US20160054064A1 - Gas slide heat exchanger - Google Patents

Gas slide heat exchanger Download PDF

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Publication number
US20160054064A1
US20160054064A1 US14/782,842 US201314782842A US2016054064A1 US 20160054064 A1 US20160054064 A1 US 20160054064A1 US 201314782842 A US201314782842 A US 201314782842A US 2016054064 A1 US2016054064 A1 US 2016054064A1
Authority
US
United States
Prior art keywords
pipe
heat exchanger
bulk material
nozzles
exchanger according
Prior art date
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.)
Abandoned
Application number
US14/782,842
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English (en)
Inventor
Dirk Lohrberg
Andreas Orth
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Outotec Finland Oy
Original Assignee
Outotec Finland Oy
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Outotec Finland Oy filed Critical Outotec Finland Oy
Assigned to OUTOTEC (FINLAND) OY reassignment OUTOTEC (FINLAND) OY ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ORTH, ANDREAS, LOHRBERG, DIRK
Publication of US20160054064A1 publication Critical patent/US20160054064A1/en
Abandoned legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
    • F28C3/00—Other direct-contact heat-exchange apparatus
    • F28C3/10—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material
    • F28C3/12—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material the heat-exchange medium being a particulate material and a gas, vapour, or liquid
    • F28C3/14—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material the heat-exchange medium being a particulate material and a gas, vapour, or liquid the particulate material moving by gravity, e.g. down a tube
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
    • F28C3/00—Other direct-contact heat-exchange apparatus
    • F28C3/10—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material
    • F28C3/12—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material the heat-exchange medium being a particulate material and a gas, vapour, or liquid
    • F28C3/16—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material the heat-exchange medium being a particulate material and a gas, vapour, or liquid the particulate material forming a bed, e.g. fluidised, on vibratory sieves
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D13/00—Heat-exchange apparatus using a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/0041—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for only one medium being tubes having parts touching each other or tubes assembled in panel form
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/10—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically
    • F28D7/106—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically consisting of two coaxial conduits or modules of two coaxial conduits

