CN1257105A - Medium pressure hydrocracking method - Google Patents
Medium pressure hydrocracking method Download PDFInfo
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Abstract
A medium pressure hydrocracking process for producing qualified aviation kerosine is characterized by utilizing new hydrogen resource to implement selective overhydrosaturation reaction of aviation kerosine fraction obtained by means of medium pressure hydrocracking reaction on the basis of existent medium pressure hydrocracking process so as to make aviation kerosine fraction under a very beneficial condition produce a qualified product which meets the index requirements.
Description
The present invention relates to a kind of middle pressure hydrocracking technology of producing high-quality automotive fuel, particularly rocket engine fuel 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, the heavy crude 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 that boat coal smoke point is higher, only need to improve the technological process that 2～3mm can 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 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 fraction 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: the full catalyzer that closes of some noble metal catalysts or metal penta 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 under the condition of paralysers such as organosulfur, nitrogen.This condition can reach by suitable arrangement technical process in the process of middle pressure hydrocracking.We know, through after the hydrocracking, and vapour, coal in the product, even the organosulfur in the diesel oil, nitrogen are general all below 5 μ g/g, and in all gases of hydrocracking, new hydrogen or hydrogen make-up also are substantially devoid of H
2S, NH
3Deng the gas phase catalysis poisonous substance.Method of the present invention is after the boat coal cut in the cracked product is told, and part is navigated, and to carry out hydrogenation once more under the effect of hydrogenation catalyst saturated for the new hydrogen of coal cut utilization, is not difficult to imagine and very can finishes the purpose of improving boat product of coal quality under the demulcent condition.Carry out the saturated method of hydrogenation separately with the coal cut that will navigate on another set of hydrogenation unit and compare, 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.Particularly: 1, needn't increase new hydrogen and circulating hydrogen compressor newly; 2, a large amount of heating and cold exchange device have been saved; 3, a shared cover separates fractionating system.In order to reach this purpose, the present invention can have multiple arrangement from technical process, and they are respectively series process, series process in parallel and multiple process etc.
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 the one-stage serial hydrocracking reactor, or the single-stage hydrocracking reactor; The hydrogenation saturation unit comprises an independent hydrogenation saturating reactor, or 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 are that the required hydrogen make-up of this middle pressure hydrocracking process (new hydrogen) is at first 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 enter the middle pressure hydrocracking unit, perhaps directly enters 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.
In the present invention, unitary operation of middle pressure hydrocracking and general middle pressure hydrocracking condition are similar, that is: 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
-1The hydrogenation saturation unit when adopting Hydrobon catalyst, temperature of reaction 250-350 ℃, pressure 4.0-8.0MPa, hydrogen to oil volume ratio 400: 1-1000: 1 and air speed 0.4-1.0h
-1When adopting hydrocatalyst for saturating, temperature of reaction 100-200 ℃, pressure 4.0-8.0MPa, hydrogen to oil volume ratio 400: 1-1000: 1 and air speed 2.0-4.0h
-1
Specifically, technical scheme of the present invention can be divided into series process, series and parallel method and multiple process.
Series process is suitable for hydrocracking raw material oil nature situation preferably, its principle process flow diagram (Fig. 1) is: stock oil (1) is through raw oil pump (2) pressurization back and from the oil of hydrogenation saturation unit (8), gas and mix from the circulation gas of recycle compressor (5), enter hydrocracking unit (3) reaction, reaction product heat exchange cooling is divided into gas after high-pressure separator (4) is called for short " high score ", the liquid two-phase, gas phase is circulated by recycle compressor (5) supercharging, liquid phase through the rear section from, fractionating system (6) is divided into different products by the weight of cut, and 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 part boat coal (10) is mixed into hydrogenation saturation unit (8) with hydrogen make-up (new hydrogen 9) after by recycle pump (7) supercharging.The hydrocracking unit promptly can adopt single hop list agent technology, also can be series connection one-stage process flow process.Catalyst system therefor promptly can be molecular sieve type, also can be the amorphous silicon aluminium class.The hydrogenation saturation unit is a simple hydrofining reaction system, and used catalyzer can be general Hydrobon catalyst or special-purpose hydrocatalyst for saturating.Series process technology is comparatively simple, compares with general hydrocracking, by the condition of selecting catalyst and reaction suitably, often only needs to increase a hot oil pump (7) and a hydrogenation saturating reactor (8) can be realized whole technological process.Though be that the kerosene of hydrogenation after saturated must pass through the hydrocracking reaction unit once more, the overall yield of boat coal will descend to some extent, the repeating utilization factor height of this flow sheet equipment, investment for trnasforming urban land is few, and is simple to operate.Table 1 to table 3 has been listed the exemplary embodiments of this technical process.For ease of relatively, provided the reaction result of general middle pressure hydrocracking process in these tables simultaneously.
