JPS63267877A - Condensing evaporator - Google Patents
Condensing evaporatorInfo
- Publication number
- JPS63267877A JPS63267877A JP32904987A JP32904987A JPS63267877A JP S63267877 A JPS63267877 A JP S63267877A JP 32904987 A JP32904987 A JP 32904987A JP 32904987 A JP32904987 A JP 32904987A JP S63267877 A JPS63267877 A JP S63267877A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- oxygen
- chamber
- flow path
- gas
- 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.)
- Granted
Links
- 239000007788 liquid Substances 0.000 claims description 88
- 239000012530 fluid Substances 0.000 claims description 32
- 238000005192 partition Methods 0.000 claims description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 59
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 59
- 239000001301 oxygen Substances 0.000 description 27
- 229910052760 oxygen Inorganic materials 0.000 description 27
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 26
- 229910052757 nitrogen Inorganic materials 0.000 description 21
- 229910001873 dinitrogen Inorganic materials 0.000 description 16
- 229910001882 dioxygen Inorganic materials 0.000 description 13
- 239000007789 gas Substances 0.000 description 11
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000004891 communication Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000001174 ascending effect Effects 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000005452 bending Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 150000002926 oxygen Chemical class 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
- F25J5/005—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger in a reboiler-condenser, e.g. within a column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/10—Boiler-condenser with superposed stages
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
- Separation By Low-Temperature Treatments (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】
〔産業上の利用分野〕
本発明は第一流体室の液媒と第二流体室の流体とで熱交
換を行なう凝縮蒸発器に関する。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a condensing evaporator that exchanges heat between a liquid medium in a first fluid chamber and a fluid in a second fluid chamber.
従来、空気液化分離装置の複精留塔の上部塔等に用いら
れる凝縮蒸発器は、多数の垂直方向平行な仕切板により
仕切られ、第一流体室、（ｉ！素室）と第二流体室（窒
素室）の二重を交互に隣接して積層され、いわゆるプレ
ートフィン式熱交換器と呼ばれているものが用いられて
おり、酸素室は上下端部で解放され、上部塔の底部空間
に溜まる液媒（液体酸素）中に浸漬されることにより液
体酸素で満たされる。そして、下部塔から窒素室に導入
される窒素ガスと熱交換を行ない、窒素ガスは凝縮して
液体窒素となり、液体酸素は蒸発して酸素ガスとなるよ
うに構成されている。Conventionally, a condensing evaporator used in the upper column of a double rectification column of an air liquefaction separation device is partitioned by a number of vertically parallel partition plates, and is divided into a first fluid chamber, (i! elementary chamber) and a second fluid chamber. A so-called plate-fin heat exchanger is used, in which double chambers (nitrogen chambers) are stacked alternately adjacent to each other, and the oxygen chambers are open at the top and bottom ends, and the oxygen chambers are open at the bottom of the upper column. The space is filled with liquid oxygen by being immersed in the liquid medium (liquid oxygen) that accumulates there. Then, heat exchange is performed with the nitrogen gas introduced into the nitrogen chamber from the lower column, so that the nitrogen gas is condensed to become liquid nitrogen, and the liquid oxygen is evaporated to become oxygen gas.
（発明が解決しようとする問題点）
しかしながら、従来の凝縮蒸発器の酸素室は、液体酸素
に浸漬されて用いるため、液深の液圧による液温や沸点
上昇（約１℃／ｍ）を生じ、凝縮蒸発器の下部は上部よ
りも温度が高く、その分窒素の凝縮温度との温度差を縮
めている。(Problems to be Solved by the Invention) However, since the oxygen chamber of a conventional condenser evaporator is immersed in liquid oxygen, the liquid temperature and boiling point rise (approximately 1°C/m) due to the liquid pressure at the depth of the liquid. The lower part of the condensing evaporator has a higher temperature than the upper part, which reduces the temperature difference with the condensing temperature of nitrogen.
