CN101305080A - Process to blend a mineral derived hydrocarbon product and a Fisher-Tropsch derived hydrocarbon product - Google Patents
Process to blend a mineral derived hydrocarbon product and a Fisher-Tropsch derived hydrocarbon product Download PDFInfo
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- CN101305080A CN101305080A CNA2006800421108A CN200680042110A CN101305080A CN 101305080 A CN101305080 A CN 101305080A CN A2006800421108 A CNA2006800421108 A CN A2006800421108A CN 200680042110 A CN200680042110 A CN 200680042110A CN 101305080 A CN101305080 A CN 101305080A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
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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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Liquid Carbonaceous Fuels (AREA)
- Lubricants (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Process to blend a mineral derived hydrocarbon product and a Fischer-Tropsch derived hydrocarbon product by providing in an Above Ground Storage Tank a quantity of mineral derived hydrocarbon product and Fischer-Tropsch derived hydrocarbon product such that initially the mineral derived hydrocarbon product is located substantially above the Fischer-Tropsch derived hydrocarbon product; a blended product produced by the process; and a use of the blended product.
Description
Technical field
The present invention relates to the method for mineral derived hydrocarbon product of blend and Fisher-Tropsch derived hydrocarbon product.
Background technology
The method of mineral derived gas oil of blend and Fisher-Tropsch derived gas oil is disclosed in WO-A-03/087273.This publication described can be in refinery environment the gas oil of blend mineral derived thing, to obtain to have the blend product of certain cetane value.
Although WO-A-03/087273 provides the method for the blend that obtains to have the certain mass performance, it still need improve aspect own in the blend operation.Method of the present invention provides this solution.
The applicant finds, can obtain the product of abundant blend by method of the present invention.Following method makes and can obtain to be suitable for directly the blend product used under refinery environment for example.
Summary of the invention
Therefore, according to the present invention, by providing a certain amount of mineral derived hydrocarbon product and Fisher-Tropsch derived hydrocarbon product in the storage tank on the ground, so that initial mineral derived hydrocarbon product is located substantially on Fisher-Tropsch derived hydrocarbon product top, thereby provide the method for mineral derived hydrocarbon product of blend and Fisher-Tropsch derived hydrocarbon product.
By in the presence of suitable Fischer-Tropsch catalyst, under the fischer-tropsch operational condition, transform the mixture of carbon monoxide and hydrogen, to obtain Fisher-Tropsch derived hydrocarbon product suitably.It is known in the art that the mixture of catalyzed conversion hydrogen and carbon monoxide becomes the employed catalyzer of Fisher-Tropsch derived paraffin products.The employed catalyzer of this method usually in the containing element periodictable metal of group VIII as catalytic active component.Specific catalytically-active metals comprises ruthenium, iron, cobalt and nickel.Cobalt is preferred catalytically-active metals.
The example of suitable fischer-tropsch synthetic method is so-called commercial Sasol method, Shell middle runnings synthesis method and AGC-21 ExxonMobil method.These and other method is for example disclosed in EP-A-0776959, EP-A-0668342, US-A-4943672, US-A-5059299, WO-A-99/34917 and WO-A-99/20720 in more detail.Can or in three-phase fluid bed reactor, carry out Fischer-Tropsch process in slurry-phase reactor, fixed-bed reactor (the particularly fixed-bed reactor of multitube).
Can be by various hydrocarbon source, biological example material, coal, mineral crude oil fractions be for example Sweet natural gas or coalbed methane gas of residue oil fraction and the gas that contains methane for example, preparation employed synthetic gas, i.e. mixture of carbon monoxide and hydrogen in Fischer-Tropsch process.
