EP3417035B1 - Procédé de désulfuration d'un mélange hydrocarboné - Google Patents

Procédé de désulfuration d'un mélange hydrocarboné Download PDF

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Publication number
EP3417035B1
EP3417035B1 EP17720561.4A EP17720561A EP3417035B1 EP 3417035 B1 EP3417035 B1 EP 3417035B1 EP 17720561 A EP17720561 A EP 17720561A EP 3417035 B1 EP3417035 B1 EP 3417035B1
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EP
European Patent Office
Prior art keywords
sodium
reactor
hydrocarbon mixture
dispersion
oil
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
EP17720561.4A
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German (de)
English (en)
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EP3417035A1 (fr
Inventor
Christian HÖLSCHER
Klaus Seikel
Edgar Bilger
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Na+s GmbH
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Na+s GmbH
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Publication date
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Priority to PL17720561T priority Critical patent/PL3417035T3/pl
Publication of EP3417035A1 publication Critical patent/EP3417035A1/fr
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Publication of EP3417035B1 publication Critical patent/EP3417035B1/fr
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Classifications

    • 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
    • C10G19/00—Refining hydrocarbon oils in the absence of hydrogen, by alkaline treatment
    • C10G19/073—Refining hydrocarbon oils in the absence of hydrogen, by alkaline treatment with solid alkaline material
    • 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
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/04—Metals, or metals deposited on a carrier
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/10—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including alkaline treatment as the refining step in the absence of hydrogen
    • 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
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P

