US3385268A - Method of operating a once-through vapor generator - Google Patents

Method of operating a once-through vapor generator Download PDF

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Publication number
US3385268A
US3385268A US42603565A US3385268A US 3385268 A US3385268 A US 3385268A US 42603565 A US42603565 A US 42603565A US 3385268 A US3385268 A US 3385268A
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vapor
tubes
fluid
once
operating
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Sprague Theodore Smith
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Babcock and Wilcox Co
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Babcock and Wilcox Co
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Priority to US42603565 priority Critical patent/US3385268A/en
Priority to DE19661526996 priority patent/DE1526996A1/de
Priority to FR46096A priority patent/FR1463672A/fr
Priority to SE58166A priority patent/SE315601B/xx
Priority to GB225066A priority patent/GB1090485A/en
Priority to NL6600647A priority patent/NL6600647A/xx
Priority to BE675283D priority patent/BE675283A/xx
Priority to US675538A priority patent/US3447509A/en
Application granted granted Critical
Publication of US3385268A publication Critical patent/US3385268A/en
Priority to NL7300178.A priority patent/NL161251C/xx
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/023—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers with heating tubes for nuclear reactors, as long as they are not classified according to a specified heating fluid, in another group
    • F22B1/026—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers with heating tubes for nuclear reactors, as long as they are not classified according to a specified heating fluid, in another group with vertical tubes between two horizontal tube sheets
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/08—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being steam

