CN1940030A - Hydrogenation cracking method of high-output diesel oil from high-nitrogen content heavy raw material - Google Patents
Hydrogenation cracking method of high-output diesel oil from high-nitrogen content heavy raw material Download PDFInfo
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Abstract
Hydrogenation cracking method for qualified diesel oil from high-nitrogen content heavy raw oil is carried out by reacting by the first hydrogenation refining reactor, entering the reactant into thermal flash pot to gas-liquid separate, entering the separated liquid-phase flow and low-nitrogen content heavy raw oil into the second hydrogenation refined reactor, hydrogenation refine reacting, mixing effluent of the second hydrogenation refining reactor with effluent hydrogenation cracking reactor, entering into high-pressure separator, low-pressure separator and fractionating tower sequentially, separating out naphtha fraction, diesel fraction and tail-oil fraction, circulating all or part tail-oil fraction to hydrogenation cracking reactor for reacting. It's efficient and saves resources.
Description
Technical field
The invention belongs to a kind of is the hydrocarbon ils cleavage method that obtains low boiler cut existing under the situation of hydrogen, more particularly, is to belong to a kind of method for hydrogen cracking by high nitrogen-containing heavy raw oil high-yield diesel oil.
Background technology
In recent years, along with the degree of depth exploitation of global crude oil, crude quality becomes worse and worse, and relative density and sulphur content constantly rise; And oil product market, the world is towards the increase in demand of intermediate oil (diesel oil and kerosene), and the direction that the demand of heavy fuel oil constantly reduces develops.Therefore, oil is as a kind of non-renewable energy, and fully its last running of reasonable use is the important means of implementing resources sustainable development.In China, on the one hand along with rapid development of national economy, the light-weight fuel oil demand constantly increases, and especially the demand amplification to diesel oil is bigger; In the oil product increase in demand, the lifting of quality product becomes the bigger challenge that oil refining enterprise faces on the other hand.Hydrocracking technology is important secondary processing means, can obtain the cleaning product of compliance with environmental protection requirements when realizing the heavy oil lighting.Therefore, the development and application hydrocracking technology becomes the most effective means that address the above problem.
The hydrocracking technology adaptability to raw material is strong, residual oil that can be from the light-weight petroleum naphtha to heavy inferior.For the fuel type hydrocracking technology, its raw material mainly comprise straight run and secondary processing gained in, heavy gas oil, as normal pressure gas oil (AGO), vacuum gas oil (VGO), coker gas oil (CGO), deasphalted oil (DAO) and gelatin liquefaction last running wet goods.The gas oil that different crude oils obtains has different nitrogen contents, and quantity differs and can reach several times, and about 500 μ g/g, and the nitrogen content of the Liao Dynastyization VGO is up to 1800 μ g/g as the nitrogen content of grand celebration VGO.Process crude oil of the same race, the nitrogen content of its AGO, VGO, CGO also difference is very big, and the CGO nitrogen content is higher, usually all between 2000～6000 μ g/g.The hydrocracking full scale plant usually with the mixing oil of several raw materials as charging, carry out cracking through after the hydrofining, obtain product then.
Present hydroeracking unit, it is the hydrocracking catalyst of carrier that cracking catalyst adopts zeolite usually.The zeolite hydrocracking catalyst has active high advantage, but relatively more responsive to the impurity in the stock oil, especially nitride.This is because nitride is adsorbed on the acid sites of zeolite easily, thereby makes the catalyzer reduction even lose cracking activity fully, and the degree of inactivation depends on the extent of damage of acid sites.The present zeolite type hydrocracking catalyst that uses, general requirement is controlled its feed nitrogen content less than 20～40 μ g/g.Therefore, the raw material of present hydroeracking unit processing high nitrogen-containing all has certain difficulty.
CN1045462C discloses a kind of method for hydrogen cracking of producing diesel oil from heavy raw oil.This method is hydrofining reactor and hydrocracking reactor serial operation, middle no separating device.This method stock oil bad adaptability, diesel yield is low.
