CN105838410A - Method for preparing aviation fuels by non-hydrogen conversion of high-water-content oils/greases - Google Patents
Method for preparing aviation fuels by non-hydrogen conversion of high-water-content oils/greases Download PDFInfo
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- CN105838410A CN105838410A CN201610396049.2A CN201610396049A CN105838410A CN 105838410 A CN105838410 A CN 105838410A CN 201610396049 A CN201610396049 A CN 201610396049A CN 105838410 A CN105838410 A CN 105838410A
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- hydrogen
- water
- hydrogen source
- fats
- oils
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
- C10G3/52—Hydrogen in a special composition or from a special source
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/47—Catalytic treatment characterised by the catalyst used containing platinum group metals or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
- C10G2300/1014—Biomass of vegetal origin
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
Abstract
The invention discloses a method for preparing aviation fuels by non-hydrogen conversion of high-water-content oils/greases, comprising: adding a biomass oil/grease and an in-situ hydrogen source into a high-pressure reactor, wherein mass/volume ratio of the biomass oil/grease to the in-situ hydrogen source is (4-5):100, adding a noble metal catalyst, and stirring and reacting at 250 DEG C for 12 hours; the in-situ hydrogen source comprises the following components: liquid hydrocarbons and water having a volume ratio of 1:0.1-9. The method needs no external hydrogen source, hydrogenation deoxygenation by in-situ hydrogen is typically high in reaction rate and may be carried out under low reaction temperature and pressure, and the requirement for high-pressure-resistant reaction equipment can be lowered. Therefore, this method is suitable for converting high-water-content oils/greases into hydrocarbon diesel efficiently with low energy consumption, reaction rate is high, and hydrocarbon diesel yield in products is up to 72%.
Description
Technical field
The invention belongs to biomass catalyzing convert and utilize field, be specifically related to a kind of hydrogen-free and convert high-moisture oils and fats system
The method of standby aviation fuel.
Background technology
Along with constantly reducing of fossil energy resource and going from bad to worse of ecological environment, the renewable energy that development and utilization is new
Source has become a urgent task.In numerous biomass resources, microalgae is due to its high cell fat content (up to 60
Wt.%) and short growth cycle it is considered to be one the most promising rechargeable energy source.At present, mainly with dry microalgae
Powder be raw material to prepare bio-fuel, but the energy needed for the dehydration of wet microalgae account for bio-fuel and produces required gross energy
90%.Although additionally, by ester exchange reaction oils and fats is converted into the technology of fatty acid alkyl esters (biodiesel) by
Industrial applications, but the biodiesel produced has the shortcoming such as poor chemical stability, low energy densities.Therefore, people will study
Turn to and utilize hydrogenation deoxidation (hydrodeoxygenation) technology that oils and fats is changed into hydro carbons diesel oil (aviation fuel), prepared
Hydro carbons diesel oil there is energy density more higher than biodiesel and non-oxidizability.
In hydrogenation deoxidation reacts, in order to obtain high oils and fats conversion ratio, it usually needs reaction is applied higher hydrogen
Pressure.Being accomplished by course of reaction using special high voltage bearing consersion unit, this will cause potential safety problem, limit
Its application in bio-fuel produces.Therefore, in course of reaction, how to reduce the dependence to hydrogen, or entirely without hydrogen
Under conditions of to realize the hydrogenation deoxidation of oils and fats be a problem the most challenging.Here, it is proposed that use and produce in situ
Hydrogen replace the molecular hydrogen in the external world, may be implemented in and under the reaction condition of gentleness, prepare the method for bio-fuel.Produce in situ
Hydrogen can be generated by two catalytic route: catalytic hydrogen transfer (CTH) and aqueous phase reforming (APR).Catalytic hydrogen transfer is by hydrogen donor
Hydrogen migration in molecule is to the method for receptor.Hydrogen donor molecule can include methanol, formic acid, ethanol, propanol etc..Aqueous phase reforming is one
Individual the liquid hydrocarbon (such as methanol, ethanol, glycerol etc.) containing hydrogen and water are reacted with produce hydrogen process.Due to former
The hydrogen that position produces can be immediately available in hydrogenation deoxidation reaction, while promoting to produce hydrogen reaction in situ, eliminates the diffusion of hydrogen
Impact on hydrogenation deoxidation reaction rate, accelerates hydrogenation deoxidation reaction.Therefore, the hydrogenation deoxidation producing hydrogen in situ is used to react
Typically there is higher reaction rate, can carry out under than relatively low reaction temperature and pressure condition.