凝縮蒸発器の窒素側と酸素側の温度差は通常１〜２℃と
なっているので、上記液体酸素の温度上昇は凝縮蒸発器
の性能上大きな問題となっている。Since the temperature difference between the nitrogen side and the oxygen side of the condensing evaporator is usually 1 to 2°C, the temperature rise of the liquid oxygen is a major problem in terms of the performance of the condensing evaporator.
即ち、下部塔を５幻ｆ／１−ｊＧで運転するためには、
凝縮蒸発器高さを約２ｍ迄にしないと適正な能力を発揮
できず、能力を上げるために凝縮蒸発器高さを高くとる
と、液体酸糸の液深を増加して液温が上昇するので下部
塔運転圧力を高めなければならないから、塔の径を太く
して配置基数を増さねばならず、塔の製作を面倒にして
いた。That is, in order to operate the lower tower at 5 phantom f/1-jG,
Appropriate performance cannot be achieved unless the height of the condenser evaporator is set to approximately 2m.If the height of the condenser evaporator is increased to increase the capacity, the depth of the liquid acid thread will increase and the temperature of the liquid will rise. Therefore, the operating pressure of the lower column had to be increased, and the diameter of the column had to be increased to increase the number of bases, which made the manufacture of the column complicated.
また液体酸素の液深による温度上昇は、下部塔運転圧力
に影響を与えている。即ち下部塔運転圧力は、下部塔頂
部の飽和窒素ガスの凝縮温度を決定しており、この凝縮
温度を下げるために゛は、液体酸素の温度を下げる必要
がある。In addition, the temperature increase due to the depth of liquid oxygen affects the operating pressure of the lower column. That is, the operating pressure of the lower column determines the condensation temperature of the saturated nitrogen gas at the top of the lower column, and in order to lower this condensation temperature, it is necessary to lower the temperature of liquid oxygen.
一方空気分離装置の動力は原料空気の圧縮、即ち下８１
Ｉ塔圧力までの昇圧にほとんど消費されているので下部
塔をより低圧で運転することが出来れば動力費が削減で
きる。しかし、凝縮蒸発器を液体酸素中に浸漬する従来
の構造では、必ず液ヘッドによる液体酸素の温度上昇効
果弁は下部塔圧力の低下が制限されてしまうと言う欠点
がある。On the other hand, the power of the air separation device is the compression of the raw air, that is, the
Most of the energy is consumed in raising the pressure to the I column pressure, so if the lower column can be operated at a lower pressure, power costs can be reduced. However, in the conventional structure in which the condensing evaporator is immersed in liquid oxygen, there is a drawback in that the valve that increases the temperature of liquid oxygen by the liquid head always limits the reduction in the pressure of the lower column.
さらに、凝縮蒸発器を設置している上部塔底部の空間に
液体酸素を溜めなければ凝縮蒸発器の能力を十分に発揮
できないため、凝縮蒸発器が液体酸素中に浸漬するまで
は下部塔還流液となる液体窒素の凝縮液も、また液体酸
素の蒸発による上部塔上昇ガスも発生しないから精留作
用が開始されず、無駄な持ち時間（起動時間）となり、
この間は動力費の損失となる。Furthermore, the capacity of the condenser-evaporator cannot be fully demonstrated unless liquid oxygen is stored in the space at the bottom of the upper column where the condenser-evaporator is installed. Since neither the condensate of liquid nitrogen nor the gas rising in the upper column due to evaporation of liquid oxygen is generated, the rectification action does not start, resulting in wasted time (start-up time).
During this time, there will be a loss in power costs.
