GB1572471A - Creación de Inventos y Patentes con Inteligencia Artificial

GB1572471A – Process for evaporation and evaporator
– Google Patents

GB1572471A – Process for evaporation and evaporator
– Google Patents
Process for evaporation and evaporator

Download PDF
Info

Publication number
GB1572471A

GB1572471A
GB16450/77A
GB1645077A
GB1572471A
GB 1572471 A
GB1572471 A
GB 1572471A
GB 16450/77 A
GB16450/77 A
GB 16450/77A
GB 1645077 A
GB1645077 A
GB 1645077A
GB 1572471 A
GB1572471 A
GB 1572471A
Authority
GB
United Kingdom
Prior art keywords
bundle
steam
header
tubes
pipe
Prior art date
1976-04-20
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

Application number
GB16450/77A
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.)

Sasakura Engineering Co Ltd

Original Assignee
Sasakura Engineering Co Ltd
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.)
1976-04-20
Filing date
1977-04-20
Publication date
1980-07-30

1977-04-20
Application filed by Sasakura Engineering Co Ltd
filed
Critical
Sasakura Engineering Co Ltd

1980-07-30
Publication of GB1572471A
publication
Critical
patent/GB1572471A/en

Status
Expired
legal-status
Critical
Current

Links

Espacenet

Global Dossier

Discuss

Classifications

C—CHEMISTRY; METALLURGY

C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE

C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE

C02F1/00—Treatment of water, waste water, or sewage

C02F1/02—Treatment of water, waste water, or sewage by heating

C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation

C02F1/08—Thin film evaporation

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01D—SEPARATION

B01D1/00—Evaporating

B01D1/04—Evaporators with horizontal tubes

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01D—SEPARATION

B01D1/00—Evaporating

B01D1/26—Multiple-effect evaporating

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

F28D5/00—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, using the cooling effect of natural or forced evaporation

F28D5/02—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, using the cooling effect of natural or forced evaporation in which the evaporating medium flows in a continuous film or trickles freely over the conduits

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

F28D7/1607—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 with particular pattern of flow of the heat exchange media, e.g. change of flow direction

F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING

F28—HEAT EXCHANGE IN GENERAL

F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION

F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings

F28F9/02—Header boxes; End plates

F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits

F28F9/0265—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by using guiding means or impingement means inside the header box