Definitions

  • Mass flow is defined as the amount of fluid passing through a specific planar area in a given period of time. It was long believed that high rates of mass flow were needed in once-through vapor generators to increase the quality at which nucleate boiling breaks down and to improve the film heat transfer coefficient at and above the point of departure from nucleate boiling.
  • nucleate boiling DNB
  • 'Nucleate boiling is characterized by the formation and release of vapor bubbles on the heat transmitting face of the heat transfer surface with the liquid still wetting the face, while in film boiling the heat transmitting face is coated with a film of vapor.
  • a temperature gradient is necessary to transfer heat from the transmitting face to the liquid. For a given set of operating conditions the magnitude of this gradient depends mainly on whether nucleate or film boiling is taking place.
  • the temperature of the heat absorbing surface is at a higher level than that resulting with nucleate boiling for the same mass flow conditions and the point at which nucleate boiling changes to film boiling is known as departure from nucleate boiling (DNB).
  • DDB departure from nucleate boiling
  • T o obtain maximum efficiency in a vapor generator, for example, a once-through type unit, it is important to maintain nucleate boiling over as wide a range of steam qualities as possible.
  • the optimum condition would be to maintain nucleate boiling during vapor generation from zero to 100 percent quality.
  • achieving such range is not always possible.
  • once-through boiler operation had to be carried out in a relatively high range of mass flow, that is above 600,000 'lbs./hr./ft. It had appeared that as a mass flow dropped off the DNB quality limit would also continue to decrease.
  • more recent research has indicated that a point exists where the DNB quality starts to increase with a further decrease in the mass 3,385,268 Patented May 28, 1968 flow. As a matter of fact, it appears that the DNB quality approaches percent for extremely low values of mass flow.
  • Another object of the invention is to incorporate superheating with such a method of once-through vapor generation.
  • a further object of the invention is to incorporate a method of preheating the secondary feedfluid so that it will be at substantially saturation temperature corresponding to secondary vapor pressure operating at the commencement of its passage in heat transfer relationship' with the primary heating fluid.
  • Still another object of the invention is to provide natural circulation induced flow of the vaporizable secondary fluid.
  • Yet another object of the invention is the utilization of a portion of the vapor generated to heat the feedfluid substantially to saturation temperature.
  • Another main object of the invention is the provision of vertically disposed tubular heat exchanger arranged to carry out the above method of once-through vapor generation.
  • a further object of the invention is to provide means for heating feedfluid in the heat exchanger in an integral section, separated from the vapor generating space. Further, the heat exchanger is arranged so that vapor may be removed from the vapor generating space and introduced into the separate feedfluid inlet space for heating the feedfluid to saturation temperature.
  • Yet another object of the invention is to provide a special baffle construction for assuring that the vapor which is generated flows a tortuous path through the superheating space of the heat exchanger.
  • the invention comprises a method of vaporizing and superheating a fluid by circulating it through a heat exchanger in indirect heat transfer relationship with a heating fluid at mass flow rates below 400,000 lbs./hr./ ft.
  • a heating fluid at mass flow rates below 400,000 lbs./hr./ ft.
  • the invention comprises a vertically elongated heat exchanger having a bundle of heat exchanger tubes extending between a pair of spaced tube sheets.
  • a cylindrically shaped shroud encloses the bundle of tubes for a substantial portion of its length, thereby providing a riser chamber about the tubes and an annular downcomer passage between the shroud and the heat exchanger shell. Openings are provided through the upper end of the shroud for admitting vapor, generated within the chamber, into the annular passageway wherein it mixes and heats the feedfluid by direct contact.
  • FIG. 1 is a veriical sectional view of a once-through vapor generator embodying the present invention
  • FIG. 2 is a plan View of the vapor generator shown in FIG. 1,
  • FIG. 3 is a transverse section taken along line 33 in FIG. 1,
  • FIG. 4 is another transverse section taken along line 44 in FIG. 1, and
  • FIG. 5 is a plot illustrating a typical relationship of mixture velocity and DNB quality for a given vapor pressure, heat flux and geometry.
  • FIG. 1 there is shown a once-through vapor generating and superheating unit comprising a vertically elongated cylindrically shaped pressure shell 12 closed at its opposite ends by an upper head member 14 and a lower head member 16.
  • a transversely arranged upper tube sheet 18 is integrally attached to the shell and upper head member 14 and forms in combination with the head member a fluid inlet chamber 20.
  • a fluid outlet chamber 24 is integrally attached to the shell and lower head member, forms in combination with the head member a fluid outlet chamber 24.
