CN103059930A - Preparation method of jet fuel - Google Patents
Preparation method of jet fuel Download PDFInfo
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- CN103059930A CN103059930A CN2011103194857A CN201110319485A CN103059930A CN 103059930 A CN103059930 A CN 103059930A CN 2011103194857 A CN2011103194857 A CN 2011103194857A CN 201110319485 A CN201110319485 A CN 201110319485A CN 103059930 A CN103059930 A CN 103059930A
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Abstract
The invention provides a preparation method of jet fuel. The method comprises the following steps: (1) mixing a heavy fraction with boiling point higher than 260 DEG C with C8-C24 n-alkanes to obtain a mixture; contacting the mixture and hydrogen with a hydrogenation isomerization catalyst under hydroisomerization conditions to obtain isomerization products; and (2) under conditions of hydrofining, contacting the isomerization products, hydrogen with a hydrofining catalyst, and fractioning to obtain jet fuel and the heavy fraction with boiling point higher than 260 DEG C. The method provided by the invention not only effectively improves the yield of jet fuel in the preparation process, but also effectively utilizes the heavy fraction obtained in a traditional preparation method of jet fuel. The jet fuel prepared by the method provided by the invention is almost entirely comprised of saturated alkanes, has stable quality, and can meet the requirements as a No. 3 jet fuel.
Description
Technical field
The present invention relates to a kind of method for preparing rocket engine fuel.
Background technology
Along with traditional fossil energy supply is becoming tight, the pressure of carbon dioxide discharge-reduction increases day by day, develops substitute energy renewable, cleaning and has become whole world common recognition.Because bioenergy has recyclability, green, come into one's own especially in recent years, be considered to solve one of the most desirable approach of global energy crisis.
Along with the demand of rocket engine fuel constantly increases, the technology for preparing rocket engine fuel from renewable raw materials more and more is subject to people's attention.These renewable raw materials comprise but do not limit to so, such as: vegetables oil (soybean oil, rapeseed oil, plam oil, jatropha curcas oil, Chinese vegetable tallow), animal tallow (lard, butter, fish oil), acidification oil, various lipid acid and acidifying wet goods.
At present, study more having, utilize vegetables oil and/or animal grease, prepare fatty acid methyl ester by transesterification reaction.Fatty acid methyl ester is a kind of renewable energy source of cleaning, is the substitute products of the petroleum diesel of high-quality, is to use at present maximum biofuel products.
Method by hydrotreatment is also arranged, vegetables oil and/or animal grease are prepared into the research of diesel component.Disclose the diesel component for preparing high hexadecane value with the method for hydrogenation such as US4992605A and US5705722A, but the diesel component of this method preparation is comprised of normal paraffin mainly, its cold filter clogging temperature is higher, has affected its scope of application.
CN101233212A discloses the method that a kind of two-step approach is produced diesel oil, and the first step generates normal paraffin by hydrogenation deoxidation, and second step reduces the cold filter clogging temperature of diesel oil by isomerization reaction.
In addition, US2009/0158637A1 discloses a kind of method that is prepared rocket engine fuel by renewable raw materials.The method obtains the normal paraffin that carbonatoms is 8-24 with vegetables oil and/or animal grease through hydrogenation deoxidation first, then passes through selective cracking and isomerization reaction, is met the rocket engine fuel of requirement through fractionation again.Yet the yield of rocket engine fuel is still lower in the method, and also there is generating portion alkene in cracking and isomerization process in the method, affects the problems such as color of rocket engine fuel.
Hydroisomerization process plays vital effect as the important step that adopts vegetables oil and/or animal grease to prepare rocket engine fuel to the process of whole preparation rocket engine fuel, it is determining character and the yield of the rocket engine fuel for preparing, therefore, how to improve hydroisomerisation catalysts and hydroisomerization process the preparation rocket engine fuel is had very important Research Significance.
Summary of the invention
The objective of the invention is on the basis of existing technology, provide a kind of jet fuel yield the higher method for preparing rocket engine fuel.
