CN1272524A - Middle-pressure hydrocracking method - Google Patents
Middle-pressure hydrocracking method Download PDFInfo
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- CN1272524A CN1272524A CN00110437A CN00110437A CN1272524A CN 1272524 A CN1272524 A CN 1272524A CN 00110437 A CN00110437 A CN 00110437A CN 00110437 A CN00110437 A CN 00110437A CN 1272524 A CN1272524 A CN 1272524A
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- hydrocracking
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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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
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Abstract
The present invention discloses a medium-pressure hydrocracking process for producing qualified aviation kerosene, and is characterized by that on the basis of existent medium-pressure hydrocracking process is utilizes new hydrogen resource and increases a hydrogenation saturation reactor to make the aviation kerosene fraction obtained by original hydrocracking system undergo the process of selective deep hydrogenation saturation reaction to make the quality of aviation kerosene fraction meet the index requirements.
Description
The present invention relates to a kind ofly produce high-quality automotive fuel special middle pressure hydrocracking-hydroprocessing process of producing the boat coal by inferior heavy oil.
Along with the continuous development of national economy, market constantly increases the demand of petroleum chemicals.Corresponding, Chinese land sweet crude oil inadequate resource needs a large amount of processing import high-sulfur crude oils.This just makes with FCC to be that the most of Chinese refinery of main force's device is faced with how to transform the needs of processing high-sulfur crude oil to adapt to.The experience of processing high-sulfur crude oil shows both at home and abroad, and hydrocracking is to solve the main means that the high-sulfur wax oil transforms.Yet the high investment that the hydrocracking high-tension apparatus is caused, and a large amount of development that the heavy demand of hydrogen resource limited widely hydrocracking.This to be limited in China even more serious relatively, and therefore urgent hope can be sought out the new process of this difficult problem of solution.
The hydrocracking general operation has plurality of advantages such as turndown ratio is big, good product quality in the pressure rating of 15.0MPa.Yet construction investment height, hydrogen consumption are greatly its unfavorable factors.For being in want of funds and the situation of cheap hydrogen source such as Sweet natural gas, contradiction will be more outstanding.But hydrocracking process is for processing various advantages that high-sulfur crude oil showed, still makes it to have to be other not available status of non-hydrogen process and effect, becomes one of process of refining slip-stick artist first-selection.In order to overcome the defective of hydrocracking technology, can people begin to inquire into the working pressure that reduce hydrocracking very early, and obtained very big progress, successfully developed middle pressure hydrocracking or MHUG technology (as patent US4971680), its working pressure can be reduced to about 7.0MPa.But this hydrocracking technology that improves catalyst performance and reduction working pressure that merely relies on also has its inherent defective, owing to be subjected to the restriction of thermodynamic(al)equilibrium, the aromatic hydrocarbons saturation depth is lower, and quality product is subjected to certain influence.Particularly to the boat coal, because a large amount of aromatic hydrocarbons is transformed into this cut and can not be effectively in addition saturated, thus the requirement that makes quality such as its smoke point not reach quality index.This just greatly reduces the applicability of middle pressure hydrocracking process.
Can develop a kind of middle pressure hydrocracking technology, make it to keep the various advantages of hydrocracking process, can overcome deficiencies such as its investment is high, the hydrogen consumption is big simultaneously again be the starting point of the present invention.More precisely be to solve the product quality problem that brings owing to the aromatic hydrocarbons desaturation under the middle pressure hydrocracking condition, the product quality problem of the coal that particularly navigates.Chat as preceding institute, simple improvement catalyzer and reduce working pressure and be difficult to solve this contradiction must be considered the method for dealing with problems from the angle of technical process.
