|Veröffentlichungsdatum||28. Aug. 1973|
|Eingetragen||13. Okt. 1971|
|Prioritätsdatum||13. Okt. 1971|
|Veröffentlichungsnummer||US 3755144 A, US 3755144A, US-A-3755144, US3755144 A, US3755144A|
|Ursprünglich Bevollmächtigter||Universal Oil Prod Co|
|Zitat exportieren||BiBTeX, EndNote, RefMan|
|Patentzitate (3), Referenziert von (40), Klassifizierungen (14), Juristische Ereignisse (2)|
|Externe Links: USPTO, USPTO-Zuordnung, Espacenet|
United States Patent [1 1 Asselin HYDROCARBON ISOMERIZATION AND SEPARATION PROCESS  Inventor: George F. Asselin, Mt. Prospect, I11.
 Assignee: Universal Oil Products Company, Des Plaines, 111.
[22} Filed: Oct. 13, 1971  Appl. No.: 188,792
Make up Hydrogen Pen ans /Hexane Fee a lsomen'za t/on Reactor High Pressure Separa/ar [451 Aug. 28, 1973 Primary Examiner-Delbert E. Gantz Assistant ExaminerS. Berger Att0rney.1ames R. Hoats'omJr. et a1.
' [57 ABSTRACT A process for isomerizing and separating a low octane C -C hydrocarbon charge stock'to provide a branched hydrocarbons product in which the charge stock is contacted with an isomerization catalyst in an isomerization zone, the effluent from the isomerization zone is separated, in a sorption zone employing a molecular sieve sorbent, into a branched hydrocarbons stream and a normal hydrocarbons stream; the branched hydrocarbons stream is fractionated, and a methylpentanes-free stream of branched hydrocarbons is recovered from the fractionation step as the product of the process.
5 Claims, 1 Drawing Figtire L ighr Gases /sapenfane D/mef/zy/bu/ane Producf Ma/ecu/ar S/e v19 Sepamr/on Zane HYDROCARBON ISOMERIZATION AND SEPARATION PROCESS BACKGROUND This invention relates to a process for isomerizing and separating a lower octane C C hydrocarbon charge stock containing normal paraffinic hydrocarbons to provide higher octane products. In one aspect, this invention relates to a hydrocarbon isomerization process utilizing fractionation and a solid sorbent to separate branched chain C and C hydrocarbons from normal C and C, hydrocarbons.
More specifically, this invention relates to a process for isomerizing and separating an isomerizable hydrocarbon charge stock containing hydrocarbons having from about five to about six carbon atoms per molecule to provide a branched hydrocarbons product, which process comprises: contacting said charge stock with an isomerization catalyst in an isomerization zone at isomerization conditions; separating the effluent from said isomerization zone in a sorption zone, employing a solid sorbent, to provide a normal hydrocarbons stream and a branched hydrocarbons stream; and, fractionating said branched hydrocarbons stream to provide a methylpentanes stream and a products stream and withdrawing said products stream as said branched chain hydrocarbons product.
Hydrocarbons comprising primarily pentanes and hexanes, such as those available in petroleum refineries, for example, as straight-run fractions of crude oil or as raffinate from reforming processes, represent a substantial potential source of high octane motor fuel components. However, these C -C fractions normally have an unleaded research octane rating of. only about 65-70, and the octane rating of such fractions is raised to only about 85-90 by the addition of 3 ml. of an alkyl lead compound per gallon of hydrocarbon. Present premium fuels for automobile engines must have an octane rating of about 100. One method of upgrading these C -C fractions, to improve their utility as motor fuel components, is by eliminating low octane normal paraffins from them by isomerizing the normal paraffms to higher octane branched isomers. It is well known that the more highly branched hydrocarbons such as isopentane and the dimethylbutanes possess a higher unleaded octane than do nonnal pentane and normal hexane. For example, isopentane and 2,2-dimethylbutane each have an unleaded research octane of about 93, while n-pentane and n-hexane have unleaded octane ratings of about 62 and 30 respectively. By eliminating at least a part of the n-pentane and n-hexane from a typical C -C refinery fraction, the octane rating of the fraction can, therefore, be substantially improved. With the advent of a strong demand for unleaded motor fuel for automobiles, there is an even more pressing need for motor fuel components which have a high octane rating without the addition of alkyl leads. It is essential to upgrade the available C -C, fractions if they are to be useful in unleaded motor fuels. The process herein disclosed provides a novel and economically superior method for producing high octane products from these low octane petroleum fractions.
lsomerization of hydrocarbons is well known in the petroleum refining art. Generally, hydrocarbon stocks have been isomerized and fractionated to recover valuable components. The combination of isomerization with fractionation and molecular sieve separation disclosed in the process of this invention makes possible a sharper separation, smaller isomerization reactor requirement and higher quality product than is generally available from current commercial processes.
