US20170175014A1 - Fractionation process for a process for oligomerising light olefins - Google Patents

Fractionation process for a process for oligomerising light olefins Download PDF

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US20170175014A1
US20170175014A1 US15/388,232 US201615388232A US2017175014A1 US 20170175014 A1 US20170175014 A1 US 20170175014A1 US 201615388232 A US201615388232 A US 201615388232A US 2017175014 A1 US2017175014 A1 US 2017175014A1
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fraction
process according
head
cut
debutaniser
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Isabelle Prevost
Jerome Pigourier
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Axens SA
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Axens SA
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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
    • C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
    • C10G57/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with polymerisation
    • 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
    • C10G7/00—Distillation of hydrocarbon oils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • 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
    • C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
    • 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
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/02—Stabilising gasoline by removing gases by fractioning
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1088—Olefins
    • C10G2300/1092—C2-C4 olefins
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/06—Gasoil
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/28—Propane and butane

Definitions

  • the invention relates to the field of the production of oligomers from light olefins, and more particularly oligomers having more than 8 carbon atoms with boiling points in the range of gasolines, kerosene and gasoil.
  • the invention relates to the step of separating the products obtained in the course of an oligomerisation process.
  • Oligomerisation reactions lead to different products having different boiling points, and therefore downstream of the oligomerisation section a fractionation section is necessary in order to isolate the desired products such as liquefied petroleum gas (LPG), gasolines and middle distillates.
  • LPG liquefied petroleum gas
  • the fractionation section of an oligomerisation process enabling LPG, gasolines and middle distillates to be obtained employs two fractionation columns.
  • the effluent from the oligomerisation section is passed to a first distillation, the debutaniser, which enables the lightest components, mainly hydrocarbons containing 4 or fewer carbon atoms, to be separated, so as to produce a light gasoline cut whose vapour pressure is between 0.005 and 0.09 MPa.
  • the debutaniser produces at the head a hydrocarbon-rich flow containing 4 or fewer carbon atoms, which is passed to a liquefied petroleum gas (LPG) store, and at the bottom a mixture of gasoline and distillate which is then fractionated in a second distillation, the separator (splitter according to English terminology), so as to produce the gasoline and distillate having the specifications required for refining.
  • LPG liquefied petroleum gas
  • the separator splitter according to English terminology
  • U.S. Pat. No. 4,720,600 describes an oligomerisation process for light olefins in which olefins having a number of carbon atoms between 3 and 6 are oligomerised in a reaction section in the presence of a zeolitic catalyst.
  • the effluent obtained is fractionated by means of three columns so as to obtain a distillate, which constitutes the desired product, a light fraction and a heavy fraction, which are at least partly recycled to the oligomerisation reaction section.
  • the said distillate which is in the kerosene range, includes in particular compounds having a boiling point between 165° C. and 290° C.
  • US Patent Application 2014/0134064 describes a fractionation device enabling an oligomerate to be upgraded according to two fractionation section variants containing a succession of three distillation columns in order to obtain three main products and a flow of C5 hydrocarbons, downstream of the oligomerisation reaction section.
  • the said fractionation section comprises a first fractionation column (debutaniser) separating the hydrocarbons containing 1 to 4 carbon atoms and the hydrocarbons containing at least 5 carbon atoms.
  • the fraction comprising the hydrocarbons containing at least 5 carbon atoms is added to a second fractionation column (depentaniser) which enables the hydrocarbons containing 5 carbon atoms to be recovered at the head of the column, which can be recycled to the reaction section, and the hydrocarbons containing at least 6 carbon atoms to be recovered at the bottom of the column, part of which may be upgraded as gasoline base and a second part may be passed to a third fractionation column (middle distillate recovery column), which enables a cut comprising hydrocarbons containing 6 to 9 carbon atoms and a diesel cut to be separated.
  • a second fractionation column depentaniser
  • a third fractionation column middle distillate recovery column
  • the second fractionation column (depentaniser) is replaced by a stripper adjacent to the debutaniser (side-stripper according to English terminology).
  • This stripper is supplied by a side offtake situated on the debutaniser and sufficiently at the head of the column in order to be able to sample a hydrocarbon cut containing 5 carbon atoms.
  • Part of this side offtake can be recycled to the oligomerisation reactor so as to maintain the oligomerisation reaction zone in the liquid phase, to control the exothermicity and to maximise the gasoline yield, while a second part is sent to the stripper to separate the hydrocarbons containing 4 or fewer carbon atoms, which are passed to the debutaniser and the hydrocarbons containing 5 carbon atoms.
