EP0364320B1 - Heat exchanger for heating a low-pressure catalytic-reforming feed - Google Patents
Heat exchanger for heating a low-pressure catalytic-reforming feed Download PDFInfo
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- 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
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- Prior art keywords
- exchanger
- charge
- fluid
- pipe
- exchange
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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
- 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.
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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)
- Physical Or Chemical Processes And Apparatus (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
Description
Dans les procédés de reformage catalytique, la tendance est d'opérer à des pressions de plus en plus basses. Il y a quelques années, on opérait couramment dans les réacteurs à des pressions de 10 bars (10 × 10⁵ Pascal). De nos jours on cherche à opérer autour de 3 bars (3 × 10⁵ Pascal).In catalytic reforming processes, the tendency is to operate at increasingly lower pressures. A few years ago, we commonly operated in reactors at pressures of 10 bars (10 × 10⁵ Pascal). Nowadays we try to operate around 3 bars (3 × 10⁵ Pascal).
Un procédé perfectionné de reformage consiste à opérer dans au moins deux réacteurs en série à lits mobiles, ces lits mobiles pouvant être associés éventuellement à des réacteurs en lit fixe. De tels procédés sont notamment décrits dans les brevets américains de la demanderesse N°4133733 et 4172027.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.
La charge que l'on introduit dans le premier réacteur est généralement préchauffée au moins en partie par échange thermique indirect avec l'effluent du dernier réacteur. La charge ainsi préchauffée traverse généralement un four avant d'être admise dans le premier réacteur. L'échangeur de chaleur utilisé est de type conventionnel à tubes ou à plaques.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.
La charge liquide est introduite, avec du gaz de recyclage, dans le dit échangeur et se trouve sensiblement vaporisée à la sortie de l'échangeur. Lorsque la pression utilisée dans les réacteurs et les dispositifs connexes tel que l'échangeur en question, est de l'ordre de 10 bars (· 10⁵ Pa), la valeur de cette pression permet une circulation correcte de la charge à travers les tubes ou les plaques de l'échangeur.The liquid charge is introduced, with recycling gas, into said exchanger and is substantially vaporized at the outlet of the exchanger. When 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.
L'échangeur et son utilisation ne présentent alors aucun problème particulier de mise en oeuvre. Par contre lorsque la pression utilisée dans les réacteurs est faible, selon la tendance actuelle dans le domaine du raffinage, le cheminement de la charge dans l'échangeur se fait moins bien. De plus, quand on utilise une grande pression, dans l'unité de reformage on peut se permettre une delta P (perte de charge) relativement importante dans l'échangeur.The exchanger and its use then present no particular implementation problem. On the other hand, when the pressure used in the reactors is low, according to the current trend in the refining field, the flow of the charge in the exchanger is less successful. In addition, when using high pressure, in the reforming unit we can afford a relatively large delta P (pressure drop) in the exchanger.
Mais lorsque la pression réactionnelle (donc également la pression dans l'échangeur) est choisie faible, on ne peut alors tolérer les pertes de charge (delta P) importantes et cette perte de charge doit être limitée au maximum.However, when the reaction pressure (and therefore also the pressure in the exchanger) is chosen to be low, it is not then possible to tolerate significant pressure drops (delta P) and this pressure drop must be limited as much as possible.
De ce fait, pour remédier à cet objectif, il importe que les sections des échangeurs soient alors plus larges. Or, des sections larges nuisent à une distribution correcte du mélange charge et recyclage dans l'échangeur. Par ailleurs, le faible delta P ne permet pas de garantir une circulation homogène dans toutes les sections de l'échangeur. Il en résulte que la vaporisation se fait mal même si l'on utilise des échangeurs de taille importante.Therefore, to remedy this objective, it is important that the sections of the exchangers are then wider. However, large sections interfere with correct distribution of the charge and recycling mixture in the exchanger. Furthermore, the small delta P does not guarantee uniform circulation in all sections of the exchanger. As a result, the vaporization is bad even if using large exchangers.
L'objet de la présente invention permet d'adapter aux reformages catalytiques basse pression, un système d'échangeurs capable de fonctionner correctement. L'invention concerne un nouveau procédé et un nouveau dispositif d'échange à basse pression qui permet aisément d'une part d'effectuer le chauffage correct de la charge et d'autre part de vaporiser rapidement et complètement la charge.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.
En effet, lorsque la pression est faible dans un échangeur, il est beaucoup plus facile de faire circuler dans un tel échangeur un fluide gazeux plutôt qu'un fluide mixte gaz-liquide. Le principe de l'invention consiste donc à vaporiser la charge dans un premier échangeur et à porter ensuite la charge à une température plus chaude dans un deuxième échangeur, la charge est vaporisée, il est alors plus facile de la faire circuler même si la pression est faible et même si la section de ce deuxième échangeur est grande. En outre, le système de l'invention permet de limiter au maximum les pertes de charge (delta P).Indeed, when the pressure is low in an exchanger, it is much easier to circulate in such an exchanger a gaseous fluid rather than a mixed gas-liquid fluid. 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. In addition, the system of the invention makes it possible to limit the pressure drops as much as possible (delta P).
