WO2007034556A1 - Procede permettant de produire un mazout d'hydrocarbures - Google Patents

Procede permettant de produire un mazout d'hydrocarbures Download PDF

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Publication number
WO2007034556A1
WO2007034556A1 PCT/JP2005/017522 JP2005017522W WO2007034556A1 WO 2007034556 A1 WO2007034556 A1 WO 2007034556A1 JP 2005017522 W JP2005017522 W JP 2005017522W WO 2007034556 A1 WO2007034556 A1 WO 2007034556A1
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Prior art keywords
mass
oil
catalyst
temperature
carbon atoms
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PCT/JP2005/017522
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English (en)
Japanese (ja)
Inventor
Hiroaki Hara
Toshio Shimizu
Yutaka Miyata
Original Assignee
Japan Oil, Gas And Metals National Corporation
Japan Petroleum Exploration Co., Ltd.
Cosmo Oil Co., Ltd.
Nippon Steel Engineering Corporation
Inpex Corporation
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Application filed by Japan Oil, Gas And Metals National Corporation, Japan Petroleum Exploration Co., Ltd., Cosmo Oil Co., Ltd., Nippon Steel Engineering Corporation, Inpex Corporation filed Critical Japan Oil, Gas And Metals National Corporation
Priority to US11/631,793 priority Critical patent/US20080222945A1/en
Priority to PCT/JP2005/017522 priority patent/WO2007034556A1/fr
Priority to AU2005335184A priority patent/AU2005335184B2/en
Priority to EP05785789A priority patent/EP1927645A4/fr
Priority to ZA2007/00432A priority patent/ZA200700432B/en
Publication of WO2007034556A1 publication Critical patent/WO2007034556A1/fr

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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves

Definitions

  • the present invention relates to a reaction between carbon monoxide and hydrogen, a so-called Fischer's Tropsch (FT) synthesis, a paraffinic synthetic feedstock, a hydrocarbon fuel oil or a base material thereof, particularly a kerosene equivalent fraction. It is related with the method of manufacturing.
  • FT Fischer's Tropsch
  • the present invention is a hydrocarbon fuel that does not contain sulfur and has a good low temperature fluidity, for example, a pour point and cloud point measured according to JIS K2 269, or a clogging point measured according to 3 ⁇ 4 JIS K2288.
  • the present invention relates to a method for producing oil or its base material, particularly a kerosene oil equivalent fraction.
  • Kerosene oil distillate derived from crude oil generally contains sulfur compounds, and when these oils are used as fuel, sulfur present in sulfur compounds is converted to low molecular weight sulfur compounds. And discharged into the atmosphere. In addition, in exhaust gas aftertreatment devices that have been introduced in recent years, if a sulfur compound is present in the fuel, the catalyst used may be poisoned.
  • the crude oil-derived kerosene distillate contains aromatics, which are said to increase the amount of suspended particulate matter (PM) and nitrogen oxides (NOx) in the exhaust gas. . Therefore, it is desirable that the fuel oil has a low sulfur content or aromatic content.
  • the product produced by Fischer's Tropsch synthesis (hereinafter also referred to as FT method) using a mixed gas composed of carbon monoxide and hydrogen removes impurities in the mixed gas. Compound is not included.
  • the product obtained by the FT method has normal paraffin as a main component and hardly contains aromatics.
  • the product produced by the FT method is composed mainly of normal paraffin and contains a large amount of heavy wax that is solid at room temperature and cannot be used as a liquid fuel. Therefore, for example, when distilling in the cut range equivalent to commercially available light oil derived from crude oil, low-temperature fluidity is not so good at low temperatures because it precipitates ox crystals.
  • low-temperature fluidity is not so good at low temperatures because it precipitates ox crystals.
  • JIS K2254 JIS K2254 Therefore, it is possible to reduce the mixing ratio of heavy components by keeping the measured 90% distillation temperature low, etc. This reduces the yield of diesel oil fractions because heavy components cannot be used. Therefore, there is a need for a method for effectively using these heavy and unusable fractions of kerosene from the products produced by the FT method, and obtaining fuel oil that does not impair low-temperature fluidity.
  • Patent Document 1 Japanese Patent Laid-Open No. 5-302088
  • Patent Document 2 Japanese Patent Publication No. 8-511302
  • the present invention hydrotreats heavy wax produced by the FT method, decomposes it at a reduced gasification rate, and increases the isomerization reaction that occurs simultaneously.