Series process in parallel is the improvement on the series process basis, its principle process flow diagram (Fig. 2) is: stock oil (1) mixes with the gas phase of coming self-heating high score (12) and from the circulation gas of recycle compressor (5) after raw oil pump (2) pressurization, enter hydrocracking unit (3) reaction, reaction product with from the liquid-phase mixing of high score (12) and heat exchange cooling after high score (4) is divided into gas, the liquid two-phase, gas phase is circulated by recycle compressor (5) supercharging, liquid phase through the rear section from, fractionating system (6) is divided into different products by the weight of cut, and 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 saturation unit (8) with hydrogen make-up (new hydrogen 9) after by recycle pump (7) supercharging, and reducing phlegm and internal heat after the saturated product heat exchange of hydrogenation, high score (12) carries out gas, liquid separates.The hydrocracking unit promptly can adopt single hop list agent technology, also can be series connection one-stage process flow process.Catalyst system therefor promptly can be molecular sieve type, also can be the amorphous silicon aluminium class.The hydrogenation saturation unit is a simple hydrofining reaction system, and used catalyzer can be general Hydrobon catalyst or special-purpose hydrocatalyst for saturating.Compare with series process, series process in parallel has increased a hot high score (12), and the kerosene after making hydrogenation saturated no longer enters the hydrocracking reaction unit, thereby has reduced the unnecessary loss of boat product of coal.The typical consequence of embodiment also provides to table 3 at table 1.
Multiple process is the comparatively simple process program of another kind, its principle process flow diagram (Fig. 3) is: stock oil (1) mixes with circulation gas from recycle compressor (5) after raw oil pump (2) pressurization, enter hydrocracking unit (3) reaction, reaction product mix with oil gas from hydrogenation saturation unit (8) and the heat exchange cooling after high score (4) is divided into gas, the liquid two-phase, gas phase is circulated by recycle compressor (5) supercharging, liquid phase through the rear section from, fractionating system (6) is divided into different products by the weight of cut, and 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 saturation unit (8) with hydrogen make-up (new hydrogen 9) after by recycle pump (7) supercharging.The hydrocracking unit promptly can adopt single hop list agent technology, also can be series connection one-stage process flow process.Catalyst system therefor promptly can be molecular sieve type, also can be the amorphous silicon aluminium class.The hydrogenation saturation unit is a simple hydrofining reaction system, and used catalyzer can be general Hydrobon catalyst or the special-purpose full catalyzer of hydrogenation.Compare with series process, the flow process of multiple process is basic identical, and only the reaction product of hydrogenation saturation unit is by after entering to change into before the hydrocracking reaction unit into the hydrocracking reaction unit, thereby has also avoided the unnecessary loss of boat product of coal.Its disadvantage is that hydrogen make-up directly enters high score (4), therefore needs higher recycle compressor ability.Similarly, embodiment is also represented to table 3 by table 1.
From above-mentioned narration as can be seen, middle pressure hydrocracking technology of the present invention has following characteristics:
1, increased the part circulation process of boat coal cut on the basis of original hydrocracking process flow process, making the further hydrogenation of the resulting low-quality kerosene of middle pressure hydrocracking saturated is 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.
Table 1 stock oil character
| Density (20 ℃), g/cm 3 | ????0.8864 |
| Boiling range, ℃ IBP/10% 30%/50% 70%/90% 95%/EBP | ????236/316 ????357/383 ????411/449 ????473/502 |
| Sulphur, w% | ????1.33 |
| Nitrogen, μ g/g | ????714 |
| Carbon residue, w% | ????0.03 |
| ????C/H，?w％ | ????85.99/12.75 |
| Zero pour, ℃ | ????25 |
Table 2 reaction conditions and product distribute
| Technical process | Middle pressure hydrocracking | Series process | Series process in parallel | Multiple process | |||
| Reaction member catalyzer ※ pressure, the MPa temperature, ℃ air speed, the h-1 hydrogen to oil volume ratio | Cracking 393,6/3,905 7.5 380 0.7 1000 | Cracking 393,6/3,905 7.5 382 0.9 800 | Saturated FH-5 8.0 280 0.5 250 | Cracking 393,6/3,905 7.5 380 0.7 1000 | Saturated FH-5 8.0 280 0.5 250 | Cracking 393,6/3,905 7.5 380 0.7 1000 | Saturated FH-5 8.0 280 0.5 250 |
| Product distributes, ℃ 250-350 ℃＞350 ℃ of w%＜65 ℃ 65-132 ℃ 132-250 | ? ???6.30 ???15.33 ???25.59 ???23.31 ???26.86 | ? ????6.83 ????17.92 ????23.81 ????22.65 ????24.82 | ? ????6.29 ????15.51 ????25.26 ????23.97 ????25.33 | ? ????6.70 ????15.47 ????25.83 ????23.11 ????25.92 | |||
One section catalyzer of hydrocracking that ※ 3936 produces for Fushun No.3 Petroleum Factory; 3905 two sections catalyzer of hydrocracking for Fushun No.3 Petroleum Factory's production; FH-5 is the Hydrobon catalyst that Shenyang Catalyst Plant produces.