  • a bank of straight tubes 26 Vertically extending between the tube sheets 18 and 22 is a bank of straight tubes 26. Disposed about the tubes is a cylindrically shaped lower shroud 28 which extends from a plane closely spaced above the lower tube sheet to another plane spaced a considerable distance below the upper tube sheet. This lower shroud forms a riser chamber 30 including the bank of tubes and in combination with the shell 12 forms an annular shaped downcomer passageway 31. Closely spaced below the upper end of the lower shroud 28 and passing through it are a number of openings 32 which afford communication between the riser chamber 30 and the annular downcomer passageway 31. The upper end of the annular passageway is sealed by an annular plate 34 welded about its outer edge to the shell and around its inner edge to the shroud 28. Within the riser chamber a number of lattice type tube supports 38 are spaced along the length of the bank of tubes 26.
  • a cylindrically shaped upper shroud 40 Extending upwardly from the lower shroud to a plane located below the upper tube sheet is a cylindrically shaped upper shroud 40 which also encircles the bank of tubes 26. Transversely positioned within this upper shroud 40 are a number of vertically spaced disk and doughnut flow directing bafiles 42, 44A and 44B, respectively, see FIGS. 1, 3, and 4 for imparting a tortuous flow path to the fluid flowing about the tubes.
  • Support bars 46 anchored to and extending vertically upward from the lower tube sheet 22 through the tube bundle carry the disk and doughnut baflles.
  • the space within the upper shroud 40 and extending upwardly to the lower face of the upper tube sheet provides a superheating chamber 48.
  • the space between the upper shroud and the shell forms an outlet passageway 49 from which vapor outlets 50 extend for delivering superheated vapor to a point of use.
  • a pair of feedfluid inlets 52 extend through the shell 12 and are connected to a ring shaped feedfluid header 54 which circles the lower shroud 28 at its upper extremity.
  • header has a plurality of small openings 56 in its lower surface. Between the shell and shroud at spaced locations are a number of transversely arranged centering pins 58 for properly locating the shroud.
  • a nozzle 60 provides a fluid inlet to the chamber 20, see FIGS. 1 and 2, while in the lower head a nozzle 62 forms a fluid outlet from the chamber 24. Further, in the upper and lower heads respectively manways 64, 66 are provided for gaining admission to the chambers 20, 24.
  • the vapor generator 10 At its lower end the vapor generator 10 is supported by a skirt 68 which extends downwardly from the lower end of the shell 12 to a support pad 70.
  • the secondary coolant enters the heat exchanger through the inlets 52 flowing then into the feedfluid header 54. From the header the secondary coolant or feedfluid at a temperature somewhat below its saturation temperature corresponding to the operating pressure of the secondary system is uniformly distributed into the upper end of the annular passageway 31. Coincidentally vapor is drawn off from the riser chambers 30 through the openings 32 in the shroud 28. At substantially percent quality and upon passing through the space around the feedfluid header, it mixes with the atomized feedfluid. The vapor is condensed causing a slight reduction in pressure which provides an aspirating effect causing withdrawal of vapor from within the chamber 30 into the annular passageway 31.
  • the vapor gives up its latent heat of vaporization to the feedfluid with the mixture being heated substantially to saturation temperature.
  • the secondary fluid passes into riser chamber 30 and since it is at substantially saturation temperature vapor generation immediately commences.
  • the secondary coolant flows upwardly about the tubes and nucleate boiling is maintained as it passes in counter flow and indirect heat transfer relationship with the primary heating liquid within the tubes.
  • the low rate and temperature of the secondary coolant supplied to and flowing within the annular passageway is proportioned to assure natural or thermosyphonic circulation of the secondary coolant in its upward flow about the tubes 26.
  • vapor is generated ranging from zero quality at the lower tube sheet 22 to substantially 100 percent quality adjacent the upper end of the lower shroud 28. From this point that portion of the vapor which is to be superheated passes in a tortuous or sinuous path about the disk and doughnut balfies 42, 44A and 44B and is thus superheated in chamber 48 before it reverses direction about the upper shroud 40, flows downwardly into the outlet passageway 49 between the upper shroud and the shell and finally exits from the unit through the vapor outlet 50.
  • the primary coolant is preferably in a liquid state and typical operating parameters for both the primary and secondary coolants in such a unit as follows:
  • the DNB curve illustrates qualitatively a typical relationship between DNB quality and mixture velocity.
  • the zone D At the lower end of the mixture velocity scale between zero and approximately 3 feet per second is the zone D in which natural liberation and separation of steam from a body of water occurs in the course of vapor generating. This phenomenon is characterized as pot type boiling because of its similarity to boiling in a pot of water on a stove. As the pot is heated nucleation points develop and the steam bubbles break away from the surface of the pot to pass upwardly through the water, finally leaving the liquid. It will be noted that in this zone there is an upper DNB quality limit of 100 percent.
  • zone C extending roughly between velocities of from 3 to 12 ft./second and having a DNB quality limit of percent is the normal design range of operation for natural circulation boilers.
  • Natural circulation may be achieved by effective utilization of the force produced by differences in the density of the heated fluid mixture and the feedfluid supply. As heat is imparted to a fluid it becomes less dense than the fluid supply and it is this differential density phenomenon which, in properly proportioned downcomer and riser systems, promotes natural circulation of the fluid being heated.