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

F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 – F28D20/00

F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for

F28D2021/0061—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications

F28D2021/0064—Vaporizers, e.g. evaporators

Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS

Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE

Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE

Y02A20/00—Water conservation; Efficient water supply; Efficient water use

Y02A20/124—Water desalination

Description

PATENT SPECIFICATION
( 11) 1 572 471 Application No 16450/77 ( 22) Filed 20 Apr 1977 Index at Acceptance, Bl B 303 306 403 603 715 716 KA 1 l ( 54) PROCESS FOR EVAPORATION AND EVAPORATOR Convention Application No 51/049638 ( 32) Japan (JP)
Complete Specification Published 30 Jul 1980
INT CL 3 B Ol D 1/22 Filed 20 Apr 1976 in ( 71) We, SASAKURA ENGINEERING COMPANY LIMITED, a Japanese Corporation of 6-7-5 Mitejima, Nishiyodogawaku, Osaka, Japan, do hereby declare the invention for which we pray that a Patent may be granted to us, and the method by which it is to be performed to be particularly described in and by the following statement:-
The present invention relates to an evaporation process and an evaporator.
Generally, in a multiple-effect evaporator, high-temperature steam introduced from an external source to the highest-temperature effect as a heat medium goes through the heat-transfer tubes to evaporate brine introduced around the tubes Vapour generated on the tubes is utilized as the heat medium for the next effect The above function is repeated sequentially down to the lowest effect and finally the vapour is condensed in a condensor Thus, in each effect, the steam or vapour is utilized for evaporation only once.
If vapour generated in the lowest effect is drawn with a steam ejector without being condensed and is mixed with the driving steam for reuse as a heat medium for the multiple-effect evaporator, the water production ratio, i e, the ratio of distillate output to steam input, will be increased.
The heat-transfer coefficient of heattransfer tubes of the evaporator is improved by arranging more bundles of the tubes in an evaporation chamber so that vapour will flow through one tube bundle after another at a high velocity uniformly in every tube, although such arrangement costs a little more.
There has conventionally been an evaporator of the vapour compression type having two separate bundles of horizontal heat-transfer tubes Feed-liquid is sprayed over the tubes and the evaporated portion of the liquid is compressed by an engine-driven compressor before it is fed into the upper bundle of tubes for heat-exchange Fluid in the upper tubes flows into the lower tubes from which condensate and non-condensible gases are discharged The outer surfaces of the lower tubes are subject to the hightemperature sprayed liquid as heated on the upper tubes, so that gases passing through the lower tubes will not be fully cooled and the non-condensible gases must be discharged together with a large amount of steam This increases the amount of gas discharge, necessitating a large-size gas extractor or a separate or extra vent condenser to minimize thermal losses.
These undesirable effects can be alleviated by employing an arrangement of separate bundles of heat -transfer tubes, spraying subcooled feed-liquid onto the top bundle of heat transfer tubes, and then introducing high-pressure steam mixed with lowpressure vapour into the bottom bundle of heat-transfer tubes However, if the mixed vapour is too hot, scales may form on the heat-transfer tubes Generally, as steam of high-temperature and high-pressure adiabatically expands through a steam ejector, it becomes superheated steam of low-pressure and high-temperature, which, because it is too hot, should not be used for evaporation as it is, even if mixed with vapour from the lowest-temperature effect.
It is a principle object of the present invention to achieve a process for evaporation and an evaporator for scale-free operation at a high thermal efficiency and using a small-size gas extractor.
The invention provides a process for evaporation comprising the steps of introducing steam into a bottom bundle of substantially horizontal heat-transfer tubes, leading an uncondensed portion of said steam from said bottom bundle successively into upper bundles of substantially horizontal heat-transfer tubes, the bundles being arranged one above another, the number of said tubes in each Na N_ c ( 21) ( 31) ( 33) ( 44) ( 51) ( 52) 2 1,572,471 2 bundle except the lowest being smaller than that in the next lower bundle, spraying cold feed-liquid from above the top tube bundle so that said liquid is heat-exchanged with said steam at said tubes, and cooling the steam before its introduction into the bottom bundle by mixing with it condensate from a bundle above the bottom bundle.
