DE2634493A1 - Control system for hydrocarbon hydroconversion processes - monitoring process parameters and regulating hydrogen/hydrocarbon mole ratio - Google Patents

Abstract

The hydrogen/hydrocarbon mole ratio is continuous, hydrogen-consuming, hydrocarbon hydroconversion processes, is controlled by employing analyser to monitor composition characteristics of the charge stock of the liquid reaction effluent and the hydrogen concentration of the vapour phase introduced into the reaction zone, and transmitting representative output signals to comparator/computer means which generate additional comparator output signals which are then utilised in the control system for regulating the H2/hydrocarbon ratio. The technique is applicable to processes in which the reaction zone effluent is separated into liquid and hydrogen-rich vapour phases, a portion of the later being recycled in the reaction zone. The method compensates rapidly for changes in charge stock characteristics and operating parameters and maintains catalyst activity and stability.

Description

Method and device for regulating

lation of the molar ratio of hydrogen to hydrocarbon in the reaction zone of a continuous hydrocarbon conversion process The procedure for adjusting and controlling the ratio of hydrogen to Hydrocarbon and the control system for carrying out the method according to the Invention described herein are generally applicable to methods of catalytic conversion of hydrocarbons in a hydrogen-containing atmosphere, hydrogen consumption occurring in this process. Such procedures are for example hydrocracking processes with the formation of low molecular weight Hydrocarbons, a hydrogenation of olefinic hydrocarbons to form the corresponding Paraffins and hydro refining (desulfurization) for the purpose of removal of impurities, etc. In all of these processes, as in most of the hydrogen-producing ones Process, such as catalytic reforming, includes a commonly proposed one Technique the use of a hydrogen-rich vapor phase that is recycled to it with the fresh hydrocarbon feed to the reaction zone to unite. Practical reasons for using this technique are: to maintain both the activity and the operational stability of the catalyst which is used to bring about the desired reactions, as well as the guarantee, to get the product you want. The latter is more difficult to achieve in hydrogen-consuming Procedure with regard to the generally required harsher operating conditions. In hydrogen-producing processes, such as catalytic reforming, more hydrogen than is required for recycling purposes, recovered and in others Uses processes that are integrated into the overall refinery. For example, will Excess hydrogen from a catalytic reformer, often as make-up hydrogen used in a hydrocracking process. Regardless of the specific procedure, the recycled hydrogen generally by condensing the reaction zone product outlet, most often at a temperature in the range of about 16 to about 600 C (60 to 1400 F), and introduction of the outlet thus cooled into a vapor-liquid separation zone obtain. That portion of the recovered vapor phase, the required is to meet the hydrogen requirement in the reaction zone, is recycled, to deal with the hydrocarbon feed prior to its introduction into the reaction zone to be united.

The literature is teeming with hydrocarbon conversion processes wherein a relatively hot reaction zone outlet condenses and cools and into a High pressure separation device is introduced, from which a hydrogen-rich vapor phase and recovering a normally liquid product phase. General will at least some of the vapor phase is returned to the feed material without further treatment to be combined prior to its introduction into the catalytic reaction zone. In however, in some cases, usually when working with sulfur, this proportion becomes the vapor phase to be returned is treated in order to remove contaminating influences, which would have an adverse effect on the reaction zone environment.

An example of the various procedures using this basic method and to which the present invention is directed is the process of pentane isomerization U.S. Patent No. 3,131,325. Similarly, U.S. Patent No. 3,133,012 illustrates this method in U.S. Patent No. 3,133,012 their application to a catalytic reforming system. U.S. Patent No. 3,718,575 to is directed to a two-step hydrocracking process, the reaction product effluent becomes cooled from the second stage prior to its introduction into the vapor-liquid separation zone, the hydrogen-rich stream from it is returned to the first stage to make him to unite with the feed material. The present proceedings to the Regulation of the molar ratio of hydrogen to hydrocarbon in the combined Feed to the catalytic reaction zone and the control system therefor are applicable to any hydrocarbon conversion process in which a hydrocarbon feed and hydrogen are reacted with one another in a catalytic reaction zone. Therefore, the present invention can be easily modified with minor modifications in procedures be integrated, such as hydrogenation processes, isomerization processes, hydro refining processes, Hydrocracking processes, hydrodealkylation processes, dehydrogenation processes and catalytic Reforming process.

Examples of hydrocracking processes that incorporate the present invention can be integrated are those reaction schemes and methods described in US Pat 3,252,018, 3,502,572, and 3,472,758 are described. Hydrocracking reactions are generally at elevated pressures of about 34 to about 340 atmospheres (500 to 5000 psig) carried out. Circulating hydrogen is supplied with the feed in an amount from about 3000 to about 50,000 scf / Bbl mixed1 including the make-up hydrogen from an outside source. The feed material comes into contact with the catalyst, located in the hydrocracking reaction zone at a liquid hourly space velocity from about 0.25 to about 5.0. Since the bulk of the reactions is exothermic, poses a temperature rise is observed when the reactant flow of feed material and hydrogen passes through the catalyst layer. The catalyst bed temperatures are generally at a maximum in the range of about 371 to 4820 C (700 to 9000 F) held and they will conveniently by using conventional Cooling streams are set, and these cooling streams are usually vapor and are introduced directly into the catalyst layer at a central point thereof.

The procedures briefly described above are examples of those in to which the present invention can be applied to advantage. In all such Process establishes the molar ratio of hydrogen to hydrocarbon in the combined Feed to the reaction zone is an important process variable.

Changes in the characteristics of the feed composition require changes in the molar ratio of hydrogen to hydrocarbon in order to maintain acceptable catalyst activity and stability. aside from that are changes in the severity of the conditions in the reaction zone (mainly Temperature and pressure), required if the product quality and / or product quantity change changes. However, this in turn influences the molar ratio of hydrogen / hydrocarbon. Changes in the molar ratio of hydrogen to hydrocarbon also affect it something the product quality and / or product quantity. In short, according to the present Control method sensed a characteristic of the feed composition (it can also a characteristic of the product composition can be derived), and also the Concentration of hydrogen in the vapor phase entering the reaction zone with the feed material is introduced, sensed. Appropriate representative output signals become one Parent computer sent, in turn Computer output signals generated, which are sent where they are necessary to the hardness of the Conditions in the reaction zone (temperature and pressure), the feed flow and adjust the recycle gas flow so that the molar ratio of hydrogen to hydrocarbon is regulated while maintaining the desired product quality and / or Get product quantity. In hydrogen-consuming processes, such as hydrocracking with the formation of low molecular weight hydrocarbons, are match checker output signals sent where they are required the amount of supplemental hydrogen regulate which from an outside source is introduced into the process, and around the flow of any stream for cooling the temperature in the reaction zone to regulate.

A main object of the present invention is the molar ratio from hydrogen to hydrocarbon in a catalytic hydrocarbon conversion process to control and adjust, and especially in those procedures where the reactions are hydrogen consuming. A subsequent goal is the catalyst activity and to maintain catalyst stability while producing the desired product receives.

Another goal is to have a control system and one related to it Method of controlling the molar ratio of hydrogen to hydrocarbon to get. In connection with this, it is a specific aim to obtain a procedure that quickly changes in the feed material characteristics and the operating parameters compensates for what changes an adjustment in the molar ratio of hydrogen to make hydrocarbon in the catalytic reaction zone required.

