the further description of this invention is presented with reference to the schematic drawings , fig1 and 2 . the drawings are not intended as an undue limitation on the generally broad scope of the invention as set out in the claims . only those compressors , heaters , heat exchangers , and coolers are shown that are useful in the description of the process . the depiction of other miscellaneous hardware such as pumps , instrumentation and controls , and valves has been omitted as not essential to a clear understanding of the process , the use of such hardware being well within the purview of one skilled in the art . in fig1 a charge stock stream enters the processing unit through pipeline 1 and is mixed with circulating gas flowing in pipeline 2 by means of mixing pipeline section 3 to form a reactor feed stream in pipeline 20 . the rate of charge stock addition is controlled at a particular preset value by flow controller 4 and flow control valve 41 . the circulating gas stream flowing in pipeline 2 consists mainly of hydrogen but includes hydrocarbon vapors . the reactor feed stream flows through pipeline 20 to regenerative heat exchanger 5 , where it is heated , and then through pipeline 6 to heater 7 . the feed stream is heated further in heater 7 and then flows through pipeline 9 to reactor 8 , where the desired reactions take place . the effluent stream produced in reactor 8 flows through pipeline 10 to regenerative heat exchanger 5 where it is cooled by giving up its heat to the reactor feed stream . from regenerative heat exchanger 5 , the product stream flows through pipeline 11 to cooler 12 where it is further cooled by means of a cooling medium which is water or ambient air . as a result of this cooling , liquid hydrocarbons are condensed . the effluent stream flows from cooler 12 through pipeline 13 to gas - liquid separator 14 where it separates into two streams -- a liquid product stream which flows out of the hydrocrabon processing unit through pipeline 15 and a hydrogen and hydrocarbon vapor stream , a portion of which flows through pipeline 16 to compressor 19 . pipeline 17 is connected to pipeline 16 and is used to supply hydrogen to the hydrocarbon processing unit from a source outside of the unit . pressure controller 18 and pressure control valve 42 regulate the addition of hydrogen so that a constant preset pressure will be maintained at the suction of compressor 19 . as hydrogen is consumed in the reactor , the pressure decreases , causing the valve to open to allow hydrogen to flow into the hydrocarbon processing unit . flow indicator 21 provides a measurement of gas flow at the outlet of compressor 19 ; however , it is accurate only at one particular set of operating conditions , as explained earlier . hydrogen and hydrocarbon vapor flow out of the hydrocarbon processing unit through pipeline 38 . the flow is controlled by flow control valve 37 and flow controller 34 to a value set by the plant operator . the vent flow is made necessary by the presence of light hydrocarbons in the circulating gas stream . some light hydrocarbons enter the system through pipeline 17 as part of the hydrogen feed stream , which is not pure hydrogen , and some are produced in side reactions taking place in reactor 8 . while some of the light hydrocarbons leave the system dissolved in the liquid product stream , there is usually an increase in concentration over time unless a vent stream is employed . thus the purpose of the vent stream is to remove light hydrocarbons from the process , as they would interfere with the desired reactions . the principle is similar to that of cooling tower blow - down , where a continuous stream of water is withdrawn to keep water hardness at an acceptably low level . the vent stream usually contains 60 mole percent or more of hydrogen . fig1 shows the instrumentation necessary to practice an embodiment of the invention . hydrogen concentration can be expressed as partial pressure of hydrogen . the partial pressure of hydrogen in the effluent stream in pipeline 10 is measured by a partial pressure sensor 22 such as that disclosed by h . a . hulsberg in u . s . pat . nos . 2 , 671 , 336 and 2 , 671 , 337 . pressure transmitter 23 , of conventional design , is used in conjunction with the partial pressure sensor 22 and provides a signal to a conventional automatic controller 24 which adjusts compressor capacity to maintain a preset value of hydrogen partial pressure . compressor capacity is changed by adjusting inlet guide vanes or adjusting the speed of the compressor . thus only the amount of hydrogen is circulated that is required to meet the minimum necessary to protect the catalyst and / or maintain the yield structure . by means of reducing the hydrogen flow , the power needed by the compressor driving means is reduced and the quantity of fuel burned to provide heat at heater 7 is reduced . each of the equipment items shown in fig1 and 2 may consist of several individual pieces of equipment . for example reactor 8 may consist of a single vessel or may consist of several reaction vessels with provisions to reheat the process stream between vessels . also , equipment may be added to this basic flow scheme . for example , the circulating gas stream may be passed through equipment designed to remove hydrogen sulfide . these variations and additions to the basic simple schematic are well known to those skilled in the art of hydrocarbon processing . fig2 differs from fig1 in that , since it depicts a hydrogen - producing process , the hydrogen feed stream and vent stream are replaced by a single hydrogen removal stream and a different embodiment of the invention is depicted . hydrogen produced in the reactor is removed by removing a portion of the hydrogen and hydrocarbon vapor stream flowing from gas - liquid separator 14 by means of pipeline 43 . pressure controller 45 and pressure control valve 44 regulate the removal of gas so that a constant preset pressure will be maintained at the suction of compressor 19 . as hydrogen and hydrocarbon vapors are generated , the pressure increases , causing the valve to open to allow gas to flow out of the hydrocarbon processing unit . in the embodiment of the invention depicted in fig2 the pressure in pipeline 9 is sensed by a conventional pressure transmitter 25 . the mole fraction of hydrogen in pipeline 9 is sensed by concentration transmitter 26 , which may be a conventional thermal conductivity analyzer such as the 7c series