  • a typical natural circulation boiler is disclosed in the Blazer et al. Patent No. 2,862,479 wherein the fluid to be heated flows first in an annular downcomer and then upwardly and is heated as it passes over the bank of shaped tubes.
  • the weight of the column of vaporizable fluid in the downcomer passageway is greater than the weight of steam-Water mixture Within the riser passageway because the mixture, upon being heated, becomes less dense, thereby providing a fluid density differential which promotes natural circulation flow through the unit.
  • natural circulation boilers have generally been designed for a mixture quality maximum of 20 percent by weight leaving the vapor generating section. Since the design exit quality is thus far below the limiting DNB quality of 100 percent from FIG. 5, zone C, it is apparent that for normal operating conditions of such units nucleate boiling exists throughout the entire vapor generating flow path.
  • zone A The upper portion of the plotted curve designated as zone A identifies the region of mixture velocity generally associated with forced flow, once-through boiler design.
  • units of this type employ a high temperature heat source so that high velocities and correspondingly high mass flows over or through the tubular conduits are required to avoid burnout.
  • the limiting DNB quality in this domain reduces rapidly, viz from 80 percent to 50 percent quality, for a corresponding mixture velocity reduction from 110 feet per second to 90 feet per second.
  • this distinctive characteristic would persist as the mixture velocity was further reduced and it was concluded that once-through vapor generators could not be designed for satisfactory operation below this relatively high mixture velocity.
  • the temperature of the primary coolant is relatively low and at the same time large quantities of it are available from the reactor.
  • a comparatively low pressure secondary coolant system By employing a comparatively low pressure secondary coolant system, with relatively low mass flows through the unit it is possible to achieve very high DNB quality provided the temperature of the heat source and heat flux are limited in accordance with the conditions previously discussed.
  • the change in temperature of the primary coolant as indicated previously in Table 1 is quite small, thereby limiting the deleterious effect of temperature differential within the unit and as a result limiting thermal stresses particularly on the tube walls in the region where DNB occurs.
  • the most important feature of this invention is the ability to maintain nucleate boiling throughout the entire range of vapor generation i.e., from zero to substantially percent quality.
  • the vaporizable fluid By properly coordinating the sizing of the unit and its geometric arrangement and by maintaining the operating conditions within established design limits it is possible to assure that the vaporizable fluid would be in a liquid state at substantially saturation temperature at its point of introduction into riser chamber 30 for flow about the tubes.
  • the vaporizable fluid In the heat exchanger construction shown in FIG. 1 the vaporizable fluid is transformed from a liquid at saturation temperature into a vaporous state in the course of its upward flow from the lower end of tube bank 26 to the upper portion of the tubes adjacent the upper end of the lower shroud 28.
  • the vaporizable fluid will exist as vapor at substantially 100 percent quality.
  • the rate of feedfluid supply to the unit will be equivalent to the amount of superheated vapor taken from the outlet 50, while the total flow rate in the downcomer passageway 31 will be the sum of the feedfluid and the saturated steam withdrawn from the chamber 30 through the openings 32.
  • this unit has been designated as a oncethrough unit utilizing natural circulation to effect fluid flow therethrough. It will also be observed that there is some degree of recirculation since a portion of the vapor generated is utilized to attain the saturation temperature of the feedfluid, which contributes to the uniqueness of this arrangement and the distinctive method of operation. Ordinarily, with natural circulation it is a liquid fraction of the heated fluid with is recirculated. In the present invention a portion of the vapor is Withdrawn for recirculation first in vaporous state and then as a liquid. In the Blazer et al.
  • the method of operating a once-through steam generator having a vessel occupied by a bank of tubes which comprises directing a heating fluid through the tubes, supplying a vaporizable feed fluid to the vessel at subcritical pressure and vaporizing the feed fluid by directing it over and along the tubes in indirect heat absorbing relation with the heating fluid at a mass flow less than 400,000 pounds per hour per square foot and at a velocity in the range of feet per second to 12 feet per second.
  • the method of operating a once-through steam generator having a vessel occupied by tubes which comprises directing a heating fluid through the tubes, supplying a vaporizable feed fluid to the vessel at subcritical pressure, successively vaporizing and superheating the feed fluid by directing it over and along the tubes in indirect heat absorbing relation with the heating fluid at a mass flow less than 400,000 pounds per hour per square foot and at a velocity in the range of 70 feet per second to 12 feet per second while being vaporized, and flowing most of the resulting superheated vapor to a point of use.
  • the method of operating a once-through steam generator having a vessel occupied 'by a bank of tubes which comprises directing a heating fluid through the tubes, supplying a vaporizable feed fluid to the vessel at subcritical pressure, vaporizing all the feed fluid by directing it over and along the tubes in indirect heat absorbing relation with the heating fluid at a mass flow less than 400,000 pounds per hour per square foot and at a velocity in the range of 70 feet per second to 12 feet per second, and superheating most of the resulting saturated vapor by directing it over and along the tubes, while passing the remainder of the saturated vapor into mixing relation with the feed fluid entering the vessel.