Although prior art is existing about prepare the multinomial research of rocket engine fuel with vegetables oil and/or animal grease, yet, the yield of rocket engine fuel still remains to be improved in existing every research, yet how further to improve the jet fuel yield of using vegetables oil and/or animal grease to prepare in the rocket engine fuel process and run into bottleneck, present most of investigator attempts by selecting more efficiently catalyzer (such as hydroisomerisation catalysts) to improve the yield of rocket engine fuel in this preparation process, and the present inventor is devoted to improve in the years of researches process always and uses vegetables oil and/or animal grease to prepare jet fuel yield in the rocket engine fuel process, finally finally find, even also can effectively not improve the yield of rocket engine fuel in the preparation process by improving catalyzer, the invention thinking that the present inventor proposes is: by the last running that fractionation in the preparation process is obtained turn back to carry out hydroisomerization in the hydroisomerization process can be so that the yield in the preparation process improves greatly.Further, CN1382526A discloses a kind of preparation method of catalyst for hydrogenation de-waxing, and point out that catalyzer that this preparation method prepares can be used for the Hydrodewaxing process of content of wax lubricating oil, content of wax rocket engine fuel, content of wax diesel oil, and the present inventor finds in research process, when processing the normal paraffin that obtains through hydrogenation deoxidation from animal-plant oil, this catalyzer has selective cracking and isomerized difunctional, so that it can be for the preparation of rocket engine fuel, and the rocket engine fuel for preparing can satisfy the service requirements of No. 3 rocket engine fuels.Based on aforementioned invention thinking and discovery, finished the present invention.
To achieve these goals, the invention provides a kind of method for preparing rocket engine fuel, the method comprises:
(1) with boiling point be more than 260 ℃ last running with obtain mixture after the normal paraffin of C8-C24 mixes; Under the hydroisomerization condition, described mixture, hydrogen are contacted the product that obtains behind the isomery with hydroisomerisation catalysts;
(2) under the hydrofining condition, the product behind the described isomery, hydrogen are contacted aftercut, and to obtain rocket engine fuel and described boiling point be last running more than 260 ℃ with Hydrobon catalyst.
Adopt method of the present invention not only to effectively raise the yield of rocket engine fuel in the preparation process, and, so that the last running that obtains in traditional preparation rocket engine fuel has obtained effective utilization.And the rocket engine fuel that adopts method of the present invention to prepare almost all is comprised of saturated alkane, and stable in properties is enough to satisfy the requirement as No. 3 rocket engine fuels.
Embodiment
The invention provides a kind of method for preparing rocket engine fuel, the method comprises:
(1) with boiling point be more than 260 ℃ last running with obtain mixture after the normal paraffin of C8-C24 mixes; Under the hydroisomerization condition, described mixture, hydrogen are contacted the product that obtains behind the isomery with hydroisomerisation catalysts;
(2) under the hydrofining condition, the product behind the described isomery, hydrogen are contacted aftercut, and to obtain rocket engine fuel and described boiling point be last running more than 260 ℃ with Hydrobon catalyst.
The method according to this invention, can realize preferably purpose of the present invention according to the aforementioned techniques scheme, under the preferable case, last running described in the step (1) accounts for the 10-100 % by weight of last running described in the step (2), and more preferably last running accounts for the 50-90 % by weight of last running described in the step (2) described in the step (1).
The method according to this invention, optional a wider range of the kind of described hydroisomerisation catalysts, the conventional hydroisomerisation catalysts of using all can realize purpose of the present invention, generally comprise carrier and metal active constituent, for the present invention, preferred described hydroisomerisation catalysts contains carrier and metal active constituent, and described carrier contains aluminium silicophosphate molecular sieve, and described metal active constituent contains one or more in the group VIII metallic element.
The method according to this invention, the hydroisomerisation catalysts that satisfies aforementioned requirement all can well realize goal of the invention of the present invention, under the preferable case, aluminium silicophosphate molecular sieve in the described hydroisomerisation catalysts is one or more in SAPO-11, SAPO-31, SAPO-41, ZSM-22, ZSM-23 and the ZSM-48 molecular sieve, and more preferably the degree of crystallinity of described aluminium silicophosphate molecular sieve is at least 70%.
