US20210324275A1 - Method for fractionation of hydrocarbons - Google Patents

Method for fractionation of hydrocarbons Download PDF

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US20210324275A1
US20210324275A1 US17/287,549 US201917287549A US2021324275A1 US 20210324275 A1 US20210324275 A1 US 20210324275A1 US 201917287549 A US201917287549 A US 201917287549A US 2021324275 A1 US2021324275 A1 US 2021324275A1
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separation
stripping medium
inlet
outlet
feed
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Stefan Andersen
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Topsoe AS
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Haldor Topsoe AS
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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
    • C10G7/00—Distillation of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
    • 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
    • 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
    • C10G2300/4025—Yield
    • 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
    • C10G2300/4081—Recycling aspects

Definitions

  • the present invention relates to the field of separation of hydrocarbons and similar compounds by fractionation according to boiling point.
  • Separation in a distillation column may be aided by reboiling of the heavy fraction, but this may be problematic for some feeds, which may react or decompose in the fractionation column, with yield loss and/or precipitation and fouling of the equipment as consequences.
  • Typical stripping media are steam and hydrogen, but also fuel gas (methane, ethane and possibly propane) have been used.
  • the stripping medium will be separated with the lightest fraction and will typically end up as a waste stream, which is either combusted or released otherwise, and thus the use of a stripping medium may be costly. Therefore, the amount of stripping medium is moderated in consideration of the balance between additional purity or yield and the cost of stripping medium.
  • the stripping medium may be problematic in itself; steam may cause corrosion challenges or water condensation and some stripping media such as fuel gas may be dissolved in the product with the consequence of requiring a later clean-up of product.
  • the present invention seeks to improve the separation quality, without increasing the cost of using a stripping medium during separation of hydrocarbons by recycling of the stripping medium.
  • a non-condensing stripping medium such as elemental nitrogen, methane or fuel gas is directed to contact a hydrocarbon mixture.
  • a method for separation may either be a fractionation process having several outlets based on boiling point or it may be a simpler stripping process wherein only a single liquid outlet and a single gaseous outlet are used.
  • a stripping medium shall in the following be construed as a light component directed to support a separation process.
  • Fractionation shall in the following be construed as a separation process of molecules according to boiling point, by distillation.
  • vol/vol % shall be used to signify volume percentage for a gas.
  • pressures for means of separation such as distillation columns are discussed in the following, the pressure is in accordance with the terminology of the art determined at the top of the column, i.e. typically the lowest pressure of the column.
  • a broad aspect of the present disclosure relates to a process for separation of a hydrocarbonaceous liquid phase from a gas phase comprising the steps of
  • the process further comprises the steps of
  • the operating pressure of said means of separation is from atmospheric pressure to 2 barg and said pressurizing of said recycled stripping medium involves increasing the pressure by 0.1 bar to 2 bar, with the associated benefit of designing to process for such a moderate pressurization of the recycled stripping medium being a low capital and operation cost of the means of pressurization, and specifically allowing the option of using a blower technology.
  • the operating pressure of said means of separation is from 0 mbar absolute to 200 or 500 mbar absolute and said pressurizing of said recycled stripping medium involves increasing the pressure by between 5 mbar and 50 or 200 mbar, with the associated benefit of designing to process for such a moderate pressurization of the recycled stripping medium being a low capital and operation cost of the means of pressurization, and specifically allowing the option of using a blower technology.
  • At least 95 wt/wt % or 99 wt/wt % of said feed is withdrawn from said means of separation in liquid form, with the associated benefit of the combination of non-condensable stripping medium and liquid product fractions being that an energy efficient separation of stripping medium from products is possible, allowing recycle of the stripping medium without excessive cooling or heating.
  • At least 90 vol/vol % of said stripping medium is non-condensable at 20° C. and 1 atmosphere, such as gases from the group comprising N 2 , H 2 , He, Ar, Ne, CO 2 , CH 4 and C 2 H 6 , with the associated benefit of these constituents being gaseous at relevant process conditions, and typically being compatible with product specifications and being compatible with material specifications, including corrosion stability.
