CN101410488B - Process for producing liquid fuel base - Google Patents
Process for producing liquid fuel base Download PDFInfo
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- CN101410488B CN101410488B CN200780011430.1A CN200780011430A CN101410488B CN 101410488 B CN101410488 B CN 101410488B CN 200780011430 A CN200780011430 A CN 200780011430A CN 101410488 B CN101410488 B CN 101410488B
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- hydrocracking
- liquid fuel
- hydrocracking catalyst
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
- B01J29/12—Noble metals
- B01J29/126—Y-type faujasite
-
- 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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
- C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
- C10G47/12—Inorganic carriers
- C10G47/16—Crystalline alumino-silicate carriers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/20—After treatment, characterised by the effect to be obtained to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/42—Addition of matrix or binder particles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
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- Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
A process for producing a fuel base, characterized in that paraffinic hydrocarbons are hydrocracked in the presence of a hydrocracking catalyst comprising zeolite USY having an average particle diameter of 0.8 [mu]m or smaller, so as to result in a degree of cracking as defined by the following equation (1) of 75-90 mass%.
Description
Technical field
The present invention relates to the manufacture method of liquid fuel base.
Background technology
In recent years, to the strictness that becomes rapidly of the environmental restraint of liquid fuels such as gasoline or light oil, more and more higher to sulphur composition or the expectation low, eco-friendly clean fuel liquid of aromatic hydrocarbons content.Make industry at oil fuel, people are studying the manufacture method that the sulphur composition can be reduced to the various clean fuels below the 10ppm.
As one of manufacture method of this clean fuel, can list with pitch or coal gasification or gas renormalizing and fischer-tropsch (FT) synthesis method that the hydrogen that obtains and carbon monoxide are raw material.According to the FT synthesis method, can make and be rich in paraffinic hydrocarbons and the liquid fuel base of sulfur-bearing composition not.
In the FT synthesis method, can generate wax, but also can carry out hydrocracking to this wax, the base material of its crackate as clean fuel used.When wax is carried out hydrocracking, can obtain act as a fuel the useful gasoline fraction of base material, kerosene(oil)fraction and light oil distillate with high selectivity, that is, and reduce than gasoline fraction more the growing amount of the gas of lightweight be important.The generation that suppresses this light gas helps to improve the economy of technology integral body.Therefore, people are studying the manufacture method of the optionally liquid fuel base of paying attention to these cuts.For example, the use of record load platinum and the catalyzer cause wax that forms is made the method for middle runnings on the amorphism silica alumina in the patent documentation 1.
[patent documentation 1] spy opens flat 6-41549 communique
Summary of the invention
The problem that invention will solve
Such as above-mentioned patent documentation 1 record, as the gordian technique that is used for being made by wax liquid fuel base, mainly be to concentrate one's energy employed catalyzer in the technology is carried on technical development in the past.Yet present practical situation are, can fully suppress technology that light gas generates untapped come out still.
The present invention carries out in light of this situation, and its purpose is, provides a kind of and carries out hydrocracking and when obtaining crackate when the raw material that will contain normal paraffin, can fully suppress the manufacture method of the liquid fuel base that light gas generates.
Be used for solving the means of problem
The inventor etc. study intensively in order to achieve the above object, found that, in the hydrocracking process of paraffinic hydrocarbon, the catalyzer that contains the USY zeolite of median size below 0.8 μ m by use, make the cracking rate be in the scope of regulation, just can solve above-mentioned problem, so far finish the present invention.
Namely, the manufacture method of liquid fuel base of the present invention is characterized in that, in the presence of the hydrocracking catalyst that contains the USY zeolite below the median size 0.8 μ m, the paraffinic hydrocarbon is carried out hydrocracking, make the cracking rate by following formula (1) definition reach 75～90 quality %.
According to the present invention, when the paraffinic hydrocarbon is carried out hydrocracking, can fully suppress the generation of light gas.Specifically, be benchmark with the total mass of the crackate that obtains, the light gas growing amount of carbon number 1～3 is reached below the 1.8 quality %.Therefore, the manufacture method of liquid fuel base of the present invention is very useful aspect the economy that improves the technology of making liquid fuel.