  • it is an object to efficiently obtain a liquid fuel that does not contain sulfur and has good low-temperature fluidity.
  • the inventors of the present invention are platinum group catalysts using a specific support under specific reaction conditions according to the type of support used.
  • the heavy wax produced by the FT method is hydrotreated and decomposed and isomerized, the gasification rate is reduced, and the yield of kerosene oil fractions is high.
  • the present inventors have found that the fluidity is improved and completed the present invention.
  • the present invention provides the following method for producing hydrocarbon fuel oil in order to achieve the above object.
  • a catalyst comprising 0.01 to 10% by mass of at least one platinum group metal on a catalyst basis, in terms of metal, on a support mainly containing zeolite.
  • Hydrogen partial pressure is 2 ⁇ 20MPa
  • temperature is 200 ⁇ 320 ° C
  • liquid space velocity is 0.1 ⁇ 2h
  • Hydrogen Z oil ratio is 100 ⁇ 2000LZL
  • the gasification rate is less than 10% by mass, decomposition and isomerization are performed, and the isoparaffin ratio in the fraction having 9 to 21 carbon atoms is set to 70% by mass or more.
  • a method for producing a hydrocarbon fuel oil (hereinafter referred to as the “first method” of the present invention) o
  • a catalyst comprising 0.01 to 10% by mass of at least one platinum group metal on a catalyst basis, in terms of metal, on a carrier mainly composed of silica alumina,
  • Hydrogen partial pressure is 2 ⁇ 20MPa
  • temperature is 350 ⁇ 400 ° C
  • liquid space velocity is 0.1 ⁇ 2h
  • Hydrogen Z oil ratio is 100 ⁇ 2000LZL
  • the gasification rate is less than 10% by mass, decomposition and isomerization are performed, and the isoparaffin ratio in the fraction having 9 to 21 carbon atoms is set to 70% by mass or more.
  • a heavy wax produced by the FT method is hydrotreated to produce a gas.
  • a gas By suppressing the decomposition rate and increasing the isomerization reaction that occurs at the same time, it is possible to obtain a liquid fuel efficiently without containing a sulfur content and having good low-temperature fluidity.
  • FIG. 1 is a graph showing the normal paraffin content according to the number of carbon atoms of the raw material wax used in Examples and Comparative Examples.
  • the heavy wax produced by the FT method is hydrogenated under a specific reaction condition corresponding to the type of support used with a platinum group catalyst using a specific support. It is characterized in that it is processed.
  • the catalyst used in the present invention is a platinum group catalyst in which at least one platinum group metal is contained in a support.
  • the platinum group metal include platinum, noradium, ruthenium, and rhodium, and platinum is particularly preferable. These can be used alone or in combination of two or more.
  • the platinum group metal content in the catalyst used in the present invention is 0.01 to 10% by mass in terms of metal based on the catalyst.
  • these platinum group metals have different wax decomposition rates depending on the metal species even if they have the same content, so in order to increase the yield of the desired fraction, the content of each metal species is within the above content range. It is desirable to optimize within.
  • the platinum content in the catalyst is 0.05 to 5 in terms of metal on a catalyst basis. % By mass is preferred. 0.1 to 1% by mass is more preferred.
  • the platinum group catalyst carrier used in the present invention is a carrier mainly containing zeolite.
  • zeolites may be natural or synthesized.
  • the atomic ratio Si ZA1 of kaye to aluminum in zeolite is preferably about 1 or more.
  • alkali such as sodium in zeolite is preferred. If the content of the metal ion is large, the catalytic activity is lowered. Therefore, it is usually preferable to adjust the content to about 0.5% by mass or less based on the zeolite.
  • the support is mainly composed of silica alumina.
  • the weight ratio of silica and alumina is not particularly limited, but the weight ratio of silica Z alumina in the carrier is 1 in order to promote the isomerization reaction and obtain a fuel oil having a high isoparaffin ratio and good low temperature fluidity. More than 5 is desirable.
  • reaction conditions are adopted depending on the type of support.
  • zeolite and silica-alumina it is also possible to use other carriers than the above.
  • an inorganic oxide or one or more selected from inorganic crystalline compounds or clay mineral powers can be used.
  • inorganic oxides include silica, alumina, polya, magnesia, titer, silica magnesia, silica-zinoleconia, silica-tria, silica monoberia, silica titania, silica-boria, and alumina zirconia.
  • examples of inorganic crystalline compounds or clay minerals include molecular sieves, other inorganic crystalline compounds, and clays such as montmorillonite, kaolin, bentonite, adadaval guide, bauxite, kaolinite, nacrite, and anoxite. Minerals. These can be used alone or in combination of two or more.
