EP0609191B1 - Installation pour le craquage thermique d'un mélange d'hydrocarbures liquides et gazeuses - Google Patents

Installation pour le craquage thermique d'un mélange d'hydrocarbures liquides et gazeuses Download PDF

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Publication number
EP0609191B1
EP0609191B1 EP94890007A EP94890007A EP0609191B1 EP 0609191 B1 EP0609191 B1 EP 0609191B1 EP 94890007 A EP94890007 A EP 94890007A EP 94890007 A EP94890007 A EP 94890007A EP 0609191 B1 EP0609191 B1 EP 0609191B1
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
mixture
line
liquid
gas
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.)
Expired - Lifetime
Application number
EP94890007A
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German (de)
English (en)
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EP0609191A1 (fr
Inventor
Peter Dipl.-Ing. Illyes
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.)
OMV Downstream GmbH
Original Assignee
OMV AG
OEMV AG
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by OMV AG, OEMV AG filed Critical OMV AG
Publication of EP0609191A1 publication Critical patent/EP0609191A1/fr
Application granted granted Critical
Publication of EP0609191B1 publication Critical patent/EP0609191B1/fr
Anticipated expiration legal-status Critical
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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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means

Definitions

  • the invention relates to a device for thermal splitting of a mixture with liquid and gaseous hydrocarbons in heat exchangers.
  • gaseous hydrocarbons are also used. These gaseous hydrocarbons come from mostly from the processing facilities according to Splitting plants or production plants for the most varied Product blends. This gaseous Products are usually delivered to the slitting line leading supply lines for the liquid hydrocarbons initiated. As a result, the range of uses of the Plant significantly increased and on the other hand occurs a substantial reduction in piping since parallel pipelines, u. for the gaseous Hydrocarbons and the liquid hydrocarbons, can be avoided.
  • the hydrocarbon mixtures usually need to be in several stages up to the temperature of the thermal Cleavage to be heated.
  • the throughput in each Stages, d. H. the heat exchangers is usually by volume, especially in the first stage, on partial evaporation of liquid hydrocarbons.
  • the device according to the invention for thermal splitting a mixture of liquid and gaseous hydrocarbons, with at least one pipe for that Mixture opens into a heat exchanger, which if necessary with one leading out of the heat exchanger Pipeline through a detour line with one in flow controllable shut-off device is fluidly connected, and the pipeline leading from the heat exchanger into which at least one more pipe for overheated Water vapor flows into another Heat exchanger opens, the output line in one downstream heat exchanger, if necessary with Catalyst, opens, the outlet line in a cooling and Splitting device opens, essentially exists in that seen in the direction of flow before Heat exchanger at least one gas separator for the Separation of a gaseous fraction from the mixture is provided, the detour line being a gas line, which has a shut-off device which can be regulated in the flow, from the gas separator into another heat exchanger, in particular via the further pipeline.
  • the gaseous in front of the first heat exchanger Portion separated from the starting product mixture double supply lines for the liquid or gaseous starting products can be avoided. Furthermore a mixture enters the heat exchanger, which can be essentially gas-free, so that the preferred Heat exchange to the liquid products can take place which due to the higher specific heat of Liquids are particularly effective against gases can.
  • the gas can pass through a gas separator Pipeline either in the further heat exchanger or already opens into the actual cracking furnace, be led.
  • the gas line thus serves as a detour line for the first heat exchanger, which also means the temperature the heat exchange medium, e.g. B. flue gases controlled can be. On the one hand, this allows a particularly high Heat exchange can be achieved, on the other hand one too great cooling, e.g. B. the flue gases, and thus one Falling below the dew point temperature and thus occurring corrosion can be avoided.
  • gas separator is designed as a gravity separator, so can be a simple one without great pressure loss Separation of the gaseous components from the gas / liquid mixture respectively.
  • a particularly effective separation between gas and Liquid can be done via a cyclone.
  • the gas line opens into the gas separator Flow direction seen before the further line for the Water vapor in the outgoing pipe from the heat exchanger, so can already in the further heat exchanger a product mixture of the liquid hydrocarbons, the gaseous hydrocarbons and water vapor occur so that the partial steam lowering in the Heat exchanger is taken into account particularly cheaply, which makes the liquid hydrocarbons particularly quick can evaporate and another high absorption of heat is achieved in this heat exchanger.
  • the gas line flows from the gas separator into the downstream heat exchanger, i.e. in the cracking furnace, especially in the output line from the rest Heat exchanger, so with a particularly large range of gaseous products in the mixture also in the further Heat exchanger a heat transfer without disadvantageous Influencing the gaseous starting products achieved will.
  • the gas line flows from the gas separator into the other Pipe for the water vapor, so a mixture of Water vapor and gaseous products can be achieved in turn then into the supply line for the further Heat exchanger can be initiated.
  • the gas line flows out of the gas separator into one Steam superheater, so the gas along with the water vapor be heated.
