Classifications

• • 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
  • B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
  • B01D17/02—Separation of non-miscible liquids
  • B01D17/04—Breaking emulsions
  • B01D17/045—Breaking emulsions with coalescers
• • 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
• • 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
  • 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
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
  • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
  • Y02A20/124—Water desalination

Definitions

• the present invention relates to a method and an installation for the distillation of a multicomponent mixture.
• the thermal energy required for the separation of petroleum constituents is mainly introduced by preheating the mixture to be distilled. This preheating is partly carried out with the heat that can be recovered from the thermal conditioners of the finished products and from the distillation column, thanks to lateral recirculations.
• the fluid passing through the lateral recirculation is at a temperature above 100 0 C, and up to 350 0 C or 400 0 C.
• the mixture is then superheated in a vaporization oven to finally be brought to the distillation column.
• the object of the invention is therefore to reduce the quantity of fossil fuel required for the implementation of distillation processes of multicomponent mixtures, for example oil, by recovering and recovering low-level energy available elsewhere, either in the distillation process itself, either in the near environment of this process, in the plant or refinery.
• Low-level energy is understood to mean “low temperature” calories, typically less than 100 ° C., which are otherwise released into the environment with cooling water or condensates of heating vapor.
• the document FR-2,703,600 describes a process for the distillation of complex mixtures in which, during the preheating step, at least one separation step of the mixture is provided, the vaporized part of the mixture being directly supplied to the column of distillation.
• the object of the invention is therefore to reduce the energy consumption induced by the distillation processes of multicomponent mixtures, without requiring major modifications of the process and without causing significant material investments, while ensuring the quantity and quality of the finished products. .
• the invention relates to a process for the distillation of a multicomponent liquid mixture such as crude oil comprising: (a) a step of preheating said mixture
• step (c) a step of distilling said vaporized mixture, in which process, during step (a) of preheating, is used heat from step (c) whose temperature is greater than 100 ° C. and at least one separation step of said preheated mixture is carried out in a liquid part and a vaporized part, the latter part corresponding to at least one component of the mixture and being directly treated during the distillation stage (c), and the treated mixture during the vaporization step (b) being depleted of said vaporized part, characterized in that it comprises a complementary heating step, in which low thermal level residual energies whose temperature is below 100 ° C. are used. . It is understood that this prior separation step reduces the number of constituents present in the mixture which is treated during the vaporization step and therefore, in the lower part of the column.
• This prior separation step therefore has the direct result of reducing the charge supplied to the steam oven and thus saving the energy necessary for the operation of this oven.
• This supplementary preheating stage may concern all or part of the mixture to be distilled. It can be performed in series with the step (a) preheating and upstream thereof or in parallel with a portion of step (a).
• This separation step is preferably carried out adiabatically and it advantageously intervenes after a possible preliminary treatment step of the mixture.
• This treatment step consists, for example, in a desalination when the mixture is oil.
• the preheating step (a) comprises at least two successive substeps, each of which is followed by a liquid / vapor separation step.
• the at least two substeps are performed in series or in parallel.
• a separation step may be common to at least two substeps, whether they are performed in series or in parallel.
• the invention also relates to an installation for the distillation of a multicomponent liquid mixture such as crude oil comprising: at least one means for preheating the vaporization means and a distillation column at least one liquid / vapor separation means, located after preheating means and, at the outlet of said separation means, means for directly bringing the part of said vaporized mixture and corresponding to at least one constituent, into said distillation column, characterized in that it also comprises, upstream of said at least one preheating means, a heating means using residual energies of low thermal level, the temperature of which is less than 100 ° C.
• the distillation column comprising different trays each corresponding to a given temperature and at least one component, said supply means open at the plateau of the distillation column corresponding to a temperature and at a concentration of at least a constituent close to those of the vaporized part.
• This feature makes it possible to make the best use of the beneficial effects of the prior separation of a constituent.
• the liquid / vapor separation means is located, preferably, downstream of a possible pre-treatment means of the mixture.