Hydrocracking after pressure reduces, its subject matter are that aromaticity content raises in the product because the hydrogenation scarce capacity causes.Owing to can do reformer feed, the rising of aromaticity content can not bring adverse influence concerning petroleum naphtha, and in contrast, it can reduce the operating severity of catalytic reforming, has reduced unnecessary hydrogen consumption.To diesel oil distillate because the aromaticity content of high-pressure hydrocracking corresponding product is all very low, quality index such as cetane value are superfluous greatly, few, the hydrogenation saturation depth decline of hydrogen depletion behind the reduced pressure operation, but the requirement that touches the mark of generally still ensuring the quality of products is more reasonable from the angle of economy.But to boat coal cut aromatic hydrocarbons is the important factor that influences quality product.Aromaticity content and smoke point are two important indicators of boat coal, and the high more boat coal smoke point of aromaticity content is low more, and in most cases, indexs such as the boat coal component aromatic hydrocarbons of middle pressure hydrocracking and smoke point all are underproof.The factor that influences hydrogenation saturated activity in the hydrocracking process be dynamic aspect, again the thermodynamics aspect arranged.On kinetics, the activity of hydrogenation component is very high on the catalyzer, but owing to is subjected to H
2S, NH
3And the poisoning influence of impurity such as organosulfur, nitrogen in the raw material, the hydrogenation activity of catalyzer can not get good performance, needs to improve temperature of reaction and improve speed of response, and the required temperature of cracking reaction is generally also higher in addition.On thermodynamics, be unfavorable for the hydrogenation saturated reaction and improve temperature of reaction.Under the condition of high-pressure hydrocracking, the hydrogen dividing potential drop has remedied the detrimental action of temperature to hydrogenation saturated reaction thermodynamic(al)equilibrium.But under the condition of middle pressure hydrocracking, temperature of reaction has reached very important degree to the effect of thermodynamic(al)equilibrium.
US4172815 has introduced the method that boat coal and diesel oil are produced in a kind of tail oil recycle to extinction, heavier petroleum fraction passes through hydrocracking reactor, fractionation boat coal part wherein then, with its part circulation, thereby improve the smoke point of boat product of coal, but there is significant disadvantages in this technical process, can only be applicable to boat coal smoke point technological process higher, that only need raising 2～3mm to satisfy the demand, and the boat coal smoke point of middle pressure hydrocracking generally is lower than 20mm, therefore limited this technology in the use of depressing, the coal that particularly navigates partly circulates and will inevitably reduce the boat yield of coal.
The described technology of US5026472 is to pass through gas-liquid separator, adjust the pressure and temperature of gas-liquid separator, enter hydrogenator after making boat coal cut and the remaining hydrogen of reaction mixing, after the reactant gas-liquid separation, part gas circulation enters cracking case, and a part enters the refining reaction device.Because it is to the post-treatment of boat coal component, therefore can under condition of high voltage, produce qualified boat product of coal, but shortcoming is a complex technical process, and contains a large amount of H owing to enter the hydrogen of refining reaction device
2S, NH
3, H
2Impurity such as O have reduced refining section reactivity worth, and the suitable kind of refining section catalyzer is restricted, such as: some noble metal catalysts or go back that ortho states is non-noble metal fullly to be closed catalyzer and can not be suitable for.
The objective of the invention is to overcome the defective that the middle pressure hydrocracking process is difficult to the qualified boat coal of direct production, improve the practicality of middle pressure hydrocracking technology.
Obviously, a kind of scheme of dealing with problems is that the hydrogenation saturated reaction is occurred under the best condition, does not promptly have H
2S, NH
3Reach the condition of paralysers such as organosulfur, nitrogen.This condition can reach by suitable arrangement technical process in the process of middle pressure hydrocracking.Vertical institute is known, and through after the hydrocracking, the vapour in the product, coal, diesel oil sulphur, nitrogen content are lower, and generally below 5 μ g/g, and new hydrogen or hydrogen make-up do not contain H substantially in hydrocracking process
2S, NH
3Deng the gas phase catalysis poisonous substance.Method of the present invention is that the boat coal in the cracked product is separated, and part is navigated, and to carry out hydrogenation under the hydrocatalyst for saturating effect saturated for the new hydrogen of coal cut utilization, very finishes the purpose of improving boat ature of coal amount under the demulcent reaction conditions.The characteristics that present method is the most outstanding are the abilities that made full use of the middle pressure hydrocracking system, greatly reduce investment.Be embodied in: 1 needn't increase new hydrogen and circulating hydrogen compressor; 2 have saved a large amount of heating and heat-exchange equipment; 3 shared cover separation systems do not increase fractionation apparatus.
For the convenience on narrating, middle pressure hydrocracking of the present invention system is divided into middle pressure hydrocracking unit, hydrogenation saturation unit and separation system.Wherein the middle pressure hydrocracking unit comprises single hop serial hydrocracking reactor, or two sections serial hydrocracking reactors; The hydrogenation saturation unit comprises a hydrogenation saturating reactor and a phase separator; Separation system comprises low branch, stripping tower and separation column etc.