Therefore, one embodiment of the invention is a control system for use in a continuous hydrocarbon conversion process, in which hydrogen is consumed and in the 1st a hydrocarbon-containing one Feed material and hydrogen are introduced into a preheater, has the facilities for the supply of heat from the outside that are operationally connected to it, 2. the resulting heated mixture of feedstock and hydrogen in a catalytic reaction zone is reacted, 3. the resulting effluent stream the reaction zone is condensed and separated and thereby a liquid phase and supplies a first hydrogen-containing vapor phase, 4. at least part of the first Vapor phase returned to the preheater in admixture with the feed material and 5. a second hydrogen-containing vapor phase from an external source in the process is introduced, at least a portion thereof with the first hydrogen-containing Mixed vapor phase and introduced with her into the preheater.

The control system for adjusting the molar ratio of hydrogen Su includes hydrocarbons in this reaction zone as a cooperating combination a) a first flow varying device operable with the preheater is connected to adjust the amount of heat supplied to it, b) a first flow sensing Device that controls the flow rate of the feed material into the reaction zone measures and generates a first representative process output signal, and a second flow varying means which controls the flow rate of the feed material sets, c) a first analyzer taking a sample of the feed material records and a second representative of a characteristic of the composition of the feed material Process output generated d) a second flow sensing device which the flow rate of the second hydrogen-containing vapor phase, which is in the Method is introduced and a third representative of this vapor phase Process output generated, and a third flow varying means, the adjusts the flow rate of the second vapor phase, e) a second analyzer, the one sample of the hydrogen-containing vapor phase, which in the preheater is introduced, absorbs and a representative of their hydrogen concentration fourth process output signal generated, f) a third flow-sensing device, which is the flow rate of the hydrogen-containing vapor phase entering the preheater is introduced in admixture with the feed, measures and a fifth for its flow rate representative process output generated, g) means for sensing the pressure of the separated first hydrogen-containing vapor phase, which is a sixth generate representative process output signals for this purpose, h) a comparator, who i) receives or picks up the six process outputs and is operational responsive to these, ii) first, second and third comparator output signals generated as functions thereof, the control system being further characterized is that the comparator in conjunction with the first, second and third flow-varying Device via signal transmitting devices is at least one of the Comparator output signals too at least one of the river varying Transferring devices, with at least one of the variables i) the flow of the feed material, ii) the heat supplied to the preheater and / or iii) the flow of the second hydrogen-containing vapor phase to the process, in response to these signals is adjusted and the molar ratio of hydrogen to hydrocarbon is regulated will.

In another embodiment, the present invention provides a method of regulating the molar ratio of hydrogen to hydrocarbon in the catalytic reaction zone of a continuous hydrocarbon conversion process, in which hydrogen is consumed and in which 1. a hydrocarbon-containing Feed material and hydrogen in a preheater that works with it connected has a device for supplying heat from the outside, are introduced, 2. the resulting heated mixture of feedstock and hydrogen in the catalytic reaction zone is reacted, 3. the resulting effluent stream the reaction zone is condensed and separated and a liquid phase and a first hydrogen-containing vapor phase supplies, 4. at least part of this first Vapor phase returned to the preheater in admixture with the feed material and 5. a second hydrogen-containing vapor phase from an external source of the method is introduced into this and at least part of it with the first hydrogen-containing vapor phase mixed and with her in the preheater is introduced, and this process is characterized in that a) the the preheater amount of heat supplied by setting a first flux changing device operatively connected to the preheating device regulates, b) the flow of the feed material by adjusting a second Flow changing device, sensing the rate of flow of the feed and Generating a first, for a characteristic of the composition of the charge material representative process output, c) a sample of the feed material introduces into a first analyzer and therein one for a characteristic of its composition generates a representative second process output signal, d) the flow of the second hydrogen-containing vapor phase introduced into the process by adjustment a third flow changing device, sensing the flow rate of the second hydrogen-containing vapor phase and development of a third representative of it Process output signal regulated, e) a sample of the hydrogen-containing vapor phase, introduced into the preheater, into a second analyzer and therein a fourth representative of the hydrogen concentration of this sample Process output signal generated, f) the flow rate of the hydrogen-containing Vapor phase that is introduced into the preheater, senses and a fifth, generated for them representative process output signal, g) the pressure of the separated hydrogen-containing vapor phase and a sixth, representative for him Process output signal generated, h) a sample of the separated liquid phase introduces into a third analyzer and therein one for a characteristic of the composition this sample generates a representative seventh process output signal, i) the named seven process output signals to a comparator transferred and therein a first, a second and a third comparator output signal generated as functions of said seven process output signals and j) at least one of the three comparator output signals to at least one of the first, second and third flow changing means and that of the preheating means amount of heat supplied, the flow of the feed material and / or the flow of the second hydrogen-containing vapor phase and so regulates the molar ratio of hydrogen controlled to hydrocarbon in the catalytic reaction zone.

In another embodiment directed to methods where a cooling or quenching stream goes directly into the catalytic reaction zone for temperature control is introduced therein, the control system is as well characterized in that i) a fourth flow sensing device measures the flow rate a third hydrogen-containing vapor phase measures, with this sensing device a fourth modifying the flow introduced directly into the catalytic reaction zone Device is operatively connected, the sensing device a for the flow rate the seventh process output signal representative of the third hydrogen-containing vapor phase generated and this transmits to the comparator and ii) the comparator the first, second and third comparator output signals and a fourth comparator output signal as functions of said seven process output signals.

These and other objects and embodiments of the invention will become even more clearly recognizable from the following description.

The use and integration of sophisticated control systems in A petroleum refining process are commonly referred to as technological changes in the recent past.

Honesty, however, forces one to acknowledge the fact that the published Literature is constantly evolving in this technical field. For example U.S. Patent No. 3,759,820 discusses the systematic control of a process several reaction zones depending on two different quality features of the ultimately desired product. In a special explanation, the catalytic Involving reforming a naphtha feed are the two product qualities the octane number and the measured liquid yield.

Output signals that are representative of these two product qualities are used to vary the severity of the conditions in the reaction zone to regulate from these parameters. In U.S. Patent No. 3,751,229, the severity of the conditions in the reaction zone in a catalytic reformer depending on the octane number of the outlet liquid is controlled at the pressure of the reaction zone.

U.S. Patent No. 3,756,921 describes a control system for a benzene number zinc splitting column using an octane sensing device in connection with a flow meter for both the top and bottom flow. Override devices are used to prevent the splitting column becomes empty if excessive amounts of soil material should be produced. Similar U.S. Patent No. 3,755,087 describes the control a fractional distillation column, which works as a gasoline splitter, by measuring the octane number in the head fraction and adjustment of the return of the column as a function of this.

Another control of the severity of the conditions in the reaction zone depending on the octane number in the liquid outlet from a catalytic Reforming process is described in U.S. Patent 3,649,202. This is where the sharpness becomes of the conditions in the reaction zone in each of the three reaction vessels individually in Dependence on the octane number and the temperature difference in each of the reaction zones regulated.