• the installation can in particular be a desalination tank, when the installation is intended for the distillation of oil.
• the installation preferably comprises as many liquid / vapor separation means as preheating means.
• FIG. 1 which illustrates a conventional distillation system of 2, which illustrates an installation according to the invention, corresponding to the installation of FIG. 1, in which new means have been introduced
• FIG. 3 which illustrates a variant embodiment of a preheating train of FIG. a conventional oil distillation plant
• Figure 4 which illustrates a preheating train according to the invention, corresponding to that of Figure 3, wherein new means have been introduced.
• the purpose of this description is to describe the characteristic means of the invention, their operation and their advantages.
• the conventional installation illustrated in FIG. 1 comprises a preheating train 2 with preheating means 21 to 26, through which the mixture is heated, before being brought to the steaming oven 3, the vaporized mixture then serving to supply the distillation column 4.
• the preheating of the mixture takes place in two stages, separated by a desalination step carried out in the desalination tank 5.
• a flow of crude oil is first brought into the first heating means 21 by means symbolized by the arrow 1 and heated therein.
• the latter is conventionally a heat exchanger that heats the oil through the flow of kerosene produced in the stripper 62 and transmitted to the exchanger by the means symbolized by the arrow 621.
• the recovery of kerosene at the outlet of the exchanger 21 is symbolized by the arrow 622.
• the mixture available at the outlet of exchanger 21 is supplied to heating means 22 which is also conventionally a heat exchanger.
• This exchanger uses the flow that flows in the means 71, located between the heating means 22 and the column 4.
• These means allow the circulation of fluid extracted from a tray of the column 4, from the upper part 41 of the column to the heating means 22, then the return of the cooled fluid to the upper part 41.
• These means 71 are conventionally referred to as first lateral recirculation. They contribute to the control of the thermal profile of the distillation column.
• the mixture at the outlet of the heating means 22 is supplied to the desalination tank 5.
• This reservoir 5 is conventionally a magnetic field desalination tank, in which the oil is freed from dissolved salts which are eliminated in the aqueous phase and incondensable gases which are separated in a small cutting tower which is not illustrated on FIG. 1.
• the water brought into the inlet of the tank 5 is symbolized by the arrow 50, while the water recovered at the outlet of the tank 5 is symbolized by the arrow 51.
• the mixture obtained at the outlet of the tank 5 is fed to a third heating means 23 which is an exchanger using the energy of the product coming from the stripper 61 (of the diesel) and which is transmitted to the exchanger by the means symbolized by the arrow 611.
• the diesel recovery at the outlet of the exchanger 23 is symbolized by the arrow 612.
• the mixture available at the outlet of the third heating means 23 is sent to the fourth heating means 24 which is still a heat exchanger.
• This exchanger uses the flow that circulates in the means 72, located between the heating means 24 and the column 4. These means allow the circulation of fluid extracted from the central or intermediate portion 42 of the column, to the heating means 24, then the return of the cooled fluid to the intermediate portion 42.
• These means 72 are conventionally referred to as second lateral recirculation.
• the mixture at the outlet of the heating means 24 is supplied to the fifth heating means 25.
• This is again an exchanger which allows the mixture to be heated by the diesel fuel from the stripper 60 and transmitted to the exchanger by the means symbolized by the arrow 601.
• the recovery of the diesel fuel at the outlet of the exchanger 24 is symbolized by the arrow 602.
• the mixture obtained at the outlet of the fifth heating means 25 is supplied to the sixth heating means 26, which is also a heat exchanger.
• This exchanger uses the flow that circulates in the means 73, located between the heating means 26 and the column 4.
• These means 73 allow the circulation of fluid extracted from the lower part 43 of the column to the heating means 26, then the return of the cooled fluid to the lower part 43.
• These third means 73 are conventionally referred to as third lateral recirculation.
• the preheating train 2 which has just been described represents only one embodiment example.