Definitions

  • the invention relates to a gas slide heat exchanger for treating bulk material comprising an elongated pipe having an inlet for introducing the bulk material at one end and an outlet for withdrawing the bulk material at the other end.
  • Such a heat exchanger comprises a stationary elongated housing having an inlet for the material to be treated at one end and an outlet at the other end as well as one or more screw rotors provided in the housing and extending along the length thereof.
  • the rotor comprises a central shaft and a worm gear provided on the outer surface of the shaft.
  • Within the shaft a conduit is provided which is connected to a steam supply.
  • the bulk material is introduced through the inlet into the housing and conveyed therethrough by the rotating movement of the screw conveyor. At the same time the bulk material is heated by the steam flowing in the central conduit of the shaft as well as by steam flowing in the double wall of the housing.
  • Another heat exchanger comprising a screw conveyor is known from document DE 534 988, wherein a heating or cooling medium flows through the hollow screw conveyor to heat or cool the bulk material transported through the housing.
  • Other screw conveying heat exchangers are known from documents DE 17 51 961 or DD 288 663 A5.
  • Document AT 507 100 B1 describes a process and apparatus for heat exchange wherein a bulk material is fluidized by introducing a fluidizing gas and wherein the bulk material is additionally agitated by a stirrer. Stirring arms are rotated between layers of heat exchange tubes provided in horizontal planes within the housing.
  • Document DE 10 2011 078 954 A1 describes another bulk heat exchange apparatus having a feed section, a heat exchanger section and a bulk material discharge section.
  • the bulk material feed section is divided by a bulk partition in a conveyor flow supply chamber and a counter flow supply chamber.
  • the bulk material partition continues to the bulk heat exchanger section. Thereby, a conveyor flow region and a counter flow region are formed of the heat exchanger section.
  • the heated particles After passing through the heat exchanging section, the heated particles are circulated within an upper chamber of the apparatus and fall back into an annular bed to be withdrawn.
  • This system also is quite complex and requires a specific regulation of the fluidization air.
  • fluidizing gas is injected via nozzles or membranes at the lower part of the gas slide.
  • the amount of injected gas is kept in a range that the bulk material is flowing but not expanding or circulating as it is desired for example in a fluidized bed cooler.
  • a heat exchanger comprising the features of claim 1 .
  • a plurality of heat exchange tubes extends along the longitudinal direction of the pipe, wherein a plurality of fluidization nozzles for introducing a fluidizing gas is provided at the bottom of the pipe.
  • the bulk material is fluidized and slowly flows along the elongated pipe.
  • heat is exchanged with the heat exchange medium flowing through the heat exchanging tubes.
  • the heat exchanger elements of the gas slide heat exchanger according to the present invention can be designed with a greater surface/volume ratio.
  • Multiple single heat exchange tubes can be integrated to a bundle with a much greater surface than the cylindrical surface of the screw shaft and the screw conveyor casing used in the prior art. Simultaneously, the heat exchange is promoted by the expanded surface of the bulk material fluidized by the fluidizing gas. This is not possible in the standard screw conveyor.
  • the fluidization nozzles are directed perpendicular to the conveying direction of the bulk material. Thereby, it is ensured that the bulk material is sufficiently fluidized when passing the nozzles.
  • Perfectdicular in the context of the present invention refers to an orientation of the fluidization nozzles within a range of 85 to 95°, in particular about 90°, relative to the major conveying direction of the bulk material along the pipe.
  • the pipe is tilted downwards in the conveying direction of the bulk material, preferably at an angle of 5 to 10 degrees or more preferably at an angle of 6 to 8 degrees.
  • the fluidized bulk material automatically flows down the pipe towards the outlet.
  • the pipe preferably comprises a double wall for receiving a heat exchange medium. Accordingly, heat is exchanged not only between the longitudinal heat exchange tubes within the fluidized material but also from the outer wall.
  • the pipe wall may be formed from a plurality of smaller pipes for receiving a heat exchange medium.
  • the heat exchange surface is increased.
  • a plurality of smaller pipes may be provided within the pipe for receiving the heat exchange medium.
  • transport nozzles which enter into the pipe at a location distanced from the bottom of the pipe to introduce additional transport gas.
  • the openings of the transport nozzles are located in a region extending between about 25 and 75% of the height of the pipe.
  • the transport nozzles are inclined downwards at an angle of 30 to 60°, preferably 40 to 50° and in particular about 45°.
  • the invention provides that the transport nozzles are inclined in the conveying direction of the bulk material in order to promote the conveyance of the material.
  • the transport nozzles are inclined at an angle of 30 to 60°, preferably 40 to 50° and in particular about 45°.
  • the fluidization and/or transport nozzles are located in respective rows along the longitudinal direction of the pipe, wherein preferably common supply pipes are provided for supplying fluidizing gas to each row of nozzles.
  • the flow rate of the fluidization and/or transport nozzles can be regulated, wherein preferably the fluidizing gas is injected through the transport nozzles with a low velocity in conveying direction to ensure just a proper bulk material flow.
  • the other part of the fluidizing gas can instead be injected perpendicular to the conveying direction through the fluidization nozzles with a comparatively higher velocity obtaining an expansion of the bulk material and hence a great material surface and improved heat exchange.
  • the heat exchange medium may be directed counter-currently or co-currently to the conveying direction of the bulk material depending on the specific needs of the process and material.