Fisher-Tropsch derived hydrocarbon product is liquid suitably under 0 ℃.If this product be liquid, then preferably under product is the condition of liquid, it is kept in the land storage tank.Fisher-Tropsch derived product can be the wax that directly prepares in the fischer-tropsch synthesis step.In the methods of the invention, suitably this fischer-tropsch synthesis product is at first carried out gentle hydrogenation isomerization, but with the congelation point that reduces this product and to improve its pumping and be more prone to make product be liquid state.This product is also referred to as synthetic crude (Syncrude).
Fisher-Tropsch derived hydrocarbon product also can be from isolating more lower boiling liquid distillate 35-300 ℃ of following ebullient wax fischer-tropsch products.Contain a large amount of promptly greater than these products of 80wt% n-paraffin can be used as hydrocarbon solvent, as steam cracker feed stock or as the raw material of preparation purification agent through ship.
Alternatively, this wax product is carried out hydrocracking/hydroisomerisation process, wherein obtain more lower boiling cut, for example ebullient paraffin products in petroleum naphtha, kerosene and gas oil boiling range.So the isomerized liquid product of part that obtains can be shipped to end user location as aviation fuel, diesel oil, industrial gas oil, drilling fluid, steam cracker feed stock or solvent.The isomerized wax of the part that obtains in these processing steps (being also referred to as waxy raffinate (raffinate)) can advantageously further be processed by solvent or catalytic dewaxing, but is shipped near the terminal user base oil manufacturing site location as intermediate product to obtain lubricating base oil or former state.Waxy raffinate is a distillation fraction.Also can use ebullient residue oil fraction in the base oil scope.Yet in the blend process, these products that may more be hard to keep are for liquid.The example of these methods has been described in US-A-6309432, US-A-6296757, US-A-5689031, EP-A-0668342, EP-A-0583836, US-A-6420618, WO-A-02/070631, WO-A-02/070629, WO-A-02/070627, WO-A-02/064710 and WO-A-02/070630 in more detail.Therefore making the place at fischer-tropsch carries out related hydrocracking/hydroisomerization and best dewaxing step and the above-described liquid product of gained and is suitable as the fischer-tropsch hydrocarbon product for the treatment of through ship.
The volume ratio scope of mineral derived hydrocarbon product and Fisher-Tropsch derived product can be for example 1: 99 to 99: 1 and more preferably 10: 90 to 90: 10.The T90vol% boiling point (this measures by ASTM D86) of preferred mineral derived hydrocarbon product is greater than the T50vol% boiling point of Fisher-Tropsch derived hydrocarbon product.More preferably, mineral and Fisher-Tropsch derived product greater than 50vol% and even overlapping more preferably greater than the boiling range of 80vol%.
Mineral hydrocarbon product can be extract from underground environment or derived from wherein any product.The example of this product is the residue oil fraction of crude mineral oil, gas field condensation product, factory's condensation product, petroleum naphtha, kerosene, gas oil, vacuum overhead product, deasphalting oil and crude oil.
The example that can utilize the combination of the inventive method is Fisher-Tropsch derived gas oil of the Fisher-Tropsch derived petroleum naphtha of blend mineral crude oil and synthetic crude, blend and gas field condensation product, blend and mineral derived gas oil and Fisher-Tropsch derived waxy raffinate and the vacuum overhead product of mineral oil derived and/or the deasphalted oil of mineral oil derived of blend.
Preferably, Fisher-Tropsch derived hydrocarbon product is a gas oil fraction, preferably the gas oil fraction that obtains after hydroisomerization.Therefore can obtain gas oil product by this fischer-tropsch synthesis product of rectifying, perhaps obtain by hydrocracking (hydrocracking/hydroisomerization) fischer-tropsch synthesis product.Randomly, can carry out catalytic dewaxing to gas oil handles.The mixture of above-mentioned gas oil fraction also can be used as Fisher-Tropsch derived hydrocarbon product.The example of Fisher-Tropsch derived gas oil is disclosed in middle EP-A-0583836, WO-A-97/14768, WO-A-97/14769, WO-A-00/11116, WO-A-00/11117, WO-A-01/83406, WO-A-01/83648, WO-A-01/83647, WO-A-01/83641, WO-A-00/20535, WO-A-00/20534, EP-A-1101813, WO-A-03/070857 and US-A-6204426.
