, μ g/g | 0.6 | 0.6 |
| Colourity (ASTM D1500) | 0.7 | 2.3 |
| Colourity (ASTM D1500) after placing 10 days | 0.8 | 3.5 |
As it can be seen from table 1 the feedstock oil B of embodiment 2 is a kind of high sulfur-containing diesel cut, sulfur content is 9200 μ g/g, nitrogen
Content is 429 μ g/g.From table 2 it can be seen that using the method for hydrotreating of embodiment 2, the sulfur content of product is 7 μ g/g, and colourity is only
For 0.7.The method provided using comparative example 2, due to no processing by improving colourity, although the sulphur of hydrogenated diesel oil product contains
Measure as 7 μ g/g, but colourity is up to 2.3.And the product after processing of changing colour has more preferable stability, places 10 days
Afterwards, the product colourity of embodiment 2 is 0.8, increase only 0.1, and the product colourity of comparative example 2 is 3.5, adds 1.2.It can be seen that
Product after the method provided by the present invention is handled can not only greatly improve product colourity, moreover it is possible to strengthen the colour stable of product
Property.
Claims (11)
1. a kind of diesel oil ultra-deep hydrodesulfuration method, including：
(1) diesel raw material oil and hydrogen enter reactor together, and hydrogen to oil volume ratio is 100~1000Nm3/m3, average reaction temperature
For 320~420 DEG C, 3.0~15.0MPa of system pressure, 0.5~6.0h of volume space velocity during liquid-1, in hydrogenation catalyst I effect
Lower carry out hydrogenation reaction,
(2) reactor effluent is after heat exchange, and into high pressure hot separator, the operating condition of high pressure hot separator is：Temperature
180~350 DEG C, 3.0~15.0MPa of pressure, high pressure hot separator middle part filling hydrogenation catalyst II, reactor effluent passes through
Hydrogenation catalyst II bed,
(3) the isolated liquid phase stream of high pressure hot separator obtains hydrogasoline and hydrogenated diesel oil after cooling down, being fractionated, and heat is high
The isolated gaseous stream of separator is pressed to be used through being extracted out at the top of high pressure hot separator through handling Posterior circle；
The sulfur content of liquid phase stream is less than 10 μ g/g in reactor effluent obtained by step (1).
2. in accordance with the method for claim 1, it is characterised in that described diesel raw material oil is selected from straight-run diesel oil, catalysis
One or more of mixtures in cracked diesel oil, coker gas oil, visbreaking diesel oil.
3. in accordance with the method for claim 1, it is characterised in that hydrogen to oil volume ratio in step (1) reactor for 200~
600Nm3/m3。
4. in accordance with the method for claim 1, it is characterised in that the reaction condition of step (1) reactor is：Average response temperature
Spend for 340~410 DEG C, 5.0~12.0MPa of system pressure, 1.0~4.0h of volume space velocity during liquid-1。
5. in accordance with the method for claim 1, it is characterised in that the operating condition of step (2) high pressure hot separator is：Temperature
240~300 DEG C, 5.0~12.0MPa of pressure.
6. in accordance with the method for claim 1, it is characterised in that reactor effluent leads in step (2) high pressure hot separator
Volume space velocity is 10.1~30.0h when crossing the liquid of hydrogenation catalyst II beds-1。
7. in accordance with the method for claim 1, it is characterised in that reactor effluent leads in step (2) high pressure hot separator
Volume space velocity is 12.0~20.0h when crossing the liquid of hydrogenation catalyst II beds-1。
8. in accordance with the method for claim 1, it is characterised in that reactor effluent is from high pressure hot separator in step (2)
Middle and upper part enter high pressure hot separator in, reactor effluent from top to down pass through hydrogenation catalyst II bed, and set
Vapor-liquid separation tower tray in hydrogenation catalyst II lower section, the liquid phase stream outlet port of high pressure hot separator are arranged on vapor-liquid separation
The lower section of tower tray.
9. in accordance with the method for claim 1, it is characterised in that reactor effluent is from high pressure hot separator in step (2)
Bottom enter in high pressure hot separator, reactor effluent to the lower and upper bed by hydrogenation catalyst II, and being arranged on
The vapor-liquid separation tower tray of hydrogenation catalyst II top, the liquid phase stream outlet port of high pressure hot separator are arranged on vapor-liquid separation tower
The lower section of disk.
10. in accordance with the method for claim 1, the described hydrogenation catalyst I loaded in the reactor is fixed to be supported on nothing
Group vib base metal and/or the non-noble metal catalyst of VIII, wherein group vib on type aluminum oxide and/or silica-alumina supports is non-
Noble metal is Mo and/or W, and VIII base metal is Ni and/or Co.
11. in accordance with the method for claim 1, the hydrogenation catalyst II loaded in high pressure hot separator is load
Group vib base metal and/or the non-noble metal catalyst of VIII on unformed aluminum oxide and/or silica-alumina supports, wherein
Group vib base metal is Mo and/or W, and VIII base metal is Ni and/or Co.
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| US11118123B2 (en) | 2020-02-11 | 2021-09-14 | Saudi Arabian Oil Company | Processes and systems for petrochemical production integrating coking and deep hydrogenation of coking products |
| US11142709B2 (en) | 2020-02-11 | 2021-10-12 | Saudi Arabian Oil Company | Processes and systems for petrochemical production integrating deep hydrogenation of middle distillates from gas oil hydroprocessing |
| US11142706B2 (en) | 2020-02-11 | 2021-10-12 | Saudi Arabian Oil Company | Processes and systems for petrochemical production integrating fluid catalytic cracking and deep hydrogenation of fluid catalytic cracking reaction products |
| US11124716B2 (en) | 2020-02-11 | 2021-09-21 | Saudi Arabian Oil Company | Processes and systems for petrochemical production integrating coking and deep hydrogenation of coking reaction products |
| US11142711B2 (en) | 2020-02-11 | 2021-10-12 | Saudi Arabian Oil Company | Processes and systems for petrochemical production integrating deep hydrogenation of middle distillates |
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| CN1940028A (en) * | 2005-09-28 | 2007-04-04 | 中国石油化工股份有限公司 | Diesel fraction deep desulfurization and decoloring hydrogenation |
| CN103509598A (en) * | 2012-06-15 | 2014-01-15 | 中国石油化工集团公司 | Hydrogenation system for producing ultralow-sulfur diesel oil, and method thereof |
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| CN103509598A (en) * | 2012-06-15 | 2014-01-15 | 中国石油化工集团公司 | Hydrogenation system for producing ultralow-sulfur diesel oil, and method thereof |
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