  • H 2 , CO 2 , CH 4 and C 2 H 6 are available in the process, N 2 is available at low cost and easily separated from other streams, noble gases such as He, Ar and Ne are highly inert, CH 4 and C 2 H 6 may be taken as side streams from relevant process steps and CO 2 —or a mixture of CO 2 and N 2 may be obtained from the dried flue gas of a fired heater.
  • the feed has an initial boiling point of at least 100° C., 200° C. or 300° C., with the associated benefit of a process for separation of heavy feed being especially suitable for being operated with recycle of stripping medium as the separation of stripping medium will be simpler, the positive effect on separation higher and the benefits from avoiding thermal cracking in the absence of reboiling of a fraction of the feed will also be higher.
  • the 95% boiling point of said feed is 400° C., 500° C. or 600° C. with the associated benefit of a process being able to separate a heavy feed while avoiding a very heavy bottoms product.
  • the ratio between the amount of stripping medium and the amount of feed directed to the means of separation is from 10 NL/kg, 40 NL/kg or 100 NL/kg to 200 NL/kg, 400 NL/kg or 1000 NL/kg, with the associated benefit of providing a balance between a low cost at low ratios and a high separation efficiency at higher ratios.
  • the stripping medium comprises at least an amount of a gas originating from the gas source supplying blanketing gas for product tanks, with the associated benefit of provision of blanketing gas already being enabled on the premises of a refinery, and the requirements to e.g. inertness of blanketing gas being similar to the requirements for a stripper gas.
  • said recycled stripping medium is heated by heat exchange, with the associated benefit of such heating being an increased efficiency of separation of dissolved light components.
  • a further aspect of the present disclosure relates to a process for production of a product boiling in the diesel range comprising the steps of
  • a further aspect of the present disclosure relates to a fractionation section comprising a means of separation having a feed inlet, a means of separation stripping medium inlet, one or more product outlets and a vapor outlet, and a means of pressurization having an inlet and an outlet characterized in said vapor outlet being in fluid communication with the inlet of said means of pressurization, and said outlet of said means of pressurization being in fluid communication with said means of separation stripping medium inlet.
  • the fractionation section further comprises a side column, having a side column feed inlet, a side column stripping medium inlet, a side column vapor outlet and a side column liquid outlet, wherein said side column stripping medium inlet is in fluid communication with the outlet of said means of pressurization, with the associated benefit of such a fractionation section being well suited for the side columns operating with a high amount of stripping medium, resulting in an increased separation efficiency.
  • the fractionation section further comprises a bottoms stripper having a bottoms stripper stripping medium inlet, a stripper vapor outlet, a bottoms stream inlet and a stripped bottoms outlet, and where said means of separation further has a bottoms outlet, and wherein said bottoms stream inlet is configured for being in fluid communication with said bottoms outlet, optionally via a means of heating, wherein said bottoms stripper stripping medium inlet is configured for being in fluid communication with said outlet of said means of pressurization optionally via a means of heating, and wherein said stripper vapor outlet is in fluid communication with said means of separation stripping medium inlet, with the associated benefit of such a fractionation section being suited for minimizing the amount of purge necessary from a process producing HPNA by increasing the separation efficiency of the bottoms stripper.
  • a further aspect of the present disclosure relates to a hydrocracker section comprising a hydrocracking reactor having an inlet and an outlet and a fractionation section comprising a means of separation having a feed inlet, a make up stripping medium inlet, one or more product outlets and a vapor outlet, and a means of pressurization having an inlet and an outlet characterized in said hydrocracker section being configured for directing an amount of product from the hydrocracking reactor outlet to the means of separation feed inlet vapor outlet being in fluid communication with the inlet of said means of pressurization, and said outlet of said means of pressurization being in fluid communication with said stripping medium inlet, with the associated benefit of such a process providing a highly effective separation of diesel from heavy distillate, thus allowing an increased yield of valuable product boiling in the diesel range.
  • fractional distillation or fractionation i.e. processes separation according to boiling point
  • the crude oil comprises many chemical components, having a wide boiling range, e.g. from 40° C. to more than 600° C.
  • Fractional distillation processes are carried out on the crude oil, to provide the typical fuel fractions e.g. naphtha, kerosene, diesel, lubricant and bunker fuel.