The hydrogenation deoxidation reaction of oils and fats is general with nonpolar organic matters such as dodecanes as solvent, but for high-moisture
For wet microalgae, it is possible not only to avoid energy consumption produced by wet dewatering microalgae with water for solvent, it is also possible to reduce organic solvent
Use the impact on environment.Additionally, the existence of water can also promote the carrying out that aqueous phase reforming reacts.At the document published
In, only one report use Pd/C catalyst under the reaction condition of 250 DEG C, with water as solvent, catalysis oils and fats hydrogenation
Deoxygenation.But after reacting 20 hours, in product, the yield of hydro carbons diesel oil only has 13%, and the oils and fats of the overwhelming majority is through hydrolysis
Reaction converts for oleic acid or stearic acid.After extra interpolation methanol or glycerol, the yield of hydro carbons diesel oil just increases, but still
So there is substantial amounts of unreacted oleic acid or stearic acid.Two catalytic route of the present invention hydrogen by producing in situ are mutually whole
Close, it is achieved that with noble metal as catalyst, water is solvent, 250 DEG C, oils and fats/catalyst=4.25(weight ratio) reaction condition
Under, the conversion ratio obtaining 100% in 12 hours, the yield of hydro carbons diesel oil 72%.
Summary of the invention
The invention provides a kind of method that hydrogen-free converts high-moisture oil and fat preparation aviation fuel, the method is applied to height
Hydro carbons diesel oil is prepared in water content oil hydrogenation deoxidation, has high oils and fats conversion ratio, high hydro carbons diesel oil selectivity and yield.
A kind of hydrogen-free converts the method for high-moisture oil and fat preparation aviation fuel, it is characterised in that in autoclave
Adding biomass oils and fats and hydrogen source in situ, wherein the mass/volume ratio of biomass oils and fats and original position hydrogen source is (4 ~ 5)/100, adds
Enter noble metal catalyst, at 250 DEG C, stirring reaction 12 hours；Hydrogen source is made up of following component in situ:
Liquid hydrocarbon/water (volume ratio)=1:0.1 ~ 9.
As preferably, described original position hydrogen source, it is made up of the component of following percent by volume:
Liquid hydrocarbon/water (volume ratio)=1:0.4 ~ 1.
Described liquid hydrocarbon selected from methanol, formic acid, ethanol, acetic acid, propanol, isopropanol, propylene glycol, the third three
One or more in alcohol, toluene, dodecane, hexamethylene, naphthane, decahydronaphthalene.
The preferred Pd/C of described catalyst.
Described biomass oils and fats is algae extract.
Heretofore described mass/volume ratio, employing g/mL is measurement unit, when using other unit, all converts
For g/mL.
The present invention is with Pd/C as catalyst, and liquid hydrocarbon and water are original position hydrogen source, and the hydrogen produced in situ is directly joined
With in the reaction that oil hydrogenation deoxidation is hydro carbons diesel oil, thus, this reaction has higher reaction rate, the conversion ratio that oils and fats is high
The yield high with hydro carbons diesel oil.Hydrogeneous liquid hydrocarbon is not only involved in aqueous phase reforming reaction hydrogen manufacturing, but also as hydrogen
Donor molecule provides in-situ hydrogen, accelerates the hydrogenation deoxidation reaction of oils and fats, thus improves the activity and selectivity of catalyst.
Compared with the existing technology, beneficial effects of the present invention is embodied in:
(1) during said method has taken into full account oils and fats and the product dissolubility in reaction system, oils and fats conversion reaction
The reaction rate etc. of stepwise reaction (grease hydrolysis, glycerol aqueous phase reforming, aliphatic acid hydrogenation deoxidation) affect catalytic performance because of
Element, utilizes the original position hydrogen source of difference composition to reach to optimize reactivity and selective purpose.
(2) described method without extraneous hydrogen source, avoid the highly energy-consuming dehydration of oils and fats, reduce high pressure resistant reaction
The demand of equipment, it is adaptable to by the oils and fats of high-moisture directly efficiently, be converted into low energy consumption in the production process of hydro carbons diesel oil.
It is relatively mild that the method for the oil and fat preparation aviation fuel of the present invention has reaction condition, and reaction rate is fast, in product
Hydro carbons diesel yield reaches the feature of 72%.
Detailed description of the invention
Below in conjunction with specific embodiment, the present invention is further illustrated.
Embodiment 1
The hydrogenation deoxidation reaction of oils and fats is carried out on a set of pressure autoclave type reaction unit.This device is mainly by 250 mL's
Autoclave, magnetic stirring apparatus and electric heating temperature control and thermometric pressure tester are constituted.During test, by 4.25 g greases, 1.0
The Pd/C catalyst of g pre-reduction, the volume ratio of 100mL are that the dodecane/water mixed solution of 90:10 adds in reactor,
The air being passed through after sealing in nitrogen displacement still 3 times.Starting magnetic stirring, setting speed is that 700 rpm(trial tests show this turn
The lower external diffusion impact of speed can eliminate substantially), and it is heated to design temperature with the heating rate of 5 C/min.React complete, will
Reactor is placed in tap water and is quickly cooled to room temperature, and sample analysis.
Embodiment 2
The experimental implementation using liquid hydrocarbon to be the in situ oil hydrogenation deoxygenation of hydrogen source with embodiment 1, but 12
The volume ratio of alkane/water mixed solution is 70:30.