  • the specific surface area, pore volume, and average pore diameter of the above-mentioned various carriers are not particularly limited in the present invention, but in order to obtain a catalyst having excellent hydrogenation activity, the specific surface area is 25.
  • the pore volume that is preferably Om 2 / g or more is preferably 0.1 to 1.
  • the average pore diameter that is preferably OmL / g is preferably 0.5 to 25 nm.
  • a catalyst using a carrier containing silica 20% by mass or more of silica is used in order to promote the isomerization reaction and obtain a fuel oil having a high isoparaffin ratio and good low-temperature fluidity. It is preferable that the carrier contains.
  • a method of incorporating an active metal such as a platinum-based metal into a support that is, a method of preparing a catalyst used in the present invention, can be performed using several known techniques.
  • an impregnation method in which a solution in which a metal compound of a platinum-based metal is dissolved in a solvent such as water, alcohols, ethers, and ketones is contained in the support by one or more impregnation treatments.
  • a solvent such as water, alcohols, ethers, and ketones
  • Drying and firing are performed after the impregnation treatment, but when the number of impregnation treatments is plural, drying and firing may be performed between each impregnation treatment.
  • Other methods include a spraying method in which a solution in which a metal compound of a platinum-based metal is dissolved in a support is sprayed, or a chemical vapor deposition method in which the metal component is chemically deposited.
  • Still other methods include a kneading method, a coprecipitation method, and an alkoxide method in which a carrier component before molding contains part or all of the metal component of the platinum-based metal for molding.
  • the physical properties such as the specific surface area and pore volume of the catalyst used in the present invention prepared by various methods as described above are not particularly limited in the present invention, but have excellent hydrogenation activity.
  • a catalyst having a specific surface area of 200 m 2 / g or more a pore volume of 0.1 to 1.2 mLZg, an average pore diameter of 0.5 to 25 nm, and a pore diameter distribution (MPD ⁇ 1.5 nm) 70% or more is preferable.
  • the catalyst used in the present invention can be used in the form of powder, granules, spheres, pellets, honeycombs, and any other shape, and the shape and structure are not particularly limited, but the shape according to the type of the reactor. Is preferably selected.
  • a molded product is generally used.
  • a binder such as an organic or inorganic compound, a binder, or the like may be used as long as the effects of the present invention are not impaired.
  • the reaction conditions for the decomposition and isomerization reactions are employed in order to achieve the intended purpose. That is, in the first method, decomposition and isomerization are carried out with a hydrogen partial pressure of 2 to 20 MPa, a temperature of 200 to 320 ° C, a liquid space velocity of 0.1 to 2 h—hydrogen / oil ratio of 100 to 2000 L / L. Perform the reaction.
  • the hydrogen partial pressure, liquid space velocity, and hydrogen Z oil ratio are The temperature is 350 to 400 ° C.
  • the hydrogen partial pressure, the liquid space velocity, and the hydrogen Z oil ratio are within the same ranges as in the first method and the second method.
  • Hydrogen partial pressure is 2 to: LOMPa is preferred. 2.5 to 8 MPa is more preferable.
  • the temperature is preferably 235 to 320 ° C, more preferably 245 to 315 ° C.
  • the temperature is preferably from 355 to 390. C, more preferably 370-380. C.
  • liquid hourly space velocity is less than 0.1 lh 1 , the processing efficiency decreases. If it exceeds 2 h- 1 , the contact time between the catalyst and the raw material oil becomes too short, and the catalytic activity is not fully exhibited.
  • the liquid space velocity is preferably 0.5 to lh 1 .
  • the hydrogen Z oil ratio is preferably 200 to 1500 LZL, more preferably 300 to 1200 LZL.
  • the oil to be treated (raw oil) used in the present invention is a wax containing 50% by mass or more of normal paraffins having 7 to more carbon atoms as a main component, and obtained by the FT method.
  • Liquid product synthetic hydrocarbon oil
  • the raw material oil for example, one obtained in a single lot may be used alone, or a plurality of those obtained in a plurality of lots may be mixed and used. Further, a catalyst obtained under a certain catalyst and a certain reaction condition may be used alone, or a plurality of catalysts obtained under a different catalyst and different reaction conditions may be used in combination. .
  • a kerosene oil fraction having a high isoparaffin ratio and good low-temperature fluidity can be obtained from synthetic hydrocarbon oil.
