CN1721509A - Medium pressure hydrocracking process for preparing jet fuel - Google Patents
Medium pressure hydrocracking process for preparing jet fuel Download PDFInfo
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- CN1721509A CN1721509A CN 200410068935 CN200410068935A CN1721509A CN 1721509 A CN1721509 A CN 1721509A CN 200410068935 CN200410068935 CN 200410068935 CN 200410068935 A CN200410068935 A CN 200410068935A CN 1721509 A CN1721509 A CN 1721509A
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Abstract
The jet fuel producing medium pressure hydrocracking process includes the following steps: mixing material oil with hydrogen for hydroprocessing, hydrocracking the hydroprocessing effluent directly, hot high pressure separating the hydrocracking effluent into gaseous matter flow and liquid matter flow, arene saturating of the gaseous matter flow in the second hydroprocessing reactor, lowering the pressure of the liquid matter flow and making it pass successively through hot low pressure separator, cold low pressure separator and fractionating tower, cold high pressure separating the effluent from the second hydroprocessing reactor into liquid phase flow and gas phase flow, circulating the gas phase flow, lowering the pressure of the liquid phase flow and making it pass successively through cold low pressure separator and fractionating tower, and separate liquid matter in the fractionating tower to obtain naphtha fraction, jet fuel fraction, diesel oil fraction and tail oil.
Description
Technical field
The present invention relates to a kind of is the hydrocarbon ils cleavage method that obtains lower boiling fraction existing under the situation of hydrogen, more particularly, is to belong to a kind of method for hydrogen cracking of producing rocket engine fuel.
Background technology
Hydrocracking technology be owing to can process than heavy feed stock, and has liquid and receive high, advantages such as product property is good, products scheme and device flexible operation, is one of effective means of heavy oil lighting always.Along with the strictness more of world wide environmental requirement, hydrocracking technology more and more is subjected to people's favor as producing clean fuel and oiling bonded effective means.
But traditional high-pressure hydrocracking technology because the pressure height, causes that investment is big, process cost is high, makes its industrial application be subjected to certain restriction.Therefore, twentieth century domestic and international hydrocracking technology of depressing in being devoted to develop of some oil companies and research unit since the eighties.Under middle press strip spare, operate, can reduce plant investment and process cost widely, with respect to high-pressure hydrocracking, its investment and process cost can reduce about 30%, the intermediate oil of energy greatly preparing hihg-quality adapts to the high requirement of current oil product market diesel and gasoline ratio simultaneously.Therefore, the middle pressure hydrocracking technology has stronger competitive power.
But because of working pressure is reduced to middle pressure, the aromatic hydrocarbons saturability reduces in hydrotreatment and the hydrocracking process, causes aromaticity content height in the kerosene(oil)fraction, smoke point lower, is difficult to satisfy the specification requirement of rocket engine fuel.Be raw material with vacuum gas oil (VGO) in the world at present, adopt method for hydrogen cracking to produce rocket engine fuel and still mainly be limited to high pressure range, in depress and produce the rocket engine fuel technology and still do not have full scale plant at present, develop therefore that a kind of to invest the middle pressure hydrocracking technology low, that jet fuel yield is high extremely urgent.
US5026472 discloses the method for a kind of hydrocracking and the refining combination producing high-quality rocket engine fuel of product cut oil repeated hydrogenation, its technical process can be briefly described as follows: cracking case comes out after product separates by twice high pressure hot separator, the kerosene(oil)fraction that obtains repeated hydrogenation in the refining reaction device is refining, and wherein catalyst system therefor is a noble metal catalyst; The come out heavy distillate of product and cracking case of refining reaction device is mixed into separation column.The technical characterstic of this method is only kerosene(oil)fraction to be made with extra care, and reaches the purpose of producing rocket engine fuel.But this method need increase more equipment, and the refining used catalyzer of repeated hydrogenation is precious metal, plant investment increase more and operation more complicated.