本発明は、高さ方向の形状的制限を無くして大型空気分
離装置用精留塔の上下部基の一体構造化を可能とし、液
体酸素中に浸漬せずに熱交換でき、液深による液圧を減
少して液温や沸点の上昇を無くし、原料空気圧縮圧を低
下させて動力費を削減し、かつ起動時間を短縮できる凝
縮蒸発器を提供することを目的とする。The present invention eliminates geometrical restrictions in the height direction and enables the upper and lower bases of a rectification column for large-scale air separation equipment to be integrated into an integrated structure. It is an object of the present invention to provide a condensing evaporator that can reduce pressure to eliminate increases in liquid temperature and boiling point, reduce raw material air compression pressure to reduce power costs, and shorten start-up time.
上記した目的を達成するために本発明は、多数の垂直な
仕切板により第一流体室と第二流体室とを交互に形成し
、前記第一流体室の液媒と、前記第二流体室の流体とで
熱交換を行なう凝縮蒸発器において、前記第一流体室に
上下多段に複数の伝熱板を配置して液媒の流路を形成し
、該流路の一端は開放とし、他端側に該流路と連通し、
上部を開放した複数の液溜を上下多段に設けるとともに
、液媒を各段の液溜に供給させながら前記流路に導入し
て熱交換させるように構成したことを特徴としている。In order to achieve the above object, the present invention alternately forms a first fluid chamber and a second fluid chamber by a large number of vertical partition plates, and the liquid medium in the first fluid chamber and the second fluid chamber are In a condensing evaporator that exchanges heat with a fluid, a plurality of heat transfer plates are arranged in upper and lower stages in the first fluid chamber to form a flow path for the liquid medium, one end of the flow path is open, and the other end is open. communicating with the flow path on the end side,
It is characterized in that a plurality of liquid reservoirs with open tops are provided in upper and lower stages, and a liquid medium is introduced into the flow path while being supplied to the liquid reservoirs in each stage for heat exchange.
従って液深による液温や沸点上昇を大幅に低減し得、ま
た凝縮蒸発器の高さを高くして伝熱面積の増加を図れる
ため、高さ方向の形状的−制限が無くなり、さらに起動
時間も短縮できる。Therefore, it is possible to significantly reduce the rise in liquid temperature and boiling point due to liquid depth, and the height of the condenser evaporator can be increased to increase the heat transfer area, eliminating geometrical restrictions in the height direction and further increasing the startup time. can also be shortened.
〔実施例）
以下、本発明を、蒸発する液媒を酸素、凝縮する流体を
窒素とした胸につき、第１図乃至第７図に基づいて説明
する。[Example] Hereinafter, the present invention will be explained based on FIGS. 1 to 7 using oxygen as the liquid medium to be evaporated and nitrogen as the fluid to be condensed.
まず、第１図は本発明の凝縮蒸発器の全体斜視図であり
、一部切欠いて第一流体室である酸素室の内部構造を図
示しである。第２図は酸素室を示す断面図であり、液の
流れ方向を実線矢印、ガスの流れ方向を破線矢印で示す
。First, FIG. 1 is an overall perspective view of the condensing evaporator of the present invention, with a portion cut away to illustrate the internal structure of an oxygen chamber, which is a first fluid chamber. FIG. 2 is a sectional view showing the oxygen chamber, where the direction of flow of liquid is shown by solid arrows and the direction of gas flow is shown by dashed arrows.
凝縮蒸発器１は、上下あるいは両側のサイドパー２．３
により接合された多数の垂直方向平行な仕切板４により
第一流体室５（以下酸素室という）と第二流体室６（以
下窒素室という）とを交互に多数Ｉａ層して形成されて
おり、酸素室５の液媒（以下液体酸素ＬＯという）と窒
素室６を流れる流体（以下窒素ガスＧＮという）とで熱
交換を行なうものであり、−側部には複数の液？１ｆ７
が上下多段に配設されている。The condenser evaporator 1 has upper and lower or both side pars 2.3
A first fluid chamber 5 (hereinafter referred to as an oxygen chamber) and a second fluid chamber 6 (hereinafter referred to as a nitrogen chamber) are formed by alternating a large number of Ia layers by a large number of vertically parallel partition plates 4 joined by. , heat exchange is performed between the liquid medium in the oxygen chamber 5 (hereinafter referred to as liquid oxygen LO) and the fluid flowing in the nitrogen chamber 6 (hereinafter referred to as nitrogen gas GN), and there are multiple liquids on the - side. 1f7
are arranged in multiple levels above and below.