SUMMARY 7 It is an object of this invention to provide a process for isomerizing and separating a lower octane pentanelhexane hydrocarbon fraction to produce a higher octane hydrocarbon product. Another object of this invention is to provide a hydrocarbon isomerization process utilizing a solid molecular sieve sorbent to separate normal hydrocarbons from branched and cyclic hydrocarbons to produce a higher octane, more highly branched product from a lower octane, less branched hydrocarbon fraction.
Therefore, in an embodiment, this invention relates to a process for isomerizing and separating an isomerizable hydrocarbon charge stock containing hydrocarbons having from about five to about six carbon atoms per molecule to provide a branched hydrocarbons product, which process comprises: (a) containing said charge stock with an isomerization catalyst in an isomerization zone at isomerization conditions; (b) separating the effluent from said isomerization zone in a sorption zone, employing a solid sorbent, to provide normal hydrocarbons stream and a branched hydrocarbons stream; and, (c) fractionating said branched hydrocarbons stream to provide a methylpentanes stream and a products stream and withdrawing said products stream as said branched chain hydrocarbons product.
Further objects and embodiments of the process of this invention will be more readily apparent from the following description of the accompanying drawing and detailed description of the invention.
DESCRIPTION OF THE DRAWING An understanding of the process of this invention may be aided by referring to the accompanying drawing which represents a schematic diagram of an embodiment of the process of this invention.
Referring to the drawing, hydrocarbon charge stock, comprising primarily pentanes and hexanes, is introduced through conduit 1 and passed through conduit 2 to heat exchanger 3 wherein the charge stock is heated in indirect heat exchange with effluent from isomerization zone 7. Hydrogen is commingled with the charge stock in conduit 2. The partially heated charge stock is withdrawn from exchanger 3 and passed through conduit 4 to heater 5 wherein the charge stock is further heated to' the desired temperature for isomerization conditions. The heated charge stock is passed from heater 5 via conduit 6 to isomerization reactor 7. Isomerization reactor 7 contains a fixed bed of isomerization catalyst. The hydrocarbons charged to reactor 7 are passed over the fixed bed of catalyst, maintained at a temperature and pressure sufiicient that at least a part of the charged hydrocarbons are isomerized, and withdrawn from reactor 7 through conduit 8. The isomerization reactor effluent is passed from conduit 8 into heat exchanger 3 in indirect heat exchange with fresh feed stock as described above. Cooled reactor effluent is withdrawn from heat exchanger 3 and passed through conduit 9 to high pressure separator 10, wherein the effluent forms a liquid phase and a hydrogen-rich gaseous phase. The hydrogen-rich gaseous phase is withdrawn from separator 10 through conduit 11. Make up hydrogen is charged to conduit 11 by way of conduit 12 as needed, and the combined hydrogen stream continues through conduit 11 to conduit 2 where the hydrogen is commingled with fresh charge stock as described above. The liquid phase in high pressure separator is withdrawn through conduit 13 and passed to stabilizer 14. In stabilizer 14, any light gases, such as butanes, propane, ethane and methane, as well as any other normally gaseous materials such as hydrogen halides, are separated from C,,/C hydrocarbons, passed overhead in conduit 15 and withdrawn from the process. The C .,/C hydrocarbons in stabilizer 14 are withdrawn and passed through conduit 16 to molecular sieve separation zone 17. In separation zone 17, normal C and C hydrocarbons are separated from branched chain and cyclic C and C hydrocarbons. The normal hydrocarbons are withdrawn via conduit 18 and passed therethrough to conduit 2, wherein they are commingled with fresh charge stock from conduit 1 and hydrogen from conduit 11. The branched and cyclic hydrocarbons in molecular sieve separation zone 17 are withdrawn through conduit 19 and passed to deisohexanizer 20, which comprises a fractionation vessel. In deisohexanizer 20, isopentane, dimethylbutanes and some methylpentanes are withdrawn overhead in the vapor phase and recovered through conduit 21 as the product of the process. A bottoms stream comprising primarily methylcyclopentane, and cyclohexane is recovered from deisohexanizer and withdrawn from the process through conduit 23. A side cut stream of DETAILED DESCRIPTION OF INVENTION The hydrocarbon charge stocks which are suitable for use in the process of this invention include straight and branched chain saturated C and C hydrocarbons and mixtures thereof. Typical of the suitable charge stocks is a C /C fraction derived from the fractional distillation of petroleum crude oil. Such a fraction may contain lighter and heavier components such as butanes and heptanes and may contain cyclic and aromatic compounds such as cyclopentane, cyclohexane, benzene, etc. Typically, such straight-run fractions are