The invention further provides an evaporator comprising liquid spray means located at an upper portion of a casing and over an evaporation chamber in the casing, a plurality of separate bundles of substantially horizontal heat-transfer tubes disposed in the evaporation chamber and extending between first and second headers, the bundles being arranged in series and one above another, the number of said tubes in each bundle except the lowest being smaller than that in the next lower bundle, a concentrated liquid collecting region at the bottom of said evaporation chamber, a partition positioned in said first header at a level above the bottom tube bundle and formed with an opening therethrough, a pipe extending from said opening down into a first header chamber defined in said first header under said partition and adjacent the inlet end of the bottom tube bundle said pipe serving as a down-pipe for condensate collected on said partition from a bundle above the bottom bundle to flow down by gravity into said first header chamber, and means of introducing steam in to said first header chamber, said down-pipe having its outlet in said first header chamber positioned to mix said condensate with the steam introduced by said steam-introducing means.
The present invention will be better understood from the following description of a specific embodiment given by way of example and with reference to the accompanying drawings wherein:
Fig 1 is an elevational section of the evaporator, Fig 2 is a section viewed on the line II-II of Fig 1, Fig 3 is a section viewed on the line III-III of Fig 1 and Fig 4 is a perspective view, partially broken away, of the evaporator.
In an upper zone within a casing 1 of an evaporator is provided a plate 3 having a multiplicity of small holes or orifices 2 to form a liquid spray means generally designated at 4 over an evaporation chamber 5, wherein separated bundles of substantially horizontal heat-transfer tubes 7 extend between tube plates 6 and 6 a below orifices 2.
The outer sides of both tube plates 6 and 6 a are covered by a first header 8 and a second header 8 a The interiors of the headers are partitioned by respective plates or partitions and 10 a to define several, in this instance three, separate or individual bundles 19, 34 and 35 of tubes 7 Partition 10 is positioned in header 8 between bottom bundle 19 and middle bundle 34, and partition 10 a in header 8 a between middle bundle 34 and top bundle 35 The number of tubes 7 of each 70 separate bundle is less than that of the next lower bundle so that the fluid flow rate will not be lowered within the upper tubes as the volume of fluid therewithin gets less with condensation of the fluid A space on the 75 floor of chamber 5 is utilized as a concentrated liquid collector 12 communicates with a takeout pipe 13 Spray means 4 is connected to a feed-liquid pipe 14.
Partition 10 is bored with at least one 80 opening 15 therethrough from which a condensate downflow pipe 16 extends like the letter U down into an inlet or first header chamber 20 for bottom tube bundle 19, so that condensate collected in an upper or third 85 header chamber 9 will fall by gravity into header chamber 20 through pipe 16 The upturned end 18 of pipe 16 opens adjacent to an outlet port 22 of a steam ejector 21 coupled to header chamber 20 so that the con 90 densate falling through pipe 16 will be sprayed by jet steam ejected from ejector 21.
Pipe 16 is not limited to the U shape but may be of any shape with which the pipe 16 opens at one end in the steam jet from ejector 21 95 while allowing a certain amount of condensate to be kept constantly on partition 10 so that the vapour or steam in header chamber will not be released directly into upper header chamber 9 by pressure difference 100 between the two header chambers Condensate in the curved portion of pipe 16 prevents such release of steam.
A vertical partition 23 as shown in Fig 3 defines a vapour passage 25 along the parti 105 tion plate 23 in casing 1 with a clearance 24 thereunder, through which the evaporation chamber 5 communicates with passageway which, in turn, communicates with a vapour exit 27 A mist separator 26 is interposed 110 in passage 25.
Another condensate fall pipe 28 similar to pipe 16 opens at one end in partition 10 a and at the other end in a lower or second header chamber 11 An outlet or final header 115 chamber 29 for top tube bundle 35 is provided with a gas extractor 30, such as a steam ejector When the pressure within tubes 7 is kept above the atmosphere, a simple hole through the outer wall of header chamber 29 120 may replace such a gas extractor for discharging non-condensible gases.
Feed-liquid, such as seawater, introduced through the pipe 14 is sprayed from orifices 2 uniformly over heat-transfer tubes 7 High 125 pressure steam as a heating and driving medium is fed through a pipe 32 into ejector 21 Low-pressure vapour discharged from duct 27 or, in the case of a multi-effect evaporator, generated in the lowest 130 1,572,471 1,572,471 temperature effect (not shown), is drawn through a pipe 33 and mixed with said highpressure steam The resultant mixed superheated vapour or steam is ejected into the inlet header chamber 20 through outlet port 22.
