JPS6039714B2 - Catalytic reforming method - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION Catalytic reforming techniques are well known in the petroleum refining industry and need not be described in detail here.

In summary, catalytic reforming technology primarily concerns the treatment of hydrocarbonaceous feedstocks to improve their anti-knock properties.
Generally, hydrocarbonaceous feedstocks consist of petroleum oil fractions. Such Ganlin fraction has a temperature of 50 to 1100F (10 to
38oo) first station and 325~must 50F (1 line~218
It is a total boiling point crab fraction with a final boiling point of Furthermore, this gasoline crab content has an initial boiling point of 150-250F (66-121℃) and a boiling point of 350-4250F (177-218oo).
It has a terminal point of . This higher grade point fraction is commonly referred to as naphtha. The reforming process is particularly applicable to the treatment of straight-run gasoline, which consists of relatively large concentrations of naphthenic hydrocarbons and substantially straight-chain paraffinic hydrocarbons, which are aromatized by dehydrogenation and/or cyclization reactions. Various other concomitant reactions such as isomerization and hydrogen transfer that are useful in increasing the antiknock properties of selected gasoline ingredients also occur. As described in more detail below, in a typical catalytic reforming operation, a feedstock, preferably a petroleum oil fraction, is first combined with hydrogen.

The mixture of feedstock and hydrogen is then heated to the reaction temperature,
Next, it is brought into contact with a reforming catalyst. The ~ reaction effluent is then separated to obtain a vapor phase consisting of hydrogen and a liquid phase consisting of a hydrocarbon gasoline with improved anti-knock properties and volatile C, ~C4 components dissolved therein. is recycled, at least in part, for mixing with the feedstock. The liquid phase is then stabilized to remove volatile C, to C4 components by rectification, typically in a debutanizer column. As mentioned above, various reactions occur during catalytic reforming.

These reactions include dehydrogenation, cyclization, hydrogenolysis and isomerization. Catalytic reforming is significantly endothermic. Therefore, to ensure that the reactants remain at reaction temperature, it is common to perform catalytic reforming with one or more catalyst beds to allow for reheating of the reactants. Thus, the effluent from the previous catalyst bed is reheated to reaction temperature before entering the next catalyst bed. The highly endothermic nature of catalytic reforming requires large amounts of heat.

Typically, heat for the catalytic reformer is provided by a combustion heater. The mixture of hydrocarbon and hydrogen passes through the radiation heating section of the combustion heater where it is heated to reaction temperature. Since only a portion of the total heat dissipated in the combustion heater is absorbed by the hydrocarbons and hydrogen, a large amount of fuel must be combusted in the combustion heater to ensure sufficient heat for alongside reforming. No. In order to save fuel and reduce the use of combustion heaters, it has become common practice to recover heat by preheating the feedstock and hydrogen mixture by indirect heat exchange with the pure reaction effluent. Became.

Thus, the mixture of feedstock oil and hydrogen first undergoes indirect heat exchange with the reforming reaction effluent. The heated mixture is then passed through a combustion heater for further heating to reaction temperature. Such a subthermal stage is disclosed in US Pat. No. 4,110,197 and provides fuel savings due to reduced combustion heater usage. As mentioned above, it is also common practice to treat destabilized hydrocarbon reformed gasoline in a refinement stage followed by separation from the hydrogen-containing vapor phase.

Typically, a distillation step is performed to remove hydrogen and C, to C4 hydrocarbons from the destabilized reformate. Such a crab stage requires heat input to the distillation column. Usually,
The source of such heat is a combustion heater in which the reformate removed from the bottom of the column is heated to the desired temperature and reintroduced into the column. In the combustion heaters used to heat the catalytic reforming reactants, the stabilizer tower combustion heater consumes a large amount of fuel and only accounts for 1% of the total heat released.
is absorbed by the reformed gasoline from the bottom of the column. Therefore, it is advantageous to eliminate the stabilizer tower combustion heater. As mentioned above, only 1% of the heat released in the reforming reactant combustion heater is absorbed by the hydrocarbon and hydrogen mixture in the radiation heating section of the heater.