  • Commercial kerosene oil fractions are generally those containing 9-25 carbon atoms, but when producing kerosene oil fractions according to the present invention, fractions having 9-21 carbon atoms ( It is preferable to produce a distillation temperature of about 150 to 350 ° C. in terms of easy prevention of wax precipitation.
  • the raw material oil obtained by the FT method may be used as it is (including those having approximately 5 or more carbon atoms). However, it may be used after removing light components by distillation. Preferably, light components are removed by distillation, and normal paraffins having a carbon number corresponding to the kerosene fraction in the feedstock, particularly normal paraffins having 20 or less carbon atoms, preferably 30% by mass or less, more preferably 10% by mass. % Or less is desirable. That is, it is desirable that the normal paraffin having 21 or more carbon atoms in the feedstock is preferably more than 70% by mass, more preferably more than 90% by mass.
  • normal paraffins with carbon numbers corresponding to kerosene oil fractions or lighter fractions may be gasified to cause an increase in gasification rate. This is preferable in that it can be prevented from increasing the pour point of the fuel oil obtained without being decomposed and isoparaffinized without being decomposed.
  • the melting point of the raw material oil becomes high, so that it is likely to cause clogging in a pump or a line for supplying the raw material. In order to prevent this blockage, it is necessary to heat to a higher temperature, but the cost increases.
  • the raw material oil containing a large amount of paraffins with more than 100 carbon atoms is to be decomposed, it is necessary to use more severe decomposition conditions, which increases the cost of thermal energy.
  • decomposed components that are difficult to control decomposition may not be retained in the kerosene oil fraction, but may be excessively decomposed into lighter fractions. Therefore, it is desirable for paraffins with more than 100 carbon atoms in the feedstock oil to be below the lower limit of detection (less than about 0.1% by mass) by gas chromatography or the like.
  • the catalyst is poisoned.
  • the oxygen-containing compound is added to the feedstock You may contain 0.01 mass% or more by mass ratio.
  • the gasification rate can be reduced to less than 10%, preferably less than 5% by suppressing the content of light normal paraffin as described above.
  • a kerosene fraction having a high isoparaffin ratio and good low-temperature fluidity can be obtained, but this low-temperature fluidity is good.
  • the isoparaffin ratio is 70% by mass or more.
  • a isoparaffin ratio of 70% by mass or more is desirable in order to satisfy the JIS standard for diesel oil. In other words, in order to use as light oil in Japan, it is necessary to satisfy the pour point and clogging point specified in JIS K2204. For example, No.
  • diesel oil used in a wide area has a pour point of 7.5 ° C or less and a clogging point of 5 ° C or less.
  • the pour point is defined as + 5 ° C or less (the clogging point is not specified).
  • the pour point is preferably + 5 ° C or lower even in warm regions, more preferably 7.5 ° C or lower.
  • the pour point is adjusted to the desired pour point by mixing with a substrate having better low temperature fluidity.
  • the base material with excellent low-temperature fluidity at that time may be a light hydrocarbon or a substance containing a large amount of aromatics, but when mixing light hydrocarbons, the kinematic viscosity should not be too low. It is desirable.
  • a substrate containing a large amount of aromatics increases suspended particulate matter (PM) and nitrogen oxides (NOx) in the exhaust gas of diesel vehicles. So, because of excessive PM and NOx increase
  • the catalyst is used in a suitable reactor as a fixed bed, moving bed or fluidized bed, the above-mentioned feedstock is introduced into this reactor, and the above-mentioned water What is necessary is just to process on a raw material processing condition.
  • the catalyst is maintained as a fixed bed so that feedstock passes down the fixed bed.
  • a single reactor can be used, or two or more reactors in series can be used.
  • the reaction is performed in multiple stages using two or more reactors.
  • the reaction can be carried out by charging two or more different catalysts in the reactor.
  • the catalyst can be divided into two or more layers in the reactor, and different catalysts can be divided and packed in each layer, or the catalyst can be mixed and packed in one layer.
  • different catalysts can be used for each reactor.
  • a separation device may be provided on the downstream side of the reactor, and the heavy component may be guided upstream of the reactor to perform the hydrocracking process again.
  • the hydrotreated product can be separated in a rectification column, and the heavy unconverted material can be guided to the hydrocracking apparatus to disappear and then hydrocracked again.
  • At least a part of the hydrocracked raw material is separated and treated in a single operation to produce hydrogen, and the hydrogen is at least partially used as a product. Can also be recovered.
