US3788980A - 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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US3788980A
US3788980A US00210514A US3788980DA US3788980A US 3788980 A US3788980 A US 3788980A US 00210514 A US00210514 A US 00210514A US 3788980D A US3788980D A US 3788980DA US 3788980 A US3788980 A US 3788980A
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percent
weight
feedstock
solvent
water
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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

  • the purity of the aromatics recovered from the extract is improved by introducing light aliphatic hydrocarbons consisting essentially of aliphatic and cycloaliphatic hydrocarbons having 6 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 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 mixed hydrocarbon feedstock containing small amounts of benzene and, more particularly, to the recovery of high purity aromatic hydrocarbons in high yields while making eflicient use of process components.
  • An object of this invention in the processing of hydrocarbon feedstocks of low benzene content is to improve the reflux in aqueous solvent single extractorsingle 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 extraction-distillation process for the recovery of aromatic hydrocarbons having boiling points in the range of about C. to about C. 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 one percent by weight, based on the weight of the feedstock, of benzene and 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 6 carbon atoms, a boiling point no higher than about 50 C., and being condensable at a pressure of no more than about 3 atmospheres and at a temperature of no less than about 50 C.; 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
  • step (d) recycling the reflux hydrocarbons from step (c) to to the extraction column as provided in step (b);
  • the improvement comprising introducing a sufiicient 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.
  • 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 hyrogenation, can contain as much as 70 to 98 precent BTX.
  • feedstocks also contain both aliphatic and cycloaliphatic hydrocarbons (herein sometimes referred to collectively as aliphatic hydrocarbons).
  • hydrocarbons with boiling points ranging from 25 C. to 175 C. including straight-chain and branched-chain paraflins and naphthenes, such as nheptane, isooctane, and methyl cyclohexane, and aromatics such as toluene and the CgS.
  • the aromatics fraction can include 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.
  • the particular aromatics fraction which is dealt with here contains no more than one percent benzene, based on the weight of the whole hydrocarbon feedstock.
  • 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 200 C. and having a decomposition temperature of at least about 225 C.
  • 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 dipropylene 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, diethanolamine, and triethanolamine; nitriles such as beta-beta -oxydipropionitrile and beta,beta -thiodipropionitrile; phenol and the cresols; the m hyl sultolanes; sulfoxides such as dimethyl sulfoxide and diethyl sulfoxides; lactones such as gammapropiolactone and gamma-butyrolactone.
  • amides such as formamide, acetamide, dimethylformamide, diethylformamide, and dimethylacetamide
  • amines such as diethylenetriamine and triethylenetetramine
  • 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 3 to about 25 stages and is preferably about 5 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 time the theoretical stages in the same column, e.g., in a column having 4 theoretical stages, the middle theoretical stage would include, as defined herein, the 2nd and 3rd theoretical stages and in a column having 24 theoretical stages, the middle theoretical stage would include the 7th 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 solventwater 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 50 percent by Weight aliphatics having from 5 to 7 carbon atoms and about 50 percent to about 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 are different for both in 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 rafiinate distillation or from outside the system.
  • the ratio of reflux to feedstock 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 raflinate 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 100 C. to about 200 C. and is preferably in the range of about 125 C. to about 150 0., especially for the solvent of preference.
  • the pressure in the extraction zone is maintained in the range of about 75 p.s.i.g. to about 200 p.s.i.g. 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 disillation 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 135 C. to about 200 C.
  • the pressure at the top of the stripper, an upper flash zone in this case, is in the range of about 20 p.s.i.g. to about 35 p.s.i.g.
  • the pressure is in the range of about p.s.i.g. to about 20 p.s.i.g. and is about 10 or p.s.i.g. 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 p.s.i.g. to about 25 p.s.i.g. with some variation throughout the zone.
  • the steam brought into the bottom of the distillation zone enters at a temperature of about 100 C. to about 150 C. and is under a pressure of about 15 p.s.i.g. to about 25 p.s.i.g.
  • the total water present in the distillation column is essentially in vapor form and is generally in the range of about 0.1 part to about 05 part by weight of water to one 'part by weight of aromatics in the zone and preferably in the range of about 0.1 part to about 0.3 part 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 50 C. to about 150 C.
  • 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 solvetn solution having a temperature in the range of about 125 C. to about 175 C. enters at the top tray of extractor 3 through line 4 and percolates down the column removing aromatics from the feedstock.
  • the rafiinate leaves the top of the column and passes through heat exchanger 2 where it is used to preheat the feedstock and is cooled in turn to a temperature in the range of 75 C. to about 125 C.
  • 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 25 C. to about 50 C. 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 i 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.
  • raflinate 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 raflinate 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 aliphatics.
  • an aliphatic hydrocarbons phase still called the raffinate
  • 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 aliphatics.
  • the raffinate proceeds along line 55 to raflinate still 56 where the defined light aliphatics are removed as a vapor overhead and pas through condenser 58. A portion of the condensate is returned to the top tray of rafiinate 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 raflinate 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 raflinate 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 100 percent by weight of the defined light aliphatics can be supplied in thi 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 raflinate 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 p.s.i.g. to about 40 p.s.i.g.
  • the reflux ratio is about 0.521 to about 3.0: 1.
  • Part of the ratfinate water phase can optionally be recirculated through extractor 8 via line 11, line 9 and line 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 of aliphatics. 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 mixersettler.
  • 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 in the process is in the range of about 0.1 percent to about 5 percent by weight of the aromatic hydrocarbons in the feedstock and is preferably in the range of about 0.5 percent to about 2.0 percent by weight of such aromatic hydrocarbons.
  • the slipstream washes the water in extractor 13 to remove the small amount of aliphatics, which is so detrimental to the efliciency 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 percent to about 20 percent by weight feedstock aromatics, about 2 percent to about 5 percent by weight water, about 65 percent to about 75 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 100 C. to about 125 C.
  • 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 coniprises 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. 7
  • 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 1-0 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 38 C. and 94 C. 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 5 to 7 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 0 to about 5 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 raffinate 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 raflinate 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 25 C. to aboutSO C. 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 10 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 raftinate wash.
  • the aromatic hydrocarbons phase proceeds from decanter 36 through line 26 along which an aromatics sl pstream 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 determined 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. As long 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 mixersettler or other form of extractor. Where a mixer-settler 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 with drawn 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 mixersettler 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 abou 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 joint line 53 an enter solvent regenerator 52 where the solvent is separated from low boiling and high boiling impurities by stream 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 rafiinate decanter 7 (optional) and raflinate 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 rafiinate.
  • 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.
  • sufiicient 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 make-up being added when necessary.
  • Subject process is found to be particularly advantageous for feedstocks containing at least about percent by weight aromatics and even more so for those containing about percent or more aromatics.
  • the process is found to be beneficial for feedstocks having an aromatics content of at least about 40 percent by weight, however.
  • step (d) recycling the reflux hydrocarbons from step (c) to the extraction column as provided in step (b);
  • step (e) recovering the aromatic hydrocarbons of step (c); the impovement 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,
  • step (f) introducing the raflinate formed in step (b) into a raflinate distillation zone to separate the light aliphatics defined in claim 1 therefrom;
  • step (g) recycling the defined light aliphatics from step (f) to the middle theoretical stage of the extraction column;
  • step 3 recovering the balance of the raflinate from step 3.
  • the process of claim 2 wherein the feedstock and the defined light aliphatics enter the extraction column at about the same point.
  • 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 (h) contacting the water phase of step (e) with an aromatic hyldrocarbons 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 (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 (k) recovering the aromatic hydrocarbons phase of step (g) and the aliphatic hydrocarbons phase of step (e), 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) contacting the feedstock in the extraction column (i) recovering the aromatic hydrocarbon phase of step with a mixture of water and a solvent, said solvent (f) and the aliphatic hydrocarbons phase of step (d), being a water-miscible organic liquid having a boilthe improvement comprising introducing a suflicient ing point of at least about 200 C. and having a deamount of the light aliphatics defined above into the composition temperature of at least about 225 C., extraction column at the middle theoretical stage and with reflux hydrocarbons introduced into the extraction column below the bottom theoretical stage thereof to provide the extract comprising aromatic hydrocarbons, reflux aliphatic hydrocarbons, solvent,