  • FIG. 1 is a cross section of a heat exchanger according to the present invention
  • FIG. 2 is a cross section of a first embodiment taken along line A-A in FIG. 1 ;
  • FIG. 3 is a cross section of the first embodiment of the invention wherein the heat exchange tubes are not shown, while the distribution of the bulk material within the pipe cross section is shown;
  • FIG. 4 is a cross section similar to FIG. 3 of a second embodiment of the invention taken along line A-A in FIG. 1 ;
  • FIG. 5 is a cross section similar to FIG. 3 of an alternative embodiment of the present invention taken along line A-A in FIG. 1 .
  • a gas slide heat exchanger 1 as shown in FIG. 1 includes a pipe 2 having an inlet 3 for introducing a bulk material at a first end, and an outlet 4 for withdrawing the bulk material at the other end of pipe 2 .
  • the pipe 2 is slightly downwards tilted at an angle of 6 to 8 degrees in the direction of the outlet 4 .
  • a plurality of heat exchange tubes 5 ( FIG. 2 ) extends along the longitudinal direction of pipe 2 .
  • a heating medium is introduced into the heat exchange tubes 5 via a supply port 6 and withdrawn through outlet port 7 at the other end of pipe 2 .
  • the wall 2 a of pipe 2 is designed as a double wall to receive additional heat exchange medium.
  • the heat exchanging medium preferably water, boiler feed water or thermo oil
  • the heat exchange medium can just as well be directed co-currently to the conveying direction of the bulk material in accordance with the specific requirements of the heat exchange process and the material to be treated.
  • a supply pipe 8 for fluidizing gas is provided below the pipe 2 .
  • a plurality of fluidization nozzles 9 extends in an upward direction towards pipe 2 .
  • the fluidization nozzles 9 enter the pipe 2 at its bottom 10 at approximately the center of the bottom region of pipe 2 .
  • supply pipes 11 , 12 extend along the major part of the length of pipe 2 and comprise transport nozzles 13 , 14 which enter into pipe 2 in a region located at 25 to 75%, in particular 30 to 40% of the height of pipe 2 .
  • the transport nozzles 13 , 14 are inclined downwards at an angle of approximately 45°:
  • the transport nozzles 13 , 14 further are inclined in the conveying direction of the bulk material at an angle of also about 45°.
  • the fluidization gas in particular air, that is introduced (continuously or as a pulsed stream) into the pipe 2 through the fluidization nozzles 9 and the transport nozzles 13 , 14 fluidizes the bulk material within pipe 2 and flows together with the bulk material along pipe 2 until it exits through a gas outlet 15 provided at the end of pipe 2 .
  • the heat exchanger according to the first embodiment of the present invention as shown in FIGS. 1 and 2 is basically constructed as described above. Next, its operation and advantages shall be described.
  • Bulk material such as ore fines, aluminium hydrate, ash or the like, is introduced into pipe 2 through inlet 3 .
  • the bulk material is fluidized within pipe 2 by fluidization gas introduced through the fluidization nozzles 9 and the transport nozzles 13 , 14 and flows along pipe 2 until it is withdrawn from pipe 2 through outlet 4 .
  • a part of the fluidizing gas is injected with a low velocity in conveying direction through the transport nozzles 13 , 14 , while the other part of the fluidizing gas is injected with a comparatively higher velocity through the fluidization nozzles 9 in a direction perpendicular to the conveying direction of the bulk material.
  • the bulk material is fluidized and expanded to obtain a great material surface and an improved heat exchange.
  • the velocities of the fluidizing gas introduced through the transport nozzles 13 , 14 and the fluidization nozzles 9 depend on the grain size and other properties of the bulk material. If the bulk material is fluidizable, the velocity of the fluidizing gas introduced through the fluidization nozzle 9 is typically smaller than 0.2 m/s (related to the longitudinal cross section) In case the bulk material is not fluidizable, e.g. because it is too fine or too heavy, and the transport mechanism is not based on gravity flow, the amount of fluidizing gas introduced through the transport nozzles 13 , 14 is higher than the amount of fluidizing gas introduced through nozzle 9 .
  • FIG. 3 The concept of the fluidization is illustrated in FIG. 3 wherein the bulk material is primarily transported in transport zone 20 while zone 21 indicates an area with enlarged material surface due to the expansion of the bulk material.
  • zone 21 indicates an area with enlarged material surface due to the expansion of the bulk material.
  • the heat exchanging tubes 5 are not illustrated in FIGS. 3 to 5 .
  • FIG. 4 shows an embodiment, wherein the transport nozzles 13 , 14 are arranged at a higher region of the pipe 2 so that an increased zone 21 with enlarged material surface is created.
  • a similar effect is achieved in the embodiment shown in FIG. 5 if some of the fluidization nozzles 9 a do not open at the bottom 10 of pipe 2 but extend into the upper region of the pipe 2 to create a zone 21 with enlarged material surface.
  • the transport nozzles 13 , 14 and the extended fluidization nozzles 9 a may be combined in a heat exchanger 1 .
  • the flow rate of the fluidization air supplied through fluidization nozzles 9 , 9 a and transport nozzles 13 , 14 can be regulated in order to provide for adequate fluidization and transport conditions of the bulk material within pipe 2 .
  • a gas slide heat exchanger according to the present invention is less complex to manufacture, provides a greater heat exchange surface at approximately same main dimensions and provides for an improved heat transfer due to an expanded bulk material surface.
  • the present invention is suitable for heating the bulk material by employing heated heat exchange media, but may also be used for cooling the bulk material with cold heat exchange media.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Nozzles (AREA)
US14/782,842 2013-04-10 2013-04-10 Gas slide heat exchanger Abandoned US20160054064A1 (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2013/057491 WO2014166533A1 (fr) 2013-04-10 2013-04-10 Échangeur thermique à lamelles de gaz

