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US2690056A - Hydrocarbon conversion process and apparatus - Google Patents

Hydrocarbon conversion process and apparatus Download PDF

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Publication number
US2690056A
US2690056A US148669A US14866950A US2690056A US 2690056 A US2690056 A US 2690056A US 148669 A US148669 A US 148669A US 14866950 A US14866950 A US 14866950A US 2690056 A US2690056 A US 2690056A
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United States
Prior art keywords
contact material
conduit
cooler
catalyst
heat
Prior art date
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Expired - Lifetime
Application number
US148669A
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English (en)
Inventor
Eric V Bergstrom
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ExxonMobil Oil Corp
Original Assignee
Socony Vacuum Oil Co Inc
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Filing date
Publication date
Priority to BE501734D priority Critical patent/BE501734A/xx
Application filed by Socony Vacuum Oil Co Inc filed Critical Socony Vacuum Oil Co Inc
Priority to US148669A priority patent/US2690056A/en
Priority to DES22299A priority patent/DE900333C/de
Application granted granted Critical
Publication of US2690056A publication Critical patent/US2690056A/en
Anticipated expiration legal-status Critical
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/087—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/082—Controlling processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00088—Flow rate measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling

Definitions

  • This application is directed to a process: and apparatus for converting hydrocarbons in, the presence of a particle-form solid contact mass. It has particular relation to a method and appa-- ratus for adjusting the temperature of hot granular contact material in continuous movingy bed:V conversion systems.
  • the solid contact material ist continuous-1y passed through a conversion zone: as a substantially compact moving column of particle-form material. Hydrocarbons are admitted tothe conI version zone and converted' products: removed.
  • the particle-forrny material is continuously withdrawn from the zone., contaminated. with..carbo naceous material.
  • the contaminated material' is then passed downwardly as a substantially compact column through a burning zone' whereink the carbonaceous material is b-urned from the con-l tact material, restoring the contact material substantially to its original state.
  • burning zone was: controlled partly by the number of cooling coils in service in the following cooling zone.
  • the cooling in the cooling Zone was provided, generally, by one or more levels of horizontal, spaced tubes. Water was circulated through the number of tubes necessary to give the required cooling. Thus the effective heat transfer surface was varied by the number of tubes through which cooling Water was circulated.
  • the reactor conditions vary frequently, Which, in turn, causes variations in the amount of heat generated in the kiln and, therefore, the amount of heat which must be removed in the cooling zones. This requires cutting Water iiow in and out of some of the tubes.
  • a tube which does not have water flowing through it may be at a temperature of about 1l00 F., for example, While the water used forcooling may be only 200 to 400Q F., severe stresses are set up in the tubes each time water is cut in or out. This caused ⁇ frequent fail-ure of the tubes, particularly at the location where they are sealed into the header.
  • the catalyst flow rate is increased substantially, approximately 2 or 3 times the old rate. Consequently, the carbon lay down on the catalyst during reaction is reduced because the catalyst is retained in the reactor a shorter period.
  • the temperature .reached in the regenerator therefore, is maintained below the heat damaging level because there is a smaller per cent of carbon to be burned therein.
  • the catalyst enters the kiln at approxi.- mately 850 F. and is withdrawn at approximately 1200 F., below the heat damaging temperature limit. No heat transfer tubes are needed in the kiln, permitting the kiln design to be eX- ceedingly simple and easy to service.
  • a catalyst cooler of some sort must be included in the system, usually located subsequent to the kiln.
  • Prior art catalyst or pebble coolers are not found satisfactory for a variety of reasons. inasmuch as more or less heat must be extracted from the catalyst from time to time, some means of control of the cooler characteristics is required. For example, many coolers allow the coolant to flow through exchanger tubes, being equipped with controls for preventing the flow of coolant through selected tubes. The empty tubes assume the temperature of the moving Contact material. Consequently, when they are put back in service, the cold coolant uid contacts the hot walls of the tube, causing the metal to spall and crack. This necessitates frequent cooler repair and replacement. Many of the prior coolers are disfavored because of their complexity, excessive cost or difhculty of control. Because of their tendency to develop leaks, the use of cooling iiuids under pressure was largely precluded in the prior art coolers.
