JPS59212601A - Falling liquid-film type evaporator - Google Patents
Falling liquid-film type evaporatorInfo
- Publication number
- JPS59212601A JPS59212601A JP58087281A JP8728183A JPS59212601A JP S59212601 A JPS59212601 A JP S59212601A JP 58087281 A JP58087281 A JP 58087281A JP 8728183 A JP8728183 A JP 8728183A JP S59212601 A JPS59212601 A JP S59212601A
- Authority
- JP
- Japan
- Prior art keywords
- heat transfer
- porous layer
- tube
- evaporator
- falling film
- 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.)
- Pending
Links
Classifications
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E10/00—Energy generation through renewable energy sources
- Y02E10/30—Energy from the sea, e.g. using wave energy or salinity gradient
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Epoxy Compounds (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
〔発明の技術分野〕
本発明は、例えば海水の温度差等の低熱落差エネルギを
オ０用して発電す全低熱落差発電プラント等に使用され
る流下液模式蒸発器に係の、特にその伝熱管の改良に関
する。Detailed Description of the Invention [Technical Field of the Invention] The present invention relates to a falling liquid model evaporator used in a total low heat drop power generation plant that uses low heat drop energy such as seawater temperature difference to generate electricity. The present invention relates to, in particular, improvements to heat exchanger tubes.
〔発明の技術的背景およびその問題点〕第７図は海水の
温度差を利用して発電する海洋温度差発電プラントの概
略系統図であって、例えばフロン、アンモニア等の低沸
点媒体からなる作動流体は、蒸発器／において海洋表層
部の比較的高温の海水によって加熱、蒸発せしめられ、
蒸気加減弁、２を経て蒸気タービン３に導入され、そこ
で膨張仕事を行ない蒸気タービン３を駆動し、その蒸気
タービン３によって発電機弘を回転して発電を行なう。[Technical background of the invention and its problems] Figure 7 is a schematic system diagram of an ocean temperature difference power generation plant that uses temperature differences in seawater to generate electricity. The fluid is heated and evaporated by relatively high temperature seawater in the ocean surface layer in the evaporator/,
The steam is introduced into the steam turbine 3 through the steam control valve 2, where it performs expansion work and drives the steam turbine 3, which rotates the generator and generates electricity.
一方、蒸気タービン３から排出された蒸気は、凝縮器ｊ
で海洋深層部の比較的温度が低い海水によシ凝縮され、
その凝縮水は一旦タンク乙に貯溜された後、循環ホンプ
７によって再び蒸発器／に返流される。こ＼で、上記蒸
発器／からの蒸発量は常に一定に保持され、発電機≠の
負荷変動に対しては、タービンノ々イパス弁♂を開閉す
ることによシ蒸気タービン３の１駆動力を調節すること
によって対応せしめられる。On the other hand, the steam discharged from the steam turbine 3 is sent to the condenser j
It is condensed by relatively low-temperature seawater in the deep ocean,
The condensed water is once stored in the tank B and then returned to the evaporator by the circulation pump 7. Here, the amount of evaporation from the evaporator is always kept constant, and when the generator's load fluctuates, the driving force of the steam turbine 3 can be reduced by opening and closing the turbine pass valve ♂. This can be done by adjusting.
ところで、この種のプラントにおける蒸発器としては、
プレート式、プール沸騰式、或は流下液膜式等の蒸発器
の使用が提案されている。しかし一般に、これら海洋温
度差発電プラントにおいては、プラント効率が低く、広
い設置スペースを必要とし、しかもタービン出力の増大
に伴なって機器が巨大化するので陸上での設置は困難な
状態にある。また、これらの海洋温度差発電プラントで
は、海水側のわずかな、圧力損失の増減がタービンの送
電端出力を左右するため、取水海水を陸上まで圧送する
ことは得策とはいえない。そのため大型プラントでは海
上設置形が検討されている。しかして、この場合上述の
各機器はパージ上に設置されるため、コンノξクトな機
器配置を行なう必要があシ、一般的な横形の蒸発器よシ
も縦形に構成される流下液膜式蒸発器の使用が効果的で
ある。By the way, as an evaporator in this kind of plant,
The use of plate type, pool boiling type, or falling film type evaporators has been proposed. However, in general, these ocean temperature difference power generation plants have low plant efficiency, require a large installation space, and as the turbine output increases, the equipment becomes bulky, making it difficult to install on land. In addition, in these ocean temperature difference power generation plants, the slight increase or decrease in pressure loss on the seawater side affects the output of the turbine at the transmission end, so it is not a good idea to pump the intake seawater to land. For this reason, offshore installations are being considered for large plants. In this case, each of the above-mentioned equipment is installed on the purge, so it is necessary to arrange the equipment in a con- nected manner. Use of an evaporator is effective.