US4172815 discloses the single hop circulation hydrocracking route of producing rocket engine fuel and diesel oil simultaneously, and its stock oil initial boiling point is greater than 500 °F (about 260 ℃); Temperature of reaction is lower than 900 °F (about 482 ℃); Pressure is greater than 1000psig (about 6.89MPa).Its technical process is briefly described as follows: heavy raw oil is through after the hydrocracking, and its product obtains rocket engine fuel cut, diesel oil distillate and tail oil through fractionation; The rocket engine fuel cut is all or part of to be mixed with tail oil, sends cracking case back to.Though this technical process significant disadvantages is a rocket engine fuel carries out hydrocracking again and improved quality, that its yield reduces is more, the hydrogen consumption increases, and investment also increases more.
US5885440 discloses a kind of technical process that FF heat exchange cooling back repeated hydrogenation after the hydrocracking is handled, i.e. hydrocracking reactor outlet thing cools to a certain degree through heat exchange, handles in a little reactor of special back end hydrogenation again.This flow process has been avoided back end hydrogenation to be reflected under the very high temperature carrying out, and helps removing the mercaptan sulfur in boat coal and the naphtha fraction.But to be placed directly in the cracking catalyst back be a very sophisticated method to the back catalyst for refining in hydrocracking technology, and seldom have the incomplete problem of mercaptan removal.
The technical process of a kind of hydrocracking and hydrotreatment combination is disclosed among the US6315889.Raw material is not at first lowered the temperature after hydrocracked, treated, separate at first high pressure hot separator, gaseous product enters second high pressure hot separator that temperature is lower, its gas uses as recycle hydrogen after cooling off, liquid product is further handled entering a hydrotreating reactor, hydrotreatment outflow thing is mixed into cold high pressure separator with first high pressure hot separator liquid product to be separated, and obtains the finished product through fractionation again.The entire reaction system has only a recycle compressor, new hydrogen machine system and oil product separation system.The technical characterstic of this patent is that only kerosene, diesel oil distillate being carried out repeated hydrogenation makes with extra care, and reaches the purpose that reduces content of olefin in intermediate fractional oil.But this arts demand increases more equipment, and plant investment increases more and operates more complicated.
CN1272524A discloses the technical process of a kind of middle pressure hydrocracking and the combination of kerosene Deep Hydrotreating.This flow process is that the kerosene(oil)fraction oil of the higher aromaticity content that will obtain in the middle pressure hydrocracking process is higher at a lower pressure, hydrogen purity, to carry out aromatic hydrocarbons under than the condition of low reaction temperatures saturated, and catalyst system therefor is the catalyzer that contains Pt or Ni as-reduced metal.This patent can be handled the kerosene(oil)fraction of higher aromaticity content well, obtains qualified rocket engine fuel.But this method need increase more equipment, and the internal circulating load of kerosene(oil)fraction is bigger, has increased plant investment, and operation is more complicated.
Summary of the invention
Purpose of the present invention is exactly on the prior art basis, by reasonable adjustment to technical process, be implemented in the pressure scope, with heavy, poor quality oil is raw material, both can greatly preparing hihg-quality diesel oil, can maximum produce rocket engine fuel again, produce the unconverted tail oil that part can be used as fine catalytically cracked material, preparing ethylene by steam cracking raw material or lubricant base raw material simultaneously.
Method provided by the invention comprises:
Stock oil is mixed into hydrotreating reactor with hydrogen and contacts with hydrotreating catalyst, and the hydrotreating reactor effluent directly enters hydrocracking reactor without separation and contacts with hydrocracking catalyst, carries out hydrocracking reaction; The hydrocracking reactor effluent enters high pressure hot separator after heat exchange, the high pressure hot separator liquid phase stream enters thermal low-pressure separators, cold low separator, separation column successively after step-down, the high pressure hot separator gaseous stream directly enters second hydrotreating reactor, and it is saturated to carry out aromatic hydrocarbons; Second hydrotreating reactor effluent enters cold high pressure separator after the heat exchange cooling, in cold high pressure separator, isolate liquid phase stream and gaseous stream, wherein gaseous stream circulates after recycle compressor boosts and delivers to hydrotreating reactor inlet and use as cold hydrogen, and liquid phase stream enters cold low separator, separation column successively after step-down; It is that cold low separator, separation column are isolated naphtha fraction, rocket engine fuel cut, diesel oil distillate and tail oil by separation system that cold high pressure separator, high pressure hot separator liquid phase stream mix the back.