  • the fractionation of the oligomerate required in order to separate the three desired products, namely the liquefied petroleum gas, the gasolines and the middle distillates, is a costly operation that typically represents more than 70% of the total energy consumption of an oligomerisation unit.
  • the total consumption of hot utilities of the fractionation section corresponds to the sum total of the services, duties according to English terminology, associated with reboiling of the distillations.
  • the oligomerate contains molecules with a large number of carbon atoms, the reboiling temperatures of the columns are therefore generally greater than 140° C. for the debutaniser (first column) and greater than 200° C. for the second gasoline/middle distillates separation column (separator). These reboiling temperatures depend on the composition of the oligomerate, as well as on the choice of the operating pressures. Furthermore, there are very few or even no hot fluids available in the unit with a thermal energy sufficient to permit a thermal integration.
  • Hot fluid is understood to mean a fluid of the process that undergoes a recooling.
  • Cold fluid is understood to mean a fluid of the process that undergoes a reheating.
  • Hot utility is understood to mean a fluid external to the process that undergoes a cooling in order to deliver heat to a cold fluid.
  • Cold utility is understood to mean a fluid external to the process that undergoes a reheating in order to extract heat from a hot fluid.
  • the consumption of hot utilities of a process corresponds to the total amount of heat supplied by one or more hot utilities to the said process.
  • the reboiling service corresponds to the amount of heat energy supplied to a distillation column and the condensation service corresponds to the amount of heat energy extracted from a distillation column.
  • the invention thus relates to a fractionation scheme for a process for oligomerising light olefins, comprising a prefractionation of the effluent from the reaction section.
  • the invention relates more particularly to a process for oligomerising light olefins in which the effluent from the oligomerisation section is passed to a prefractionator that provides at least one head fraction containing a mixture of liquefied petroleum gas and light gasoline and a bottom fraction containing a mixture of heavy gasoline and middle distillate, the said head fraction being passed to a debutaniser that provides at least a liquefied petroleum gas cut and a light gasoline cut, the said bottom fraction and at least part of the said light petroleum cut being passed to a separator enabling at least a gaseous fraction, a petroleum fraction and a gasoil fraction to be obtained.
  • An advantage of the present invention is that it significantly reduces the consumption of hot utilities without adversely affecting the amounts and qualities of the obtained LPG, gasoline and gasoil.
  • Another advantage of the present invention is that it permits a thermal integration by using one or more hot fluids available in the process, such as the bottom products of the second column, the inter-reactor effluent and the effluent from the last reactor of the oligomerisation reaction section.
  • Another advantage of the present invention is that two gasoline cuts can be obtained, a heavy cut rich in middle distillates obtained from the bottom of the high-temperature prefractionation column and a light cut depleted in middle distillates obtained from the bottom of the lowest temperature debutaniser, which enable the separator to be supplied at two different levels, thereby facilitating the separation of a gasoline fraction and a middle distillate fraction.
  • the oligomerisation reactions are exothermic, and the temperature of the reaction section is generally between 120° C. and 300° C.
  • an effluent produced by an oligomerisation section is passed to a fractionation section that comprises primarily a prefractionator enabling a prefractionation stage to be carried out.
  • At least part of the oligomerate obtained from the oligomerisation reaction section is therefore passed, without any treatment other than a possible heat exchange via a heat exchanger for example, to a distillation column, a so-called prefractionator, enabling a prefractionation of the said oligomerate to be carried out.
  • the said prefractionation leads to at least two fractions:
  • the prefractionator contains between 5 and 20 theoretical trays and preferably between 8 and 18 theoretical trays and operates at a pressure between 0.1 and 2 MPa, preferably between 0.3 and 1.2 MPa
  • the feedstock is fed to a tray situated at the head of the column, preferably to trays 1 to 6, the trays being numbered starting from the head of the column
  • the head vapours are withdrawn at a temperature between 100° C. and 150° C., preferably between 110° C. and 140° C.
  • the bottom liquid is withdrawn at a temperature between 170° C. and 220° C., preferably between 185° C. and 205° C.
  • the said head fraction is passed to a second column, the so-called debutaniser, which leads to at least two cuts:
  • the debutaniser contains between 15 and 35 theoretical trays and preferably between 18 and 30 theoretical trays, and operates at the same pressure as the prefractionator, the feedstock is fed between the theoretical trays 8 and 25 and preferably between the theoretical trays 10 and 18, the trays being numbered starting from the head of the column, the head vapours are removed, condensed and subcooled to a temperature between 35° and 55° C., preferably between 40° and 50° C. in an air-cooled condenser, and the bottom liquid is withdrawn at a temperature between 100° C. and 130° C., preferably between 105° and 125° C.
