US3779904A - Process for the separation of aromatic hydrocarbons from a mixed hydrocarbon feedstock - Google Patents

Process for the separation of aromatic hydrocarbons from a mixed hydrocarbon feedstock Download PDF

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US3779904A
US3779904A US00210404A US3779904DA US3779904A US 3779904 A US3779904 A US 3779904A US 00210404 A US00210404 A US 00210404A US 3779904D A US3779904D A US 3779904DA US 3779904 A US3779904 A US 3779904A
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percent
weight
feedstock
aromatic hydrocarbons
solvent
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D Kubek
A Kosseim
G Somekh
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Katalistiks International Inc
Honeywell UOP LLC
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Union Carbide Corp
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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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents

Definitions

  • ABSTRACT The process involves a combination of continuous solvent extraction-steam distillation for the recovery of aromatic hydrocarbons from a mixed feedstock.
  • the feedstock is contacted with a solvent-water mixture at temperatures in the range of about 75 to 200C and the extract and raft'mate streams are separated into their components.
  • the purity of the aromatics recovered from the extract is improved by introducing light aliphatic hydrocarbons consisting essentially of aliphatic and cycloaliphatic hydrocarbons of no more than five carbon atoms with the feedstock at the middle theoretical stage of the extraction column.
  • the light aliphatics are introduced in amounts in the range of 5 to 12 percent, based on the weight of the feedstock.
  • This invention relates to an improvement in a process for the separation of aromatic hydrocarbons from a fixed hydrocarbon feedstock and, more particularly, to the recovery of high purity aromatic hydrocarbons in high yields while making efficient use of process components.
  • An object of this invention is to improve the reflux in aqueous solvent single extractor-single distillation column systems whereby heating requirements are reduced and the purity of the aromatics is raised to previously unattained levels.
  • high purity aromatic hydrocarbons are effectively recovered using minimal heat in a continuous solvent extractiondistillation process for the recovery of aromatic hydrocarbons having boiling points in the range of about 80C. to about 175C. from a feedstock containing aliphatic hydrocarbons and at least about 40 percent by weight, based on the weight of the feedstock, of aromatic hydrocarbons wherein the feedstock contains no more than about 4 percent by weight, based on the weight of the feedstock, of light aliphatics consisting essentially of aliphatic and cycloaliphatic hydrocarbons,-each having no more than 5 carbon atoms, a boiling point no higher than about 50C., and being condensable at a pressure of no more than about 3 atmospheres and at a temperature of no less than about 50C.; a single extraction column having about 3 to about 25 theoretical stages is used for the solvent extraction to provide an extract; and a single distillation column is used to distill the extract to provide a mixture of the aromatic hydrocarbons comprising the following steps:
  • the improvement comprising introducing a sufficient amount of the light aliphatics defined above into the extraction column at the middle theoretical stage thereof to provide a total percent by weight of said light aliphatics, based on the weight of the feedstock, in the range of about 5 percent to about 12 percent.
  • FIGURE is a schematic flow diagram of an illustrative embodiment of the present invention.
  • BTX which is available in high proportion,e.g., at least about 40 percent by weight, in a wide variety of hydrocarbon feedstocks such as reformed gasolines; coke oven light oils; cracked gasolines; and dripolenes, which, after hydrogenation, can contain as much as to 98 percent BTX.
  • feedstocks also contain both aliphatic and cycloaliphatic hydrocarbons (herein sometimes referred to collectively as aliphatic hydrocarbons).
  • hydrocarbons with boiling points ranging from 25C. to C. including straight-chain and branchedchain paraffms and naphthenes, such as n-heptane, isooctane, and methyl cyclohexane, and aromatics such as BTX.
  • the BTX fraction can include benzene, toluene, the C aromatics including ortho-xylene, meta-xylene, para-xylene, and ethyl benzene, and C aromatics, which, if present at all, usually appear in the smallest proportion in relation to the other components.
  • a typical breakdown of the defined light aliphatic fraction, in percent by weight based on the total weight of the fraction, is about percent to about 95 percent of the full range of C aliphatics, about 0 percent to about 5 percent of C aliphatics, and a small proportion, about 0 percent to about 1 percent, of C to C aliphatics.
  • the solvents used in the subject process are, as described above, water-miscible organic liquids, (at process temperatures) having a boiling point of at least about 200C. and having a decomposition temperature of at least about 225C.