In the present invention, consider from the viewpoint of the growing amount of more abundant inhibition light gas that hydrocracking catalyst preferably contains the following USY zeolite of median size 0.5 μ m.In addition, consider that from same viewpoint hydrocracking catalyst preferably contains the aluminum oxide boron oxide.
In addition, in the present invention, the paraffinic hydrocarbon is preferably the wax (FT wax) that adopts Fischer-Tropsch synthesis to make.This is because FT wax is rich in paraffinic hydrocarbons, is substantially free of the sulphur composition simultaneously.
The invention effect
According to the present invention, provide a kind of when obtaining crackate when the raw material that contains normal paraffin is carried out hydrocracking, can fully suppress the manufacture method of the liquid fuel base that light gas generates.
Description of drawings
Fig. 1 is the explanatory view that fixed-bed reactor one example of the present invention's use is shown.
Nomenclature
1... reaction tower, 2... hydrocracking catalyst layer.
Embodiment
Below explain the preferred embodiments of the invention.
Fig. 1 is the explanatory view that preferred fixed-bed reactor one example of using among the present invention is shown.
In fixed-bed reactor shown in Figure 1, in reaction tower 1, be provided with hydrocracking catalyst layer 2.In addition, at the top of reaction tower 1, be connected with for the pipeline L1 that in reaction tower 1, supplies with hydrogen, at upstream side pipeline L1 and connection section reaction tower 1, be connected with the pipeline L2 for supply chain alkanes hydrocarbon.On the other hand, in the bottom of reaction tower 1, be connected with the pipeline L3 that draws from reaction tower 1 for the crackate after the hydrocracking, the other end of pipeline L3 then is connected on the atmospheric distillation plant 3.
Utilize water distilling apparatus 3, crackate can be fractionated into each cut.As by the cut of fractionation, for example can list, boiling point is lower than light oil distillate and the wax slop of boiling point more than 360 ℃ of 260～360 ℃ of kerosene(oil)fraction, boiling points of 160～260 ℃ of naphtha fraction, boiling points of 30 ℃ 30～160 ℃ of gas fraction, boiling points.In water distilling apparatus 3, the pipeline (L4～L8) respectively be delivered in each subsequent handling of each cut that fractionation is come out by being connected with water distilling apparatus 3.
The paraffinic hydrocarbon that uses as raw material refers to be the low compositions of hydrocarbons of the side chain degree of principal constituent with normal paraffin.Total mass with the paraffinic hydrocarbon is benchmark, and the containing ratio of normal paraffin is preferably more than the 80 quality %, more preferably more than the 85 quality %.
Carbon number for hydrocarbon contained in the paraffinic hydrocarbon does not have particular restriction, is generally the scope of carbon number 15～100.As this wax, for example can list the slack wax in the oil system, Microcrystalline Wax etc.; The so-called FT wax that in synthetic system, adopts the FT synthesis method to make.Consider from the viewpoint that reduces carrying capacity of environment, as wax, preferred especially FT wax.
Constitute the hydrocracking catalyst of hydrocracking catalyst layer 2, as its carrier, containing median size is the following USY zeolite of 0.8 μ m.Consider that from the viewpoint of the growing amount of more abundant inhibition light gas the median size of USY zeolite is more preferably below the 0.5 μ m.If the median size of USY zeolite surpasses 0.8 μ m, then be difficult to fully suppress the growing amount of light gas.
In addition, consider from the viewpoint of the growing amount of more abundant inhibition light gas, the amorphous solid acid more than a kind that hydrocracking catalyst preferably contains the USY zeolite and selects from silica alumina, aluminum oxide boron oxide and silicon-dioxide zirconium white more preferably contains USY zeolite and aluminum oxide boron oxide.
The mol ratio of the silica/alumina in the USY zeolite (silica alumina ratio) is preferably 25～50.If silica alumina ratio is less than 25, then the growing amount of light gas has the tendency of increase; On the other hand, if silica alumina ratio surpasses 50, then because catalyst activity reduces and must improve temperature of reaction, thus the tendency that catalyst life is had shorten.