Definitions

  • the invention relates to a process for the desulfurization of a hydrocarbon mixture containing organic sulfur compounds according to the preamble of claim 1.
  • a disadvantage of this process is that as the sulfur content decreases, the hydrogen requirement for removing the sulfur increases disproportionately to the amount of sulfur removed. This is because some sulfur compounds are less reactive than others in terms of the chemical reactions that play a role in hydrodesulfurization. At the same time, however, other side reactions occur in which hydrogen is consumed. Examples can be the conversion of unsaturated to saturated hydrocarbons or the splitting of hydrocarbons to form hydrocarbons with a higher hydrogen / carbon ratio. Accordingly, the cost of hydrodesulfurization trying to keep the lowest possible To reach residual sulfur levels in the hydrocarbon mixture disproportionately.
  • the invention is therefore based on the object of demonstrating a desulfurization process of the type mentioned at the outset which can be sensibly implemented on an industrial scale.
  • the object is achieved by a generic method for the desulfurization of a hydrocarbon mixture containing organic sulfur compounds with the characterizing features of claim 1.
  • the object is achieved in that the reactor in which the reaction takes place is a turbulent-flow reactor, preferably a tubular reactor.
  • a plug reactor with an internal oscillating is preferred driven transport screw are used, in which it is ensured by appropriate technical devices that a turbulent flow arises and the design ensures a sufficient residence time of the hydrocarbon mixture to be desulfurized.
  • the reaction parameters can be set in a reactor, preferably a tubular reactor or a plug reactor, with turbulent flow such that an extremely low residual sulfur content can be achieved when a mixture of a sodium dispersion and a hydrocarbon mixture is passed through this reactor.
  • residual sulfur content refers to the sulfur which is still present in the form of organic sulfur compounds after the reaction has been carried out. It is understood that for the final removal of the sulfur by sodium, in particular inorganic, preferably in the form of Na2S, bound sulfur still has to be separated from the mixture with the sodium. A number of separation processes known from the prior art are available for this.
  • the tubular reactor Due to the turbulent flow in the reactor, preferably in the tubular reactor or in the plug reactor, sufficient mixing of the reaction mixture can be generated in order to be able to carry out the reaction until low residual sulfur contents are reached, in order to ensure economical desulfurization.
  • the tubular reactor has a corresponding length for this. This is preferably at least 100 m, more preferably at least 200 m. It has been shown that with these very long pipe lengths, suitable flow conditions can be realized with a corresponding sufficient dwell time in order to successfully carry out the process on an industrial scale.
  • the tube of the tubular reactor does not have to be straight, it can rather have a meandering, coiled or similar course, in particular in order to enable a space-saving construction of the reactor.
  • the reaction tube of the tube reactor can of course also be composed of a plurality of tubes.
  • the length of the tube reactor therefore means the effective length of the flow path through the tube reactor, which in the present case the medium flowing through the mixture of sodium dispersion and hydrocarbon mixture under reaction conditions.
  • Appropriate technical devices such as the oscillating drive, the turbulent flow and the dwell time are used in the plug reactor guaranteed, and can be regulated if necessary by the speed control of the screw conveyor and / or the duration of the oscillations.
  • the reactor can advantageously have internals to promote mixing. Such internals are helpful in order to ensure turbulent flow and the associated mixing, which promotes the reaction rate.
  • the reactor can particularly preferably have so-called static mixers, that is to say immovable internals which, due to their geometry, influence the flow accordingly.
  • the temperature in the reactor is at least 250 ° C. It is also advantageous if the temperature in the reactor does not exceed 310 ° C. It has been shown that there are particularly favorable conditions for the desired chemical reactions in this temperature range.
  • the volume-equivalent spherical diameter of at least 80%, preferably at least 90% of the sodium particles in the dispersion is at most 25 ⁇ m, preferably at most 12 ⁇ m and particularly preferably at most 5 ⁇ m. It has been shown that a sodium dispersion which is both very fine and has the narrowest possible spectrum of particle distribution is particularly advantageous with regard to the reaction rate.
  • the volume-equivalent spherical diameter of a sodium particle is the diameter that a spherical sodium particle of the same volume would have. Due to the low melting point of sodium, this is regularly in liquid form under reaction conditions, as a result of which the sodium particles actually form a spherical shape.
  • the volume-equivalent sphere diameter is ideal for clearly characterizing the particle size in the suspension. It is also particularly advantageous if at least 90%, preferably at least 95%, of the sodium particles have a volume-equivalent spherical diameter that is less than 5 ⁇ m.
  • the production of the sodium dispersion according to the rotor-stator principle has proven to be particularly advantageous with regard to the method according to the invention.
  • dispersing devices are used in which the dispersion is generated by a relative movement between a rotor and a stator at a high peripheral speed. It has been found that sodium dispersions produced by such a dispersion process in particular have very narrow particle size distributions and are particularly suitable for the process according to the invention.
  • the sodium for the preparation of the sodium dispersion is dispersed in an oil, which can be a paraffinic white oil in a particularly advantageous manner. It has been shown that dispersions of sodium in such liquid phases are particularly advantageous for the process according to the invention.