On the other hand, condensate produced in the heat-transfer tubes of middle bundle 34 flows therein with the steam flow and collects on partition 10 The condensate then falls through pipe 16 and overflows from the exit 18, where it is converted into a mist by said high-velocity mixed steam from the discharge port 22 The mist is diffused in the inlet header chamber 20 and distributed to wet the internal surfaces of heat-transfer tubes 19 In this manner, said heat-transfer tubes are prevented from being heated beyond the saturation temperature equivalent to the pressure of the mixed steam, with the result that, virtually, the steam is desuperheated to the temperature of saturated steam.
The thus desuperheated steam is heatexchanged with the feed liquid sprayed over the tubes of bottom bundle 19, and a portion of the steam is condensed to collect on the bottom of second header chamber 11, from which it is drained through the pipe 31 The uncondensed steam will enter middle tubes 34 wherein a further portion of the steam is condensed and collected on partition 10 The condensate then falls through pipe 16 and is mixed with the steam mixture from the ejector 21 Remaining uncondensed steam will enter top tubes 35 wherein a still further portion thereof is condensed and collects on partition 10 a, from which it falls through pipe 28 and is added to the condensate pro40, duced in the bottom tubes 19 before it is removed through the pipe 31 The noncondensible gases are released into the atmosphere by gas extractor 30 The vapur produced from the feed liquid by heat exchange in chamber 5 flows through the clearance 24 and passage 25, with its droplets removed by mist separator 26, into exit or duct 27 In a multi-effect evaporator, the vapour then is drawn through pipe 33 and reheated by ejector 21 The concentrated liquid collected on the floor of chamber 5 is discharged through pipe 13 and may be fed to the next effect in a multi-effect evaporator.
As described hereinbefore in detail, the heating steam is fed into the heat-transfer tubes of the bottom bundle and finally into the tubes of the top bundle onto which cold feed-liquid at a temperature below evaporation point, named subcooled liquid, is sprayed and falls successively onto the lower tube bundles Thus, the steam containing non-condensible gases passing through the top tubes is heat-exchanged with the coldest feed-liquid and cooled sufficiently to minimize the ratio of steam to non-condensible gases Accordingly, almost only the noncondensible gases and very little steam are discharged from the evaporator so that a small-size gas extractor will suffice for the 70 discharge or, when no such extractor will suffice for the discharge or, when no such extractor is used, heat loss of discharged steam will be prevented without providing a vent condensor 75 The number of heat-transfer tubes of an upper bundle is smaller so that the flow of fluid in the tubes will not be slowed down as the steam is decreased in volume with condensation therein while it flows from the bot 80 tom tubes up to the upper tubes This prevents the heat-transfer coefficient from being lowered due to the slow rate of flow of the fluid, thereby improving the heat-transfer coefficient in each tube bundle Exit 18 of the 85 condensate downflow pipe 16 extending from partition 10 is located adjacet to the outlet port 22 of the ejector 21, so that the high-velocity superheated steam discharged from said ejector atomizes the condensate 90 overflowing the exit 18 A mixture of the steam and atomized condensate enters the heat-transfer tubes to heat the feed liquid on the external surfaces of the tubes, thereby preventing scaling as the result of evapora 95 tion so as to prolong continuous operation.
Because of the lowermost position of the first tube bundle, the condensate on partition 10 falls by gravity to the vicinity of the discharge port of the steam ejector without a pump 100 And the downflow pipe 16 need not have any specially devised outlet means but the exit 18 is only designed to open adjacent to the discharge port 22 of the steam ejector All these features lead to a simplified construction 105 which is trouble-free Since the flow velocity of steam at the ejector discharge port is high, the atomization of condensate in the first header chamber 20 is made uniform and yields vortex flows so that, even when the 110 number of heat-transfer tubes is large, water-droplets of the mixed steam and atomized condensate can uniformly wet the inner wall of the tubes which will not be superheated, thus preventing scaling 115 Thus the present arrangement provides a plurality of separate bundles of heat-transfer tubes so as to improve thermal efficiency in heat-exchange at the tubes and to minimize the gas extractor in size The arrangement 120 also provides simple means for cooling the heat-transfer tubes by the aid of the steam ejector so as to prevent scales which are the worst obstacle to the operation of evaporators 125