The present invention is under middle pressure and hydrocracking condition, and stock oil is contacted with hydrocracking catalyst, and reaction product is isolated gas-liquid two-phase through high score, and gas-phase product is circulated to the hydrocracking unit as recycle hydrogen; Liquid product enters separation column and isolates petroleum naphtha, boat coal, diesel oil and tail oil, improvements be the required hydrogen make-up of this middle pressure hydrocracking process (new hydrogen) at first under hydrocatalyst for saturating and hydrogenation saturation conditions through a boat coal hydrogenation saturation unit, and then enter the middle pressure hydrocracking unit, the saturated raw material of said boat coal hydrogenation is from the part in the separation column overhead product boat coal cut, promptly utilize this part hydrogen, catalyzer exist and the hydrogenation saturation conditions under, the part of middle pressure hydrocracking output navigated, and to carry out hydrogenation saturated for coal.In the effluent of boat coal hydrogenation saturation unit, gas hydrogen as a supplement continues to enter the middle pressure hydrocracking unit, and product liquid can directly enter separation system.In this process, coal is saturated by deep hydrogenation under extremely superior condition because part is navigated, and boat product of coal quality is significantly improved, and can reach the product index requirement.Hydrocracking unit wherein can be a period of hydrocracking flow process or two-stage hydrocracking flow process.
In the present invention, employed catalyzer in middle pressure hydrocracking unit and operational condition and general middle pressure hydrocracking condition are similar, promptly select middle pressure hydrocracking catalyzer commonly used, processing condition are generally: temperature of reaction 360-400 ℃, pressure 4.0-8.0MPa, hydrogen to oil volume ratio 800: 1-1500: 1 and air speed 0.5-1.5h
-1
In the present invention, the hydrogenation saturation unit adopts hydrocatalyst for saturating, and this catalyzer can be a noble metal catalyst, also can be non-precious metal catalyst, because it is higher to go back the catalyst activity of ortho states, so catalyzer preferably carries out former also activation before use.Reductive method and condition can select conventional method of reducing and condition to carry out.
The saturated processing condition that adopt of hydrogenation are: temperature of reaction 100-280 ℃, and preferred 100-200 ℃, reaction pressure 1.0-5.0MPa, preferred 1.0-2.0MPa, hydrogen to oil volume ratio 200: 1-1000: 1, volume space velocity 1.0-6.0h
-1The boat coal and the product boat coal weight ratio (hereinafter to be referred as reflux ratio) that enter the hydrogenation saturation unit can be determined according to the needed quality of product, are generally 1: 6-6: 1.
Fig. 1 is the present invention program's a concrete technical process.
Further specify technical solution of the present invention below in conjunction with accompanying drawing.
The present invention program's principle technical process (Fig. 1) is: stock oil (1) through raw oil pump (2) pressurization back with also pressurize from phase separator (1 2) after gas phase and mix from the circulation gas of recycle compressor (5), add hydrocracking unit (3) reaction, after high score (4) is divided into gas-liquid two-phase, gas phase is circulated by recycle compressor (5) supercharging reaction product through the heat exchange cooling.Liquid phase separates the system of heating up in a steamer (6) and is divided into different products by the weight of cut through the rear section, tail oil (11) can loop back the hydrocracking system, also can directly go out device.An isolated kerosene(oil)fraction part goes out product boat coal, and a part (10) is mixed into hydrogenation saturating reactor (8) by recycle pump (7) and hydrogen make-up (new hydrogen 9), goes phase separator (12) to carry out gas-liquid separation after the saturated product heat exchange of hydrogenation.Go to cracking unit (3) after the gas phase supercharging, liquid phase is directly gone fractionating system.The hydrocracking unit can adopt single hop list agent technology or two sections tandem process processes.The single hop technical process can be adopted unformed hydrocracking catalyst, also can adopt the molecular sieve type hydrocracking catalyst; Two-stage process also can adopt the one stage hydrofining catalyzer, second section hydrocracking catalyst.The hydrogenation saturation unit is a simple hydrogenation saturation system, and pressure can be lower than 2.0MPa, and therefore investment is very low.The condition and the result of embodiment provide in table 4.
From above-mentioned narration as can be seen, middle pressure hydrocracking technology of the present invention has following characteristics:
1, on the basis of original hydrocracking process flow process, increased the part circulation process of boat coal cut, the resulting low-quality kerosene of middle pressure hydrocracking has further been improved produce high-quality boat product of coal.