  • Particularly high levels of desulfurization can be achieved in particular if the proportion of sodium in the dispersion is 1 to 40% by weight, preferably 10 to 33% by weight, based on the total weight of the dispersion. It is particularly advantageous for desulfurization if 1 to 40% by weight of sodium is dispersed in oil and preferably at least 80% of the sodium particles have a volume-equivalent spherical diameter which is less than 25 ⁇ m. It is further preferred if 10 to 33% by weight of sodium is dispersed in white oil and preferably at least 90% of the sodium particles have a volume-equivalent spherical diameter which is less than 12 ⁇ m, preferably less than 5 ⁇ m. The best results for desulfurization can be achieved under the aforementioned conditions.
  • the liquid phase which is used for dispersing the sodium preferably has a viscosity of at least 4 mm 2 / s, particularly preferably at least 12 mm 2 / s, and / or at most 20 mm 2 / s, particularly preferably at most 17 mm 2 / s s.
  • the density of the liquid phase used for the dispersion is preferably at least 0.84 kg / l and or at most 0.89 kg / l.
  • the liquid phase used to disperse the sodium has a flash point of at least 150 ° C., preferably at least 200 ° C.
  • the hydrocarbon mixture to be desulfurized is first treated with a further desulfurization process for the pre-desulfurization. Desulphurization then takes place later by treatment with a desulphurization process according to the invention.
  • This procedure has the advantage that the advantages of conventional desulfurization processes, in particular hydrogenating desulfurization processes, can be combined with the advantages of desulfurization with a sodium dispersion. It makes sense to first remove that part of the sulfur that can still be removed comparatively easily with a hydrogenating desulfurization process. This will remove most of the sulfur. The process based on the sodium dispersion is then used to further reduce the residual sulfur content.
  • the desulfurization by means of the sodium dispersion does not have to directly and directly follow the preferably hydrodesulfurization. It is entirely possible in the meantime to subject the resulting hydrocarbon mixture to further process steps, to separate parts of the hydrocarbon mixture or to mix the hydrocarbon mixture with other substances, in particular other hydrocarbon mixtures. This also applies accordingly to the sequence between the preparation of the dispersion and the addition of the sodium dispersion to the hydrocarbon mixture to be desulfurized.
  • the process variants described above for producing the sodium dispersion have the advantage that the sodium dispersion is correspondingly stable, ie it can easily stored or transported between production sites before it is added to the hydrocarbon mixture.
  • the hydrocarbon mixture to be desulfurized is a fuel or a fraction of a hydrocarbon mixture intended for further processing into a fuel.
  • mineral oil fractions for specific later uses for example the production of diesel fuels - are separated from each other at an early stage and processed further using different process routes.
  • the fractions used for the use of diesel and / or petrol have a certain proportion of low boilers.
  • the pressure in the reactor is at least 6 bar, preferably at least 8 bar. In this way, a reliable conversion can also be carried out, in particular, of low-boiling constituents in the liquid phase.
  • Another advantageous process variant provides that the pressure in the reactor is at most 3 bar, preferably at most 1.5 bar.
  • This process variant is particularly advantageous when the proportion of low boilers in the hydrocarbon mixture is low. Such operation is particularly advantageous when comparatively small and compact systems can be used. Due to the low pressure, the material stresses decrease, in particular the comparatively long tubular reactors can be designed much thinner, which has an extremely positive effect with regard to the size and weight of the plant.
  • the process according to the invention can be used particularly advantageously, in particular in comparatively compact plants, for the desulfurization of hydrocarbon mixtures which originate from a liquefaction process for the recovery of liquid hydrocarbons from solids.
  • Such methods are used in particular when liquid hydrocarbon mixtures for use as fuels are to be obtained from waste.
  • Low-boiling components often play a subordinate role in these mixtures, whereas the possibility of constructing inexpensive and / or compact plants often represents a considerable economic advantage.
  • Slop oil is a contaminated mixture containing mineral oil, which occurs, for example, and especially when rinsing tanks on ships.
  • mineral oil which occurs, for example, and especially when rinsing tanks on ships.
  • These can be, for example, the tanks of mineral oil tankers, but also fuel tanks of ships operated in particular with heavy oil. Cooling circuits and the like on ships of this type, in particular in the area of ship engines, are regularly not completely sealed, so that sea water and other contaminants, including marine life and the like, penetrate into the tanks in question and in the tanks to form the so-called slop oil as residue that is difficult to recover.
  • slop oil and / or products which are obtained from a process for the preparation of slop oil in particular a process in which the first constituents of the slop oil are already separated off, can be treated particularly well using the desulfurization process according to the invention.
  • the invention is described below with reference to Fig. 1 exemplified schematically.
  • a hydrocarbon mixture 1 is provided, which originates, for example, from a liquefaction process for the extraction of liquid hydrocarbons or a processing process of slop oil (or a mixture thereof). Furthermore, sodium 2 is dispersed with an oil 3 in the example shown in a process step S1. Dispersion based on the rotor-stator principle is preferably used for this. A paraffinic white oil is preferably used as the oil 1. In a further step S2, the sodium dispersion that was produced in step S1 and the hydrocarbon mixture 1 are mixed.
  • the reaction step S3 is preferably carried out in a tubular reactor with a turbulent flow, the tubular reactor preferably having a length of at least 200 m.
  • the reactor can, for example, be designed in a meandering shape.
  • the use of an oscillating plug reactor with an internal transport screw is advantageous.
  • the process according to the invention occurs in process step S3 underlying chemical reactions, in which the sulfur is dissolved out of the organic sulfur compounds and reacts to inorganic sulfur compounds, in particular to Na2S.
  • step S4 the inorganic sulfur-containing constituents, in particular Na2S 5, formed from the desulfurized hydrocarbon product 4 are separated off.