In addition, the content of USY zeolite is benchmark with the total amount of hydrocracking catalyst, is preferably 1～30 quality %.If the content of USY zeolite is less than 1 quality %, then because catalyst activity reduces and must improve temperature of reaction, thus the tendency that catalyst life is had shorten, on the other hand, if surpass 30 quality %, then the growing amount of light gas has the tendency of increase.
When hydrocracking catalyst contained USY zeolite and aluminum oxide boron oxide, the content of aluminum oxide boron oxide was benchmark with the total amount of hydrocracking catalyst, is preferably 5～70 quality %.If the content of aluminum oxide boron oxide, then adds the effect of the aluminum oxide boron oxide inadequate tendency that becomes less than 5 quality %, if surpass 70 quality %, then the growing amount of light gas has the tendency of increase.
In the aluminum oxide boron oxide, the mass ratio of aluminum oxide/boron oxide is preferably 1.2～7.8.If the mass ratio of aluminum oxide/boron oxide is beyond above-mentioned scope, then the growing amount of light gas has the tendency of increase.
In addition, hydrocracking catalyst can also contain and is useful on the tackiness agent that makes the carrier moulding.Tackiness agent is not had particular restriction, as preferred adhesive, can list boehmite or silicon-dioxide, wherein preferred boehmite.The shape of carrier does not have particular restriction, can be granular, cylindric shapes such as (particles).
In addition, as hydrocracking catalyst, the catalyzer that forms of the metal that load is selected from periodictable VIa family and group VIII on above-mentioned carrier preferably.As the metal of VIa family, can list chromium, molybdenum, tungsten particularly; As the metal of group VIII, can list cobalt, nickel, rhodium, palladium, iridium, platinum particularly.In these metals, more preferably palladium and platinum, further preferred platinum.These loaded metals can use a kind separately, perhaps will be used in combination more than 2 kinds.The charge capacity of metal does not have particular restriction, when supported palladium and platinum, is that the charge capacity of benchmark generally is in the scope of 0.05～2.0 quality % with the carrier quality.
When containing above-mentioned metal in the hydrocracking catalyst that constitutes hydrocracking catalyst layer 2, preferably before hydrocracking, in reducing gas atmosphere such as hydrogen, carry out the reduction of metal in advance.Reductive condition is not had particular restriction, as reduction temperature, be preferably 300～360 ℃, as the recovery time, be preferably 1～6 hour.
Use fixed-bed reactor shown in Figure 1, carry out the hydrocracking of paraffinic hydrocarbon.In order fully to suppress the growing amount of light gas (carbon number 1～3), must carry out hydrocracking according to the condition that the cracking rate that makes above-mentioned formula (1) definition reaches 75～90 quality % (being preferably 77～88 quality %) herein.If the cracking rate is less than 75 quality %, then the growing amount of wax slop increases, and is difficult to reach the selectively producing liquid making fluid fuel base material with high.On the other hand, if the cracking rate surpasses 90 quality %, then the growing amount of light gas increases.
In addition, reaction conditions when carrying out hydrocracking about the paraffinic hydrocarbon, as long as the cracking rate of above-mentioned formula (1) definition is 75～90 quality %, just there is not particular restriction, as representational reaction conditions, temperature of reaction is 250～370 ℃, and the hydrogen dividing potential drop is 0.5～10.0MPa, and the liquid hourly space velocity of paraffinic wax is 0.1～5.0h
-1, hydrogen/oil ratio is 150～2000NL/L.If carry out hydrocracking under the reaction conditions beyond the above-mentioned scope, then the growing amount of light gas has the tendency of increase.
Should illustrate, in the reaction conditions with hydrocracking is set in above-mentioned scope after, for the defined cracking rate of formula (1) is adjusted to desirable value, for example, as long as the conditioned reaction temperature.
The present invention is not limited to above-mentioned embodiment.For example, in the above-described embodiment, though hydrocracking catalyst layer 2 is single layer structure, also different types of hydrocracking catalyst can be built up multilayered structure layer by layer.In addition, as the device of the hydrocracking of carrying out the paraffinic hydrocarbon, though what illustrate is fixed-bed reactor,, so long as can make paraffinic hydrocarbon and the contacted device of hydrocracking catalyst, just do not have particular restriction.For example, also can be fluidized bed reaction.