The control system of the present invention also regulates the severity of the operating conditions in one or more reaction zones of one Hydrocarbon conversion process. However, there is one major improvement in that one prolonged use of the catalyst in the reaction zone in his gets optimal activity and that a maximum volume yield of the target product is realized through the economically effective total catalyst life. The present method consists in that of the molar ratio of hydrogen to hydrocarbon as a function of changes in feed composition and product composition, the composition of the reaction zone outlet and the running time of the catalyst is controlled at this point in time and thus a target product quality Gets effective catalyst activity over a long period.

In short, the preferred method is to have the product with regard to one feature, the feed with regard to one Characteristic of their composition and the recycled vapor phase in terms of Hydrogen concentration analyzed and operating variables such as reaction zone temperatures, Pressure, flow rates, etc. Output signals relevant to these parameters are representative are sent to a computer comparator which provides further output signals generated that regulate the severity of the conditions in the reaction zone, flow rates, etc. can be used.

A complete refinery in the petroleum industry includes a variety of hydrocarbon conversion processes used for the main purpose of obtaining a specially desired product quality are linked to one another. Such procedures are for example catalytic reforming of naphtha fractions with formation of a liquid product with a relatively high octane number, hydrocracking with formation low molecular weight hydrocarbons, some of which are used as feed / the catalytic reforming unit can be used to form paraffin dehydration of olefins, hydrocarbon isomerization and hydro refining for the purpose the removal of impurities, etc. Also contain numerous refineries Process for the production of special compounds used as petrochemicals will. Examples of this are aromatic isomerization with the formation of paraxylene or an alkylation with formation of alkyl-substituted aromatics. These procedures close hydrogen-consuming reactions and / or hydrogen-producing reactions Reactions and are generally caused by the fact that the hydrocarbon-containing Feed material with a catalyst in a hydrogenous atmosphere at treated at elevated temperature and pressure.

For the sake of abbreviation, the following discussion of the invention concept, its function and the method used to implement this concept on hydrogen consuming Procedures and specifically on well-known and carefully documented hydrocracking procedures directed. However, such a special discussion is not intended to serve to explain the present To limit inventive ideas in any way.

In catalytic hydrocarbon conversion processes such as those above have been cited by way of example, a common practice is the recycling of a hydrogen-rich Steam phase to combine with the fresh batch. The experience has taught that this method maintains a "clean" catalyst: what a promotes acceptable catalyst activity and stability which are required are designed to function effectively over a long period of time. Regardless of whether you are now a one-step process or a multi-step process is obtained the recirculated hydrogen-rich vapor phase from the outlet of the reaction zone via high pressure separation at a temperature in the range of about 16 to 600 C (60 to 1400 F). In a hydrogen-consuming process, such as hydrocracking, is the proportion of the separated outflow from the reaction zone that contains hydrogen, insufficient and must be supplemented with hydrogen from a suitable external source of the process, such as hydrogen from a catalytic reforming process, which forms abundant hydrogen.

Besides the reaction zone temperatures, pressures and space velocities it is generally accepted that the molar ratio of hydrogen to hydrocarbon the combined feed to the reaction zone is an extremely important operating variable represents. Require constantly changing characteristics of the feed composition corresponding changes in the molar ratio of hydrogen to hydrocarbon, to maintain acceptable catalyst activity and stability. If the product quality and / or the amount of product changes, the sharpness must the conditions of the reaction zone, mainly temperature and pressure, of necessity can be set. But this in turn influences the molar ratio of hydrogen to hydrocarbon.

According to the present control method and in the present control system a characteristic of the feed composition is sensed, and the Concentration of hydrogen in the vapor phase introduced into the reaction zone is also sensed. The latter is in a hydrogen-consuming Process partially separated hydrogen and partially supplemented hydrogen from an outside source. A compositional characteristic is also included in a preferred system a separated liquid product-containing stream sensed. Appropriate output signals are sent to a comparator computer, which in turn is computer Output signals generated that are passed on in such a way that they reduce the sharpness of the Conditions in the reaction zone (temperature and pressure3, the feed flow and adjust the flow of the make-up hydrogen-containing vapor phase as necessary is, to regulate the molar ratio of hydrogen to hydrocarbon. As already has been found, in many hydrogen-consuming processes the exothermic Heat of the reactions, which causes a substantial rise in temperature, though the reactants cross the catalyst, within certain limits by the Use of a hydrogen cooling stream discontinued. An additional procedure output signal representative of the flow rate of the cooling stream is sent to the comparator. This is related as a function of the same with the other process output signals, an output signal develops and closes sent to the flow changing device, through which the flow rate the cooling current is set. Also, output signals that are representative for the inlet and outlet temperature of the reaction zone and for the pressure of the vapor phase, which is separated from the product outlet of the reaction zone, to the comparator computer sent. In one embodiment, the signal emitted by the print of the separated liquid phase is dependent, be transferred directly in such a way that it increases the flow rate of the make-up hydrogen introduced from the external source. To this The comparator output signals are representative of all operating variables, which is the molar ratio of hydrogen to hydrocarbon or the hydrogen partial pressure affect in the reaction zone as well as the product quality and / or product quantity.

Before commissioning a hydrocracking plant or other hydrocarbon conversion plant first the different Operating variables determined, by looking at a predictable product quality and / or product quantity Directed yield estimate based on a relatively detailed analysis of the hydrocarbon feed undertakes. Feed material analyzes generally include molecular weight, the specific gravity, the boiling range and the relative concentrations of the different types of hydrocarbons.

The estimated hydrogen to hydrocarbon molar ratio required is calculated and the computer comparator is programmed accordingly to do the Maintain specified molar ratio. Changes in feed composition characteristics are transmitted to the computer comparator as from the flow rate of the Feed. The pressure and flow rate of the recycled vapor phase as well as their hydrogen concentration are also transmitted to the computer comparator. The latter calculates the required molar ratio of hydrogen to hydrocarbon back and transmits corresponding output signals to the values determined in this way to adjust. A later change in product quality and / or product quantity is sensed and the computer comparator adjusts the furnace firing accordingly such that the reaction zone temperatures are regulated, and / or he sets the operating pressure in the reaction zone so that the desired product properties maintains. The computer comparator then compares the resulting molar ratio from hydrogen to hydrocarbon and in turn transmits corresponding output signals, to achieve the optimum.

The control system of the present invention uses at least three catalysts, two of which are used to determine Compositional features mainly serve liquid streams and the third of which is the hydrogen concentration determined in the part of the hydrogen-containing vapor phase that is mixed with the Feed material is introduced into the reaction zone. One of the hydrocarbon catalysts generates an output signal that is correlated with a compositional property of the hydrocarbonaceous charge and representative of this characteristic is. Details of such a hydrocarbon analyzer can be found in US Pat 3 463 613. As is stated there, a compositional characteristic a hydrocarbon sample by burning it in a combustion tube be determined under conditions that produce a stabilized cool flame. The position of the flame front is automatically determined and used to generate a signal which in turn is used to set a combustion parameter such as the combustion pressure, the induction zone temperature or the air flow, in one Way of changing the flame front regardless of changes in composition immobilized on the hydrocarbon sample. The change in the combustion parameter, which is required to remove the flame front after a change in composition immobilizing the sample is correlated with the change in the compositional characteristic bring to. A suitable reading device associated therewith can relate to be calibrated with the desired identifiers, such as molecular weight, the boiling point, the ratio of vapor to liquid, etc.