The remainder of the heat released by the combustion exits the mirror portion of the heater with the hot combustion gases. These hot combustion gases serve as a heat source for the stabilizer column by indirect heat exchange with the reformate from the refiller. However, traditional unit operation requires the use of small combustion heaters to control heat input to the tower, thereby part of the benefits to be derived from eliminating stabilizer tower combustion heaters. is lost. Now, without using a second combustion heater for control,
It has been found that significant fuel savings can be achieved by utilizing a reforming reactant combustion heater as a heat source for a reformed gasoline stabilizer column.

Therefore, it is possible to fully realize the benefits of eliminating the stabilizer tower combustion heater by utilizing the catalytic reactant combustion heater as the heat source for pure gasoline stabilization. Instead of utilizing a small combustion heater to control the heat input into the reactor, it has been found that the reforming reaction effluent can be used as an alternative heat source to control the heat input into the stabilizer column. The reforming reaction effluent undergoes indirect heat exchange with the reformate from the bottom of the stabilizer column prior to heat exchange with the feedstock and hydrogen mixture. Next,
The heated reformate is returned to the tower. The use of the reforming reaction zone effluent as a stabilizer tower heat input control source increases the use of the reforming reactant combustion heater and increases the amount of heat utilized in the reaction effluent to subheat the feedstock and hydrogen mixture. becomes less. Despite the increased use of reforming reactant combustion heaters, the benefits of reforming reactant combustion heaters as a heat source for the stabilizer column are significant compared to traditional methods that utilize separate stabilizer column combustion heaters. resulting in overall fuel savings. Accordingly, it is an object of the present invention to achieve a significant reduction in the combustion consumption of the catalytic reforming process by providing substantially all of the heat demand to the reformed gasoline stabilizer column by indirect heat exchange.

More specifically, it is an object of the present invention to provide substantially all of the heat demand from indirect heat exchange with the reformate reaction effluent and from the reformate reactant combustion heater. In one of its broad aspects, the invention provides 'a}
A mixture of hydrocarbonaceous feedstock oil and hydrogen is heated in a Korean heating section of a combustion heater, and then the heated mixture is brought into contact with a reforming catalyst under reforming conditions to produce a reaction effluent;
b} subjecting at least a portion of the reaction effluent to a first indirect heat exchange with a portion of hydrocarbon reformed gasoline; {c} subjecting at least a portion of the reaction effluent to a first indirect heat exchange prior to heating in a combustion heater;
performing a second indirect heat exchange with the mixture of hydrocarbonaceous feedstock and hydrogen to separate the skin reaction effluent into a hydrogen-rich vapor phase and a substantially liquid hydrocarbon phase; At least a portion of the phase is recycled for mixing with the hydrocarbonaceous feedstock, and the liquefied phase is introduced into a stabilizer column which contains a mixture of normally gaseous hydrocarbons at standard temperature and pressure. Maintaining distillation conditions sufficient to provide a top fraction and a bottom fraction consisting of hydrocarbon reformate gasoline, [f] a first predetermined amount of hydrocarbon reformate gasoline is transferred to step [a '
By indirect heat exchange with the hot combustion gas in the convection heating section of the combustion heater, the recovered and reheated reformed gasoline is returned to the stabilizer tower to supply a fixed amount of heat to the IJ boiler ( g) Recovering a second portion of hydrocarbon reformed gasoline, subjecting it to indirect heat exchange with the reaction effluent in stage [b}, and returning this second portion to the stabilizer column to meet the remainder of the column boiler heat demand. and (h) recovering a third portion of the hydrocarbon reformed gasoline as a product.

One aspect of this invention is that in a preferred embodiment, the fixed amount of heat provided by the first predetermined amount of hydrocarbon reformate is 50-80% of the IJ boiler heat requirement of the stabilizer column. be.

