EP2451903B1 - Verfahren zur entschwefelung olefinhaltiger einsatzstoffe durch regelung des olefinanteils - Google Patents

Verfahren zur entschwefelung olefinhaltiger einsatzstoffe durch regelung des olefinanteils Download PDF

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Publication number
EP2451903B1
EP2451903B1 EP10739852.1A EP10739852A EP2451903B1 EP 2451903 B1 EP2451903 B1 EP 2451903B1 EP 10739852 A EP10739852 A EP 10739852A EP 2451903 B1 EP2451903 B1 EP 2451903B1
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EP
European Patent Office
Prior art keywords
olefin
stream
proportion
feed stream
regulating
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Application number
EP10739852.1A
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German (de)
English (en)
French (fr)
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EP2451903A2 (de
Inventor
Thilo Von Trotha
Frank Urner
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ThyssenKrupp Industrial Solutions AG
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ThyssenKrupp Industrial Solutions AG
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Priority to PL10739852T priority Critical patent/PL2451903T3/pl
Publication of EP2451903A2 publication Critical patent/EP2451903A2/de
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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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1088—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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/207—Acid gases, e.g. H2S, COS, SO2, HCN
    • 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
    • C10G2300/80—Additives
    • C10G2300/802—Diluents

Definitions

  • the invention relates to a process for the hydrogenation of olefin- and sulfur-containing material streams, as often occur, for example, in petroleum refineries.
  • the sulfur compounds contained in these streams are completely or partially converted into hydrogen sulfide by hydrogenation in a reactor and the olefins contained in these streams are completely or partially converted into alkanes by hydrogenation.
  • the regulation of the process and in particular the temperature distribution in the reactor is achieved by controlling the olefin content in the feed streams to be fed into the reactor.
  • the WO 2009/071180 A1 describes a process for the hydrogenation of olefin-containing streams which contain organic sulfur compounds and which are converted into hydrogen sulfide during the hydrogenation.
  • the hydrogenation allows the sulfur compounds to be removed from the material flow used by removing the hydrogen sulfide from the product gas as a mixture of substances obtained by gas scrubbing after the hydrogenation.
  • the feed streams are passed through a reactor which contains a plurality of successive catalyst beds in the gas flow direction in which a successive hydrogenation is carried out.
  • the feed streams are typically a gas or a vaporized liquid.
  • Behind each catalyst bed there is an inlet device for a further feed stream, with which further feed stream can be passed into the gas stream in the reactor. Since the catalyst beds and the gas stream in the reactor heat up again after each hydrogenation step, the temperature distribution in the reactor can be controlled by distributing the feed stream downstream of the individual catalyst beds. The addition of fresh feed stream after the respective catalyst bed cools the feed stream down again.
  • the invention solves this problem by adding feed streams which contain precisely regulated olefin proportions. Since the gas stream and the catalyst bed in the reactor are only heated by the heat of reaction of the hydrogenation reaction of the olefins, the temperature distribution in the reactor can be regulated by adding feed streams with different olefin content.
  • a feed stream is always to be understood as a gaseous material stream.
  • Part of the total amount of olefin is fed in via the top of the reactor.
  • the temperature at the top of the reactor is usually about 300 ° C., at which the hydrogenation reaction can be carried out well.
  • the proportion of olefins in the first olefin-containing feed stream can advantageously be regulated by adding a low-olefin or an olefin-free diluent stream or both diluent streams to the first feed stream. This results in an olefin-containing feed stream.
  • the low-olefin and olefin-free feed streams can be added as a mixture, it being possible for these substances to be added separately in two separately regulated streams or in premixed form. By adding these two substance mixtures as diluent streams, it is then possible to set the desired proportion of olefins in the feed stream and, moreover, to control the temperature in the reactor. It is also possible, depending on the desired procedure, to introduce a further stream which contains a low-olefin or an olefin-free gas into the feed stream. The feed stream can then be further diluted in this way.
  • the proportion of olefins in the first feed stream can also be increased by separately adding an olefin-rich stream to the first feed stream. In principle, the first feed stream used already contains olefins.
  • a low-olefin and an olefin-free stream are added as a dilution stream to the first feed stream.
  • the hydrogenation can be controlled via the olefin content in this stream so that it delivers a precisely defined amount of heat.