Claims (7)

WHAT WE CLAIM IS:-

1 A process for evaporation comprising the steps of introducing steam into a bottom bundle of substantially horizontal heat-transfer tubes, 130 1,572,471 leading an uncondensed portion of said steam from said bottom bundle successively into upper bundles of substantially horizontal heat-transfer tubes, the bundles being arranged one above another, the number of said tubes in each bundle except the lowest being smaller than that in the next lower bundle, spraying cold feed-liquid from above the top tube bundle so that said liquid is heatexchanged with said steam at said tubes, and cooling the steam before its introduction into the bottom bundle by mixing with it condensate from a bundle above the bottom bundle.

2 A process as claimed in claim 1, wherein the final uncondensed portion of said steam is discharged from an outlet of said top tube bundle to outside.

3 An evaporator comprising liquid spray means located at an upper portion of a casing and over an evaporation chamber in the casing, a plurality of separate bundles of substantially horizontal heat-transfer tubes disposed in the evaporation chamber and extending between first and second headers, the bundles being arranged in series and one above another, the number of said tubes in each bundle except the lowest being smaller than that in the next lower bundle, a concentrated liquid collecting region at the bottom of said evaporation chamber, a partition positioned in said first header at a level above the bottom tube bundle and formed with an opening therethrough, a pipe extending from said opening down into a first header chamber defined in said first header under said partition and adjacent the inlet end of the bottom tube bundle, said pipe serving as a down-pipe for condensate collected on said partition from a bundle above the bottom bundle to flow down by gravity into said first header chamber, and means for introducing steam in to said first header chamber, said down-pipe having its outlet in said first header chamber positioned to mix said condensate with the steam introduced by said steam-introducing means.

4 An evaporator as claimed in claim 3, further comprising an extractor for extracting and discharging uncondensed steam and gases to outside from an outlet of the top tube bundle.

An evaporator as claimed in claim 3 or claim 4, wherein said partition in said first header is 6 positioned at a level between the bottom tube bundle and the next tube bundle above, and another down-pipe for condensate depending therefrom.

6 An evaporator as claimed in claim 3 or claim 4 or claim 5, wherein the/or each down-pipe includes a U-bend.

7 An evaporator substantially as described with reference to the accompanying drawings.
For the Applicants LLOYD WISE, BOULY & HAIG, Chartered Patent Agents, Norman House, 105-109 Strand, London WC 2 R OAE.
Printed for Her Majesty’s Stationery Office, by Croydon Printing Company Limited, Croydon Surrey, 1980.
Published by The Patent Office, 25 Southampton Buildings, London, WC 2 A IAY, from which copies may be obtained.
another partition is positioned in said second header at a level between the top tube bundle and the next lower tube bundle with

GB16450/77A
1976-04-20
1977-04-20
Process for evaporation and evaporator

Expired

GB1572471A
(en)

Applications Claiming Priority (1)

Application Number
Priority Date
Filing Date
Title

JP4963876

1976-04-20

Publications (1)

Publication Number
Publication Date

GB1572471A
true

GB1572471A
(en)

1980-07-30

Family
ID=12836744
Family Applications (1)

Application Number
Title
Priority Date
Filing Date

GB16450/77A
Expired

GB1572471A
(en)

1976-04-20
1977-04-20
Process for evaporation and evaporator

Country Status (7)

Country
Link

US
(1)

US4141410A
(en)

BE
(1)

BE853753A
(en)

DE
(1)

DE2717543C3
(en)

FR
(1)

FR2348725A1
(en)

GB
(1)

GB1572471A
(en)

IT
(1)

IT1080363B
(en)

NL
(1)

NL174018C
(en)

Families Citing this family (16)

* Cited by examiner, † Cited by third party

Publication number
Priority date
Publication date
Assignee
Title

US4158295A
(en)

1978-01-06
1979-06-19
Carrier Corporation
Spray generators for absorption refrigeration systems

FR2442646A1
(en)

1978-11-29
1980-06-27
Commissariat Energie Atomique

METHOD AND DEVICE FOR DISTILLATION OR CONCENTRATION OF A SOLUTION

US4243094A
(en)

1979-01-11
1981-01-06
Karmazin Products Corporation
Condenser header construction

US4371034A
(en)

1979-08-03
1983-02-01
Hisaka Works, Limited
Plate type evaporator

AU1623183A
(en)

1982-07-01
1984-01-05
Pyrox Ltd.
Heat exchanger

US4478206A
(en)

1984-01-05
1984-10-23
Intertherm Inc.
Furnace having water vapor-condensing secondary heat exchanger

DE9000488U1
(en)

1990-01-18
1990-03-01
Magdy El-Allawy, Mohamed, 2800 Bremen, De

DE4027835A1
(en)

1990-09-03
1992-03-05
Freudenberg Carl

CONDENSER FOR VAPOROUS SUBSTANCES

TWI410600B
(en)

2008-01-31
2013-10-01
Univ Southern Taiwan Tech
Internal jet shell-and-tube heat exchanger

US8535538B1
(en)

