US2173844A - Heat exchange - Google Patents
Heat exchange Download PDFInfo
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- US2173844A US2173844A US32170A US3217035A US2173844A US 2173844 A US2173844 A US 2173844A US 32170 A US32170 A US 32170A US 3217035 A US3217035 A US 3217035A US 2173844 A US2173844 A US 2173844A
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- fluid
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
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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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/10—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with stationary catalyst bed
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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
- 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
- B01J2208/00044—Temperature 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
- B01J2208/00026—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
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
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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
- 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
- B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
- B01J2208/00283—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant liquids
Definitions
- This invention relates to heat exchange in its application to the thermal control of operations, particularly those involving the use of contact masses.
- the operations may be either endothermic or exothermic and the contact masses may be mere solid spreading material, or of porous, absorbent nature, possessing to a large or small degree adsorptive or catalytic activity.
- the specific development herein particularly described relates to the treatment or conversion of hydrocarbons, especially mineral oils from any source.
- the invention may be considered as an improvement upon or further development of certain prior disclosures which include Patent No. 1,386,768, issued to D. E. Day on August 9, 1921;, Patent No. 1,828,146, issued to A. Joseph on October 20, 1931; Patent No. 1,989,- 927, issued to me on February 5, 1935; and the copending application of A. Joseph, Serial No. 440,199 filed March 31, 1930.
- petroleum oils of high viscosity such as, for example, petroleum tars or residuae or fractions in the fuel oil range
- This invention contemplates a process wherein the heavy oil is brought into intimate relation with a porous contact mass, such as, for example, pumice, suitable blends of silica and alumina of controlled activity or other contact mass at a suitable temperature.
- a porous contact mass such as, for example, pumice, suitable blends of silica and alumina of controlled activity or other contact mass at a suitable temperature.
- carbon or carbonaceous and sulphurous material is deposited on the mass, and must periodicallybe removed in a so-called regenera- 55 version or viscosity breaking is an endothermic tion step to clean up the pores in the mass and.
- reaction whereas the regeneration is an exothermic reaction.
- heat must be supplied to maintain the contact mass at reaction temperature throughout every cross section of it. Again during regeneration, heat must be removed to maintain the temperature of the mass within a safe range; otherwise certain necessary properties of the mass will be impaired or destroyed.
- Fig. 1 showsan elevational view, partly in section, of a suitable converter, together with ducts, etc., appurtenant thereto;
- Fig. 2 is a plan view taken on line H of Fig. 1;
- Fig. 3 shows in reduced size an elevational view, partly in section, of the converter shown in Fig. 1, together with a furnace, ducts, etc., for supplying gases to the converter;
- Fig. 4 shows a detail view of an oil injector for the converter shown in Fig. 1;
- Fig. 5 shows a plan view of one of the annular perforated conduits shown horizontally arranged in Fig. 1;
- Fig. 6 shows a section through the annular conduit shown in Fig. 5;
- Fig. '7 shows a view of a wall of the annular chamber of-Fig. 1, developed
- Fig. 8 is similar to Fig. '7, except that it shows an alternative design and arrangement of fins
- Fig. 9 is a variation of the converter shown in Fig. 1.
- um -oil or tar is passed through heater I and atomizer 2, where it is mixed with a gaseous carrier such as steam and thence into annularly shaped injector 3, from which it is sprayed through openings 3a (Fig. 4), primarily in the form of mist or vapor onto the top of contact mass 4 located within the annular chamber 5, which is confined between cylindrical walls 8 and -'I.
- the contact mass 4 is confined at top and bottom by circular, disc-shaped grids or screens 8 and 8a and consists of porous spreading material in bits, fragmentsmr molded pieces, adapted for regeneration in place, which may have some catalytic activity or which may be mixed with or contain active ingredients.
- One suitable material is that disclosed in Patent No. 1,818,403, issued to Alfred Joseph on August 11, 1931.
- the heavy oil passes into the annular chamber and is taken up and retained by the contact mass 4 until converted by the contact action of the latter and heat into vapor form, whereupon it passes therefrom through screen 80. into circular duct 9, from which it passes into lead-ofi main I0, thence to be led to other treating equipment (not shown) or to storage. Any of the oil which may find its way through the reaction chamber in liquid form is led off through pipe 24.
- heat is generated in furnace II, for example, by burning fuel oil or gas therein, and is transferred to a heat-carrying fluid, for example, flue gas, which is passed through ducts I2a and I2b into annular conduits I3a and I3b, respectively, which side.
- a heat-carrying fluid for example, flue gas
- the gases are first distrib ted uniformly therearound through circular duct 23, having openings which lead therefrom into said conduit I311.
- the inner conduit is made annular because of the dummy member I4 which is employed to increase the fiow'of gases close to the inner circular wallof annular chamber 5.
- the total fiow and also the relative flow of gases between ducts I21: and I 2b are controlled by ad-
- the gases pass from the annular conduit I3a into stack I6 controlled by valve Ifia and from annular conduit I3b through duct I'I, controlled by valve IIa, which leads back to furnace II.
- Duct I1 is also connected with stack I6 by conduit I8, controlled by valve I8a.
- Intervening in duct I'I, between the junction with conduit I8 and furnace I I, is a blower I9.
- the proportion of gases recycled can be controlled as desired, and thereby the temperature of gases and speed of their fiow through annular conduits I3a and I3b are controlled.
- the amount of heat introduced into the system can, of course, also be controlled by regulating the rate fuel is admitted to the furnace II bound the aforesaid annular chaniber 5 on either A heavy petrolethe sections or beds of mass.
- the introduction of oil may be cut off and steam passed through annular chamber 5 to purge it of oil vapors.
- the steam is shut off and the apparatus is ready for the regeneration step.
- the regenerating medium may be admitted at once or the hot gases may be allowed to continue to flow through annular conduits I3a and I3! for a while to bring up the temperature from the range suitable for viscosity breaking, i. e., about 775 to 875 F.
- Regeneration is carried out by passing air or other oxygen-bearing gas, e. g., a mixture of air and inert diluent, such as flue gases, or steam, or both, into and through the contact mass to burn away the flammable deposits of carbonaceous and other materials.
- air or other oxygen-bearing gas e. g., a mixture of air and inert diluent, such as flue gases, or steam, or both
- This is accomplished by introducing the regenerating medium through pipe 26 into manifold 21, (Fig. 1), whence it flows through the several pipes 28 into respective annular distributing tubes 29, shown mounted in recesses in the edges of fins 25d, and therefrom through perforations or openings 30 (Figs, 5 and 6) into contact mass 4.
- Pipes 28 and 28a may be provided with individual valves, not shown, where it is desirable to cut off all communication between the contact mass 4 and the manifolds 21 and 21a, during the on-stream part of the complete cycle of operation.
- the regeneration is continued at least until the bulk of burnable deposits, laid down during the on-stream or viscosity breaking operation are removed by combustion. As'regeneration approaches completion, the amount of cooling necessary will become less and less.
- the temperature may be measured with the aid of pyrometers, not shown, and the temperature and speed at which heat-carrying fluid is circulated through annular conduits I30. and
- Dummy member [4 is supported by gussets 3
- Thedummy member has openings 33a and 33b at its top and bottom, respectively, to avoid a dead space therewithin.
- the outer annular conduit 13b is surrounded with suitable insulation 34 to minimize heat losses.
- the annular injector 3 is fed by a conduit leading tangentially thereinto and is of reduced cross section toward its latter end; that is, the small diameter of the annular injector gets smaller as you go around it in the direction in which the entering fluid passes. While only one step of reduced cross section is shown in Fig. 4, any plurality of steps of reduction is contemplated.