  • Moving bed catalyst systems of hydrocarbon conversion are effectively replacing xed bed systems of operation. They have proved to be economical in the larger units of a size about 10,000 to 15,000 barrels per day.
  • the kiln is divided into a series of stages with burning stages f day of charging stock, the cost of the kiln was found not to reduce in proportion to reduction in cost of the remaining equipment.
  • the unit has been found to provide an economically feasible moving bed system for the small refiner.
  • a catalyst or pebble cooler in which is located a heat exchanger, adapted to place particle-form contact material in indirect heat exchange relationship with a cooling fluid.
  • the heat exchanger is maintained flooded with coolant fluid throughout the entire contact surface area.
  • Molten salts such as potassium nitrate or nitrite may be used as the coolant fluid, as well as molten metals but liquid water, maintained under pressure, is preferred..
  • water pressures 300-350 pounds per square inch may be used, with the temperature being maintained Constant at the boiling temperature by maintaining the water pressure at a fixed value.
  • the terrperature of the contact material is controlled by varying the volume of the contact material brought into contact with the cooling surface.
  • the object of this invention is to provide a simple method of cooling and adjusting the temperature of hot granular contact material.
  • a further object of this invention is to provide a simple cooler for cooling and adg'usting the temperature of hot, particle-form contact material.
  • Another object of this invention is to provide an improved hydrocarbon conversion process.
  • Another object of this invention is to provide an improved process for the catalytic cra-cking of hydrocarbons.
  • Figure 1 is a diagrammatic showing of the relationship of the several elements making up a plant for the conversion of hydrocarbons to ethylene.
  • Figure 2 is a detail view in section of the reactor outlet port of Figure l and the cooler located therebelow.
  • Figure 3 is a plant for conducting hydrocarbon conversion in accordance with adiabatic TCC principles.
  • Figure 4 is a view, partially in section, of the cooler used in the plant of Figure 3.
  • Figure 5 is a vertical section showing a variant form of cooler design.
  • Figure 6 is a vertical section showing a further embodiment of the invention.
  • Figure 'l is a plan View of the iris valve shown on plane 7 7 of Figure 6.
  • a hot granular solid is heated to a suitable high temperature in heater i0 and transferred by feed leg I l through a steam sealing zone i2 to a reactor
  • a charge for the reaction is introduced by a plurality of inlet tubes l0 depending from ring manifolds l5 at the top of the reactor.
  • the charge is passed in direct ccntact with the highly heated granular solids a' d is thus rapidly converted to a vapor phase mixture having the temperature desired for the reaction.
  • the reaction mixture Upon leaving the contact bed, the reaction mixture is quenched by the injection of water supplied from inlet l0 and is passed by conduit I'I to a quencher I8 wherein it is passed through a moving bed of relatively cool granular solids for further reduction in temperature.
  • the quenched reaction mixture is transferred by line i9 to a spray condenser 20 from which product vapors are taken overhead by line iii to a suitable gas plant for purification and recovery of the gaseous products of the reaction.
  • Oil and water from the bottom of condenser 20 are passed to a settler 22 wherein they separate into an upper oil layer which is cooled in heat exchanger 23 before transfer to processing or storage and a lower water layer which is cooled in heat exchanger 24 to be recycled in part to the spray condenser by line 25.
  • water from the bottom of settler 22 may be used in the charge, since contamination of the charge water has no detrimental eect in such operations, the contaminants accepte bein-'gr either.' vaporized: with. the:A waterv or de'- posited on the granular solidf from: whichv 'they may be removed byfbunningI inthe heater.