The method according to this invention, optional a wider range of the kind of described metal active constituent, as long as it is in the group VIII metallic element one or more, under the preferable case, described metal active constituent is one or more among Fe, Co, Ni, Ru, Rh, Pb, Os, Ir, the Pt, more preferably Pt.That specifically uses in the embodiments of the invention is Pt.
The method according to this invention, optional a wider range of the content of various components in the described hydroisomerisation catalysts is under the preferable case, with total restatement of catalyzer, described metal active constituent is take the content of element as the 0.1-10 % by weight, and the content of described carrier is the 90-99.9 % by weight; Wherein, the content of aluminium silicophosphate molecular sieve is the 5-100 % by weight in the preferred vector.
In the aforementioned bearer of hydroisomerisation catalysts of the present invention except containing aluminium silicophosphate molecular sieve, various other that can also contain prior art can be used as the material that carrier uses, such as containing the heat-resistant inorganic oxides such as aluminum oxide, silicon oxide, those skilled in the art all can know this, not repeat them here.
The method according to this invention, the present invention to the preparation method of described hydroisomerisation catalysts without particular requirement, as long as satisfy the aforementioned requirement to catalyzer of the present invention, for example the preferred aforementioned hydroisomerisation catalysts of the present invention can according to disclosed preparation method's preparation among the CN1382526A, no longer be carried out emphasis at this and describe.
The method according to this invention, optional a wider range of described hydroisomerization condition, for the present invention, under the preferable case, described hydroisomerization condition comprises: temperature is 250-450 ℃, is preferably 300-350 ℃; Pressure is 1-7MPa, is preferably 3-6MPa; Volume space velocity is 0.1-5h
-1, be preferably 1-3h
-1Hydrogen to oil volume ratio is 100-800: 1 (Nm
3/ m
3), be preferably 400-600: 1 (Nm
3/ m
3).
The method according to this invention, optional a wider range of described hydrofining condition, under the preferable case, described hydrofining condition comprises: temperature is 100-250 ℃, and pressure is 1-7MPa, and volume space velocity is 0.5-5h
-1, hydrogen to oil volume ratio is 100-500: 1 (Nm
3/ m
3).
The method according to this invention, under the preferable case, described Hydrobon catalyst can adopt the conventional Hydrobon catalyst that uses in this area, preferred described Hydrobon catalyst contains heat-resistant inorganic oxide carrier and the hydrogenation component that loads on this carrier, and hydrogenation component is selected from one or more in the group VIII metallic element, and preferred described hydrogenation component is platinum and/or palladium, more preferably, take the gross weight of catalyzer as benchmark, in element, the content of platinum and/or palladium is the 0.1-5 % by weight.
The method according to this invention, described heat-resistant inorganic oxide carrier can be prior art various heat-resistant inorganic oxide carriers commonly used, for example can be for being obtained by one or more moulding in aluminum oxide, silicon oxide, titanium oxide, zirconium white and the molecular sieve, the present invention to this without particular requirement.
The method according to this invention is prepared rocket engine fuel in order effectively to utilize vegetables oil and/or animal grease, and is preferred, and described normal paraffin, is contacted with hydrogenation deoxidation catalyst and to obtain under the hydrogenation deoxidation condition by vegetables oil and/or animal grease and hydrogen.
The method according to this invention, optional a wider range of described hydrogenation deoxidation condition, for the present invention, under the preferable case, it is 200-400 ℃ that described hydrogenation deoxidation condition generally comprises temperature, and pressure is 1-7MPa, and volume space velocity is 0.5-5h
-1, hydrogen to oil volume ratio is 300-1500: 1 (Nm
3/ m
3).