  • water-miscible includes those solvents which are completely miscible over a wide range of temperatures and those solvents which have a high partial miscibility at room temperature since the latter are usually completely miscible at process temperatures.
  • the solvents are also polar and are generally comprised of carbon, hydrogen and oxygen with some exceptions.
  • solvents which may be used in the process of this invention are dipro' pylene glycol, tripropylene glycol, dibutylene glycol, tributylene glycol, ethylene glycol, diethylene glycol, ethylene glycol monomethyl ether, ethylene glycol monoethyl ether, diethylene glycol monomethyl ether, diethylene glycol monoethyl ether, sulfolane, N-methyl pyrrolidone, triethylene glycol, tetraethylene glycol, ethylene glycol diethyl ether, propylene glycol monoethyl ether, pentaethylene glycol, hexaethylene glycol, and mixtures thereof.
  • the preferred group of solvents is the polyalkylene glycols and the preferred solvent is tetraethylene glycol.
  • Additional solvents which may be used alone or together, or with the aforementioned solvents are amides such as formamide, acetamide, dimethylformamide, diethylformamide, and dimethylacetamide;- amines such as diethylenetriamine and triethylenetetramine; alkanolamines such as monoethanolamine, diethanol-- amine, and triethanolamine; nitriles such as beta,betaoxydipropionitrile and beta,beta -thiodipropionitrile;
  • phenol and the cresols methyl sulfolanes
  • sulfoxides such as dimethyl sulfoxide and diethyl sulfoxides
  • lactones such as gamma-propiolactone and gammabutyrolactone.
  • the apparatus used in the process both for the main extraction and distillation is conventional, e.g., an extraction column of the multistage reciprocating type containing a plurality of perforated plates centrally mounted on a vertical shaft driven by a motor in an oscillatory manner can be used as well as columns containing pumps with settling zones, sieve trays with upcomers, or even a hollow tube while the distillation can be conducted in a packed or bubble plate fractionating column. Countercurrent flows are generally utilized in both extraction and distillation columns.
  • Heat exchangers, decanters, reservoir, solvent regenerator, and raffinate still are also conventional as well as various extractors other than the main extractor. These other extractors are preferably single stage mixer-settlers, but can be any of the well known types.
  • the number of theoretical stages in the extraction column can be about three to about 25 stages and is preferably about five to about 12 stages.
  • the middle theoretical stage of the column is defined to include the theoretical stages running from 0.25 times the theoretical stages in the column plus one to 0.75 times the theoretical stages in the same column, e.g., in a column having four theoretical stages, the middle theoretical stage would include, as defined herein, the second and third theoretical stages and in a column having 24 theoretical stages, the middle theoretical stage would include the seventh to the 18th theoretical stages, inclusive. It will be recognized by those skilled in the art that the number of theoretical stages is to be considered as based on functioning theoretical stages and that the bottom theoretical stage is located just above the reflux inlet no matter what the actual physical layout of the column is.
  • the feed and the defined light aliphatics can be introduced anywhere in the middle theoretical stage; however, it is preferred that both be introduced at the same point in the middle theoretical stage to obtain the full benefits of the process.
  • the solvent is used as an aqueous solution thereof containing water in an amount of about 1 percent to about 8 percent by weight based on the weight of the solvent and preferably containing water in an amount of about 2 percent to about 5 percent by weight.
  • This aqueous solution is referred to hereafter in some instances as a solvent-water mixture.
  • the ratio of solvent (exclusive of water) to feedstock in the extractor is in the range of about 4 to about 8 parts by weight of solvent to one part by weight of feedstock.
  • This broad range can be expanded upon where nonpreferred solvents are used.
  • a broad range of about 3 to about 12 parts by weight of solvent to one part by weight of feedstock and a preferred range of about 5 parts to about 7 parts of solvent per part of feedstock can be used successfully for the solvent of preference and other like solvents.
  • the ratio is selected by the technician based on experience with the particular feedstock and depends in part upon whether high recovery or high purity is being emphasized, although the instant process will improve purity in any case.
  • the reflux to the extraction zone is generally made up of about 20 percent to about percent by weight aliphatics having from five to seven carbon atoms and about 50 percent to about 80 percent by weight aromatics, both based on the total weight of the reflux.