2009-01-27
2013-09-17
Fairmount Brine Processing, LLC
Brine water recycle process

JP2010249414A
(en)

2009-04-15
2010-11-04
Tlv Co Ltd
Heat exchanger

CN102233193A
(en)

2010-04-28
2011-11-09
笹仓机械工程有限公司
Evaporation concentration device

EP2574742B1
(en)

2011-09-28
2014-09-17
Orcan Energy GmbH
Device and method for condensation of steam from ORC systems

FR2995395B1
(en)

2012-09-13
2017-10-20
Dcns

DEVICE FOR CONDENSING A HEAT PUMP FLUID FOR A CIRCUIT OF AN ENERGY PRODUCTION PLANT INTENDED TO BE IMMERED UNDER WATER EXTENSION, INSTALLATION AND ASSOCIATED METHOD

DE102016107984A1
(en)

2016-04-29
2017-11-02
Wärtsilä Serck Como Gmbh

Seawater desalination apparatus for desalination of seawater

CN106730954A
(en)

2016-12-06
2017-05-31
甘肃蓝科石化高新装备股份有限公司
Antiscaling type Falling Film Evaporator of Horizontal Tube

Family Cites Families (13)

* Cited by examiner, † Cited by third party

Publication number
Priority date
Publication date
Assignee
Title

DE244551C
(en)

US1200996A
(en)

1912-10-14
1916-10-10
Techno Chemical Lab Ltd
Method of evaporation, &c.

US1435612A
(en)

1919-04-01
1922-11-14
Ljungstroms Angturbin Ab
Air-cooled condenser

GB284413A
(en)

1926-11-01
1928-02-01
Harold Tindale
Improvements in the method of cooling or heating industrial gases and apparatus therefor

US1972811A
(en)

1932-04-07
1934-09-04
Wilkes Avery Company
Heat pump temperature regulating unit

DK70637C
(en)

1946-04-24
1950-02-20
Rolf Andersen

Method and plant for distilling water.

DE1444321B2
(en)

1963-04-30
1981-02-19
Aqua-Chem., Inc., Waukesha, Wis. (V.St.A.)

Evaporator with vapor compression

US3389059A
(en)

1965-01-27
1968-06-18
Aqua Chem Inc
Method and apparatus for purifying water by distillation while preventing corrosionby selective phosphate and acid addition

US3488261A
(en)

1967-01-30
1970-01-06
Aqua Chem Inc
Vapor compression evaporation with vent condenser and engine exhaust gas boiler

JPS4929070B1
(en)

1970-07-08
1974-08-01

US3675710A
(en)

1971-03-08
1972-07-11
Roderick E Ristow
High efficiency vapor condenser and method

JPS5119425B1
(en)

1971-05-14
1976-06-17

IL37225A
(en)

1971-07-05
1974-05-16
Israel Desalination Eng Ltd
Multieffect evaporator

1977

1977-04-18
US
US05/788,113
patent/US4141410A/en
not_active
Expired – Lifetime

1977-04-20
IT
IT7722661A
patent/IT1080363B/en
active

1977-04-20
NL
NLAANVRAGE7704291,A
patent/NL174018C/en
not_active
IP Right Cessation

1977-04-20
BE
BE2055844A
patent/BE853753A/en
not_active
IP Right Cessation

1977-04-20
GB
GB16450/77A
patent/GB1572471A/en
not_active
Expired

1977-04-20
FR
FR7711904A
patent/FR2348725A1/en
active
Granted

1977-04-20
DE
DE2717543A
patent/DE2717543C3/en
not_active
Expired

Also Published As

Publication number
Publication date

NL174018C
(en)

1984-04-16

NL7704291A
(en)

1977-10-24

US4141410A
(en)

1979-02-27

IT1080363B
(en)

1985-05-16

FR2348725B1
(en)

1982-01-08

BE853753A
(en)

1977-08-16

DE2717543A1
(en)

1977-11-03

DE2717543B2
(en)

1979-09-13

DE2717543C3
(en)

1984-08-30

FR2348725A1
(en)

1977-11-18

NL174018B
(en)

1983-11-16

Información de contacto