contaminated by sulfur compounds and water, and it is desirable to eliminate such contaminants before a charge stock is utilized in this process. Generally, the charge stock should comprise less than about 10 wt. percent of C-, and heavier hydrocarbons, although this requirement is not essential to the operation of the process. It is also desirable to limit the aromatics content of the charge stock to less than about 10 percent of the feed, by weight, primarily because the aromatics have higher octane rating than the products formed from them in the isomerization reaction. Suitable charge stocks may contain unsaturated hydrocarbons, such as pentenes, hexenes, pentadienes, etc. When the charge stock is obtained from the raffinate of a hydrocarbon reforming process, it will usually contain several wt. percent of such unsaturates. Such a feed stock is suitable for use in the present process. It will be obvious to one skilled in the art that the present process is basically applicable to C JC charge stocks containing a greater-than-equilibrium fraction of normal pentane and normal hexane, since the octane rating improvement resulting from processing stocks having a high branched chain, cyclic and aromatic hydrocarbons content would be negligible. A typical straight run C,,/C feed stock, suitable for use as a feed in the present process, could comprise, by weight, 20 percent isopentane, 30 percent n-pentane, 1 percent cyclopentane, 2 percent dimethylbutanes, 19 percent methylpentanes, 19 percent n-hexane, 5 percent methylcyclopentane, 1 percent benzene and 3 percent heavier hydrocarbons.
Isomerization catalysts suitable for use in the process of this invention include all catalysts capable of isomerizing normal paraffinic hydrocarbons to produce branched chain parafiinic hydrocarbons. Friedel-Crafts metal halides, e.g., aluminum chloride, are well known as isomerization catalysts. These catalysts may be used as such or combined with other materials such as hy drogen halides. Typical catalysts of this type, suitable for use in the present process, are aluminum chloride with hydrogen chloride added as a promoter and antimony chloride having aluminum chloride dissolved therein. Friedel-Crafts metal halides may be utilized suitably in combination with substantially inert supporting materials. Another suitable type of isomerization catalyst which may be used in this process is a composite of a metal from Group VIII of the Periodic Table with a solid support. The platinum group metals, and platinum in particular, are preferred for use as components of such a catalyst in this process. Solid supports which are suitable for a catalyst of this type include silica, alumina, magnesia, zirconia, chromia, titania, bauxite, kaolin, Kieselguhr, vanadium oxide, boron oxide, etc., and combinations thereof. Catalysts comprising a Group VIII metal component and a solid support may be utilized with promoting components such as hydrogen halides, organic halides, etc. For example, the composite may be treated, before or during use, with hydrogen halide or with an organic halide such as carbon tetrachloride, chloroform, etc. A hydrogen halide or organic halide may be admixed with the hydrocarbons to be isomerized in a continuous operation whereby a definite concentration of halide is provided in the feed to the isomerization zone. A similar type of catalyst suitable for use in the process of this invention comprises a Group VIII metal component and one or more combined halogen components on a solid support. For example, a catalyst comprising, by weight, about 0.01 to about 2.0 percent platinum, about 0.01 to about 8 percent chlorine, about 0.01 to about 8 percent fluorine on a silica-alumina support is suitable for use in this process. One isomerization catalyst preferred for use in the present process is described in U. S. Pat. Ser. No. 2,999,074. This preferred catalyst comprises a calcined and reduced composite of a refractory oxide containing chemically combined hydroxyl groups and from about 0.01 percent to about 2 percent by weight of a platinum group metal, said calcined composite being impregnated with from about 10 percent to about percent by weight of an anhydrous Frie del-Crafts metal halide in which the halogen is selected from chlorine and bromine and said hydroxyl groups having been reacted with the metal halide in a reaction resulting in the elimination from the composite of at least 0.5 mole but not more than 2.0 moles of hydrogen Various other suitable catalysts have been disclosed in prior art. For example, catalytic composites containing more than one metallic component, e.g., a platinum group metal and a metal from Group VIB or Group IB of the Periodic Table have been found to'be useful as isomerization catalysts. Certain forms of crystalline aluminosilicates have also been found to act as isomerization catalysts, and may suitably be used as such in the process of this invention. Such catalytic composits commonly require isomerization conditions very similar to those discussed below in connection with the use of the preferred catalysts, so that the isomerization conditions discussed are generally applicable to them.