  • the reflux, percentages, and ratios discussed in this paragraph are not considered to include and do not apply to the defined light aliphatics, although the latter might be referred to as an auxiliary reflux. There is some overlap in composition, however, in that some of the components which make up the reflux are the same as some of the defined light aliphatics. These similar components in the reflux should not be included when determining whether the percentage of defined light aliphatics meets the stated requirements.
  • the sources, other than the feedstock, are different for bothin that the major source of the reflux is the distillate from the main distillation column while the source of the defined light aliphatics is from raffinate distillation or from outside the system.
  • the ratio of reflux to feed-stock in the extraction zone is, generally, maintained in the range of about 0.5 to about 1.5 parts by weight of reflux to one part by weight of feedstock and preferably about 0.6 to about 1.25 parts by weight of reflux to one part by weight of feedstock, but, again, is selected by the technician just as the ratio of solvent to feedstock.
  • the reflux aliphatics pass into the extract rather than being taken overhead with the raffinate and are recycled to the extractor from the reflux decanter as will be seen hereinafter.
  • the temperature in the extraction zone is maintained in the range of about 100C. to about 200C. and is preferably in the range of about 125C. to about 150C, especially for the solvent of preference.
  • the pressure in the extraction zone is maintained in the range of about 75 psig. to about 200 psig. As is well known in the art, however, one selected pressure is not maintained throughout the extraction zone, but, rather, a high pressure within the stated range is present at the bottom of the zone and a low pressure again within the stated range is present at the top of the zone with an intermediate pressure in the middle of the zone.
  • the pressures in the zone depend on the design of the equipment and the temperature, both of which are adjusted to maintain the pressure within the stated range.
  • the temperature at the top of the distillation zone which, in terms of the apparatus used, may be referred to as a distillation column or stripper, is at the boiling point of the mixture of aromatics present in the zone while the temperature at the bottom of the stripper is generally in the range of about 135C. to about 200C.
  • the pressure at the top of the stripper, an upper flash zone in this case, is in the range of about 20 psig to about 35 psig.
  • the pressure in a lower flash zone just beneath the upper flash zone and connected thereto is in the range of about psig to about 20 psig and is about 10 or psig lower than the pressure in the upper flash zone.
  • the pressure in the rest of the distillation zone is maintained in the range of about 15 psig to about 25 psig with some variation throughout the zone.
  • the steam brought into the bottom of the distillation zone enters at a temperature of about 100C. to about 150C. and is under a pressure of about 15 psig to about 25 psig.
  • the total water present in the distillation column is essentially in vapor form and is generally in the range of about 0.1 parts to about 0.5 parts by weight of water to one part by weight of aromatics in the zone and preferably in the range of about 0.1 parts to about 0.3 parts by weight of water to one part by weight of aromatics.
  • the water used for the steam may be called stripping water. A small amount of water is present in liquid form in the distillation zone dissolved in the solvent.
  • the feedstock and defined light aliphatics are introduced through line 1 into heat exchanger 2 where they are preheated to a temperature in the range of about 50C. to about 150C.
  • the mixture then continues through line 1 to enter extractor 3 at the middle tray thereof, which is the equivalent of the middle theoretical stage.
  • An aqueous solvent solution having a temperature in the range of about 125C. to about 175C. enters at the top tray of extractor 3 through line 4 and percolates down the column removing aromatics from the feedstock.
  • the raffinate leaves the top of the column and passes through heat exchanger 2 where it is used to preheat the feedstock and is cooled in tum to a temperature in the range of C. to about 125C.
  • the raffinate comprises about percent to about 98 percent by weight aliphatics, about 1 percent to about 3 percent by weight dissolved and entrained solvent, and about 0 percent'to about 3 percent by weight aromatics.
  • the raffinate then passes through cooler 6 where it is further cooled to about 25C. to about 50C. and proceeds along line 5 to decanter 7 where it separates into two phases, an aliphatic hydrocarbons phase and a solvent phase, the solvent being contaminated with aliphatics.
  • phase is named after its main component, which is present in the phase in an amount of at least 50 percent by weight and, in most cases, in an amount of at least 90 percent by weight.
  • the aliphatic hydrocarbons phase which can still be referred to as the raffinate, now contains about 96 percent to about 99 percent by weight aliphatics, about 0 percent to about 1 percent by weight dissolved and entrained solvent, and about 0 percent to about 3 percent by weight aromatics.