  • a shut-off device which can be regulated in the flow, provided by the pipeline after the Gas separator, which opens into the heat exchanger, branches off, and preferably in the further pipeline after the Confluence of the gas pipeline, so can also bursty oversupply of liquid hydrocarbons without pressure overload of the heat exchanger intercepted and controlled if necessary.
  • Heat exchangers can also be used as groups of heat exchangers be constructed.
  • the pipes R 1 and R 2 which conduct liquid hydrocarbons (gasoline) or gaseous hydrocarbons with two to four carbon atoms, lead to the pipe R 3 , which in turn opens into the gas separator G.
  • the liquid products are then passed through the pipe R 3 into the heat exchanger W 1 .
  • the gaseous products from the gas separator G pass through the gas line G 1 , which serves as a detour line for the heat exchanger W 1 , into the pipeline R 4 leading from the heat exchanger W 1 .
  • a steam line D 1 which forwards the steam from the steam superheater D, also opens into this pipeline R 4 .
  • the further heat exchanger W 2 in which the pipeline R 4 opens, is connected via an output line R 5 to the cracking furnace, the downstream heat exchanger S.
  • a pipe R 6 leads from the heat exchanger S into a cooling and separation device K + A.
  • the steam superheater D in which steam is optionally generated, the cracking furnace, the heat exchanger S and the heat exchangers W 1 and W 2 are designed as shell-and-tube heat exchangers, with flue gas serving as the heat transfer medium.
  • a valve V 1 which can be regulated in the flow can be provided in the gas line G 1 and is closed when it is desired that the entire product mixture is passed through the pipe R 3 into the heat exchanger W 1 .
  • a gas line G 2 can also lead into the outlet line R 5 of the heat exchanger W 2 , or, like the gas line G 3, also lead directly into the cracking furnace, the heat exchanger S.
  • These gas lines can have valves V 2 and V 3 which can be regulated in the flow.
  • the gas can be fed via a line G 4 to the steam superheater D or, if appropriate, to a steam generator.
  • a further detour line U 1 can also be provided, which branches off from the pipe line R 3 in front of the heat exchanger W 1 and opens into the pipe line R 4 after the heat exchanger W 1 .
  • This detour line U 1 has a flow controllable valve V 4 .
  • the heat exchangers W 1 and W 2 as well as the steam superheater D and the cracking furnace, the heat exchanger S are successively flowed through by flue gases, which serve as heat exchange medium.
  • the flue gases pass according to arrow X 1 through the cracking furnace, the heat exchanger S, then into a high-pressure steam superheater, not shown, in which high-pressure steam can be generated, which does not have to be fed to the process.
  • the flue gas then enters the steam superheater D according to the arrow X 3, in which process steam is introduced according to the arrow Z.
  • the flue gas From the steam superheater D, the flue gas enters according to the arrow X 4 into the heat exchanger W 2 , from which it can enter a boiler feed water preheater, not shown, which is also not required in the process according to the invention. From this preheating, the flue gas enters the heat exchanger W 1 according to arrow X 6 , from which the flue gases are then fed to the chimney according to arrow X 7 .
  • the arrangement of the heat exchangers is carried out in accordance with the required heat potential, the cracking furnace, the heat exchanger S requiring the highest temperature of the flue gases, whereas the heat exchanger W 1 requires flue gases with a much lower temperature.
  • the gas separator G shown schematically in FIG. 2 has a cylindrical tube 1 which serves as an outer container.
  • the pipeline R 3 into which the product mixture is introduced in liquid and gaseous form, opens into this outer container.
  • the cylindrical tube 1 there is an extreme slowdown in the flow velocity, at the same time a separation of the gaseous and the liquid phase occurs.
  • the liquid phase is discharged via the exiting pipeline R 3
  • the gaseous phase is discharged via the cylindrical pipe 2, which continues into the gas line G 1 , and thus reaches the pipeline R 4 with the valve V 1 open.
  • FIG. 3 there is a cyclone, the pipe R 3 opening tangentially into the conical container 3.
  • the product mixture moves downwards in a spiral along the outer container wall and separates.
  • the liquid phase is withdrawn via the pipeline R 3 located on the bottom, whereas the gaseous phase is withdrawn via the gas line G 1 .
  • the incoming product mixture was heated to 440 ° C in the heat exchanger W 2 .
  • the product mixture heated in this way is then passed through the pipe R 5 with a nominal diameter of 80 mm into the cracking furnace S.
  • the cracking furnace is designed as a heat exchanger in which the mixture has been heated further.
  • a mixture at 855 ° C. emerged from the pipeline R 6 .
  • a gas separator with a gas line G 1 was provided.
  • the product mixture entering the heat exchanger W 1 had a temperature of 60 ° C.
  • heating to 220 ° C occurred.
  • 15 vol .-% of the gaseous phase and no portion of the liquid phase of the product were passed through the gas line G 1 , which was therefore not heated.
  • the product mixture then reached the pipeline R 4 , into which water vapor at 483 ° C. and in an amount of 1,300 kg / h with a nominal width of 80 mm was introduced into the heat exchanger W 2 .
  • the incoming product mixture was heated to 450 ° C in the heat exchanger W 2 .
  • the product mixture heated in this way was then fed into the cracking furnace S via the pipeline R 5 with a nominal diameter of 80 mm. Heating was also carried out in the cracking furnace itself.
  • a mixture at 855 ° C. emerged from the pipeline R 6 .