Publications (1)

Publication Number Publication Date
US20160054064A1 true US20160054064A1 (en) 2016-02-25

Family

ID=48092957

Family Applications (1)

Application Number Title Priority Date Filing Date
US14/782,842 Abandoned US20160054064A1 (en) 2013-04-10 2013-04-10 Gas slide heat exchanger

Country Status (7)

Country Link
US (1) US20160054064A1 (fr)
EP (1) EP2984432B1 (fr)
KR (1) KR20150139551A (fr)
CN (1) CN105164485B (fr)
EA (1) EA029071B1 (fr)
RS (1) RS56234B1 (fr)
WO (1) WO2014166533A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10710043B2 (en) 2014-09-24 2020-07-14 Raven Sr, Llc Compact and maintainable waste reformation apparatus

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105698561A (zh) * 2016-01-18 2016-06-22 巢湖瑞丰油脂有限公司 一种烘炒芝麻冷却设备及使用方法

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US3584792A (en) * 1969-04-18 1971-06-15 Patent And Dev Of N C Inc Device for liquid atomization and fluid blending
US3672069A (en) * 1969-02-22 1972-06-27 Metallgesellschaft Ag Fluidized-bed cooler and method of cooling particulate solid material
US3713303A (en) * 1970-01-22 1973-01-30 Stal Refrigeration Ab Means for breaking down aqueous jelly-like solutions and thus separating water and solid constituents from each other by means of freezing and subsequent melting
US4610310A (en) * 1982-09-30 1986-09-09 Miller Dennis R Fire protection system
US5178210A (en) * 1989-10-24 1993-01-12 Gaz De France Vapor pump employing counterflow exchange between air and combustion products without an intermediate fluid
US5329886A (en) * 1993-08-02 1994-07-19 Westinghouse Electric Corporation Steam generator
US5364457A (en) * 1989-11-01 1994-11-15 Cecebe Technologies Inc. Electrostatic gas cleaning apparatus
US5894883A (en) * 1998-03-25 1999-04-20 Phillips Petroleum Company Shell and tube heat exchanger
US6106789A (en) * 1993-12-30 2000-08-22 Phillips Petroleum Company Alkylation reactor with internal acid cooling zones
US20050097990A1 (en) * 2000-09-01 2005-05-12 Minogue Gerard R. Rapid surface cooling of solder droplets by flash evaporation
US20080020247A1 (en) * 2006-07-20 2008-01-24 Modine Manufacturing Company Compact air preheater for solid oxide fuel cell systems
US20100319395A1 (en) * 2008-01-11 2010-12-23 Johnson Controls Technology Company Heat exchanger
US20110186275A1 (en) * 2008-09-23 2011-08-04 Jiri Jekerle Tube bundle heat exchanger for controlling a wide performance range
US8278363B2 (en) * 2009-03-23 2012-10-02 Thomas Charles Holcombe Fischer-tropsch reactions using heat transfer tubes with a catalyst layer on the outside surfaces

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US3672069A (en) * 1969-02-22 1972-06-27 Metallgesellschaft Ag Fluidized-bed cooler and method of cooling particulate solid material
US3584792A (en) * 1969-04-18 1971-06-15 Patent And Dev Of N C Inc Device for liquid atomization and fluid blending
US3713303A (en) * 1970-01-22 1973-01-30 Stal Refrigeration Ab Means for breaking down aqueous jelly-like solutions and thus separating water and solid constituents from each other by means of freezing and subsequent melting
US4610310A (en) * 1982-09-30 1986-09-09 Miller Dennis R Fire protection system
US5178210A (en) * 1989-10-24 1993-01-12 Gaz De France Vapor pump employing counterflow exchange between air and combustion products without an intermediate fluid
US5364457A (en) * 1989-11-01 1994-11-15 Cecebe Technologies Inc. Electrostatic gas cleaning apparatus
US5329886A (en) * 1993-08-02 1994-07-19 Westinghouse Electric Corporation Steam generator
US6106789A (en) * 1993-12-30 2000-08-22 Phillips Petroleum Company Alkylation reactor with internal acid cooling zones
US5894883A (en) * 1998-03-25 1999-04-20 Phillips Petroleum Company Shell and tube heat exchanger
US20050097990A1 (en) * 2000-09-01 2005-05-12 Minogue Gerard R. Rapid surface cooling of solder droplets by flash evaporation
US20080020247A1 (en) * 2006-07-20 2008-01-24 Modine Manufacturing Company Compact air preheater for solid oxide fuel cell systems
US20100319395A1 (en) * 2008-01-11 2010-12-23 Johnson Controls Technology Company Heat exchanger
US20110186275A1 (en) * 2008-09-23 2011-08-04 Jiri Jekerle Tube bundle heat exchanger for controlling a wide performance range
US8278363B2 (en) * 2009-03-23 2012-10-02 Thomas Charles Holcombe Fischer-tropsch reactions using heat transfer tubes with a catalyst layer on the outside surfaces

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10710043B2 (en) 2014-09-24 2020-07-14 Raven Sr, Llc Compact and maintainable waste reformation apparatus
US11179693B2 (en) 2014-09-24 2021-11-23 Raven Sr, Inc. Compact and maintainable waste reformation apparatus

Also Published As

Publication number Publication date
EP2984432A1 (fr) 2016-02-17
WO2014166533A1 (fr) 2014-10-16
RS56234B1 (sr) 2017-11-30
CN105164485B (zh) 2017-08-08
EA029071B1 (ru) 2018-02-28
EP2984432B1 (fr) 2017-08-02
CN105164485A (zh) 2015-12-16
EA201591777A1 (ru) 2016-03-31
KR20150139551A (ko) 2015-12-11

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Owner name: OUTOTEC (FINLAND) OY, FINLAND

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:LOHRBERG, DIRK;ORTH, ANDREAS;SIGNING DATES FROM 20151016 TO 20151019;REEL/FRAME:036969/0728

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION