CN101429455B - Hydrocracking process for fabricating distillate from fisher-tropsch waxes - Google Patents
Hydrocracking process for fabricating distillate from fisher-tropsch waxes Download PDFInfo
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- CN101429455B CN101429455B CN200810177856.0A CN200810177856A CN101429455B CN 101429455 B CN101429455 B CN 101429455B CN 200810177856 A CN200810177856 A CN 200810177856A CN 101429455 B CN101429455 B CN 101429455B
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- reactor
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- 0 CC1(C)C=C*C1 Chemical compound CC1(C)C=C*C1 0.000 description 3
Classifications
-
- 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
- C10G47/18—Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- 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
- C10G47/20—Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1022—Fischer-Tropsch products
Abstract
A method for obtaining a petroleum distillate product is provided, the method includes subjecting a Fischer-Tropsch wax to a process of hydrocraking carried out at a pressure which is substantially lower that the pressure previously used. A catalyst including a noble metal is used in this method. An apparatus for carrying out the method is also provided.
Description
Technical field
Generally, the present invention relates to hydrocracking technology, more specifically, relate to for by produce the catalytic hydrocracking technique of overhead product based on the wax (for example f-t synthetic wax or gatch) of alkane.
Background technology
Known Fischer-Tropsch synthesis is for the production of the multiple product mixtures that mainly comprises alkane, also comprises multiple alkene and oxidation products.Each compound in this mixture can contain the most nearly 200 carbon, and carbon number is generally 20 to 150, and mean number is 60.This mixture is called " f-t synthetic wax " in the art.Usually, f-t synthetic wax comprises the sulfur-bearing of no more than trace or nitrogenous product or aromatics, and may comprise the oxygenatedchemicals of quite large concentration.
Heavy f-t synthetic wax is a kind of oil plant that is generally used in catalytic hydrocracking technique, is used for obtaining various petroleum chemicalss, light hydrocarbons for example, and the overhead product of kerosene stock and diesel oil for example, petroleum naphtha, and be used for the base oil of lubricating oil, etc.
Hydrocracking is the technique that combines catalytic cracking and the hydrogenation of heavy feed stock, and heavy feed stock cracking under hydrogen exists produces lighter product (Trimethylmethane that for example, is used for raw material for alkylation) and various product for obtaining the high-quality overhead product.This technique is carried out under very harsh high pressure and hot conditions usually, and uses catalyzer.Normally used conventional catalyst comprises dual-function catalyst, it can be used for acid cracking and metal hydride, wherein acid cracking provides by the catalyst component as soft silica-alumina supporter or crystalline zeolite material, metal hydride provides by slightly being dispersed in base metal sulfide on solid support material or the noble metal component of reduction, and described noble metal component comprises for example nickel, tungsten, cobalt or molybdenum, platinum and/or palladium.
This hydrocracking process can be summarized as follows.At first, will mix with fresh and/or hydrogen circulation through pre-warmed raw material, and be sent to reactor, in reactor, sulfur-bearing and nitrogenous compound are removed after changing hydrogen sulfide and ammonia into.Aromatic hydrocarbons is by fractional saturation.Also can carry out limited single-pass conversion in this stage.Then, make this reactor effluent through the hydrocarbon separator.Hydrogen is circulated to raw material, and makes the liquid that is produced by the separation of hydrocarbons device through fractionator.The fractionator column bottom product is mixed with fresh feed and hydrogen stream, and can repeat this process.
Therefore, catalytic hydrocracking is used for transforming the high molecular weight component of non-refinable crude overhead product, and relates to the process of hydrogenation and carbon carbon bond fracture.Simultaneously, contain oxygen, sulphur and/or nitrogen compound if exist, they at least major part be removed, and alkene is generally by saturated and generate alkane.