- the idea of the reduced cross section is to maintain the velocity ofthe fluid in all sections around the circumference of the annular injector substantially uniform, thereby to obtain a substantially uniform distribution of fluid around the top of annular chamber 5.
- the fluid passes from the injector through perforations or openings 3a, which are of such size in relation to the design of the injector as to insure the discharge of the reactant material from all openings in the form of mist or fog of vapors and atomized liquid.
- the end 3b of the annular injector opens back into its beginning, at the point of introduction of fluid thereinto, thereby providing a continuous swirling action and eliminating the dead end which would otherwise exist. This is a further advantage in getting uniform velocity around the annular injector and consequent uniform discharge through openings or perforations 3a therein.
- the injectors As shown, 35 are the injectors and 36 are the tubes for eduction of fluid.
- the same set of tubes may be used during regeneration as serve during the onstream part of the operation, ,the oil supply being cut oil and air or other oxygen bearing gas being sent through the contacting chamber, for example, in the same direction.
- the regeneration may be preceded by a suitable steaming out operation as desired.
- the liquid to be treated for example, petroleum oil or tar
- the liquid to be treated is passed through heater la and manifold 31 and thence, by valve controlled lines, into and through the several atomizers 2a. and from each, through respective connections, into injectors 35.
- the oil or other material passes from each injector through suitable perforations or openings spaced around the circumference thereof, for example, as the openings are spaced around the circumference of distributing tubes 29, as illustrated in Fig. 6. It then contacts the contact mass la and the resultant products leave the annular chamber in by entering annular eduction tubes 36 through suitable openings or perforations in the surface thereof.
- valve 38b The fluid products collected ineach of the eduction tubes pass therefrom, through respective connections, into manifold 38 and leave the manifold through valve 38a, passing to suitable condensers, storage or elsewhere, as During this portion of the cycle of operation valve 38b is closed.
- Steam is supplied to steam manifold 39 and may be introduced with the charging stock by passing the same into heater id or by admitting it into atomizers 2a, or both, as desired, by suitable control of the valves shown.
- the steam supply may be employed for steaming out the annular chamber 5a after the admission of charging stock is cut ed and prior to regeneration.
- an oxygen'bearing gas supplied to manifold to, is passed into chamber 5a by means'of the connections shown and is distributed therein by perforated annular injectors 35, just as charging stock is introduced.
- Products of combustion are collected in eduction tubes 36, pass into manifold 38 and therefrom'through valve 3% to suitable heat exchangers or eisewhere, valve 3811 being closed during this part of the cycle of operation.
- a heat-carrying fluid is circulated through annular conduits Ba and Nb, as above described in connection with Fig. 1 and Fig. 3,.
- annular conduits Ba and Nb as above described in connection with Fig. 1 and Fig. 3,.
- conduit 53a such fluid is introduced into conduit 53a by passing it into circular duct 9a. It passes from the duct through spaced openings M and then up through annular conduit l3a, in a state of substantially uniform circumferential dissemination.
- FIG. 8 The developed section of the wall 6 of annular chamber 5, illustrated in Fig. '1, shows fins extending from top to bottom of the chamber.
- a development of wall I would appear practically identical, except that the horizontal spacing of the fins is somewhat greater.
- a modified and in some instances a preferable arrangement and design of fins are illustrated in Fig. 8, where, in-
- the converter might consist of a plurality of concentric annular chambers, or chambers of other shape and arrangement, each spaced from another to provide intervening spaced or passageways through which a liquid or gaseous heat-carrying fluid may be circulated. That is, the reaction space may be divided into a plurality of separated chambers, each chamber having, or not, as desired, a plurality of elongate intercommunicating beds or sections of catalyst. As above illustrated, heat exchange fluid walls from the chambers or sections in which the catalyst or contact mass is confined or contained. Where separate chambers, as just described, are employed, one or more may be on stream while another one or more is in regeneration, in accordance with the foregoing description.
- annular or annular chamber for example are used, they will be understood to include ring-like cross sectional configurations, whether in the form of a circle, a rectangle or other polygonal or irregular shape, although a circular ring is the normally expected configuration.
- contact mass or contact material or catalyst or an equivalent expression is employed, it will be understood that I contemplate a contact or catalytic material, for example, in the form of fragments, particles, molded pieces or bits, which are distinct and separate from the walls or portions of the structure which conflne'the reaction zone or chamber of my apparatus.
- P ocess for the treatment of fluid in the presen e of a bed of contact material which comprises dividing the contact material into a plurality of smaller beds, passing reactants longitudinally through the smaller beds of material, permitting fluid to pass from one smaller bed to an adjacent smaller bed in the event of an obstruction to the flow of the fluid in one of said smaller beds, and utilizing an extraneous heat exchange medium for indirect heat exchange with the contact material in said smaller beds along areas dividing the material and forming said beds thereby to adjust and control reaction temperature of said contact material.
- Process for the treatment of fluid in the presence of a bed of contact material which comprises dividing the contact material into a plurality of smaller elongate beds, supplying-fluid simultaneously to all of said beds of material for passage longitudinally through said beds in substantial parallelism, permitting fluid to pass from one bed to another in the event of blocking of the flow in one bed, and utilizing an extraneous heat exchange medium for indirect heat exchange with the contact material in said smaller beds along areas dividing the material and forming said beds thereby to adjust and control reaction temperature of said contact material.
- Process for the conversion or refining of fluids with the aid of contact material or catalyst in the form of pieces or particles comprising maintaining the contact material in a plurality of elongate intercommunicating sections partially separated from each other by heat conducting surfaces, passing fluid hydrocarbon reactants longitudinally through said sections of said contact material, said fluid passing from one section to an adjacent intercommunicating section in the event of an obstruction in the one section, passing an extraneous heat exchange fluid at controlled temperature through passageways separate from but adjacent said contact material and in heat conducting relation with said surfaces, and maintaining the temperature of said heat exchange fluid such that heat is conducted by said surfaces from said heat exchange fluid to said contact material during endothermic reactions and vice versa during exothermic reactions.
- steps of process which comprise employing a reaction zone containing a deep bed of contact material in the form of pieces or particles, dividing said contact material into a plurality of elongate intercommunicatlng sections, passing fluid reactants longitudinally through contact material within said sections, said fluid passing from one section to an adjacent intercommunicating section in the event of an obstruction in the one section, circulating heat exchange fluid at controlled temperature through passages adjacent -to but separated from fluid communication with the contact material within said sections, and transferring heat through uninterrupted paths of good heat conductivity between the said heat exchange fluid and portions of said sections of contact material remote from said passages.
- Apparatus for effecting fluid reactions at controlled temperatures which comprises a casing having walls providing a confined elongate reaction chamber and heat exchange passages adjacent said reaction chamber, said reaction chamber being out of fluid communication with said heat exchange passages, catalytic material within said reaction chamber, means for introducing fluid reactants into said reaction chamber and means for withdrawing fluid products of reaction therefrom, means for circulating heat exchange fluid at controlled temperature through said heat exchange passages, and metallic fins attached to said walls and extending therefrom into interior portions of said catalytic material so as to divide the said reaction chamber into a plurality of elongate intercommunicating sections and to provide uninterrupted conduction of heat. between said heat exchange passages and interior portions of said catalytic material.