Another catalyst preferred for use in the process of this invention comprises a halogen component on a solid support comprising an alumina matrix having suspended therein a finely divided crystalline aluminosilicate and a Group VIII or Group VIB metallic component. Such a catalyst may be prepared by distributing finely divided crystalline aluminosilicate particles throughout an aluminum hydroxyl halide sol, to form a mixture, gelling the resulting mixture to form substantially spherical hydrogel particles, aging, washing and calcining the particles, and adding platinum thereto. The crystalline aluminosilicate, preferably mordenite, should comprise from about 2 percent to about percent by weight, of the support, and the platinum component should comprise from about 0.05 percent to about 2.0 percent of the final weight of the catalyst.
In using the preferred isomerization catalysts, it is desirable to eliminate sulfur and water from the feed stock before it is contacted with the catalyst. Typically, C,,-C, fractions available for isomerization have been desulfurized by prior processing, but, if necessary, sulfur may be removed by contacting the feed stock with hydrogen at elevated temperatures and pressures, whereby the sulfur is converted to hydrogen sulfide and is easily separated from the heavier hydrocarbons. Various methods for eliminating water from the feed to the process are known including pre-fractionation and molecular sieve drying. The latter method is preferred. Dual function isomerization catalysts such as the preferred catalysts require that hydrogen gas be present in the isomerization zone. It is necessary to eliminate water from fresh hydrogen which will enter the isomerization zone. It is preferred that the fresh hydrogen be dried using molecular sieves.
The isomerization step in the process of this invention may be performed in a batch reaction scheme or a continuous reaction scheme. The particular manner in which the isomerization step is performed will depend, in part, on the choice of isomerization catalyst. Generally, a continuous operation is preferred. When a batch operation is utilized, a quantity of the charge stock is placed in an appropriate vessel and contacted therein with an isomerization catalyst. The stock is maintained at a particular temperature and pressure for a predetermined length of time and then separated from the catalyst and recovered. In a continuous scheme, the catalyst may be employed as a fixed bed in a suitable reaction vessel and the hydrocarbon stock passed across the bed continuously. In another suitable method, the catalyst may be employed in a moving bed scheme, or a fluidized bed operation in which catalyst and hydrocarbons are continuously contacted, either cocurrently or countercurrently, and separated. It is preferred that a fixed bed of catalyst be maintained iii the reaction zone.
Isomerization conditions include a temperature in the range from about 0F. to about 1,200F. and a pressure in the range from 1 atmosphere to about 200 atmospheres or more. Preferred isomerization conditions include a temperature of from about 200F. to about 800F. and a pressure of from about 10 atmospheres to about atmospheres. It is contemplated that gases such as helium, nitrogen, argon, etc.,may be charged to the isomerization zone if desired. In an embodiment of the present process using one of the preferred catalysts, a gas comprising hydrogen is passed to the iSOrfi-J erization zone and commingled with the hydrocarbon to be isomerized. Hydrogen should be charged at a rate in the range from about 0.1 to about 10 moles per mole of charged hydrocarbons. Hydrocarbons, either in the gaseous or the liquid phase, are passed through the isomerization zone at a liquid hourly space velocity (volume of hydrocarbons charged per hour divided by the volume of catalyst in the isomerization zone) of from about 0.1 to about 20 or more.