The method according to this invention, described hydrogenation deoxidation catalyst can be prior art various hydrogenation deoxidation catalysts commonly used, generally speaking described hydrogenation deoxidation catalyst contains heat-resistant inorganic oxide carrier and the hydrogenation activity component that loads on this carrier, contain group vib metal and group VIII metal in the described hydrogenation activity component, further contain cobalt and/or nickel and molybdenum and/or tungsten in the preferred described hydrogenation activity composition; More preferably, take the weight of catalyzer as benchmark, in oxide compound, the content of molybdenum and/or tungsten is the 5-40 % by weight, and the total amount of cobalt and/or nickel is the 1-10 % by weight.
According to method provided by the invention, described hydrogenation deoxidation catalyst preferably uses as hydrogenation deoxidation catalyst behind over cure, under the preferable case, in order to keep the sulfuration form of hydrogenation deoxidation catalyst, sulphur can be in stock oil, replenished, also sulphur can be in recycle hydrogen, added.Therefore, for the present invention, contain vulcanizing agent in preferred described vegetables oil and/or the animal grease, the concentration of described vulcanizing agent is the 0.01-0.5 % by weight.Described vulcanizing agent can be the various S-contained substances that can gasify under the hydrogenation deoxidation condition and hydrogenation deoxidation catalyst is vulcanized, and under the preferable case, described vulcanizing agent is H
2S, CS
2, in dimethyl disulfide, Dimethyl sulfide, normal-butyl thioether and the thiophene one or more.Further, in order to reduce the water that generates in the hydrogenation deoxidation process to the impact of catalyzer and to reduce the temperature rise in the reactor in the preparation process, can be with the thinner of the product behind the hydrogenation deoxidation as charging (such as vegetables oil and/or animal grease), soon the product behind the hydrogenation deoxidation returns to enter in the reactor after charging mixes and contacts, for the present invention, the amount of returning of the product behind the preferred hydrogenation deoxidation is 2-10 with the volume ratio of charging (such as vegetables oil and/or animal grease): 1.Therefore, under the preferable case, vegetables oil and/or animal grease, hydrogen carry out with contacting in the presence of thinner of hydrogenation deoxidation catalyst in the step (1), and described thinner is the product (after dewatering or not dewatering) behind step (1) the gained hydrogenation deoxidation.Under aforementioned hydrogenation deoxidation condition of the present invention, may comprise olefins hydrogenation, hydrogenation deoxidation, hydrogenation decarbonylation base, hydrogenation decarboxylation and direct decarboxylation are in interior various reactions, the hydrogenation deoxidation reaction product that finally obtains is mainly the normal paraffin of C8-C24, water and on a small quantity other gaseous matter such as propane, carbon monoxide and carbonic acid gas etc., therefore all be normal paraffin (99-100 % by weight) substantially with the product behind the hydrogenation deoxidation through the product that dehydration obtains generally, can directly carry out without divided gas flow material (the general direct volatilization of gaseous matter) hydroisomerization of step (2).Those skilled in the art all can know this, in this no longer emphasis description.The hydrogenation deoxidation catalyst that uses in the specific embodiment of the present invention is the hydrogenation deoxidation catalyst behind over cure, and the method for sulfuration can be carried out with reference to prior art, no longer emphasis description among the present invention.
The method according to this invention, the kind of described heat-resistant inorganic oxide carrier is described aforementioned, does not repeat them here.
The method according to this invention, described vegetables oil can be various herbaceous plant oil and xylophyta oil or its mixture, for example, can be soybean oil, rapeseed oil, Oleum Gossypii semen, Semen Maydis oil, Rice pollard oil, sunflower oil, peanut oil, Viscotrol C, sesame oil, Fructus Zanthoxyli oil, tea oil, Oleum Cocois, sweet oil, coptis wood oil, plam oil, tung oil, one or more in rosin oil and the Chinese vegetable tallow.The preferred described vegetables oil of the present invention is one or more in soybean oil, rapeseed oil, Oleum Gossypii semen, Semen Maydis oil, Fructus Zanthoxyli oil, coptis wood oil and the plam oil.
The method according to this invention, described animal grease can be the greases of various animals, for example, can be one or more in lard, butter, sheep oil, the fish oil.