窒素室６は、従来の装置と略同様に構成されるもので、
仕切板４．４と仕切板両側のサイドパー３．３とによっ
て構成され、上部には窒素ガスＧＮを導入するための入
口ヘッダ−８と入口配管９を設け、下部には凝縮した液
体窒素ＬＮを集合するための出口ヘッダ−１０と出口配
管１１、及び窒素ガスＧＮ中に含まれるヘリウムガス等
の不凝縮ガスＧＸの排出管１２を設けている。The nitrogen chamber 6 is configured almost in the same way as a conventional device.
It is composed of a partition plate 4.4 and side pars 3.3 on both sides of the partition plate, and an inlet header 8 and an inlet pipe 9 for introducing nitrogen gas GN are provided in the upper part, and condensed liquid nitrogen LN is provided in the lower part. An outlet header 10 and an outlet pipe 11 for collecting the nitrogen gas GN, and a discharge pipe 12 for a non-condensable gas GX such as helium gas contained in the nitrogen gas GN are provided.
入口ヘッダ−８から各窒素室６に分配された窒素ガスＧ
Ｎは、窒素室６内に垂直に配設された有孔波形伝熱フィ
ンからなる伝熱板１３内を、隣接する酸素室５の液体酸
素［０と熱交換しながら凝縮液化して流下し、出口ヘッ
ダ−１０に集合する。Nitrogen gas G distributed from the inlet header 8 to each nitrogen chamber 6
N is condensed and liquefied while exchanging heat with the liquid oxygen [0] in the adjacent oxygen chamber 5 and flows down inside the heat transfer plate 13 consisting of perforated wave-shaped heat transfer fins arranged vertically in the nitrogen chamber 6. , gather at the exit header-10.
一方、窒素室６と気密に仕切られる酸素室５は、仕切板
４．４と上下のサイドパー２．２とにより形成され、そ
の内部に流路１４を形成する複数の伝熱板１５を上下多
段に配置しているもので、流路１４の一端は前記液溜７
と連通しており、他端１４ａを開放して酸素ガスＧｏの
ガス出口としている。On the other hand, the oxygen chamber 5, which is airtightly partitioned from the nitrogen chamber 6, is formed by a partition plate 4.4 and upper and lower side pars 2.2. One end of the flow path 14 is connected to the liquid reservoir 7.
The other end 14a is opened to serve as a gas outlet for oxygen gas Go.
上記伝熱板１５は、前記仕切板４．４の間を区切るもの
で、各段につき１枚づつ用いても良いが通常は波形伝熱
フィンを用いる。本実施例ではこの伝熱板１５は波形伝
熱フィンを用い、その折り曲げ線を液溜７側から流路１
４の他端１４ａに向けて病り勾配を有するように傾斜さ
せて垂直方向に多段に配置し、上下の伝熱板１５の傾斜
面間を液体酸素ＬＯ及び酸素ガスＧＯの流路１４として
おり、一つの液１ｆｉｆ７に対し上下複数の流路１４が
連通している。The heat transfer plate 15 separates the partition plates 4.4, and although one plate may be used for each stage, corrugated heat transfer fins are usually used. In this embodiment, the heat transfer plate 15 uses corrugated heat transfer fins, and the bending line extends from the liquid reservoir 7 side to the flow path 1.
The heat transfer plates 15 are arranged vertically in multiple stages so as to have a slope toward the other end 14a of the heat exchanger plates 15, and a flow path 14 for liquid oxygen LO and oxygen gas GO is provided between the inclined surfaces of the upper and lower heat exchanger plates 15. , a plurality of upper and lower channels 14 communicate with one liquid 1fif7.