- apparatus for passing a fluid at controlled temperature through a contact mass comprising walls forming an elongated annular reaction chamber having a fluid inlet and a fluid outlet at opposite ends thereof, a
- Apparatus for efiecting fluid reactions at controlled temperature which comprises, in combination, walls forming an elongated annular reaction chamber, contact material within said chamber, means providing confined heat exchange chambers adjacent the inner and outer walls of said annular chamber, metallic members attached to each of said walls and extending both into said reaction chamber and oppositely into said heat exchange chambers, for conducting heat between interior portions 01' said contact material and centrally located points within both of said confined heat exchange chambers, said metallic members which extend into said reaction chamber serving to divide said contac material into a plurality of elongate intercom unicating sections, means for altering the temperature of a heat-carrying fluid, conduitsadapted to conduct fluid from said' lastmentioned means to said heat exchange chambers, and means adapted to proportion the flow of heat-carrying fluid between said heat exchange chambers as desired.
- apparatus for passing a fluid at controlled temperature into contact with a contact mass which comprises an upright elongated annular chamber, a contact mass in the form of pieces or fragments within said chamber, means for injecting fluid onto said contact mass in a state of substantially uniform distribution, an outlet from said annular chamber for withdrawing therefrom fluid resulting after contacting said contact mass, a confined heat exchange chamber in direct heat-conducting relationship with at least one of the circular walls oi" said annular chamber and a plurality of elongated metal fins arranged in approximately upright position and afiixed to the said one of the walls of said annular chamber, one' series extending inwardly into the interior of the said contact mass and another series extending oppositely into said heat-exchange chamber, fins of each of said series being in substantially uninterrupted heat-conducting relationship with each other, thereby to provide means for a ready and quick conduction of heat from said heat exchange chamber to the interior of said contact mass, or vice versa, when a difference in temperature between the chambers is
- Apparatus as described in claim 9 whose fins comprise short lengths of metal, aplurality of fins being required to extend the length 01' the said annular chamber, each fin being spaced from the fins adjacent either of its ends, so as to permit contact mass to be interspersed between adjacent ends of separable fins along the length of the annular chamber.
- apparatus for passing a fluid at controlled temperature into contact with a contact mass which comprises an elongated annular reaction chamber having its axis at least substantially vertical, 9. contact mass withinsaid chamber consisting of porous particles, means for injecting fluid to be treated into the top of said chamber in a state of substantially uniform distribution, an outlet for withdrawing fluid resulting, after contacting-said contact mass, from said annular chamber, confined heat exchange chambers in direct heat-conducting relationship with the inner and outer walls of said chamber, means for introducing heat-carrying fluid at a controlled temperature into and through said heat-exchange chambers and for proportioning the rates of flow therebetween as desired, and a plurality of metal fins aflixed to the inner and outer walls of said annular chamber, one series extending inwardly, from each wall respectively, into the interior of the said contact mass and another series extending oppositely, from each wall respectively, into the inner and outer heatexchange chambers respectively, said fins comprising. short lengths of metal each arranged in approximately upright position,
- apparatus for passing a fluid at controlledtemperature into contact with a contact mass which comprises an elongated annular chamber, a contact mass within said chamber, means for injecting fluid onto said 75 contact mass in a state of substantially uniform distribution, an outlet for withdrawing fluid resulting, after contacting said contact mass, from said annular chamben-confined, heat exchange chambers in heat transfer relationship with the inner and outer walls of said annular chamber, and elements of good heat conductivity extending in substantially uninterrupted heat-conducting relationship from points within at least one of said heat exchange chambers to points within the contact mass within said annular chamber.
- apparatus for passing a fluid at controlled temperature into contact with a contact mass which comprises an enlongated annular chamber, a bed of contact material in the form of particles within said chamber, confined heat. exchange chambers in direct heatconducting relationship with the inner and outer walls of said annular chamber, through which a heat-carrying fluid is adapted to flow, and heat-conducting metal elements extending in uninterrupted heat-conducting relationship from points within at least one of said heat exchange chambers to interior portions of the contact mass within said annular chamber.
- apparatus for passing a fluid at controlled temperature in contact with a contact mass which comprises an elongated annular chamber having an inlet and an outlet, a contact mass within said chamber, confined heat exchange chambers adjacent the inner and outer surfaces of said annular chamber, the walls of said annular chamber forming one side of each of said heat exchange chambers, means for altering the temperature of a heat-carrying fluid, conduits of relatively controllable effective size leading from the last-mentioned means to the inner and outer heat-exchange chambers, respectively, thereby to proportion the flow of heat-carrying fluid between the said heatexchange chambers as desired, and means including a valved duct for returning any desired proportion of the heat-carrying fluid therefrom back to the said means for altering its temperature, thereby to control the temperature and speed of circulation of said heat-carrying fluid.
- apparatus for passing a I fluid at controlled temperature into contact with a contact mass which comprises an enlongated annular chamber, a bed of contact mass within said chamber, confined heat-exchange chambers in direct heat-conducting relationship with the inner and outer walls of said annular chamber, through which a heat-carrying fluid is adapted to flow, means for injecting fluid reactants onto said contact mass in a state of substantially uniform distribution, an outlet from said annular chamber for withdrawing fluid resulting from contacting said contact mass, means cooperating with aforesaid means for periodically stopping the injection of fluid onto the contact mass, substantially annular distributing tubes, spaced from each other and arranged in series between the two ends of the aforesaid annular chamber, means for feeding a fluid into and through said distributing tubes during the periods when injection of fluid onto the said contact mass is interrupted, and a complementary series of collecting or withdrawal annular tubes interspersed between the said distributing tubes and spaced therefrom and from each other.
- Apparatus for eflecting reactions at controlled temperature which comprises, in combination,.an elongated annular reaction chamber, a bed of contact material within said chamber, confined heat exchange chambers in direct heatconducting relationship with the inner and outer 5 surfaces of said reaction chamber, a plurality of perforate, annular injectors situate within said reaction chamber, one above another, between the two ends thereof, and spaced from each other and arranged in approximate parallelism with 10 each other, and a plurality of annular eduction tubes interspersed therebetween and spaced therefrom and from each other.
- apparatus for passing a fluid at controlled temperature into contact with 5 a contact mass which comprises an elongated annular chamber having its axis at least substantially vertical, a contact mass within said chamber consisting of porous particles, means for injecting fluid to be treated into the top of 20 said chamber in-a state of substantially uniform distribution, an outlet for withdrawing fluid resulting, after contacting said contact mass, from said annular chamber, confined heat exchange chambers in direct heat-conducting relationship gg;
- each fin being spaced from the ends of the fins adjacent either of its ends to permit the contact mass to come between the ends of adjacent fins, means cooperating with the aforesaid means for injecting fluid to be treated and for stopping periodically the injec-r tion of such fluid, substantially annular distributing tubes, approximately horizontally arranged, spaced from each other heightwise throughout the height of the annular chamber,
- An element of apparatus adapted-to introduce fluid into a reaction chamber in a state of substantially uniform distribution which comprises a perforate anular tube having an opening through which fluid may be introduced at least approximately tangentially thereinto, the
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- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Description
E. J. HOUDRY HEAT EXCHANGE Sept. 26, 1939.
4 Sheets-Sheet 1 Filed July 19, 1935 5 I fl I m" W I INVENTQR EUGENE J. HOUDRY BY Sept. 26, 1939; E. J. HOUDRY HEAT EXCHANGE Filed July 19, 1955 4 Sheets-Sheet 2 lNVENfOR Euc-ENcdHpunRY ATTORNEY Sept- 1939. E: J. HOUDRY 2,173,844
' HEAT EXCHANGE Filed July 19, 1935 4 Sheets-Sheet 3 INVENTOR f EUGENEJHOUDRY W QMAWL ATTORNEY E. J. HOUDRY Sept. 26, 1939.