  • the solvent phase contains about 90 percent to about 96 percent by weight solvent, about 2 percent to about 5 percent by weight water, and about 2 percent to about 4 percent by weight aliphatics.
  • raffinate extractor 8 which can be a single stage mixersettler or other conventional type of extractor.
  • the solvent phase passes through line 10 to join line 12 referred to hereinafter or it can be optionally recycled to the top of extractor 3 along line 20 (connection to extractor not shown).
  • the raffinate is washed with a portion of the water phase from reflux decanter 29 and separated in raffinate extractor 8 into an aliphatic hydrocarbons phase (still called the raffinate) which is essentially free of solvent and water and contains about 97 percent to about 100 percent by weight aliphatics and about 0 percent to about 3 percent by weight aromatics, and a raffinate water phase as bottoms which contains about 75 percent to about 90 percent by weight water, about 10 percent to about 25 percent by weight solvent, and about 0.1 percent to about 1 percent by weight aliphat-
  • the raffinate proceeds along line 55 to raffinate still 56 where the defined light aliphatics are removed as a vapor overhead and pass through condenser 58.
  • a portion of the condensate is returned to the top tray of raffinate still 56 as a reflux which aids in purifying the lights by knocking down the high boilers.
  • the heavier aliphatics are removed as bottoms and pass through line 62 where a portion is diverted through reboiler 63 and returns to raffinate still 56 below the bottom tray as a vapor to provide most of the heating requirement.
  • the balance of the heavy aliphatics proceeds along line 62 to storage (not shown).
  • the balance of the condensate proceeds along line 60 where it joins line 1 thus supplying a high proportion of the defined light aliphatics for the process.
  • This raffinate distillation is the preferred and most satisfactory mode for supplying the bulk of the defined light aliphatics for the process.
  • About 50 percent to about lOO percent by weight of the defined light aliphatics can be supplied in this manner although initially the necessary defined light aliphatics must be provided from an outside source (not shown) to line 1 and make-up defined light aliphatics may be added from time to time to maintain the required level.
  • the raffinate still is similar to stripper 23 except that it can be half the height and half the diameter thus reducing its cost and heating requirements.
  • the temperature in the bottom of the raffinate still is maintained in the range of about 45 C. to about 200 C.
  • the pressure is maintained in the range of about 5 psig to about 40 psig
  • the reflux ratio is about 0.5:l to about 3.0:].
  • Part of the raffinate water phase can optionally be recirculated through extractor 8 via line 11, line 9 and line 5 as shown.
  • This recirculation is conventional with a mixer-settler arrangement, but may not be advantageous with other types of extractors.
  • this water phase still contains, along with the water and solvent, a small amount ofaliphatics. All of the balance of the water phase is, therefore, directed from line 11 along line 12 to extractor 13, which can again be a single-stage mixer-settler.
  • Feeding into line 12 via line 50 is an aromatics slipstream, which at its source (see line 14) is an essentially pure stream of aromatics, i.e., having a purity of at least 95 percent by weight, or in other words, at least 95 percent by weight of the slipstream is aromatic hydrocarbons.
  • the purity of the slipstream is preferably about 98 percent and for optimum performance, i.e., to obtain the highest purity product, about 99 percent or even higher. It is called a slipstream or sidestream because the amount of aromatics fed into the water phase passing through line 12 is very small. The amount of slipstream aromatic hydrocarbons used.
  • the slipstream washes the water in extractor 13 to remove the small amount of aliphatics, which is so detrimental to the efficiency of the process.
  • This aromatics slipstream can be recycled along line 15 through extractor 13 to further wash the water phase where a mixer settler extractor is used and it is then, preferably, sent along line 16 to line 1 where it is reintroduced into the feedstock and passes into the system once more.
  • the water which is essentially devoid of aliphatics, but contains solvent, then passes as bottoms from extractor 13 through line 17 and into water reservoir 51 via line 37.
  • the solvent solution of aromatics comes into countercurrent contact with a reflux liquid, which enters extractor 3 below the bottom tray (or theoretical stage) along line 18.
  • the reflux percolates up the lower half of extractor 3 progressively dissolving in and purifying the solvent solution of aromatics.
  • the solution which is formed, i.e., the extract comprises about 10 percent toabout 20 percent by weight feedstock aromatics, about 2 percent to about 5 percent by weight water, about 65 percent to about percent by weight solvent, about 4 percent to about 8 percent by weight reflux aromatics, and about 3 percent to about 6 percent by weight reflux aliphatics, all based on the total weight of the extract.