In using the preferred isomerization" catalysts, itis: preferred that an organic halide-be addedtothe? feed to the isomerization zone. This-procedurere'sults in the production of some hydrogen halid'einthe' isoni'eriza tion zone, and beneficially affects the activity of the catalyst. In embodiments of the presentp'roc'ess utilizing hydrogen, organic halide, etc., in the-isomerization" step, it is necessary to provide equipmentforseparating hydrogen and other light gases from the heavier hydro;-
carbons. Various methods for making such aseparatio'ii are well known. One suitable metIiOdempIQystWo's'epQ aration zones, the first zone operatingathigh' pressure and the second .at a lowerpr'essure. In" the first,- highpressure separation zonea gaseous stie'an'i corrfpi'isin'g primarily hydrogenis separated. The-hydrogen recov-' ered from the high pressure separation mneisrecirculated to the isomerization zone. In the second, lower" pressure separationzone, any C, and lighter'h'y'dro'car bons, hydrogen halides, etc., are separated from" the heavier hydrocarbons comprising primarily C and C saturates.
The isomerization zone effluent C, and heavier hydrocarbons are charged to a sorption zone, wherein normal hydrocarbons are separated from branched chain and cyclic hydrocarbons. The separation of nor crystalline aluminosilicate is a Type A zeolite manufac tured by the-Linde'Di'vision of Union CarbidCoifii,
particularly the-5A zeolites of this'typei' Zeolites 'rnay be characterized ashaving a porous structure,- with the pores being interconnected by smaller diameter pore? openings. When the pore openings are ab'out 5-Ainidi ameter, normal hydrocarbons can enter"the'-pores,'but
cyclic and branched chain hydrocarbon's'cannot enter because of their larger molecular diameters. When-a;- mixture of normal, branched and cyclic hydrocarbons 11 is contacted with a zeolite of this type, the zoliteacts as a molecular sieve admitting normal hydrocarbons to the pores but excluding branched and cyclichydrocar bons. The branched and cyclic hydrocarbons are then withdrawn from contact with the zeolite relatively free of normal hydrocarbons, and the relatively branched chain-free normal hydrocarbons are subsequently desorbed from the zeolite.
The zeolite crystal structure consists of threedimensional networks of the fundamental units, which are silicon-centers SiO, and aluminum-centered A10 tetrahedra. These units are interconnected by sharing apical oxygen atoms. To preserve electrochemical neutrality, the A10 tetrahedra are associated with a cation such as an alkaline earth or alkali metal ion. Both natural and synthetic zeolites may be utilized as a sorbent in the process of this invention, including those in which A10 tethedra are bonded with alkali and alkaline earth metal cations, as well as those where the cations have been replaced by ion exchange or treatment with acids or bases. The zeolite may be composited with binding materials such as refractory inorganic oxides, preferably those inert with respect to catalytic and molecular sieve properties. The sorbent may be employed in a batch, moving bed, fixed bed or other type of operation. For example, one suitable type'of separation technique, employing a simulated moving bed operation, is described in U. S. Pat. No. 2,985,589.
In general, the use of a desorbent is required to recover the adsorbed normal hydrocarbons from a molecular sieve sorbent. Desorbents preferred for use in the process of this invention include those which can be easily separated from normal hexane. in operations making use of a desorbent, the preferentially adsorbed feed component, in this case normal pentanes and hexanes, and the desorbent are removed from the solid sorbent in admixture. Easy separation of the normal hydrocarbons from the desorbent is, therefore, essential to the economy of the operation. One preferred type of desorbent is a normal hydrocarbon having either a higher or lower boiling point than normal hexane or normal pentane, respectively, such as n-octane or nbutane. Another preferred type of desorbent is a mixture of a normal hydrocarbon and a branched hydrocarbon both having lower or higher boiling points than n-pentane or n-hexane such as a mixture of n-butane and isobutane,- or a mixture of n-octane and isooctanes. Another method of desorbing the normal hydrocarbons from the solid sorbent is by adsorbing the normal hydrocarbons at a higher pressure, and then desorbing them utilizing a lower pressure to produce a vacuum effect. The normal hydrocarbons may also be desorbed by heating the sorbent, vaporizing the adsorbed normal hydrocarbons and withdrawing them. A desorbent may also be employed in operations utilizing vacuum or heating desorption. For example, a gas such as hydrogen, nitrogen, argon, etc., may be utilized as a desorbent. The desorbent and normal hydrocarbons are subsequently separated, for example, by fractionation when a hydrocarbon desorbent is utilized, or by flash separation when a gas is used. A stream of relatively pure normal hydrocarbons is thereby produced and the desorbent recovered may be recycled for further use.