sold by beckman instruments , inc . the product of pressure times mole fraction , which is partial pressure , is obtained in multiplying relay 27 . automatic controller 28 adjusts the capacity of compressor 19 to maintain a preset value of partial pressure . as in fig1 the concentration of hydrogen is set at the minimum value , thus accomplishing conservation of utilities . in fig1 the sensing point for hydrogen concentration is downstream of the reactor 8 , at pipeline 10 , rather than upstream of the reactor as shown in fig2 . since the reaction of fig1 consumes hydrogen , the hydrogen concentration will decrease from the inlet to the outlet of the reactor means . the point of lowest hydrogen concentration will be at the outlet of the reactor means , i . e ., in the reactor effluent stream . in contrast , in a hydrogen - producing process such as that of fig2 the point of lowest hydrogen concentration will be at the entrance to the reactor means . the hydrogen concentration should be measured at the point where it is expected to be lowest in order to achieve the goal of maintaining as low as possible a concentration in order to conserve utilities while still protecting the catalyst and / or yield structure . in some cases , it may be desirable to vary the location of the hydrogen concentration sensor while keeping it downstream of the reactor means . the sensor can be located in pipeline 10 on pipeline 11 . the reason for changing sensor location would normally be to expose it to less severe conditions . the considerations involved in choice of sensor location are familiar to those skilled in the art . for example , it must not be placed in pipeline 11 if liquid drops condense out in heat exchanger 5 . the method of measuring hydrogen content is totally independent of sensing location . for example , a partial pressure sensor as disclosed in the hulsberg patents and an associated pressure transmitter can be used in place of pressure transmitter 25 and concentration transmitter 26 in fig2 . the functions performed by the automatic controllers and arithmetic relays shown in fig1 and 2 can be accomplished by a digital computer which would receive process measurements and provide control signals in place of the automatic controllers and arithmetic relays . the method of practicing the invention is not changed by substitution of a digital computer for the automatic controllers and arithmetic relays and the depiction of controllers and relays in the figures can be taken as showing computer functions . with use of a digital computer , different control algorithms are possible which might prove more efficient under certain circumstances . control by a digital computer or microprocessor - based control units are included within the scope of this invention . it is important to note that partial pressure is the parameter most relevant to protection of catalyst and yield structure . the invention can be practiced using any convenient method of measuring hydrogen concentration . however , for maximum precision , concentration of hydrogen should be expressed in terms of partial pressure . in the context of this invention , partial pressure is considered to be a form of expression of concentration . often , the concentration of hydrogen can be measured by any convenient means without any loss of precision , since system pressure is relatively constant . but mole fraction , volume percent , and the like , do not completely correlate with improvement of catalyst activity and stability and yield . pressure must be taken into account . if the amount of hydrogen in the circulating gas stream is held constant and the pressure is increased , the partial pressure of hydrogen increases . catalyst activity and stability and yield will be improved by the pressure increase , though percent hydrogen has not changed . the following example will illustrate the utility savings which are available from the practice of the instant invention . the following table presents certain operating parameters for a hydrogen recycle process , more specifically a catalytic reforming unit processing 10 , 000 barrels per day of naphtha charge stock . ______________________________________ case a case b case c______________________________________separator temperature , ° f . 100 80 80orifice dp , inches water 42 42 36circulating gas , lb - mol / hr 5 , 271 5 , 623 5 , 215circulating gas , mol . % 86 . 9 87 . 8 87 . 8hydrogencirculating hydrogen , lb - mol / hr 4 , 579 4 , 936 4 , 579circulating gas , mol . wt . 6 . 82 6 . 18 6 . 18circulating gas , lb / hr 35 , 940 34 , 570 32 , 207heating load , 10 . sup . 6 btu / hr base + 0 . 211 - 0 . 349compression load , hp base + 116 - 38______________________________________ case a shows parameters when the unit shown in fig2 is operating with the design maximum cooling medium temperature , at which the gas - liquid separator 14 operating temperature will be 1oo ° f . orifice dp is the measured pressure drop across the orifice plate at flow indicator 21 and is the value which is converted into flow rate by means of the flow indicator scale . the circulating gas and circulating hydrogen parameters are all taken at pipeline 2 . the heating load refers to heat which is supplied to heater 7 . compression load refers to the power required to drive compressor 19 . case b shows the parameters when the cooling medium temperature is such that gas - liquid separator 14 is operating at 80 ° f . and the invention is not practiced . orifice pressure drop is maintained at the same value as case a by an operator or automatic controller . the amount of hydrogen in the circulating gas stream is increased from case a . the heating load and compression load is increased from case a . case c shows the same parameters when the cooling medium temperature is the same temperature as case b but where the invention is practiced . the heat decrease over case b is 560 , 000 btu / hr ; allowing for firing inefficiencies , this results in fuel savings of approximately 700 , 000 btu / hr . the power savings over case b is 154 horsepower . on a yearly basis , at realistic 1981 rates of $ 5 . 00 per million btu &# 39 ; s , and $ 350 . 00 per horsepower - year , and assuming 11 months operation at conditions which average out to case c conditions , practice of this invention results in a cost savings of approximately $ 77 , 500 . 00 in this relatively small reforming unit . reforming units of six times the capacity of this unit have been built .