  • a purge gas su'ch assteam ⁇ is admitted to theV bottom of the reactor at inlet 26 and afpressuring medium, whichY may alson be steam; is admitted at inlet 27: to' be used: to provide a pressure seal in the insulation of" theve'ss'et for preventingv deposition of carbonaceous substances in the reac'tor insulation.
  • the granular solids are withdrawn fromthebottom. et reactor. I3L by pipe- 28.
  • fuel from inlet 3'4 isburned in preheated air supplied at to generatel a flame in direct contact with the solid granules andy thus.v heat the latter to the desired degree.
  • Elue gasesv are withdrawn at 35 and passed. to anJ economizer. or stack.
  • the quencher is an element of a similar cycle of granular solids-and-Whereinthe granules serve to cool vaporous reaction mixture from reactor I3 and are then purged by steam admitted at 31 and passed by pipe38 through the cooler 39 and depressuring pot 40 to' an elevator 4I. From the top of the elevator 4l the solids are discharged by pipe 42' through a classifier 43 to a hopper 44. Solids are supplied through feed leg 45 to an air preheater 46 wherein they are contacted with air from blower 41 to preheat the same. The preheated air is then transferred by line 48 to inlet 3.5 of heater I0.
  • the outlet of the reactor projects through the topof the cooler 29; Within the coolertheoutlet conduit of the reactor is surrounded by an axially laligned conduit 5l which is adapted to be ⁇ raised or loweredV with respect to the' outlet conduit.
  • the exterior portion of the conduit possesses a rack gear E2 adapted to mate with the pinion gear 53 providing a telescoping motion for the aligned' conduits.
  • the pinion gear isdriven by a suitable prime mover, such ⁇ as; an electric: motor, not shown.
  • Ther cooling' fluid.l is introduced through the conduit 6B froma source not shown and removed through thefc'onduit 61.
  • the amount of. heat to be' extractedr from the granular material'variesfw-ithLa number of factors such as; for example;l the' amount and type of reactants fed to the bed ofv granular material in the reactor ⁇ I3.. It is obviously desirable to extract. only suflicient head from the granular material tof prevent ⁇ damaging the elevator and its related' parts rornthe excessive temperature of the. contact-'material
  • 53theslidingconduit-l may be raised or lowered. to'cause the' pile li'to spread out over a larger or Asmaller areay of the tube sheet 5ft. The pile willonly nowy untilzthe angle of repose of.
  • the contact materialA iss reached, making the area of the tube sheet coveredl dependent' upon the height of. the'bottom of therconduit 5i above the upper tube.y sheet.' 54.. As less area of the tube sheet is covered, fewer of the vertical tubes 56. will beA used ⁇ for transferring the granular materialt through the. heat exchanger. inasmuch as the temperature of.y the coolant fluid. is maintained: 'constant by the. thermsyphon principle ci operation, less'heatwill be extracted from the granular material when fewer tubesv are used for thetra-nsfer of the contact material because less volume of the contact material is brought into Contact with the cooling. surface.
  • FIG. 3 a system is shown for carryingout adiabaticregeneration in a TCC process
  • a downwardly moving column of catalyst particles in the reactor 710 is contacted with the hydrocarbon charge admitted through the conduit 'it from a stock. preparation zone, not shown-
  • TheV products produced by the catalytic conversion of the hydrocarbon charge are removed through the conduit 12 to other apparatus, nots'hown, for further treatment.
  • the fouled contact material is removed from the bottom of the reactor lilA through the conduit 73 to the' regenerator'll
  • the flow of. contact material in the condmitl 7:3 ⁇ is controlledA by the valve 15.
  • Air is admitted tothe regenera-tor T4 through the conduit-'ld-.toburn off theca-rbona'cecus'material from the' surface of thev contact material moving through the vessel as a descending substantially solid column.
  • the flue gasformedzinth'e regenen ator is removed through the conduit ll.
  • the-'catalyst llow rate is suiciently rapid to prevent the contact material being overheatedl in the: regenerator.