Embodiment
Below based on embodiment and comparative example, be described more specifically the present invention, but the present invention is not subjected to any restriction of following examples.
The preparation of＜hydrocracking catalyst 〉
(catalyzer 1)
Will by the USY zeolite of median size 0.7 μ m (silica alumina ratio: 30) mixture that constitutes of 5 mass parts and boehmite (tackiness agent) 95 mass parts fully mixing after, it is shaped to φ 1.6mm (1/16 inch), is about the columned carrier of 3mm.This formed body after under 120 ℃ dry 3 hours, 500 ℃ of following roastings 1 hour, is obtained carrier thus.Make the aqueous solution of these carrier impregnation dichloro four ammino platinum (II), load is the platinum of 0.5 quality % with respect to carrier on carrier.It after under 120 ℃ dry 3 hours, 500 ℃ of following roastings 1 hour, is obtained hydrocracking catalyst (catalyzer 1) thus.
(catalyzer 2)
Use is by the USY zeolite (silica alumina ratio: 32) the abundant mixing material that forms of mixture warp of 5 mass parts and boehmite (tackiness agent) 95 mass parts formation of median size 0.4 μ m, be made into formed body, in addition, similarly obtain hydrocracking catalyst (catalyzer 2) with catalyzer 1.
(catalyzer 3)
Use is by the USY zeolite (silica alumina ratio: 32) 5 mass parts, the aluminum oxide boron oxide (mass ratio of aluminum oxide/boron oxide: 5.5) the abundant mixing material that forms of mixture warp of 55 mass parts and boehmite (tackiness agent) 40 mass parts formation of median size 0.4 μ m, be made into formed body, making the charge capacity with respect to the platinum of carrier is 0.4 quality %, in addition, similarly obtain hydrocracking catalyst (catalyzer 3) with catalyzer 1.
(catalyzer 4)
Use is by the USY zeolite (silica alumina ratio: 30) the abundant mixing material that forms of mixture warp of 5 mass parts and boehmite (tackiness agent) 95 mass parts formation of median size 1.2 μ m, be made into formed body, in addition, similarly obtain hydrocracking catalyst (catalyzer 4) with catalyzer 1.
(catalyzer 5)
(mol ratio of silica/alumina: 2.3) mixture of 70 mass parts and boehmite (tackiness agent) 30 mass parts formation is through the abundant mixing material that forms by silica alumina in use, be made into formed body, in addition, similarly obtain hydrocracking catalyst (catalyzer 5) with catalyzer 1.
The rerum natura of the formation of the carrier of catalyzer 1～5, USY zeolite and the charge capacity of platinum are shown in Table 1.
[table 1]
The hydrocracking of＜paraffinic hydrocarbon 〉
(embodiment 1)
Catalyzer 1 (100ml) is filled in the reaction tower 1 of fixed-bed reactor shown in Figure 1, forms the hydrocracking catalyst layer, use this reaction unit, carry out the hydrocracking of paraffinic hydrocarbon.
At first, in hydrogen stream and under 345 ℃, the reduction that the hydrocracking catalyst of filling carried out 4 hours is handled.Then, carry out the hydrocracking of paraffinic hydrocarbon.As the paraffinic hydrocarbon, use FT wax (carbon number 23～80 (boiling temperature is more than 361 ℃), normal paraffin containing ratio: 88 quality %).In addition, the reaction conditions of hydrocracking is that the liquid hourly space velocity that makes FT wax is 2.0h
-1(flow stream velocity of FT wax: 200ml/h), making the hydrogen dividing potential drop is 5MPa, and making hydrogen/oil ratio is 700NL/L, and making temperature is 320 ℃.Crackate is carried out the result of distillation test, and under this reaction conditions, the cracking rate of formula (1) definition is 79 quality %.
The amount of contained light gas (carbon number 1～3) is carried out quantitatively with online vapor-phase chromatography in the crackate.The total mass that has illustrated in the table 2 with crackate is the growing amount of the light gas of benchmark.Show temperature of reaction and the cracking rate of employed hydrocracking catalyst, hydrocracking in the table 2 simultaneously.