This method in depress the rocket engine fuel of producing low arene content, high smoke point, have characteristics such as investment is low, process cost is low, easy and simple to handle, on existing apparatus, also implement easily by appropriate reconstruction.
Description of drawings
Accompanying drawing is the middle pressure hydrocracking method synoptic diagram of production rocket engine fuel provided by the invention.
Embodiment
Method provided by the invention is so concrete enforcement:
Stock oil is mixed into hydrotreating reactor with hydrogen and contacts with hydrotreating catalyst, and the hydrotreating reactor effluent directly enters hydrocracking reactor without separation and contacts with hydrocracking catalyst, carries out hydrocracking reaction; The hydrocracking reactor effluent enters high pressure hot separator after heat exchange, the high pressure hot separator liquid phase stream enters thermal low-pressure separators, cold low separator, separation column successively after step-down, the high pressure hot separator gaseous stream directly enters second hydrotreating reactor, and it is saturated to carry out aromatic hydrocarbons; Second hydrotreating reactor effluent enters cold high pressure separator after the heat exchange cooling, in cold high pressure separator, isolate liquid phase stream and gaseous stream, wherein gaseous stream circulates after recycle compressor boosts and delivers to hydrotreating reactor inlet and use as cold hydrogen, and liquid phase stream enters cold low separator, separation column successively after step-down; It is that cold low separator, separation column are isolated naphtha fraction, rocket engine fuel cut, diesel oil distillate and tail oil by separation system that cold high pressure separator, high pressure hot separator liquid phase stream mix the back.
The boiling range of described stock oil is 180～700 ℃ and is preferably 350～550 ℃, and its sulphur content is not more than 5.0wt%, and nitrogen content is not more than 1.0wt%.This stock oil is selected from one or more mixture of this group material of being made of atmospheric gas oil (AGO), light cycle oil (LCO), VGO, coker gas oil (CGO), deasphalted oil (DAO).
The processing condition of above-mentioned three reactors are: hydrogen dividing potential drop 4.0～15.0MPa; 280～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～20h
-1, hydrogen-oil ratio 300～2000v/v.
Two used hydrotreating catalysts of hydrotreating reactor can be VIB or the VIII family non-precious metal catalysts that loads on unformed aluminum oxide or the silica-alumina supports, and hydrocracking catalyst is VIB or the VIII family non-precious metal catalyst that loads on the y-type zeolite molecular sieve.The proportional range that the catalyst volume of first hydrotreating reactor, hydrocracking reactor, second hydrotreating reactor accounts for whole catalyst volume is respectively 40%～60%, 30%～40% and 1%～20%.
When foreign matter content is high, an amount of protective material that needs to pack at first hydrotreating reactor top, the volume ratio of itself and first kind of hydrotreating catalyst is 0.03～0.3.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Accompanying drawing is the middle pressure hydrocracking method synoptic diagram of production rocket engine fuel provided by the invention, has omitted equipment such as process furnace, the pump etc. of many necessity among the figure.
