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Publication numberUS3075580 A
Publication typeGrant
Publication dateJan 29, 1963
Filing dateAug 31, 1956
Priority dateAug 31, 1956
Publication numberUS 3075580 A, US 3075580A, US-A-3075580, US3075580 A, US3075580A
InventorsDavis Jr William L
Original AssigneeUnited States Steel Corp
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Heat exchanger and method
US 3075580 A
Abstract  available in
Images(2)
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Claims  available in
Description  (OCR text may contain errors)

Jan. 29, 1963 w. L. DAVIS, JR 3,075,530

HEAT EXCHANGER AND METHOD Filed Aug. 31, 1956 2 Sheets-Sheet 2 COUN TE RCURRE N T SYSTEM E k r; FLU/0 1 1: E k 2 E FLUID 2 DISTANCE FROM INLET COCURRENT SYS TEM g v; FLU/0 1 r 2 8i ,4 FLU/0 2 [u OUT DISTANCE FROM INLET FLUID/ZED BED SYSTEM L FLU/D 1 L L 7'; E FLU/D 2 k OUT D/STA/VCE FROM INLET //VVEA/7'0R.' W/LL/AM L. DAV/S, Jr.,

his Af/omey.

waited rates This invention relates to an improved recuperative-type heat exchanger and heat exchanging method.

The present application is a continuation-in-part of my earlier co-pending application Serial No. 476,969, filed December 22, 1954, and now abandoned.

In a recuperator which utilizes a gas to heat or cool another gas, each gas has its own fiow passage'out of communication with the other. rated by walls of heat conductive metal, and one means for increasing the rate of heat transfer between them is to include static beds of solid particles within one or both passages. Flow of the two gases can be either countercurrent or cocurrent, but in either event there is a substantial heat gradient between the inlet and outlet. This gradient creates thermal stresses within the equipment, which is thereby mechanicallyweakened. The coefficient of heat transfer, and hence the efliciency, usually changes with the temperature and varies in different parts of the apparatus.

An object of the present invention is to provide an improved recuperativetype heat exchanger and heat exchanging method applicable to gases wherein temperature gradients are substantially eliminated.

A more specific object is to provide a recuperativetype heat exchanger and method involving recuperative principles in which both flow systems contain beds of fluidized solids each maintained at a uniform temperature by vertical back mixing, thereby promoting eilicient heat transfer therebetween and eliminating the usual temperature gradient.

in accomplishing these and other objects of the invention, I have provided improved details of structure, preferred forms of which are shown in the accompanying drawings, in which:

FIGURE 1 is a diagrammatic vertical longitudinal section of one form of heat exchanger constructed in accordance with my invention;

FIGURE 2 is a diagrammatic cross section on line Il-li of FIGURE 1;

FIGURE 3 is a diagrammatic cross section of a modification;

FIGURE 4 is a diagrammatic cross section of another modification;

FlGURE 5 is a graph showing a typical relation between two fluids in a conventional countercurrent recuperative heat exchange system;

FIGURE 6 is a similar graph in a conventional cocurrent system; and

FTGURE 7 is another similar graph in a cocurrent fluidized bed system in accordance with my invention.

The heat exchanger shown in FTGURES l and 2 comprises outer and inner cylindrical walls it) and 12 which define an annular flow passage 13 and a central cylindrical flow passage 14. The outer wall it} is insulated to prevent loss of. heat therethrough, while the inner wall 12 is of heat conductive material. Preferably the outer wall has conical upper and lower end portions 15 and to. A perforate member 17 (for example, a screen or a perforated plate) is fixed within the outer wall it} and extends across the annular passage 13 adjacent the bottom. A circular perforate member 18 is similarly fixed within the inner wall 12 and extends across the cylindrical passage 14 adjacent the bottom. The inner wall 12 The passages are sepa- I ice is impervious throughout, whereby there is no communication betwcen the passages 13 and 14.

Both passages 13 and 14 contain captive beds of finely divided solids, referred to in the art as a thermophore, supported on the perforate members 17 and 18. The thermophore can be any of numerous materials that have high heat capacity, melting points higher than the temperature encountered, and are not reactive to the gases involved. Examples of materials suitable for use with hot gases are silica, silicon carbide, alumina, or hematite, and with cold gases powdered metals. The thermophore is of a particle size preferably between 10 and mesh, smaller sizes being avoided to minimize dust losses. There is an approximately uniform size distribution of particles between the two extremes. The two passages are equipped with upper and lower pipes 19 and 2%, each of which contain a pair of normally closed valves for introducing or removing the thermophore. The minimum bed depth is about 3 feet and the minimum horizontal dimension about 4 inches. With a bed of circular cross section and minimum diameter, the maximum depth-todiameter ratio is about 20. This ratio is important with small diameters because too great a depth hinders vertical back mixing, but becomes less important as the horizontal dimension increases.