上下多段に配設された液１７は、上部を開放した箱状に
形成されており、その−側を酸素室５側に開放して前記
流路１４と連通させ、最下段の液ｆｆ１ｆ！７ａを除い
てオーバーフロー管１６を設けて液体酸ＩＩＬＯを順次
下段の液Ｍ７に流下させているもので、上下の隣接する
液溜７間は間隔１７を開けて配設される。The liquids 17 arranged in multiple stages above and below are formed in a box shape with an open top, and the - side thereof is opened to the oxygen chamber 5 side to communicate with the flow path 14, and the liquid ff1f! of the lowest stage is formed. An overflow pipe 16 is provided except for 7a to allow the liquid acid IILO to flow down sequentially to the lower liquid M7, and the upper and lower adjacent liquid reservoirs 7 are disposed with an interval 17 between them.
この液溜７ｆｔ！ｆｌの間隔１７により、液体酸素ＬＯ
は各液溜７で酸素室５の気体側に圧力を開放されて液体
酸素ＬＯの雰囲気圧力は全段同一となり、液深が小さく
なって液圧による波瀾の上昇がほとんど無くなり、凝縮
蒸発器１を高くすることが可能となる。This liquid reservoir is 7ft! The fl spacing 17 allows liquid oxygen LO
The pressure is released to the gas side of the oxygen chamber 5 in each liquid reservoir 7, so that the atmospheric pressure of liquid oxygen LO becomes the same in all stages, the liquid depth becomes small, there is almost no rise in ripples due to liquid pressure, and the condensing evaporator 1 It becomes possible to increase the
最上部の液溜７に導入された液体酸素１０の一部は、前
記流路１４に流入し、伝熱板１５及び仕切板４を介して
隣室の窒素室６を流れる窒素ガスＧＮと熱交換し、その
一部が蒸発して酸素ガスＧＯの気泡となり、液体酸素１
０と共に流路１４を上界後、端部１４ａで液体酸素ＬＯ
と分離して上昇し、蒸発しなかった液体酸素ＬＯは下方
に流下する。A part of the liquid oxygen 10 introduced into the uppermost liquid reservoir 7 flows into the flow path 14 and exchanges heat with the nitrogen gas GN flowing through the nitrogen chamber 6 in the adjacent room via the heat transfer plate 15 and the partition plate 4. Then, a part of it evaporates and becomes bubbles of oxygen gas GO, and liquid oxygen 1
After ascending the flow path 14 with 0, liquid oxygen LO at the end 14a
The liquid oxygen LO that is not evaporated flows downward.
また、残部の液体酸素ＬＯは、オーバーフロー管１６に
より順次下段の液溜７に流下して各流路１４に流入し、
各流路１４に流入する以上の液体酸素ＬＯは最下段の液
溜７ａの側壁からオーバーフローして流下する。In addition, the remaining liquid oxygen LO sequentially flows down to the lower liquid reservoir 7 through the overflow pipe 16 and flows into each flow path 14.
The liquid oxygen LO in excess of the amount flowing into each channel 14 overflows from the side wall of the lowermost liquid reservoir 7a and flows down.
各流路１４の傾斜角度は接続する液溜７の深さや流路１
４の長さ等により選定される。流路１４は水平に設ける
ことも可能であるが、水平よりも昇り勾配に設けた方が
蒸発生成した酸素ガスＧ。The inclination angle of each channel 14 is determined by the depth of the connected liquid reservoir 7 and the channel 1.
4. Selection is made based on the length, etc. Although it is possible to provide the flow path 14 horizontally, it is better to provide the flow path 14 on an upward slope rather than horizontally so that the evaporated oxygen gas G is produced.
の気泡がその浮上刃で流路１４から流出し易いとともに
、液体酸素ＬＯの流動を促進し、熱伝達率を高める。The floating blades make it easy for the bubbles to flow out of the channel 14, promoting the flow of liquid oxygen LO and increasing the heat transfer coefficient.