• a preheating train conventionally comprises a plurality of exchangers making it possible to preheat the mixture by heat exchange with, in particular, the condenser of the top products of the column, the conditioning exchangers downstream of the strippers of the finished products, such as naphtha, kerosene, turbosene, light gas oil and heavy diesel fuel and lateral recirculations for controlling the thermal profile of the distillation column.
• the lateral recirculation and the exchangers make it possible to evacuate an excess of heat within the distillation column, thanks to a cooling of the fluids passing through the lateral recirculations. This cooling is carried out outside the distillation column while according to the invention, this cooling is partly ensured by the organic vapors within the column itself.
• the mixture supplied at the outlet of the sixth heating means 26 and therefore at the outlet of the preheating train 2 is supplied to the vaporization oven 3.
• This direct fire oven is powered by natural gas and air, the supply of which is shown schematically by the arrow 30.
• This oven comprises two parts 31 and 32.
• the combustion chamber constitutes the lower part 31 which is intended for heating the mixture or the load, while the upper part 32, called fabric, is used to produce water vapor which will serve as entrainment steam in column 4 and its three strippers 60, 61 and 62.
• the arrow 33 symbolizes the exit of the furnace combustion gases.
• the vaporized charge is fed (arrow 34) to the distillation column 4, in the zone 44 located at the lower end of the column, called the zone of the overflash or washing zone (wash zone), from which the vaporized charge is conveyed to the rectification zone 45, using a steam flow.
• the latter flows from the bottom to the top of the column. It is symbolized by the arrow 48.
• This column 4 comprises a number of trays and / or packings. The number of trays is typically between 20 and 40. It is also provided with complementary elements. There may be mentioned in particular a head condenser 46 and a flash 47 where the light gases and the liquid naphtha water, the kerosene stripper 60, the turbosene stripper 61 and the diesel stripper 62 are separated.
• the flow from the distillation column 4 and entering the condenser 46 is symbolized by the arrow 460.
• the condensate outlet from the condenser 46 is symbolized by the arrow 461.
• the steam supply of the strippers from the furnace is symbolized by the arrows 600, 610 and 620 respectively.
• the residue that can be recovered at the bottom of the distillation column can either feed a vacuum distillation column or be returned before the vaporization oven 3, for use in the preheating train 2.
• the recovery of the residue is symbolized by the arrow 49.
• FIG. 2 illustrates an example of an installation according to the invention, made from the conventional installation illustrated in FIG. 1.
• a complementary heating means 8 which uses the residual energy of low thermal level coming from the installation or the rest of the refinery. It is preferably a heat exchanger. Residual energies come, for example, from steam condensates, in the case of an oil refinery.
• heat for preheating can be recovered from the distillation column, for example from the top condenser 46 of the column and the lateral recirculation 71 to 73, but also from the coolers of the finished products.
• this heat is available at various temperatures, ranging from 100 ° C. to about 350 ° -400 ° C., depending on the level at which it is extracted from the distillation column.
• a stream withdrawn from the distillation column at a temperature above 100 ° C can then be used in successive heat exchangers of the preheating process at temperatures that have become less than 100 0 C.
• the crude oil is generally fed at the temperature of the storage tank.
• the oil flow is reheated before the flow of oil is introduced into the preheating train 2.
• This means 8 may consist of one or more exchangers arranged in series and / or in parallel.
• this means 8 added to the conventional preheating train, makes it possible to use low-level heat recovered, moreover, in the installation and more specifically in the refinery. Part of the total energy consumed during the implementation of the process according to the invention then comes from heat of low level of recovery, heat which is normally lost in a conventional refinery.
• an installation according to the invention is distinguished from a conventional installation by the presence of several liquid / vapor separators inside the preheating train 2.
• a vapor and liquid separator consists of a simple empty container and is conventionally referred to as "flash".
• FIG. 2 illustrates here three separators 91, 92 and 93 which are here all located downstream of the desalination tank 5. It could also be provided at least one separator upstream of the tank 5.
• the first separator 91 is located downstream of the third heating means 23.
• the mixture available downstream of this heating means 23 is supplied to the first separator 91.