The flow process of this method is described in detail as follows: raw material is after feedstock pump boosts to reaction pressure, mix with hydrogen-rich gas through pipeline 1 from pipeline 2, enter hydrotreating reactor 3, by contacting with the hydrotreating catalyst bed, remove impurity such as metal in the stock oil, sulphur and nitrogen, in desulfurization, denitrogenation, generation aromatic hydrocarbons is saturated, alkene is saturated and mild cracking.Because hydrofining is strong exothermal reaction, need in the middle of reactor, to introduce cold hydrogen with control reaction temperature through pipeline 31.The hydrotreatment reaction effluent directly enters hydrocracking reactor 5 through pipeline 4 without separating, the hydrocracking reaction effluent through heat exchange after pipeline 6 enters high pressure hot separator 7, in high pressure hot separator, be separated into two bursts of logistics, one is a gaseous stream, mainly be hydrogen, petroleum naphtha and kerosene, comprise partial vulcanization hydrogen, ammonia and light hydrocarbon simultaneously, another strand is liquid phase stream, mainly is diesel oil distillate and tail oil.This gaseous stream directly enters second hydrotreating reactor 9 through pipeline 8, mainly carries out the aromatic hydrocarbons saturated reaction, improves the kerosene(oil)fraction smoke point.This liquid phase stream through step-down after pipeline 14 enters thermal low-pressure separators 15 separates, the liquid phase stream of thermal low-pressure separators 15 enters separation column 18 through pipeline 17, the gaseous stream of thermal low-pressure separators 15 then through pipeline 16 with after the liquid phase stream of cold high pressure separator 10 mixes, enter cold low separator 12 through pipeline 11.Second hydrotreating reactor 9 outlet logistics enters cold high pressure separator 10 and is separated into gas phase and two bursts of logistics of liquid phase after the heat exchange cooling, wherein gaseous stream mainly is a hydrogen, also contain partial vulcanization hydrogen, ammonia and lighter hydrocarbons, hydrogen-rich stream enters recycle compressor 28 through pipeline 27, hydrogen-rich stream after boosting is with after new hydrogen from pipeline 26 mixes, loop back reactor 3 through pipeline 30, the liquid phase stream of cold high pressure separator 10 through after the step-down with after gaseous stream from the thermal low-pressure separators 15 of pipeline 16 mixes, enter cold low separator 12 through pipeline 11, isolate two bursts of logistics at cold low separator 12, wherein one is drawn through pipeline 29 for gaseous stream, enter the gas net gas that acts as a fuel after treatment, another strand for liquid phase stream through pipeline 13 with enter separation column 18 after thermal low-pressure separators liquid phase stream from pipeline 17 mixes.Hydrocracking generates oil and draws through pipeline 19,20,21,22 and 23 respectively at the isolated gas of separation column, naphtha fraction, kerosene(oil)fraction, diesel oil distillate and tail oil.
Technological operation of the present invention has very big handiness, and maximum is produced petroleum naphtha or rocket engine fuel, diesel oil and tail oil as requested.
When being raw material, being suitable for maximum production rocket engine fuel with VGO (or mixing refining AGO), it also is fully feasible being used to produce fine-quality diesel oil certainly.In this mode of operation, the hydrogen dividing potential drop is the preferred 6.0～10.0MPa of 5.0～12.0MPa, 280～450 ℃ preferred 350～430 ℃ of temperature of reaction, and liquid hourly space velocity is 0.1～20h
-1Preferred 0.2～3.0h
-1, hydrogen-oil ratio is the preferred 600～1000v/v of 300～2000v/v.Produce in maximum under the operating method of rocket engine fuel, the light naphthar boiling range is generally C5～65 ℃, and the heavy naphtha boiling range is generally 65～135 ℃, and the rocket engine fuel boiling range is generally 135～280 ℃.If improve transformation efficiency or full the conversion, tail oil also can be mixed into hydrotreating reactor 3 with raw material, or through improve temperature and boost after enter hydrocracking reactor 5 and carry out cracking.