  • the temperature downstream of the first catalyst bed is set in such a way that, when mixed with the second feed stream, it delivers precisely the temperature that is required for passage through the second catalyst bed.
  • olefin-rich stream into the feed stream, if this appears necessary, so that the proportion of olefins in the first feed stream is increased. This can be done temporarily or permanently.
  • the olefin-rich stream can be added separately or premixed with another stream.
  • an olefin-free, low-olefin and olefin-rich stream can be added separately to the first feed stream, so that this regulates the proportion of olefins in the first feed stream.
  • a premix of these streams can also be metered in. The premixing can take place in any combination and in any proportion.
  • the reactor can also contain more than two catalyst beds.
  • the material flow obtained in the reaction is passed through a third catalyst bed, whereby this and the gas flow passed through are heated. This means that after the second catalyst bed, a third feed stream is added laterally behind the second catalyst bed into the reactor to the material stream heated by the second hydrogenation and the gas stream for hydrogenation flows through a third catalyst bed after passing through the second catalyst bed.
  • a third feed stream is added laterally behind the second catalyst bed into the reactor to the material stream heated by the second hydrogenation, and the material stream for the hydrogenation flows through a third catalyst bed after being passed through the second catalyst bed. It is possible to pass the stream obtained after passing through the third partial amount of the hydrogenating desulfurization catalyst through a further or several further partial amounts of a hydrogenating desulfurization catalyst and to add a further feed stream into the reactor laterally behind the catalyst beds.
  • a low-olefin and an olefin-free stream are likewise fed into the feed line for the second feed stream behind the first catalyst bed.
  • the proportion of olefins in this second feed stream can also be controlled through the admixture of the individual streams. This in turn makes it possible to control the temperature in the third catalyst bed.
  • the olefin-free gas is preferably hydrogen, methane or a mixture of these substances.
  • the low-olefin gas is also preferably a gas which contains hydrogen or methane or both as the main component.
  • a different gas can be, for example, alkanes or carbon dioxide.
  • the olefin-rich, the olefin-poor or the olefin-free stream can be mixed as desired. They also advantageously do not contain any undesired foreign gases.
  • the feed stream is preferably fed to the hydrogenation reaction via the top of the reactor.
  • the proportion of the gas fed in via the top can in principle be as desired, but is preferably 1 to 99 percent by mass. Ideally, the flow rate of the gas fed in overhead is 5 to 15 percent by mass.
  • a feed stream can be obtained which contains a proportion of organic sulfur compounds of less than 100 ppb.
  • the hydrogen sulfide can be removed by a subsequent gas scrub, so that an essentially sulfur-free gas is obtained.
  • the feed stream as feed stream for the hydrogenating desulphurization contains light olefins which are in gaseous form at the use temperature. These are in the C number range from 2 to 6.
  • the hydrogenation reaction is carried out at a temperature of 250 to 400 ° C.
  • the feed stream is therefore preferably fed into the reactor at a temperature of 200 to 400.degree.
  • the feed stream is fed into the reactor at a temperature of 250.degree. C. to 350.degree.
  • the respective temperature in the reactor then results from the corresponding reaction procedure.
  • the reaction mixture cools down.
  • the pressure in the reactor can be controlled much better. This is 0.1 to 10 MPa for a favorable type of design.
  • the heating of the feed stream to the temperature necessary for the reaction can take place at will. This can take place, for example, using burners or steam heating devices.
  • the feed stream is preferably heated via heat exchangers. This can be done anywhere.
  • the heated material flow in the reactor can serve as the heating medium for this.
  • the heat exchangers can be heated at any point. This can be done, for example, on the individual feed streams. However, this can also take place on the material flows that are added to the feed flows. This can also be done on the feed stream that is fed into the reactor head.
  • the process for hydrogenating desulfurization is followed by gas scrubbing or a separation for hydrogen sulfide.
  • gas scrubbing or a separation for hydrogen sulfide This can be of any type and can be carried out at any point in the process.
  • the process for hydrogenating desulphurization is followed by an adsorption process with a chemical adsorbent.
  • feed lines that enable an olefin-rich stream to be fed into the corresponding feed stream.
  • This can be a feed line with which an olefin-rich stream is fed into the feed stream.
  • the olefin content in the feed stream increases and the temperature in the subsequent catalyst bed increases accordingly.
  • these can also be feed lines for a low-olefin or olefin-free stream in order to reduce the olefin content of the feed streams accordingly.
  • the feed lines for material flows can be located at any point on the reactor or in the feed lines for the feed streams. These can also be present in any combination.