  • the method of operating a once-through steam generator having a vessel occupied by a bank of upright tubes which comprises directing a heating fluid through the tubes, supplying a vaporizable feed fluid to the vessel at subcritical pressure, vaporizing all the feed fluid by directing it over and along a portion of the length of the tubes in indirect heat absorbing relation with the heating fluid at a mass flow less than 400,000 pounds per hour per square foot and at a velocity in the range of 70 feet per second to 12 feet per second, and superheating most of the resulting saturated vapor by directing it over and along the remaining length of the tubes, while passing the remainder of the saturated vapor into mixing relation with the feed fluid entering the vessel.
  • the method of operating a once-through steam generator having a vessel occupied by a bank of straight vertical tubes which comprises directing a heating fluid through the tubes, supplying a vaporizable feed fluid to the vessel at subcritical pressure, vaporizing all the feed fluid by directing it over and along a portion of the length of the tubes in indirect heat absorbing relation with the heating fluid at a mass flow less than 400,000 pounds per hour per square foot and at a velocity in the range of 70 feet per second to 12 feet per second, and
  • the method of operating a once-through steam generator having a vessel occupied by a bank of straight vertical tubes which comprises directing a heating fluid through the tubes, supplying a vaporizable feed fluid to the vessel at subcritical pressure, vaporizing all the feed fluid by directing it over and along a portion of the length of the tubes in indirect heat absorbing relation with the heating fluid at a mass flow less than 400,000 pounds per hour per square foot and at a velocity in the range of 70 feet per second to 12 feet per second, and directing a part of the resulting saturated vapor into mixing relation with the feed fluid inflow to the vessel in a quantity sufficient to provide feed fluid at saturation temperature as it starts to flow over the tubes,
  • the method of operating a once-through steam generator having a vessel occupied by a bank of upright tubes which comprises directing a heating fluid through the tubes, supplying a vaporizable feed fluid to the vessel at subcritical pressure, vaporizing the feed fluid by directing it over and along a portion of the length of the tubes in counterflow indirect heat absorbing relation with the heating fluid at a mass flow less than 400,000 pounds per hour per square foot and at a velocity in the range of 70 feet per second to 12 feet per second, superheating most of the resulting saturated vapor by directing it over and along the remaining length of the tubes, and withdrawing a portion of the feed fluid at a point in the course of its passage along the tubes and delivering it in mixing relation with the feed fluid entering the vessel.
  • the method of operating a once-through steam generator having a vessel occupied by a bank of upright tubes which comprises directing a heating fluid through the tubes, supplying a vaporizable feed fluid to the vessel at subcritical pressure, vaporizing the feed fluid by directing it over and along a portion of the length of the tubes in counterflow indirect heat absorbing relation with the heating fluid at a mass flow in the range of 100,000 to 300,000 pounds per hour per square foot and at a velocity in the range of 70 feet per second to 12 feet per second, superheating most of the resulting vapor by directing it over and along the remaining length of the tubes, and withdrawing a portion of the feed fluid at a point in the course of its passage along the tubes and delivering it in mixing relation with the feed fluid entering the vessel.
  • the method of operating a once-through steam generator having a vessel occupied by a bank of straight vertical tubes which comprises directing a low temperature subcritical pressure heating fluid through the tubes, supplying a subcooled vaporizable feed fluid to the vessel at subcritical pressure, vaporizing the fed fluid by directing it over and along a portion of the length of the tubes in indirect counterflow heat absorbing relation with the heating fluid at a mass flow less than 400,000 pounds per hour per square foot and at a velocity in the range of 70 feet per second to 12 feet per second, superheating most of the resulting vapor by directing it over and along the remaining length of the tubes, and withdrawing a portion of the feed fluid at a point in the course of its passage along the tubes and delivering it in mixing relation with the feed fluid entering the vessel.
  • the method of operating a once-through steam generator having a vessel divided by tube sheets into heating fluid inflow and outflow compartments and a tube bank compartment, and a bank of straight vertical tubes in the tube bank compartment connected to the tube sheets, said method comprising directing a heating fluid to the inflow compartment through the tubes to the outflow compartment, supplying a vaporizable feed fluid to the bank compartment, vaporizing the feed fluid directing it over and along a portion of the length of the tubes in indirect heat absorbing relation with the heating fluid at a mass flow in the range of 100,000 to 300,000 pounds per hour per square foot and at a velocity in the range of 70 feet per second to 12 feet per second, and superheating most of the resulting saturated vapor by directing it through a tortuous path over and along the remaining length of the tubes, while passing the remainder of the saturated vapor into mixing relation with the feed fluid entering the vessel.