The present invention adopts " online additional hydrogenation " operational path, main consideration is to increase a little hydrotreating reactor in middle pressure hydrocracking flow process (high pressure hot separator flow process), the high pressure hot separator gaseous stream directly enters this little reactor without heat exchange with separating, and replenishes hydrogenation.Contain naphtha fraction and kerosene(oil)fraction in the high pressure hot separator gaseous stream, certainly also comprise hydrogen and lighter hydrocarbons, it is saturated that this part logistics is mainly carried out aromatic hydrocarbons at hydrotreating reactor, reduces aromaticity content in the kerosene(oil)fraction, improve smoke point, satisfy the specification requirement of rocket engine fuel.Such flow arrangement just increases a very little hydrotreating reactor in original middle pressure hydrocracking flow process, do not need the device other parts are adjusted or changed, and does not also influence flexibility of operation.Temperature by suitable control high pressure hot separator just can be told from the high pressure hot separator top most kerosene(oil)fraction with the gas phase form, it is saturated to carry out aromatic hydrocarbons.And in conventional middle pressure hydrocracking all liquid product, light naphthar, heavy naphtha, diesel oil and tail oil all have good quality, are final quality products or intermediates; But kerosene(oil)fraction is difficult to satisfy the specification requirement of rocket engine fuel because of its aromaticity content height, and it is handled separately again, needs the investment and the process cost of increase higher.It is saturated that the present invention carries out aromatic hydrogenation separately to lighting end, therefore, adopts above-mentioned Technology to produce rocket engine fuel and have characteristics such as investment is low, process cost is low, easy and simple to handle, also implements easily by appropriate reconstruction on existing apparatus.In addition, in conventional hydrocracking technology, for mercaptan sulfur and the corrosion that guarantees rocket engine fuel meets the demands, directly load part back end hydrogenation catalyzer in the back of hydrocracking reactor bottom, hydrocracking catalyst usually, the air speed of this catalyzer is generally at 10～20h
-1, this is because produce the part olefin(e) compound in hydrocracking process, and the hydrogen sulfide in olefin(e) compound and the reaction atmosphere is combined to mercaptan compound.In " online additional hydrogenation " operational path, the following cut of kerosene also will be handled at little hydrotreating reactor again, and the back end hydrogenation catalyzer can omit in the hydrocracking reactor, thereby can dwindle the hydrocracking reactor volume.Original in addition sweetening reaction is unfavorable for removing of mercaptan sulfur in running (generally about 400 ℃) under the higher temperature; And little hydrotreating reactor bed temperature of reaction is about 320 ℃, more helps removing of mercaptan sulfur.All in all, use " online additional hydrogenation " operational path, the catalyzer cumulative volume can not increase or increase seldom.As everyone knows, adopt common middle pressure hydrocracking operational path, the rocket engine fuel cut of producing often smoke point can not satisfy specification requirement, it is the aromaticity content that reduces in this cut that the present invention adopts " online additional hydrogenation " operational path main purpose, improve jet pigment smoke point, reach the purpose of improving quality product.
Another advantage of the present invention is to change technological operation flexibly according to motor spirit supply/demand and market value, reaches maximum and produces diesel oil (not going out the rocket engine fuel cut) or maximum production rocket engine fuel, and be that oil refining enterprise is created maximum economic benefit.In addition, the present invention also can adopt different operating method according to the stock oil different in kind.
The following examples will give further instruction to present method, but therefore not limit present method.
The hydrotreating catalyst and the hydrocracking catalyst trade mark used in embodiment and the Comparative Examples are respectively RN-2 and RT-1, produce by the Chang Ling catalyst plant.The ratio that the catalyst volume of three reactors accounts for whole catalyst volume is followed successively by RN-2 58%, RT-1 38% and RN-2 4%.
Comparative Examples 1
This Comparative Examples adopts conventional middle pressure hydrocracking technology, and promptly the hydrocracking reaction effluent directly carries out the refining or aftertreatment in back without separating.Table 1～table 4 is respectively stock oil character, process conditions, product yield and main products character.As can be seen from Table 4, the aromatic hydrocarbons of rocket engine fuel is up to 30w%, and its smoke point only has 17mm.
Compare with Comparative Examples 1, the gaseous stream of the hydrocracking reaction effluent of present embodiment after high pressure separates carries out hydrotreatment, and other condition is all identical.Table 1～table 4 is respectively stock oil character, process conditions, product yield and main products character.