US0085154 discloses a kind of method for hydrogen cracking of handling the high nitrogen-containing distillate.This method adopts two hydrofining reactors and hydrocracking reactor serial operation, establishes flash tank between hydrofining reactor with cutting out partial foreign gas.This method adopts the parallel feeding mode, promptly circulate tail oil with enter first hydrofining reactor, flash tank, second hydrofining reactor and hydrocracking reactor successively after fresh feed mixes, therefore the hydrogen consumption is big, and the recycle hydrogen flow is big, and the circulating hydrogen compressor load is big.In addition, because this method is that the refining reaction product directly enters hydrocracking reactor, so product selectivity is poor, and diesel yield is low.
US6106694 discloses a kind of method for hydrogen cracking of high-yield diesel oil.This method has a hydrofining reactor and a hydrocracking reactor.Fresh heavy feed stock enters hydrofining reactor with the reaction product of hydrocracking reactor; The hydrofining reactor effluent separates in separation column, and last running is circulated back to hydrocracking reactor and carries out cracking reaction at the bottom of the separation column.Because cracking case outflow product and stock oils all in this method together enter hydrofining reactor, have therefore increased the load of hydrofining reactor.
Summary of the invention
The objective of the invention is on the prior art basis, a kind of method for hydrogen cracking by high nitrogen-containing heavy raw oil high-yield diesel oil is provided.
Method provided by the invention comprises: high nitrogen-containing heavy raw oil and hydrogen are mixed into first hydrofining reactor, under the effect of Hydrobon catalyst, react, the effluent of first hydrofining reactor enters hot flash tank, and the gaseous stream that heat-lightening steams the tank top goes high-pressure separator; Heat-lightening steams the liquid phase stream of pot bottom and optional low nitrogen content heavy raw material oil is mixed into second hydrofining reactor with hydrogen, under the effect of Hydrobon catalyst, react, the effluent of second hydrofining reactor with enter high-pressure separator, light pressure separator, separation column successively after the effluent of hydrocracking reactor mixes, isolate naphtha fraction, diesel oil distillate and tail oil cut through separation column; All or part of tail oil cut is recycled to hydrocracking reactor, contacts with hydrocracking catalyst in the presence of hydrogen, carries out hydrocracking reaction; Be divided into three strands from the isolated hydrogen rich stream of high-pressure separator, one with enter first hydrofining reactor after new hydrogen mixes, other does not enter second hydrofining reactor and hydrocracking reactor by two stocks.
The present invention carries out the cracked method to last running again by refining reaction device reaction product is separated earlier, has avoided the cracking reaction of diesel oil distillate in cracking case, thereby has improved the yield of diesel oil.Owing between two refining reaction devices, establish hot flash tank, reaction can be generated NH
3, H
2Gaseous impurities such as S are separated, thereby improve the hydrodenitrification efficient of the second refining reaction device, and have effectively reduced total consumption of Hydrobon catalyst.
Description of drawings
Accompanying drawing is the method for hydrogen cracking schematic flow sheet by high nitrogen-containing heavy raw oil high-yield diesel oil provided by the present invention.
Embodiment
Hydrocracking raw material mainly comprise straight run and secondary processing gained in, heavy gas oil, the gas oil that different crude oils obtains has different nitrogen contents, quantity differs and can reach several times; Nitrogen content in the crude oil processing gained gas oil of the same race also differs greatly, and for straight run gas oil, cut diazonium content more is high more, and the nitrogen content of secondary processing gained CGO and DAO is then far above straight run gas oil.The gelatin liquefaction oil composition is based on ring molecule, and its nitrogen content is also up to thousands of μ g/g.
Nitride is the poisonous substance of hydrocracking catalyst, hydrocracking raw material need earlier through hydrofining with charging in nitrogen content be removed to lower level, below general requirement 20～40 μ g/g.In addition, because the aromaticity content of hydrocracking section feeding has tangible influence to cracking conversion rate, the aromaticity content of treated oil is high more, and cracking conversion rate is low more under the similarity condition, therefore the effect of hydrofining section also is to make the aromatic hydrocarbons in the raw material saturated, is beneficial to carrying out smoothly of hydrocracking reaction.
Method provided by the invention is so concrete enforcement:
The present invention just is divided into two portions with hydrocracking raw material by nitrogen content, and nitrogen content is the high nitrogen-containing heavy raw oil greater than the heavy raw oil of 1500 μ g/g, and nitrogen content is low nitrogen content heavy raw material oil less than the heavy raw oil of 1500 μ g/g.The high nitrogen-containing heavy raw oil is a kind of in heavy vacuum gas oil, CGO, DAO, the gelatin liquefaction heavy distillate or more than one mixture wherein; Low nitrogen content heavy raw material oil is AGO, decompression light gas oil or its mixture.