Suitably, Fisher-Tropsch derived gas oil is by 90wt% at least, more preferably the isoparaffin of 95wt% and linear paraffins are formed at least.The weight ratio of isoparaffin and n-paraffin is suitably greater than 0.3.This ratio can maximum 12.This ratio is 2-6 suitably.Part is by being used for being measured by the hydroconversion process that fischer-tropsch synthesis product prepares Fisher-Tropsch derived gas oil the actual value of this ratio.Can there be some cyclic-paraffins.By fischer-tropsch process, Fisher-Tropsch derived gas oil has the sulphur and the nitrogen (perhaps undetectable content) of zero content basically.These heteroatomic compounds are poisonous substances of Fischer-Tropsch catalyst, be from removing as the synthetic gas of fischer-tropsch process raw material.In addition, this method does not produce aromatic hydrocarbons, does not produce aromatic hydrocarbons when perhaps as usually operating basically.The content of the aromatic hydrocarbons of measuring by ASTM D 4629 typically is lower than 1wt%, preferably is lower than 0.5wt% and most preferably is lower than 0.1wt%.
Fisher-Tropsch derived gas oil has distillation curve suitably, and is wherein most of in 150-400 ℃ typical gas oil range.The T90wt% of fischer-tropsch gas oil is 320-400 ℃ suitably, and the density under 15 ℃ is 0.76-0.79g/cm
3, cetane value is that 74-82 and the viscosity under 40 ℃ are the 1.9-4.5 centistoke greater than 70 suitably.
Above-mentioned Fisher-Tropsch derived gas oil preferably with the mixture blend of mineral derived kerosene or gas oil or described kerosene and gas oil.Preferred mineral derived gas oil or kerosene are by refining and randomly (hydrogenation) processing crude mineral raw material and the gas oil or kerosene or isolating gas oil or the kerosene(oil)fraction from the condensation product of gas field that obtain.Mineral derived gas oil can be the single gas oil stream that obtains in this refinery practice, or the blend of several gas oil fraction that obtain in refinery practice by different processing routes.The example of the gas oil fraction that these that produce in refinery are different is straight run gas oil, vacuum gas oil, the gas oil that obtains in thermocracking process and the lightweight that obtains in fluid catalytic cracking unit and heavy recycle stock and gas oil that obtains from the hydrocracker unit or kerosene(oil)fraction of equal value.
Straight run gas oil or kerosene(oil)fraction are the cuts that obtains in air distillation crude mineral refinery stock.Above-mentioned cut rise an initial boiling point (IBP) be suitably 150-280 ℃ and finally boiling point (FBP) be 290-380 ℃.Vacuum gas oil is the gas oil fraction that obtains in vacuum distilling residual oil, and described residual oil is to obtain in the thick mineral refinery stock of above-mentioned air distillation.It is 340-380 ℃ with FBP that the IBP of vacuum gas oil is 240-300 ℃.Thermocracking process also produces the gas oil fraction that can use in step (a).It is 320-380 ℃ with FBP that the IBP of this gas oil fraction is 180-280 ℃.It is 320-380 ℃ with FBP that the IBP of the light cycle oil fraction that obtains in fluid catalytic cracking process is 180-260 ℃.It is 340-380 ℃ with FBP that the IBP of the heavy recycle stock cut that obtains in fluid catalytic cracking process is 240-280 ℃.These raw materials can have the above sulphur content of 0.05wt%.Maximum sulfur is about 2wt%.Although Fisher-Tropsch derived gas oil comprises sulphur hardly, may still need to reduce the sulphur content of mineral derived gas oil, so that satisfy harsh at present low-sulfur technical specification.Typically, by these gas oil fraction of processing in hydrogenating desulfurization (HDS) unit, thus the reduction of realization sulphur.