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  • Organic Chemistry (AREA)
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US00210514A 1971-12-21 1971-12-21 Process for the separation of aromatic hydrocarbons from a mixed hydrocarbon feedstock Expired - Lifetime US3788980A (en)

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JP (1) JPS4868531A (fr)
BE (1) BE793088A (fr)
DE (1) DE2262320A1 (fr)
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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4664783A (en) * 1984-03-13 1987-05-12 Krupp-Koppers Gmbh Method for the separation of aromates from hydrocarbon mixtures containing aromatics
US4781820A (en) * 1985-07-05 1988-11-01 Union Carbide Corporation Aromatic extraction process using mixed polyalkylene glycols/glycol ether solvents
US5022981A (en) * 1989-09-18 1991-06-11 Uop Aromatic extraction process using mixed polyalkylene glycol/glycol ether solvents
US5139651A (en) * 1989-09-18 1992-08-18 Uop Aromatic extraction process using mixed polyalkylene glycol/glycol ether solvents
US5529612A (en) * 1995-05-23 1996-06-25 Southern Petroleum Laboratories, Inc. Method and system for removing volatile organics from landfill gas
US5563315A (en) * 1993-12-22 1996-10-08 Uop Separation of aromatic hydrocarbons from a mixture of aromatic and non-aromatic hydrocarbons by solute swing extraction

Families Citing this family (3)

* 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
CH682721A5 (de) * 1991-01-17 1993-11-15 Galipag Verfahren für den Stoffaustausch zwischen flüssigen und gasförmigen Medien.

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4664783A (en) * 1984-03-13 1987-05-12 Krupp-Koppers Gmbh Method for the separation of aromates from hydrocarbon mixtures containing aromatics
US4781820A (en) * 1985-07-05 1988-11-01 Union Carbide Corporation Aromatic extraction process using mixed polyalkylene glycols/glycol ether solvents
US5022981A (en) * 1989-09-18 1991-06-11 Uop Aromatic extraction process using mixed polyalkylene glycol/glycol ether solvents
US5139651A (en) * 1989-09-18 1992-08-18 Uop Aromatic extraction process using mixed polyalkylene glycol/glycol ether solvents
US5563315A (en) * 1993-12-22 1996-10-08 Uop Separation of aromatic hydrocarbons from a mixture of aromatic and non-aromatic hydrocarbons by solute swing extraction
US5529612A (en) * 1995-05-23 1996-06-25 Southern Petroleum Laboratories, Inc. Method and system for removing volatile organics from landfill gas

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Publication number Publication date
FR2164767A2 (fr) 1973-08-03
BE793088A (fr) 1973-06-20
FR2164767B2 (fr) 1976-10-29
NL7217369A (fr) 1973-06-25
JPS4868531A (fr) 1973-09-18
DE2262320A1 (de) 1973-06-28

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