High nitrogen-containing heavy raw oil and hydrogen are mixed into first hydrofining reactor, under the effect of Hydrobon catalyst, carry out reactions such as hydrogenating desulfurization, hydrodenitrification, aromatic hydrocarbons fractional saturation, reaction conditions is hydrogen dividing potential drop 5.0～20.0MPa, 260～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 200～3000Nm
3/ m
3, volume space velocity 0.2～10.0h
-1
The effluent of first hydrofining reactor enters hot flash tank.The effect of hot flash tank is with NH
3, H
2Gaseous impurities such as S separate with reaction product.The NH that hydrodenitrification generated
3Easily competitive adsorption produces restraining effect to hydrodenitrification and aromatic hydrocarbons saturated reaction on the hydrogenation sites of Hydrobon catalyst, if therefore with the NH that generates
3In time isolate reaction system, then can improve the hydrogenation activity of follow-up hydrogenation catalyst for refining greatly.The pressure of hot flash tank is identical with the first hydrofining reactor top hole pressure, and its service temperature is 100～350 ℃.The gaseous stream that heat-lightening steams the tank top goes high-pressure separator.
Heat-lightening steams the liquid phase stream of pot bottom and optional low nitrogen content heavy raw material oil is mixed into second hydrofining reactor with hydrogen, under the effect of Hydrobon catalyst, react, reaction conditions is: hydrogen dividing potential drop 5.0～20.0MPa, 260～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 200～3000Nm
3/ m
3, volume space velocity 0.2～10.0h
-1The effluent of second hydrofining reactor with enter high-pressure separator after the effluent of hydrocracking reactor mixes.The logistics of high-pressure separator bottom enters light pressure separator and carries out further gas-oil separation, and the light pressure separator bottoms enters separation column, obtains naphtha fraction, diesel oil distillate and tail oil cut by fractionation.
All or part of tail oil cut is recycled to hydrocracking reactor, contact with hydrocracking catalyst in the presence of hydrogen, carry out hydrocracking reaction, reaction conditions is: hydrogen dividing potential drop 5.0～20.0MPa, 280～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 300～3000Nm
3/ m
3, volume space velocity 0.1～10.0h
-1The tail oil recycle to extinction enters hydrocracking reactor, the problem that dizzy stupid (coronene), ovalene condensed-nuclei aromaticss such as (eight benzo naphthalenes) gathers can occur, and causes the obstruction of interchanger, air cooling etc.Therefore, the present invention takes the tail oil recycle to extinction but the method for getting rid of a small amount of tail oil outward, gathers to prevent condensed-nuclei aromatics.
Be divided into three strands from the isolated hydrogen rich stream in high-pressure separator top, one with enter first hydrofining reactor after new hydrogen mixes, other does not enter second hydrofining reactor and hydrocracking reactor by two stocks, recycles as recycle hydrogen.
The volume ratio of first hydrofining reactor and second hydrofining reactor is 1: 1～1: 5, and this can be determined by the feed properties and the ratio of high nitrogen-containing heavy feed stock and low nitrogen content heavy raw material.The Hydrobon catalyst of filling is VIB and/or the VIII family non-precious metal catalyst that loads on unformed aluminum oxide or the silica-alumina supports in first hydrofining reactor and second hydrofining reactor, catalyzer in two refining reaction devices can be identical, also can be different.
The hydrocracking catalyst of filling is VIB and/or the VIII family non-precious metal catalyst that loads on amorphous silicon aluminium and/or the Zeolite support in the hydrocracking reactor.