It is 320-380 ℃ with FBP that the IBP of the gas oil that obtains in fuels hydrocracker suitably, is 150-280 ℃.
The cetane value of the blend of above-described mineral derived gas oil is preferably greater than 40 and less than 70.If also have other performance for example cloud point, CFPP (cold filter clogging temperature), flash-point, density, two+-distillation temperature of aromaticity content, polyaromatic and/or 95% rate of recovery is also consistent with local regulation, then this blend can be advantageously used for diesel component.
Preferably, the sulphur content of gas oil product that contains the final blend of fischer-tropsch and mineral derived gas oil is the sulphur of maximum 2000ppmw (parts by weight of per 1,000,000 weight parts), preferably is not more than 500ppmw, most preferably is not more than 50ppmw or even 10ppmw.The density of this blend under 15 ℃ is typically less than 0.86g/cm
3And preferably under 15 ℃ less than 0.845g/cm
3Compare with the gas oil blend of routine, the lower density source of this blend is from low-density relatively Fisher-Tropsch derived gas oil.For example act as a fuel in rotor pump, in-line pump, modular pump, electronic unit injector or the common rail type in the diesel engine that above-mentioned fuel composition is adapted at injecting indirectly or at the diesel engine that directly injects.
Final gas oil blend can be doped oil or doped oil not.If oil fuel is doped oil, then it will contain a spot of one or more additives.
The fuel dope that contains purification agent is known and commercially available.This additive can be joined in the fuel, its content is used to reduce, remove or the accumulation of the engine deposits that slow down.The example that is suitable for the purification agent that uses at the fuel dope that is used for the object of the invention comprises the succinimide or the succinic diamide of the polyamines that polyolefine replaces, for example polyisobutenyl succinimide or polyisobutylene amine succinamides, aliphatic amine, Mannich base or amine and polyolefine (for example polyisobutene) maleic anhydride.Among GB-A-960493, EP-A-0147240, EP-A-0482253, EP-A-0613938, EP-A-0557516 and the WO-A-98/42808 succinimide dispersant additives is being disclosed for example.The succinimide that special preferred polyolefm replaces, for example polyisobutenyl succinimide.
Other binder component comprises: lubricity additive, comprising ester group and acidic group additive; Demisting agent, for example alkoxide novolac polymer; Defoamer (for example polyether-modified polysiloxane); Ignition improver (cetane number improver) (for example nitric acid 2-ethylhexyl (EHN), cyclohexyl nitrate, ditertiary butyl peroxide and those disclosed in the 27th row-Di 3 hurdles, the 2nd hurdle of US-A-4208190 the 21st row); Rust-preventive agent (the propane of tetrapropylene base succsinic acid-1 for example, 2-glycol half ester, or the polyol ester of succinic acid derivative, on at least one alpha-carbon atom of succinic acid derivative, has the aliphatic hydrocarbyl that does not replace or replace that contains 20-500 carbon atom, for example the pentaerythritol diester of the succsinic acid of polyisobutene-replacement); Corrosion inhibitor; Deodovization agent; Anti-wear additive; Antioxidant (phenols for example, for example 2,6 di t butyl phenol, or phenylenediamine, N for example, N '-two sec-butyls-Ursol D); Metal inactivator; And combustion improving agent.
The preferred 1%w/w at most of the concentration of the additive of each this additional component in containing the fuel composition of additive, more preferably scope is 5-1000ppmw, advantageously is 75-300ppmw, for example 95-150ppmw.