The hydrocarbon analyzer includes a generator for a stabilized cool flame with a servo-controlled flame front. The type of received Analysis is not an analysis of connection by connection as is the case with instruments, such as mass spectrometers or vapor phase chromatographs. In contrast, the Analysis represented by a continuous output signal that is dependent on of the hydrocarbon composition stands and displays it and more specifically in correlation with one or more conventional identifications or specifications can be brought from petroleum products.

Other examples of generators and a cool flame with servo-controlled Flame fronts and their use for the analysis of hydrocarbon compositions and for sensing the same, see U.S. Patents 3,533,745, 3,533,746, and 3,533 747. It is this type of hydrocarbon analyzer that is also used for sensing one or more compositional features of the liquid stream is preferred, which is separated from the effluent containing product from the reaction zone.

Regarding the hydrogen concentration in the in the reaction zone introduced vapor phase are chromatographic sensing devices of the gas-solid type using a bed of zeolitic molecular sieves. Also is a density sensor calibrated for mole percent hydrogen is useful for use as an analyzer. Still other suitable analyzers are pressure difference sensing devices, which determine the partial pressure of hydrogen, the through a diaphragm diffused from hot palladium. In either case, the two hydrocarbon analyzers produce and the hydrogen analyzer output signals relevant to the composition characteristics and the hydrogen concentration are representative, and these output signals become transmitted to the computer comparator.

The present control system and the procedure for regulating the Molar ratio of hydrogen to hydrocarbon uses a computer comparator, the various output signals from the current analyzers and operating variable indicators or transmitters, generates computer output signals and transmits them to various Control devices and / or control loops throughout the process transmitted. Signals recorded by the computer are recorded in advance with it Signals compared to the actual value of the stream composition characteristics and to determine the hydrogen concentration. Preferably the computer determines also their change. More output signals recorded by the computer represent those associated with the transition zone or zones Temperatures, the flow rate of the fresh feed, the flow rate the vapor phase introduced into the reaction zone with the feed material, the Temperature of the feed material after heat exchange with the hot outlet stream the reaction zone, the flow of the entire vapor phase from the high pressure separator and the pressure of the vapor phase from the separator. Still other process output signals, which are transmitted to the comparator computer represent the amount of supplementary hydrogen-containing vapor phase, which in the process of an external Source introduced the amount of which corresponds to the vapor phase of the Reaction zone outlet is combined, and the amount of reaction zone cooling used hydrogen-rich vapor phase.

As follows in more detail with reference to the drawing is described, the computer comparator, which was previously programmed in such a way, generates that he selects the optimal molar ratio of hydrogen to hydrocarbon, further comparator output signals depending on all of the recorded signals, leading to a control loop that allows adjustment of the amount of fuel too the heater into which the reaction zone feed is introduced causes to feed flow control devices, to control devices that control the flow of additional hydrogen-containing vapor phase, which is introduced into the process, adjust, and to control devices that control the amount of vapor phase used as cooling agent is introduced directly into the reaction zone, regulated, transmitted. if a part of the separated vapor phase is removed from the process, a comparator output signal be communicated so as to control the facility adjusting their amount. Any one or more of the additional computer output signals indicate that there is no change in any of the variables described above Regulations is required. The computer comparator can include the accessories, which for a comparison of the actual values of the received signals with previously determined th deviation limits and for generating adjustment signals is required depending on this comparison.

For example, the practical maximum catalyst bed temperature can be in any particular process critical to catalyst activity and product quality be. Should the comparator set a trend to exceed the relevant Display limit, a corresponding setting signal is transmitted. This is especially important in a hydrogen-consuming process where a rising Temperature gradient is determined when the reactants pass through the catalyst layer go through. In a hydrocracking process, the maximum catalyst temperature could be at 5100 C (9500 F) so that appropriate adjustment signals are transmitted if other computer output signals tend to go beyond this To indicate deviation.

The accompanying drawing explains various embodiments of the present control system, which integrates into a one-step hydrocracking process is. However, it is not intended to limit the invention thereby. For Modifications to the schematic flow diagram are available to those skilled in the art Hand.

The hydrocracking process chosen as an example is for a single stage Plant shown, which has a reaction zone or a reactor 7, a heat exchanger 3, a feed heater 5, a high pressure separator 13, a blower 18, an overload drum 15 and a computer comparator 95. The latter receives one or more different process output signals over the instrument lines 40, 44, 98, 49, 52, 57, 62, 66, 69, 73, 80, 85, 90 and 94, generate other computer output signals and sends it over instrument lines 36, 46, 58, 81 and 86. The hydrocarbon analyzer 37 receives a sample of the feed material from line 1, generates one for one Composition characteristic of the same representative starting material and sends this Starting material via the instruments line 40 to the computer comparator 95. The analyzer 78 takes a sample of the recycled hydrogen-rich vapor phase in line 2, produces a representative of the hydrogen content of the same Output signal and transmits this signal via the instrument line 80. The Composition properties of the feed (line 1) and the separated liquid phase (line 16), which are determined by analyzers 37 and 91, are mainly due to the special hydrogen-consuming process in to which they are applied. Similar to a hydrocracking process these compositional characteristics based on the particular feed material and the product composition to be obtained therefrom. Consequently the analyzers can be identical or not identical.

The hydrocarbon analyzers 37 and 91, the samples of the hydrocarbon containing Generators can take up charge or the separated liquid phase Use for a stabilized cool flame with a servo-controlled flame front. The flow for oxidizer (air) and fuel (the sample received) are fixed, and also the induction temperature. The combustion pressure is the parameter that is changed to immobilize the flame front of the cool flame. If a change is found in the selected compositional characteristic, delivers the Change the combustion pressure as required is to immobilize the flame front, a signal that is a direct follow-up indication The change is common operating conditions for these hydrocarbon analyzers are: an air flow of 3500 cc / min. (STP) r a fuel flow of 1.0 ccm / min., an induction zone temperature in the range of about 343 to about 441 C (650 to 8250 F) and a varying combustion pressure of about 0.272 to 1.36 atmospheres (about 4.0 to about 20.0 psig).

For example, if the hydrogen consuming process is a hydrocracking process is where the desired result is maximum production of hydrocarbons If the gasoline boiling range is made of heavier material, the analyzer can take the shape of an analyzer for the ratio of vapor to liquid similar to that described in U.S. Patent 3,491,585. In situations where the feed material is intended for LPG (liquefied petroleum gas), in which propane and butane predominate, a boiling point monitor or a chromatographic analyzer can be used. The sample is vaporized into the carrier stream, generally helium, and with this in promoted the chromatographic column. The column prevents the passage of the Materials in the sample as a function of their boiling points and carbon chain lengths. When the carrier gas leaves the column and is introduced into the detector, it carries it with itself components in the order according to their respective boiling points.

To control the molar ratio of hydrogen to hydrocarbon To effect, the hydrogen concentration in the vapor phase must be that with the fresh Feed material is mixed, be known. This is how the Analyzer 78 provides a process output representative of the hydrogen content the vapor phase in line 2 is. The sample is introduced via line 79, and the representative output signal is transmitted via line 80. As stated above the analyzer 78 is only required to provide a process output that is representative of the hydrogen concentration. So he can from a variety of suitable devices described in the prior art are selected.