In the present process, a raffinate of non-adsorbed hydrocarbons, comprising branched and cyclic C, and C, saturates is withdrawn from contact with the sorbent and passed out of the sorption zone, leaving the adsorbed normal pentane and normal hexane. The adsorbed hydrocarbons are subsequently desorbed, preferably by employing a desorbent. The normal pentane and normal hexane are then separated from the'desorbent, if any, and withdrawn from the sorption zone. The stream of normal hydrocarbons so formed is recycled to the isomerization step.
The stream of branched and cyclic hydrocarbons recovered as the sorption zone raffinate is further separated by fractionation. It is desirable to recover a branched product comprising isopentane and the maximum fraction possible to dimethylbutanes from this fractionation step, while retaining a recycle stream of as large a fraction of methylpentanes as possible. The
very small difference in boiling point between 2,3- t.
dimethylbutane and 2-methylpentane makes a complete separation of these isomers by fractionation virtually impossible. Depending upon the particular embodiment of this invention, the product of the process may comprise substantially methylpentane-free isopentane and 2,2-dimethylbutane, or the product may comprise isopentane, 2,2- and 2,3-dimethylbutane with a fraction of methylpentane. By variations in fractionation conditions well known to those skilled in the art, the amount of methylpentanes taken overhead with the desired products may be varied over a wide range, and the product of the process may be varied in octane rating accordingly. For example, if fractionation conditions are imposed which provide an overhead product consisting essentially of isopentane and 2,2- dimethylbutane, the product will possess an unleaded research octane of about 93. If much of the high octane 2,3-dimethylbutane is also recovered overhead, it is also necessary to take overhead some methylpentane. In this embodiment, a product also having an unleaded research octane of about 93 may be recovered, and a smaller and less costly recycle stream of methylpentanes will result. When fractionation conditions are adjusted to take overhead more than about 10 volume percent of the methylpentanes in the fractionator feed, the octane rating of the product will be correspondingly less, while the recycle stream will be smaller. Regardless of the desired octane of the product, it is essential to the concept of the present process that at least a portion of the methylpentanes in the feed to the fractionation step be separated from the product and, preferably, recycled to the isomerization step.
In general, the feed to the fractionation step will contain at least some methylcyclopentane and cyclohexane. These hydrocarbons will invariably be retained in the recycle, bottoms portion of the fractionator. Although it may be possible to isomerize these cyclic compounds to the desired branched paraffinic isomers by recycling them to the isomerization step, it may be more economical to separate them from the recycle stream of methylpentanes and withdraw them from the process. One preferred method for accomplishing such a separation is to withdraw the recycle methylpentanes stream as a side cut from the lower section of a frac tionation vessel and to withdraw the cyclics in the bottoms from the fractionator, while the product of the process is recovered overhead. Thus the desired separation can be produced by simply enlarging the fractionator necessary to the process.
I claim as my invention:
1. A process for the conversion of a C C, hydrocarbon fraction into more valuable products which comprises isomerizing said fraction, separating from the resultant effluent a C C. isomerate, contacting the latter with a solid sorbent to separate the isomerate into a C -C1 normal hydrocarbons stream and a C -C branched hydrocarbons stream, fractionating the last-mentioned stream to separate the same into an isopentane-dimethylbutane overhead product, a methylcyclopentane-cyclohexane bottoms product and a methylpentane side cut, recycling said C -C nonnal hydrocarbons stream and said side cut to the isomerizing step, and separately recovering said overhead product and said bottoms product.
2. The process of claim 1 further characterized in that said fraction is isomerized in contact with a catalyst comprising a refractory inorganic oxide component, a combined halogen component and platinum group metal component.