  • the proportion of olefins in the feed streams can be precisely metered.
  • the temperature in the reactor can also be precisely controlled.
  • a device for dividing the feed flow is located directly on the feed line for the fresh feed.
  • the device also includes valves with which the supply of the gas to the individual injection or injection devices in the reactor can be precisely controlled. Depending on the heating of the gas in the individual catalyst beds, the amount of substance supplied is then dosed. In this way, the temperature in the reactor can be kept within the prescribed temperature limits.
  • the amount fed and the composition of the feed stream into the reactor are preferably controlled via the temperature as a parameter. Therefore, temperature sensors or thermometers can be located anywhere in the reactor. Heating devices or cooling devices with which the temperature can additionally be regulated can also be located at any point in the device. Of course, the device also includes the control devices required for control, regardless of whether they are electrical, electronic or mechanical in nature.
  • the amount and composition of the supplied material flow can also be regulated via other signals, for example via the sulfur or olefin content of the gas or a combination of these measured values. For this purpose, measuring sensors can be located at any point in the supply lines or in the reactor.
  • the device is in principle already in the patent DE 102007059243 A1 shown. This differs from the present device in particular through the additional pipelines for olefin-containing feed streams. Furthermore, in the context of the present invention, the international application with the publication number WO 2008/148081 to get expelled.
  • the device can furthermore comprise devices at any point which are necessary to maintain optimal operation. These can be, for example, valves, pumps, gas distributors or gas delivery devices. However, these can also be sensors, thermometers, flow meters or analytical devices. These can be located anywhere in the device.
  • the method according to the invention and the device allow the hydrogenating desulfurization of olefin-containing gases with little equipment and without complex cooling or heating devices.
  • the desulfurization is effective, so that the sulfur content of the feed stream in the subsequent gas scrubbing can be reduced to the ppb range (ppb: parts per billion, 10 -7 mol percent).
  • the method allows reliable and safe temperature control and handling of the method.
  • the process according to the invention results in a product gas which essentially only contains hydrogen sulfide as a sulfur compound.
  • FIG. 1 shows an example of a reactor with three catalyst beds for carrying out hydrogenation desulphurisation.
  • the feed stream (1) is divided into three feed streams (3, 4, 5) by a gas distributor (2) .
  • the feed stream usually already contains the necessary amount of olefins.
  • three valves (3a, 4a, 5a) are installed to regulate the feed flow.
  • the first feed stream (3) is preheated with a heating device (6) or a heat exchanger (with heat flow, 6a) and introduced into the reactor (7) via the reactor head (3b) (8a).
  • the temperature when the first stream is introduced is 300 ° C.
  • the first feed stream meets the first catalyst bed (8) there and is heated there.
  • the catalyst bed (8) contains the catalyst (8b) on suitable carrier particles and a grid (8c) or another suitable holding device.
  • the temperature at the outlet at the lower grid floor for the first catalyst bed (8) can be up to 390 ° C, but is typically 370 ° C.
  • the temperature in this first catalyst bed is regulated via the flow rate of the first feed stream (3b).
  • the first catalyst bed (8) is heated by a higher proportion of olefins in the first feed stream.
  • the olefin fraction can in turn be regulated via various streams (9a, b, c) , which are passed into the first feed stream (3) here, for example, as a diluent gas stream.
  • a further dilution stream (4) is introduced into a second feed stream (10a) after the first catalyst bed (8) without further regulation.
  • the material flow cools down again, ideally to 300 ° C.
  • This stream thus meets the second catalyst bed (10) with catalyst (10b) on a holding device (10c).
  • the stream of material is heated up again by the hydrogenation reaction.
  • a further feed stream (11a) is then introduced downstream of the catalyst bed (8) .
  • the resulting stream then meets a third catalyst bed (11) with catalyst (11b) .
  • the catalyst is held in the reactor by grids (8c, 10c, 11c) or other holding devices.
  • a product gas (12) is obtained which essentially only contains hydrogen sulfide as a sulfur compound.
  • the product gas is discharged (13) at the end of the reactor (7 ).
  • the first feed stream (3b ) is preheated here, for example, via a heat exchanger (6) .
  • the thermal energy of the feed stream (1) is also used (14a) to preheat the low-olefin material stream (9b) via a heat exchanger (14) , which is fed into the first feed stream (3) .
  • the feed stream (3) can, if necessary, be further heated via a further heat exchanger (14b) to set the temperature.
  • the individual material flows (9a, b, c) can be regulated via valves (15a, b, c) . Typical reactor temperatures are indicated on the side.