  • Fractional distillation is also carried out on a wide range of intermediate products, e.g. where an intermediate fraction with a homogeneous boiling range has been treated in a chemical process, such that products with different boiling point are produced.
  • the chemical processes involve hydroprocessing, in which crude oil reacts with hydrogen, in the presence of catalysts.
  • Hydroprocessing may be in the form of hydrotreatment, which maintain the structure of the crude oil hydrocarbons, but release light components, such as NH 3 , H 2 O and H 2 S. Hydroprocessing may also be in the form of hydrocracking, in which the structure of hydrocarbons is broken down to form smaller compounds.
  • the separation of products is typically carried out in a fractional distillation process, where a means of separation, typically a distillation column with multiple trays and multiple outlets is used.
  • a means of separation typically a distillation column with multiple trays and multiple outlets.
  • the temperature decreases from the inlet towards the top of the distillation column, and from each outlet a fraction can be withdrawn, which comprises the condensed product.
  • this stream is divided in a liquid stream and a gaseous stream.
  • the gaseous stream is returned to the main column. From such a column each outlet will provide a stream boiling in a defined range, but the separation will be imperfect with overlapping fractions.
  • Separation especially in the case of simple gas/liquid separations, may be carried out at the process pressure, which typically is elevated. This is convenient especially where the products are to be further treated at elevated pressure.
  • separation since the boiling point of a component is dependent on the pressure, separation may be more efficient at low pressure.
  • the separation is often carried out slightly above atmospheric pressure, e.g. at 0.1 barg to 3 barg (where barg means bar gauge, e.g. pressure relative to atmospheric pressure), which involves the simplest equipment.
  • barg means bar gauge, e.g. pressure relative to atmospheric pressure
  • Such separation is called atmospheric separation.
  • Even more efficient separation may be carried out at reduced pressure, e.g. 0 bar to 0.2 or 0.5 bar (absolute pressure), which may also have the benefit of avoiding excessive heating to temperatures where the components are unstable.
  • Such separation is called vacuum separation.
  • Stripping medium may beneficially be used to aid separation at all pressures, but the physical equipment to be used will differ, depending on the pressure of operation.
  • the heaviest bottom fraction may also be reboiled, i.e. directed to be heated, such that at least an amount of the bottom fraction is evaporated, and returned to the column.
  • This improves separation, but during reboiling the high temperatures may lead to thermal cracking, and thus reduce the total recuperation of hydrocarbons and cause fouling of equipment leading to more frequent interruption of operation to clean the affected items.
  • the economy of a separation process depends on the balance between operational expense for the process and the value of the products.
  • the products must adhere to standards, and thus a poor separation must be compensated by a restrictive limitation of boiling point.
  • an increased yield of more valuable product may be obtained by improved separation, and therefore it may be beneficial to accept increased operational expense to gain product value.
  • the operational expenses related to separation may also be balanced against the operational expense of downstream processes.
  • stripping medium is one example of added operational expense which provides a net economic benefit.
  • the typical stripping medium is steam, and the production, and thus production and use of steam is related to a consumption of energy, which has a cost.
  • the separation efficiency may be increased, such that each fraction comprises a high amount of components well suited for the fraction.
  • the temperature will be low and steam is collected as liquid water, which must be heated and vaporized to be used as stripping medium again.
  • the separation efficiency may be further increased, but the balance between cost and gain will reach a maximum at some level, beyond which the cost of steam and equipment size exceeds the value of improved separation.
  • the use of steam increases the requirements to corrosion resistance of materials and causes a need for removal of water from the products.
  • a stripping medium being gaseous at standard temperature, such as N2, and furthermore to recirculate the stripping medium around the separation process, which is not possible when the stripping medium is steam, since the used steam is condensed as liquid water.
  • the use of a gaseous stripping medium has the benefit that the separation of stripping medium from the light feed fraction being uncomplicated, especially if the boiling points of the stripping medium and the light feed fraction are remote from each other.
  • the use of recirculation has the benefit that the cost of providing stripping medium is reduced, since only a minor amount released to the surroundings or dissolved in the separated feed fractions must be replenished. As the cost of stripping medium is reduced, the balance between the cost of stripping medium and the value of separation efficiency will be shifted towards a higher separation efficiency, and thus less requirement for distancing the fractionation cut point from the classification limits of products.