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (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)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

Claims (8)

  1. Dispositif de craquage thermique d'un mélange d'hydrocarbures liquides et gazeux, dans lequel au moins une canalisation (R3) pour le mélange débouche dans un échangeur de chaleur (W1), canalisation qui éventuellement est reliée de manière à pouvoir conduire des fluides à une canalisation (R4) partant de l'échangeur de chaleur par l'intermédiaire d'un conduit de déviation pourvu d'un organe d'arrêt (V1) réglable quant au débit, la canalisation (R4) qui part de l'échangeur de chaleur (W1) et dans laquelle débouche au moins une canalisation supplémentaire (D1) pour de la vapeur d'eau surchauffée, débouchant à son tour dans un échangeur de chaleur supplémentaire (W2) dont le conduit de sortie (R5) débouche dans un échangeur de chaleur (S) monté en aval, éventuellement avec catalyseur, dont le conduit de sortie (R6) débouche dans un dispositif de refroidissement et de séparation (K+A), caractérisé en ce que, vu dans le sens d'écoulement, au moins un séparateur de gaz est prévu pour la séparation d'une fraction gazeuse à partir du mélange en amont de l'échangeur de chaleur (W1), le conduit de déviation étant un conduit à gaz (G1) qui présente un organe d'arrêt (V1) réglable quant au débit et qui, partant du séparateur de gaz (G), débouche dans un échangeur de chaleur supplémentaire (W2, S, D), en particulier par l'intermédiaire de la canalisation supplémentaire (R4).
  2. Dispositif de craquage thermique d'un mélange d'hydrocarbures liquides et gazeux suivant la revendication 1, caractérisé en ce que le séparateur de gaz (G) est réalisé sous la forme d'un séparateur par gravité.
  3. Dispositif de craquage thermique d'un mélange d'hydrocarbures liquides et gazeux suivant la revendication 1, caractérisé en ce que le séparateur de gaz (G) est réalisé sous la forme de cyclone.
  4. Dispositif de craquage thermique d'un mélange d'hydrocarbures liquides et gazeux suivant l'une des revendications 1, 2 et 3, caractérisé en ce que le conduit à gaz (G1) partant du séparateur de gaz (G) débouche, vu dans le sens d'écoulement, avant le conduit (R4) partant de l'échangeur de chaleur (W1) en amont du conduit supplémentaire (D1) pour de la vapeur d'eau.
  5. Dispositif de craquage thermique d'un mélange d'hydrocarbures liquides et gazeux suivant l'une des revendications 1 à 4, caractérisé en ce que le conduit à gaz (G2) partant du séparateur de gaz (G) débouche dans l'échangeur de chaleur monté en aval (S), en particulier dans le conduit de sortie (R5) provenant de l'échangeur de chaleur supplémentaire (W2).
  6. Dispositif de craquage thermique d'un mélange d'hydrocarbures liquides et gazeux suivant l'une des revendications 1 à 5, caractérisé en ce que le conduit à gaz (G2) partant du séparateur de gaz débouche dans la canalisation supplémentaire (D1).
  7. Dispositif de craquage thermique d'un mélange d'hydrocarbures liquides et gazeux suivant l'une des revendications 1 à 6, caractérisé en ce que le conduit à gaz (G4) partant du séparateur de gaz (G) débouche dans un surchauffeur de vapeur (D).
  8. Dispositif de craquage thermique d'un mélange d'hydrocarbures liquides et gazeux suivant l'une des revendications 1 à 6, caractérisé en ce qu'un conduit de déviation supplémentaire (U1) par rapport à l'échangeur de chaleur (W1) est prévu, conduit de déviation qui, après le séparateur de gaz (G), bifurque à partir de la canalisation (R3) débouchant dans l'échangeur de chaleur (W1), et qui de préférence débouche dans la canalisation supplémentaire (R4) après l'embouchure du conduit à gaz (G1).
EP94890007A 1993-01-27 1994-01-14 Installation pour le craquage thermique d'un mélange d'hydrocarbures liquides et gazeuses Expired - Lifetime EP0609191B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT137/93 1993-01-27
AT0013793A AT398428B (de) 1993-01-27 1993-01-27 Vorrichtung zum thermischen spalten eines gemisches mit flüssigen und gasförmigen kohlenwasserstoffen