Although have many advantages, also there are many shortcoming and defect in conventional catalytic hydrocracking.For example, use high pressure to consume mass energy, sometimes dangerous, and require special equipment.Hydrocracking catalyst often due to fouling, poisoning and sedimentation of coke on catalyst substrate and inactivation must adopt special means to avoid this inactivation.
For fear of or the impact that alleviates defects, and in order to improve overhead product selectivity and total process efficiency, need to use better hydrocracking process for the wax (for example f-t synthetic wax or gatch) based on alkane.
Brief summary of the invention
The contriver provides the method that obtains the petroleum distillate product.A kind of method is included in 0 to 20Kg/cm
2Pressure, under the existence of catalyzer, the wax that mainly contains the alkane composition is carried out hydrocracking, described catalyzer comprises one or more metals that selects the group that free precious metal and/or base metal form; With recovery petroleum distillate product.
The wax that carries out hydrocracking can be f-t synthetic wax, can be also gatch.Described catalyzer can be the form of spherical bead.Catalyzer can comprise precious metal, such as palladium, platinum etc.Described catalyzer can also comprise base metal, such as nickel, tungsten, molybdenum etc.Metal load is in amorphous substrate or contain in the substrate of zeolite.
The contriver also provides the system with this wax hydrocracking.A kind of system comprises: be used under catalyzer exists the reactor of wax hydrocracking is produced petroleum distillate and spent catalyst in this reactor, wherein this reactor is suitable for removing continuously described spent catalyst; The continuous catalyst regenerating unit that is connected with reactor, wherein this continuous catalyst regenerating unit is constructed to receive continuously and regenerate described spent catalyst; With the reactor loop that is communicated with reactor fluid, wherein this reactor loop is used for the pressure of reactor is remained on 0 to 20Kg/cm
2
Brief description of drawings
Fig. 1 has schematically shown the system with the wax catalytic hydrocracking of being used for according to one embodiment of the present invention.
Detailed Description Of The Invention
Unless otherwise indicated, hereinafter use following definition:
Term " f-t synthetic wax " refers to comprise the mixture that carbon number is 20 to 150 normal alkane, and this mixture also randomly comprises a part of oxygenatedchemicals, and optional trace naphthenic hydrocarbon and/or the aromatics of comprising.
Term " gatch " refers to by waxy stone paraffin distillate is cooling and that the solvent press filtration produces.
Term " hydrocracking " refers to mainly comprise that with weight molecule catalytic cracking and hydrocracking be the technique of lighter molecule.
Term " catalyzer " is defined as the speed that changes chemical reaction or the material of productive rate, but itself substantially is not consumed or chemical transformation otherwise occurs in this process.
Term " precious metal " refers to opposite with most of base metals, has high corrosion resistance or scale resistance and does not allow diffluent metal.The example includes but not limited to platinum, palladium, gold and silver and tantalum.
Term " hydrocarbon " is defined as the organism that its molecule only is comprised of carbon and hydrogen.
Term " alkane " is defined as the hydrocarbon take saturated carbon chains as feature, and it can be (" naphthenic hydrocarbon ") normal alkane (straight chain), side chain or ring-type, with general formula C
nH
2n+2(for straight or branched alkane) or general formula C
nH
2n(naphthenic hydrocarbon) is described, and wherein n is integer.
Term " alkene " has another name called " alkene ", is defined as the compound that comprises at least one carbon-to-carbon double bond (C=C).
Term " aromatics " is defined as a kind of compound that comprises cyclic conjugated molecular entity, and due to delocalization, the stability of this compound significantly has the stability of the compound of imaginary localization structure (for example Ke Kule structure) greater than those.Aromatics can be monocycle, dicyclo and many rings, and the example of aromatic residue includes but not limited to phenyl, xenyl, naphthyl, dihydro naphthyl, tetrahydro naphthyl, indenyl, 2,3-indanyl, Azulene base, anthryl, phenanthryl, fluorenyl, pyrenyl etc.