• the lightest products have already been vaporized thanks to the heat input of the heating means 21, 22 and 23 and also complementary heating means 8.
• the vaporized portion of the mixture is transmitted by the means 91a directly into the upper part 41 of the column 4. Furthermore, the liquid portion is returned to the inlet of the fourth preheating means 24 to be preheated by the second lateral recirculation 72.
• FIG. 2 illustrates a second separator 92 which is situated downstream of the fifth heating means 25.
• the feedstock which is fed to the inlet of the second separator 92 has already been depleted of the vaporized part of the mixture, supplied by the means 91a in the column distillation. This charge is partly vaporized by the heat input of the heating means 24 and 25.
• the second separator will make it possible to extract the vaporized part of the charge to bring it, thanks to the means 92a, to the central part 42 of the column 4.
• the liquid part of the charge, already depleted twice, is then brought sixth heating means 26.
• a third separator 93 is provided downstream of the sixth heating means 26.
• Each separation is preceded by preheating so that separation can occur.
• the temperature of the mixture at a separator is substantially the temperature of the mixture at the outlet of the preceding heating means.
• This third separator 93 receives the charge, partly vaporized, from this sixth heating means and separates the vaporized portion which is transmitted in the lower part 43 of the column, by means 93a and the liquid part which is supplied at the entrance of the vaporization oven 3.
• the latter consumes less energy to vaporize the part of the mixture that it receives from the separator 93 than to vaporize the entire mixture, as in the installation illustrated in FIG. Figure 1. Now, it is a fossil source energy.
• the supplementary means of preheating 8 makes it possible to fill this deficit.
• this supplementary means 8 uses residual low level thermal energy which are generally lost in a conventional refinery. It is therefore understood that the invention makes it possible to compensate for a reduction in the high level of energy consumption by the use of residual energies which are conventionally lost.
• the vaporized part of the mixture which is introduced into the column 4 at the outlet of the separator may comprise several constituents. This is the case during the distillation of oil in particular.
• FIG. 2 The example illustrated in FIG. 2 is absolutely not limiting.
• a separator or flash may be provided after each heating means of the preheating train 2. This would correspond to providing an additional separator between the fourth and fifth heating means illustrated in FIG. 2.
• the separators used operate adiabatically.
• FIG. 3 represents a variant of the preheating train illustrated in FIG. 1.
• This preheating train 20 comprises preheating means 210 to 290, 300 and 310.
• the preheating train comprises two sub-trains of parallel preheating means that meet.
• the first sub-train comprises preheating means 210, 230, 250, 260, 270 and 290.
• the second preheating sub-train comprises preheating means 220, 240, 260 and 280. These two sub-trains meet in output of the preheating means 290 and 280, the preheating train ending with the preheating means 300 and 310 arranged in series.
• each preheating sub-train could have its own desalination tank.
• the exchangers 210 and 230 are arranged in series.
• the exchanger 210 receives the naphtha stream from the flash 47 (arrow 471).
• the recovery of the naphtha at the outlet of the exchanger 210 is symbolized by the arrow 473.
• the mixture available at the outlet of exchanger 210 is supplied to exchanger 230.
• This uses kerosene from stripper 62 (arrow 621).
• the recovery of kerosene at the outlet of the exchanger 230 is symbolized by the arrow 622.
• the mixture at the outlet of the exchanger 230 is supplied to the desalination tank 5.
• the second preheating sub-train comprises an exchanger 220 corresponding to the condenser of head 46 shown in Figures 1 and 2. It receives the flow of oil symbolized by the arrow 12 and the heating through the vapors from the distillation column 4 (arrow 460). The condensate recovery at the outlet of the exchanger 220 is symbolized by the arrow 461. The mixture at the outlet of the exchanger 220 is also supplied to the desalination tank 5.
• Tank 5 will not be described again.
• the mixture obtained at the outlet of the tank 5 is divided to be fed into each preheating sub-train.