3. The process of claim 1 further characterized in that said solid sorbent is a zeolitic molecular sieve-type sorbent.
4. The process of claim 3 further characterized in that said sorbent selectively adsorbs normal hydrocarbons and rejects branched chain and cyclic hydrocarbons.
5. A process for isomerizing and separating a lower octane isomerizable hydrocarbon charge stock containing hydrocarbons having from about five to six carbon atoms per molecule to produce a higher octane branched hydrocarbons product, which process comprises the steps of:
a. contacting said charge stock with hydrogen and with a composite comprising a refractory inorganic oxide component, a platinum group metal component and a combined halogen component, in an isomerization zone at isomerization condition;
b. separating the effluent from said isomerization zone into a hydrogen-rich gaseous phaseand a liquid isomerate phase;
0. separating said isomerate phase in a sorption zone, utilizing a solid zeolite sorbent, to provide a normal hydrocarbons stream and a branched hydrocarbons stream and introducing said normal hydrocarbons stream into said isomerization zone;
d. fractionating said branched hydrocarbons stream to provide a product stream comprising isopentane and dimethylbutanes, a recycle stream comprising methylpentane, and a bottoms stream comprising methylcyclopentane and cyclohexane, and recovering said products stream as said branched hydrocarbons product; and,
(e) withdrawing said bottoms stream from the process and introducing at least a portion of said recycle stream into-said isomerization zone.
|US2918511 *||9. Mai 1958||22. Dez. 1959||Texaco Inc||Isomerizing a c6 hydrocarbon fraction|
|US2921104 *||8. Nov. 1957||12. Jan. 1960||Universal Oil Prod Co||Combination process of isomerization and selective fractionation followed by a sorption process|
|PK110716A *||Titel nicht verfügbar|
|Zitiert von Patent||Eingetragen||Veröffentlichungsdatum||Antragsteller||Titel|
|US4014743 *||10. Jan. 1973||29. März 1977||Penick & Ford, Limited||Method for continuous preparation of cooked thinned starch pastes|
|US4343958 *||28. Apr. 1981||10. Aug. 1982||Uop Inc.||Hydrocarbon isomerization process|
|US4717784 *||10. Dez. 1986||5. Jan. 1988||Shell Oil Company||Total isomerization process with mono-methyl-branched plus normal paraffin recycle stream|
|US4804802 *||25. Jan. 1988||14. Febr. 1989||Shell Oil Company||Isomerization process with recycle of mono-methyl-branched paraffins and normal paraffins|
|US4855529 *||25. Apr. 1988||8. Aug. 1989||Shell Oil Company||Isomerization process with preliminary normal paraffin and mono-methyl paraffin feed capture step|
|US4982048 *||24. Febr. 1989||1. Jan. 1991||Shell Oil Company||Isomerization process with preliminary normal paraffin and mono-methyl paraffin feed capture step|
|US5026951 *||9. Jan. 1990||25. Juni 1991||Uop||Process for paraffin isomerization with liquid phase adsorptive product separation|
|US5043525 *||30. Juli 1990||27. Aug. 1991||Uop||Paraffin isomerization and liquid phase adsorptive product separation|
|US5073667 *||9. Okt. 1990||17. Dez. 1991||Shell Oil Company||Process for the isomerization of a hydrocarbon feed|
|US5107052 *||31. Dez. 1990||21. Apr. 1992||Uop||Extraction of dimethyl paraffins from isomerates|
|US5139646 *||30. Nov. 1990||18. Aug. 1992||Uop||Process for refractory compound removal in a hydrocracker recycle liquid|
|US5146037 *||29. Nov. 1990||8. Sept. 1992||Uop||Isomerization with distillation and psa recycle streams|
|US5177299 *||30. Dez. 1991||5. Jan. 1993||Uop||Recovery of high octane components from isomerates|
|US5245102 *||14. Aug. 1992||14. Sept. 1993||Uop||Isomerization with distillation and psa recycle streams|