  • the material enters the regenerator'at a temperature of about 856 F. and' is removed'. therefrom at a temperature 4ot about 1200" I'nthis system no heat exchanger tubes are required' in the regenerator.
  • the regeneration gas ilow may be limited to a value slightly in excess of that required for complete combustion of the coke.
  • the flow of air to the regenerator may be limited to a rate of flow Which is about 20 per cent in excess of that required for chemically correct combustion of the coke deposits present on the catalyst.
  • the contact material removed from the regenerator 'l0 is passed through the conduit 18 into a cooler 88 disclosed in more detail on Figure 4.
  • the cooled catalyst is discharged from the cooler Sti, is passed through the conduit 8l and lifted by the gas lift 82.
  • the valve 83 in the conduit i3! is used to control the discharge of catalyst from the cooler.
  • Lift gas is introduced near the bottom of the lift through the conduit 84 and the catalyst is lifted by the lift gas and raised to the top of the lift.
  • the lift gas may be inert gas, steam, iiue gas or air.
  • the catalyst is separated from the gas in the disengaging chamber 85, and delivered through the conduit 86 to the hopper 8l'.
  • the lift gas is discharged from the disengaging chamber through the conduit 88.
  • the catalyst flows from the hopper 87 through the connecting feed leg 89 into the reactor l0, thereby completing the continuous catalyst flow path.
  • Various seals are used to prevent the transfer of gases from one vessel to another; inert gases are used to purge catalyst moved from one vessel to another.
  • Sufficient heat is extracted from the catalyst withdrawn from the regenerator in the cooler to leave enough sensible heat and potential hydration heat in the catalyst to supply the total heat required in the reactor. This may be only reaction heat or it may be reaction heat plus sensible and latent heat to get the reactants into Vapor phase at the desired reaction temperature.
  • the reactor can be operated with concurrent or countercurrent flow of reactants and catalyst mass, and the reactants may be charged in liquid form, vapor form, or a mixture of both liquid and vapor.
  • the continuous system may be operated at a catalyst to oil ratio of about l-20 pounds of catalyst per pound of oil, and at space velocities of about 0.5-10 volumes of oil (measured at 60 F.) per hour per volume of contact material column within the conversion zone.
  • the conditions will vary somewhat with catalyst material, catalyst activity, type of feed stock, etc. In such processes it is found desirable to limit the particle size broadly within the range of about 3 to 100 mesh and preferably Within the range of about 4 to 20 mesh Tyler Standard Screen analysis. The percentage of fines present in the contact material mass should be maintained as low as possible.
  • FIG 4 an enlarged vieuv of the cooler of Figure 3 is shown, partially in section.
  • the catalyst introduced into the cooler S8 forms a pile below the conduit 78.
  • the short conduit 19 below the conduit 78 is somewhat larger in cross-section than the conduit "i3 and is adapted to be raised or lowered by; the lever G5 pivoted in the bearing 96.
  • the conduit "i9 is operated by the wheel 6'! which operates the mating gears 68, 69.
  • the shaft Eil maintains the conduit 'i9 in substantial alignment with the conduit 78.
  • a series of cooling conduits or tube bundle is located in the cooler 90, with or without deecting ams. The bundle is arranged to provide paths for the catalyst which bring the catalyst in contact with the cooling surface during its downward travel.
  • the cooled catalyst is discharged from the bottom of the cooler through the conduit 8 i, the flow being controlled. by the valve 83.
  • the tube bundle 90 is supplied with a suitable coolant from a source, not shown, through the conduit 9
  • FIG. 5 another embodiment of the invention is shown.
  • Downwardly moving contact material is introduced through the conduit into the top of the cooler 99.
  • the contact material is received in the enclosed chamber 98 and discharged from the bottom of the chamber 96 through a multiplicity of conduits Sl adapted to distribute the contact material evenly across the cross-sectional area of 'the cooler.
  • Valves 98 are located in the conduits il? for controlling the flow of contact material through the conduits. By closing the Valves in the outer conduits the pile of contact material below the valves may be made to cover a smaller area of the cross-section of the cooler.