In another preferred embodiment of the invention, the amount of the portion of the reaction effluent that undergoes the first indirect heat exchange with the hydrocarbon reformate is dependent on a predetermined stabilizer column boiler temperature. determined. Other objects and specific examples will become apparent from the description below.

Catalytic reforming of petroleum Ganlin fraction is a vapor phase operation, generally at about 500 to 10,500 F (about 260 to 556 oo).
, preferably about 600 to 10,000F (about 316 to 53
Conversion conditions are carried out including catalyst bed temperatures in the range of 8:00 AM).

Other reforming conditions are approximately 50 to 100 sjg (approximately 34
5-6900 kpa gauge), preferably about 75-3
5 sig (approximately 520 to 2400 kpa gauge) pressure,
and a liquid hourly space velocity (defined as the volume of liquid freshly charged per volume of catalyst per hour) of about 0.2 to 1 wind r-1. The reforming reaction is generally about 0.5:1,0-10
．． It is carried out in the presence of sufficient hydrogen to give a hydrogen/hydrocarbon molar ratio of 0:1.0. The catalytic reforming reaction is carried out at the above-mentioned reforming conditions in a reaction chamber consisting of either a fixed or moving catalyst bed.

Typically, the reaction castle consists of a plurality of catalyst beds, commonly referred to as stages, either stacked in a single reactor or contained in individual reactors arranged side by side. The reaction zone generally consists of 2 to 4 catalyst beds in either stacked or side-by-side configuration. In any event, as noted above, the endothermic nature of the Yabutomu reforming requires heating of both the fresh feed and the catalyst bed effluent before introduction into the next catalyst bed. The amount of catalyst used in each of the catalyst beds is varied to compensate for the endothermic nature of the reforming reaction. For example, three catalyst beds are used to illustrate one preferred embodiment of the present invention, using about 12 volume percent in the first bed followed by about 4 volumes each in the second and third beds. Generally, the first bed contains about 10 to 3 ft capacity and the second bed contains about 25 to 45 mts.
%, and the third bed contains about 40-6% tear. For 4 catalyst beds, etc., suitable catalyst loadings are about 5-1% by volume in the first bed, about 15-2% by volume in the second bed, about 25-33% by volume in the third bed, and about 2% by volume in the fourth bed. The amount of capacitance is 35-5%.

The unequal catalyst distribution increasing in the continuous direction of the reactant stream facilitates and enhances the reaction as well as the distribution of heat throughout the reaction. The method of the present invention contemplates the use of reforming catalyst compositions well known in the prior art.

As mentioned above, catalytic reforming reactions are diverse and include dehydrogenation of naphthenes to aromatics, dehydrocyclization of paraffins to aromatics, and hydrogenation of long mirror paraffins to low-boiling liquid substances. Includes decomposition and isomerization of paraffins. These reactions generally involve a combination of a halogen (e.g. chlorine and/or fluorine) and a porous support such as alumina.
This is accomplished through the use of catalysts consisting of one or more of the Group VIII metal groups (eg, platinum, osmium, iridium, rhodium, ruthenium, palladium). Recent research has shown that beneficial results can be obtained through the joint use of catalytic modifiers, and these modifiers are generally composed of iron, cobalt, copper,
It has been shown that the metals are selected from the group consisting of nickel, gallium, zinc, germanium, tin, cadmium, rhenium, bismuth, vanadium, alkali and alkali metals, and mixtures thereof. As noted above, the reforming operation further includes separation of a hydrogen-rich vapor phase from the reaction effluent recovered from the reaction zone, at least a portion of which is recycled to the reaction castle.