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
EP10739852.1A 2009-07-10 2010-07-07 Verfahren zur entschwefelung olefinhaltiger einsatzstoffe durch regelung des olefinanteils Active EP2451903B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL10739852T PL2451903T3 (pl) 2009-07-10 2010-07-07 Sposób odsiarczania surowców zawierających olefiny przez regulowanie udziału olefin

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102009032802A DE102009032802A1 (de) 2009-07-10 2009-07-10 Verfahren zur Entschwefelung olefinhaltiger Einsatzstoffe durch Regelung des Olefinanteils
PCT/EP2010/004092 WO2011003585A2 (de) 2009-07-10 2010-07-07 Verfahren zur entschwefelung olefinhaltiger einsatzstoffe durch regelung des olefinanteils

Publications (2)

Publication Number Publication Date
EP2451903A2 EP2451903A2 (de) 2012-05-16
EP2451903B1 true EP2451903B1 (de) 2020-09-02

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EP10739852.1A Active EP2451903B1 (de) 2009-07-10 2010-07-07 Verfahren zur entschwefelung olefinhaltiger einsatzstoffe durch regelung des olefinanteils

Country Status (14)

Country Link
US (1) US20130030235A1 (https=)
EP (1) EP2451903B1 (https=)
CN (1) CN102471703B (https=)
CA (1) CA2767397A1 (https=)
CO (1) CO6612178A2 (https=)
DE (1) DE102009032802A1 (https=)
DK (1) DK2451903T3 (https=)
EA (1) EA028944B1 (https=)
IN (1) IN2012DN01106A (https=)
MX (1) MX2012000429A (https=)
MY (1) MY172046A (https=)
PL (1) PL2451903T3 (https=)
WO (1) WO2011003585A2 (https=)
ZA (1) ZA201200993B (https=)

Families Citing this family (1)

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Publication number Priority date Publication date Assignee Title
US10597593B2 (en) * 2016-10-07 2020-03-24 Haldor Topsoe A/S Process for hydrotreatment of a fuel gas stream containing more than 4% olefins

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GB104771A (en) * 1916-04-04 1917-03-22 Augustus Bever Improvements in Explosive Projectiles.
GB1044771A (https=) 1963-04-02 1900-01-01
US3506567A (en) 1966-08-04 1970-04-14 Standard Oil Co Two-stage conversion of nitrogen contaminated feedstocks
US3983029A (en) 1973-03-02 1976-09-28 Chevron Research Company Hydrotreating catalyst and process
US4017382A (en) * 1975-11-17 1977-04-12 Gulf Research & Development Company Hydrodesulfurization process with upstaged reactor zones
NL191763C (nl) * 1979-09-26 1996-07-02 Shell Int Research Werkwijze voor ontmetalliseren van een koolwaterstofolie.
CA2614020C (en) 2005-07-04 2014-02-11 Neste Oil Oyj Process for the manufacture of diesel range hydrocarbons
ES2550259T5 (es) * 2005-07-04 2023-06-08 Neste Oyj Proceso para la fabricación de hidrocarburos en el intervalo del diésel
AR066682A1 (es) * 2007-05-25 2009-09-02 Shell Int Research Un proceso para remover azufre a partir de sendas corrientes de gas de combustible, menos reactivas y mas reactivas que contienen azufre organico y olefinas livianas
DE102007059243A1 (de) 2007-12-07 2009-06-10 Uhde Gmbh Verfahren zur Entschwefelung olefinhaltiger Einsatzstoffe
US9279087B2 (en) * 2008-06-30 2016-03-08 Uop Llc Multi-staged hydroprocessing process and system
DE102008059243A1 (de) 2008-11-21 2010-05-27 Newfrey Llc, Newark Fügebauteil und Verfahren zum Herstellen eines Fügebauteils
ES2385693T3 (es) * 2009-03-04 2012-07-30 IFP Energies Nouvelles Procedimiento para la hidrogenación continua de materias primas que contienen triglicéridos

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Also Published As

Publication number Publication date
CO6612178A2 (es) 2013-02-01
MX2012000429A (es) 2012-06-08
ZA201200993B (en) 2012-09-26
PL2451903T3 (pl) 2021-03-08
EA201290030A1 (ru) 2012-07-30
DE102009032802A1 (de) 2011-01-13
MY172046A (en) 2019-11-12
CA2767397A1 (en) 2011-01-13
CN102471703A (zh) 2012-05-23
WO2011003585A2 (de) 2011-01-13
WO2011003585A3 (de) 2011-06-16
DK2451903T3 (da) 2020-11-23
CN102471703B (zh) 2015-12-16
US20130030235A1 (en) 2013-01-31
IN2012DN01106A (https=) 2015-04-10
EP2451903A2 (de) 2012-05-16
EA028944B1 (ru) 2018-01-31

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