第２図は、上記流下液膜式蒸発器の概略構成図であって
、流下液膜式蒸発器１０のケーシング／／内には仕切壁
／、２ 、 ／３ 、 ／’ｉ４によって上方から順に
加熱流体流入室／Ｓ、被加熱流体流入室／６、蒸発室／
７および加熱流体出口室／とがそれぞれ区劃形成されて
おり、上記加熱流体流入室１５および被加熱流体流入％
／６にはそれぞれ加熱流体導入管ｔｓｈおよび被加熱流
体導入管／Ａａが連接されている。また、蒸発室／７に
は、その中間高さ位置に蒸気流出管／７ａが連接され、
下部に被加熱流体導出管／７ｂが連接されておシ、加熱
流体出口室／ざには加熱流体導出管／ざａが連接されて
いる。FIG. 2 is a schematic configuration diagram of the falling film evaporator 10. Inside the casing // of the falling film evaporator 10, there are partition walls /, 2, /3, /'i4 in order from the top. Heating fluid inflow chamber/S, heated fluid inflow chamber/6, evaporation chamber/
7 and a heating fluid outlet chamber/are respectively formed into sections, and the heating fluid inflow chamber 15 and the heated fluid inflow %
A heated fluid introduction pipe tsh and a heated fluid introduction pipe /Aa are connected to /6, respectively. Further, a vapor outlet pipe/7a is connected to the evaporation chamber/7 at an intermediate height position,
A heated fluid outlet pipe/7b is connected to the lower part, and a heated fluid outlet pipe/zone is connected to the heated fluid outlet chamber/zone.
一方、上記ケーシング／／内には、頂端が前記加熱流体
流入室１５に開口し、下端が加熱流体出口室７ｇに開口
する多数本の伝熱管／９が配列されている。On the other hand, a large number of heat transfer tubes/9 are arranged inside the casing///, the top end of which opens into the heating fluid inlet chamber 15, and the lower end of which opens into the heating fluid outlet chamber 7g.
上記伝熱管／？の外表面には、第３図に示すようをで、
熱貫流率を向上するため軸線方向に延びる多数の凹凸溝
／９ａが形成されている。The above heat exchanger tube/? As shown in Figure 3, the outer surface of the
A large number of uneven grooves/9a extending in the axial direction are formed to improve the heat transmission coefficient.
しかして、加熱流体である表層海水は加熱流体入口室／
Ｓに供給され、伝熱管／の内を流動し、加熱流体出口室
／ざを経て器外に排出される。一方、被加熱流体は被加
熱流体導入管／６ａを介して被加熱流体入口室／６内に
流入し仕切壁／３上に貯溜され、この仕切壁／３と伝熱
管／９との間隙から各伝熱管１７の外表面に沿って流下
し、その間伝熱管／ｑ内を流れる加熱流体と熱交換して
加熱され、その一部が蒸発せしめられる。そしてその蒸
発した被加熱流体は蒸気流出管／７ａを経て蒸発タービ
ンへと供給され、また蒸発できなかった被加熱流体は被
加熱流体導出管／７ｂから流出し、図示しないポンプを
介して再び被加熱流体入口室／乙に還流される。Therefore, the surface seawater, which is the heating fluid, enters the heating fluid inlet chamber.
The fluid is supplied to S, flows through the heat exchanger tube, and is discharged outside the vessel through the heated fluid outlet chamber. On the other hand, the heated fluid flows into the heated fluid inlet chamber/6 through the heated fluid introduction pipe/6a and is stored on the partition wall/3, and from the gap between the partition wall/3 and the heat transfer tube/9. It flows down along the outer surface of each heat exchanger tube 17 and is heated by exchanging heat with the heating fluid flowing inside the heat exchanger tube /q, and a part of it is evaporated. The evaporated fluid to be heated is supplied to the evaporation turbine through the steam outlet pipe/7a, and the fluid to be heated that has not been evaporated flows out from the fluid to be heated pipe/7b and is heated again via a pump (not shown). The heated fluid is refluxed to the inlet chamber/B.