Vegetables oil described in the present invention and/or animal grease can be waste oil from restaurant.
The rocket engine fuel for preparing according to preceding method of the present invention all can satisfy the standard as No. 3 rocket engine fuels except density.And in concrete application process, in order to make rocket engine fuel density of the present invention also can satisfy the standard of existing No. 3 rocket engine fuels, the rocket engine fuel mixing use that rocket engine fuel of the present invention and existing employing refining of petroleum method can be obtained, mix in the use procedure, the weight concentration of rocket engine fuel of the present invention is the 10-70 % by weight, is preferably the 30-50 % by weight.
The method of fractionation is conventional fractionating method among the present invention, is generally fractionation by distillation.
Below will describe the present invention by embodiment.
Hydrogenation deoxidation catalyst adopts RN-10 catalyzer (catalyst Co. Chang Ling catalyzer branch office of China Petrochemical Industry, chief component is alumina catalyst support and metal active constituent nickel and tungsten, wherein nickel is take the content of oxide compound as 2.3 % by weight, and tungsten is take the content of oxide compound as 25.3 % by weight).Hydrobon catalyst employing RLF-10W catalyzer (catalyst Co. Chang Ling catalyzer branch office of China Petrochemical Industry, chief component is alumina catalyst support and metal active constituent platinum, wherein metal active constituent platinum is take the content of element as 0.5 % by weight).
In following examples, the color of rocket engine fuel, freezing point, flash-point are to record according to the method for GB/T3555, GB/T2430 and GB/T261 respectively, and olefin(e) centent, aromaticity content are that method according to GB/T11132 records in the rocket engine fuel.Mass yield refers to the mass percent of the stock oil of the quality of the rocket engine fuel for preparing and adding.
What describe among the embodiment is the preparation process after the steady running rather than the state when reacting initial, for example, when preparation process has just begun, it is the adding that does not have last running in the step (2), and under steady operational status, obtained last running owing to step (3), therefore, step (2) is carried out in the presence of last running under the steady operational status.Specifically described technical scheme is readily appreciated that this those skilled in the art according to the present invention.
Preparation Example 1
Method according to 6 Kaolinite Preparation of Catalysts of embodiment among the CN1382526A prepares hydroisomerisation catalysts: (alumina content is 60 % by weight to take by weighing the catalyzer C1 of 1 preparation of embodiment among the 40g CN1382526A and 22g solid oxide aluminium colloidal sol, Inst., of Alunite Comprehensive Utilization, Zhejiang Prov. produces) to mix, be extruded into circumscribed circle diameter be 1.8 millimeters trilobal bar, 120 ℃ of oven dry, then 550 ℃ of roastings 4 hours are the Pt (NH of 0.3 % by weight with the platinum constituent content
3)
4Cl
2H
2O aqueous solution 53.2g dipping, 120 ℃ of oven dry are the hydrogen reducing 4 hours of 800 ml/min at 450 ℃ with flow, obtain catalyst A and (contain degree of crystallinity among the A and be 77% SAPO-11 molecular sieve 75 % by weight, in element platinum content 0.3 % by weight, all the other are aluminum oxide).
Preparation Example 2
Method Kaolinite Preparation of Catalyst according to embodiment among the CN1382526A 6, just replace embodiment 1 prepares among the CN1382526A reference agent C1 to obtain catalyst B with the reference agent B1 of preparation in the CN1382526A Comparative Examples 1 and (contain degree of crystallinity among the B and be 67% SAPO-11 molecular sieve 75 % by weight, in element platinum content 0.3 % by weight, all the other are aluminum oxide).
Embodiment 1
(1) under the hydrogenation deoxidation condition, plam oil (vulcanizing agent Methyl disulfide ether content is 0.02 % by weight), hydrogen are contacted with hydrogenation deoxidation catalyst RN-10, and the hydrogenation deoxidation condition comprises: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 1.0h
-1, hydrogen to oil volume ratio is 1000: 1 (Nm
3/ m
3);
(2) under the hydroisomerization condition, with the normal paraffin of the C13-C20 that obtains behind the product dehydrate behind the aforementioned hydrogenation deoxidation and last running, the H of 90 % by weight that step (3) obtains
2A contacts with hydroisomerisation catalysts, wherein, comprises under the hydroisomerization condition: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3);
(3) under the hydrofining condition, with the product behind the aforementioned hydroisomerization, H
2RLF-10W contacts with Hydrobon catalyst, and the hydrofining condition comprises: temperature is 150 ℃, and pressure is 5.0MPa, and volume space velocity is 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3); Product fractionation after the hydrofining is obtained 150-260 ℃ rocket engine fuel cut and the last running more than 260 ℃, and wherein the character of gained rocket engine fuel is as shown in table 1.
Embodiment 2
(1) under the hydrogenation deoxidation condition, (wherein the weight ratio of plam oil and lard is 4: 1 with the mixture of plam oil and lard, vulcanizing agent Methyl disulfide ether content is 0.02 % by weight), hydrogen contacts with hydrogenation deoxidation catalyst RN-10, the hydrogenation deoxidation condition comprises: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 1.0h
-1, hydrogen to oil volume ratio is 1000: 1 (Nm
3/ m
3);
(2) under the hydroisomerization condition, with the normal paraffin of the C13-C20 that obtains behind the product dehydrate behind the aforementioned hydrogenation deoxidation and last running, the H of 75 % by weight that step (3) obtains
2A contacts with hydroisomerisation catalysts, wherein, comprises under the hydroisomerization condition: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3);
(3) under the hydrofining condition, with the product behind the aforementioned hydroisomerization, H
2RLF-10W contacts with Hydrobon catalyst, and the hydrofining condition comprises: temperature is 150 ℃, and pressure is 5.0MPa, and volume space velocity is 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3); Product fractionation after the hydrofining is obtained 150-260 ℃ rocket engine fuel cut and the last running more than 260 ℃, and wherein the character of gained rocket engine fuel is as shown in table 1.
Comparative Examples 1
(1) under the hydrogenation deoxidation condition, plam oil, hydrogen are contacted with hydrogenation deoxidation catalyst RN-10, the hydrogenation deoxidation condition comprises: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 1.0h
-1, hydrogen to oil volume ratio is 1000: 1 (Nm
3/ m
3);
(2) under the hydroisomerization condition, with normal paraffin, the H of the C13-C20 that obtains behind the product dehydrate behind the aforementioned hydrogenation deoxidation
2A contacts with hydroisomerisation catalysts, wherein, comprises under the hydroisomerization condition: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3);
(3) under the hydrofining condition, with the product behind the aforementioned hydroisomerization, H
2RLF-10W contacts with Hydrobon catalyst, and the hydrofining condition comprises: temperature is 150 ℃, and pressure is 5.0MPa, and volume space velocity is 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3); Product fractionation after the hydrofining is obtained rocket engine fuel cut and the last running more than 260 ℃ of lighting end, 150-260 ℃ less than 150 ℃, and wherein the character of gained rocket engine fuel is as shown in table 1.
Comparative Examples 2
Method according to Comparative Examples 1 prepares rocket engine fuel, and different is, reaction raw materials is the mixture of plam oil and lard, and wherein the weight ratio of plam oil and lard is 4: 1, and the character of gained rocket engine fuel is as shown in table 1.
Embodiment 3
(1) under the hydrogenation deoxidation condition, plam oil (vulcanizing agent Methyl disulfide ether content is 0.02 % by weight), hydrogen are contacted with hydrogenation deoxidation catalyst RN-10, and the hydrogenation deoxidation condition comprises: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 1.0h
-1, hydrogen to oil volume ratio is 1000: 1 (Nm
3/ m
3);
(2) under the hydroisomerization condition, with the normal paraffin of the C13-C20 that obtains behind the product dehydrate behind the aforementioned hydrogenation deoxidation and last running, the H of 30 % by weight that step (3) obtains
2B contacts with hydroisomerisation catalysts, wherein, comprises under the hydroisomerization condition: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3);
(3) under the hydrofining condition, with the product behind the aforementioned hydroisomerization, H
2RLF-10W contacts with Hydrobon catalyst, and the hydrofining condition comprises: temperature is 150 ℃, and pressure is 5.0MPa, and volume space velocity is 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3); Product fractionation after the hydrofining is obtained 150-260 ℃ rocket engine fuel cut and the last running more than 260 ℃, and the character of gained rocket engine fuel is as shown in table 1.
