EP0364320B1 - Echangeur de chaleur pour chauffer la charge d'un reformage catalytique fonctionnant sous basse pression - Google Patents

Echangeur de chaleur pour chauffer la charge d'un reformage catalytique fonctionnant sous basse pression Download PDF

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Publication number
EP0364320B1
EP0364320B1 EP89402640A EP89402640A EP0364320B1 EP 0364320 B1 EP0364320 B1 EP 0364320B1 EP 89402640 A EP89402640 A EP 89402640A EP 89402640 A EP89402640 A EP 89402640A EP 0364320 B1 EP0364320 B1 EP 0364320B1
Authority
EP
European Patent Office
Prior art keywords
exchanger
charge
fluid
pipe
exchange
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
EP89402640A
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German (de)
English (en)
French (fr)
Other versions
EP0364320A1 (fr
Inventor
Pierre Ham
Jean De Bonneville
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.)
IFP Energies Nouvelles IFPEN
Original Assignee
IFP Energies Nouvelles IFPEN
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 IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN
Priority to AT89402640T priority Critical patent/ATE70852T1/de
Publication of EP0364320A1 publication Critical patent/EP0364320A1/fr
Application granted granted Critical
Publication of EP0364320B1 publication Critical patent/EP0364320B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming

Definitions

  • An improved reforming process consists in operating in at least two reactors in series with movable beds, these movable beds possibly being associated with reactors in a fixed bed. Such methods are described in particular in the US patents of the Applicant Nos. 4133733 and 4172027.
  • the feed which is introduced into the first reactor is generally at least partially preheated by indirect heat exchange with the effluent from the last reactor.
  • the charge thus preheated generally passes through an oven before being admitted into the first reactor.
  • the heat exchanger used is of the conventional tube or plate type.
  • the liquid charge is introduced, with recycling gas, into said exchanger and is substantially vaporized at the outlet of the exchanger.
  • the pressure used in the reactors and related devices such as the exchanger in question is of the order of 10 bars ( ⁇ 105 Pa)
  • the value of this pressure allows correct circulation of the charge through the tubes or the heat exchanger plates.
  • the object of the present invention makes it possible to adapt to low pressure catalytic reformings, a system of exchangers capable of functioning correctly.
  • the invention relates to a new process and a new low-pressure exchange device which makes it easy, on the one hand, to effect correct heating of the load and, on the other hand, to quickly and completely vaporize the load.
  • the principle of the invention therefore consists in vaporizing the charge in a first exchanger and then bringing the charge to a warmer temperature in a second exchanger, the charge is vaporized, it is then easier to circulate it even if the pressure is small and even if the section of this second exchanger is large.
  • the system of the invention makes it possible to limit the pressure drops as much as possible (delta P).
  • the device according to the invention is a combination of two exchangers in series through which the load passes.
  • the first exchanger is an indirect tube exchanger with circulation against the current of the feedstock and the reaction effluent
  • the second exchanger is an indirect plate or tube exchanger.
  • the liquid charge, mixed with recycling gas from the catalytic reforming unit is sent to a temperature between 80 and 110 ° C., in a first exchange zone, operating in diphase (liquid-gas) in which, at a pressure between 1 and 7 bars (105 Pascal and 7 ⁇ 105 Pascal) preferably between 2 and 6.5 bars (2 ⁇ 105 and 6.5 ⁇ 105 Pascal) where the charge is substantially vaporized by indirect contact (and preferably against the current with the reaction effluent); then the charge vaporized in the first exchange zone is sent to a second exchange zone operating in mono-phase (gas) at a pressure slightly lower than the pressure used in the first exchange zone due to a slight pressure drop.
  • diphase liquid-gas
  • a charge is recovered at a temperature between approximately 430 and 520 ° C.
  • the pressure drop between the outlet of the load from the second exchanger and the inlet of the load into the first exchanger is between 0.3 and 1.5 bar (0.3 ⁇ 105 and 1.5 ⁇ 105 Pascal).
  • the reaction effluent from the catalytic reforming unit circulates against the charge in each of the two exchange zones. It enters the second exchange zone at a temperature between 450 and 580 ° C. and leaves the second exchange zone at a temperature generally between 80 and 110 ° C. As for the charge withdrawn from the second exchange zone, it is sent to the first catalytic reforming zone after possibly passing through an oven to obtain the appropriate temperature of the charge.
  • the ratio of the exchange surfaces between the first and the second exchange zones is between 1/10 and 5/10 preferably between 2/10 and 4.5 / 10 and more particularly between 2 , 5/10 and 4/10.
  • Another advantage of the method and of the device according to the invention is as follows when a plate exchanger is used for the second exchanger and a tube exchanger for the first exchanger: it is during the condensation of the effluent that the walls (with which the effluent is in contact) become clogged. The latter being removable it can therefore be easily cleaned.
  • the plate heat exchangers are not removable. If they get dirty, there is no other remedy than chemical cleaning of the exchanger.
  • the charge which circulates in the second exchanger, and which preferably is a plate exchanger is already vaporized. There is therefore no fouling of the second exchanger.
  • the first exchanger is a tube exchanger and the second exchanger is a plate exchanger.
  • FIGS 1 and 2 illustrate the invention.
  • the liquid charge arriving via a line (4) is mixed in line (5) with the recycling gas from the reforming unit, this gas coming from the line (1) through the pump (2 ) and the pipe (3).
  • the mixed fluid (or double gas-liquid phase) enters a heat exchanger (6) with tubes (7) against the indirect flow of the reaction effluent entering the exchanger (6) by the line (18) and leaving by the line (19), to the pump (20) and the line (21).
  • the charge, fully vaporized, and the recycle gas leave the exchanger (6) via the line (8) and enter a plate exchanger (9) where they are heated by indirect contact with the reaction effluent (line 17 ) of the last reactor (16) of a series of reforming reactors, a reactor supplied with charge by a pipe (15).
  • the charge and the recycling gas are withdrawn from the plate heat exchanger (9) by the pipe (10), pass through the furnace (11) and by the pipe (12) feed the first reforming reactor (13) to then continue via line (14) to other reforming reactors.
  • FIG. 2 shows a particular embodiment of the device of the invention comprising the stack of an exchanger (6) with tubes (7) and a plate exchanger (9).
  • a tube exchanger and a plate exchanger were used in series preceding a catalytic reforming unit operating at 3 bars (3 ⁇ 105 Pascal).
  • each exchanger had an exchange surface of 5500 m2, therefore equal to the totality of the exchange surfaces of the two exchangers of the previous example.
  • the inlet temperatures of the mixed fluid and the reforming or reforming effluent were 89 ° C and 500 ° C, respectively.