|US5326928 *||5. März 1993||5. Juli 1994||Institute Francais Du Petrole||Separation of aliphatic paraffins by adsorption|
|US5530172 *||3. Nov. 1994||25. Juni 1996||Uop||Process for alkane isomerization using reactive chromatography|
|US5602291 *||14. Juni 1994||11. Febr. 1997||Institut Francais Du Petrole||Process for isomerizing C5 /C6 normal paraffins with recycling normal paraffins and methyl-pentanes|
|US6416657 *||31. März 1999||9. Juli 2002||Total Raffinage Distribution S.A.||Method for the isomerization of gasoline with a high benzene content|
|US6759563||9. Okt. 2001||6. Juli 2004||Uop Llc||Liquid phase adsorptive separation with hexane desorbent and paraffin isomerization|
|US6881385||28. März 2002||19. Apr. 2005||Total Raffinage Distribution S.A.||Device for the isomerization of gasoline with a high benzene content|
|US6979396||21. Juni 2004||27. Dez. 2005||Uop Llc||Combination reforming and isomerization process|
|US7015175||21. Juni 2004||21. März 2006||Uop Llc||High-activity isomerization catalyst and process|
|US7022889||19. März 2004||4. Apr. 2006||Uop Llc||Isomerization process using novel catalyst|
|US7223898||11. März 2005||29. Mai 2007||Uop Llc||Isomerization process|
|US7435329||6. Sept. 2005||14. Okt. 2008||Uop Llc||Combination reforming and isomerization process|
|US7514590||11. März 2005||7. Apr. 2009||Uop Llc||Isomerization process with adsorptive separation|
|US7875757||29. Mai 2008||25. Jan. 2011||Uop Llc||Combination reforming and isomerization process|
|US20020139712 *||28. März 2002||3. Okt. 2002||Total Raffinage Distribution S.A.||Method and device for the isomerization of gasoline with a high benzene content|
|US20040249230 *||19. März 2004||9. Dez. 2004||Gillespie Ralph D.||Isomerization process using novel catalyst|
|US20050023189 *||21. Juni 2004||3. Febr. 2005||Gillespie Ralph D.||Combination reforming and isomerization process|
|US20050027154 *||21. Juni 2004||3. Febr. 2005||Vassilakis James G.||High-activity isomerization catalyst and process|
|USRE37089||31. Aug. 1999||13. März 2001||Millennium Fuels Usa Llc||Refining process and apparatus|
|USRE37142||31. Aug. 1999||24. Apr. 2001||Millennium Fuels Usa Llc||Refining process and apparatus|
|CN1037111C *||6. März 1993||21. Jan. 1998||法国石油公司||N-c5/c6 alkane isomerization process having the cycle of n-alkane and methyl pantane|
|EP0488757A1 *||29. Nov. 1991||3. Juni 1992||Uop||Combination of C5 to C6 isomerisation and pressure swing adsorption|
|EP0512635A2 †||4. Mai 1992||11. Nov. 1992||Shell Internationale Research Maatschappij B.V.||A process for the production of isoparaffins|
|EP0528089A1||20. Aug. 1991||24. Febr. 1993||Uop||Integrated isomerization and adsorption steps for upgrading C5 and C6 hydrocarbons|
|EP0559510A1 *||18. Febr. 1993||8. Sept. 1993||Institut Francais Du Petrole||Separation of aliphatic paraffines by adsorption|
|EP0559518A1 *||22. Febr. 1993||8. Sept. 1993||Institut Francais Du Petrole||Process for the isomerisation of normal C5/C6 paraffins with normal paraffins et methyl pentanes recycling|
|WO2006098883A2 *||2. März 2006||21. Sept. 2006||Lynn H Rice||Isomerization process|
|US-Klassifikation||208/95, 585/736, 585/365, 585/738, 208/139|
|Internationale Klassifikation||C07C5/22, C07C7/13, C10G67/06|
|Unternehmensklassifikation||C10G2400/02, C07C5/226, C07C2523/40, C07C7/13|
|Europäische Klassifikation||C07C5/22B8, C07C7/13|
|27. Apr. 1989||AS||Assignment|
Owner name: UOP, A GENERAL PARTNERSHIP OF NY, ILLINOIS
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:UOP INC.;REEL/FRAME:005077/0005
Effective date: 19880822
|21. Sept. 1988||AS||Assignment|
Owner name: UOP, DES PLAINES, IL, A NY GENERAL PARTNERSHIP
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:KATALISTIKS INTERNATIONAL, INC., A CORP. OF MD;REEL/FRAME:005006/0782
Effective date: 19880916