One of advantage of the present invention is to compare with conventional hydrocracking technology, under the situation of the same high nitrogen-containing heavy feed stock of processing, can effectively reduce the consumption of Hydrobon catalyst.The present invention separates charging with high nitrogen-containing heavy feed stock and low nitrogen content heavy raw material, establishes hot flash tank between two hydrofining reactors.Because a large amount of gaseous impurities NH that the present invention generates high nitrogen-containing heavy feed stock hydrogenation reaction
3Separate through hot flash tank, therefore improved the denitrogenation and the aromatic hydrocarbons saturation efficiency of the second hydrofining reactor catalyzer greatly, thereby reduced total consumption of Hydrobon catalyst.In addition, gaseous impurities NH
3Hydrocracking reaction is also had bigger inhibition, so the present invention has guaranteed that also hydrocracking reaction can be at small amount of N H
3Atmosphere in carry out, thereby brought into play the activity of hydrocracking catalyst better, make the quality product that obtains more excellent.
Another major advantage of the present invention is the diesel yield height.In hydrofining reactor, because Hydrobon catalyst has certain acid function, therefore generally be attended by slight cracking reaction, cause and contain the part diesel oil distillate in the hydrofining reaction product.React if the refining reaction product directly enters cracking case, this part diesel product will be given birth to reaction at cracking case relaying supervention, generate the lighter product of boiling range.In the present invention, the effluent of hydrofining reactor is introduced into separation column to be separated, and light-end products is separated, and last running enters hydrocracking reactor again and reacts, owing to avoided the cracking once more of lighting end in the refined products, thereby improved diesel yield effectively.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Accompanying drawing is the method for hydrogen cracking schematic flow sheet by high nitrogen-containing heavy raw oil high-yield diesel oil provided by the present invention.Some utility appliance among the figure such as interchanger etc. do not mark, but this is known to those of ordinary skills.
Method for hydrogen cracking flow process by high nitrogen-containing heavy raw oil high-yield diesel oil provided by the present invention is as follows:
From the high nitrogen-containing heavy raw oil of pipeline 1, after feedstock pump 3 boosts, with mix from new hydrogen, the recycle hydrogen of pipeline 5,20 respectively after enter first hydrofining reactor 6, carry out hydrofining reaction.The resultant of reaction of first hydrofining reactor 6 enters hot flash tank 7, at this isolated gas phase impurity NH that contains
3, H
2The gas of S enters high-pressure separator 10 after being discharged by hot flash tank 7 tops.The liquid stream of hot flash tank 7 bottoms with mix from pipeline 2 and the low nitrogen content heavy raw material after feedstock pump 4 boosts, this mixing raw material and enter the second refining reaction device 8 from the recycle hydrogen of pipeline 20 carries out hydrofining reaction at this.The resultant of reaction of second hydrofining reactor 8 is with after the resultant of reaction of hydrocracking reactor 9 mixes, enter high-pressure separator 10 together, carry out gas-oil separation at this, isolated hydrogen-rich gas removes circulating hydrogen compressor 11, is extracted out by pipeline 20 after compression to recycle as recycle hydrogen; Isolated liquid stream enters light pressure separator 12 and carries out further gas-oil separation after discharging from high-pressure separator 10 bottoms.Light pressure separator 12 top expellant gas are through pipeline 13 withdrawing devices, and the liquid stream of light pressure separator 12 bottoms enters separation column 14.The gas at separation column 14 tops is through pipeline 15 dischargers; Extract out by pipeline 16,17 respectively through naphtha fraction, diesel oil distillate that fractionation obtains; Tail oil cut at the bottom of separation column 14 towers is divided into two portions, and a part of tail oil cut loops back hydrocracking reactor 9 through pipeline 19 and carries out cracking reaction, and another part tail oil cut is through pipeline 18 withdrawing devices.
The following examples will give further instruction to present method, but therefore not limit present method.
Embodiment
Used stock oil A is the high nitrogen-containing heavy feed stock among the embodiment, and stock oil B is low nitrogen content heavy raw material, and its character is as shown in table 1, by table 1 as seen, the nitrogen content of two kinds of stock oils has big gap, and the nitrogen content of stock oil A is 3100 μ g/g, and the nitrogen content of stock oil B is 810 μ g/g.
The used Hydrobon catalyst and the trade names of hydrocracking catalyst are respectively RN-2 and RT-30 among the embodiment, are the production of Sinopec catalyzer branch office Chang Ling catalyst plant.