The gas Whose temperature is farther from that of the surrounding atmosphere (either higher or lower), is introduced to the bottom of the central passage 14 via an inlet 21 and discharges from the top via an outlet 22. The other gas, which is to be heated or cooled, is introduced to the bottom of the annular passage 13 via an inlet 23 and discharges at the top via an outlet 24. Preferably the outlets 22 and 24 are equipped with dust collectors 25 shown only schematically. The gas streams in both the passages 13 and 14 travel upwardly in a cocurrent direction and at a sufficient velocity (superficially 0.5 to 2 feet per second) to fluidize the thermophore beds within these passages. In accordance with known principles, these beds physically resemble boiling liquids. They have an apparent density of 30 to pounds per cubic foot. The particles in the central passage 14% quickly and uniformly acquire the temperature of gas therein, and by their movement transmit this temperature through the inner Wall 12 to the particles in the annular passage 13. The gas in the latter passage quickly and uniformly acquires the temperature of the particles therein. There is little or no temperature gradient within either bed because of the vertical back mixing which results under the conditions I have described.

FIGURE 3 shows a modification in which the single central passage is replaced by a plurality of internal passages 26. FIGURE 4 shows a modification in which the heat exchanger is of rectangular cross section and is divided by a series of partitions 27 and 28 into passages 29 and 30 of rectangular cross section. The passages 29 carry one substance and the passages 30 the other. The passages in these modifications contain thermophore, and the modifications operate in the same fashion as the embodiment shown in FIGURES l and 2. However, they may furnish more efficient heat transfer since the passages are of relatively smaller cross section. The form shown in FIGURE 3 is particularly useful for supplying or removing heat of a chemical reaction.

FIGURES 5, 6 and 7 illustrate typical temperature relations between two gases in different recuperative heat exchange systems Where no exothermic or endothermic reaction occurs. In a conventional countercurrent system shown in FIGURE 5 both gases have a decreasing temperature gradient from the hot gas inlet to the hot gas outlet. In a conventional cocurrent system shown in FIGURE 6 the hot gas has a decreasing temperature gradient from its inlet to its outlet, while the cooler gas has an increasing gradient. In a fluidized bed system shown in FIGURE 7 there is virtually no temperature gradient except immediately adjacent the inlet. This absence of temperature gradient has several important advantages. Thermal stresses are virtually eliminated, since all parts of the apparatus are at the same temperature, thereby simplifying mechanical design, increasing equipment life and cutting maintenance costs. Throughout the apparatus there is a uniform rate of heat transfer, the coefiicient of which usually varies with the temperature. Uniform temperature overcomes any localized overheating.

While I have shown and described certain preferred embodiments of my invention, it is apparent that other modifications may arise. Therefore, I do not wish to be limited to the disclosure set forth but only by the scope of the appended claims.

I claim:

1. A recuperator comprising an insulated outer wall defining a first passage, a heat conductive inner wall spaced within said outer wall defining a second passage surrounded by said first passage in heat exchange relation thereto, both said passages having a minimum horizontal dimension of about 4 inches, perforate members extending across each of said passages adjacent the bottoms thereof, beds of finely divided thermophore of a uniformly distributed particle size approximately between 10 mesh and 100 mesh and adapted for fluidization and vertical back mixing in each of said passages supported on said members, said beds having a minimum depth of about 3 feet, gas inlets to the bottoms of said passages below said members for introducing upwardly flowing cocurrent streams of gases to said beds to fiuidize them and to transfer heat from one gas to the other through said inner wall, gas outlets from said passages above said beds, and means positively confining said thermophore to the respective passages.