As stated above, the hydrocracking occurs in an or in several catalytic reaction zones with a fixed catalyst bed, depending on the desired product quality from a given feed material. For example U.S. Patent No. 3,771-8,575 describes a multi-stage hydrocracking process for LPG production. The feed material boils above the gasoline boiling range, such as a full boiling range gas oil with an initial boiling point of about 2600 C (5000 F) and a final boiling point above 5380 C (10000 F). In its original condition if such a feed material contains impurities in the form of nitrogen and sulfur compounds and is therefore initially subjected to hydro refining, in which these detrimental impurities in ammonia, hydrogen sulfide and Hydrocarbon are converted. Hydro refining is one of the most hydrogen consuming Method in which the control system according to the invention can be used to advantage can.

Hydrocracking reactions will occur at catalyst bed temperatures in the range from about 3430 C to about 5100 C (650 to 9500 F), and preferably at about 3710 C to about 4820 C (700 to 9000 F). The reaction zones are under one applied pressure of about 34 to about 340 atmospheres (500 to 5000 psig), wherein generally the upper limit is about 170 atmospheres (2500 psig). The speed of the hydrocarbon feed flow is liquid hourly space velocity from 0.25 to about 5.0 and the hydrogen concentration is in the range of 3000 up to about 50,000 scf / bbl.

Of all the hydrogen-consuming processes, this shows hydrocracking the greater degree of exotherm. To control the temperature rise when the reactants go through the catalyst layer, therefore becomes a cooling stream, generally a hydrogen-containing cooling stream, directly into the catalyst bed one or more intervening places of the same introduced.

The selection of the catalytic composition for use in the hydrocracking zones is mainly based on a detailed analysis of the fresh Feed material and the estimate of the yield of the desired material based thereon The product determines and is based on the product quality and quantity. Although the catalyst composition tailored for the intended use is, it generally comprises at least one metal component from the groups VIB and VIII of the Periodic Table of the Elements, Rhenium, Tin and Germanium, the be combined with a silica-containing refractory material, which about 12.0 to about 30.0 weight -% contains clay. The stand the art shows that a catalyst is preferred where the metal components pass through Impregnation or ion exchange in a crystalline aluminosilicate molecular sieve and various such molecular sieves are commonly referred to as "Zeolites" referred to.

Such a catalyst that has the desired characteristics of activity and shows stability, is a composition of, for example, about 5.3% by weight Nickel and a synthetically produced faujasite that is present in the entire silica base is distributed. Other suitable zeolitic materials are, for example, mordenite, Molecular sieves of the type X or Y as well as zeolitic materials, which are in an amorphous Alumina, silica or alumina-silica base material are dispersed. The exact composition of the catalyst used in hydrocracking or in any the conversion processes described above, in which hydrogen is consumed, is used does not constitute an essential feature of the present invention In addition, it is not intended that the invention be directed to a method with a specific number be limited to individual reaction zones. Although the invention as a one-step Procedures related to. the drawing is explained, so it is easily applicable to a two-step or three-step process.

Than understanding the catalytic reaction mechanisms in hydrogen consuming Procedures and especially when Hydrokrakken increased, it became possible to change the operating methods and operating conditions with specific catalysts in correlation with each other and to the feed material properties to put to so the To improve the quality and quantity of the target product. Although the intended Hydrocracking in all situations is the same for higher molecular weight hydrocarbons To crack in lower molecular weight hydrocarbons requires operating conditions and to select operating methods that ensure the reasonably effective time during which the selected catalyst retains its intended function. Problems and difficulties associated with controlling a hydrocracking process, to wisely promote effective catalyst life (commonly defined as Barrels of fresh feed per pound of catalyst in the reaction zone) are essential more amazing than many other hydrocarbon conversion processes, especially those classified as hydrogen producing processes.

Some of these problems have been at least partially addressed by the introduction various procedural methods facilitated. For example, if the temperature increase is excessively large, direct cooling currents are used. Also feed material diluents, generally lower boiling range, are somewhat effective.

Essential problems and difficulties remain and come from one Variety of aspects including a constantly changing composition the fresh loading with the accompanying effect of the desired product quality and the required changes in the severity of the reaction zone conditions. This appeals to the fact that a common method is to remove that portion of the Product discharge that boils at temperatures above the desired product, due to i.e. for example when producing a liquid Product in the naphtha boiling range is returned to that part of the outlet that boils above about 1990 C (3900 F). Different compositions of the total outlet the reaction zone also affect the product quality and quantity and the severity of operation in the reaction zone as a result of a change in the Vapor phase and liquid phase compositions used in the high pressure separator separated from each other. In addition, the introduction of the cooling stream or of cooling streams directly into the catalyst in the reaction zone is a factor that contributes to the procedural control concerned. Also is normal deterioration of the active components in the catalytic converters, their speed partly by using recycled hydrogen in amounts based on the flow of fresh feed is decreased.

In terms of the above, the achievement is continuous the target product quality and target product quantity with simultaneous extension The effective life of the selected catalyst poses a dilemma for the refiner disturbs.

A control of the hydrogen to hydrocarbon molar ratio according to the present invention effectively solves the problems and thus avoids them difficulties associated with them.

The present method of controlling the molar ratio of hydrogen to hydrocarbon in a catalytic hydrocarbon conversion process, in which hydrogen is consumed and the control system for this become clearer under Understandable with reference to the accompanying schematic drawing. Although the drawing is based on a one-step catalytic process with fixed Is directed to the catalyst bed, the process is equally well suited for multi-stage hydrogen-consuming processes as mentioned above. Although the descriptive explanation continues on the production of liquid Petroleum gas (LPG) is directed from hydrocarbons from the naphtha boiling range, should the invention should by no means be limited thereto. In the drawing are process flow lines including sampling points and larger system parts therein than solid ones Lines shown, while the dashed lines signal transmitters to and from the computer comparator and in the cascade control loops shown mean. The drawing is described in connection with a large-scale plant, which is designed to contain maximum amounts of a propene / butene concentrate of 10 200 Bbl / day of a comparatively light naphtha fraction with a specific one Weight of 64.00 API, an initial boiling point of about 790 C (1750 F) and one Final boiling point of around 1200 C (2480 F) produced. In the procedure according to the drawing become 1016.0 mol / hour the fresh naphtha charge into the process via line 1 in a mixture at 548.7 mol / hour.

a recycled liquid pentane + stream introduced, the Source of the latter is described below. A hydrogen-rich one, mainly vapor phase in line 2 is thus in an amount of 9981.5 mol / hour. (79.3 % Hydrogen) and the mixture continues through line 1 into the heat exchanger 3. The heat exchanger 3 is an indirect one Heat exchanger generally of the tube and cup type.

The mixture of hydrogen and hydrocarbon is at a temperature at about 72 ° C (161 ° F) and a pressure of about 78.5 atmospheres (1155 psig). The heating medium is the relatively hot reaction zone outlet into the heat exchanger is introduced via line 9. The thus preheated mixture is via line 4 with a temperature of about 3210 C (6100 F) and a pressure of about 76.5 atü (1125 psig) is introduced into a direct fired furnace heater 5. Although the heater 5 some kind of heat exchanger using different heating media, such as water vapor, hot oil, hot steam, flue gas etc. can be to the required To get high temperature, the heater is generally a direct fired oven, as illustrated.