This separation is typically carried out at substantially the same pressure in the reaction chamber to give a pressure drop in the system, from about 60 to 1200 F (
The process is carried out at temperatures ranging from 16 to 49 degrees Celsius, resulting in a vapor phase consisting of relatively pure hydrogen. The primarily liquid hydrocarbon phase is further processed in a product stabilizer column for the recovery of a reformed product, commonly referred to as diesel gasoline. Reformulated gasoline product stabilizers are generally C
It is operated at conditions chosen to separate hydrocarbons, or if necessary, a usually gaseous hydrocarbon fraction consisting of C 2 hydrocarbons and usually some residual hydrogen. The operating conditions are
Typically about 100 to 30 snakesig (about 690 to 210
0 kpa gauge), which is generally lower than the pressure at which the hydrogen-rich vapor phase is separated from the reaction effluent to avoid the need to pump the liquid hydrocarbon phase into the stabilizer column. is also low. Other operating conditions are approximately 40
Includes a low column temperature of 0 to 5000F (about 200 to 260 qo) and a overhead temperature of about 110 to 2000F (about 43 to 93C). In the past, most of the thermal requirements of a stabilizer column were generally provided by a separate combustion heater. However, contrary to past practice, the present invention utilizes a reforming reactant combustion heater as the heat source for the stabilizer column without the use of a separate combustion heater. The combustion heaters used in the present invention are those commonly used in the petroleum and chemical industries. These are fired with gas or oil. Box or rectangular as well as center wall updraft combustion heaters are used. Such heaters consist of one or more tubes and include specular heating sections that carry fluid along different wall surfaces placed to receive the radiation from the burner. In the center wall configuration, the Korean radiant heat section consists of rows of burners firing against both sides of a longitudinally elongated center compartment wall, and the resulting radiant heat is transferred to process fluid tubes placed along each side wall. is supplied to
An alternative to traditional tube arrangement, US Pat. No. 3,566,84
It is also possible to use an inverted U-shaped tube as disclosed in No. 5. The preferred process fluid tubing geometry and heater design is disclosed in U.S. Pat.
It is stated in No. 6. Despite the shape of the mirror heating section, the heat released by the combustion of the fuel is not absorbed by the process fluid in the mirror heating section.

Rather, a substantial amount of heat leaves the specular heating section with the combustion gases. It has become practical to recover this heat from the hot combustion gases in the convection heating section of combustion heaters. Like the cervical heating section, the convection heating section also has a variety of shapes. These are designed so that a uniform flow of combustion gases passes through the convection heater. On the other hand, non-uniform flow of the combustion gases can also be used by changing the symmetry of the combustion gas flow path. Regardless of its exact shape, the convection section places the hot combustion gases in contact with the process fluid tubes, thereby effecting convective heat transfer between the gases and the tubes. The above discussion of combustion heaters is provided as a general description and is not intended to unduly limit the scope of the invention. The present invention will be described below with reference to the drawings with reference to one preferred example.

The data in the description is indicative of detailed calculations made for design purposes. The various hardware, equipment uses and controls, such as pumps, compressors, heat exchangers, valves, etc., are not necessarily essential to an understanding of the method, and the use of such hardware is within the skill of those skilled in the art. Since they are well known, they have been omitted or reduced in number. Regarding the drawing, the petroleum derived naphtha crab fraction is approximately R-1 by line 1.
is charged to the process at a rate of about 529.8 moles per hour with a liquid hourly space velocity of .

It is then mixed with about 36.2 moles per hour of hydrogen-rich gaseous flow consisting of about 71 mole percent hydrogen introduced from line 2 at a hydrocarbon/hydrogen ratio of about 4.5. The fresh feedstock passes through heat exchanger 3 in line 1 where it is preheated to approximately 8790F (470 qo) by indirect heat exchange with the effluent stream in line 13 recovered from reactor 11. The preheated reaction mixture passes through line 1 to the gas-fired heater 4, passes through the charge heating coil la of its head heating section, and enters the catalyst bed of the reactor 5 at an inlet temperature of approximately 9900F (530q
o). The reactors 5 each have a capacity of approximately 990T (530T).
The first of three countervessels consisted of a catalytic reforming reactor maintained at reforming conditions including a temperature of 100 m and a pressure of about 325 psig (40 kpa gauge). The reforming conditions further include the use of a platinum-containing catalyst. The heated reaction mixture is transferred from the heater 4 via line 6 to the first reactor 5. Since the catalytic reforming reaction is endothermic, the flow of effluent from reactor 5 is directed through line 7 to another heating coil 7a of the cervical heating section of combustion heater 4.