Le dispositif selon l'invention est une combinaison de deux échangeurs en série traversés par la charge. De préférence, la premier échangeur est un échangeur indirect à tubes avec circulation à contre courant de la charge et de l'effluent réactionnel, et le deuxième échangeur est un échangeur indirect à plaques ou à tubes.The device according to the invention is a combination of two exchangers in series through which the load passes. Preferably, the first exchanger is an indirect tube exchanger with circulation against the current of the feedstock and the reaction effluent, and the second exchanger is an indirect plate or tube exchanger.
L'invention concerne un procédé de reformage catalytique à basse pression comprise entre 1 et 7 bars, d'une charge liquide d'hydrocarbures dans au moins une zone de réaction, avec formation d'un effluent réactionnel accompagné de gaz, le dit gaz (ou gaz de recyclage) étant recyclé au moins en partie dans une dite zone de réaction, le procédé étant caractérisé en ce que un fluide mixte gaz-liquide constitué:
- a.
- de la charge liquide, initialement à une température comprise entre 80 et 110°C et
- b.
- du gaz de recyclage
est chauffé par contact indirect avec une partie au moins de l'effluent réactionnel dans deux zones d'échange thermique disposées en série, procédé dans lequel la charge est introduite dans la première zone d'échange où elle est sensiblement vaporisée, puis est envoyée dans la deuxième zone d'échange thermique, procédé caractérisé en ce que en outre l'effluent réactionnel est introduit d'abord dans la deuxième zone d'échange à une température comprise entre 450 et 580°C, puis est introduit dans la première zone d'échange d'où il est soutiré à une température comprise entre 80 et 110°C, la perte de charge entre le point de sortie de la charge dans la deuxième zone d'échange et le point d'entrée de la charge dans la première zone d'échange étant comprise entre 0,3 et 1,5 bar (0,3 × 10⁵ et 1,5 × 10⁵ Pascal).The invention relates to a process for catalytic reforming at low pressure of between 1 and 7 bars, of a liquid charge of hydrocarbons in at least one reaction zone, with the formation of a reaction effluent accompanied by gas, the so-called gas ( or recycling gas) being recycled at least in part in a said reaction zone, the process being characterized in that a mixed gas-liquid fluid consisting of:
- at.
- of the liquid charge, initially at a temperature between 80 and 110 ° C and
- b.
- recycling gas
is heated by indirect contact with at least part of the reaction effluent in two heat exchange zones arranged in series, process in which the charge is introduced into the first exchange zone where it is substantially vaporized, then is sent to the second heat exchange zone, process characterized in that, in addition, the reaction effluent is first introduced into the second exchange zone at a temperature between 450 and 580 ° C., then is introduced into the first zone d exchange from which it is withdrawn at a temperature between 80 and 110 ° C, the pressure drop between the point of exit of the charge in the second exchange zone and the point of entry of the charge in the first exchange zone being between 0.3 and 1.5 bar (0.3 × 10⁵ and 1.5 × 10⁵ Pascal).
Plus précisément, dans le procédé selon l'invention, la charge liquide, en mélange avec du gaz de recyclage de l'unité de reformage catalytique est envoyée à une température comprise entre 80 et 110°C, dans une première zone d'échange, fonctionnant en di-phasique (liquide-gaz) dans laquelle, à une pression comprise entre 1 et 7 bars (10⁵ Pascal et 7 × 10⁵ Pascal) de préférence entre 2 et 6,5 bars (2 × 10⁵ et 6.5 × 10⁵ Pascal) où la charge est sensiblement vaporisée par contact indirect (et de préférence à contre-courant avec l'effluent réactionnel); ensuite la charge vaporisée dans la première zone d'échange est envoyée dans une deuxième zone d'échange fonctionnant en mono-phasique (gaz) à une pression légèrement inférieure à la pression utilisée dans la première zone d'échange du fait d'une légère perte de charge.More specifically, in the process according to the invention, 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.
A la sortie de la deuxième zone d'échange, on récupère une charge à une température comprise entre 430 et 520°C environ. La perte de charge entre la sortie de la charge du deuxième échangeur et l'entrée de la charge dans le premier échangeur est comprise entre 0,3 et 1,5 bar (0,3 × 10⁵ et 1,5 × 10⁵ Pascal).At the exit from the second exchange zone, 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).