ところが、このような流下液膜式蒸発器を発電端出力２
ｒ００ ＫＷのプラントに適用した場合には、伝熱管本
数 ｙｏｏθ本
伝熱管全長 ／７ｍ
蒸発器全高 ２０ｔ１を
蒸発器シェル径 Ａｍ組立重量
乙００ Ｔｏｎ
となシ、かなり大形な構造物となる。したがって、この
ような大形構造物をパージ上に設置することは、ノ々−
ジの強度および安定性の面から好捷しくない。However, with such a falling film evaporator, the power generation end output is 2.
When applied to a r00 KW plant, the number of heat transfer tubes: yooθ Total length of heat transfer tubes: /7m Total height of evaporator: 20t1: Evaporator shell diameter: Am assembled weight:
It will be a fairly large structure. Therefore, it is difficult to install such a large structure on the purge.
unfavorable in terms of strength and stability.
本発明はこのような点に鑑み、パージ上にも十分設置す
ることができ、伝熱効率が高くコン・ぐクトな流下液膜
式の蒸発器を得ることを目的とする。In view of these points, it is an object of the present invention to provide a falling film type evaporator that can be sufficiently installed on the purge, has high heat transfer efficiency, and is highly conducive.
本発明は、伝熱管内を流下する加熱流体によって、上記
伝熱管の管外表面に沿って流下する被加熱流体を加熱す
る流下液膜式蒸発器において、蒸発室内における上記伝
熱管の外表面上半部に適宜高さ範囲にわたって多孔質層
７設けるとともに、下半部にその多孔質層に引き続き管
軸方向に延びる凹凸溝を形成したことを特徴とする。The present invention provides a falling film type evaporator that heats a heated fluid flowing down along the outer surface of the heat transfer tube by a heating fluid flowing down inside the heat transfer tube, in which a heating fluid flowing down the heat transfer tube is heated on the outer surface of the heat transfer tube in the evaporation chamber. It is characterized in that a porous layer 7 is provided over a suitable height range in the half part, and an uneven groove extending in the tube axis direction following the porous layer is formed in the lower half part.
以下、第≠図乃至第２図７参照して本発明の一実施例に
ついて説明する。なお、第≠図において第２図と同一部
分には同一符号を付しその詳細な説明は省略する。An embodiment of the present invention will be described below with reference to FIGS. In addition, in FIG. 2, the same parts as in FIG. 2 are given the same reference numerals, and detailed explanation thereof will be omitted.
第弘図は本発明の流下液模式蒸発器の縦断面図であって
、ケーシング／／内に配列された多数本の伝熱管／９の
外表面には、蒸発室／７におけるその上半部の適宜高さ
範囲にわたって溶射加工にょ多形成された多孔質層２／
が形成され、さらにその下半部には上記多孔質層２／に
引き続いて管軸方向に延びる多数の凹凸溝Ｕが形成され
ている。その他の点は第２図に示す従来のものを全く同
一である。Fig. 7 is a vertical cross-sectional view of the falling liquid model evaporator of the present invention, in which the outer surface of a large number of heat transfer tubes /9 arranged in the casing // has an upper half thereof in the evaporation chamber /7. Porous layer 2/
is formed, and a large number of uneven grooves U extending in the tube axis direction following the porous layer 2/ are formed in the lower half thereof. Other points are exactly the same as the conventional one shown in FIG.
−ところで、上記多孔質層２／は粒度、２００メツシー
以下の銅または銅合金の粉末を、５−ｏ−３−００μｍ
の厚さに火炎溶射することにより形成され、凹凸溝シは
溝深さが０−３〜／、 ０７１１ｊＡで／ 〜／、 Ｊ
−７１１ＪＲ（Ｄヒｙ ｆで設けられている。丑た、多
孔質層２／部がら凹凸溝ｎ形成部への遷移部Ｊにおいて
は、第Ｊ図に示すように、多孔質層、２／部の母管の外
径Ｄ１と凹凸溝Ｕ形成部の最大外径Ｄ２とが同じ大きさ
に形成してあり、多孔質層ユ／はその厚さが所定値より
漸次減少され、完全にその厚さが零となった位置から凹
凸溝ｎの溝深さが次第に増加され、所定の溝深さ０．３
〜／」となるようにしである。- By the way, the porous layer 2/ is made of copper or copper alloy powder with a particle size of 200 mcs or less, 5-o-3-00 μm.