Term " carbon ion " is defined as than corresponding free radical and lacks an electronics and with the organic cation of positive charge, this positive charge can but needn't be positioned on carbon atom.
Term " overhead product " is defined as the petroleum distillation product that comprises middle boiling range and low boiling range product, comprises light gas, petroleum naphtha, kerosene, rocket engine fuel, diesel oil and heating oil.Term " No. second overhead product " refers to special overhead product well known in the art.
Term " kerosene " is defined as a kind of petroleum fractions, and it comprises the hydro carbons slightly heavier than the hydrocarbon that exists in gasoline and petroleum naphtha, as C
9-C
16Hydrocarbon, and boiling point under atmospheric pressure is 150 ℃ to 300 ℃.
It is the petroleum fractions of 25 ℃ to 200 ℃ that term " petroleum naphtha " is defined as boiling point under a kind of normal atmosphere, and it was separated before kerosene when petroleum fractionating.
Abbreviation " CCR " refers to term " continuous catalyst regenerating ", is defined as the technique for regeneration of spent catalyst, also the device of fingering row spent catalyst regeneration.In one embodiment of the present of invention, useless spherical hydrocracking catalyst can be regenerated in CCR technique and CCR device.
The petroleum distillate product can pass through to obtain based on the catalytic hydrocracking of the wax (for example f-t synthetic wax or gatch) of alkane.The method of this acquisition petroleum fractions comprises uses wax (for example f-t synthetic wax) as raw material, and make it through hydrocracking process, this process is included in catalyzer reacts wax and gaseous hydrogen under existing, and described catalyzer has for example above-mentioned precious metal that loads on amorphous substrate or zeolite base or the catalyzer of base metal of comprising.This process can be carried out at following selected pressure and the temperature of the selectable rising of those skilled in the art.
Spendable temperature range is between 200 ℃ to 400 ℃.Can select the speed of required hydrogen supply.For example, hydrogen can be with every 1m
3Raw material (being f-t synthetic wax used) corresponding to 170 to 1,700m
3The speed of hydrogen provides, and more specifically, speed is every 1m
3The unconverted wax of wax and/or circulation corresponding to 675 to 1180m
3Hydrogen.
In the past, the typical pressure used of this technique was 60 to 70Kg/cm
2Normally used catalyzer, namely the stability of nickel, tungsten, cobalt or molybdenum base amorphous catalyst is obviously lower under lower pressure.Therefore, than lower pressure, the past is higher pressure more preferably.
Although the way in this past is arranged, we find that hydrocracking can carry out under obviously lower pressure.Be not limited to any particular theory, as described below, the possibility of this pressure decreased hydrocracking process of f-t synthetic wax used due to may be carried out (seeing following reaction icon I-V) by generating alkene and carbon ion.The path for transformation of this wax is dominant on kinetics under lower pressure; In addition, this conversion under low pressure has more selectivity.
Therefore, realization can be 0 to 20Kg/cm based on the hydrocracking of wax (for example f-t synthetic wax or the gatch) conversion of alkane
2Pressure carry out, for example, 7 to 20Kg/cm
2Pressure carry out.The catalyzer that contains precious metal is conducive to hydrocracking process usually under lower pressure.
Multiple catalysts can be used for carrying out above-mentioned hydrocracking process.For example, used catalyst can comprise one or more and loads on the basic spherical suprabasil precious metal that is.More particularly, catalyzer can be that diameter is that 1.5 to 3 millimeters basic is the form of spherical bead.Catalyzer contains unbodied or zeolite base, is the form of shell with precious metal (for example palladium and/or platinum), and described precious metal is incorporated in shell.Perhaps, catalyzer can be based on some base metals, as nickel, tungsten, molybdenum, their combination, etc.