L'effluent réactionnel de l'unité de reformage catalytique circule à contre-courant de la charge dans chacune des deux zones d'échange. Il pénètre dans la deuxième zone d'échange à une température comprise entre 450 et 580°C et sort de la deuxième zone d'échange à une température généralement comprise entre 80 et 110°C. Quant à la charge soutirée de la deuxième zone d'échange, elle est envoyée dans la première zone de reformage catalytique après avoir éventuellement traversé un four pour obtenir la température adéquate de la charge. D'une façon préférée, le rapport des surfaces d'échange entre la première et la deuxième zones d'échange est compris entre 1/10 et 5/10 de préférence entre 2/10 et 4,5/10 et plus particulièrement entre 2,5/10 et 4/10.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. Preferably, 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.
Un autre avantage du procédé et du dispositif selon l'invention est le suivant lorsqu'on utilise un échangeur à plaques pour le deuxième échangeur et un échangeur à tubes pour le premier échangeur: c'est au cours de la condensation de l'effluent que les parois (avec lesquelles l'effluent est en contact) s'encrassent. Ce dernier étant démontable il peut donc être nettoyé facilement. On sait que les échangeurs à plaques ne sont pas démontables. S'ils se salissent, il n'y a pas d'autre remède que le nettoyage chimique de l'échangeur. Dans le procédé et le dispositif de l'invention, la charge qui circule dans le deuxième échangeur, et qui de préférence est un échangeur à plaques, est déjà vaporisée. Il n'y a donc pas d'encrassage du deuxième échangeur.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. We know that the plate heat exchangers are not removable. If they get dirty, there is no other remedy than chemical cleaning of the exchanger. In the method and the device of the invention, 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.
L'invention concerne également un dispositif caractérisé en ce qu'il comporte en combinaison (voir figure 1):
- ― un premier échangeur de chaleur (6) muni d'une conduite d'introduction (5) d'un premier fluide contenant la charge liquide et un gaz de recyclage en provenance d'une unité de reformage catalytique, muni d'une conduite de soutirage (8) de ce premier fluide, muni également d'une conduite de soutirage (19) et d'une conduite d'introduction (18) d'un deuxième fluide en provenance du deuxième échangeur (9) défini ci-après.
- ― un deuxième échangeur de chaleur (9) muni d'une conduite d'introduction (8) et d'une conduite de soutirage (10) dudit premier fluide en provenance du premier échangeur de chaleur et muni d'une conduite d'introduction (17) et d'une conduite de soutirage (18) dudit deuxième fluide, ce deuxième fluide étant au moins en partie constitué de l'effluent d'un réacteur de reforming ou reformage, ledit deuxième fluide étant en contact indirect avec ledit premier fluide dans chacun des deux échangeurs (6) et (9).
- - 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).
D'une façon préférée, le premier échangeur est un échangeur à tubes et le deuxième échangeur est un échangeur à plaques.Preferably, the first exchanger is a tube exchanger and the second exchanger is a plate exchanger.
Les figures 1 et 2 illustrent l'invention.Figures 1 and 2 illustrate the invention.
Dans la figure 1, la charge liquide arrivant par une conduite (4) est mélangée dans la ligne (5) avec le gaz de recyclage de l'unité de reformage, ce gaz provenant de la conduite (1) à travers la pompe (2) et la conduite (3). Le fluide mixte (ou double phase gaz-liquide) pénètre dans un échangeur (6) à tubes (7) à contre courant indirect de l'effluent réactionnel entrant dans l'échangeur (6) par la ligne (18) et sortant par la ligne (19), vers la pompe (20) et la conduite (21). La charge, entièrement vaporisée, et le gaz de recyclage sortent de l'échangeur (6) par la conduite (8) et pénètrent dans un échangeur à plaques (9) où ils sont chauffés par contact indirect avec l'effluent réactionnel (ligne 17) du dernier réacteur (16) d'une série de réacteurs de reformage, réacteur alimenté en charge par une conduite (15). La charge et le gaz de recyclage sont soutirés de l'échangeur à plaques (9) par la conduite (10), traversent le four (11) et par la conduite (12) alimentent le premier réacteur (13) de reformage pour continuer ensuite par la ligne (14) vers d'autres réacteurs de reformage.In FIG. 1, 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.
La figure 2 montre une réalisation particulière du dispositif de l'invention comportant l'empilement d'un échangeur (6) à tubes (7) et d'un échangeur à plaques (9).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 titre d'exemple, on a utilisé en série un échangeur à tubes et un échangeur à plaques précédant une unité de reformage catalytique fonctionnant sous 3 bars (3 × 10⁵ Pascal).
A titre d'exemple comparatif, on a utilisé successivement un échangeur unique à plaques et un échangeur unique à tubes. Chaque échangeur avait une surface d'échange de 5500 m², donc égale à la totalité des surfaces d'échange des deux échangeurs de l'exemple précédent. Les températures d'entrée du fluide mixte et de l'effluent de reformage ou reforming étaient respectivement 89°C et 500°C.By way of comparative example, successively a single plate exchanger and a single tube exchanger were used. 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.