Stock oil A advances first hydrofining reactor, its resultant of reaction enters hot flash tank, the liquid phase stream of heat-lightening steaming pot bottom and stock oil B and hydrogen are mixed into second hydrofining reactor, carry out hydrofining reaction, and the weight ratio of stock oil A and stock oil B is 1: 1.The effluent of second hydrofining reactor with enter high-pressure separator, light pressure separator, separation column successively after the effluent of hydrocracking reactor mixes, isolate naphtha fraction, diesel oil distillate and tail oil cut through separation column; All the tail oil cut is recycled to hydrocracking reactor, contacts with hydrocracking catalyst in the presence of hydrogen, carries out hydrocracking reaction.
Reaction conditions is as shown in table 2, and liquid product distribution and main character are as shown in table 3.By table 3 as seen, the yield of diesel oil is 70.2 heavy %, and cetane value is 57, sulphur content＜10 μ g/g, the heavy % in polycyclic aromatic hydrocarbon content＜11.This shows, by adopting method of the present invention, can process the poor heavy raw material of high nitrogen, and maximum obtain the fine-quality diesel oil product under than the demulcent processing condition.
Table 1
| The stock oil title | A | B |
| Density (20 ℃), g/cm 3 | 0.9500 | 0.9159 |
| Nitrogen content, μ g/g | 3100 | 810 |
| Boiling range D1160, | ||
| 5％ | 363 | 358 |
| 50％ | 404 | 436 |
| 95％ | 482 | 488 |
Table 2
| The first refining reaction device: | |
| The hydrogen dividing potential drop, MPa | 12.0 |
| Temperature of reaction, ℃ | 365 |
| Volume space velocity, h -1 | 1.2 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 500 |
| Reaction outlet effluent nitrogen content, μ g/g | 210 |
| The hp flash drum temperature, ℃ | 300 |
| The second refining reaction device: | |
| The hydrogen dividing potential drop, MPa | 12.0 |
| Temperature of reaction, ℃ | 368 |
| Volume space velocity, h -1 | 1.3 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 700 |
| Reaction outlet effluent nitrogen content, μ g/g | ＜10 |
| Cracking case: | |
| The hydrogen dividing potential drop, MPa | 12.0 |
| Temperature of reaction, ℃ | 350 |
| Volume space velocity, h -1 | 2.0 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 800 |
Table 3
| Liquid product distributes | |
| Naphtha yield, heavy % | 26.3 |
| Diesel yield, heavy % | 70.2 |
| The tail oil yield, heavy % | 3.5 |
| The product main character: | |
| Petroleum naphtha: virtue is dived, heavy % | 55 |
| Diesel oil: cetane value | 57 |
| Sulphur content, μ g/g | ＜10 |
| Polycyclic aromatic hydrocarbons, heavy % | ＜11 |
| Tail oil: BMCI value | ＜10 |
Claims (5)
1, a kind of method for hydrogen cracking by high nitrogen-containing heavy raw oil high-yield diesel oil comprises the following steps:
(1), high nitrogen-containing heavy raw oil and hydrogen are mixed into first hydrofining reactor, under the effect of Hydrobon catalyst, react, the effluent of first hydrofining reactor enters hot flash tank, and the gaseous stream that heat-lightening steams the tank top goes high-pressure separator;
(2), the liquid phase stream of heat-lightening steaming pot bottom and optional low nitrogen content heavy raw material oil are mixed into second hydrofining reactor with hydrogen, under the effect of Hydrobon catalyst, react, the effluent of second hydrofining reactor with enter high-pressure separator, light pressure separator, separation column successively after the effluent of hydrocracking reactor mixes, isolate naphtha fraction, diesel oil distillate and tail oil cut through separation column;
(3), all or part of tail oil cut is recycled to hydrocracking reactor, contacts with hydrocracking catalyst in the presence of hydrogen, carries out hydrocracking reaction;
(4) be divided into three strands from the isolated hydrogen rich stream of high-pressure separator, one with enter first hydrofining reactor after new hydrogen mixes, other does not enter second hydrofining reactor and hydrocracking reactor by two stocks.
2,, it is characterized in that described high nitrogen-containing heavy raw oil is a kind of in heavy vacuum gas oil, coker gas oil, deasphalted oil, the gelatin liquefaction heavy distillate or more than one mixture wherein according to the method for claim 1; Low nitrogen content heavy raw material oil is atmospheric gas oil, decompression light gas oil or its mixture.