  • the extract leaves the bottom of extractor 3 through line 19 and passes through heat exchanger 22 where it is cooled to a temperature in the range of about 100C. to about 125C.
  • the extract proceeds along line 19 and enters stripper 23, the distillation zone, at upper flash chamber 24, which, as noted heretofore, is at a lower pressure than the extractor.
  • Part of the extract flashes on entering the flash chamber and is taken overhead through line 18 in vapor form.
  • Another part of the extract passes as a liquid into lower flash chamber 21, which is operated at an even lower pressure and further flashing occurs.
  • the balance of the extract percolates down the column into the fractionation zone where it comes into countercurrent contact with the stripping vapors, i.e., steam, and more vapors are generated. A part of the vapor rises to the top of the column and mixes with the flashed vapors in flash chamber 21 as noted.
  • the overhead distillate comprises about 40 to about 75 percent by weight aromatics, about 20 to about 40 percent aliphatics, about 2 percent to about 10 percent by weight water, and about 0 percent to about 5 percent by weight solvent, all based on the total weight of the overhead distillate.
  • the side-stream distillate is comprised of about 65 to about percent by weight aromatics, about 10 to about 30 percent by weight water, and about 1 percent to about 10 percent by weight of solvent, based on the total weight of the side-stream distillate.
  • overhead distillate is a combination of flashed vapors and fractionated vapors having the aforementioned composition.
  • This overhead distillate is also known as a reflux distillate.
  • the vapor is first condensed and cooled to between about 38C. and 94C. in reflux condenser 25.
  • the condensate then passes into reflux decanter 29 where a reflux hydrocarbons phase is decanted from a water phase.
  • the reflux hydrocarbons phase comprises about 20 to 50 percent by weight aliphatics having from five to seven carbon atoms, and about 50 to about 80 percent by weight aromatics and is recycled as reflux through line 18 to extractor 3 as previously described.
  • the water phase contains about 95 to about 99 percent by weight water, about to about percent by weight solvent, and about 0.1 to about 0.5 percent by weight aliphatics. It passes through line 31 and is split in two streams, lines 32 and 33, a rafflnate wash stream and an aromatics wash stream, respectively. These washes can take place as shown by splitting the stream or the entire stream can be used to wash the rafflnate first and then the aromatics providing that the water is treated with an aromatics slipstream before the aromatics wash.
  • the side-stream distillate is withdrawn in vapor form from stripper 23 through line 26 and condensed in aromatics condenser 34 and further cooled to a temperature in the range of about 25C. to about 50C. in cooler 35, which can be a heat exchanger or other type of cooling device.
  • the condensate then passes into aromatics decanter 36 where an aromatic hydrocarbons phase containing about 99.8 to about 99.9 percent by weight aromatics, and about 0.1 to about 0.2 percent by weight solvent and a water phase containing about 90 percent to about 98 percent by weight water, about 2 percent to about percent by weight solvent, and about 0.1 percent to about 0.5 percent by weight aromatics are formed.
  • the water phase passes through line 37 to water reservoir 51.
  • all of part of the water phase can be directed through valved line 38 to join line 32 for use as rafflnate wash.
  • the aromatic hydrocarbons phase proceeds from decanter 36 through line 26 along which an aromatics slipstream is taken through line 14 to wash water coming from reflux decanter 29 along line 33.
  • this slipstream can be in the range of about 0.10 percent to about 5.0 percent of the total aromatics in the feedstock and is preferably in the range of about 0.50 percent to about 2.0 percent of the total aromatics in the feedstock. These percentages are by weight.
  • the weight of the total aromatics is deter mined by analysis of a sample portion of the feedstock.
  • Aromatics added, e. g., as slipstream, during the process cycle are included in the determination.
  • the slipstream can, alternatively, be obtained from another source such as the overhead product of a benzene fractionating column, which is not shown in the drawing, or from a source completely removed from the system. Aslong as the slipstream has the previously noted high aromatics content, it will be satisfactory in this process.
  • wash extractor 39 which can be a single stage mixer-settler or other. form of extractor. Where a mixersettler is used, it is advantageous to use an aromatics recycle which passes along line 42 and joins lines 33 and 14 returning to wash extractor 39.