In order to obtain this globule, precious metal can be impregnated in the catalyzer shell.Those skilled in the art can manufacture and design the most suitable method of this catalyzer globule.Use this catalyzer, can improve expense
-The selectivity that the holder synthetic wax transforms, and can use with the amorphous catalyst that comprises base metal (for example cobalt or tungsten) of routine and compare catalyzer more stable under lower pressure.
Can use multiple f-t synthetic wax in method as herein described, include but not limited to from the wax of manufacturers's purchase, such as South Africa Sasol Ltd. (such as Arge FT wax), Houston ExxonMobilCorp., TX etc.The operable f-t synthetic wax of accepting can be comprised of the alkane composition of basic 100 quality %.The alkane composition can comprise one or more straight-chain paraffins, also can comprise at least a branched paraffin.This straight chain and branched paraffin are the main components of this alkane composition.Except straight-chain paraffin and branched paraffin, the alkane composition can further comprise at least some oxygenatedchemicalss.In the f-t synthetic wax that some embodiment uses, can also there be naphthenic hydrocarbon, alkyl aromatic compound and many alkyl aromatic compounds of trace.
Representational hydrocracking process is schematically illustrated in following reaction icon I-V, the conversion process of the f-t synthetic wax that substantially is comprised of n-paraffin with explanation in more detail.Can find out, the hydrocracking mechanism of n-paraffin comprises formation and the hydrogenation of unsettled carbon ion intermediate.
More specifically, at first, due to the existence of metal in catalyzer, the n-paraffin dehydrogenation forms alkene, as shown in reaction icon I:
Then, the rapid alpha proton reaction with being present in acidity of catalyst point of the alkene that forms as mentioned above, then reset and form carbon ion (reaction icon II):
The carbon ion that forms as shown in reaction icon II itself is unsettled, and in order to become more stable, isomerization at once forms different carbon ions.Simultaneously, initial carbon ion forms another positively charged ion and alkene in β position generation cracking.Along with carbon ion continues isomerization and cracking, secondary cracking has occured.These crackings and isomerization reaction are schematically illustrated in reaction icon III:
Last in process, the formerly further conversion of product experience that obtains of stage, for example reaction of carbon ion and alkene (reaction icon IV), then hydrogenation (reaction icon V), formation alkane (for example Trimethylmethane, as shown shown in V):
As mentioned above, the f-t synthetic wax that is used for transforming can comprise the naphthenic hydrocarbon of at least one tittle except straight chain and/or branched paraffin.If this naphthenic hydrocarbon is present in wax, except the conversion process of the n-paraffin that shows by reaction icon I-V, hydrocracking process also comprises the conversion of naphthenic hydrocarbon.A kind of transformation mechanism of naphthenic hydrocarbon is schematically illustrated in reaction icon VI-X.The hydrocracking mechanism of naphthenic hydrocarbon comprises formation and the hydrogenation of unsettled carbon ion intermediate.
Form naphthenic hydrocarbon hydrocracking process in the alkane composition of wax for general description, observed methylcyclopentane and the height ratio of hexanaphthene in the isocrackate of naphthenic hydrocarbon, usually over thermodynamic(al)equilibrium.Main alkane product is Trimethylmethane.
More particularly, can be found out by reaction icon VI-X, the naphthenic hydrocarbon hydrocracking generally comprises dissociative reaction, and wherein some alkyl is optionally removed, and the integrity of saturated rings itself is kept.Relate to the hydrocracking mechanism of naphthenic hydrocarbon with consistent about the description of straight-chain paraffin hydrocracking mechanism before.In order to illustrate, reaction icon VI-X uses 1,2,3,4-tetramethyl-ring hexane as initial naphthenic hydrocarbon.