  • In the lower section of the cooler are located upper and lower tube sheets 99,
  • ' temperature of the vcoolant may be-'maintained substantially constant by suitable control vof the valves Ulli, located in the conduits
  • T-his ⁇ may suitably be done by a controller m5 connected to a temperature 'indicator Il, and adapted to automatically control the valves iM,
  • l The cooled contact material is discharged from the cooler 96 through the conduit
  • the valves 98 v may be controlled by a central controller
  • FIG. 6 is shown still .another embodiment of this invention.
  • the conduit . adapted to introducey contact material onto the shelfor fioor H2.
  • the shelf or floor H2 has an Yorifice in .its lcenter adapted to pass contact material therethrough onto the top of an iris diaphragm lle.
  • tube sheets and transfer tubes similar to those previously described, adapted topermit the transfer of contact material downwardly through the tubes in contact with a cooling fluid.
  • the iris diaphragm may be opened or closed to cause the pile of contact material on the upper tube sheet to cover a large or smaller area of the tube sheet, thereby controlling the number of transfer tubes through which the contact material is passed.
  • the iris diaphragm H3 is driven by the motor Ild through the speed reducer H5.
  • the motor l I4 can be controlled by a controller I6 adapted to maintain the temperature of the contact material in the outlet conduit substantially constant.
  • the iris diaphragm serves only as a baiiie and is not a throttling device. The diaphragm completely closed will permit the transfer of suflicient contact material to meet the needs of the system.
  • Figure '7 shows a plan View of the iris diaphragm of Figure 6 as seen on plane '1 1 of Figure 6.
  • the leaves l IB of the diaphragm are attached by the members
  • is fastened to a second frame by the cap screws
  • 24 is attached to the ring l2! by the bar
  • 24 eifected by rotation of a mating pinion gear not shown, causes the ring
  • 8 causes the central opening to increase or decrease, depending upon the direction of rotation of the leaves
  • This application shows broadly a method and apparatus for cooling granular contact material which is related, in some of its broader aspects, to the copending application Serial Number 154,130, filed April 15, 1950.
  • a cooler for comminuted solid contact ma-y terial comprising an enclosed vessel, a downwardly directed feeding conduit projected into the top of said vessel and terminating near the top thereof, a short conduit telescoping the end of said conduit adapted for movement in an axial direction, said short conduit having an axially aligned rack gear located on its outer surface, a pinion gear disposed adjacent said short conduit and adapted to engage and drive said rack gear, means for driving said pinion 10 gear, ⁇ cooling means defining a multiplicity of downwardly directed paths disposed in.
  • a cooler for granular contact material in which ⁇ a ⁇ heat exchanger is located in the bottom portion thereof arranged to provide a mulvtiplioityrof downwardly'directed paths substantially equally distributed *acrossv the cross-section of the cooler,the method of operation which comprises: the steps of maintaining the heat exchanger flooded with cooling fluid, introducing the .contact material into the cooler at a location near Athe top thereof, gravitating the contact material through a depending conduit termi- -nated at a location above the heat exchanger,
  • the method of changing the temperature of a particle-form solid contact material which comprises: passing the contact material through a conned heat exchange zone to contact a heat transfer surface along at least a portion of one side thereof, subjecting substantially the entire area of the opposite side of said heat transfer surface to the inliuence of a iiuid heat exchange medium existing at a temperature substantially different from that of said contact material and maintained out of communication with the contact material, discharging the contact material from said heat exchange zone and selectively controlling the temperature of the contact material discharged at the desired level by adjustably controlling the volume of contact material within said Zone which is at any instant under the influence of said heat transfer surface.