  • the requirements to the feed and the stripping medium for use in a process where the stripping medium is recycled include, as mentioned, that the boiling point is remote from that of the lightest feed, such that the product is at least 95 wt/wt % condensing, while the stripping medium is non-condensing in the fractionation section, which typically includes an overhead drum having a lower temperature than the column.
  • the lowest temperature is typically in the overhead drum, which typically is 20-120° C. depending on environmental conditions. This means that for atmospheric fractionation it is preferred that the product does not include significant amounts of fuel gas, e.g. methane, ethane and propane. For a vacuum fractionation, even butane and pentane may be undesired in the product.
  • the stripping medium is non-condensing allows at least N 2 , H 2 , He, Ar, Ne, CO 2 , CH 4 and C 2 H 6 as stripping media. It is also beneficial that the stripping medium is inert and has a low solubility in the hydrocarbon products, to avoid a loss of stripping medium and a product in accordance with the specifications, which makes N 2 a preferred stripping medium. Another benefit of N 2 is that it is typically available in refineries in pure form, for the purpose of blanketing storage tanks.
  • the present disclosure is also relevant for hydroprocessing, especially a hydrocracking process, in which a heavy feedstock is hydrocracked and directed to a fractionation process employing a recycled stripping medium.
  • a hydrocracking process is especially well suited for being combined with such a fractionation process, as a cascade of vapor/liquid separators will ensure that the feed for separation contains little or no non-condensing product, such that purification of the stripping liquid is avoided or minimized.
  • Hydrotreatment processes involving heavy products may also benefit from such a configuration, especially if the amount of light products is minimal.
  • FIG. 1 shows a fractionation section according to the present disclosure.
  • FIG. 2 shows a fractionation section according to the prior art.
  • FIG. 3 shows a hydrocracking section, with a fractionation section according to the present disclosure.
  • FIG. 1 shows an aspect of the present disclosure.
  • Two hydrocracked fossil feeds for separation 102 and 104 are directed to a feed inlet of a means of separation 106 .
  • An amount of stripping medium 108 is directed to a stripping medium inlet of the means of separation 106 .
  • Liquid product fractions 112 , 122 are withdrawn from a number of positions of said means of separation 106 , and each of these fractions are purified in secondary means of separation such as side column strippers 114 , 124 , where a further amount of stripping medium is added as side stripper stripping medium 116 , 126 , stripped liquid fractions 118 , 128 are withdrawn and the side stripper gaseous fractions 120 , 130 are directed to the means of separation 106 .
  • the lightest fraction 142 is withdrawn, and optionally separated in a three phase separator 144 , from which the liquid hydrocarbon fraction 145 may be directed to the column as recycle 146 and/or withdrawn as product 148 .
  • the gaseous fraction 150 from the three phase separator is directed to a means of pressurization such as a blower or a compressor 152 , typically after but optionally before being heated e.g. in heat exchanger 154 , and recycled as stripping medium 158 , in combination with a limited amount of make-up stripping medium 160 . From the bottom of the means of separation a bottoms product 162 is withdrawn.
  • a means of pressurization such as a blower or a compressor 152 , typically after but optionally before being heated e.g. in heat exchanger 154 , and recycled as stripping medium 158 , in combination with a limited amount of make-up stripping medium 160 .
  • a purge of stripping medium may be withdrawn with the objective of avoiding concentrating impurities.
  • the impurities may gaseous product hydrocarbons or oxygen from equipment leaks.
  • the purge stream may be directed to an absorbent or a reactor for removing the impurities. Removal of oxygen may be carried out by catalytic oxidation of hydrocarbons or hydrogen or liquid or solid scavenging and the gaseous products may be collected e.g. in an amine wash. Gaseous hydrocarbons may be directed to other means of separation.
  • FIG. 2 shows an aspect of the prior art.
  • Two hydrocracked fossil feeds for separation 202 and 204 are directed to a feed inlet of a means of separation 206 .
  • An amount of stripping medium, typically steam 208 is directed to a stripping medium inlet of the means of separation 206 .