As follows, at first formed alkene (namely 1,2 as shown in reaction icon VI, 3,6-tetramethyl--1-tetrahydrobenzene), then in the naphthenic hydrocarbon hydrocracking process by this alkene intermediate Formed ion, then isomerization forms more stable carbon ion, as shown in reaction icon VII:
Then the carbon ion 1 that forms shown in reaction icon VII carries out further isomerization, form more stable carbon ion 3 by intermediate product carbon ion 2, then cycloolefin (being 1-methyl isophthalic acid-cyclopentenes) and another carbon ion 4 are produced in carbon ion 3 crackings, as shown in reaction icon VIII:
In the final stage of this process, the cycloolefin that forms shown in reaction icon VIII becomes saturated by carrying out hydrogenation, and generation naphthenic hydrocarbon (that is, in this case, the 1-methylcyclopentane) (as shown in reaction icon IX).The carbon ion that forms as shown in reaction icon VIII loses proton by hydride transfer, the generation n-paraffin (that is, in this case, Trimethylmethane) (as shown in reaction icon X):
As mentioned above, f-t synthetic wax of the present invention is generally without aromatics.Yet even there is in some embodiments aromatics (for example trace), they also can transform by catalytic hydrocracking.The hydrocracking of alkyl aromatic compound may relate to many reactions, wherein particularly including isomerization, dealkylation, division, cyclisation and alkyl migration.
The principal reaction that the alkyl aromatic compound hydrocracking relates to comprises the transfer of dealkylation and alkyl, especially for form the various dimethylbenzene products of heavy aromatics through quick transalkylation.Cyclization generally only has and enough just occurs when forming dicyclic compound greatly when alkyl group side chain.
The reaction mechanism that relates in many alkyl aromatic compounds hydrocracking process and the typical paring reaction of above-mentioned naphthenic hydrocarbon are similar, and minimum ring scission and methanogenesis expection can produce the Trimethylmethane of high yield.
The hydrocracking of Ppolynuclear aromatic relates to very complicated mechanism, comprises the transfer of the butyl that partial hydrogenation and ring scission form, and comprises that further cyclisation forms more senior ring intermediate, then cracking.Polynuclear aromatics also can carry out condensation, forms the polynuclear aromatics with a plurality of condensed ring.
No matter whether wax has special composition, and no matter whether has naphthenic hydrocarbon and various aromatics, and the final product of the catalytic hydrocracking of above-mentioned any f-t synthetic wax is all overhead product.As mentioned above, overhead product generally comprises the product of low boiling range and middle boiling range, comprises light gas, petroleum naphtha, kerosene, rocket engine fuel, diesel oil and heating oil, comprises overhead product No. second.
Ratio between the concrete composition of overhead product and each component that wherein comprises depends on character and concrete composition of wax used especially.In an example, 80 quality % to 90 quality % of overhead product comprise the composition that is comprised of kerosene and diesel oil.
Multiple systems and device can be used for carrying out the hydrocracking process of the wax (for example f-t synthetic wax or gatch) based on alkane.Under the lower pressure of reaction system, a certain amount of coke may form, and deposition and agglomeration are on the surface of catalyzer.This can cause the minimizing of metal effective surface area, and therefore makes the catalyzer total efficiency descend.Therefore, consider above-mentioned factor, need to select suitable system or device.For example, can use the CCR system of following general description.
Correspondingly, the applicant provides the continuous catalyst regenerating system.This CCR system is used for the spent catalyst that basic continous removes reactor, then makes its regeneration and with the live catalyst Returning reactor.This CCR system helps to overcome fixed bed process to the stability limit of catalyzer, and operation can be carried out under the lower reactor pressure in the above scope.Equally as noted above, use lower pressure to be conducive to the hydrocracking of f-t synthetic wax on kinetics, and the selectivity to rocket engine fuel and diesel oil is provided preferably.
A representative enforcement as shown in Figure 1 of this low pressure hydrocracking system, and be described below.System 100 comprises reactor 1, in this reactor, carries out the hydrocracking of wax under hydrogen and catalyzer existence.Before adding wax W in reactor 1, the wax that will be about to hydrocracking with heat exchanger network 2 is heated to the temperature that needs, namely 200 ℃ to 425 ℃.In the wax that the opening at 3 places will heat adds reactor 1.