On a cherché à avoir une perte de charge minimum de façon à ce que la pression réactionnelle de reformage ou reforming soit 3 bars (3 × 10⁵ bars) comme dans l'exemple 1.We tried to have a minimum pressure drop so that the reforming or reforming reaction pressure is 3 bars (3 × 10⁵ bars) as in Example 1.
Dans ces conditions, la vaporisation de la charge ne se produit pas convenablement et le fonctionnement de l'échangeur est instable.Under these conditions, the vaporization of the charge does not occur properly and the operation of the exchanger is unstable.
Claims (6)
is heated by indirect contact with at least part of the reaction effluent in two heat exchange zones arranged in series, the charge being introduced into the first exchange zone where it is substantially vaporized and is then passed into the second heat exchange zone and also characterized in that the reaction effluent is at least partly introduced into the second exchange zone at a temperature between 450 and 580°C and then into the first exchange zone from which it is withdrawn at a temperature between 80 and 110°C, the pressure drop between the exit point of the charge in the second exchange zone and the inlet point of the charge in the first exchange zone being between 0.3 and 1.5 bar (0.3 × 10⁵ and 1.5 × 10⁵ Pascal).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT89402640T ATE70852T1 (en) | 1988-10-13 | 1989-09-27 | HEAT EXCHANGER FOR HEATING INSERT FOR LOW PRESSURE CATALYTIC REFORMING. |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR8813627 | 1988-10-13 | ||
| FR8813627A FR2637908B1 (en) | 1988-10-13 | 1988-10-13 | HEAT EXCHANGER FOR HEATING THE LOAD OF A LOW PRESSURE CATALYTIC REFORMING |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0364320A1 EP0364320A1 (en) | 1990-04-18 |
| EP0364320B1 true EP0364320B1 (en) | 1991-12-27 |
Family
ID=9371080
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP89402640A Expired - Lifetime EP0364320B1 (en) | 1988-10-13 | 1989-09-27 | Heat exchanger for heating a low-pressure catalytic-reforming feed |
Country Status (8)
| Country | Link |
|---|---|
| US (2) | US4973400A (en) |
| EP (1) | EP0364320B1 (en) |
| JP (1) | JP2840771B2 (en) |
| AT (1) | ATE70852T1 (en) |
| CA (1) | CA1337341C (en) |
| DE (1) | DE68900609D1 (en) |
| FR (1) | FR2637908B1 (en) |
| GR (1) | GR3003787T3 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2731693B1 (en) * | 1995-03-16 | 1997-05-23 | Air Liquide | PROCESS AND PLANT FOR GENERATING NITROGEN FOR HEAT TREATMENT |
Family Cites Families (6)
| 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 (en) * | 1977-01-31 | 1978-08-03 | Inst Francais Du Petrol | CATALYTIC PROCEDURE FOR REFORMING OR PRODUCTION OF FLAVORED HYDROCARBONS |
| US4518574A (en) * | 1983-03-07 | 1985-05-21 | Exxon Research & Engineering Co. | Catalytic gas synthesis process |
| DE3327795A1 (en) * | 1983-08-02 | 1985-02-21 | Dynamit Nobel Ag, 5210 Troisdorf | CYCLIC PHENOLORGANOSILANES AND METHOD FOR THE PRODUCTION THEREOF |
| JPH07115841B2 (en) * | 1987-06-29 | 1995-12-13 | 日本酸素株式会社 | Steam reforming method for methanol |
-
1988
- 1988-10-13 FR FR8813627A patent/FR2637908B1/en not_active Expired - Lifetime
-
1989
- 1989-09-27 DE DE8989402640T patent/DE68900609D1/en not_active Expired - Fee Related
- 1989-09-27 EP EP89402640A patent/EP0364320B1/en not_active Expired - Lifetime
- 1989-09-27 AT AT89402640T patent/ATE70852T1/en not_active IP Right Cessation
- 1989-09-29 CA CA000614974A patent/CA1337341C/en 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/en 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
Also Published As
| Publication number | Publication date |
|---|---|
| US4973400A (en) | 1990-11-27 |
| DE68900609D1 (en) | 1992-02-06 |
| JP2840771B2 (en) | 1998-12-24 |
| FR2637908A1 (en) | 1990-04-20 |
| EP0364320A1 (en) | 1990-04-18 |
| GR3003787T3 (en) | 1993-03-16 |
| FR2637908B1 (en) | 1991-01-11 |
| CA1337341C (en) | 1995-10-17 |
| US5073350A (en) | 1991-12-17 |
| JPH02166193A (en) | 1990-06-26 |
| ATE70852T1 (en) | 1992-01-15 |
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