上記実施例では流路１４を昇り勾配に形成したので、蒸
発した酸素ガスＧｏの気泡がその浮上刃で液体酸素ＬＯ
の流動を促進して他端１４ａ側から流出する。そのため
、液体酸素１０の蒸発が効果的に行われ無駄に流下する
のを防止でき、蒸発した酸素ガスＧｏの滞留も生じない
ので凝縮蒸発器１の効率を向上させる。In the above embodiment, the flow path 14 is formed to have an upward slope, so that the bubbles of the evaporated oxygen gas Go flow into the liquid oxygen LO with the floating blades.
flows out from the other end 14a side. Therefore, the liquid oxygen 10 can be effectively evaporated and can be prevented from flowing down in vain, and the evaporated oxygen gas Go will not remain, thereby improving the efficiency of the condenser evaporator 1.
液体酸素ＬＯの各流路１４への流入量は、液溜７の液深
を調節すること、あるいは流路１４の流路長や傾斜ある
いは開口断面積を調節することにより行う。The amount of liquid oxygen LO flowing into each channel 14 is controlled by adjusting the liquid depth of the liquid reservoir 7, or by adjusting the channel length, inclination, or opening cross-sectional area of the channel 14.
尚、最上部の流路１４ｂ及び最下部の流路１４Ｃは一端
が閉じているのでこの部分の伝熱板１５としては流路１
４間が連通している有孔板等を用いて酸素ガスＧＯの滞
留を防止することが好ましい。Note that the uppermost channel 14b and the lowermost channel 14C are closed at one end, so the heat exchanger plate 15 in this part is the channel 1.
It is preferable to use a perforated plate or the like in which the four spaces are in communication to prevent the oxygen gas GO from stagnation.
第３図及び第４図（第４図は第３図のｒＶ−ＩＶ矢視図
である）に示す酸素室１８は、前記の最上部の流路１４
ｂ及び最下部の流路１４ｃを閉じるスラントバー１９を
配置して窒素室６と連通させ、酸素ガスＧＯの滞留部を
無くす例を示している。The oxygen chamber 18 shown in FIGS. 3 and 4 (FIG. 4 is a view taken along the rV-IV arrow in FIG. 3) is located at the uppermost channel 14.
An example is shown in which a slant bar 19 is arranged to close the flow path 14c at the lowermost portion of the flow path 14b and communicate with the nitrogen chamber 6, thereby eliminating a stagnation portion of the oxygen gas GO.
また第３図及び第４図に示す液溜２０は、上部に１１１
２１を有する側壁２０ａを斜辺と七だ逆台形状に形成さ
れ、該層２１から順次下段の液溜２０に液体酸素ＬＯを
流下させるもので、斜辺部の側壁２０ａで流下する液体
酸素し０を受けるとともに気体側に圧力を開放し、前述
のオーバーフロー管１６と同一のｉ能を有する。尚、第
３図に示すように酸素室にスラントバー１９を配置した
場合、液溜２０のオーバーフロ一手段を堰２１に限定す
るものではなく他の方法によっても良い。In addition, the liquid reservoir 20 shown in FIGS. 3 and 4 has a 111
The side wall 20a having 21 is formed in the shape of an inverted trapezoid with 7 vertices, and the liquid oxygen LO flows down from the layer 21 to the lower liquid reservoir 20 in order. It receives pressure and releases pressure to the gas side, and has the same function as the overflow pipe 16 described above. In addition, when the slant bar 19 is arranged in the oxygen chamber as shown in FIG. 3, the means for overflowing the liquid reservoir 20 is not limited to the weir 21, and other methods may be used.