Landscapes

  • 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)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Catalysts (AREA)
EP89402640A 1988-10-13 1989-09-27 Echangeur de chaleur pour chauffer la charge d'un reformage catalytique fonctionnant sous basse pression Expired - Lifetime EP0364320B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT89402640T ATE70852T1 (de) 1988-10-13 1989-09-27 Waermeaustauscher fuer das heizen von einsaetzen fuer das katalytische reformieren unter niedrigem druck.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8813627 1988-10-13
FR8813627A FR2637908B1 (fr) 1988-10-13 1988-10-13 Echangeur de chaleur pour chauffer la charge d'un reformage catalytique fonctionnant sous basse pression

Publications (2)

Publication Number Publication Date
EP0364320A1 EP0364320A1 (fr) 1990-04-18
EP0364320B1 true EP0364320B1 (fr) 1991-12-27

Family

ID=9371080

Family Applications (1)

Application Number Title Priority Date Filing Date
EP89402640A Expired - Lifetime EP0364320B1 (fr) 1988-10-13 1989-09-27 Echangeur de chaleur pour chauffer la charge d'un reformage catalytique fonctionnant sous basse pression

Country Status (8)

Country Link
US (2) US4973400A (enrdf_load_stackoverflow)
EP (1) EP0364320B1 (enrdf_load_stackoverflow)
JP (1) JP2840771B2 (enrdf_load_stackoverflow)
AT (1) ATE70852T1 (enrdf_load_stackoverflow)
CA (1) CA1337341C (enrdf_load_stackoverflow)
DE (1) DE68900609D1 (enrdf_load_stackoverflow)
FR (1) FR2637908B1 (enrdf_load_stackoverflow)
GR (1) GR3003787T3 (enrdf_load_stackoverflow)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2731693B1 (fr) * 1995-03-16 1997-05-23 Air Liquide Procede et installation de generation d'azote pour le traitement thermique

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3882014A (en) * 1972-10-26 1975-05-06 Universal Oil Prod Co Reaction zone effluents separation and hydrogen enrichment process
US4058452A (en) * 1976-07-19 1977-11-15 Uop Inc. Alkylaromatic hydrocarbon dealkylation process
DE2803284A1 (de) * 1977-01-31 1978-08-03 Inst Francais Du Petrol Katalytisches verfahren zur reformierung bzw. herstellung von aromatischen kohlenwasserstoffen
US4518574A (en) * 1983-03-07 1985-05-21 Exxon Research & Engineering Co. Catalytic gas synthesis process
DE3327795A1 (de) * 1983-08-02 1985-02-21 Dynamit Nobel Ag, 5210 Troisdorf Cyclische phenolorganosilane und verfahren zu deren herstellung
JPH07115841B2 (ja) * 1987-06-29 1995-12-13 日本酸素株式会社 メタノ−ルの水蒸気改質法

Also Published As

Publication number Publication date
FR2637908B1 (fr) 1991-01-11
US5073350A (en) 1991-12-17
CA1337341C (fr) 1995-10-17
FR2637908A1 (fr) 1990-04-20
DE68900609D1 (de) 1992-02-06
JPH02166193A (ja) 1990-06-26
JP2840771B2 (ja) 1998-12-24
US4973400A (en) 1990-11-27
EP0364320A1 (fr) 1990-04-18
GR3003787T3 (enrdf_load_stackoverflow) 1993-03-16
ATE70852T1 (de) 1992-01-15

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