In the heater 4, the effluent stream is reheated to provide an inlet temperature of about 9900F (about 530C) to the catalyst bed of reactor 9. A stream of reheated reactor 5 effluent is removed from heater 4 and introduced by line 8 into a second reactor 8 . The effluent from the reactor 9 is collected by a line 10 and sent to another heating coil 10 of the cervical heating section of the combustion heater 4.
a and is reheated before being introduced into reactor 11 after a series of reactors consisting of a catalytic reactor.

The reheated effluent is removed from the heater and introduced by line 12 into the reactor 11. The flow of effluent from reactor 11 after the procedure is at a rate of about 4540.5 moles per hour at a temperature of about 9700 F (520 qo).
is taken out through. Effluent flow of about 183.7 moles per hour is diverted from line 13 to line 14 and this diverted stream passes through heat exchanger 15 with stabilizer column 16. The diverted effluent stream is utilized in the exchanger 15 to provide indirect heat exchange, and a portion of the reformate product is recovered from the stabilizer column 16 and recycled via line 24. The effluent of reactor 11 diverted to exchanger 15 is controlled by control valve 26. From the exchanger 15, the diverted effluent flow passes through line 14 and the reactor 11 effluent flow from line 13 recombines with the main portion. The main part of this is about 4356.
8 moles of heat is sent through exchanger 3 to preheat the fresh feedstock passing through line 1. Reactor 11 re-enacted
The effluent stream is passed through a cooler 17 included in line 14 into a separator 18 at a temperature of about 1000F (total Celsius). Separator 18 is maintained at conditions sufficient to separate the hydrogen-rich gas phase into a substantially liquid hydrocarbon phase. The conditions are approximately 305ps at a temperature of approximately 1000F (fine degrees Celsius).
ig (152 kpa gauge) pressure, approximately 71 mol%
A hydrogen-enriched gas phase consisting of 30% of hydrogen is withdrawn through overhead line 19, at a rate of approximately 33% per hour.
36.2 moles are diverted through line 2 and mixed with the naphtha fraction charged to the process through line 1. Separator 1
The remainder of the gas phase from 8 is discharged from the process through line 19 at a rate of P moles per hour. A substantially liquid hydrocarbon phase is removed from separator 18 by line 20 and maintained at a temperature and pressure sufficient to separate the overhead fraction, which typically consists of gaseous hydrocarbons, i.e., C4 hydrocarbons. stabilizer tower 16.

This overhead crab material is removed from the stabilizer column through line 21 at a rate of about 122 moles per hour.

The waste gasoline product is removed as a resid fraction from stabilizer column 16 via line 22 at a rate of about 1322.3 moles per hour at a temperature of about 4590F (237o0). Approximately 820.8 moles per flow hour of reformate product are diverted into line 23, with a predetermined amount of approximately 75% of the flow passing through line 23, and the combustion of an indirect heat exchanger through which the hot combustion gases pass. It is processed by the heating coil 23a in the convection heating section of the heater 4. In this case, the predetermined amount is chosen to provide about 75% of the stabilizer tower boiler heat requirement. This predetermined amount is controlled by conventional means such as a pump or flow controller. The flow of Kaikin Gasoline live vocals is as follows:
After heating in the convection heating section, approximately 50yF (26 to 0)
is returned to the stabilizer column via lines 25 and 24 at a temperature of . Approximately 25% of the reformate product stream diverted to line 23 is recycled via line 24 through heat exchanger 15 to stabilizer column 16. In the heat exchanger 15, the flow thus recycled is approximately 503. F
(26°) to provide the remainder of the stabilizer tower's IJ boiler heat requirement, in this case about 25%. The effluent of reactor 11 passes through line 14 and the recycle stream is heated in heat exchanger 15 by indirect heat exchange. As previously mentioned, the flow of the reactor 11 effluent diverted to the heat exchanger 15 is controlled by the control valve 26. The control valve 26 is operated by any suitable means depending on the stabilizer tower boiler temperature. The predetermined boiler temperature is selected to provide the desired overhead and bottoms product quality. A predetermined amount of repoiler heat demand is determined to be obtained from the scale heater convection heating section. control valve 2
6 act in sequence to divert a sufficient amount of reactor 11 effluent from line 13 to heat exchanger 15 to provide the remainder of the heat necessary to obtain the predetermined stabilizer reboiler temperature. Control valve 26 further operates to maintain a predetermined boiler temperature by diverting the flow of reactor I1 effluent to heat exchanger 15 as required. A comparison of the fuel consumption of the combustion heater of the present invention with that of a conventional reforming process as described in the above embodiments clearly shows the advantages achieved by the use of the present invention.