Table 3 main products character
| Technical process | Middle pressure hydrocracking | Series process | Series process in parallel | Multiple process |
| 65-132 ℃ of petroleum naphtha density (20 ℃), g/cm 3S/N, μ g/g virtue is dived w% | ? ????0.7442 ????＜0.5/＜1 ????61.0 | ? ??0.7395 ??＜0.5/＜1 ??58.5 | ? ????0.7433 ????＜0.5/＜1 ????60.5 | ? ????0.7433 ????＜0.5/＜1 ????60.0 |
| 130-250 ℃ of kerosene(oil)fraction density (20 ℃), g/cm 3Aromatic hydrocarbons, the v% smoke point, the mm freezing point, ℃ flash-point, ℃ | ? ????0.8184 ????27.3 ????15 ????＜-60 ????38 | ? ??0.7935 ??10.3 ??27 ??＜-60 ??39 | ? ????0.8086 ????13.2 ????26 ????＜-60 ????38 | ? ????0.8053 ????12.7 ????26 ????＜-60 ????38 |
| 250-350 ℃ of diesel oil density (20 ℃), g/cm 3The cetane value zero pour, ℃ | ? ????0.8360 ????49.9 ????-16 | ? ??0.8321 ??53.0 ??-11 | ? ????0.8357 ????50.0 ????-13 | ? ????0.8339 ????51.0 ????-13 |
| ＞350 ℃ of tail oil density (20 ℃), g/cm 3Zero pour, ℃ BMCI value | ? ????0.8463 ????31 ????12.7 | ? ??0.8400 ??30 ??15.0 | ? ????0.8442 ????30 ????14.0 | ? ????0.8462 ????30 ????13.0 |
Claims (9)
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 is at first 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 enters the middle pressure hydrocracking unit or directly enters separation system.
2, according to the method for claim 1, it is characterized in that separating the part boat coal cut that fractionates out and at first enter a hydrogenation saturation unit with new hydrogen, contact with hydrocatalyst for saturating under the hydrogenation saturation conditions, its product turns back to the hydrocracking unit together with the hydrogen of surplus.
3, according to the method for claim 1, it is characterized in that separating the part boat coal cut that fractionates out and at first enter a hydrogenation saturation unit with new hydrogen, under the hydrogenation saturation conditions, contact with hydrocatalyst for saturating, its product is through being separated, the hydrogen of telling enters the hydrocracking unit, as the supplemental hydrogen source of hydrocracking; The liquid product of telling then enters the cooling separation after the hydrocracking unit.
4, according to the method for claim 1, it is characterized in that separating the part boat coal cut that fractionates out and enter a hydrogenation saturation unit with new hydrogen, under the hydrogenation saturation conditions, contact with hydrocatalyst for saturating, its product turns back to hydrocracking unit cooling separation afterwards together with the hydrogen of surplus, and hydrogen wherein is as the supplemental hydrogen source of hydrocracking.
5, according to the method for claim 2, it is characterized in that said hydrogenation saturation unit is a hydrogenation saturating reactor, its charging is the new hydrogen from the part of fractionating system boat coal cut and whole middle pressure hydrocracking system.
6, according to the method for claim 3, it is characterized in that said hydrogenation saturation unit is made of a hydrogenation saturating reactor and a phase separator, its charging is the new hydrogen from the part of fractionating system boat coal cut and whole middle pressure hydrocracking system.
7, according to 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.
8,, it is characterized in that the saturated employing Hydrobon catalyst of said hydrogenation, at temperature of reaction 250-350 ℃, pressure 4.0-8.0MPa, hydrogen to oil volume ratio 400: 1-1000: 1 and air speed 0.4-1.0h according to the method for claim 1
-1Operate under the condition.
9,, it is characterized in that the saturated employing hydrocatalyst for saturating of said hydrogenation, at temperature of reaction 100-200 ℃, pressure 4.0-8.0MPa, hydrogen to oil volume ratio 400: 1-1000: 1 and air speed 2.0-4.0h according to the method for claim 1
-1Operate under the condition.
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Cited By (1)
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|---|---|---|---|---|
| CN105542851A (en) * | 2014-10-29 | 2016-05-04 | 中国石油化工股份有限公司 | Aviation kerosene production method |
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|---|---|---|---|---|
| JPS62199687A (en) * | 1986-04-28 | 1987-09-03 | ユニオン・オイル・コンパニ−・オブ・カリフオルニア | Hydrogenation using catalyst having large pores |
| US4859312A (en) * | 1987-01-12 | 1989-08-22 | Chevron Research Company | Process for making middle distillates using a silicoaluminophosphate molecular sieve |
| US5026472A (en) * | 1989-12-29 | 1991-06-25 | Uop | Hydrocracking process with integrated distillate product hydrogenation reactor |
| CN1045462C (en) * | 1996-07-22 | 1999-10-06 | 中国石油化工总公司 | Middle-pressure hydrocracking process for heavy fractional oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105542851A (en) * | 2014-10-29 | 2016-05-04 | 中国石油化工股份有限公司 | Aviation kerosene production method |
| CN105542851B (en) * | 2014-10-29 | 2017-05-24 | 中国石油化工股份有限公司 | Aviation kerosene production method |
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