The heated reaction mixture is from the direct fired heater 5 withdrawn via line 6 and into a reaction zone 7 with a fixed catalyst layer having a temperature of about 3430 C (6500 F) and a pressure of about 74.1 atmospheres (1090 psig) was introduced. In this example the catalyst contains in the reaction zone 7 about 5.0% by weight of a nickel component (calculated as elemental metal) combined with a carrier material made of dispersed in a silica base material synthetic faujasite. Since the main reaction is a hydrocracking reaction, the relative is strongly exothermic, as stated above, one gets a temperature rise, when the reactant stream traverses the catalyst bed.

In this particular case, the operating methods determine a maximum Temperature rise of about 380 C (1000 F). Therefore becomes a hydrogen-rich one Stream via line 8 into the middle of the reaction zone at a temperature of about 490 C (1200 F) introduced. The outlet from the reactor 7 goes through line 9 into the Heat exchanger 3, in which it is used as a heating medium for the fresh feed and the recycled hydrogen before it is introduced into the direct-fired one Preheat heater 5. After the heat exchange, the reaction zone becomes the outlet in line 10 in the cooler thus a temperature of about 1060 C (2230 F) and introduced at a pressure of about 69.0 atmospheres (1015 psig). The reaction zone outlet cooled in this way is via line 12 in the high pressure separation device 13 with a temperature of about 38 C (100 F) and a pressure of about 68 atm (1000 psig).

A mainly vapor phase is produced by the separation device 13 withdrawn via line 14 and introduced from there into an overload drum 15. The LPG-rich, mainly liquid phase is drawn off via line 16 and in suitable separation devices for the removal of vaporous material, mainly hydrogen, methane and ethane, and hydrocarbons with more than about 4 carbon atoms per molecule resulted from it. The latter are in a Amount of about 548.7 moles / hour. returned to them with the feed material to be combined in line 1 before the sample is introduced into analyzer 37. The final product in an amount of about 12800 bbl / day (1942 mol / hour) contains about 99.1% propane and mixed butanes. The overload drum 15 is used to carry along, normally liquid material from the separated vapor phase in line 14 to remove, and this material will be periodic via line 19 withdrawn with valve 20. The remaining vapor phase is drawn off via line 17 and thereby introduced into the blower 18 to be returned via line 2 to line 1 where it is mixed with the hydrocarbon feed and into the heat exchanger 3 is introduced. At least part of the recycled vapor phase in line 2 is diverted via line 8 and directly into the reaction zone 7 as a cooling stream or quenching current introduced.

Make-up hydrogen to that consumed in reaction zone 7 Replacing hydrogen is introduced into the process via line 21. The hydrogen concentration is about 85.0% on a mole basis. This complementary hydrogen-rich Current is passed over the fan 18 through line 22, from which he with the cooled reaction zone product outlet in line 12 is mixed to thereby in the high pressure separator 13 to be introduced. Situations arise where clever operating methods include removing some of the recycled vapor phase make necessary in line 17 through line 23 with control valve 24. Although the control valve 24 can operate in dependence on a computer output signal, which via the instrument line 81 (as explained) is transmitted, it can also through Transmission of the signal from a pressure transmitter 68 (not explained) set directly will. Similarly, the control valve 25 in the make-up hydrogen line 21 can either via a computer output from an instrument line 86 or directly in Dependence on the signal which is transmitted via line 26 from the pressure indicator 68 will be set. The person skilled in the art recognizes of course that both control valves 24 and 25 receive output signals in a particular situation can.

The withdrawal of the mainly liquid phase from the high pressure separator 13 via line 16 is made by using a liquid level control system set and controlled, that from a liquid level sensing device that has a liquid level output signal through the instrument line 74 transmitted to the liquid level control device 75, which in turn regulates the operation of the control valve 77 by sending an appropriate signal through the instrument line 76 is transmitted. The liquid level sensing device can be a floating lever mechanism, a dielectric probe, a DP cell or any similar device capable of being in the lower section the high-pressure separating device 13 has a closure for a fixed liquid level maintain.

In the illustrated hydrocracking embodiment, the hydrocarbon analyzer is 91 set up to act as a boiling point monitor. A sample loop connects the analyzer 91 with the normally liquid separator bottom material in line 16 and consists of line 92 which carries a sample at a rate of about 100 ccm / min. removed, and line 93, the excess sample with a Speed of about 99 cc / min. returns. The sample itself is made from the Analyzer peeled off any middle section of the sample loop and at full line pressure and a carefully controlled speed of 1.0 cc / min. injected. The starting material can be calibrated as boiling points be and is this preferably and is fed to the computer comparator 95 via line 94 transmitted, which responds to the boiling point output signal and in turn a Comparator output generated as a function of the same.

In order to have optimal control of the molar ratio of hydrogen too To effect hydrocarbon in the reaction zone, the computer comparator takes 95 has a number of other output signals in addition to the output signal that representative of the compositional feature of the separated liquid phase in Line 16 is and these other process outputs indicate operating conditions in the process and other compositional features. The process output signals respectively.

Input signals to the computer comparator 95 include one that is representative of at least one compositional feature of the hydrocarbons Feed in line 1 is.

A sample of 100 cc / min. the feed material is through conduction 38 withdrawn and introduced into the hydrocarbon analyzer 37, the excess is returned via line 39. Appropriate compositional characteristics with which the process output signal is to be correlated, are for example the boiling point, the molecular weight, the density, etc. Of these, the molecular weight is of the feed material is preferred, since changes in it carry the greatest weight for the desired product quality and the molar ratio of hydrogen to hydrocarbon to have. It is, of course, within the concept of the inventive control system, use multiple analyzers to sense different feed material characteristics. This is how the instrument management mediates 40 one or more output signals, those representative of one or more compositional characteristics of the feed material are. The more process output signals transmitted to the computer comparator 95 naturally, the better the control of the molar ratio of hydrogen to hydrocarbon.

As stated above, the hydrogen concentration in the Vapor phase leading to the directly fired heater 5 in admixture with the feed material is returned in line 1, be known. The analyzer 78 thus generates a Process output signal representing the hydrogen content in the vapor phase in the line 2 is representative and can be correlated with it. The sample will is introduced via line 79 and the representative output is sent to the computer comparator 95 transmitted over line 80. Since in this example the analyzer 78 is only required is to produce a process output indicative of the hydrogen concentration is representative, it can be selected from a variety of suitable ones described in the prior art Facilities are selected.

Other process output signals that are generated and sent to the computer comparator 95 are operating variables and are used to set the present Control system to further improve and so the overall operation of the hydrogen consuming Process to improve. A basic operating variable is the pressure at which the vapor phase from the reaction zone outlet of the high pressure separation device 13 is separated. The output signal representative of this is transmitted via line 67 sensed by the pressure indicator 68 and via the instrument line 69 transmitted to the computer comparator 95. In addition, the flow indicator 43 senses the Feed material flow rate through line 1 via 42, such as measured by a flow-determining device 41, the latter being a venturi, Orifice, turbine meter or any other suitable device. That Feedstock representative of the feed material flow rate is transmitted via instrument line 44. In the same way is the flow rate the hydrogen-rich vapor phase, which is returned via line 2, through the flow determination device 59 measured via line 60 and flow indicator 61 and sensed, the output signal is transmitted via line 62.