For comparison, a conventional reforming process with two separate combustion heaters and a charge rate comparable to that of the above example would yield about 23.7 x 1 pi BTU/hr (25.0 x 1 pi BTU/hr). h
r) reforming reactant combustion heater capacity and approximately 5.8 x 1 BT
It has a stabilizer reboiler-combustion heater capacity of U/hr (6.1 x 1 ki/hr). All-infrared reforming reactant combustion heaters that do not use a convection heating section typically
It has a heater efficiency of about 54% based on the lower heating value of the fuel. Therefore, the waste reactant combustion heater is 23.7×
To reach a heater capacity of 1 pi BTU/hr (25.6 x 1 pi BTU/hr), approximately 43.9 x l pi BTU/hr (
It is necessary to burn 46.3 x 1 km/hr).

Stabilizer reboiler combustion heaters are typically
1000F with heated fuel gas and low heating value fuel
It has a heater efficiency of about 84.5% based on nearby temperatures. This means that to reach the stabilizer reboiler combustion heater capacity is approximately 6.8 x 1 pi BTU/hr (7.2 x
1 ki/hr) of fuel is required to be combusted. All conventional processes are 43.9 x 1 BTU/h
r+6.8×1 BTU/hr or 50.7×1 B
It requires combustion of TU/hr (46.3 x 1 x kj/hr + 7.2 x 1 x kj/h or 53.5 x 1 x ki/hr) of fuel and 1.23.7 x 1 pi/hr. BTU/hr+5.8
xlpiBTU/hr50.7×1piBTU'hr or 58.1% (25.0×1piBTU'hr+6.1×1pipi kj/hr
) (53.5 x 1 pkj/hr).

In contrast, the catalytic reforming method according to one embodiment of the present invention has a
5.0×1piBTU/hr (26.4×1piBTU/hr
) has a reforming reactant combustion heater capacity.

It should be noted that this heater capacity is greater than the corresponding conventional heater capacity. This results from the fact that, according to the invention, a portion of the heat of the reactor 11 effluent is utilized to reboil the stabilizer and is therefore not available for co-heating the fresh feedstock. In the process of secondary technology, all of the reactor effluent is utilized for condensation of the reactor feedstock, so the feedstock enters the modified reactant combustion heater at a higher inlet temperature and the feedstock enters the combustion heater at a higher inlet temperature. Reduce capacity. Since the 25 x 1 pi BTU/hr (26 x 1 pi BTU/hr) heater capacity in the example combustion heater is substantially picked up in the specular heating section, the heater efficiency is approximately 54% as before. It is. Thus, the base of fuel burned to achieve heater capacity is 46.2 x 1 BTU/hr (487 x 1 ki/hr).
hr). In addition, about 75% of the stabilizer repoiler capacity or about 4.3 x 1 pi BTU/hr (4.5
x1 'ki/hr) is picked up in the convection heating section of the combustion heater. However, this heat is due to the heating of the gas rather than from the combustion of additional fuel. Therefore, in the present invention, 25.0xl pi BTU'hr + 4.3
xlpiBTU/hr46.2xlpiBTU/hr or approximately 63.2%
) (48.7 x 1 pkj/hr).

Significantly, the present invention yielded higher efficiency even though the reforming reactant combustion heater had greater capacity than the corresponding heater in prior art processes.