HEAT EXCHANGE Filed Ju1y19, 1935 4 Sheets-Sheet 4- INVENTOR EUGENE d.HounRY 144 0/. ATTORNEY Patented Sept. 26, 1939 UNITED STATES HEAT EXCHANGE Eugene J. Houdry, Rosemont, Pa., assignor to Houdry Process Corporation, Dover, Del., a corporation of Delaware Application July 19, 1935, Serial No. 32,170
18 Claims.
This invention relates to heat exchange in its application to the thermal control of operations, particularly those involving the use of contact masses. The operations may be either endothermic or exothermic and the contact masses may be mere solid spreading material, or of porous, absorbent nature, possessing to a large or small degree adsorptive or catalytic activity. While adapted for general use'in the chemical field, the specific development herein particularly described relates to the treatment or conversion of hydrocarbons, especially mineral oils from any source. In certain aspects the invention may be considered as an improvement upon or further development of certain prior disclosures which include Patent No. 1,386,768, issued to D. E. Day on August 9, 1921;, Patent No. 1,828,146, issued to A. Joseph on October 20, 1931; Patent No. 1,989,- 927, issued to me on February 5, 1935; and the copending application of A. Joseph, Serial No. 440,199 filed March 31, 1930.
While not limited to particular types of hydrocarbon materials, the invention has special application to and may be illustrated by a discussion of the treating of petroleum oils of high viscosity, such as, for example, petroleum tars or residuae or fractions in the fuel oil range, to produce a clean product or a product of reduced viscosity. This'operation may be conveniently termed viscosity breaking. From a heavy hydrocarbon, such as petroleum tar, by or with the aid of a suitable contact mass, there may be produced primarily a product of viscosity and general properties which make it suitable as a cracking stock, to be used in place of the ordinary gas oil fraction. Usually there is also produced simultaneously therewith small amounts of light products, such as gasoline and gas, and there is commonly separated some carbon or 40 solidcarbonaceous material and mineral ash. This invention contemplates a process wherein the heavy oil is brought into intimate relation with a porous contact mass, such as, for example, pumice, suitable blends of silica and alumina of controlled activity or other contact mass at a suitable temperature. During the course of the operation, carbon or carbonaceous and sulphurous material is deposited on the mass, and must periodicallybe removed in a so-called regenera- 55 version or viscosity breaking is an endothermic tion step to clean up the pores in the mass and.
reaction; whereas the regeneration is an exothermic reaction. During conversion,-to insure a uniform product and to control the reaction to maintain the best conditions, heat must be supplied to maintain the contact mass at reaction temperature throughout every cross section of it. Again during regeneration, heat must be removed to maintain the temperature of the mass within a safe range; otherwise certain necessary properties of the mass will be impaired or destroyed.
To introduce heat into the mass during the viscosity breaking step and to withdraw heat during the regeneration step, and to accomplish this in such a way that the temperature of the entire contact mass remains within the proper operative range, are among the objects of this invention. This has been a difiicult problem because the contact mass is ordinarily an extremely poor conductor of heat. Interlocked with this problem is the additional problem of providing a method and apparatus whereby fluids which are difficult to subject to contact treatment, for example, heavy oil, such as petroleum tar, can be uniformly and successfully contacted, so as to produce as nearly uniform a product as possible. Each problem needed a solution which would not interfere with the solution to the other, and both required solution in such a way as not to complicate the job of regeneration. To provide a combined and individual solution to these problems, and to provide a solution which is as economical and eflicient as possible are among the further objects of this invention. These and other objects and advantages will become apparent from the specification taken as a whole.
The invention can be best understood by reference to the accOmpanyingJdraWings, showing an illustrative embodiment of suitable apparatus, in which:
Fig. 1 showsan elevational view, partly in section, of a suitable converter, together with ducts, etc., appurtenant thereto;
Fig. 2 is a plan view taken on line H of Fig. 1;
Fig. 3 shows in reduced size an elevational view, partly in section, of the converter shown in Fig. 1, together with a furnace, ducts, etc., for supplying gases to the converter;
Fig. 4 shows a detail view of an oil injector for the converter shown in Fig. 1;
Fig. 5 shows a plan view of one of the annular perforated conduits shown horizontally arranged in Fig. 1;
Fig. 6 shows a section through the annular conduit shown in Fig. 5;
- justment of valves I5a and I5!) (Fig. 3).
Fig. '7 shows a view of a wall of the annular chamber of-Fig. 1, developed;
Fig. 8 is similar to Fig. '7, except that it shows an alternative design and arrangement of fins;
and
Fig. 9 is a variation of the converter shown in Fig. 1.
Referring more in detail to the drawings in the several figures of which like reference characters denote similar parts, and illustrating the invention in connection with the treatment of a particular material, first we shall consider the on-stream or viscosity breaking part of the complete cycle of operation. um -oil or tar is passed through heater I and atomizer 2, where it is mixed with a gaseous carrier such as steam and thence into annularly shaped injector 3, from which it is sprayed through openings 3a (Fig. 4), primarily in the form of mist or vapor onto the top of contact mass 4 located within the annular chamber 5, which is confined between cylindrical walls 8 and -'I. The contact mass 4 is confined at top and bottom by circular, disc-shaped grids or screens 8 and 8a and consists of porous spreading material in bits, fragmentsmr molded pieces, adapted for regeneration in place, which may have some catalytic activity or which may be mixed with or contain active ingredients. One suitable material is that disclosed in Patent No. 1,818,403, issued to Alfred Joseph on August 11, 1931. The heavy oil passes into the annular chamber and is taken up and retained by the contact mass 4 until converted by the contact action of the latter and heat into vapor form, whereupon it passes therefrom through screen 80. into circular duct 9, from which it passes into lead-ofi main I0, thence to be led to other treating equipment (not shown) or to storage. Any of the oil which may find its way through the reaction chamber in liquid form is led off through pipe 24.
During such operation, which is endothermic, heat is generated in furnace II, for example, by burning fuel oil or gas therein, and is transferred to a heat-carrying fluid, for example, flue gas, which is passed through ducts I2a and I2b into annular conduits I3a and I3b, respectively, which side. Before entering annular co duit I3b, however, the gases are first distrib ted uniformly therearound through circular duct 23, having openings which lead therefrom into said conduit I311. The inner conduit is made annular because of the dummy member I4 which is employed to increase the fiow'of gases close to the inner circular wallof annular chamber 5. The total fiow and also the relative flow of gases between ducts I21: and I 2b are controlled by ad- The gases pass from the annular conduit I3a into stack I6 controlled by valve Ifia and from annular conduit I3b through duct I'I, controlled by valve IIa, which leads back to furnace II. Duct I1 is also connected with stack I6 by conduit I8, controlled by valve I8a. Intervening in duct I'I, between the junction with conduit I8 and furnace I I, is a blower I9. By controlling the speed of the blower and the adjustment of valves I60, lid and I8a, the proportion of gases recycled can be controlled as desired, and thereby the temperature of gases and speed of their fiow through annular conduits I3a and I3b are controlled. The amount of heat introduced into the system can, of course, also be controlled by regulating the rate fuel is admitted to the furnace II bound the aforesaid annular chaniber 5 on either A heavy petrolethe sections or beds of mass.
through line 20. Fresh air is admitted to the furnace through ports 2 I Heat taken up by walls 6 and I and fins 25a and 25b (Figs. 1 and 2) from the hot gases passing thereover, through annular conduits I3a and I3b, is transmitted directly to and into contact mass 4 within annular chamber 5, or at least to those parts of the mass against and adjacent the-inner faces of walls 6 and I and the fins 25c and 25d, respectively, in a path of uninterrupted metal conduction. The walls 6 and fins 25c and the walls I and fins 2511 provide intercommunieating elongate sections of catalyst or contact material. The arrangement of fins illustrated in Fig. 8 provides intercommunication at the ends, as well as the sides, of adjacent elongate sections or beds of contact or catalytic mass, and induces fluids or reactant vapors to assume a somewhat tortuous path in passing up or down through It will be obvious that where, in the course-of use of the apparatus, an obstruction or clogging occurs at a point in any one section, reactants passing longitudinally through that section may get past the obstruction by fiowing around through an adjacent intercommunicating section.