Comparing result shows that the present invention has reached and produced qualified 3 under catalyst volume increase situation seldom
#The requirement of rocket engine fuel, and product distributes and the other products change of properties is little.
Comparative Examples 2
This Comparative Examples adopts conventional middle pressure hydrocracking technology, and promptly the hydrocracking reaction effluent directly carries out the refining or aftertreatment in back without separating.Table 5～table 8 is respectively stock oil character, process conditions, product yield and main products character.
Compare with Comparative Examples 2, the gaseous stream of the hydrocracking reaction effluent of present embodiment after high pressure separates carries out hydrotreatment, and other condition is all identical.Table 5～table 8 is respectively stock oil character, process conditions, product yield and main products character.
Comparing result shows that the present invention has reached and produced qualified 3 under catalyst volume increase situation seldom
#The requirement of rocket engine fuel, and product distributes and the other products change of properties is little.
Table 1
| Stock oil character | |
| Density (20 ℃), g/cm 3 | 0.9235 |
| S，m％ | 3.1 |
| N，ppm | 898 |
| Boiling range (D-1160), | 379/446 528/553 |
Table 2
| Comparative Examples 1 | | |
| Technology | Conventional middle pressure hydrocracking | The present invention |
| Processing condition | ||
| The hydrogen dividing potential drop, MPa | 8.0 | 8.0 |
| Temperature of reaction, ℃ refining/cracking/back end hydrogenation | 375/372/372 | 375/372/330 |
| Air speed, h -1Refining section/cracking/back end hydrogenation | 1.0/1.5/15 | 1.0/1.5/8 * |
| Hydrogen-oil ratio, v/v makes with extra care section/cracking zone | 700/1000 | 700/1000 |
*Calculate with fresh feed
Table 3
| Product distribution (is benchmark with the fresh feed) | |
| 280～360 ℃ of diesel oil＞360 ℃ tail oils of 135～280 ℃ of kerosene of 65～135 ℃ of heavy naphtha of C5～65 ℃ light naphthar | 4.5m％ 14.3m％ 27.7m％ 16.0m％ 32.2m％ |
Table 4
| Comparative Examples 1 | | |||||
| Technology | Conventional middle pressure hydrocracking | The present invention | ||||
| Product | Kerosene | Diesel oil | Tail oil | Kerosene | Diesel oil | Tail oil |
| Density (20 ℃), g/cm 3 | 0.8206 | 0.8389 | 0.8408 | 0.8122 | 0.8366 | 0.8410 |
| S， | 6 | 9 | 25 | 3 | 5 | 30 |
| Condensation point, ℃ | - | -22 | 42 | - | -22 | 42 |
| Smoke point, mm | 17 | - | - | 27 | - | - |
| Aromatic hydrocarbons, w% | 30 | - | - | 13 | - | - |
| Cetane index D4737 | - | 63 | - | - | 65 | - |
| The BMCI value | - | - | 11.5 | - | - | 11.7 |
Table 5
| Stock oil character | |
| Density (20 ℃), g/cm 3 | 0.9118 |
| S，m％ | 2.5 |
| N，ppm | 1100 |
| Boiling range (D-1160), | 368/448 527/555 |
Table 6
| Comparative Examples 2 | | |
| Technology | Conventional middle pressure hydrocracking | The present invention |
| Processing condition | ||
| The hydrogen dividing potential drop, MPa | 10.0 | 10.0 |
| Temperature of reaction, ℃ refining/cracking/back end hydrogenation | 373/375/375 | 373/375/330 |
| Air speed, h -1Refining section/cracking/back end hydrogenation | 1.0/1.5/15 | 1.0/1.5/8 * |
