US3749155A - Exchange process - Google Patents

Exchange process Download PDF

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Publication number
US3749155A
US3749155A US00162047A US3749155DA US3749155A US 3749155 A US3749155 A US 3749155A US 00162047 A US00162047 A US 00162047A US 3749155D A US3749155D A US 3749155DA US 3749155 A US3749155 A US 3749155A
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US
United States
Prior art keywords
fluid
cold
exchanger
exchange
vaporization
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US00162047A
Inventor
J Buffiere
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GEORGES CLAUDE SA
SA Georges Claude fr
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GEORGES CLAUDE SA
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Priority to FR7026212A priority Critical patent/FR2096919B1/fr
Application filed by GEORGES CLAUDE SA filed Critical GEORGES CLAUDE SA
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Publication of US3749155A publication Critical patent/US3749155A/en
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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28FDETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/06Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
    • F28F13/08Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media by varying the cross-section of the flow channels
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J5/00Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28DHEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D3/00Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium flows in a continuous film, or trickles freely, over the conduits
    • F28D3/02Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium flows in a continuous film, or trickles freely, over the conduits with tubular conduits
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28FDETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F1/00Tubular elements; Assemblies of tubular elements
    • F28F1/10Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
    • F28F1/12Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element
    • F28F1/14Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element and extending longitudinally
    • F28F1/16Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element and extending longitudinally the means being integral with the element, e.g. formed by extrusion
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28FDETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F1/00Tubular elements; Assemblies of tubular elements
    • F28F1/10Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
    • F28F1/42Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being both outside and inside the tubular element
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28FDETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F1/00Tubular elements; Assemblies of tubular elements
    • F28F1/10Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
    • F28F1/42Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being both outside and inside the tubular element
    • F28F1/422Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being both outside and inside the tubular element with outside means integral with the tubular element and inside means integral with the tubular element
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28FDETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/06Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28FDETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/14Arrangements for modifying heat-transfer, e.g. increasing, decreasing by endowing the walls of conduits with zones of different degrees of conduction of heat
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28DHEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0061Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications
    • F28D2021/0064Vaporizers, e.g. evaporators

Abstract

An exchange process between a fluid which is to be heated and/or vaporized and circulating in a chamber, and an externally circulating liquid heating agent, in which the said chamber comprises means so that the speed of the fluid in the hot exchange zone is higher than that of the fluid in the cold zone. These means consist of a mandrel, of which the diameter becomes greater as the hot end is approached and is possibly formed of several sections of increasing diameters.

Description

.5 Sheets-Sheet 1 Patented July 31, 1973 3 Sheets-Sheet 2 \SQQQ Patented July 31, 1973 3 Sheets-Sheet 5 known type, the fluid to be treated, i.e., to be heated and/or vaporized, circulates from bottom to top in vertical tubes which are cooled externally by water which is flowing by gravity.

It was found that, by providing the vertical tubes with longitudinal external fins, it was possible to obtain a continuous flow of the water along the tube without any detachment of the water film, and thus to obtain a better exchange between the fluid to be treated, i.e., to be heated and/or vaporized and the stream of heating water.

In fact, in the construction of these heat exchangers, it is necessary to yield to the two following needs firstly, of not withdrawing from inside the tube more cold units than the wall is capable of evacuating therefrom on the water side without excessive formation of ice, and secondly to supply the cold units as uniformly as possible at all points of the internal wall of the tube, so as to utilize to the best possible the exchange surface, and to control the dangers of ice formation.

The finned heat exchangers of known type make possible a uniform supply of the cold units and, in order to permit the evacuation of the cold units in accordance with the first of the two needs previously referred to, must have the largest possible exchange surface on the water side. Actually, the known arrangements either require excessive tube lengths or too large a number of parallel tubes, which has particularly the disadvantage of making the cost of the conventional exchangers relatively high.

The present invention has for its object an improvement in the exchange processes between a fluid to be heated and/or vaporized, which permits the disadvantages of the known processes to be overcome.

Within the scope of the present specification and the claims defining the extent of the protection applied for, there is understood by fluid to be treated both the heating and vaporization and possibly the superheating of a fluid.