Comparative Examples 3
(1) under the hydrogenation deoxidation condition, plam oil, hydrogen are contacted with hydrogenation deoxidation catalyst RN-10, the hydrogenation deoxidation condition comprises: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 1.0h
-1, hydrogen to oil volume ratio is 1000: 1 (Nm
3/ m
3);
(2) under the hydroisomerization condition, with normal paraffin, the H of the C13-C20 that obtains behind the product dehydrate behind the aforementioned hydrogenation deoxidation
2B contacts with hydroisomerisation catalysts, wherein, comprises under the hydroisomerization condition: pressure is that 5.0MPa, temperature are that 320 ℃, volume space velocity are 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3);
(3) under the hydrofining condition, with the product behind the aforementioned hydroisomerization, H
2RLF-10W contacts with Hydrobon catalyst, and the hydrofining condition comprises: temperature is 150 ℃, and pressure is 5.0MPa, and volume space velocity is 2.0h
-1, hydrogen to oil volume ratio is 500: 1 (Nm
3/ m
3); Product fractionation after the hydrofining is obtained rocket engine fuel cut and the last running more than 260 ℃ of lighting end, 150-260 ℃ less than 150 ℃, and the character of gained rocket engine fuel is as shown in table 1.
Table 1
Result by table 1 can find out that the rocket engine fuel that adopts method of the present invention to prepare can satisfy the requirement of No. 3 rocket engine fuels except density, can be used as No. 3 rocket engine fuels.
Claims (14)
1. method for preparing rocket engine fuel, the method comprises:
(1) with boiling point be more than 260 ℃ last running with obtain mixture after the normal paraffin of C8-C24 mixes; Under the hydroisomerization condition, described mixture, hydrogen are contacted the product that obtains behind the isomery with hydroisomerisation catalysts;
(2) under the hydrofining condition, the product behind the described isomery, hydrogen are contacted aftercut, and to obtain rocket engine fuel and described boiling point be last running more than 260 ℃ with Hydrobon catalyst.
2. method according to claim 1, wherein, last running described in the step (1) accounts for the 10-100 % by weight of last running described in the step (2).
3. method according to claim 2, wherein, last running described in the step (1) accounts for the 50-90 % by weight of last running described in the step (2).
4. the described method of any one according to claim 1-3, wherein, described hydroisomerisation catalysts contains carrier and metal active constituent, and described carrier contains aluminium silicophosphate molecular sieve, and described metal active constituent contains one or more in the group VIII metallic element.
5. method according to claim 4, wherein, described aluminium silicophosphate molecular sieve is one or more in SAPO-11, SAPO-31, SAPO-41, ZSM-22, ZSM-23 and the ZSM-48 molecular sieve, and the degree of crystallinity of described aluminium silicophosphate molecular sieve is at least 70%.
6. method according to claim 4, wherein, described metal active constituent is one or more among Fe, Co, Ni, Ru, Rh, Pb, Os, Ir, the Pt.
7. method according to claim 6, wherein, described metal active constituent is Pt.
8. method according to claim 4, wherein, with total restatement of hydroisomerisation catalysts, described metal active constituent is take the content of element as the 0.1-10 % by weight, and the content of described carrier is the 90-99.9 % by weight; Wherein, the content of aluminium silicophosphate molecular sieve is the 5-100 % by weight in the carrier.