2, consider the kinetics and the thermodynamic characteristics of hydrogenation saturated reaction from the angle of technical process fully, the hydrogenation saturated reaction of boat coal cut is occurred under the optimal conditions, improved the efficient of catalyzed reaction greatly.
3, utilizing new hydrogen at first the advantage that boat coal cut carries out the hydrogenation saturated reaction to be produced in hydrocracking is not have H in the new hydrogen
2S, NH
3Deng the paralyser of hydrogenation saturated reaction, thereby guaranteed that the hydrogenation saturated reaction can take place under highly active condition.
4, resulting boat coal cut after the hydrocracking is carried out hydrogenation is saturated to have a special advantage, because impurity such as the sulphur of hydrocracking boat coal cut, nitrogen remove substantially, can not cause the hydrocatalyst for saturating poisoning and deactivation, guarantee saturated efficiently the carrying out of aromatic hydrocarbons.
5, adopting the advantage of boat coal cut part circulation process is the ability of having simplified technical process widely, having made full use of hydrocracking equipment, makes investment compare increase seldom with common middle pressure hydrocracking.Particularly, it is saturated to utilize new hydrogen earlier boat coal cut to be carried out hydrogenation before entering the hydrocracking system, and new hydrogen system is reused under extremely limited investment condition fully; Boat coal hydrogenation saturated products enters the hydrocracking system once more, the shared cover of itself and isocrackate is separated and fractionating system, thereby make it need not increase extra investment basically.
6, will navigate that the coal cut fraction hydrogenation is saturated to engage with middle pressure hydrocracking, valuable hydrogen resource is obtained fully, effectively and reasonably application.Comparatively speaking, novel process has promptly kept the advantage of middle pressure hydrocracking, has overcome middle pressure hydrocracking can not guarantee the to navigate shortcoming of coal cut fraction hydrogenation saturation depth again.Change an angle, novel process can make that to be used in the limited hydrogen resource set that boat coal cut is carried out deep hydrogenation saturated, has avoided image height to press hydrocracking like that petroleum naphtha and diesel oil distillate to be carried out unnecessary deep hydrogenation.
7, the hydrocatalyst for saturating that uses the present invention program to provide can be finished the hydrogenation saturated reaction of boat coal under lower pressure, reduce facility investment and process cost greatly.
The effect of technical solution of the present invention is described below by embodiment.
Table 1 is a kind of typical middle pressure hydrocracking stock oil main character, and following examples and comparative example all adopt this raw material.
Comparative example 1
Processing condition that middle pressure hydrocracking two-stage process flow process is adopted and product distribute.See Table 2.
Comparative example 1 produces boat coal character and sees Table 3.Higher by the boat coal aromaticity content that the visible middle pressure hydrocracking of table 3 is produced, smoke point is 18, does not reach boat coal index request, and this just greatly reduces the operability of middle pressure hydrocracking process.
On the basis of comparative example 1 hydrocracking process, only increase a boat coal hydrogenation saturation unit, under different processing condition, produce boat coal and other product.Processing condition and the results are shown in Table 4, as can be seen from Table 4, the boat coal that adopts the inventive method to produce can reduce aromaticity content significantly, improves smoke point, is the fine rocket engine fuel.
Table 1 stock oil character
| Density (20 ℃), g/cm 3 | ????0.9047 |
| Boiling range, ℃ IBP/10% 30%/50% 70%/90% 95%/EBP | ????328/376 ????403/423 ????440/466 ????483/508 |
| Sulphur, w% | ????0.55 |
| Nitrogen, μ g/g | ????1599 |
Table 2 two-stage process flow process middle pressure hydrocracking reaction conditions and product distribute
(3936 Hydrobon catalysts, 3905 hydrocracking catalysts) for Fushun No.3 Petroleum Factory's catalyst plant production for Fushun No.3 Petroleum Factory's catalyst plant production