When the viscosity breaking or on-stream operation has proceeded for such a period of time that the desired quality of product is no longer being produced or the efficiency of the apparatus has fallen off 'very materially, or both, the introduction of oil may be cut off and steam passed through annular chamber 5 to purge it of oil vapors. When this is accomplished, the steam is shut off and the apparatus is ready for the regeneration step. The regenerating medium may be admitted at once or the hot gases may be allowed to continue to flow through annular conduits I3a and I3!) for a while to bring up the temperature from the range suitable for viscosity breaking, i. e., about 775 to 875 F.
to that suitable for regeneration, i. e., about 900 F. or higher.
Regeneration is carried out by passing air or other oxygen-bearing gas, e. g., a mixture of air and inert diluent, such as flue gases, or steam, or both, into and through the contact mass to burn away the flammable deposits of carbonaceous and other materials. This is accomplished by introducing the regenerating medium through pipe 26 into manifold 21, (Fig. 1), whence it flows through the several pipes 28 into respective annular distributing tubes 29, shown mounted in recesses in the edges of fins 25d, and therefrom through perforations or openings 30 (Figs, 5 and 6) into contact mass 4. ,The products of combustion are removed from the chamber by passing through similar openings or perforations in the nearest annular collecting or withdrawal tubes 29a, which are arranged in alternation with distributing tubes 29, thence into respective pipes 28a which lead into manifold 21a and finally are led away, to heat exchangers or elsewhere, through pipe 26a. Pipes 28 and 28a may be provided with individual valves, not shown, where it is desirable to cut off all communication between the contact mass 4 and the manifolds 21 and 21a, during the on-stream part of the complete cycle of operation.
As soon as regeneration gets under way, the operation being exothermic, there is a natural tendency for the temperature in the contact mass 4 to build up. Since it is harmful for the mass to be heated above a predetermined maximum, say 1200 or 1500 F. (655 or 815 C.) for example,
depending on the composition and structure of the particular mass used, it is desirable to main tain the mass below such temperature, and this can be accomplished bywithdrawing the generated heat by circulating gasesthrough conduits I and I3b at a temperature such that there will be the proper and desired heatexchange from the contact mass to the circulating gases. This can be accomplished with the apparatus shown, for example, by cutting off (or reducing) the supply of fuel to the furnace and circulatmg gases through the system, heat being eliminated from the system by venting a portion of the gases through the stack I6. The amount of cooling desired may be regulated by suitable adjustment of the valves and control of the speed of blower I9. i
The regeneration is continued at least until the bulk of burnable deposits, laid down during the on-stream or viscosity breaking operation are removed by combustion. As'regeneration approaches completion, the amount of cooling necessary will become less and less. The temperature may be measured with the aid of pyrometers, not shown, and the temperature and speed at which heat-carrying fluid is circulated through annular conduits I30. and |3b will be controlled accordingly.
Dummy member [4 is supported by gussets 3|, (Fig. 1) which in turn are fastened to fins 25a, and is maintained in centered relationship inside of the inner annular wall 6 of annular chamber 5 by centering lugs 32, which also are attached to fins 25a. Thedummy member has openings 33a and 33b at its top and bottom, respectively, to avoid a dead space therewithin.
The outer annular conduit 13b is surrounded with suitable insulation 34 to minimize heat losses.
. The annular injector 3 is fed by a conduit leading tangentially thereinto and is of reduced cross section toward its latter end; that is, the small diameter of the annular injector gets smaller as you go around it in the direction in which the entering fluid passes. While only one step of reduced cross section is shown in Fig. 4, any plurality of steps of reduction is contemplated. The idea of the reduced cross section is to maintain the velocity ofthe fluid in all sections around the circumference of the annular injector substantially uniform, thereby to obtain a substantially uniform distribution of fluid around the top of annular chamber 5. The fluid passes from the injector through perforations or openings 3a, which are of such size in relation to the design of the injector as to insure the discharge of the reactant material from all openings in the form of mist or fog of vapors and atomized liquid. The end 3b of the annular injector opens back into its beginning, at the point of introduction of fluid thereinto, thereby providing a continuous swirling action and eliminating the dead end which would otherwise exist. This is a further advantage in getting uniform velocity around the annular injector and consequent uniform discharge through openings or perforations 3a therein.
In place of having a single injector located at the top of the annular contacting chamber, in certain cases there are advantages in providing several injectors, spaced one above another between the two ends of such chamber, with a layer of contact mass below each. Or, as shown in Fig. 9, there may be a plurality of injectors imbedded in the contact mass and a corresponding desired.
plurality of annular tubes for withdrawing fluids from the contacting chamber. As shown, 35 are the injectors and 36 are the tubes for eduction of fluid. The same set of tubes may be used during regeneration as serve during the onstream part of the operation, ,the oil supply being cut oil and air or other oxygen bearing gas being sent through the contacting chamber, for example, in the same direction. The regeneration may be preceded by a suitable steaming out operation as desired.
Considering the apparatus of Fig. 9 more in detail, during the on-stream part of the cycle of operation the liquid to be treated, for example, petroleum oil or tar, is passed through heater la and manifold 31 and thence, by valve controlled lines, into and through the several atomizers 2a. and from each, through respective connections, into injectors 35. The oil or other material passes from each injector through suitable perforations or openings spaced around the circumference thereof, for example, as the openings are spaced around the circumference of distributing tubes 29, as illustrated in Fig. 6. It then contacts the contact mass la and the resultant products leave the annular chamber in by entering annular eduction tubes 36 through suitable openings or perforations in the surface thereof. The fluid products collected ineach of the eduction tubes pass therefrom, through respective connections, into manifold 38 and leave the manifold through valve 38a, passing to suitable condensers, storage or elsewhere, as During this portion of the cycle of operation valve 38b is closed.
Steam is supplied to steam manifold 39 and may be introduced with the charging stock by passing the same into heater id or by admitting it into atomizers 2a, or both, as desired, by suitable control of the valves shown. By the connections shown, the steam supply may be employed for steaming out the annular chamber 5a after the admission of charging stock is cut ed and prior to regeneration. During regeneration an oxygen'bearing gas, supplied to manifold to, is passed into chamber 5a by means'of the connections shown and is distributed therein by perforated annular injectors 35, just as charging stock is introduced. Products of combustion are collected in eduction tubes 36, pass into manifold 38 and therefrom'through valve 3% to suitable heat exchangers or eisewhere, valve 3811 being closed during this part of the cycle of operation.
A heat-carrying fluid is circulated through annular conduits Ba and Nb, as above described in connection with Fig. 1 and Fig. 3,. However,
such fluid is introduced into conduit 53a by passing it into circular duct 9a. It passes from the duct through spaced openings M and then up through annular conduit l3a, in a state of substantially uniform circumferential dissemination.