The uneven grooves are formed by flame spraying to a thickness of 0-3~/, 0711jA/~/, J
-711JR (provided at The outer diameter D1 of the main pipe of the part and the maximum outer diameter D2 of the uneven groove U forming part are formed to have the same size, and the thickness of the porous layer U/ is gradually reduced from a predetermined value to completely reduce its thickness. The groove depth of the uneven groove n is gradually increased from the position where the thickness becomes zero, until the predetermined groove depth is 0.3.
~/''.
しかして、被加熱流体流入室／６に流入した被加熱流体
は、仕切壁／３と伝熱管／９との間隙から流出し伝熱管
／９を膜状に覆いながら流下し、多孔質層２７部におい
て管内を流れる表層海水によって加熱されて核沸騰し、
その一部が蒸発する。未蒸発液は凹凸溝２２部において
管内を流れる表層海水によってさらに加熱されて残シの
一部がさらに蒸発し、未蒸発液は蒸発室１７の下部に接
続されている被加熱流体導出管／７１）から導出される
。一方、前記伝熱管１９の表面で蒸発した蒸気は蒸気流
出管／７ａを経て蒸気タービンに送られる。The heated fluid that has flowed into the heated fluid inflow chamber /6 flows out from the gap between the partition wall /3 and the heat exchanger tube /9, flows down while covering the heat exchanger tube /9 in a film-like manner, and flows down into the porous layer 27. The water is heated by the surface seawater flowing inside the pipe and undergoes nucleate boiling.
Some of it evaporates. The unevaporated liquid is further heated by the surface seawater flowing inside the pipe in the uneven groove 22 portion, and a part of the remaining liquid is further evaporated. ) is derived from On the other hand, the steam evaporated on the surface of the heat transfer tube 19 is sent to the steam turbine via the steam outlet tube/7a.
この場合伝熱管１９が前述のように構成されているため
、管外表面を流下する液膜が遷移部において管表面よ）
剥離することなく、全量が有効に熱伝達に寄与し、その
熱効率が向上せしめられる・ところで、第６図は外表面
に凹凸溝を設けた伝熱管の流下液膜熱伝達係数の性能試
験の結果を示す線図であり、凹凸溝のピッチが７〜／、
！眉で伝熱性能が最も高くなる。In this case, since the heat exchanger tube 19 is configured as described above, the liquid film flowing down the outer surface of the tube is lower than the tube surface at the transition part.
The entire amount effectively contributes to heat transfer without peeling, improving its thermal efficiency.By the way, Figure 6 shows the results of a performance test of the falling liquid film heat transfer coefficient of a heat transfer tube with uneven grooves on the outer surface. is a diagram showing the pitch of the uneven grooves from 7 to /,
! Heat transfer performance is highest in the eyebrows.
また、第７図は、加熱流体と被加熱流体との温度差に対
する管外側流下液膜熱伝達係数の変化を、作動流体（被
加熱流体）としてフロン／／３を用いて行なった試験結
果を示す線区であって、（ａ）は管外表面に凹凸溝のみ
を有する伝熱管の試験結果、（ｂ）は管外表面に溶射加
工にょ多形成した多孔質層のみを有する伝熱管の試験結
果２示す。ずなゎぢ。Furthermore, Figure 7 shows the results of a test conducted using Freon//3 as the working fluid (heated fluid) to determine the change in the heat transfer coefficient of the falling liquid film on the outside of the tube with respect to the temperature difference between the heating fluid and the heated fluid. In the line sections shown, (a) is the test result of a heat exchanger tube with only uneven grooves on the outer surface of the tube, and (b) is the test result of a heat exchanger tube with only a porous layer formed by thermal spraying on the outer surface of the tube. Results 2 are shown. Zunawaji.