The present invention has for its object an exchange process between a fluid to be treated, i.e., to be heated and/or vaporized, circulating in a chamber, on the one hand, and an externally circulating liquid heating agent, on the other hand, in which means are provided in the said chamber so that the speed of the fluid in the hot exchange zone is higher than that of the fluid in the cold zone.

It is thus possible firstly to control the ice formation in the cold exchange zone and secondly to reduce to a reasonable height the height necessary for the vaporization in the hot exchange zone.

According to one embodiment of the invention, the said means consist at least of one mandrel, of which the diameter is larger as the hot zone is approached, which mandrel has a regularly increasing section or may be formed of several sections of increasing diameters.

According to another embodiment of the invention, the said mandrel is in addition associated with a variable pitch helix, of which the pitch is larger in the cold zone than in the hot exchange zone.

According to yet another embodiment of the invention, the said means consist in the cold zone of an insulating internal lining and in the hot zone of fins fixed to the said chamber.

Other objects and advantages of the present invention will be apparent from reading the following specification and the non-limitative embodiments'which are described and illustrated.

FIG; 1 is a diagrammatic longitudinal section showing one embodiment of an exchanger for carrying out the process according to the present invention.

FIG. 2 is a diagrammatic longitudinal section of another embodiment of an exchanger according to the invention.

FIG. 3 is a section along the line III-Ill of FIG. 2.

FIG. 4 is another embodiment of an exchanger permitting the process according to the invention to be carried out.

The exchanger 1 according to FIG. 1 comprises a central mandrel 2 which has a diameter which is larger as the hot zone or the hot end of the exchanger is approached this central mandrel comprises in fact four sections 4, 5, 6 and 7, respectively, of increasing diameters.

FIG. 2 shows an exchanger 1 which, according to a modification of the invention, is provided with internal fins 3 which in particular permit the exchange surface at the hot end to be increased,

It is thus possible to cause the ratio between the exchange surface on the water side and the exchange surface on the fluid side to vary from 2 to 4. These internal fins 3 can be seen more particularly in FIG. 3. According to another modification, the exchanger 1 can comprise external fins 9 designed to assist the heat exchanges. The choice of the number of fins is determined as a function of the problems connected with the surface treatment of the metal being used, and designed to avoid the corrosion caused by the possible use of sea water or corrosive industrial water. The protection of the metal is generally assured by metallization, preferably by zinc-spraying, although the use of a plastic material may be justified.

The central core 2 can be formed by the assembly of tubes of variable diameter and is attached at its lower part 10.

According to the embodiment shown in FIG. 4, the mandrel 2 can be formed of a mandrel which has a section increasing regularly from the hot end to the cold end.

The operation of the arrangements as illustrated is as follows The fluid to be treated, i.e., to be heated and/or vaporized circulates with an ascending movement inside the exchanger I, in the space contained between the internal wall of this exchanger and the mandrel 2. This fluid is heated and/or vaporized by thermal exchange with a liquid heating agent, in this case water, which is circulating by gravity along the external wall of the exchanger The longitudinal external fins 9 with which the exchanger is equipped permit of obtaining a continuous flow of water along the exchanger and of avoiding the detachment of the water film. It is thus possible to obtain a better exchange between the fluid to be treated and the stream of heating water. By means of the internal fins 3, this exchange is further improved.

It is convenient to point out that the speed of circulation of the treated fluid, if it remains in the liquid state and is not subjected to vaporization, would normally be increased in passing to the hot end from the cold end, because of the decrease-in the passage section provided between the internal wall of the exchanger and the mandrel in passing from the cold end to the hot end.

In fact, the fluid thus treated experiences a vaporization and its volume is considerably increased, and this causes a considerable acceleration in the speed of travel of the fluid, in passing from the cold end to the hot end. It is thus possible to overcome all the disadvantages of the known processes and particularly to prevent the formation of too large a quantity of ice around the exchanger 1.

Obviously, the distributors for the externally circulating liquid heating agent and the cold fluid, as well as the headers designed to collect the vaporized or heated fluid at the top of the exchangers, and the trickling water which has served for the vaporization fluid at the bottom of the exchanger, have not been illustrated solely for the purpose of simplification, and it is obvious that it is possible to use any means whatsoever which permit these objects to be achieved.