| Catalyzer | ????3936/3905 |
| Pressure, MPa | ????7.5 |
| Temperature, ℃ | ????377/380 |
| Air speed, h -1 | ????0.7/1.60 |
| Hydrogen to oil volume ratio | ????1000∶1 |
| Product distributes, ℃ | |
| ????＜82 | ????6.5 |
| ????82-132 | ????12.1 |
| ????132-282 | ????36.3 |
| ????282-350 | ????9.3 |
| ????＞350 | ????32.8 |
Table 3 comparative example 1 produces boat coal character
| Boat coal cut character: | |
| Density (20 ℃), g/cm 3 | ????0.8173 |
| Boiling range, ℃: | ????ASTM?D?86 |
| ????IBP/10％ | ????148/164 |
| ????30％/50％ | ????179/198 |
| ????70％/90％ | ????219/244 |
| ????98％/FBP | ????261/263 |
| Freezing point, ℃ | ????＜-60 |
| Flash-point, ℃ | ????39 |
| Smoke point, mm | ????18 |
| Aromatic hydrocarbons, v% | ????20.9 |
| Sulphur content, μ g/g | ????9 |
Table 4 the present invention produces boat coal hydrogenation saturated result
| Embodiment | Embodiment |
| 1 | | | |
| Catalyzer | Base metal is ortho states also | Base metal also ortho states is urged | Noble metal catalyst |
| Rerum natura before catalyzer uses | |||
| Weight metal is formed | Elemental nickel, 34% | Elemental nickel, 29% | Pd/Pt atomic ratio=0.2 |
| Nickel oxide, 20% | Nickel oxide, 17% | ????Pd+Pt＝1.0％ | |
| Aluminum oxide, m% | Surplus | Surplus | Surplus |
| Specific surface area, m 2/g | ??156 | ??142 | ????302 |
| Pore volume, ml/g | ??0.25 | ??0.28 | ????0.31 |
| Processing condition | |||
| Boat coal reflux ratio | ??1∶1 | ??3∶1 | ????1∶3 |
| The hydrogen dividing potential drop, MPa | ??1.2 | ??1.3 | ????4.0 |
| Temperature, ℃ | ??120 | ??130 | ????250 |
| Air speed, h -1 | ??2.0 | ??3.0 | ????4.0 |
| Hydrogen to oil volume ratio | ??300∶1 | ??400∶1 | ????400∶1 |
| Product boat coal character | |||
| Density (20 ℃), g/cm 3 | ??0.8080 | ??0.8101 | ????0.7981 |
| Boiling range, ℃: | ???????????????????????ASTM?D?86 | ||
| ????IBP/10％ | ??147/164 | ??150/164 | ????146/159 |
| ????30％/50％ | ??177/198 | ??179/200 | ????169/189 |
| ????70％/90％ ???????????????? | ??218/243 | ??220/246 | ????210/238 |
| ????98％/FBP | ??260/263 | ??262/265 | ????260/264 |
| Smoke point, mm | ??27 | ??28 | ????31 |
| Aromatic hydrocarbons, v% | ??5 | ??4 | ????0.7 |
Claims (7)
1, a kind of middle pressure hydrocracking method under middle pressure and hydrocracking condition, makes stock oil contact with hydrocracking catalyst, and reaction product is isolated gas-liquid two-phase through high score, and gas-phase product is circulated to the hydrocracking unit as recycle hydrogen; Liquid product enters separation column and isolates petroleum naphtha, boat coal, diesel oil and tail oil, it is characterized in that the required hydrogen make-up of this middle pressure hydrocracking process at first under hydrocatalyst for saturating and hydrogenation saturation conditions through a boat coal hydrogenation saturation unit, and then enter the middle pressure hydrocracking unit, the saturated raw material of said boat coal hydrogenation is from the part in the separation column overhead product boat coal cut, in the effluent of boat coal hydrogenation saturation unit, gas hydrogen as a supplement continues to enter the middle pressure hydrocracking unit, and product liquid directly enters above-mentioned separation column.
2, in accordance with the method for claim 1, it is characterized in that said hydrocracking unit is a period of hydrocracking flow process or two-stage hydrocracking flow process.
3, in accordance with the method for claim 1, it is characterized in that said hydrogenation saturation unit is made of a hydrogenation saturating reactor and a phase separator, its charging is from the part boat coal cut of fractionating system and the new hydrogen of part of middle pressure hydrocracking system.
4, in accordance with the method for claim 1, it is characterized in that the middle pressure hydrocracking reactor is at temperature of reaction 360-400 ℃, pressure 4.0-8.0MPa, hydrogen to oil volume ratio 800: 1-1500: 1 and air speed 0.5-1.5h
-1Operate under the condition.
5, in accordance with the method for claim 1, it is characterized in that said hydrogenation saturation process condition is: temperature 100-280 ℃, pressure 1.0-5.0MPa, hydrogen to oil volume ratio 200: 1-1000: 1, air speed 1.0-6.0h
-1Operate under the condition, reflux ratio is 1: 6～6: 1.
6, in accordance with the method for claim 5, it is characterized in that described temperature is 100-200 ℃, pressure is 10-2.0MPa.