  • the said bottom fraction and at least part of the said bottom cut are passed to a third distillation column, the so-called separator, in order to separate the various desired products from one another.
  • the main products obtained are gasoline and middle distillate (kerosene and/or gasoil).
  • the separator contains between 20 and 40 theoretical trays and preferably between 25 and 35 theoretical trays and operates at a lower pressure than the pressure of the said debutaniser, between 0.01 MPa and 0.6 MPa and preferably between 0.05 and 0.3 MPa.
  • the said bottom fraction obtained from the prefractionator is fed between the trays 5 and 15 and preferably between the trays 7 and 12, the said bottom cut obtained from the debutaniser is fed between the theoretical trays 2 and 12 and preferably between the trays 2 and 6, the trays being numbered starting from the head of the column.
  • the head vapours are removed, condensed and subcooled to a temperature between 40° C. and 80° C., preferably between 50° C. and 70° C. in the air-cooled condenser, the bottom liquid is removed at a temperature between 200° C. and 240° C., preferably between 210° C. and 230° C.
  • the said bottom fraction and the said bottom cut feed the separator at two different levels, in order to facilitate the gasoline/middle distillate separation.
  • the separator generally contains between 20 and 40 theoretical trays.
  • the said bottom fraction is preferably introduced between the theoretical trays 7 and 15 and the said bottom cut is introduced above the latter, preferably between the trays 2 and 12, the trays being numbered starting from the head of the column.
  • the said bottom cut is also in part passed to the gasoline pool, in part purged, in part returned to the oligomerisation reaction section, or preferably in part recycled to the prefractionation column.
  • the said bottom cut is preferably introduced to several trays above the reboiler.
  • the degree of recycling of the said bottom cut is between 5% by weight and 20% by weight and more preferably between 7% by weight and 15% by weight.
  • the prefractionator arranged upstream of the debutaniser leads to a reduction of at least 30° C. of the reboiling temperature required for the functioning of the debutaniser, which allows a thermal integration in particular thanks to a hot fluid of the process that is available at a temperature greater than or equal to 130° C. or thanks to a hot utility that is available at a relatively low temperature.
  • the partial recycling of the said bottom cut to the said prefractionation column also leads to a reduction of the reboiling temperature of the said prefractionator of between 5° C. and 15° C.
  • the different hot fluids of the process enable several forms of implementation of the said thermal integration to be envisaged.
  • the bottom effluent of the said separator is used for a heat exchange with the reboiler of the said debutaniser.
  • the effluent obtained from the first reactor is cooled before its pressure is reduced and it is introduced into the prefractionator, which enables heat to be recovered and the reboiler of the said debutaniser to be reheated.
  • FIG. 1 shows a conventional fractionation process scheme according to the prior art for obtaining a LPG fraction, a gasoline fraction and a middle distillate fraction.
  • the oligomerate ( 1 . 1 ) is passed to a debutaniser ( 1 .A), which separates at least two fractions, namely a column head fraction ( 1 . 2 ) and a column bottom fraction ( 1 . 3 ).
  • the said column bottom fraction ( 1 . 3 ) is then passed to a separator ( 1 .B) that separates in turn two fractions ( 1 . 4 and 1 . 5 ).
  • FIG. 2 shows an embodiment of the process according to the invention in which a prefractionation column ( 2 .C) is installed upstream of the process shown in FIG. 1 .
  • the head fraction containing a mixture of liquefied petroleum gas and light gasoline ( 2 . 6 ) from the prefractionator ( 2 .C) is passed to the debutaniser ( 2 .A), while the bottom fraction containing a mixture of heavy gasoline and the middle distillate ( 2 . 7 ) is passed directly to the separator ( 2 .B).
  • FIG. 3 shows an embodiment similar to that shown in FIG. 2 of the process according to the invention in which, in addition, a part of the bottom fraction containing a mixture of heavy gasoline and middle distillate ( 3 . 7 ) from the debutaniser ( 3 .A) is recycled ( 3 . 8 ) to the said prefractionator ( 3 .C).
  • the liquefied petroleum gas contains 2% by weight of hydrocarbons containing 5 or more carbon atoms.
  • the gasoline is characterised by an initial boiling point D 86 of 13° C. and a final boiling point D 86 of 140° C., and a content of hydrocarbons containing 4 or fewer carbon atoms of only 1.9% by weight.
  • the middle distillate is characterised by an initial boiling point D 86 of 164° C. and a flash point determined by the Nelson method of 43.9° C.