This is because the reactor 11 effluent is utilized to provide a portion of the heat demand for the stabilizer and is not utilized to preheat the feedstock mixture. Accordingly, the reforming reactant combustion heater capacity is increased to compensate for the low level of feedstock heat. For this reason, it is not readily apparent that utilizing the reactor effluent and convective heating section to reboil the stabilizer will increase fuel efficiency. The heater capacity is effectively higher because it is shifted from the higher efficiency stabilizer repoiler combustion heater of the prior art to the lower efficiency trout irradiation heating section of the modified reactant combustion heater in the present invention. There is no expectation that shifting heater capacity from a higher efficiency heater to a lower efficiency heater will result in the overall increase in fuel efficiency achieved by the present invention. It will of course be apparent to those skilled in the art that various reactor effluent heat exchange flow patterns can be utilized in the present invention, although not with equal results. In the embodiment of the drawing, the portion of the reactor effluent that undergoes a first indirect heat exchange with the reformate is the portion of the reactor effluent that undergoes a second indirect heat exchange with a mixture of hydrocarbonaceous feedstock and hydrogen. are different parts. On the other hand, the flow pattern of the heat exchange of the reactor effluent is such that the part of the reactor effluent that undergoes the second indirect heat exchange with the hydrocarbon feedstock and hydrogen previously undergoes the first indirect heat exchange with the reformed gasoline. It can also be prepared to contain at least a portion of the reactor effluent. The simple illustrations in the drawings are flow sheets of one embodiment of the present invention.

Claims (1)

[Claims] 1 (a) A mixture of hydrocarbon feedstock oil and hydrogen is heated in a radiant heating section of a combustion heater, and then the heated mixture is brought into contact with a reforming catalyst under reforming conditions to react and flow out. (b) performing a first indirect heat exchange of at least a portion of the reaction effluent with a portion of hydrocarbon reformed gasoline;
c) subjecting at least a portion of the reaction effluent to a second indirect heat exchange with said mixture of hydrocarbonaceous feedstock and hydrogen prior to heating in a combustion heater; (d) enriching the reaction effluent with hydrogen; separating a vapor phase and a substantially liquid hydrocarbon phase, recycling at least a portion of the hydrogen-rich vapor phase for mixing with the hydrocarbonaceous feedstock, and (e) converting the liquid phase into a stabilizer. into a column, the column being maintained at rectifying conditions sufficient to provide an overhead fraction consisting of normally gaseous hydrocarbons and a bottom fraction consisting of hydrocarbon reformed gasoline at standard temperature and pressure; (f) recovering and reheating a first predetermined quantity of hydrocarbon reformate gasoline by indirect heat exchange with hot combustion gas in the convection heating section of the combustion heater of step (a); returning the reheated reformate to the stabilizer column to provide a fixed amount of heat to the column reboiler; (g) recovering a second portion of hydrocarbon reformate, which is used as the reaction effluent in step (b); catalytic reforming comprising the steps of: (h) recovering a third portion of the hydrocarbon reformed gasoline as product; quality law. 2. The fixed amount of heat supplied by the first predetermined amount of hydrocarbon reformed gasoline is between 50 and 80% of the heat requirement of the reboiler of the stabilizer column. Method of scope 1. 3. The method according to claim 1 or 2, wherein the amount of the reaction effluent that undergoes first indirect heat exchange with hydrocarbon reformed gasoline is determined according to a predetermined stabilizer tower reboiler temperature. . 4. A patent in which the portion of the reaction effluent that undergoes the first indirect heat exchange with the reformed gasoline is different from the portion of the reaction effluent that undergoes the second indirect heat exchange with the mixture of hydrocarbonaceous feedstock and hydrogen. The method according to claim 1. 5. A patent claim in which the portion of the reaction effluent that undergoes second indirect heat exchange with the hydrocarbonaceous feedstock and hydrogen includes at least a portion of the portion of the reaction effluent that previously underwent first indirect heat exchange with reformed gasoline. The method according to the first term of the scope.