7, in accordance with the method for claim 1, it is characterized in that said hydrocatalyst for saturating be contain Pt or nickel go back the ortho states catalyzer.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00110437A CN1114679C (en) | 2000-05-19 | 2000-05-19 | Middle-pressure hydrocracking method |
| SG200102992A SG94823A1 (en) | 2000-05-19 | 2001-05-18 | A medium-pressure hydrocracking process |
| US09/860,353 US20020008050A1 (en) | 2000-05-19 | 2001-05-18 | Medium-pressure hydrocracking process |
| US10/842,814 US7238276B2 (en) | 2000-05-19 | 2004-05-11 | Medium-pressure hydrocracking process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00110437A CN1114679C (en) | 2000-05-19 | 2000-05-19 | Middle-pressure hydrocracking method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1272524A true CN1272524A (en) | 2000-11-08 |
| CN1114679C CN1114679C (en) | 2003-07-16 |
Family
ID=4580427
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN00110437A Expired - Lifetime CN1114679C (en) | 2000-05-19 | 2000-05-19 | Middle-pressure hydrocracking method |
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| Country | Link |
|---|---|
| US (1) | US20020008050A1 (en) |
| CN (1) | CN1114679C (en) |
| SG (1) | SG94823A1 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100448956C (en) * | 2005-10-19 | 2009-01-07 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN101148614B (en) * | 2006-09-20 | 2010-08-18 | 中国石油化工股份有限公司 | One-stage serial hydrocracking method |
| CN101724455B (en) * | 2008-10-29 | 2012-09-12 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN107177375A (en) * | 2016-03-10 | 2017-09-19 | 中国石油化工股份有限公司 | A kind of straight-run diesel oil produces the method for hydrogen cracking of jet fuel |
| CN111318300A (en) * | 2018-12-13 | 2020-06-23 | 中国石油化工股份有限公司 | Hydrocracking catalyst, and preparation method and application thereof |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100351346C (en) * | 2004-07-14 | 2007-11-28 | 中国石油化工股份有限公司 | Medium pressure hydrocracking process for preparing jet fuel |
| CN106770891A (en) * | 2016-12-30 | 2017-05-31 | 神华集团有限责任公司 | Catalyst test apparatus and evaluation method |
| CN113969180A (en) * | 2021-10-27 | 2022-01-25 | 中国石油化工股份有限公司 | Low-pressure hydrogenation dearomatization method for hydrocracking diesel oil fraction |
| CN114149828B (en) * | 2021-11-24 | 2023-05-23 | 中国石油化工股份有限公司 | No. 5 industrial white oil and preparation method thereof |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1152028C (en) * | 1996-07-01 | 2004-06-02 | 陶氏环球技术公司 | Process for the direct oxidation of olefins to olefin oxides |
| US6645388B2 (en) * | 1999-12-22 | 2003-11-11 | Kimberly-Clark Corporation | Leukocyte depletion filter media, filter produced therefrom, method of making same and method of using same |
| US6379535B1 (en) * | 2000-04-25 | 2002-04-30 | Uop Llc | Hydrocracking process |
-
2000
- 2000-05-19 CN CN00110437A patent/CN1114679C/en not_active Expired - Lifetime
-
2001
- 2001-05-18 US US09/860,353 patent/US20020008050A1/en not_active Abandoned
- 2001-05-18 SG SG200102992A patent/SG94823A1/en unknown
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100448956C (en) * | 2005-10-19 | 2009-01-07 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN101148614B (en) * | 2006-09-20 | 2010-08-18 | 中国石油化工股份有限公司 | One-stage serial hydrocracking method |
| CN101724455B (en) * | 2008-10-29 | 2012-09-12 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN107177375A (en) * | 2016-03-10 | 2017-09-19 | 中国石油化工股份有限公司 | A kind of straight-run diesel oil produces the method for hydrogen cracking of jet fuel |
| CN107177375B (en) * | 2016-03-10 | 2020-10-16 | 中国石油化工股份有限公司 | Hydrocracking method for producing jet fuel from straight-run diesel oil |
| CN111318300A (en) * | 2018-12-13 | 2020-06-23 | 中国石油化工股份有限公司 | Hydrocracking catalyst, and preparation method and application thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1114679C (en) | 2003-07-16 |
| SG94823A1 (en) | 2003-03-18 |
| US20020008050A1 (en) | 2002-01-24 |
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