  • the slipstream now containing a small amount of aliphatics, passes overhead from wash extractor 39 into line 42 and along line 50 to join lines 12 and 15 and proceeds into wash extractor 13 as discussed previously.
  • Reflux water now essentially free of aliphatics, is withdrawn from wash extractor 39 and proceeds along line 43, which joins line 26, and passes into aromatics extractor 44, which can be a single stage mixer-settler or other type of extractor.
  • aromatics extractor 44 which can be a single stage mixer-settler or other type of extractor.
  • This reflux water along with water recycled from the settling zone in the case of a mixer-settler via line 45, which joins line 43, and process makeup water from line 46 (source not shown) contacts the aromatic product proceeding along line 26 into aromatics extractor 44 and recovers essentially all of the small amount of solvent remaining in the aromatics.
  • This water with solvent then proceeds along line 47 to join line 17, which joins line 37 and enters water reservoir 51.
  • High purity aromatic product is withdrawn from the process through line 26.
  • the water purge stream can be in the range of about 0.25 percent to about 2.0 percent by weight of the total water in the system and is preferably in the range of about 0.5 percent to about 1.0 percent by weight of the water in the system.
  • the total water in the system can be determined easily because the amount of water introduced can be controlled. Allowances must be made for water losses through leakage, entrainment and upsets, however.
  • Solvent can be recovered from this purge by directing the water through line 49 to join line 53 and enter solvent regenerator 52 where the solvent is separated from low boiling and high boiling impurities by steam distillation under vacuum. The solvent is recovered and recycled along line 54 to extractor 3 (connection not shown) and the water and impurities discarded.
  • the slipstream taken through line 14 is first used to wash the water phase from reflux decanter 29 (i.e., one stream) and then the water phases from rafflnate decanter 7 (optional) and rafflnate extractor 8.
  • This procedure can be varied so that a different slipstream from a different source is used for each wash or, as previously mentioned, a single slipstream is used to wash one water phase where stream 31 is not split, but is first used to wash rafflnate.
  • the slipstream picks up some aliphatics in extractor 39 before proceeding to extractor 13. It should be pointed out that the purity of this slipstream containing the small amount of aliphatics is only reduced by about one percent and that it still has a purity of at least about 95 percent by weight and preferably about 98 percent so that the definition of the slipstream with respect to purity is fulfilled.
  • the description of the invention is in terms of a continuous process which has already been initiated.
  • it is necessary to supply to the system from an outside source, sufficient of the defined light aliphatics to first saturate the extract or the reflux loop and then a sufficient amount to bring the defined light aliphatics up to the prescribed level. This is also done for the solvent and water. Once the process is initiated, these components are recycled with makeup being added when necessary.
  • Subject process is found to be particularly advantageous for feedstock containing at least about 80 percent by weight aromatics and even more so for those containing about 90 percent or more aromatics. Optimum performance is achieved when the benzene content is also high, i.e., at least about 25 percent by weight of the feedstock. The process is found to be beneficial for feedstocks having an aromatics content of at least about 40 percent by weight, however.
  • step (c) recycling the reflux hydrocarbons from step (c) to the extraction column as provided in step (b);
  • the improvement comprising introducing a sufficient amount of the light aliphatics defined above into the extraction column at the middle theoretical stage thereof to provide a total percent by weight of said light aliphatics, based on the weight of the feedstock, in the range of about 5 percent to about 12 percent.
  • step (b) introducing the rafflnate formed in step (b) into a raffinate distillation zone to separate the light aliphatics defined in claim 1 therefrom;
  • step (f) recycling the defined light aliphatics from step (f) to the middle theoretical stage of the extraction column;
  • step 3 recovering the balance of the raffinate from step 3.
  • the amount of water in the extraction column is about 1 percent to about 8 percent by weight based on the weight of the solvent in said column;
  • the ratio of reflux to feedstock in the extraction column is in the range of about 0.5 to about 1.5 parts by weight of reflux to one part by weight of feedstock;
  • the ratio of water to aromatic hydrocarbons in the distillation column is in the range of about 0.1 to about 0.5 part by weight of water to one part by weight of aromatic hydrocarbons in said column.