Embodiment 3
The experimental implementation using liquid hydrocarbon to be the in situ oil hydrogenation deoxygenation of hydrogen source with embodiment 1, but 12
The volume ratio of alkane/water mixed solution is 50:50.
Embodiment 4
The experimental implementation using liquid hydrocarbon to be the in situ oil hydrogenation deoxygenation of hydrogen source with embodiment 1, but 12
The volume ratio of alkane/water mixed solution is 10:90.
Embodiment 5
The experimental implementation using liquid hydrocarbon to be the in situ oil hydrogenation deoxygenation of hydrogen source with embodiment 1, but 12
The volume ratio of alkane/water mixed solution is 0:100.
Embodiment 6
The experimental implementation using liquid hydrocarbon to be the in situ oil hydrogenation deoxygenation of hydrogen source with embodiment 1, but 12
Alkane/water mixed solution replaces with toluene/water mixed solution.
Embodiment 7
The experimental implementation using liquid hydrocarbon to be the in situ oil hydrogenation deoxygenation of hydrogen source with embodiment 1, but 12
Alkane/water mixed solution replaces with decahydronaphthalene/water mixed solution.
Result with the difference oil hydrogenation deoxygenation of hydrogen source catalysis in situ is as shown in table 1.Along with dodecane/water volume
The minimizing of ratio, the selectivity of hydro carbons diesel oil is to decline, and intermediate product oleic acid and stearic acid amount are to increase, and this illustrates to increase
The carrying out of the concentration of liquid hydrocarbon beneficially hydrogenation deoxidation reaction.During with toluene for solvent, oleic acid content is more, explanation
The hydrogen amount produced in situ is little.And the most than toluene and dodecane of the in-situ hydrogen that decahydronaphthalene produces, therefore intermediate product oil
Sour and stearic amount is minimum, and the selectivity of hydro carbons diesel oil is the highest.
Claims (5)
1. the method that a hydrogen-free converts high-moisture oil and fat preparation aviation fuel, it is characterised in that add in autoclave
Entering biomass oils and fats and original position hydrogen source, wherein the mass/volume ratio of biomass oils and fats and original position hydrogen source is (4 ~ 5)/100, addition
Catalyst, at 250 DEG C, stirring reaction 12 hours；Hydrogen source is made up of following component in situ:
Liquid hydrocarbon/water (volume ratio)=1:0.1 ~ 9.
2. the method converting high-moisture oil and fat preparation aviation fuel according to a kind of hydrogen-free described in claim 1, its feature exists
In: described original position hydrogen source, it is made up of the component of following percent by volume:
Liquid hydrocarbon/water (volume ratio)=1:0.4 ~ 1.
3. the method converting high-moisture oil and fat preparation aviation fuel according to a kind of hydrogen-free described in claim 1 or 2, its feature
It is: described liquid hydrocarbon is selected from methanol, formic acid, ethanol, acetic acid, propanol, isopropanol, propylene glycol, glycerol, first
One or more in benzene, dodecane, hexamethylene, naphthane, decahydronaphthalene.
4. the method converting high-moisture oil and fat preparation aviation fuel according to a kind of hydrogen-free described in claim 1, its feature exists
In: the preferred Pd/C of described catalyst.
5. the method converting high-moisture oil and fat preparation aviation fuel according to a kind of hydrogen-free described in claim 1, its feature exists
In: described biomass oils and fats is algae extract.
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| CN201610396049.2A CN105838410B (en) | 2016-06-07 | 2016-06-07 | A kind of method of hydrogen-free conversion high-moisture oil and fat preparation aviation fuel |
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| CN201610396049.2A CN105838410B (en) | 2016-06-07 | 2016-06-07 | A kind of method of hydrogen-free conversion high-moisture oil and fat preparation aviation fuel |
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| CN105838410B CN105838410B (en) | 2017-11-17 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107814676A (en) * | 2016-09-14 | 2018-03-20 | 中国科学院大连化学物理研究所 | A kind of preparation method of decahydronaphthalene and naphthane |
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2016
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Patent Citations (3)
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| US20130310620A1 (en) * | 2012-05-18 | 2013-11-21 | Uop Llc | Integrated hydrolysis/hydroprocessing process for converting feedstocks containing renewable glycerides to paraffins |
| CN104371758A (en) * | 2014-10-29 | 2015-02-25 | 华东师范大学 | Method for preparing biological aviation kerosene by coactivating grease and hydrogen-donor solvent |
| CN105567283A (en) * | 2016-03-04 | 2016-05-11 | 浙江大学 | Method for preparing long-chain alkane through hydrolysis and in-situ hydrogenation and decarboxylation of micro-algal oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107814676A (en) * | 2016-09-14 | 2018-03-20 | 中国科学院大连化学物理研究所 | A kind of preparation method of decahydronaphthalene and naphthane |
| CN107814676B (en) * | 2016-09-14 | 2021-12-28 | 中国科学院大连化学物理研究所 | Preparation method of decahydronaphthalene and tetrahydronaphthalene |
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| CN105838410B (en) | 2017-11-17 |
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