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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)

Claims (14)

  1. Procédé de désulfuration d'un mélange hydrocarboné contenant des composés organiques soufrés, comprenant les étapes consistant à :
    a) produire une dispersion de sodium
    b) ajouter la dispersion de sodium au mélange hydrocarboné à désulfurer
    caractérisé en ce que le mélange de la dispersion de sodium et du mélange hydrocarboné est dirigé à travers un réacteur, dans lequel les conditions de réaction, en particulier la pression et la température, sont choisies de manière à faire réagir le sodium avec les composés organiques soufrés, où des atomes de soufre se détachent des composés organiques soufrés et se lient au sodium, le réacteur étant un réacteur parcouru par turbulence, de préférence un réacteur tubulaire ou un réacteur à écoulement piston oscillant avec une vis sans fin de transport interne, et la température dans le réacteur est au moins de 250°C et au plus de 310°C.
  2. Procédé selon la revendication 1, caractérisé en ce que le réacteur est un réacteur tubulaire et présente de préférence une longueur d'au moins 100 m, plus préférablement d'au moins 200 m.
  3. Procédé selon la revendication 1 ou 2, caractérisé en ce que le réacteur présente des installations pour transporter le mélange, en particulier des mélangeurs statiques.
  4. Procédé selon une des revendications précédentes, caractérisé en ce que le diamètre des billes équivalant en volume de 90 % des particules de sodium dans la dispersion de sodium, en particulier de 95 % des particules de sodium dans la dispersion de sodium, est inférieur à 25 µm, de préférence inférieur à 5 µm.
  5. Procédé selon une des revendications précédentes, caractérisé en ce que la production de la dispersion de sodium se fait selon le principe du rotor-stator.
  6. Procédé selon une des revendications précédentes, caractérisé en ce que le sodium pour la production de la dispersion de sodium est dispersé dans une huile sous la forme d'une phase liquide, en particulier dans une huile blanche paraffinique.
  7. Procédé selon une des revendications précédentes, caractérisé en ce que la phase liquide utilisée pour la dispersion présente une viscosité d'au moins 4 mm2/s, de préférence d'au moins 12 mm2/s, et/ou d'au plus 20 mm2/s, de préférence d'au plus 17 mm2/s.
  8. Procédé selon une des revendications précédentes, caractérisé en ce que la phase liquide utilisée pour la dispersion présente une densité d'au moins 0,84 kg/l et/ou d'au plus 0,89 kg/1.
  9. Procédé selon une des revendications précédentes, caractérisé en ce que la phase liquide utilisée pour la dispersion présente un point d'inflammation d'au moins 150°C, de préférence d'au moins 200°C.
  10. Procédé selon une des revendications précédentes, caractérisé en ce que le mélange hydrocarboné à désulfurer est d'abord traité pour une pré-désulfuration avec une autre méthode de désulfuration, de préférence hydrogénante, puis avec un procédé de désulfuration selon une des revendications précédentes.
  11. Procédé selon une des revendications précédentes, caractérisé en ce que le mélange hydrocarboné à désulfurer est obtenu à partir d'une méthode de liquéfaction pour obtenir des hydrocarbures liquides à partir de matières solides, en particulier à partir de déchets et/ou est du gasoil et/ou est obtenu à partir d'une méthode de préparation de gasoil, en particulier à partir de processus de nettoyage de réservoirs de bateaux.
  12. Procédé selon une des revendications précédentes, caractérisé en ce qu'au moins 0,05 % en poids de sodium, de préférence au moins 0,1 % en poids de sodium et particulièrement préféré au moins 1,5 % en poids de sodium, est utilisé par rapport au poids total du mélange hydrocarboné à désulfurer.
  13. Procédé selon une des revendications précédentes, caractérisé en ce que la pression dans le réacteur est au maximum de 3 bars, de préférence au maximum de 1,5 bars.
  14. Procédé selon une des revendications 1 à 11, caractérisé en ce que le mélange hydrocarboné à désulfurer est un carburant ou une fraction d'un mélange hydrocarboné définie pour une transformation en un carburant, en particulier d'une huile minérale, et la pression dans le réacteur est au moins de 6 bars, de préférence au moins de 8 bars.
EP17720561.4A 2016-02-19 2017-02-13 Procédé de désulfuration d'un mélange hydrocarboné Active EP3417035B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL17720561T PL3417035T3 (pl) 2016-02-19 2017-02-13 Sposób odsiarczania mieszaniny węglowodorów

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016102933.5A DE102016102933A1 (de) 2016-02-19 2016-02-19 Verfahren zur Entschwefelung eines Kohlenwasserstoffgemisches
PCT/IB2017/000101 WO2017141097A1 (fr) 2016-02-19 2017-02-13 Procédé de désulfuration d'un mélange hydrocarboné

Publications (2)

Publication Number Publication Date
EP3417035A1 EP3417035A1 (fr) 2018-12-26
EP3417035B1 true EP3417035B1 (fr) 2020-07-29

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EP17720561.4A Active EP3417035B1 (fr) 2016-02-19 2017-02-13 Procédé de désulfuration d'un mélange hydrocarboné

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EP (1) EP3417035B1 (fr)
DE (1) DE102016102933A1 (fr)
DK (1) DK3417035T3 (fr)
PL (1) PL3417035T3 (fr)
WO (1) WO2017141097A1 (fr)

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB759283A (en) 1952-12-24 1956-10-17 British Petroleum Co Improvements relating to the refining of petroleum hydrocarbons
US7527724B1 (en) * 2005-11-17 2009-05-05 Trans Ionics Corporation Process for desulfurization of hydrocarbons
MX2009009166A (es) * 2007-02-26 2009-11-26 Trans Ionics Corp Desulfurizacion de corrientes del petroleo utilizando sodio metalico.

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

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Publication number Publication date
PL3417035T3 (pl) 2021-01-25
DE102016102933A1 (de) 2017-08-24
DK3417035T3 (da) 2020-10-12
WO2017141097A1 (fr) 2017-08-24
EP3417035A1 (fr) 2018-12-26

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