3, according to the method for claim 1, it is characterized in that the reaction conditions of described first hydrofining reactor and second hydrofining reactor is: hydrogen dividing potential drop 5.0～20.0MPa, 260～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 200～3000Nm
3/ m
3, volume space velocity 0.2～10.0h
-1The reaction conditions of hydrocracking reactor is: hydrogen dividing potential drop 5.0～20.0MPa, 280～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 300～3000Nm
3/ m
3, volume space velocity 0.1～10.0h
-1
4,, it is characterized in that the Hydrobon catalyst of filling in described first hydrofining reactor and second hydrofining reactor is VIB and/or the VIII family non-precious metal catalyst that loads on unformed aluminum oxide or the silica-alumina supports according to the method for claim 1.
5,, it is characterized in that the hydrocracking catalyst of filling in the described hydrocracking reactor is VIB and/or the VIII family non-precious metal catalyst that loads on amorphous silicon aluminium and/or the Zeolite support according to the method for claim 1.
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| CN102453537A (en) * | 2010-10-14 | 2012-05-16 | 中国石油化工股份有限公司 | Method for maximum production of clean diesel oil by shale oil whole fraction hydrogenation |
| CN102465018A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Technological method for hydrogenation of coker full-range distillate |
| CN103102966A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | High nitrogen raw material hydrocracking method |
| CN103789021A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | Hydroprocessing method of high-nitrogen raw materials |
| CN104419462A (en) * | 2013-08-30 | 2015-03-18 | 中国石油天然气股份有限公司 | Technique for producing clean diesel |
| CN113930256A (en) * | 2020-06-29 | 2022-01-14 | 中国石油化工股份有限公司 | Hydrocracking method for producing chemical raw materials from high-nitrogen crude oil |
| CN114437804A (en) * | 2020-10-19 | 2022-05-06 | 中国石油化工股份有限公司 | Hydrocracking method of high-nitrogen raw oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6106694A (en) * | 1998-09-29 | 2000-08-22 | Uop Llc | Hydrocracking process |
| CN1202218C (en) * | 2002-11-02 | 2005-05-18 | 中国石油化工股份有限公司 | Medium pressure hydrocracking and catalytic cracking combined process for producing low sulfur diesel oil |
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2005
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| CN102453537B (en) * | 2010-10-14 | 2014-07-23 | 中国石油化工股份有限公司 | Method for maximum production of clean diesel oil by shale oil whole fraction hydrogenation |
| CN102453537A (en) * | 2010-10-14 | 2012-05-16 | 中国石油化工股份有限公司 | Method for maximum production of clean diesel oil by shale oil whole fraction hydrogenation |
| CN102465018A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Technological method for hydrogenation of coker full-range distillate |
| CN102465018B (en) * | 2010-11-05 | 2014-07-23 | 中国石油化工股份有限公司 | Technological method for hydrogenation of coker full-range distillate |
| CN103102966A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | High nitrogen raw material hydrocracking method |
| CN103102966B (en) * | 2011-11-10 | 2015-07-22 | 中国石油化工股份有限公司 | High nitrogen raw material hydrocracking method |
| CN103789021B (en) * | 2012-11-03 | 2015-10-21 | 中国石油化工股份有限公司 | A kind of high-nitrogen stock hydroprocessing process |
| CN103789021A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | Hydroprocessing method of high-nitrogen raw materials |
| CN104419462A (en) * | 2013-08-30 | 2015-03-18 | 中国石油天然气股份有限公司 | Technique for producing clean diesel |
| CN113930256A (en) * | 2020-06-29 | 2022-01-14 | 中国石油化工股份有限公司 | Hydrocracking method for producing chemical raw materials from high-nitrogen crude oil |
| CN113930256B (en) * | 2020-06-29 | 2023-06-09 | 中国石油化工股份有限公司 | Hydrocracking method for producing chemical raw material from high-nitrogen crude oil |
| CN114437804A (en) * | 2020-10-19 | 2022-05-06 | 中国石油化工股份有限公司 | Hydrocracking method of high-nitrogen raw oil |
| CN114437804B (en) * | 2020-10-19 | 2023-07-04 | 中国石油化工股份有限公司 | Hydrocracking method of high-nitrogen raw oil |
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|---|---|
| CN100443572C (en) | 2008-12-17 |
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