The developed section of the wall 6 of annular chamber 5, illustrated in Fig. '1, shows fins extending from top to bottom of the chamber. A development of wall I would appear practically identical, except that the horizontal spacing of the fins is somewhat greater. A modified and in some instances a preferable arrangement and design of fins are illustrated in Fig. 8, where, in-
stead of extending continuously from top to bottom of the chamber, a number of short sections of fin replace each long section and are spaced endwise from each other. This allows the contact mass to get between adjacent ends of adjacent sections and thereby eliminates all chance of unvaporized or condensed oil flowing from top to bottom of the annular contact chamber 5 along the vertical surface of a fin. Of course this is of primary importance in connection with the fins within chamber 5 but the same arrangement can be made of the fins protruding into annular conduits [3a and. Nb.
While the invention is particularly illustrated in connection with the treatment of a heavy petroleum oil or tar, for which it is particularly adapted, yet it may be employed for various other contacting actions and the illustration used is not to be construed as a limitation. Other compositions of contact material than those herein mentioned may be used, and different reactants, hydrocarbon or otherwise, may be subjected to treatment, with a view to arriving at a similar or entirely. differentproduct.
Various other modifications or embodiments of the invention will occur 'to those skilled in the art. For example, in place of having a single annular contacting chamber, as herein specifically described, the converter might consist of a plurality of concentric annular chambers, or chambers of other shape and arrangement, each spaced from another to provide intervening spaced or passageways through which a liquid or gaseous heat-carrying fluid may be circulated. That is, the reaction space may be divided into a plurality of separated chambers, each chamber having, or not, as desired, a plurality of elongate intercommunicating beds or sections of catalyst. As above illustrated, heat exchange fluid walls from the chambers or sections in which the catalyst or contact mass is confined or contained. Where separate chambers, as just described, are employed, one or more may be on stream while another one or more is in regeneration, in accordance with the foregoing description.
Again, in place of having the distributing and collecting tubes in the reaction chamber arranged horizontally and of annular form, straight tubes, vertically arranged, might be substituted. Obviously many other systems of ducts and heating means could be readily devised, upon reading this specification, to perform the functions of the apparatus illustrated. Further, many other styles and arrangements of fins could be substituted for those illustrated. All such equivalent constructions and obvious variations are comprehended within the scope of the appended claims.
Where herein or in the appended claims the terms annular or annular chamber, for example are used, they will be understood to include ring-like cross sectional configurations, whether in the form of a circle, a rectangle or other polygonal or irregular shape, although a circular ring is the normally expected configuration.
Where herein orv in the appended claims the terms contact mass or contact material or catalyst", or an equivalent expression is employed, it will be understood that I contemplate a contact or catalytic material, for example, in the form of fragments, particles, molded pieces or bits, which are distinct and separate from the walls or portions of the structure which conflne'the reaction zone or chamber of my apparatus.
t I claim is:
1. P ocess for the treatment of fluid in the presen e of a bed of contact material which comprises dividing the contact material into a plurality of smaller beds, passing reactants longitudinally through the smaller beds of material, permitting fluid to pass from one smaller bed to an adjacent smaller bed in the event of an obstruction to the flow of the fluid in one of said smaller beds, and utilizing an extraneous heat exchange medium for indirect heat exchange with the contact material in said smaller beds along areas dividing the material and forming said beds thereby to adjust and control reaction temperature of said contact material.
2. Process for the treatment of fluid in the presence of a bed of contact material which comprises dividing the contact material into a plurality of smaller elongate beds, supplying-fluid simultaneously to all of said beds of material for passage longitudinally through said beds in substantial parallelism, permitting fluid to pass from one bed to another in the event of blocking of the flow in one bed, and utilizing an extraneous heat exchange medium for indirect heat exchange with the contact material in said smaller beds along areas dividing the material and forming said beds thereby to adjust and control reaction temperature of said contact material.
3. Process for the conversion or refining of fluids with the aid of contact material or catalyst in the form of pieces or particles comprising maintaining the contact material in a plurality of elongate intercommunicating sections partially separated from each other by heat conducting surfaces, passing fluid hydrocarbon reactants longitudinally through said sections of said contact material, said fluid passing from one section to an adjacent intercommunicating section in the event of an obstruction in the one section, passing an extraneous heat exchange fluid at controlled temperature through passageways separate from but adjacent said contact material and in heat conducting relation with said surfaces, and maintaining the temperature of said heat exchange fluid such that heat is conducted by said surfaces from said heat exchange fluid to said contact material during endothermic reactions and vice versa during exothermic reactions.
4. In effecting chemical reactions and controlling the temperature thereof, the steps of process which comprise employing a reaction zone containing a deep bed of contact material in the form of pieces or particles, dividing said contact material into a plurality of elongate intercommunicatlng sections, passing fluid reactants longitudinally through contact material within said sections, said fluid passing from one section to an adjacent intercommunicating section in the event of an obstruction in the one section, circulating heat exchange fluid at controlled temperature through passages adjacent -to but separated from fluid communication with the contact material within said sections, and transferring heat through uninterrupted paths of good heat conductivity between the said heat exchange fluid and portions of said sections of contact material remote from said passages.
5. In the endothermic conversion of hydrocarbon reactants in a confined reaction zone, the steps of process which comprise dividing said zone into elongate sections and separating them by heat exchange surfaces. filling said secpassageways adjacent to but out of fluid communication with the catalyst in such sections, at
intervals regeneratingeach of said sections of catalyst by interrupting the passage of reactant hydrocarbons therethroughand passing an oxygen-containing regenerating fluid therethrough, and transferring heat by uninterrupted conduction between said heat exchange fluid and boundary portions of said sections of catalyst,
said heat'exchange fluid being controlled in,
temperature so as to absorb heat from said sections of said catalyst when in regeneration and to supply heat to said sections when on stream.
6. Apparatus for effecting fluid reactions at controlled temperatures which comprises a casing having walls providing a confined elongate reaction chamber and heat exchange passages adjacent said reaction chamber, said reaction chamber being out of fluid communication with said heat exchange passages, catalytic material within said reaction chamber, means for introducing fluid reactants into said reaction chamber and means for withdrawing fluid products of reaction therefrom, means for circulating heat exchange fluid at controlled temperature through said heat exchange passages, and metallic fins attached to said walls and extending therefrom into interior portions of said catalytic material so as to divide the said reaction chamber into a plurality of elongate intercommunicating sections and to provide uninterrupted conduction of heat. between said heat exchange passages and interior portions of said catalytic material.
7. In combination, apparatus for passing a fluid at controlled temperature through a contact mass comprising walls forming an elongated annular reaction chamber having a fluid inlet and a fluid outlet at opposite ends thereof, a
contact mass within said annular chamber, means providing confined heat-exchange chambers adjacent the inner and outer walls of said annular chamber, metallic members for conducting heat through said walls between interior portions of said contact mass and points located within both of said confined heat exchange chambers, means for altering the temperature of a heat.- carrying fluid, a conduit oi controllable effective diameter for leading fluid from said lastmentioned means to said heat exchange chambers, and means including a valved duct for returning any desired proportion of the heat-carrying fluid therefrom back to the said means for altering its temperature.
8. Apparatus for efiecting fluid reactions at controlled temperature which comprises, in combination, walls forming an elongated annular reaction chamber, contact material within said chamber, means providing confined heat exchange chambers adjacent the inner and outer walls of said annular chamber, metallic members attached to each of said walls and extending both into said reaction chamber and oppositely into said heat exchange chambers, for conducting heat between interior portions 01' said contact material and centrally located points within both of said confined heat exchange chambers, said metallic members which extend into said reaction chamber serving to divide said contac material into a plurality of elongate intercom unicating sections, means for altering the temperature of a heat-carrying fluid, conduitsadapted to conduct fluid from said' lastmentioned means to said heat exchange chambers, and means adapted to proportion the flow of heat-carrying fluid between said heat exchange chambers as desired.