• the part of the mixture symbolized by the arrow 13 is brought into the inlet of the continuation of the first preheating sub-train, while the other part of the flow, symbolized by the arrow 14, is brought into the input of the continuation of the second preheating sub-train.
• the first preheating sub-train therefore still includes exchangers 250, 270 and 290 arranged in series. These three exchangers are arranged in parallel with the other three exchangers of the second preheating sub-train, the exchangers 240, 260 and 280, also arranged in series.
• the exchanger 250 receives as input the mixture symbolized by the arrow 13 and the heating by means of diesel from the stripper 61 (arrow 611).
• the diesel recovery at the outlet of the exchanger 250 is symbolized by the arrow 612.
• the mixture available at the outlet of the exchanger 250 is sent to the exchanger 270 which heats it by means of the gas oil recovered at the outlet of the exchanger 300.
• the supply of the diesel fuel to the exchanger 270 is symbolized by the arrow 602.
• the diesel fuel recovered at the outlet of the exchanger 270 is symbolized by the arrow 603.
• the mixture at the outlet of the exchanger 270 is supplied to the exchanger 290 which heats it by means of the flow of residue coming from the exchanger 310 and symbolized by the arrow 490.
• the recovery of the residue at the outlet of the exchanger 290 is symbolized by the arrow 491.
• the exchanger 240 of the second preheating sub-train receives as input the mixture symbolized by the arrow 14 and the heater by the flow flowing in the means 71.
• the mixture obtained at the outlet of exchanger 240 is supplied to exchanger 260 which uses the flow flowing in means 72 to heat it.
• the mixture available at the outlet of the exchanger 260 is supplied to the exchanger 280 which heats it by means of the flow flowing in the means 73.
• the means 71 to 73 are the first, second and third lateral recirculations described with reference to FIGS. 1 and 2.
• the mixtures available at the outlet of exchangers 290 and 280 are supplied to exchanger 300.
• the two preheating sub-trains first arranged in parallel, meet at this exchanger 300.
• the diesel recovery at the outlet of the exchanger 300 is symbolized by the arrow 602.
• the gas oil recovered at the outlet of exchanger 300 is supplied at the inlet of exchanger 270.
• the mixture available at the outlet of exchanger 300 is supplied to the last exchanger 310 of the preheating train. This heats the mixture with the residue from the bottom of the distillation column (arrow 49).
• Figure 3 shows that the preheating train can be made to use all the products from the distillation of oil. It can, moreover, be realized in a rather complex manner.
• FIG. 4 illustrates a preheating train of an installation according to the invention, this preheating train being produced from that illustrated in FIG.
• a complementary heating means 80 is advantageously provided upstream of the second preheating sub-train.
• this additional heating means 80 receives as input the portion of the crude oil stream, symbolized by the arrow 12.
• the oil flow heated by this means 80 is then fed to the inlet of the preheating means 220 of the second preheating sub-train.
• this additional heating means 80 thus only heats a portion of the oil flow fed to the preheating train inlet.
• the additional heating means 8 is intended to heat the entire flow of oil that feeds the preheating train.
• this means 80 is located upstream of the second preheating sub-train and in parallel with the first preheating sub-train.
• this complementary heating means 80 preferably consists of a heat exchanger or of several exchangers arranged in series and / or in parallel, these exchangers using the low-level residual energies. thermal energy from the facility or the rest of the refinery, whose temperature is less than 100 0 C. It is therefore understood that this means 80 is necessarily placed upstream exchangers that use higher temperature energies.
• This means 80 has the advantages that have been described for the means 8.
• the preheating train according to the invention differs from that illustrated in FIG. 3 by the presence of several liquid / vapor separators referenced 910 to 970.
• the first separator 910 is located downstream of the heating means 250 located in the first preheating sub-train.
• the vaporized portion of the mixture available downstream of the heating means 250, is transmitted by the means 910a directly to the column 4. Furthermore, the liquid portion of the mixture is returned to the inlet of the preheating means 270.
• Another separator is located downstream of this preheating means 270, whereby the already depleted charge of the vaporized portion of the mixture has also been partially vaporized.