(embodiment 2)
Catalyzer 2 (100ml) is filled in the reaction tower 1, forms the hydrocracking catalyst layer, the temperature of reaction that makes hydrocracking is 318 ℃, in addition, carries out the mensuration of the growing amount of the hydrocracking of paraffinic hydrocarbon and light gas similarly to Example 1.Should illustrate, as the paraffinic hydrocarbon, use FT wax similarly to Example 1.According to the reaction conditions of present embodiment, the cracking rate that obtains is 82 quality %.The results are shown in the table 2.
(embodiment 3)
Catalyzer 3 (100ml) is filled in the reaction tower 1, forms the hydrocracking catalyst layer, the temperature of reaction that makes hydrocracking is 304 ℃, in addition, carries out the mensuration of the growing amount of the hydrocracking of paraffinic hydrocarbon and light gas similarly to Example 1.Should illustrate, as the paraffinic hydrocarbon, use FT wax similarly to Example 1.According to the reaction conditions of present embodiment, the cracking rate that obtains is 87 quality %.The results are shown in the table 2.
(comparative example 1)
Catalyzer 4 (100ml) is filled in the reaction tower 1, forms the hydrocracking catalyst layer, the temperature of reaction that makes hydrocracking is 322 ℃, in addition, carries out the mensuration of the growing amount of the hydrocracking of paraffinic hydrocarbon and light gas similarly to Example 1.Should illustrate, as the paraffinic hydrocarbon, use FT wax similarly to Example 1.According to the reaction conditions of present embodiment, the cracking rate that obtains is 80 quality %.The results are shown in the table 2.
(comparative example 2)
Catalyzer 5 (100ml) is filled in the reaction tower 1, forms the hydrocracking catalyst layer, the temperature of reaction that makes hydrocracking is 363 ℃, in addition, carries out the mensuration of the growing amount of the hydrocracking of paraffinic hydrocarbon and light gas similarly to Example 1.Should illustrate, as the paraffinic hydrocarbon, use FT wax similarly to Example 1.According to the reaction conditions of present embodiment, the cracking rate that obtains is 81 quality %.The results are shown in the table 2.
[table 2]
| Embodiment 1 | |
|
Comparative example 1 | Comparative example 2 | |
| Employed catalyzer | Catalyzer 1 | |
|
Catalyzer 4 | Catalyzer 5 |
| Temperature of reaction (℃) | 320 | 318 | 304 | 322 | 363 |
| Cracking rate (quality %) | 79 | 82 | 87 | 80 | 81 |
| The growing amount of light gas (quality %) | 1.5 | 1.5 | 1.6 | 1.9 | 2.2 |
As mentioned above, in the hydrocracking of paraffinic hydrocarbon, contain the hydrocracking catalyst that median size is the USY zeolite below the 0.8 μ m by use, can fully suppress the generation of light gas.
Industrial applicability
According to the present invention, provide a kind of when obtaining crackate when the raw material that contains normal paraffin is carried out hydrocracking, can fully suppress the manufacture method of liquid fuel base of the generation of light gas.
Claims (5)
1. the manufacture method of liquid fuel base, it is characterized in that, in the presence of the hydrocracking catalyst that contains the USY zeolite below the median size 0.8 μ m, the paraffinic hydrocarbon is carried out hydrocracking, make the cracking rate by following formula (1) definition reach 75～90 quality %, the mol ratio of the silica/alumina in the USY zeolite is that the content of 25～50, USY zeolite is benchmark with the total amount of hydrocracking catalyst, be 1～30 quality %
2. the manufacture method of the described liquid fuel base of claim 1 is characterized in that, above-mentioned hydrocracking catalyst contains the following USY zeolite of median size 0.5 μ m.
3. the manufacture method of claim 1 or 2 described liquid fuel bases is characterized in that, above-mentioned hydrocracking catalyst contains the aluminum oxide boron oxide.
4. the manufacture method of claim 1 or 2 described liquid fuel bases is characterized in that, above-mentioned paraffinic hydrocarbon is by the synthetic wax of making of fischer-tropsch.