  • Liquid product fractions 212 , 222 are withdrawn from a number of positions of said means of separation 206 , and each of these fractions are purified in secondary means of separation such as side column strippers 214 , 224 , where a further amount of stripping medium is added as side stripper stripping medium 216 , 226 , stripped liquid fractions 218 , 228 are withdrawn and the side stripper gaseous fractions streams 220 , 230 are directed to the means of separation 206 .
  • the lightest fraction 242 is withdrawn, and after cooling separated in a three phase separator to a gas fraction 264 , a liquid hydrocarbon fraction 245 and a water fraction 268 in three phase separator 244 .
  • the liquid fraction 266 from the three phase separator 244 may be directed to the column as recycle 246 and/or withdrawn as product 248 . From the bottom of the means of separation a bottoms product 262 is withdrawn.
  • FIG. 3 shows an aspect of the present disclosure.
  • a feed 372 is directed to a hydrocracking reactor 374 comprising a hydrocracking catalyst.
  • the hydrocracked product 376 is directed to a cascade of separators, 378 , 380 , 382 , 384 from which a cold product stream 386 and a hot product stream 388 are withdrawn and directed to a stripper 390 .
  • From the stripper vapor 391 and liquid product stream 392 are withdrawn.
  • the liquid product stream 392 is preheated and separated in flash vessel 394 into a vapor product stream 304 and a liquid product 396 .
  • the liquid product is heated in heater 398 .
  • the heated liquid product 302 and the vapor product stream 304 are directed to a means of separation 306 .
  • An amount of stripping medium 308 is directed to a stripping medium inlet of the means of separation 306 .
  • Liquid product fractions 312 , 322 are withdrawn from a number of positions of said means of separation 306 , and each of these fractions are purified in secondary means of separation such as side column strippers 314 , 324 , where a further amount of stripping medium is added as side stripper stripping medium 316 , 326 , stripped liquid fractions 318 , 328 is withdrawn and the side stripper vapor gaseous fractions streams 320 , 330 are directed to the means of separation 306 .
  • the lightest fraction 342 is withdrawn, and optionally separated in a three phase separator 344 , from which the liquid hydrocarbon fraction 345 may be directed to the column as recycle 346 and/or withdrawn as product 348 .
  • the gaseous fraction 350 from the three phase separator is directed to a means of pressurization such as a blower or a compressor 352 optionally before or after being heated 354 , and recycled as stripping medium 358 , in combination with a limited amount of make-up stripping medium 360 .
  • the make up stripping medium 360 may optionally be supplied as a side stream of the blanket gas used in the storage tanks of products. From the bottom of the means of separation a bottoms product 362 is withdrawn.
  • Example 1 the product of a hydrocracking process is directed to a fractionation according to the present disclosure, as described in FIG. 1 , in which the stripping medium is N 2 , and the total N 2 :HC ratio into the column and side columns is 1.7 mol/kg, and N 2 is recycled to be used as stripping medium.
  • the performance of the fractionation process is shown in Table 1. According to this example, 0.35% of the N 2 must be added as make up gas due to N 2 being dissolved in the products. If a 2% purge of stripping N 2 was included, it would be required to add 2.35% as make up N 2 .
  • Example 2 the product of a hydrocracking process is directed to a fractionation according to the prior art, as described in FIG. 2 , in which the stripping medium is steam and the total H 2 O:HC ratio into the column and side columns is 0.7 mol/kg. H 2 O is condensed at the outlet of the column, but cannot be recycled to be used as stripping medium, unless it is heated and vaporized in a steam drum.
  • Example 1 and Example 2 are compared in Table 3. It is seen that an extra yield of valuable products like kerosene and diesel is obtained and the yield of less valuable products like naphtha and unconverted oil (UCO) is reduced.
  • UOU unconverted oil
  • Example 2 In addition to the increased yield, the use of recycled nitrogen as stripping medium in Example 1 will furthermore have the benefit of having a lower operational expense, compared to the required amount of steam in Example 2.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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DKPA201800763 2018-10-23
DKPA201800763 2018-10-23
PCT/EP2019/078735 WO2020083915A1 (fr) 2018-10-23 2019-10-22 Procédé de fractionnement d'hydrocarbures

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