The following examples are given simply by way of illustration and have no limiting character. They were carried out in an exchanger such as defined above, the heating agent being water at 14 C and the fluid being heated or vaporized being up to C.

Example 1 Vaporization of liquid methane at 75 bars.

The central core 2 is formed of four successive sections, 4, 5, 6 and 7 (FIG. 1) with diameters of respectively 25, 36, 45 and 48 mm over lengths which are respectively equal to l m, lm, 1.50 m,'and 2 in.

Under these conditions, the quantity of heat change per tube is 70,000 Kcal/h.

Example 2 Vaporization of liquid ethylene at 40 bars.

The core is formed of two successive sections of 45 mm and 48 mm, over respective lengths of 1.50 m and 4 m.

Under these conditions, the quantity of heat exchanged per tube is about 50,000 Kcal/h.

Example 3 Vaporization of liquid ethylene at 20 bars.

The same installation is used as in the case of Example 2.

Under these conditions, the quantity of changed per tube is 25,000 Kcal/h.

Example 4 Vaporization of liquid nitrogen at 40 bars.

The core is formed of three successive sections, with diameters equal to 48, 45 and 35 mm, respectively, over heights of 1.50 m, 0.50 m and 3.50 in.

Under these conditions, the quantity of heat exchanged per tube is 50,000 Kcal/h.

Example 5 Vaporization of liquid nitrogen at 20 bars.

The same installation is used as in the case of Example 4.

Under these conditions, the quantity of heat exchanged per tube is 30,000 Kcal/h.

it is obvious that the invention is not limited to the embodiments described and illustrated and it is capable of numerous other variants available to the person skilled in the art, depending on the proposed applications and without thereby departing from the scope of the invention.

What I claim is: l. A method for vaporizing a liquefied gas comprising:

flowing a cold stream of the liquefied gas inside a vertical vaporization tube in an ascending direction;

flowing a warm film of a heating liquid by gravity outside said vaporization tube, on the external surface thereof, in a descending direction, whereby there is heat exchanged between said cold stream and said warm film; and

gradually increasing the speed of said cold stream as it ascends from the cold end to the warm end of said vaporization tube.

heat ex-

Claims (1)

1. A method for vaporizing a liquefied gas comprising: flowing a cold stream of the liquefied gas inside a vertical vaporization tube in an ascending direction; flowing a warm film of a heating liquid by gravity outside said vaporization tube, on the external surface thereof, in a descending direction, whereby there is heat exchanged between said cold stream and said warm film; and gradually increasing the speed of said cold stream as it ascends from the cold end to the warm end of said vaporization tube.
US00162047A 1970-07-16 1971-07-13 Exchange process Expired - Lifetime US3749155A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
FR7026212A FR2096919B1 (en) 1970-07-16 1970-07-16

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US3749155A true US3749155A (en) 1973-07-31

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US00162047A Expired - Lifetime US3749155A (en) 1970-07-16 1971-07-13 Exchange process

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US (1) US3749155A (en)
JP (1) JPS5627793B1 (en)
CA (1) CA941816A (en)
ES (1) ES393297A1 (en)
FR (1) FR2096919B1 (en)
GB (1) GB1361421A (en)