| Hydrogen-oil ratio, v/v makes with extra care section/cracking zone | 700/1000 | 700/1000 |
*Calculate with fresh feed
Table 7
| Product yield (is benchmark with the fresh feed) | |
| 280～360 ℃ of diesel oil＞360 ℃ tail oils of 135～280 ℃ of kerosene of 65～135 ℃ of heavy naphtha of C5～65 ℃ light naphthar | 4.0m％ 16.5m％ 24.4m％ 16.0m％ 35.8m％ |
Table 8
| Comparative Examples 2 | | |||||
| Technology | Conventional middle pressure hydrocracking | The present invention | ||||
| Product | Kerosene | Diesel oil | Tail oil | Kerosene | Diesel oil | Tail oil |
| Density (20 ℃), g/cm 3 | 0.8084 | 0.8258 | 0.8369 | 0.8035 | 0.8244 | 0.8371 |
| S， | 8 | 8 | 13 | 5 | 6 | 15 |
| Condensation point, ℃ | - | -15 | 39 | - | -15 | 39 |
| Smoke point, mm | 23 | - | - | 28 | - | - |
| Aromatic hydrocarbons, w% | 14 | - | - | 6 | - | - |
| Cetane index D4737 | - | 64 | - | - | 65 | - |
| The BMCI value | - | - | 10.8 | - | - | 11.0 |
Claims (6)
1, a kind of middle pressure hydrocracking method of producing rocket engine fuel, it is characterized in that stock oil and hydrogen are mixed into hydrotreating reactor and contact with hydrotreating catalyst, the hydrotreating reactor effluent directly enters hydrocracking reactor without separation and contacts with hydrocracking catalyst, carries out hydrocracking reaction; The hydrocracking reactor effluent enters high pressure hot separator after heat exchange, the high pressure hot separator liquid phase stream enters thermal low-pressure separators, cold low separator, separation column successively after step-down, the high pressure hot separator gaseous stream directly enters second hydrotreating reactor, and it is saturated to carry out aromatic hydrocarbons; Second hydrotreating reactor effluent enters cold high pressure separator after the heat exchange cooling, in cold high pressure separator, isolate liquid phase stream and gaseous stream, wherein gaseous stream circulates after recycle compressor boosts and delivers to hydrotreating reactor inlet and use as cold hydrogen, and liquid phase stream enters cold low separator, separation column successively after step-down; It is that cold low separator, separation column are isolated naphtha fraction, rocket engine fuel cut, diesel oil distillate and tail oil by separation system that cold high pressure separator, high pressure hot separator liquid phase stream mix the back.
2,, it is characterized in that described stock oil is selected from one or more mixture of this group material that is made of vacuum gas oil, atmospheric gas oil, light cycle oil, coker gas oil, deasphalted oil according to the method for claim 1.
3, according to the method for claim 1, it is characterized in that the processing condition of three reactors are: hydrogen dividing potential drop 4.0～15.0MPa; 280～450 ℃ of temperature of reaction; Liquid hourly space velocity 0.1～20h
-1, hydrogen-oil ratio 300～2000v/v.
4,, it is characterized in that the used hydrotreating catalyst of described two hydrotreating reactors can be VIB 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 described hydrocracking catalyst is VIB or the VIII family non-precious metal catalyst that loads on the y-type zeolite molecular sieve according to the method for claim 1.