  • the hydrogenation reaction was performed at a reaction temperature of 360 ° C., and the activity was evaluated.
  • Table 4 shows the evaluation results.
  • activity evaluation was performed as follows. That is, the raw material wax was supplied downward to the cylindrical fixed bed flow type reaction apparatus upright.
  • the reactor was 12 mm in inner diameter (3 mm thick) and packed with 18 mL of catalyst.
  • a pretreatment reduction was performed at 300 ° C. for 2 hours using a heater provided in the reactor under hydrogen flow.
  • the hydrogen flow rate at that time is 150 mLZmin, and the hydrogen partial pressure is 3. OMPa.
  • Two stages of product recovery traps are provided, the first stage is heated to 200 ° C, the second stage is cooled with ice water, and the heavy and light fractions are collected respectively. .
  • the gasification rate was determined by the mass% of the recovered product with respect to the mass of the raw material charged in the activity evaluation.
  • the kerosene oil yield was determined by first analyzing the product recovered in the activity evaluation with a gas chromatograph to determine the total mass% of substances having 9 to 21 carbon atoms. After that, the 100 mass% force was also defined by multiplying the mass% excluding the gasification rate by the total mass% of substances having 9 to 21 carbon atoms.
  • Isoparaffins ratio in kerosene and gas oil are, when formed into a 100 wt% material having a carbon number of 9 to 21 in a gas chromatograph was defined by the mass 0/0 isoparaffins therein.
  • the hydrogenation reaction was carried out at a reaction temperature of 230 ° C, and the activity was evaluated.
  • Table 4 shows the evaluation results.
  • the activity was evaluated in the same manner as in Example 3 except that the reaction temperature was 240 ° C. Table 4 shows the evaluation results.
  • the raw material was subjected to a hydrotreating reaction at a reaction temperature of 300 ° C, and the activity was evaluated.
  • Table 4 shows the evaluation results.
  • the activity was evaluated in the same manner as in Example 6 except that the reaction temperature was 310 ° C. Table 4 shows the evaluation results.
  • the activity was evaluated in the same manner as in Example 1 except that the reaction temperature was 400 ° C. Table 4 shows the evaluation results.
  • the activity was evaluated in the same manner as in Example 1 except that the reaction temperature was 410 ° C. Table 4 shows the evaluation results.
  • the activity was evaluated in the same manner as in Example 6 except that the reaction temperature was 280 ° C. Table 4 shows the evaluation results.
  • the activity was evaluated in the same manner as in Example 6 except that the reaction temperature was 320 ° C. Table 4 shows the evaluation results.
  • wax-2 has a higher gasification rate than that of Example 8 and has a carbon number of 9 to 21 because normal paraffins having 21 or less carbon atoms exceed 30% by mass.
  • the normal paraffin that remained undecomposed remains in the kerosene fraction, resulting in a low isoparaffin ratio.
  • the hydrogenation reaction was carried out at a reaction temperature of 210 ° C, and the activity was evaluated.
  • Table 4 shows the evaluation results.
  • Example 1 4.2 50.3 71.5 Example 2 5.3 80.3 85.8 Example 3 0.0 28.1 72.8 Example 4 1.5 41.9 87.2
  • Example 5 2.0 72.8 98.4
  • Example 6 2 4 57.0 89.8
  • Example 7 6.0 47.6 96 7
  • Example 8 7.8 35.8 74.4 Comparative Example 1 2 6 33.3 59.2 Comparative Example 2 1 1.2 54.2 94.1 Comparative Example 3 23.2 38.5 94.6 Comparative Example 4 10.3 38.4 97.4 Comparative Example 5 0.8 22.6 65.0 Comparative Example 6 43.0 40.8 90.0 Comparative Example 7 14.6 17.1 77.4 Comparative Example 8 9.2 43.8 56.5 Comparative Example 9 13.1 38.0 62.4 Comparative Example 10 9.2 50.0 68.7 (Example 9)
  • Example 5 The oil produced in Example 5 was distilled at a cut range of 225 ° C. to 250 ° C. to evaluate low temperature fluidity. This low-temperature fluidity evaluation is based on the fraction obtained by distilling the oil to be evaluated in the cut range of the specified temperature range using an apparatus conforming to the crude oil distillation method shown in ASTM-D2892. It is a thing. The evaluation results are shown in Table 5.
  • isoparaffins ratio when formed into a 100 wt% material having a carbon number of 9 to 21 in a gas chromatograph was defined by the mass 0/0 isoparaffins therein.