Although not essential to the present control system for control the molar ratio of hydrogen to hydrocarbon, is preferred from the standpoint of the overall operation, are the flow rates of the liquid phase and the Vapor phase, which are separated from one another in the high-pressure separation device 13. The former is measured by flow meter 70 via line 71 to the flow indicator 72 transmitted, the output signal via line 73 to the computer comparator 95 is transmitted. The flow rate of the vapor phase that is separated and is withdrawn via line 14, is measured by the flow determination device 63, which transmits a signal via line 64 to the flow indicator 65, its output signal in turn transmitted to the computer comparator 95 via the instrument line 66 will.

Other output signals, the process conditions in the explained Conversion processes show are representative of various temperatures therein. One such temperature is that of the combined feed stream entering the heat exchanger 3 is preheated and introduced via line 4 into the directly fired heater 5. The temperature of the preheated stream is measured via line 96 and the temperature indicator 97 sensed. The latter transmits a representative output signal to the computer comparator 95 via instrument line 98. The inlet and outlet temperatures of the reaction zone is sensed and appropriate signals are sent to the computer comparator or sent. As noted above, the temperature difference (AT) is across to the catalyst bed is an important variable in a hydrogen consuming process regarding product specifications and catalyst activity and catalyst stability. The AT across the catalyst bed in reactor 7 is determined by the inlet temperature, with the aid of the temperature sensing device 51 and the temperature indicator 50 is sensed, and the outlet temperature determined with the aid of the temperature sensing device 48 and the temperature indicator 47 is sensed, determines the representative Output signals are transmitted via the instrument lines 52 and 49, respectively. It it should be noted that the pressure indicator 68 and the temperature indicator 50, 47 and 97 can also work blindly. That is, they can just be their concerned Transmit output signals and not at the same time the measurement on any control display to register.

Still other process output signals useful in explaining the operation of the Control system and thus the overall operation of the process Further improve, include, for example, that representative of the flow rate of the make-up hydrogen, which is introduced via line 21. This flow rate is measured by the flow determining device 82, which the corresponding signal communicated to the flow indicator 84 via line 83, and that indicator transmits in turn the output on line 85. The flow rate becomes similar that portion of the make-up hydrogen stream through line 22, which with the Reaction product outflow in line 12 is to be mixed with the aid of the flow determination device 87, line 88 and flow indicator 89 measured. The corresponding output signal, the is representative of this is to the computer comparator 95 via the instrument line 90 transmitted. One of the functions of the computer comparator 95 is that of quantity of the hydrogen coolant coming from line 2 via line 8 directly into the catalyst bed is diverted in the reactor 7 to determine. Its flow rate is determined by the flow meter 54, line 55 and flow indicator 56, and the latter transmits the corresponding process output signal via the instrument line 57.

The computer comparator 95 is internally programmed to is responsive to the various process output signals so generated and computer output signals generated that are used to make the required settings in the process to make and so adjust the molar ratio of hydrogen to hydrocarbon, that is required for the quality and quantity of the liquid product so over a long period of time maintain acceptable catalyst activity. The computer output signal communicated by means of the instrument line 36 is generated in a manner that is sufficient to adjust the temperature level in the reaction zone 7. Heat is supplied to the reaction zone 7 by introducing a suitable one combustible fuel in the directly fired heater 5.

The fuel, which is a liquid, a gas or a mixture of these can be is burned in the combustion zone, and the hot combustion gases go through the stove and eus the refinery chimney. The heat input to the reactant mixture is controlled by adjusting the rate of fuel flow to the heater 5, wherein the fuel is introduced via line 27 and combustion nozzle 29 will. Control of this flow is achieved through the flow control loop, the the flow sensing device 30, such as a turbine meter, the control valve 28, the Flow control device 32 and the flow signal line 31 comprises, and this transmits the flow signal from sensing device 30 to controller 34. The flow controller 32, which is equipped with an automatically adjustable setpoint, then transmits an appropriate adjustment signal to the control valve 28.

In addition to the flow control loop that is in the fuel delivery system of the directly fired heater 5 is provided, this is preferably in Cascade connection connected to a temperature recorder controller, which also has an automatic has an adjustable setpoint and senses the temperature of the reaction mixture, if it comes from the direct fired heater comes. It's a thermocouple 35 shown in the reactor inlet line 6, which sends a temperature signal to the temperature controller 34 transmitted. The controller 34 generates an output signal, which via line 33 to the flow controller 32 is transmitted to its automatically adjustable setpoint set or reset. The temperature control device 34, which also has an adjustable setpoint, takes the corresponding computer output signal via line 35. The computer comparator 95 thus provides the information relating to the reactor 7 associated temperature by resetting the setpoint of the temperature controller 34, which in turn sets the automatically adjustable setpoint of the flow regulator 32 resets.

In addition to the comparator output signals described above, provided in the computer program that the flow rate of the fresh charge, the flow rate of the hydrogen-rich recycled vapor phase, the Flow rate of the cooling stream introduced directly into the reaction zone and the amount of make-up hydrogen removed from the process through line 25 be regulated. The flow indicator 43 transmits a process output signal, representative of the feed flow rate, via the instrument line 44 to the computer comparator 95. This signal determines the necessary settings, in order to then achieve the best molar ratio of hydrogen to hydrocarbon, and a corresponding computer output is sent over the instrument line 46 transmitted to adjust the flow control valve 45 and thereby control the flow of Feed material through line 1 to either increase or decrease.

The flow rate of the recirculated gaseous is similar Phase mixed with the feed material in line 1 through the flow indicator 59 is sensed and a representative signal is generated and applied over line 62 transmitted to the computer comparator. This signal is related to the representative of the isolator pressure and by the pressure gauge 68 is sensed and used in common to feed a computer output signal into Line 86 to generate. These process output signals are also used by the computer comparator 95 are considered together and can simultaneously control the operation of the control valve 24 via the instrument line 81. A comparator output becomes also transmitted via the instrument line 58 to regulate the control valve 53, which in turn determines the amount of cooling stream that is introduced via line 8, to raise or lower. Regarding the amount of via line 22 in the control valve 25 introduced supplementary hydrogen are the main output signals, to which the computer comparator responds, those which it receives via the instrument cables 57, 66, 62, 85 and 90 are transmitted.

From the above discussion, those skilled in the art are familiar with the method according to which the present control system works, easy to understand. They are too numerous advantages of this procedure are easily recognizable. Among these advantages there is mainly the continuous sensing that is the catalyst stability improves and maintains catalyst activity by increasing the molar ratio from hydrogen to hydrocarbon in the reaction zone continuously at the optimum that is held in compliance with the desired product quality and product quantity stands. Known control systems that only have a compositional feature feel the separated product-containing liquid phase and only the sharpness of the Adjust reaction zone conditions (mainly the temperature) depending on must necessarily accept whatever with the catalyst activity and Catalyst stability happens. In contrast, the present control system represents the molar ratio of hydrogen to hydrocarbon such that the catalyst stability improves or increases the length of time that the catalyst is reasonably operating while maintaining the desired product quality. The present Invention recognizes the need for additional features of the feed material and its flow rate as well as the flow and the hydrogen content of the to sense different vapor phases in the overall process.