9. In combination, apparatus for passing a fluid at controlled temperature into contact with a contact mass which comprises an upright elongated annular chamber, a contact mass in the form of pieces or fragments within said chamber, means for injecting fluid onto said contact mass in a state of substantially uniform distribution, an outlet from said annular chamber for withdrawing therefrom fluid resulting after contacting said contact mass, a confined heat exchange chamber in direct heat-conducting relationship with at least one of the circular walls oi" said annular chamber and a plurality of elongated metal fins arranged in approximately upright position and afiixed to the said one of the walls of said annular chamber, one' series extending inwardly into the interior of the said contact mass and another series extending oppositely into said heat-exchange chamber, fins of each of said series being in substantially uninterrupted heat-conducting relationship with each other, thereby to provide means for a ready and quick conduction of heat from said heat exchange chamber to the interior of said contact mass, or vice versa, when a difference in temperature between the chambers is provided.
10. Apparatus as described in claim 9 whose fins comprise short lengths of metal, aplurality of fins being required to extend the length 01' the said annular chamber, each fin being spaced from the fins adjacent either of its ends, so as to permit contact mass to be interspersed between adjacent ends of separable fins along the length of the annular chamber.
11. In combination, apparatus for passing a fluid at controlled temperature into contact with a contact mass which comprises an elongated annular reaction chamber having its axis at least substantially vertical, 9. contact mass withinsaid chamber consisting of porous particles, means for injecting fluid to be treated into the top of said chamber in a state of substantially uniform distribution, an outlet for withdrawing fluid resulting, after contacting-said contact mass, from said annular chamber, confined heat exchange chambers in direct heat-conducting relationship with the inner and outer walls of said chamber, means for introducing heat-carrying fluid at a controlled temperature into and through said heat-exchange chambers and for proportioning the rates of flow therebetween as desired, and a plurality of metal fins aflixed to the inner and outer walls of said annular chamber, one series extending inwardly, from each wall respectively, into the interior of the said contact mass and another series extending oppositely, from each wall respectively, into the inner and outer heatexchange chambers respectively, said fins comprising. short lengths of metal each arranged in approximately upright position, to avoid obstruction to flow of reactants through the reaction chamber. 1
12. In combination, apparatus for passing a fluid at controlledtemperature into contact with a contact mass which comprises an elongated annular chamber, a contact mass within said chamber, means for injecting fluid onto said 75 contact mass in a state of substantially uniform distribution, an outlet for withdrawing fluid resulting, after contacting said contact mass, from said annular chamben-confined, heat exchange chambers in heat transfer relationship with the inner and outer walls of said annular chamber, and elements of good heat conductivity extending in substantially uninterrupted heat-conducting relationship from points within at least one of said heat exchange chambers to points within the contact mass within said annular chamber.
13. In combination, apparatus for passing a fluid at controlled temperature into contact with a contact mass which comprises an enlongated annular chamber, a bed of contact material in the form of particles within said chamber, confined heat. exchange chambers in direct heatconducting relationship with the inner and outer walls of said annular chamber, through which a heat-carrying fluid is adapted to flow, and heat-conducting metal elements extending in uninterrupted heat-conducting relationship from points within at least one of said heat exchange chambers to interior portions of the contact mass within said annular chamber.
14. In combination, apparatus for passing a fluid at controlled temperature in contact with a contact mass which comprises an elongated annular chamber having an inlet and an outlet, a contact mass within said chamber, confined heat exchange chambers adjacent the inner and outer surfaces of said annular chamber, the walls of said annular chamber forming one side of each of said heat exchange chambers, means for altering the temperature of a heat-carrying fluid, conduits of relatively controllable effective size leading from the last-mentioned means to the inner and outer heat-exchange chambers, respectively, thereby to proportion the flow of heat-carrying fluid between the said heatexchange chambers as desired, and means including a valved duct for returning any desired proportion of the heat-carrying fluid therefrom back to the said means for altering its temperature, thereby to control the temperature and speed of circulation of said heat-carrying fluid.
15. In combination, apparatus for passing a I fluid at controlled temperature into contact with a contact mass which comprises an enlongated annular chamber, a bed of contact mass within said chamber, confined heat-exchange chambers in direct heat-conducting relationship with the inner and outer walls of said annular chamber, through which a heat-carrying fluid is adapted to flow, means for injecting fluid reactants onto said contact mass in a state of substantially uniform distribution, an outlet from said annular chamber for withdrawing fluid resulting from contacting said contact mass, means cooperating with aforesaid means for periodically stopping the injection of fluid onto the contact mass, substantially annular distributing tubes, spaced from each other and arranged in series between the two ends of the aforesaid annular chamber, means for feeding a fluid into and through said distributing tubes during the periods when injection of fluid onto the said contact mass is interrupted, and a complementary series of collecting or withdrawal annular tubes interspersed between the said distributing tubes and spaced therefrom and from each other.
16. Apparatus for eflecting reactions at controlled temperature which comprises, in combination,.an elongated annular reaction chamber, a bed of contact material within said chamber, confined heat exchange chambers in direct heatconducting relationship with the inner and outer 5 surfaces of said reaction chamber, a plurality of perforate, annular injectors situate within said reaction chamber, one above another, between the two ends thereof, and spaced from each other and arranged in approximate parallelism with 10 each other, and a plurality of annular eduction tubes interspersed therebetween and spaced therefrom and from each other.
17. In combination, apparatus for passing a fluid at controlled temperature into contact with 5 a contact mass which comprises an elongated annular chamber having its axis at least substantially vertical, a contact mass within said chamber consisting of porous particles, means for injecting fluid to be treated into the top of 20 said chamber in-a state of substantially uniform distribution, an outlet for withdrawing fluid resulting, after contacting said contact mass, from said annular chamber, confined heat exchange chambers in direct heat-conducting relationship gg;
with the inner and outer walls of said chamber, means for introducing heat-carrying fluid at a controlled temperature into and through said heat-exchange chambers and for proportioning the rates of flow therebetween as desired, a plu 30 rality of metal fins affixed to the inner and outer walls of said annular chamber, one series extending inwardly, from each wall respectively, into the interior of the said contact mass and another series extending oppositely, from each wall re- 35 spectively, into the inner and outer heatexchange chambers respectively, said fins comprising short lengths of metal each arranged in approximately upright position, a plurality of fins being required to extend the height of said .10
annular chamber, each fin being spaced from the ends of the fins adjacent either of its ends to permit the contact mass to come between the ends of adjacent fins, means cooperating with the aforesaid means for injecting fluid to be treated and for stopping periodically the injec-r tion of such fluid, substantially annular distributing tubes, approximately horizontally arranged, spaced from each other heightwise throughout the height of the annular chamber,
means for feeding a gas into and through said distributing tubes during the periods when injecting into said annular chamber of fluid to be treated is interrupted, and a complementary series of annular collecting or withdrawal tubes interspersed between the said distributing tubes and spaced therefrom and from each other in heightwise relationship.
18. An element of apparatus adapted-to introduce fluid into a reaction chamber in a state of substantially uniform distribution which comprises a perforate anular tube having an opening through which fluid may be introduced at least approximately tangentially thereinto, the
diameter of said tube becoming progressively I CERTIFICATE OF coaREcTIdiI. Patent No. 2,173,8hh'. September 26, 1959.
v EUGENE J. HOUDRY.