  • Example 1 The process of Example 1 is shown in FIG. 1 .
  • the oligomerate ( 1 . 1 ) is passed to a debutaniser ( 1 .A) which separates it into at least two fractions, namely a column head fraction ( 1 . 2 ) and a column bottom fraction ( 1 . 3 ).
  • the said column bottom fraction ( 1 . 3 ) is then passed to a separator ( 1 .B) that separates in turn two fractions ( 1 . 4 and 1 . 5 ).
  • the bottom product from the debutaniser ( 1 . 4 ) exchanges its heat with the effluent feeding it ( 1 . 3 ).
  • the debutaniser and the separator operate with 23 theoretical trays, their feed positions being optimised so as to minimise the heat dispensed to the reboilers. Accordingly the feed of the debutaniser ( 1 .A) is located at tray 13 and the feed of the separator ( 1 .B) is located at tray 8, the trays being numbered starting from the head of the column.
  • the debutaniser ( 1 .A) operates at 0.65 MPa and the separator ( 1 .B) operates at 0.2 MPa.
  • Example 2 The process of Example 2 is shown in FIG. 2 .
  • a prefractionation column ( 2 .C) is installed upstream of the process of Example 1.
  • the head fraction from the prefractionator ( 2 . 6 ) is passed to the debutaniser ( 2 .A) while the bottom fraction ( 2 . 7 ) is passed directly to the separator ( 2 .B).
  • the prefractionator ( 2 .C) comprises 14 theoretical trays and operates at 0.65 MPa.
  • the bottom effluent from the separator ( 2 . 5 ) is used for a heat exchange with the reboiler of the debutaniser ( 2 .A) before it is cooled and stored.
  • the bottom cut of the debutaniser ( 2 . 3 ) and the bottom fraction ( 2 . 7 ) obtained from the prefractionation are passed in whole to the separator ( 2 .B), respectively to tray 4 and to tray 10, the trays being numbered starting from the head of the column.
  • Example 3 The process of Example 3 is shown in FIG. 3 .
  • Example 3 the same process as in Example 2 ( FIG. 2 ) is implemented, with in addition the recycling ( 3 . 8 ) of 0.5 t/hour of the said bottom cut ( 3 . 3 ) from the debutaniser ( 3 .A) to the prefractionator ( 3 . c ) at the level of tray 12, the trays being numbered starting from the head of the column and the column containing 14 trays.
  • Example Example Example 1 2 3 Prefractionator Flow rate (tons/hour) 11.9 11.9 Reboiler service (MW) 0.63 0.58 Reboiler temperature (° C.) 197.6 187.1 First column Reflux rate (tons/hour) 13.9 12.8 12.8 Side reboiler service (MW) Side reboiler temperature (° C.) Reboiler service (MW) 1.0 0.53 0.52 Reboiler temperature (° C.) 145.0 116.7 116.4 Condenser service (MW) 1.9 1.75 1.75 Condenser temperature 45.0 45.0 45.0 45.0 (° C.) Second column Reflux rate (tons/hour) 5.4 4.2 4.1 Reboiler service (MW) 1.20 1.08 1.13 Reboiler temperature (° C.) 224 224 224 Condenser service (MW) 1.7 1.4 1.4 Condenser temperature 45.0 61.0 61.0 (° C.) Total reboiler services 2.2 2.24 2.23 Total hot utilities (MW) 2.2 1.71 1.
  • the process according to the invention enables, for the same amounts and specifications of obtained products, the consumption of hot utilities to be reduced in the fractionation stage of the oligomerate by 22% compared to a simple fractionation carried out by means of two successive distillations without a prefractionation section.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US15/388,232 2015-12-22 2016-12-22 Fractionation process for a process for oligomerising light olefins Abandoned US20170175014A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR1563036 2015-12-22
FR1563036A FR3045652B1 (fr) 2015-12-22 2015-12-22 Procede de fractionnement pour un procede d'oligomerisation d'olefines legeres

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US (1) US20170175014A1 (fr)
EP (1) EP3184609B1 (fr)
KR (1) KR102736543B1 (fr)
CN (1) CN106916602B (fr)
FR (1) FR3045652B1 (fr)
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FR3045652B1 (fr) 2018-01-12
KR102736543B1 (ko) 2024-11-29
CN106916602B (zh) 2020-12-15
EP3184609B1 (fr) 2018-08-01
TW201739908A (zh) 2017-11-16
KR20170074793A (ko) 2017-06-30
EP3184609A1 (fr) 2017-06-28
CN106916602A (zh) 2017-07-04
FR3045652A1 (fr) 2017-06-23

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