表層海水と作動流体との温度差が大きい領域では、多孔
質層を有する伝熱管が高い熱伝達性能を発揮し、上記温
度差が小さくなると凹凸溝を有する伝熱管が高い熱伝達
性能を発揮する。In areas where there is a large temperature difference between the surface seawater and the working fluid, heat transfer tubes with porous layers exhibit high heat transfer performance, and when the temperature difference becomes small, heat transfer tubes with uneven grooves exhibit high heat transfer performance. .
したがって、伝熱管を前述のように構成すれば、管外側
流下液膜熱伝達係数は第ｇ図に示すように方り、従来の
凹凸溝のみを設けた伝熱管に比べて篩い伝熱効率を達成
することができる。また、上述のように伝熱効率が高く
なることによって、本発明の流下液膜式蒸発器を発電端
出力２３００ ＫＷのプラントに適用した場合には、
伝熱管本数 ２０００本
伝熱管全長 ／３ ｍ
蒸発器全高 ／乙ｍ
蒸発器シェル匝 Ａ ｔｙｔ組立重量
ｔ、ｔ！；ＯＴｏｎ
となり、蒸発器全高、組立重量を大幅に低減せしめるこ
とができる。Therefore, if the heat transfer tube is configured as described above, the heat transfer coefficient of the falling liquid film on the outside of the tube will be as shown in Figure g, achieving a higher heat transfer efficiency than the conventional heat transfer tube provided with only uneven grooves. can do. Furthermore, due to the high heat transfer efficiency as described above, when the falling film evaporator of the present invention is applied to a plant with a power generation output of 2300 kW, the number of heat transfer tubes: 2000 total length of heat transfer tubes /3 m Evaporation Overall height of vessel / m Evaporator shell weight A tyt Assembled weight t, t! ;OTon, and the total height of the evaporator and assembly weight can be significantly reduced.
以上説明したように、本発明においては、蒸発室におけ
る伝熱管の上半部外表面に適宜高さ範囲にわたって多孔
質層を設けるとともに、その多孔質層に引、き続き管軸
方向に延びる凹凸溝を形成したので、従来の装置に比べ
管外側流下液膜熱伝達係数を７．！〜２倍程度向上させ
ることができ、それによって蒸発全高、組立重量の低減
を図ることができ、海上設置に際してパージの強度に対
する影響を少なくできて安定性を向上させることができ
る。As explained above, in the present invention, a porous layer is provided over an appropriate height range on the outer surface of the upper half of the heat exchanger tube in the evaporation chamber, and the porous layer is followed by unevenness extending in the tube axis direction. Since the grooves are formed, the heat transfer coefficient of the falling liquid film on the outside of the tube is 7. ! It is possible to improve the performance by about 2 times, thereby reducing the total height of evaporation and the assembly weight, reducing the influence on the strength of purge when installed at sea, and improving stability.
第１図は海洋温度差発電プラントの概略系統図、第２図
は従来の流下液膜式蒸発器の縦断面図、第３図は上記蒸
発器の伝熱管の横断面図、第グ図は本発明の流下液膜式
蒸発器の縦断面図、第５図は同上蒸発器の伝熱管の遷移
部の縦断面図、第４図は凹凸溝のピッチに対する管外側
流下液膜熱伝達係数の変化線図、・第７図は加熱流体と
被加熱流体との温度差に対する管外ｆｆ１１１作〒液噴
熱私達係数の変化線図、第ｒ図は本発明における伝熱管
の伝熱性能を示す図である。
１５・・・加熱流体流入室、／６・・・被加熱流体流入
室、／７・・・蒸発室、／９・・・伝熱管、２／・・・
多孔質層、工・・・凹凸溝。
出願人代理人 猪 股 清躬１菌
躬３奮」
第４目
（１５Figure 1 is a schematic system diagram of an ocean temperature difference power generation plant, Figure 2 is a vertical cross-sectional view of a conventional falling film evaporator, Figure 3 is a cross-sectional view of the heat transfer tube of the evaporator, and Figure A vertical cross-sectional view of the falling film type evaporator of the present invention, FIG. 5 is a vertical cross-sectional view of the transition part of the heat transfer tube of the same evaporator, and FIG. Change diagram, Figure 7 is a change diagram of the liquid jet heat coefficient created by outside the tube ff111 for the temperature difference between the heating fluid and the heated fluid, and Figure R shows the heat transfer performance of the heat transfer tube in the present invention. FIG. 15... Heating fluid inflow chamber, /6... Heated fluid inflow chamber, /7... Evaporation chamber, /9... Heat exchanger tube, 2/...