2. A recuperative methodiof exchanging heat between two gases comprising passing a stream of the gas whose temperature is nearer that of the surrounding atmosphere in an upward direction at a superficial velocity of 0.5 to 2 feet per second through a first bed of finely divided solids chemically inert to this gas and of a uniformly distributed particle size approximately between 10 mesh and mesh and thus effecting fiuidization and vertical back mixing of the first bed, simultaneously passing a stream of the gas whose temperature is farther from that of the surrounding atmosphere in an upward direction at a superficial velocity ofv 0.5 to 2 feet per second cocurrent to the first gas through a second bed of finely divided solids chemically inert to the second gas and of a uniformly distributed particle size approximately between 10 mesh and 100 mesh and thus effecting fiuidization and vertical back mixing of the second bed, and positively confining the solids in both beds to their original passages out of contact with each other, said first bed surrounding said second bed in heat exchange relation to eifect transfer of heat therebetween, the vertical back mixing minimizing the temperature gradient within each bed.

References Cited in the file of this patent UNITED STATES PATENTS 1,716,333 Vuilleumier June 4, 1929 2,520,637 Henwood Aug. 29, 1950 2,698,171 Schoenmakers et al. Dec. 28, 1954 2,779,716 Neuman Jan. 29, 1957 2,858,110 Blaskowski Oct. 28, 1958

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US1716333 *Oct 14, 1916Jun 4, 1929Safety Car Heating & LightingHeat-exchange apparatus
US2520637 *Oct 10, 1946Aug 29, 1950Selas Corp Of AmericaApparatus for heat-treating granular materials
US2698171 *Jul 30, 1952Dec 28, 1954Shell DevHeat transfer method and apparatus using segregated upwardly and downwardly flowing fluidized solids
US2779716 *Nov 28, 1952Jan 29, 1957Houdry Process CorpMethod and apparatus for contacting fluids with solids
US2858110 *Aug 4, 1955Oct 28, 1958Combustion EngRegenerative heat exchanger
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US3203470 *Jul 1, 1963Aug 31, 1965British Aluminium Co LtdMethod of rapidly cooling solid bodies
US3512577 *Dec 11, 1968May 19, 1970Alfa Laval AbMethod and apparatus for intergas heat exchange
US3621905 *Feb 3, 1970Nov 23, 1971Nordstjernan Rederi AbMethod of improving the heat transport in a tube of an evaporator or other cooking apparatus
US3889042 *Dec 10, 1973Jun 10, 1975Allied ChemMethod and apparatus for cooling and insulating electrical equipment
US3922147 *Apr 5, 1974Nov 25, 1975Lummus CoHydrolysis reactor
US3933195 *Mar 13, 1972Jan 20, 1976St Clair John CLiquid-liquid heat exchanger made of plastic sheets imbedded in mass of pebbles
US4066430 *Nov 26, 1976Jan 3, 1978Ppg Industries, Inc.Method of tempering in a fluidized quenching medium
US4149586 *Feb 21, 1978Apr 17, 1979The Governing Council Of The University Of TorontoHeat transfer process and apparatus
US4245693 *Oct 11, 1978Jan 20, 1981Phillips Petroleum CompanyWaste heat recovery
US4372774 *Jul 21, 1981Feb 8, 1983Pilkington Brothers LimitedThermal treatment of glass
US4400193 *Oct 19, 1979Aug 23, 1983Pilkington Brothers LimitedMethod of thermal toughening of glass in a fluidized bed
US4585051 *Dec 6, 1983Apr 29, 1986University Of QueenslandHeat exchange between solids
US4865122 *May 16, 1988Sep 12, 1989Iowa State University Research Foundation, Inc.Aggregatively fluidized liquid heat exchanger
US20130025836 *Aug 3, 2012Jan 31, 2013Renewability Energy Inc.Helical coil-on-tube heat exchanger
DE2456321A1 *Nov 28, 1974Jun 12, 1975Pieper Gustav AdolfVerfahren zum waermeaustausch und waermetauscher
DE2559885C2 *Jul 21, 1975Nov 10, 1983Emhart (U.K.) Ltd., Wheatley Doncaster, Yorkshire, GbTitle not available
EP0144324A1 *Dec 6, 1983Jun 19, 1985University Of QueenslandHeat exchange between gas-solids mixtures
EP0144324A4 *Dec 6, 1983Dec 2, 1985Univ QueenslandHeat exchange between gas-solids mixtures.
Classifications
U.S. Classification165/104.16, 422/146, 165/174
International ClassificationB01J8/18, F28D13/00
Cooperative ClassificationB01J2208/00132, B01J8/1836, B01J2208/00513, F28D13/00, B01J2208/00495
European ClassificationB01J8/18H, F28D13/00