  • a cooler for comminuted solid contact material comprising an enclosed, vessel, cooling means dening a multiplicity of downwardly extending paths disposed in the lower section of said Vessel through which contact material may be lowered as substantially compact columns, means for introducing cooling fluid into the cooling means, means for withdrawing cooling fluid from the cooling means, said cooling means adapted to bring the cooling fluid into indirect heat exchange relationship with the contact material throughout the entire length of the paths, means defining an inlet in the upper portion of the vessel for the introduction of contact material, baffling means operatively connected to said inlet means for controlling the area of the top of said cooling means covered by said contact material, means for adjusting the baflling means,
  • a cooler for comminuted solid contact material adapted for gravitation therethrough of a compact column of hot contact material comprising: an enclosed vessel, cooling means defining at least one downwardly extending path for ow of solid contact material within said vessel, means for introducing coolant uid into the cooling means, means for withdrawing coolant fluid from the cooling means, said cooling means adapted to provide a predetermined surface area for contact with the column of contact material Which is in flooded contact With cooling fluid at all times and which places the contact material in indirect heat exchange relationship with the cooling fluid, means defining an inlet for the introduction of contact material into the upper portion of the vessel, baiing means operatively connected With said inlet, adapted to direct the column of the contact material into contact with at least a portion of the cooling means, means for adjusting the baling means, to vary the amount of cooling surface contacted with contact material and means dening an outlet in the bottom of said vessel through which the Contact column may be withdrawn.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
US148669A 1950-03-09 1950-03-09 Hydrocarbon conversion process and apparatus Expired - Lifetime US2690056A (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
BE501734D BE501734A (de) 1950-03-09
US148669A US2690056A (en) 1950-03-09 1950-03-09 Hydrocarbon conversion process and apparatus
DES22299A DE900333C (de) 1950-03-09 1951-03-09 Verfahren und Vorrichtung zum Kuehlen von koernigen Kontaktstoffen, insbesondere von koernigen Katalysatoren bei der Umwandlung von Kohlenwasserstoffen

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US148669A US2690056A (en) 1950-03-09 1950-03-09 Hydrocarbon conversion process and apparatus

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2819951A (en) * 1955-02-23 1958-01-14 Shell Dev Apparatus for the regeneration of catalyst
US2897139A (en) * 1955-01-14 1959-07-28 Socony Mobil Oil Co Inc Temperature control in a moving bed system employed for hydrocarbon conversion
US2943922A (en) * 1953-04-01 1960-07-05 Hydrocarbon Research Inc Solids cooling means and riser conduit
US2971746A (en) * 1957-08-27 1961-02-14 Foster Wheeler Corp Pressure safety assembly for heat exchangers
US3267024A (en) * 1954-02-12 1966-08-16 Union Oil Co Hydrocarbon conversion process

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1052035B (de) * 1955-01-14 1959-03-05 Socony Mobil Oil Co Inc Verfahren und Vorrichtung zum Einstellen der Temperatur eines sich kontinuierlich bewegenden Kontaktbettes von aus festen Teilchen bestehendem Material bei der Kohlenwasserstoffumwandlung
DE102004041375A1 (de) * 2004-03-24 2005-10-13 Coperion Waeschle Gmbh & Co. Kg Vorrichtung zum Temperieren von Schüttgut
DE102005031660A1 (de) * 2005-07-05 2007-01-11 Coperion Waeschle Gmbh & Co. Kg Schüttgut-Temperier-Anlage
DE202007015617U1 (de) * 2007-11-09 2009-03-26 Coperion Gmbh Vorrichtung zum Kühlen und/oder Heizen von Schüttgut
DE102007054212A1 (de) * 2007-11-12 2009-05-14 Grochowski, Horst, Dr. Fluidbehandlungsanlage mit parallel betriebenen Schüttgutbetten sowie Verfahren zum Betreiben einer solchen Anlage
PL71177Y1 (pl) * 2017-11-24 2020-01-31 Univ Technologiczno Przyrodniczy Im Jana I Jedrzeja Sniadeckich W Bydgoszczy Konstrukcja ruchomego sita do opróżniania suszarki komorowej

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BE501734A (de)

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