Publications (2)

Publication Number Publication Date
EP0609191A1 EP0609191A1 (fr) 1994-08-03
EP0609191B1 true EP0609191B1 (fr) 1998-07-29

Family

ID=3482516

Family Applications (1)

Application Number Title Priority Date Filing Date
EP94890007A Expired - Lifetime EP0609191B1 (fr) 1993-01-27 1994-01-14 Installation pour le craquage thermique d'un mélange d'hydrocarbures liquides et gazeuses

Country Status (11)

Country Link
EP (1) EP0609191B1 (fr)
AT (1) AT398428B (fr)
CZ (1) CZ283129B6 (fr)
DE (1) DE59406524D1 (fr)
DK (1) DK0609191T3 (fr)
ES (1) ES2121177T3 (fr)
FI (1) FI115466B (fr)
HU (1) HU214480B (fr)
NO (1) NO306681B1 (fr)
SI (1) SI9400032A (fr)
SK (1) SK279373B6 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20240043759A1 (en) 2020-12-10 2024-02-08 Totalenergies Onetech Belgium Method for improving feedstock flexibility of steam cracking
EP4074809A1 (fr) 2021-04-14 2022-10-19 Total Research & Technology Feluy Procédé et appareil de craquage d'une charge d'alimentation thermiquement stable

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4479869A (en) * 1983-12-14 1984-10-30 The M. W. Kellogg Company Flexible feed pyrolysis process
JPH0819420B2 (ja) * 1988-09-05 1996-02-28 三井石油化学工業株式会社 低品位原料の分解処理方法
DE4105095A1 (de) * 1991-02-19 1992-08-20 Linde Ag Verfahren zur prozesssteuerung in spaltoefen zur olefinherstellung

Also Published As

Publication number Publication date
HU9400231D0 (en) 1994-05-30
ATA13793A (de) 1994-04-15
CZ17394A3 (en) 1994-08-17
NO940252L (no) 1994-07-28
SI9400032A (en) 1994-09-30
SK279373B6 (sk) 1998-10-07
SK8194A3 (en) 1994-11-09
FI940385A0 (fi) 1994-01-26
AT398428B (de) 1994-12-27
DK0609191T3 (da) 1999-04-26
NO940252D0 (no) 1994-01-25
CZ283129B6 (cs) 1998-01-14
FI115466B (fi) 2005-05-13
NO306681B1 (no) 1999-12-06
ES2121177T3 (es) 1998-11-16
EP0609191A1 (fr) 1994-08-03
DE59406524D1 (de) 1998-09-03
HUT69458A (en) 1995-09-28
HU214480B (hu) 1998-03-30
FI940385A (fi) 1994-07-28

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