  • step (e) contacting the water phase of step (e) with an aromatic hydrocarbons stream containing at least 95 percent aromatic hydrocarbons, the amount of said stream being in the range of about 0.1 percent to about 5 percent by weight of the total aromatic hydrocarbons in the feedstock, to form an aromatic hydrocarbons phase and a water phase;
  • step (b) j. recycling the reflux hydrocarbons phase of the overhead distillate and the bottoms of step (c) to the extraction zone to provide reflux hydrocarbons and mixture of water and solvent, respectively, for step (b);
  • step' (g) recovering the aromatic hydrocarbons phase of step' (g) and the aliphatic hydrocarbons phase of p the improvement comprising introducing a sufficient amount of the light aliphatics defined above into the extraction column at the middle theoretical stage thereof to provide a total percent by weight of said light aliphatics, based on the weight of the feedstock, in the range of about 5 percent to about 12 percent.
  • step (d) contacting the water phase of step (d) with an aromatic hydrocarbons stream containing at least percent aromatic hydrocarbons, the amount of said stream being in the range of about 0.1 percent to about 5 percent by weight of the total aromatic hydrocarbons in the feedstock, to form an aromatic hydrocarbons phase and a water phase;
  • step (f) recycling the water phase of step (f) to the distillate zone where said water phase is essentially converted to steam;
  • step (b) recycling the reflux hydrocarbons phase of the overhead distillate and the bottoms of step (c) to the extraction zone to provide reflux hydrocarbons and mixture of water and solvent, respectively, for step (b);
  • step (f) recovering the aromatic hydrocarbons phase of step (f) and the aliphatic hydrocarbons phase of p the improvement comprising introducing a sufficient amount of the light aliphatics defined above into the extraction column at the middle theoretical stage thereof to provide a total percent by weight of said light aliphatics, based on the weight of the feedstock, in the range of about 5 percent to about 12 percent.

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Cited By (5)

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US4690733A (en) * 1985-03-20 1987-09-01 Union Carbide Corporation Process for the separation of hydrocarbons from a mixed feedstock
US4781820A (en) * 1985-07-05 1988-11-01 Union Carbide Corporation Aromatic extraction process using mixed polyalkylene glycols/glycol ether solvents
US4909927A (en) * 1985-12-31 1990-03-20 Exxon Research And Engineering Company Extraction of hydrocarbon oils using a combination polar extraction solvent-aliphatic-aromatic or polar extraction solvent-polar substituted naphthenes extraction solvent mixture
US5529612A (en) * 1995-05-23 1996-06-25 Southern Petroleum Laboratories, Inc. Method and system for removing volatile organics from landfill gas
US20100270213A1 (en) * 2009-04-28 2010-10-28 Noe Robert J L Extractive distillation process and system

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BR7402696A (pt) * 1974-02-05 1975-12-09 Union Carbide Corp Processo de extracao por solvente de destilacao a vapor para recuperacao de hidrocarbonetos aromaticos
US4604683A (en) * 1984-12-10 1986-08-05 Advanced Computer Communications Communication controller using multiported random access memory

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US3037062A (en) * 1956-05-16 1962-05-29 Universal Oil Prod Co Selective solvent extraction process for the separation of mixtures of aromatic and non-aromatic hydrocarbons
US3173966A (en) * 1960-06-17 1965-03-16 Universal Oil Prod Co Solvent extraction process for recovery of aromatic hydrocarbons
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4690733A (en) * 1985-03-20 1987-09-01 Union Carbide Corporation Process for the separation of hydrocarbons from a mixed feedstock
US4781820A (en) * 1985-07-05 1988-11-01 Union Carbide Corporation Aromatic extraction process using mixed polyalkylene glycols/glycol ether solvents
US4909927A (en) * 1985-12-31 1990-03-20 Exxon Research And Engineering Company Extraction of hydrocarbon oils using a combination polar extraction solvent-aliphatic-aromatic or polar extraction solvent-polar substituted naphthenes extraction solvent mixture
US5529612A (en) * 1995-05-23 1996-06-25 Southern Petroleum Laboratories, Inc. Method and system for removing volatile organics from landfill gas
US20100270213A1 (en) * 2009-04-28 2010-10-28 Noe Robert J L Extractive distillation process and system
US8282816B2 (en) 2009-04-28 2012-10-09 Uop Llc Extractive distillation process and system

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FR2164770B2 (is") 1976-10-29
DE2262238A1 (de) 1973-06-28
NL7217372A (is") 1973-06-25
JPS4868530A (is") 1973-09-18
FR2164770A2 (is") 1973-08-03
BE793087A (fr) 1973-06-20

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