Can randomly with hydrogen heating in same heat exchanger network 2 separately, then add reactor 1 as the air-flow that is independent of the wax stream that has heated.Perhaps, as shown in Figure 1, can with hydrogen and wax W and randomly with the unconverted wax RW pre-mixing that is recycled, then heat this mixture, and the mixture that will heat adds reactor 1 as combination raw materials, also add by the opening at 3 places.Hydrogen enters with the speed of above-mentioned discussion, for example every 1m
3The unconverted wax of wax and/or circulation corresponding to 675 to 1,180m
3Hydrogen.
Response circuit unit 4 is the equipment that is connected with reactor 1, the pressure that needs in its generation and maintenance reactor 1.As mentioned above, pressure can remain on 0 to 20Kg/cm
2, be generally 7 to 20Kg/cm
2The catalyzer (not shown) can add reactor 1 by opening 5, when catalyzer with may remain on above-mentioned temperature required and pressure under wax/when the hydrogen raw material contacted, hydrocracking process began.
Above-mentioned hydrocracking process has produced reaction effluent and spent catalyst.As mentioned above, at the stress level that the present invention uses, coke may form and be deposited on catalyst surface.The agglomeration of this coke is not wish event, can cause the reduction of catalyst efficiency.
Hydrocracking system 100 is used for alleviating this negative impact.Correspondingly, remove spent catalyst opening 6 basic continous that can be by reactor 1, and be sent to that basic continous is accepted and the continuous catalyst regenerating unit of regeneration of spent catalyst 7 in.During spent catalyst that then, will remove from reactor 1 like this by opening 5, regeneration in continuous catalyst regenerating unit 7 turns back to reactor 1.
As mentioned above, reactor 1 produces petroleum distillate, and then this overhead product stands further processing.More particularly, reaction effluent leads to heat exchanger network 9 by the opening 8 of reactor 1, and reaction effluent is cooled at this temperature that is suitable for back gas/liquid sepn process most.When effluent becomes enough cold, enter gas/liquid separation 10, carry out separating of hydrogen, hydrocarbon and water at this.Sepn process is carried out according to standard program and rules, and can change as required and adjust.
After sepn process, hydrocarbon stream 11 is sent to fractionator device (not shown), separates and reclaim the various cuts of hydrocarbon at this by technology and equipment known in the art.To mix with the hydrogen of the additional content that adds by logistics 12 from the hydrogen that separator 10 reclaims, to replenish the hydrogen that consumes in hydrocracking.Then with hydrogen stream 13 circulations that mix, as mentioned above individually or with the wax pre-mixing after send heat exchanger network 2 back to.Then, whole hydrocracking process can repeat.
Although with reference to above-mentioned reaction and structrual description the inventive method and system, modifications and variations are considered to fall in the essence of the present invention and scope that claims limit.
Claims (10)
1. method that obtains the petroleum distillate product comprises:
0 to 20Kg/cm
2Pressure and the temperature of 200-425 ℃ under, under the existence of catalyzer, the wax that mainly contains the alkane composition is carried out hydrocracking, described catalyzer comprises the freely metal of the group that forms of at least a precious metal and at least a base metal of choosing; Remove continuously the spent catalyst in hydrocracking reactor, then make its regeneration and live catalyst is returned to hydrocracking reactor in the continuous catalyst regenerating system, wherein catalyzer continuous circulation between reactor and regeneration system rapidly; With
Reclaim the petroleum distillate product.
2. the process of claim 1 wherein that described wax is f-t synthetic wax.
3. the process of claim 1 wherein that described alkane composition comprises at least a straight-chain paraffin and at least a branched paraffin, and further randomly comprise at least a naphthenic hydrocarbon.
4. the process of claim 1 wherein that hydrocracking is being 7 to 20Kg/cm
2Pressure carry out.