6, according to the method for claim 1, the proportional range that the catalyst volume that it is characterized in that first hydrotreating reactor, hydrocracking reactor, second hydrotreating reactor accounts for whole catalyst volume is respectively 40%～60%, 30%～40% and 1%～20%.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN100436570C (en) * | 2006-12-04 | 2008-11-26 | 中国石油化工集团公司 | Hydrogenation method for making clean fuels |
| CN102227394A (en) * | 2008-11-26 | 2011-10-26 | 埃莱文斯可更新科学公司 | Methods of producing jet fuel from natural oil feedstocks through metathesis reactions |
| CN102863985A (en) * | 2011-07-07 | 2013-01-09 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN103013559A (en) * | 2011-09-22 | 2013-04-03 | 中国石油化工股份有限公司 | Hydrocracking method for selective increasing of aviation kerosene yield |
| CN103421537A (en) * | 2012-05-15 | 2013-12-04 | 中国石油天然气股份有限公司 | Hydrogenation technology method ensuring heavy naphtha satisfying reforming feeding requirements |
| CN103773469A (en) * | 2012-10-25 | 2014-05-07 | 中国石油化工股份有限公司 | Hydrogenization method for producing high-value product by catalytic cracking diesel oil |
| CN104531212A (en) * | 2014-12-05 | 2015-04-22 | 何巨堂 | High aromatic hydrocarbon hydrogenation upgrading method by utilizing refined diesel component hydrogenation upgrading reaction process |
| CN104611019A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Low energy consumption hydrocracking method for producing high-quality jet fuel |
| CN105087061A (en) * | 2014-05-05 | 2015-11-25 | 何巨堂 | Hydrocracking method in pre-upgrading region of high aromatic hydrocarbon hydrogenation refined heavy oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1053691C (en) * | 1996-07-25 | 2000-06-21 | 刘世凯 | Hydrogenation technology |
| US6315889B1 (en) * | 1999-10-21 | 2001-11-13 | Uop Llc | Low conversion once-through hydrocracking process |
| CN1114679C (en) * | 2000-05-19 | 2003-07-16 | 中国石油化工集团公司 | Middle-pressure hydrocracking method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN100436570C (en) * | 2006-12-04 | 2008-11-26 | 中国石油化工集团公司 | Hydrogenation method for making clean fuels |
| CN102227394B (en) * | 2008-11-26 | 2014-09-24 | 埃莱文斯可更新科学公司 | Methods of producing jet fuel from natural oil feedstocks through metathesis reactions |
| CN102227394A (en) * | 2008-11-26 | 2011-10-26 | 埃莱文斯可更新科学公司 | Methods of producing jet fuel from natural oil feedstocks through metathesis reactions |
| CN102863985A (en) * | 2011-07-07 | 2013-01-09 | 中国石油化工股份有限公司 | Combined hydrogenation method |
| CN103013559A (en) * | 2011-09-22 | 2013-04-03 | 中国石油化工股份有限公司 | Hydrocracking method for selective increasing of aviation kerosene yield |
| CN103013559B (en) * | 2011-09-22 | 2015-02-25 | 中国石油化工股份有限公司 | Hydrocracking method for selective increasing of aviation kerosene yield |
| CN103421537A (en) * | 2012-05-15 | 2013-12-04 | 中国石油天然气股份有限公司 | Hydrogenation technology method ensuring heavy naphtha satisfying reforming feeding requirements |
| CN103421537B (en) * | 2012-05-15 | 2015-02-25 | 中国石油天然气股份有限公司 | Hydrogenation technology method ensuring heavy naphtha satisfying reforming feeding requirements |
| CN103773469A (en) * | 2012-10-25 | 2014-05-07 | 中国石油化工股份有限公司 | Hydrogenization method for producing high-value product by catalytic cracking diesel oil |
| CN103773469B (en) * | 2012-10-25 | 2016-08-24 | 中国石油化工股份有限公司 | A kind of method of hydrotreating being produced high-value product by catalytic cracking diesel oil |
| CN104611019A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Low energy consumption hydrocracking method for producing high-quality jet fuel |
| CN104611019B (en) * | 2013-11-05 | 2016-08-17 | 中国石油化工股份有限公司 | A kind of low energy consumption method for hydrogen cracking producing high-quality jet fuel |
| CN105087061A (en) * | 2014-05-05 | 2015-11-25 | 何巨堂 | Hydrocracking method in pre-upgrading region of high aromatic hydrocarbon hydrogenation refined heavy oil |
| CN104531212A (en) * | 2014-12-05 | 2015-04-22 | 何巨堂 | High aromatic hydrocarbon hydrogenation upgrading method by utilizing refined diesel component hydrogenation upgrading reaction process |
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