It is hereby certified that error appears in the printed specification of the above numbered patent requiring correction as follows Page 1, first column, line 27, for "residuae" read residue; page 1 first column, line 29, for "spaced" read spaces; page 5, second column, line hl, claim 10, for the word "separable" read separate; page 6, first column, lines lLy-andlfi,
claims 15 and 15 respectively, for Fenlongated" read elongated; same page, second column, line 52-55, for "injecting" read inject-ion; line 62, claim 18, for "anular" read I annularg'and that the said Letters Patent should be read with this correction therein thatthe same may conform to the record of-the case in the Patent Office;
Signed and sealed this 7th day of November, A. D. 1959.
Henry .Van Arsdale; (Seal) Acting Cornmissionercof Patents.
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
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US32170A US2173844A (en) | 1935-07-19 | 1935-07-19 | Heat exchange |
GB18703/36A GB477846A (en) | 1935-07-19 | 1936-07-06 | Process of and apparatus for the treatment or catalysis of hydrocarbons or other fluids and for heat exchange |
FR812384D FR812384A (en) | 1935-07-19 | 1936-07-17 | Converter device for treatment of gases or mixtures of gases and vapors |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US32170A US2173844A (en) | 1935-07-19 | 1935-07-19 | Heat exchange |
Publications (1)
Publication Number | Publication Date |
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US2173844A true US2173844A (en) | 1939-09-26 |
Family
ID=21863483
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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US32170A Expired - Lifetime US2173844A (en) | 1935-07-19 | 1935-07-19 | Heat exchange |
Country Status (3)
Country | Link |
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US (1) | US2173844A (en) |
FR (1) | FR812384A (en) |
GB (1) | GB477846A (en) |
Cited By (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2417359A (en) * | 1943-11-06 | 1947-03-11 | Phillips Petroleum Co | Carbon removal and regenerative gas requirements in catalyst reactivation |
US2421651A (en) * | 1939-02-16 | 1947-06-03 | Standard Oil Dev Co | Conversion of hydrocarbon oils |
US2449016A (en) * | 1943-12-11 | 1948-09-07 | Socony Vacuum Oil Co Inc | Activation of petroleum adsorbents |
US2454943A (en) * | 1945-07-17 | 1948-11-30 | Lummus Co | Heater for hydrocarbon fluids |
US2520146A (en) * | 1947-08-06 | 1950-08-29 | Houdry Process Corp | Art of producing hydrocarbon vapors |
US2592121A (en) * | 1948-07-08 | 1952-04-08 | Socony Vacuum Oil Co Inc | Regeneration of a moving bed catalyst at a uniform burning rate |
US2599611A (en) * | 1945-08-07 | 1952-06-10 | Joris Daniel Heijligers | Heat exchanger for hot gas piston engines |
US2659392A (en) * | 1947-09-15 | 1953-11-17 | Frenkel Meyer | Heat exchanger |
US3119671A (en) * | 1960-09-28 | 1964-01-28 | Chemical Coustruction Corp | Upright fluid heating furnace with heat recovery system |
US3129065A (en) * | 1960-09-14 | 1964-04-14 | Chemical Construction Corp | Upright fluid heating furnace with integral heat recovery means |
US3231512A (en) * | 1963-07-10 | 1966-01-25 | Atlantic Res Corp | Adsorption device |
US3492097A (en) * | 1966-10-14 | 1970-01-27 | Nat Lead Co | Metal halide generator |
US3620685A (en) * | 1969-07-30 | 1971-11-16 | Phillips Petroleum Co | Radial flow catalyst reactor |
US3635682A (en) * | 1969-06-13 | 1972-01-18 | United Aircraft Corp | Fuel cell reactor-burner assembly |
US5171455A (en) * | 1991-10-18 | 1992-12-15 | International Environmental Systems, Inc. | Method and apparatus for separation of toxic contaminants by nebulization |
US20100307834A1 (en) * | 2009-06-03 | 2010-12-09 | National Oilwell Varco, L.P. | Vessel to Condition Dry Drill Cuttings |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA1107039A (en) * | 1976-12-22 | 1981-08-18 | Ronald J. Masters | Upflow catalytic reaction apparatus with anti- fluidization means |
FR2374948A1 (en) * | 1976-12-22 | 1978-07-21 | United Technologies Corp | IMPROVEMENT OF ENDOTHERMAL CATALYTIC REACTION EQUIPMENT WITH MULTIPLE REACTORS |
FR2374947A1 (en) * | 1976-12-22 | 1978-07-21 | United Technologies Corp | COMPACT MULTI-REACTOR APPARATUS FOR CATALYTIC REACTIONS |
GB2238487A (en) * | 1989-11-25 | 1991-06-05 | Methan Limited | Reforming apparatus |
CN111468043B (en) * | 2020-03-13 | 2022-04-08 | 宁波巨化化工科技有限公司 | Fixed bed reactor with bed temperature uniformly distributed |
-
1935
- 1935-07-19 US US32170A patent/US2173844A/en not_active Expired - Lifetime
-
1936
- 1936-07-06 GB GB18703/36A patent/GB477846A/en not_active Expired
- 1936-07-17 FR FR812384D patent/FR812384A/en not_active Expired
Cited By (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2421651A (en) * | 1939-02-16 | 1947-06-03 | Standard Oil Dev Co | Conversion of hydrocarbon oils |
US2417359A (en) * | 1943-11-06 | 1947-03-11 | Phillips Petroleum Co | Carbon removal and regenerative gas requirements in catalyst reactivation |
US2449016A (en) * | 1943-12-11 | 1948-09-07 | Socony Vacuum Oil Co Inc | Activation of petroleum adsorbents |
US2454943A (en) * | 1945-07-17 | 1948-11-30 | Lummus Co | Heater for hydrocarbon fluids |
US2599611A (en) * | 1945-08-07 | 1952-06-10 | Joris Daniel Heijligers | Heat exchanger for hot gas piston engines |
US2520146A (en) * | 1947-08-06 | 1950-08-29 | Houdry Process Corp | Art of producing hydrocarbon vapors |
US2659392A (en) * | 1947-09-15 | 1953-11-17 | Frenkel Meyer | Heat exchanger |
US2592121A (en) * | 1948-07-08 | 1952-04-08 | Socony Vacuum Oil Co Inc | Regeneration of a moving bed catalyst at a uniform burning rate |
US3129065A (en) * | 1960-09-14 | 1964-04-14 | Chemical Construction Corp | Upright fluid heating furnace with integral heat recovery means |
US3119671A (en) * | 1960-09-28 | 1964-01-28 | Chemical Coustruction Corp | Upright fluid heating furnace with heat recovery system |
US3231512A (en) * | 1963-07-10 | 1966-01-25 | Atlantic Res Corp | Adsorption device |
US3492097A (en) * | 1966-10-14 | 1970-01-27 | Nat Lead Co | Metal halide generator |
US3635682A (en) * | 1969-06-13 | 1972-01-18 | United Aircraft Corp | Fuel cell reactor-burner assembly |
US3620685A (en) * | 1969-07-30 | 1971-11-16 | Phillips Petroleum Co | Radial flow catalyst reactor |
US5171455A (en) * | 1991-10-18 | 1992-12-15 | International Environmental Systems, Inc. | Method and apparatus for separation of toxic contaminants by nebulization |
US20100307834A1 (en) * | 2009-06-03 | 2010-12-09 | National Oilwell Varco, L.P. | Vessel to Condition Dry Drill Cuttings |
US8708065B2 (en) * | 2009-06-03 | 2014-04-29 | National Oilwell Varco, L.P. | Vessel to condition dry drill cuttings |
Also Published As
Publication number | Publication date |
---|---|
FR812384A (en) | 1937-05-08 |
GB477846A (en) | 1938-01-06 |
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