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US42603565 1965-01-18 1965-01-18 Method of operating a once-through vapor generator Expired - Lifetime US3385268A (en)

Priority Applications (9)

Application Number Priority Date Filing Date Title
US42603565 US3385268A (en) 1965-01-18 1965-01-18 Method of operating a once-through vapor generator
DE19661526996 DE1526996A1 (de) 1965-01-18 1966-01-15 Verfahren zum Betreiben eines Waermeaustauschers und Ausfuehrung desselben
SE58166A SE315601B (OSRAM) 1965-01-18 1966-01-17
FR46096A FR1463672A (fr) 1965-01-18 1966-01-17 Perfectionnements aux procédés et aux installations de production de vapeur
GB225066A GB1090485A (en) 1965-01-18 1966-01-18 Improvements in or relating to a method of and apparatus for generating vapour
NL6600647A NL6600647A (OSRAM) 1965-01-18 1966-01-18
BE675283D BE675283A (OSRAM) 1965-01-18 1966-01-18
US675538A US3447509A (en) 1965-01-18 1967-10-16 Once-through vapor generator
NL7300178.A NL161251C (nl) 1965-01-18 1973-01-05 Warmtewisselaar.

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US42603565 US3385268A (en) 1965-01-18 1965-01-18 Method of operating a once-through vapor generator

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US3385268A true US3385268A (en) 1968-05-28

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US (1) US3385268A (OSRAM)
BE (1) BE675283A (OSRAM)
DE (1) DE1526996A1 (OSRAM)
FR (1) FR1463672A (OSRAM)
GB (1) GB1090485A (OSRAM)
NL (1) NL6600647A (OSRAM)
SE (1) SE315601B (OSRAM)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3576178A (en) * 1969-12-24 1971-04-27 Combustion Eng Shell-and-tube steam generator with economizer
US3661123A (en) * 1970-12-31 1972-05-09 Combustion Eng Steam generator feedwater preheater
US3724532A (en) * 1970-03-02 1973-04-03 Babcock & Wilcox Co Once-through vapor generator
JPS5134521B1 (OSRAM) * 1970-11-20 1976-09-27
US4312303A (en) * 1979-09-25 1982-01-26 Westinghouse Electric Corp. Recirculating steam generator with super heat
US4422899A (en) * 1980-01-24 1983-12-27 Rintekno Oy Apparatus and method for the vaporization of liquid
US20070187079A1 (en) * 2006-01-31 2007-08-16 Sang Baek Shin Baffle structure improving heat transfer efficiency of reactor or heat exchanger
CN104613452A (zh) * 2014-12-18 2015-05-13 方萌 一种大排量蒸汽供应设备

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3635287A (en) * 1970-03-02 1972-01-18 Babcock & Wilcox Co Once-through vapor generator
US3653363A (en) * 1970-12-10 1972-04-04 Combustion Eng Downcomer flow control
GB1524815A (en) * 1974-08-23 1978-09-13 Babcock & Wilcox Ltd Heat exchangers
SE430716B (sv) * 1982-04-22 1983-12-05 Stal Laval Apparat Ab Mellanoverhettare