Except above-mentioned gas oil component, the fuel element of oxygenatedchemicals type that also can have relative small portion in final blend to be obtaining diesel oil, as described in the WO-A-2004/035713.Can have content is 2-20wt%, the more preferably oxygenatedchemicals fuel of 2-10wt%, and this measures in the final fuel composition.Oxygenatedchemicals is the compound that contains aerobic, preferably only contains the compound of carbon, hydrogen and oxygen.It may suitably be the compound that contains one or more hydroxyl-OH and/or one or more carbonyl C=O and/or one or more ether-O-and/or one or more ester group-C (O) O-.It preferably contains 1-18 carbon atom and is 1-10 carbon atom in some cases.It is biodegradable ideally.It is derived from organic substance suitably, as obtainable " biofuel " at present for example the situation of vegetables oil and derivative thereof.
The preferred oxygenatedchemicals that uses is an ester, for example the alkyl carboxylates of vegetables oil, preferably C1-C8 or C1-C5 alkyl ester, for example methyl esters or ethyl ester.Carboxylic acid in this case can be the optional straight or branched that replaces list-, two-or polyfunctional C1-C6 carboxylic acid, typical substituting group comprises hydroxyl, carbonyl, ether and ester group.Oxygenatedchemicals suitable example (iii) comprises succinate and levulinate.
Ether also can be used as oxygenatedchemicals (iii), for example dialkyl group (typically C1-C6) ether, for example dibutyl ether and dimethyl ether.
Alternatively, oxygenatedchemicals can be an alcohol, and described alcohol can be primary, the second month in a season or the tertiary alcohol.It can be the C1-C6 alcohol that replaces the straight or branched of (but preferably not replacing) especially, and suitable example is methyl alcohol, ethanol, n-propyl alcohol and Virahol.Typical case's substituting group comprises carbonyl, ether and ester group.For example can use methyl alcohol and particularly ethanol.
Oxygenatedchemicals (iii) typically is liquid at ambient temperature, and its boiling point is preferably 100-360 ℃, more preferably 250-290 ℃.Its density is 0.75-1.2g/cm suitably under 15 ℃
3, more preferably 0.75-0.9g/cm
3(ASTM D4502/IP 365), and its flash-point is greater than 55 ℃.
Can in procedure of the present invention, carry out the interpolation of additive and/or oxygenatedchemicals.Even, add at least a portion additive and/or oxygenatedchemicals more preferably when discharging from storage vessel during blend product.Preferably add by blend in the so-called pipeline.This is favourable because so the blend that obtains can be directly as finished product fuel with for use as motor vehicle gas oil (AGO) or industrial gas oil (IGO).
" being located substantially on ... the top " on the inventive method meaning be meant at least 50, preferred at least 70 and even more preferably at least the Fisher-Tropsch derived product of 90vol% be present in lower part of land storage tank.When using bottom pad device load land storage tank, preferably at first supply mineral hydrocarbon product, next supplies Fisher-Tropsch derived product.
" blend product " be meant wherein the sample (being called d10) that obtains at 10% liquid height place below the liquid level and the density of the sample (being called d90) that obtains at 90% liquid height place below the liquid level between density difference little, the ratio of preferred feasible (d10-d90)/d10 is more preferably less than 0.001 mixture less than 0.01.
On meaning of the present invention, " land storage tank " (being also referred to as AST) is the storage facility that is fixed on the ground surface.Preferably, land storage tank is the part of so-called blend facility or tank farm.The reservoir volume of land storage tank is suitably greater than 3000m
3, more preferably greater than 10000m
3The upper limit of storage facility is 100000m suitably in the single land storage tank
3Land storage tank can be furnished with the interior extra hybrid device that exists of storage tank on the ground.The advantage of the inventive method is that this device can save or uses under lower speed.
The invention still further relates to the blend product of producing by blend method according to the present invention.
The invention further relates to the direct application that the blend product that obtains by method of the present invention acts as a fuel, more preferably use as motor vehicle gas oil or as industrial gas oil.
Embodiment
Set forth the present invention by following indefiniteness embodiment.
Embodiment
In following experiment, use typical mineral deutero-gas oil (further being called AGO) and typical fischer-tropsch gas oil (further being called GTL) with the listed performance of table 1.