9. the described method of any one according to claim 1-3, wherein, described hydroisomerization condition comprises: temperature is 250-450 ℃, and pressure is 1-7MPa, and volume space velocity is 0.1-5h
-1, hydrogen to oil volume ratio is 100-800: 1Nm
3/ m
3
10. the described method of any one according to claim 1-3, wherein, described hydrofining condition comprises: temperature is 100-250 ℃, and pressure is 1-7MPa, and volume space velocity is 0.5-5h
-1, hydrogen to oil volume ratio is 100-500: 1Nm
3/ m
3
11. the described method of any one according to claim 1-3, wherein, described normal paraffin, is contacted with hydrogenation deoxidation catalyst and to obtain under the hydrogenation deoxidation condition by vegetables oil and/or animal grease and hydrogen.
12. method according to claim 11, wherein, described hydrogenation deoxidation condition comprises: temperature is 200-400 ℃, and pressure is 1.0-7.0MPa, and volume space velocity is 0.5-5.0h
-1, hydrogen to oil volume ratio is 300-1500: 1Nm
3/ m
3
13. method according to claim 11, wherein, described vegetables oil is one or more in soybean oil, rapeseed oil, Oleum Gossypii semen, Semen Maydis oil, Rice pollard oil, sunflower oil, peanut oil, Viscotrol C, sesame oil, Fructus Zanthoxyli oil, tea oil, Oleum Cocois, sweet oil, coptis wood oil, plam oil, tung oil, rosin oil and the Chinese vegetable tallow, and described animal grease is one or more in lard, butter, sheep oil and the fish oil.
14. method according to claim 11, wherein, described vegetables oil and/or animal grease are waste oil from restaurant.
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| CN201110319485.7A CN103059930B (en) | 2011-10-19 | 2011-10-19 | A kind of method preparing rocket engine fuel |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103801295A (en) * | 2014-03-07 | 2014-05-21 | 南开大学 | Catalyst for reaction of preparing aviation kerosene by castor oil and a preparation method of catalyst |
| CN106256880A (en) * | 2015-06-18 | 2016-12-28 | 中国石油化工股份有限公司 | A kind of method being prepared jet fuel by animal and plant fat |
| CN106281402A (en) * | 2015-06-23 | 2017-01-04 | 中国石油化工股份有限公司 | A kind of method being prepared jet fuel by renewable raw materials |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101952392A (en) * | 2007-12-21 | 2011-01-19 | 环球油品公司 | Prepare aviation fuel from biological renewable raw materials |
| CN102124080A (en) * | 2008-07-01 | 2011-07-13 | 耐思特石油公司 | Process for the manufacture of hydrocarbons of biological origin |
| US20110219676A1 (en) * | 2008-11-20 | 2011-09-15 | Jx Nippon Oil & Energy Corporation | Aviation fuel base oil and aviation fuel composition |
-
2011
- 2011-10-19 CN CN201110319485.7A patent/CN103059930B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101952392A (en) * | 2007-12-21 | 2011-01-19 | 环球油品公司 | Prepare aviation fuel from biological renewable raw materials |
| CN102124080A (en) * | 2008-07-01 | 2011-07-13 | 耐思特石油公司 | Process for the manufacture of hydrocarbons of biological origin |
| US20110219676A1 (en) * | 2008-11-20 | 2011-09-15 | Jx Nippon Oil & Energy Corporation | Aviation fuel base oil and aviation fuel composition |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103801295A (en) * | 2014-03-07 | 2014-05-21 | 南开大学 | Catalyst for reaction of preparing aviation kerosene by castor oil and a preparation method of catalyst |
| CN106256880A (en) * | 2015-06-18 | 2016-12-28 | 中国石油化工股份有限公司 | A kind of method being prepared jet fuel by animal and plant fat |
| CN106256880B (en) * | 2015-06-18 | 2018-04-13 | 中国石油化工股份有限公司 | A kind of method that jet fuel is prepared by animal and plant fat |
| CN106281402A (en) * | 2015-06-23 | 2017-01-04 | 中国石油化工股份有限公司 | A kind of method being prepared jet fuel by renewable raw materials |
| CN106281402B (en) * | 2015-06-23 | 2018-04-13 | 中国石油化工股份有限公司 | A kind of method that jet fuel is prepared by renewable raw materials |
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