Porous layer, texture... uneven grooves. Applicant's representative Inomata Kiyomi 1 Bacteria 3 Iku" No. 4 (15)
Claims (1)
の管外表面に沿って流下する被加熱流体を加熱する流下
液膜式蒸発器において、蒸発室における上記伝熱管の外
表面上半部に、適宜高さ範囲にわたって多孔質層を設け
るとともに、下半部にその多孔質層に引続き管軸方向に
延びる凹凸溝を形成したことを特徴とする、流下液膜式
蒸発器。 シ多孔質層は、伝熱管外表面に粒度、！００メツシー以
下の銅または銅合金の粉末を５０〜ｊＯ０μｍの厚さに
火炎溶射することによ多形成されていることを特徴とす
る特許請求の範囲第１項記載の流下液膜式蒸発器。 ３、凹凸溝はピッチ／〜／、Ｊ−Ｍ、溝深さ０．３〜／
、ＯＩ／ＩＪＩであることを特徴とする特許請求の範囲
第１項記載の流下液膜式蒸発器。 久多孔質層部から凹凸溝部への遷移部では、多孔質層の
厚さが漸次減少し、多孔質層の厚さが零となった位置か
ら溝深さが次第に増加し所定溝深さとなるようにしであ
ることを特徴とする特許請求の範囲第１項記載の流下液
膜式蒸発器０[Scope of Claims] 1. In a falling film evaporator that heats a fluid to be heated flowing down along the outer surface of the heat transfer tube by a heating fluid flowing down inside the heat transfer tube, the heat transfer tube in the evaporation chamber A falling liquid film type, characterized in that a porous layer is provided over an appropriate height range on the upper half of the outer surface of the tube, and an uneven groove extending in the tube axis direction following the porous layer is formed on the lower half of the tube. Evaporator. The porous layer has a grain size on the outer surface of the heat transfer tube! 2. The falling film evaporator according to claim 1, wherein the falling film evaporator is formed by flame spraying copper or copper alloy powder having a thickness of 50 to 0 μm. 3. The uneven groove has a pitch of /~/, J-M, groove depth of 0.3~/
, OI/IJI.A falling film evaporator according to claim 1, wherein the falling film evaporator is OI/IJI. At the transition part from the porous layer to the uneven groove, the thickness of the porous layer gradually decreases, and from the position where the thickness of the porous layer reaches zero, the groove depth gradually increases until it reaches a predetermined groove depth. A falling film type evaporator 0 according to claim 1, characterized in that:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58087281A JPS59212601A (en) | 1983-05-18 | 1983-05-18 | Falling liquid-film type evaporator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58087281A JPS59212601A (en) | 1983-05-18 | 1983-05-18 | Falling liquid-film type evaporator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS59212601A true JPS59212601A (en) | 1984-12-01 |
Family
ID=13910398
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58087281A Pending JPS59212601A (en) | 1983-05-18 | 1983-05-18 | Falling liquid-film type evaporator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59212601A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014526009A (en) * | 2011-06-27 | 2014-10-02 | デ・セ・エヌ・エス | Thermal energy system and method of operating thermal energy system |
| JP2017096621A (en) * | 2009-07-16 | 2017-06-01 | ロッキード マーティン コーポレーション | Helical tube bundle arrangements for heat exchangers |
| US10209015B2 (en) | 2009-07-17 | 2019-02-19 | Lockheed Martin Corporation | Heat exchanger and method for making |
-
1983
- 1983-05-18 JP JP58087281A patent/JPS59212601A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2017096621A (en) * | 2009-07-16 | 2017-06-01 | ロッキード マーティン コーポレーション | Helical tube bundle arrangements for heat exchangers |
| US10209015B2 (en) | 2009-07-17 | 2019-02-19 | Lockheed Martin Corporation | Heat exchanger and method for making |
| JP2014526009A (en) * | 2011-06-27 | 2014-10-02 | デ・セ・エヌ・エス | Thermal energy system and method of operating thermal energy system |
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