Table 1
| The fuel mark | Unit | AGO | GTL |
| Cetane index (ASTM D613) | 51.5 | ＞74.8 | |
| Sulphur | mg/kg | 7 | ＜5 |
| VK under 40 ℃ | cSt | 2.559 | 3.606 |
| Distillation curve | |||
| IBP | ℃ | 167.8 | 211 |
| 50％ | ℃ | 263.5 | 298 |
| 90％ | ℃ | 325.3 | 339 |
| 95％ | ℃ | 341.6 | 349 |
| FBP | ℃ | 351.2 | 354 |
| HPLC aromatic hydrocarbons | |||
| Amount to | wt％ | 26.9 | 0 |
In order to carry out this assessment, adopt two kinds of methods to add fuel, but the maintenance of the essence of these two experiments is identical.These methods are funnel technique and beaker technology.
The purpose of each technology is to minimize turbulent flow (with the mixing that therefore causes) in adding the process of second kind of fuel, is that the length of duration of contact causes so that the major part of these two kinds of fuel is mixed.These two technology all relate to 2 * 2 liters of glass beakers of preparation, and one of them contains 800mlAGO, and another contains 800ml GTL.Use 1 liter of glass cylinder, spend about 2 minutes and add 800ml GTL (blend A) among the clockwise AGO lentamente.Repeat this technology and add AGO (800ml) to GTL (blend B).In order to estimate the uniformity coefficient of blend, after for some time section, at 400ml and 1200ml, measure the density of fuel blends, with the bottom of assessing each blend and the density at top from beaker bottom.The funnel technique of adding fuel relates on the outside surface of the glass funnel of putting upside down topples over the fuel that is added, and the described glass funnel of putting upside down makes its base (spout of funnel) contact with the inwall of glass beaker.It is designed on big surface-area to produce fuel adds minimizing turbulent flow, and therefore is minimized in the mixing of two-layer fuel bed in the process of adding second kind of fuel.
The beaker technology that fuel adds relates at the beaker inwall directly topples over the fuel that is added downwards.Compare with funnel technique, this produces the interpolation of fuel on less surface-area, thus in adding the process of second kind of fuel more turbulent flow and therefore two-layer fuel bed more mix.
The theoretical density that density is observed uniform 50: 50 blends of volume/volume, linear blend rule and AGO that is studied and GTL sample is 813.3kg/m
3Therefore, can use the density measurement of this blend to calculate existing each components contents.
Table 2 has been described at the density result of each component of taking a sample with the degree of depth place of graduated beaker upper volume 400ml (bottom) and 1200ml (top) representative and the percentage ratio that is calculated.It should be noted that for blend A the density result that " bottom "-funnel method obtains is 841.8kg/m
3, greater than the density 841.4kg/m of pure AGO
3Yet this result does not drop within the reproducibility of IP365 method, and this result shows that " bottom " sample is 100%AGO.
Be not thought of as analytic density and repeatedly the time of (sub) sampling must be identical, because in 24 hours observed time period, the outward appearance of each blend seems not change.
Table 2
For each method, when considering respectively to organize blend A and B, it is evident that, at top and place, bottom, the percentage ratio of existing each component should add AGO not having to provide best blend under the condition of stirring in each blend on the GTL top, then is false on the contrary.
Claims (10)
1. the method for mineral derived hydrocarbon product of blend and Fisher-Tropsch derived hydrocarbon product, wherein by providing a certain amount of mineral derived hydrocarbon product and Fisher-Tropsch derived hydrocarbon product in the storage tank on the ground, so that initial mineral derived hydrocarbon product is located substantially on Fisher-Tropsch derived hydrocarbon product top.
2. the process of claim 1 wherein that the Fisher-Tropsch derived product of initial at least 50% volume is present in lower part of land storage tank.
3. claim 1 or 2 method, wherein mineral and Fisher-Tropsch derived product are overlapping greater than 50% boiling range.
