EP0364320A1 - Wärmeaustauscher für das Heizen von Einsätzen für das katalytische Reformieren unter niedrigem Druck - Google Patents

Wärmeaustauscher für das Heizen von Einsätzen für das katalytische Reformieren unter niedrigem Druck Download PDF

Info

Publication number: EP0364320A1
Authority: EP; European Patent Office
Prior art keywords: exchanger; charge; fluid; zone; exchange zone
Prior art date: 1988-10-13
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.): Granted

Application number

EP89402640A

Other languages

English (en)

French (fr)

Other versions

EP0364320B1 (de

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.)

1988-10-13

Filing date

1989-09-27

Publication date

1990-04-18

1989-09-27 Application filed by IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN

1989-09-27 Priority to AT89402640T priority Critical patent/ATE70852T1/de

1990-04-18 Publication of EP0364320A1 publication Critical patent/EP0364320A1/de

1991-12-27 Application granted granted Critical

1991-12-27 Publication of EP0364320B1 publication Critical patent/EP0364320B1/de

2009-09-27 Anticipated expiration legal-status Critical

Status 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 reactors and related devices, such as the exchanger in question is of the order of 10 bars, the value of this pressure allows correct circulation of the charge through the tubes or plates of the exchanger.
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 di-phase (liquid-gas) in which, at a pressure between 1 and 7 bars (105 Pascal and 7 x 105 Pascal) preferably between 2 and 6.5 bars (2 x 105 and 6.5 x 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.
di-phase liquid-gas
a charge is recovered at a temperature between approximately 430 and 520 ° C.
the pressure drop between the outlet of the charge from the second exchanger and the inlet of the charge into the first exchanger is between 0.3 and 1.5 bar (0.3 x 105 and 1.5 x 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 invention also relates to a device characterized in that it comprises in combination (see FIG. 1): - a first heat exchanger (6) provided with an introduction pipe (5) of a first fluid containing the liquid charge and a recycling gas coming from a catalytic reforming unit, provided with a withdrawal (8) of this first fluid, also provided with a withdrawal line (19) and an introduction line (18) of a second fluid from the second exchanger (9) defined below.
a second heat exchanger 9 provided with an introduction pipe (8) and with a withdrawal pipe (10) of said first fluid coming from the first heat exchanger and provided with an introduction pipe ( 17) and a draw-off line (18) of said second fluid, this second fluid being at least partly made up of the effluent from a reforming or reforming reactor, said second fluid being in indirect contact with said first fluid in each of the two exchangers (6) and (9).
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.
Figure 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).
First heat exchanger - inlet temperature of the mixed fluid charge - recycling gas: 89 ° C - mixed fluid inlet pressure: (bars) 6.2 (6.2 x 105 Pascal) - effluent outlet temperature: 102 ° C - effluent outlet pressure: 3.8 bars (3.8 x 105 Pascal) - effluent inlet temperature: 200 ° C
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 of the reforming or reforming effluent were respectively 89 ° C and 500 ° C.

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 Wärmeaustauscher für das Heizen von Einsätzen für das katalytische Reformieren unter niedrigem Druck Expired - Lifetime EP0364320B1 (de)

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

Publications (2)

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

Family

ID=9371080

Family Applications (1)

Application Number	Title	Priority Date	Filing Date
EP89402640A Expired - Lifetime EP0364320B1 (de)	1988-10-13	1989-09-27	Wärmeaustauscher für das Heizen von Einsätzen für das katalytische Reformieren unter niedrigem Druck

Country Status (8)

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

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

Citations (1)

* 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

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number	Priority date	Publication date	Assignee	Title
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

1988
- 1988-10-13 FR FR8813627A patent/FR2637908B1/fr not_active Expired - Lifetime
1989
- 1989-09-27 DE DE8989402640T patent/DE68900609D1/de not_active Expired - Lifetime
- 1989-09-27 AT AT89402640T patent/ATE70852T1/de not_active IP Right Cessation
- 1989-09-27 EP EP89402640A patent/EP0364320B1/de not_active Expired - Lifetime
- 1989-09-29 CA CA000614974A patent/CA1337341C/fr not_active Expired - Fee Related
- 1989-10-12 US US07/365,259 patent/US4973400A/en not_active Expired - Lifetime
- 1989-10-13 JP JP1267954A patent/JP2840771B2/ja not_active Expired - Lifetime
1990
- 1990-08-27 US US07/572,584 patent/US5073350A/en not_active Expired - Lifetime
1992
- 1992-02-11 GR GR920400213T patent/GR3003787T3/el unknown

Patent Citations (1)

* 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

Also Published As

Publication number	Publication date
US4973400A (en)	1990-11-27
FR2637908A1 (fr)	1990-04-20
EP0364320B1 (de)	1991-12-27
US5073350A (en)	1991-12-17
CA1337341C (fr)	1995-10-17
ATE70852T1 (de)	1992-01-15
GR3003787T3 (de)	1993-03-16
JP2840771B2 (ja)	1998-12-24
FR2637908B1 (fr)	1991-01-11
DE68900609D1 (de)	1992-02-06
JPH02166193A (ja)	1990-06-26

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