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5096942A (en) * 1973-12-24 1975-08-01
EP0002687A1 (en) * 1977-12-24 1979-07-11 Küppersbusch Aktiengesellschaft Apparatus using heat exchange
US4186798A (en) * 1978-01-27 1980-02-05 Gritsuk Lev D Tubular cooled members of metallurgical furnace
WO1984002392A1 (en) * 1982-12-15 1984-06-21 Svante Thunberg Ventilation plant
US4470709A (en) * 1980-03-04 1984-09-11 Ford Aerospace & Communications Corporation Cylindrical tapered sleeve optimized for weight and heat conduction
EP0167161A2 (en) * 1984-07-05 1986-01-08 Apd Cryogenics Inc. Parallel wrapped tube heat exchanger
US5454429A (en) * 1992-05-23 1995-10-03 Neurauter; Peter Rods and mandrel turbulators for heat exchanger
WO1999031452A1 (en) 1997-12-16 1999-06-24 York International Corporation Counterflow evaporator for refrigerants
NL1018672C2 (en) * 2001-07-31 2003-02-06 Stichting Energie System for stripping and rectifying a fluid mixture.
US6681764B1 (en) * 1997-06-16 2004-01-27 Sequal Technologies, Inc. Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator
US20070022754A1 (en) * 2003-12-16 2007-02-01 Active Power, Inc. Thermal storage unit and methods for using the same to head a fluid
US20090308100A1 (en) * 2005-04-28 2009-12-17 Erik Jensen Rectification apparatus using a heat pump
DE102008028728A1 (en) 2008-06-17 2009-12-24 Bayerische Motoren Werke Aktiengesellschaft Heat exchanger for heating cryogenic fluid by particularly flowing heat transfer medium, has design of flow cross section in colder channel-area
DE102008028731A1 (en) 2008-06-17 2009-12-24 Bayerische Motoren Werke Aktiengesellschaft Heat exchanger for heating low cold hydrogen for drive equipment of motor vehicle, has channel for running parallel to other set of channels, where hydrogen is made to flow through former channel when medium possesses higher temperature
DE102008028724A1 (en) 2008-06-17 2009-12-24 Bayerische Motoren Werke Aktiengesellschaft Heat exchanger for heating cryogenic fluid by particularly flowing heat transfer, has channel, in which fluid reaches, where channel is arranged in solid matter block
USRE43398E1 (en) * 1997-06-16 2012-05-22 Respironics, Inc. Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator
US20160245598A1 (en) * 2013-10-02 2016-08-25 Intergas Heating Assets B.V. Tube for a heat exchanger with an at least partially variable cross-section, and heat exchanger equipped therewith
CN107191958A (en) * 2017-05-11 2017-09-22 中国北方车辆研究所 A kind of burner exhaust heat of heat exchange structure length change utilizes heat-exchanger rig
CN107270747A (en) * 2017-05-11 2017-10-20 中国北方车辆研究所 A kind of burner exhaust heat of heat exchange structure spacing change utilizes heat-exchanger rig

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2422126B1 (en) * 1978-04-04 1980-10-17 Inst Ochistke Tekhnolog Gazo
DE3005751A1 (en) * 1980-02-15 1981-08-20 Schmitz Kuehler Baierbrunn Method and device for increasing the heating output of evaporators
FR2477276B1 (en) * 1980-02-29 1982-07-30 Air Liquide
FR2491202B1 (en) * 1980-10-01 1986-02-28 Air Liquide Atmospheric heater
PL422945A1 (en) * 2017-09-22 2019-03-25 Normax-Invest Spółka Z Ograniczoną Odpowiedzialnością Method for limiting of the cooling liquid quantity, preferably the liquid that is subject to phase transitions in the tubular heat exchangers, and the deflector for execution of this method