5. the manufacture method of the described liquid fuel base of claim 3 is characterized in that, above-mentioned paraffinic hydrocarbon is by the synthetic wax of making of fischer-tropsch.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2006100182A JP2007270061A (en) | 2006-03-31 | 2006-03-31 | Method for producing liquid fuel base |
| JP100182/2006 | 2006-03-31 | ||
| PCT/JP2007/054942 WO2007114003A1 (en) | 2006-03-31 | 2007-03-13 | Process for producing liquid fuel base |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101410488A CN101410488A (en) | 2009-04-15 |
| CN101410488B true CN101410488B (en) | 2013-08-21 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200780011430.1A Active CN101410488B (en) | 2006-03-31 | 2007-03-13 | Process for producing liquid fuel base |
Country Status (6)
| Country | Link |
|---|---|
| JP (1) | JP2007270061A (en) |
| CN (1) | CN101410488B (en) |
| AU (1) | AU2007231962B2 (en) |
| MY (1) | MY148342A (en) |
| RU (1) | RU2428456C2 (en) |
| WO (1) | WO2007114003A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US8345890B2 (en) | 2006-01-05 | 2013-01-01 | Audience, Inc. | System and method for utilizing inter-microphone level differences for speech enhancement |
| US8744844B2 (en) | 2007-07-06 | 2014-06-03 | Audience, Inc. | System and method for adaptive intelligent noise suppression |
| US8143620B1 (en) | 2007-12-21 | 2012-03-27 | Audience, Inc. | System and method for adaptive classification of audio sources |
| JP5730104B2 (en) * | 2011-03-31 | 2015-06-03 | 独立行政法人石油天然ガス・金属鉱物資源機構 | Support selection method and hydrotreating catalyst production method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0321303A2 (en) * | 1987-12-18 | 1989-06-21 | Exxon Research And Engineering Company | Process for the hydroisomerization of wax to produce middle distillate products |
| WO2005092500A1 (en) * | 2004-03-29 | 2005-10-06 | Nippon Oil Corporation | Hydrocracking catalyst and process for producing liquid hydrocarbon |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5814109A (en) * | 1997-02-07 | 1998-09-29 | Exxon Research And Engineering Company | Diesel additive for improving cetane, lubricity, and stability |
| AU2003266527A1 (en) * | 2002-09-24 | 2004-04-19 | Nippon Oil Corporation | Hydrocracking catalyst and process for production of liquid hydrocarbons |
| JP4047206B2 (en) * | 2003-03-20 | 2008-02-13 | 株式会社ジャパンエナジー | Environment-friendly diesel oil and method for producing the same |
-
2006
- 2006-03-31 JP JP2006100182A patent/JP2007270061A/en active Pending
-
2007
- 2007-03-13 MY MYPI20083514 patent/MY148342A/en unknown
- 2007-03-13 WO PCT/JP2007/054942 patent/WO2007114003A1/en active Application Filing
- 2007-03-13 AU AU2007231962A patent/AU2007231962B2/en active Active
- 2007-03-13 CN CN200780011430.1A patent/CN101410488B/en active Active
- 2007-03-13 RU RU2008143258/04A patent/RU2428456C2/en active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0321303A2 (en) * | 1987-12-18 | 1989-06-21 | Exxon Research And Engineering Company | Process for the hydroisomerization of wax to produce middle distillate products |
| WO2005092500A1 (en) * | 2004-03-29 | 2005-10-06 | Nippon Oil Corporation | Hydrocracking catalyst and process for producing liquid hydrocarbon |
Non-Patent Citations (1)
| Title |
|---|
| JP特表2001-522382A 2001.11.13 |
Also Published As
| Publication number | Publication date |
|---|---|
| RU2008143258A (en) | 2010-05-10 |
| RU2428456C2 (en) | 2011-09-10 |
| CN101410488A (en) | 2009-04-15 |
| AU2007231962B2 (en) | 2011-09-01 |
| AU2007231962A1 (en) | 2007-10-11 |
| MY148342A (en) | 2013-03-29 |
| WO2007114003A1 (en) | 2007-10-11 |
| JP2007270061A (en) | 2007-10-18 |
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