4. each method of claim 1-3, wherein mineral hydrocarbon product comprises the residual oil part of crude mineral oil, gas field condensation product, factory's condensation product or petroleum naphtha, kerosene, gas oil, vacuum overhead product, deasphalted oil or crude oil.
5. the method for claim 4, wherein blend product is: the blend of mineral crude oil and fischer-tropsch synthetic crude, the blend of Fisher-Tropsch derived petroleum naphtha and gas field condensation product, the blend of Fisher-Tropsch derived gas oil and mineral derived gas oil, or the blend of the deasphalted oil of the vacuum overhead product of Fisher-Tropsch derived waxy raffinate and mineral oil derived and/or mineral oil derived.
6. the method for claim 5 wherein prepares the blend of Fisher-Tropsch derived gas oil and mineral derived gas oil.
7. the method for claim 6 is wherein when pouring out blend product, to wherein adding the blend additive from land storage tank.
8. the blend product of producing of the method by aforementioned each claim.
9. the purposes that acts as a fuel of the blend product of claim 8.
10. the purposes of claim 9, wherein fuel is motor vehicle gas oil or industrial gas oil.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP05108729 | 2005-09-21 | ||
| EP05108729.4 | 2005-09-21 |
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| Publication Number | Publication Date |
|---|---|
| CN101305080A true CN101305080A (en) | 2008-11-12 |
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| CNA2006800421108A Pending CN101305080A (en) | 2005-09-21 | 2006-09-20 | Process to blend a mineral derived hydrocarbon product and a Fisher-Tropsch derived hydrocarbon product |
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|---|---|
| US (1) | US20070135664A1 (en) |
| EP (1) | EP1926802A1 (en) |
| JP (1) | JP5281404B2 (en) |
| CN (1) | CN101305080A (en) |
| AU (1) | AU2006298850A1 (en) |
| BR (1) | BRPI0616281A2 (en) |
| WO (1) | WO2007039460A1 (en) |
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| FR2909097B1 (en) * | 2006-11-27 | 2012-09-21 | Inst Francais Du Petrole | METHOD FOR CONVERTING GAS TO LIQUIDS WITH SIMPLIFIED LOGISTICS |
| CN101889070A (en) * | 2007-12-07 | 2010-11-17 | 国际壳牌研究有限公司 | Base oil formulations |
| WO2018077976A1 (en) * | 2016-10-27 | 2018-05-03 | Shell Internationale Research Maatschappij B.V. | Process for preparing an automotive gasoil |
| WO2018206729A1 (en) * | 2017-05-11 | 2018-11-15 | Shell Internationale Research Maatschappij B.V. | Process for preparing an automotive gas oil fraction |
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| US20060065573A1 (en) * | 2004-09-28 | 2006-03-30 | Chevron U.S.A. Inc. | Fischer-tropsch wax composition and method of transport |
-
2006
- 2006-09-20 CN CNA2006800421108A patent/CN101305080A/en active Pending
- 2006-09-20 AU AU2006298850A patent/AU2006298850A1/en not_active Abandoned
- 2006-09-20 WO PCT/EP2006/066533 patent/WO2007039460A1/en active Application Filing
- 2006-09-20 BR BRPI0616281A patent/BRPI0616281A2/en not_active IP Right Cessation
- 2006-09-20 JP JP2008531692A patent/JP5281404B2/en not_active Expired - Fee Related
- 2006-09-20 EP EP20060793664 patent/EP1926802A1/en not_active Ceased
- 2006-09-21 US US11/534,112 patent/US20070135664A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| WO2007039460A1 (en) | 2007-04-12 |
| JP5281404B2 (en) | 2013-09-04 |
| EP1926802A1 (en) | 2008-06-04 |
| JP2009509020A (en) | 2009-03-05 |
| US20070135664A1 (en) | 2007-06-14 |
| BRPI0616281A2 (en) | 2016-08-23 |
| AU2006298850A1 (en) | 2007-04-12 |
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