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB536592A (en) * 1939-11-18 1941-05-20 Ervin George Bailey Improvements in or relating to tubulous vapour generators
US2336832A (en) * 1941-11-01 1943-12-14 Badenhausen John Phillips Steam generator
FR1140383A (fr) * 1954-10-09 1957-07-19 Tno Procédé de transfert de chaleur à un liquide
US2862479A (en) * 1956-04-06 1958-12-02 Babcock & Wilcox Co Vapor generating unit
US3076444A (en) * 1962-01-31 1963-02-05 Foster Wheeler Corp Vapor generators
US3088494A (en) * 1959-12-28 1963-05-07 Babcock & Wilcox Co Ribbed vapor generating tubes
US3129697A (en) * 1959-01-14 1964-04-21 Trepaud Georges Heat exchanger and boiler, particularly to use the heat given off by nuclear reactors
US3179573A (en) * 1962-02-08 1965-04-20 Commissariat Energie Atomique Cell structure for heat exchanger
US3250258A (en) * 1964-06-29 1966-05-10 Foster Wheeler Corp Straight tubes in a vertical shell steam generator

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB536592A (en) * 1939-11-18 1941-05-20 Ervin George Bailey Improvements in or relating to tubulous vapour generators
US2336832A (en) * 1941-11-01 1943-12-14 Badenhausen John Phillips Steam generator
FR1140383A (fr) * 1954-10-09 1957-07-19 Tno Procédé de transfert de chaleur à un liquide
US2862479A (en) * 1956-04-06 1958-12-02 Babcock & Wilcox Co Vapor generating unit
US3129697A (en) * 1959-01-14 1964-04-21 Trepaud Georges Heat exchanger and boiler, particularly to use the heat given off by nuclear reactors
US3088494A (en) * 1959-12-28 1963-05-07 Babcock & Wilcox Co Ribbed vapor generating tubes
US3076444A (en) * 1962-01-31 1963-02-05 Foster Wheeler Corp Vapor generators
US3179573A (en) * 1962-02-08 1965-04-20 Commissariat Energie Atomique Cell structure for heat exchanger
US3250258A (en) * 1964-06-29 1966-05-10 Foster Wheeler Corp Straight tubes in a vertical shell steam generator

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3576178A (en) * 1969-12-24 1971-04-27 Combustion Eng Shell-and-tube steam generator with economizer
US3724532A (en) * 1970-03-02 1973-04-03 Babcock & Wilcox Co Once-through vapor generator
JPS5134521B1 (OSRAM) * 1970-11-20 1976-09-27
US3661123A (en) * 1970-12-31 1972-05-09 Combustion Eng Steam generator feedwater preheater
US4312303A (en) * 1979-09-25 1982-01-26 Westinghouse Electric Corp. Recirculating steam generator with super heat
US4422899A (en) * 1980-01-24 1983-12-27 Rintekno Oy Apparatus and method for the vaporization of liquid
US20070187079A1 (en) * 2006-01-31 2007-08-16 Sang Baek Shin Baffle structure improving heat transfer efficiency of reactor or heat exchanger
US8043583B2 (en) * 2006-01-31 2011-10-25 Lg Chem, Ltd. Baffle structure improving heat transfer efficiency of reactor or heat exchanger
CN104613452A (zh) * 2014-12-18 2015-05-13 方萌 一种大排量蒸汽供应设备

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BE675283A (OSRAM) 1966-05-16
DE1526996A1 (de) 1970-01-15
GB1090485A (en) 1967-11-08
FR1463672A (fr) 1966-12-23
SE315601B (OSRAM) 1969-10-06
NL6600647A (OSRAM) 1966-07-19

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Elgandelwar et al. Study of circulation ratio for natural circulation in water-tube boiler at different operating conditions.