5. the process of claim 1 wherein that described catalyzer comprises the basic spherical metallic globule that is.
6. the process of claim 1 wherein that described precious metal selects the group of free palladium, platinum and combination composition thereof.
7. the process of claim 1 wherein that the petroleum distillate product comprises lighting end, liquefied petroleum gas (LPG), petroleum naphtha, kerosene or diesel oil.
8. the method for claim 7, wherein the petroleum distillate of 80 quality % to 90 quality % comprises the composition that is comprised of kerosene and diesel oil.
9. for the device (100) of the wax hydrocracking that will mainly contain the alkane composition, this device comprises:
(a) be used under catalyzer exists the reactor of wax hydrocracking, this reactor produces spent catalyst and petroleum distillate, and wherein this reactor is suitable for removing continuously described spent catalyst;
(b) the continuous catalyst regenerating unit that is connected with reactor, wherein this continuous catalyst regenerating unit is constructed to receive continuously and regenerate described spent catalyst; With
(c) reactor loop (4) that is communicated with reactor (1) fluid, wherein reactor loop (4) is used for the pressure of reactor (1) is remained on 0 to 20Kg/cm
2
10. the device of claim 9 (100), wherein the petroleum distillate that produces in reactor (1) of 80 quality % to 90 quality % comprises the composition that is comprised of kerosene and diesel oil.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US11/899,710 US20090065394A1 (en) | 2007-09-07 | 2007-09-07 | Hydrocracking process for fabricating distillate from fisher-tropsch waxes |
| US11/899,710 | 2007-09-07 |
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| Publication Number | Publication Date |
|---|---|
| CN101429455A CN101429455A (en) | 2009-05-13 |
| CN101429455B true CN101429455B (en) | 2013-06-19 |
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| CN200810177856.0A Expired - Fee Related CN101429455B (en) | 2007-09-07 | 2008-09-05 | Hydrocracking process for fabricating distillate from fisher-tropsch waxes |
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| US (1) | US20090065394A1 (en) |
| CN (1) | CN101429455B (en) |
| AU (1) | AU2008207434B2 (en) |
| ZA (1) | ZA200807670B (en) |
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| GB201811914D0 (en) * | 2018-07-20 | 2018-09-05 | Univ Cape Town | Low pressure hydrocracking process for the production of a high yield of middle distillates from a high boiling hydrocarbon feedstock |
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-
2007
- 2007-09-07 US US11/899,710 patent/US20090065394A1/en not_active Abandoned
-
2008
- 2008-08-21 AU AU2008207434A patent/AU2008207434B2/en not_active Ceased
- 2008-09-05 CN CN200810177856.0A patent/CN101429455B/en not_active Expired - Fee Related
- 2008-09-05 ZA ZA200807670A patent/ZA200807670B/en unknown
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4684756A (en) * | 1986-05-01 | 1987-08-04 | Mobil Oil Corporation | Process for upgrading wax from Fischer-Tropsch synthesis |
| CN1033831A (en) * | 1987-11-27 | 1989-07-12 | 国际壳牌研究有限公司 | Heavy oil cracking process |
| CN1089641A (en) * | 1992-08-20 | 1994-07-20 | 史东及韦伯斯特工程公司 | The catalyst cracking method that contains the paraffin-rich feedstock of high and low Kang Laxun carbon residue component |
| CN1836028A (en) * | 2003-06-19 | 2006-09-20 | 切夫里昂美国公司 | Fuels and lubricants using layered bed catalysts in hydrotreating waxy feeds, including fischer-tropsch wax |
Also Published As
| Publication number | Publication date |
|---|---|
| ZA200807670B (en) | 2009-12-30 |
| CN101429455A (en) | 2009-05-13 |
| AU2008207434A1 (en) | 2009-03-26 |
| AU2008207434B2 (en) | 2010-10-21 |
| US20090065394A1 (en) | 2009-03-12 |
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