• the separator 920 extracts this vaporized portion of the charge to bring it, through the means 920a, to the column 4.
• the liquid portion of the load, depleted by two times, is then fed to the heating means 290.
• Another separator 930 is provided downstream of the heating means 290. It will be described later.
• the two separators 940 and 950 present in the second preheating sub-train will be described more succinctly.
• the separator 940 is placed between the outlet of the heating means 240 and the inlet of the heating means 260.
• the vaporized portion of the mixture from the heating means 240 is extracted by the separator 940 and fed, by the means 940a, to the column 4.
• the separator 950 is placed between the heating means 260 and 280. It makes it possible to extract the vaporized part of the mixture delivered by the heating means 260 to bring it, by means 950a, to the column 4.
• the mixtures available at the outlet of the exchangers 290 and 280 are supplied to the separator 930.
• this separator extracts the vaporized part of the mixture resulting from these two heating means to bring it, by means 930a, to the column 4.
• the liquid portion of the mixture, at the outlet of the separator 930, is returned to the inlet of the exchanger 300.
• Another separator 960 is provided between the exchangers 300 and 310.
• the separator 960 extracts the vaporized portion of the feedstock from the exchanger 300 and feeds it through the means 960a to the column.
• a last separator 970 is provided at the outlet of the exchanger 310. This separator extracts the vaporized part of the mixture delivered by the exchanger 310 to bring it, through means 970a, to the column.
• the liquid part of the mixture is fed to the inlet of the vaporization oven 3.
• FIG. 4 shows that certain separators may be common to exchangers located in parallel in the train of preheating. This is the separator 930 which is common to the exchangers 290 and 280.
• the fossil fuel economy can exceed 40 kJ / kg of distilled petroleum at the level of the vaporization furnace. compared to the installation according to FIG.
• the separators 910 to 930 return vapors to the distillation column and cause internal cooling of the column.
• the flow rate of the lateral recirculations is reduced, for example in comparison with the flows generated in the installation illustrated in FIG. 3.
• the part of the mixture preheated in the second preheating sub-train therefore receives a reduced energy input.
• the complementary preheating means 80 makes it possible to fill this deficit, by using residual energies which are usually lost, therefore without additional cost.
• the separation step causes internal cooling of the distillation column and the heat deficit generated in step a) by reducing the flow of the lateral recirculation is compensated by the supply of residual energy during preheating.
• the addition of liquid / vapor separators in the preheating train makes it possible to separate some of its lighter components from the mixture before it is supplied to the steamer. As a result, the number of components of the filler fed to the vaporization furnace is reduced. This results in a reduction in the energy consumed by the steamer to vaporize the charge as well as a reduction in CO 2 emissions.
• the cost of installing, maintaining and controlling a flash type separator is relatively low.
• the process according to the invention does not involve significant additional cost at the distillation plant.
• This method can be easily implemented with already existing installations, since the hardware modifications are reduced and easy to achieve. Indeed, this adaptation does not involve any major modification of equipment, the operation and control of conventional processes being maintained.
• the process according to the invention is very flexible since it can be adapted to any type of multicomponent mixture and in particular to any type of oil, according to its more or less heavy nature.
• the process according to the invention also makes it possible to reduce the amount of driving water vapor which is injected at the bottom of the distillation column.
• the size of the heating means can be reduced. Indeed, in a heat exchanger, for example, the necessary exchange area is less important. It will be the same for the vaporization furnace and possibly the distillation column.

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• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Physics & Mathematics (AREA)
• Thermal Sciences (AREA)
• Engineering & Computer Science (AREA)
• General Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

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• 2009
  • 2009-04-16 FR FR0901851A patent/FR2944452B1/fr not_active Expired - Fee Related
• 2010
  • 2010-04-15 WO PCT/FR2010/000307 patent/WO2010119189A1/fr active Application Filing
  • 2010-04-15 EP EP10718237A patent/EP2419186A1/de not_active Withdrawn

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