  • the cloud point and the flow point were measured according to JIS K2269.
  • Table 5 also shows the 10% distillation temperature and 90% distillation temperature measured by the distillation test method shown in JIS K2254 for the fraction obtained by distillation in the cut range of the predetermined temperature range.
  • the low temperature fluidity was evaluated in the same manner as in Example 9 except that the distillation cut range was 250 ° C to 275 ° C. Table 5 shows the evaluation results.
  • the low temperature fluidity was evaluated in the same manner as in Example 9 except that the distillation cut range was 275 ° C to 300 ° C. Table 5 shows the evaluation results.
  • the low temperature fluidity was evaluated in the same manner as in Example 9 except that the distillation cut range was 300 ° C to 325 ° C. Table 5 shows the evaluation results.
  • a naphtha fraction, a kerosene fraction, and a light oil fraction are simultaneously generated in addition to the wax.
  • the light fractions produced simultaneously with wax-1 shown in Table 2 and Fig. 1 are hydrotreated with a catalyst with nickel supported on diatomaceous earth to remove olefins and oxygenated compounds, Distillation was performed at a cut range of 225 ° C to 250 ° C to evaluate low-temperature fluidity.
  • Table 5 shows the evaluation results.
  • the low temperature fluidity was evaluated in the same manner as in Comparative Example 11 except that the distillation cut range was 250 ° C to 275 ° C. Table 5 shows the evaluation results.
  • the low temperature fluidity was evaluated in the same manner as Comparative Example 11 except that the cut range of distillation was 275 ° C to 300 ° C. Table 5 shows the evaluation results.
  • the low temperature fluidity was evaluated in the same manner as in Comparative Example 11 except that the distillation cut range was 300 ° C to 325 ° C. Table 5 shows the evaluation results.
  • the heavy wax produced by the FT method is hydrotreated to decompose at a low gasification rate, and at the same time increase the isomerization reaction that occurs, thereby containing a sulfur content.
  • the low temperature fluidity is good, and liquid fuel can be obtained efficiently.

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  • Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'objet de cette invention est de produire un carburant liquide ne possédant pas de contenu de soufre et faisant preuve d'une bonne fluidité à basse température avec une bonne efficacité, par hydrogénation d'une paraffine lourde produite au moyen de la synthèse Fisher-Tropsh (FT) pour décomposer la paraffine tout en diminuant le taux de gazéification et augmentant la réaction d'isomérisation qui se produit simultanément à la décomposition. Plus spécifiquement, l'invention concerne un procédé de production d'un mazout d'hydrocarbures, lequel consiste à soumettre une paraffine lourde produite par synthèse (FT) à un traitement d'hydrogénation, au moyen d'un catalyseur du groupe platine possédant un zéolite ou une silice-alumine en tant que support, dans des conditions de réaction spécifiques sélectionnées en fonction du type de support, pour ainsi décomposer et isomériser la paraffine.
PCT/JP2005/017522 2005-09-22 2005-09-22 Procede permettant de produire un mazout d'hydrocarbures WO2007034556A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
US11/631,793 US20080222945A1 (en) 2005-09-22 2005-09-22 Method for Producing Hydrocarbon Fuel Oil
PCT/JP2005/017522 WO2007034556A1 (fr) 2005-09-22 2005-09-22 Procede permettant de produire un mazout d'hydrocarbures
AU2005335184A AU2005335184B2 (en) 2005-09-22 2005-09-22 Method for producing hydrocarbon fuel oil
EP05785789A EP1927645A4 (fr) 2005-09-22 2005-09-22 Procede permettant de produire un mazout d'hydrocarbures
ZA2007/00432A ZA200700432B (en) 2005-09-22 2007-01-26 Method for producing hydrocarbon fuel oil

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US20090065394A1 (en) * 2007-09-07 2009-03-12 Uop Llc, A Corporation Of The State Of Delaware Hydrocracking process for fabricating distillate from fisher-tropsch waxes
DE102010005704A1 (de) * 2010-01-26 2011-07-28 Süd-Chemie AG, 80333 Verbesserter Katalysator auf Zeolithbasis zur Herstellung von Olefinen und zur Oligomerisierung von Olefinen
CN105548377B (zh) * 2015-12-02 2017-10-17 中国石油天然气股份有限公司 一种判断原油产出层的方法及装置

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JP2002526637A (ja) * 1998-10-05 2002-08-20 セイソル テクノロジー （プロプライエタリー） リミテッド 中間留出物の生産方法及びその方法によって生産された中間留出物
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