Cited By (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5096942A (en) * 1973-12-24 1975-08-01
EP0002687A1 (en) * 1977-12-24 1979-07-11 Küppersbusch Aktiengesellschaft Apparatus using heat exchange
US4186798A (en) * 1978-01-27 1980-02-05 Gritsuk Lev D Tubular cooled members of metallurgical furnace
US4470709A (en) * 1980-03-04 1984-09-11 Ford Aerospace & Communications Corporation Cylindrical tapered sleeve optimized for weight and heat conduction
WO1984002392A1 (en) * 1982-12-15 1984-06-21 Svante Thunberg Ventilation plant
US4567943A (en) * 1984-07-05 1986-02-04 Air Products And Chemicals, Inc. Parallel wrapped tube heat exchanger
EP0167161A2 (en) * 1984-07-05 1986-01-08 Apd Cryogenics Inc. Parallel wrapped tube heat exchanger
EP0167161A3 (en) * 1984-07-05 1987-07-15 Air Products And Chemicals, Inc. Parallel wrapped tube heat exchanger
US5454429A (en) * 1992-05-23 1995-10-03 Neurauter; Peter Rods and mandrel turbulators for heat exchanger
US6681764B1 (en) * 1997-06-16 2004-01-27 Sequal Technologies, Inc. Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator
USRE43398E1 (en) * 1997-06-16 2012-05-22 Respironics, Inc. Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator
US6698423B1 (en) * 1997-06-16 2004-03-02 Sequal Technologies, Inc. Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator
WO1999031452A1 (en) 1997-12-16 1999-06-24 York International Corporation Counterflow evaporator for refrigerants
US6530421B1 (en) 1997-12-16 2003-03-11 York International Corporation Counterflow evaporator for refrigerants
US6092589A (en) * 1997-12-16 2000-07-25 York International Corporation Counterflow evaporator for refrigerants
NL1018672C2 (en) * 2001-07-31 2003-02-06 Stichting Energie System for stripping and rectifying a fluid mixture.
US20040200602A1 (en) * 2001-07-31 2004-10-14 Hugill James Anthony System for stripping and rectifying a fluid mixture
US7111673B2 (en) 2001-07-31 2006-09-26 Stichting Energieonderzoek Centrum Nederland System for stripping and rectifying a fluid mixture
WO2003011418A1 (en) * 2001-07-31 2003-02-13 Stichting Energieonderzoek Centrum Nederland System for stripping and rectifying a fluid mixture
US20070022754A1 (en) * 2003-12-16 2007-02-01 Active Power, Inc. Thermal storage unit and methods for using the same to head a fluid
US20090308100A1 (en) * 2005-04-28 2009-12-17 Erik Jensen Rectification apparatus using a heat pump
US7972423B2 (en) * 2005-04-28 2011-07-05 Holm Christensen Biosystemer Aps Rectification apparatus using a heat pump
DE102008028728A1 (en) 2008-06-17 2009-12-24 Bayerische Motoren Werke Aktiengesellschaft Heat exchanger for heating cryogenic fluid by particularly flowing heat transfer medium, has design of flow cross section in colder channel-area
DE102008028724A1 (en) 2008-06-17 2009-12-24 Bayerische Motoren Werke Aktiengesellschaft Heat exchanger for heating cryogenic fluid by particularly flowing heat transfer, has channel, in which fluid reaches, where channel is arranged in solid matter block
DE102008028731A1 (en) 2008-06-17 2009-12-24 Bayerische Motoren Werke Aktiengesellschaft Heat exchanger for heating low cold hydrogen for drive equipment of motor vehicle, has channel for running parallel to other set of channels, where hydrogen is made to flow through former channel when medium possesses higher temperature
DE102008028731B4 (en) * 2008-06-17 2020-01-30 Bayerische Motoren Werke Aktiengesellschaft Heat exchanger for heating cryogenic hydrogen taken from cryogenic tanks
US20160245598A1 (en) * 2013-10-02 2016-08-25 Intergas Heating Assets B.V. Tube for a heat exchanger with an at least partially variable cross-section, and heat exchanger equipped therewith
CN107191958A (en) * 2017-05-11 2017-09-22 中国北方车辆研究所 A kind of burner exhaust heat of heat exchange structure length change utilizes heat-exchanger rig
CN107270747A (en) * 2017-05-11 2017-10-20 中国北方车辆研究所 A kind of burner exhaust heat of heat exchange structure spacing change utilizes heat-exchanger rig
CN107191958B (en) * 2017-05-11 2019-02-26 中国北方车辆研究所 A kind of burner exhaust heat of heat exchange structure length variation utilizes heat-exchanger rig
CN107270747B (en) * 2017-05-11 2019-03-15 中国北方车辆研究所 A kind of burner exhaust heat of heat exchange structure spacing variation utilizes heat-exchanger rig

Also Published As

Publication number Publication date
GB1361421A (en) 1974-07-24
CA941816A (en) 1974-02-12
FR2096919B1 (en) 1974-09-06
ES393297A1 (en) 1974-09-16
FR2096919A1 (en) 1972-03-03
JPS5627793B1 (en) 1981-06-26
CA941816A1 (en)

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