L e r s e i t e

Claims (15)

Claims 1. A method for regulating the molar ratio from hydrogen to hydrocarbon in the catalytic reaction zone of a continuous Hydrocarbon conversion process in which hydrogen is consumed and in which 1. a hydrocarbonaceous feed and hydrogen into a preheater with a feed device connected to it externally introduced, 2. the resulting heated mixture of feed material and hydrogen is reacted in the catalytic reaction zone, 3. the resulting The outlet stream of the reaction zone is condensed and separated and thereby a liquid Phase and a first hydrogen-containing vapor phase supplies, 4. at least a part the first vapor phase in admixture with the feed material to the preheater and 5. a second hydrogen-containing vapor phase from a source is introduced into this outside of the process and at least part of it mixed with the first hydrogen-containing vapor phase and with it in the preheating device is introduced, characterized in that a) the to the preheating device guided amount of heat by setting a first interacting with the preheating device Flow changing device regulates, b) the flow of the feed material through Setting a second flow changing device, sensing the flow rate of the feed material and production of one for a compositional characteristic regulates the same representative first process output signal, c) a sample introduces the feed material into a first analyzer and therein a second, process starting material representative of a compositional characteristic of this sample generates, d) the flow of the second hydrogen-containing vapor phase, which is in the process is introduced by setting a third flux changing device, sensing the flow rate of the second hydrogen-containing vapor phase and generation regulates a third process output signal representative of this vapor phase, e) a sample of the hydrogen-containing vapor phase going into the preheating device into a second analyzer and a fourth one for the hydrogen concentration this sample generates a representative process output signal, f) the flow rate senses the hydrogen-containing vapor phase passing through the preheater and generates a fifth process output signal representative of this vapor phase, g) the pressure of the separated hydrogen-containing vapor phase senses and a for this pressure representative sixth process output signal generated, h) a Introduces sample of the separated liquid phase into a third analyzer and therein a seventh, representative of a compositional characteristic of this sample Process output signal generated i) the seven process output signals into one Comparator or measure comparator transmitted and therein a first, second and third comparator output as functions of the seven process outputs and j) at least one of the three comparator output signals to at least one of the first, second and third flow changing means is transmitted and the amount of heat supplied to the preheater, the flow of the feed material and / or regulates the flow of the second hydrogen-containing vapor phase in this way and so is the molar ratio of hydrogen to hydrocarbon in the catalytic Reaction zone regulates. 2. The method according to claim 1, characterized in that the hydrocarbon conversion process is a hydrocracking process and the first analyzer is a process output which is representative of the molecular weight of the feed. 3. Control system for carrying out the method according to claim 1 and 2, characterized by a) a cooperating with the preheating device, the first flow changing device adjusting the amount of heat supplied to the preheating device, b) a first, the rate of flow of the feed material to the reaction zone measuring and a first process output signal representative of this flow rate first flow sensing device generating the flow rate of the feed material adjusting second flux changing means, c) a first analyzer which holds a sample of the feedstock and one for a compositional characteristic this Sample generates a representative second process output signal, d) a second flow sensing device, the flow rate of the second, introduced into the process, containing hydrogen Measures vapor phase and a third process output signal representative of this flow rate generated, and a third adjusting the flow rate of this second vapor phase Flow changing device, e) a second analyzer, which takes a sample of the in the preheating introduced hydrogen-containing vapor phase receives and a fourth process output signal representative of their hydrogen concentration generated, f) a third sensing device, the the flow rate of the in the Hydrogen-containing preheating device introduced in a mixture with the charge material Measures vapor phase and a fifth method representative of this flow rate output signal generated, g) a pressure of the separated first hydrogen-containing Vapor phase sensing and a sixth process output signal representative of this pressure generating device and h) a comparator or measure comparator, the (i) the receives six process outputs; and (ii) as a function of those process outputs generates first, second and third comparator output signals, the comparator via signal-transmitting devices, the at least one of the comparator output signals communicated to at least one of the flow changing devices, in connection with of the first, second and third flux changing means, whereby the flux of the feed material, the amount of heat supplied to the preheating device and / or the flow of the second hydrogen-containing vapor phase introduced into the process set as a function of these comparator output signals and so the molar ratio is regulated from hydrogen to hydrocarbon. 4. Control system according to claim 3, characterized by a fourth Flow sensing device that controls the flow rate of a third hydrogen-containing Measures vapor phase which is introduced directly into the catalytic reaction zone, a seventh process output signal representative of this flow rate generated and transmitted to the comparator and with a fourth flux changing device cooperates, and a comparator which, in addition to the first, second and third comparator output signals a fourth comparator output as functions of the seven process outputs generated. 5. Control system according to claim 3 and 4, characterized in that at least one of the four comparator output signals to at least one of the four Flow changing devices is transmitted, whereby the flow of the feed material, the amount of heat supplied to the preheater, the flow of the second hydrogen-containing Vapor phase to the process and / or the flow of the third hydrogen-containing vapor phase, which is introduced directly into the catalytic reaction zone, depending on these comparator output signals is set. 6. Control system according to claim 3 to 5, characterized by a third analyzer that takes a sample of the separated liquid phase and an eighth process output signal representative of this sample and a comparator which receives this eighth process output and, as functions of the eight process output signals, four comparator output signals generated. 7. Control system according to claim 3 to 6, characterized in that that the first and third analyzers generate stabilized cool flame generators include with servo-controlled flame fronts. 8. Control system according to claim 3 to 7, characterized in that that the first temperature sensing means has a first temperature in the reaction zone senses, a ninth process output signal representative of that temperature and this ninth process output signal is transmitted to the comparator. 9. Control system according to claim 3 to 8, characterized in that the comparator provides an output signal as a function of the first reaction zone temperature and the compositional characteristic of the separated liquid phase and this Output signal transmitted to the first flow changing device and on this Way depending on this output signal the preheater supplied Adjusts the amount of heat. 10. Control system according to claim 3 to 9, characterized in that that the second temperature sensing means has a second temperature in the reaction zone senses a tenth process output signal representative of this temperature generated and transmitted to the comparator. 11. Control system according to claim 3 to 10, characterized in that that the comparator provides a comparator output as a function of the first and second Reaction zone temperature and the compositional characteristic of the separated liquid Phase generated and this comparator output to the first flux changing means transmitted and in this way, depending on this output signal, the Adjusts the amount of heat supplied to the preheater. 12. Control system according to claim 3 to 11, characterized in that that the first temperature sensing means has a first temperature in the outlet section in the reaction zone, the second temperature sensing device a second Temperature in the inlet section of the reaction zone senses the ninth generated and the tenth output signal are transmitted to the comparator and the comparator as a function of the difference between the first and second temperatures and the Composition feature of the separated liquid phase is a comparator output signal and the comparator output to the first flux changing means transmitted. 13. Control system according to claim 3 to 12, characterized in that that the first flow changing device is a flow control loop with a flow regulator with adjustable setpoint that regulates the heat supply to the preheater, comprises, wherein the setpoint is adjusted as a function of the comparator output signal will. 14. Control system according to claim 3 to 13, characterized by a Temperature control device with an adjustable setpoint, the one for the heated Mixture of feed material and hydrogen from the preheater a representative controller output signal is generated and transmitted to the flow controller, the setpoint of the same adjusted as a function of this output signal and the comparator output signal is transmitted to the temperature control device is, whereby its setpoint is adjusted depending on this output signal will. 15. Control system according to claim 3 to 14, characterized in that that the comparator has a fifth comparator output signal as a function of the sixth Process output signal generated and the fifth comparator output signal to the fifth flow changing device transmitted, which with the first hydrogen-containing Vapor phase interacts, as a result of which part of the same is withdrawn from the process will.