第５図に示す酸素室２２は、液溜への液体酸素しＯの供
給方法の他の実施例を示している。酸素室２２の液体酸
素ＬＯの入口側端部に前述の液溜と同様に気体側に圧力
を開放された液″１ｌｌｆｆ２３を上下多段に設けてい
る。更に液溜２３の各々は連通管２５を介してマニホー
ルド管２４と連結されており、マニホールド管２４の上
端には液受け２６を設けている。６液１２３に供給する
液体酸素ＬＯを、液受け２６に供給することにより、マ
ニホールド管２４．３１通管２５を介して全ての液溜２
３に配分供給することができる。マニホールド管２４内
の液ヘッドによって、各液溜２３への供給量が異なるの
を防止し、均等邑を配分供給するために、連通管２５の
流路断面積を液ヘッドの高低相当分だけ増減させている
。上記手段によって液ヘッドによる沸点上昇の少ない液
体酸素ＬＯを酸素室２２に均等に供給することができる
。The oxygen chamber 22 shown in FIG. 5 shows another embodiment of the method of supplying liquid oxygen and O to the liquid reservoir. At the inlet side end of the liquid oxygen LO of the oxygen chamber 22, a liquid "1llff23" whose pressure is released to the gas side, similar to the aforementioned liquid reservoir, is provided in upper and lower stages in multiple stages. A liquid receiver 26 is provided at the upper end of the manifold pipe 24. By supplying the liquid oxygen LO to be supplied to the 6 liquid 123 to the liquid receiver 26, the manifold pipe 24. 31 to all liquid reservoirs 2 via the pipe 25
It can be distributed and supplied to 3. In order to prevent the amount of liquid supplied to each reservoir 23 from differing depending on the liquid head in the manifold pipe 24 and to distribute the amount evenly, the flow passage cross-sectional area of the communication pipe 25 is increased or decreased by the height of the liquid head. I'm letting you do it. By the above means, liquid oxygen LO whose boiling point does not increase due to the liquid head can be uniformly supplied to the oxygen chamber 22.
勿論、液溜２３への液媒供給手段を、液溜２３のオーバ
ーフローと連通管２５とを組合せて構成してもよい。Of course, the liquid medium supply means to the liquid reservoir 23 may be configured by combining the overflow of the liquid reservoir 23 and the communication pipe 25.
第６図及び第７図は、前記の凝縮蒸発器１を複精留塔に
設置した例を示すもので、第６図左側の凝縮蒸発器は酸
素室部分を、右側は窒素室部分を示しており、第７図は
第６図のＶｌ −ｖｔ断面を示している。 ・
凝縮蒸発器１は、複精留塔３０の上部塔３１と下部塔３
２を仕切る隔板３３上の窒素ガス主管３４を中心とした
円周上に４基並列に収納！ｉＱ置されており、酸素室５
及び液溜７は上部塔３１の気体空間３５に開放されてい
る。Figures 6 and 7 show an example in which the aforementioned condenser evaporator 1 is installed in a double rectification column. The condenser evaporator on the left side of Figure 6 shows the oxygen chamber part, and the right side shows the nitrogen chamber part. 7 shows the Vl-vt cross section of FIG. 6. - The condensing evaporator 1 includes an upper column 31 and a lower column 3 of a double rectification column 30.
4 units are housed in parallel on the circumference centered on the nitrogen gas main pipe 34 on the partition plate 33 that partitions the two! iQ is located, oxygen chamber 5
The liquid reservoir 7 is open to the gas space 35 of the upper column 31.
各凝縮蒸発器１と窒素ガス主管３４０間には各段一体に
連通する液溜７．７が配設され、最上部の液溜７には液
体酸素の導入管３６が挿入されている。A liquid reservoir 7.7 is provided between each condenser evaporator 1 and the nitrogen gas main pipe 340 and communicates with each stage, and a liquid oxygen introduction pipe 36 is inserted into the uppermost liquid reservoir 7.
窒素ガスＧＮは下部塔３２頂部から窒素ガス主管３４を
玉貸して各入口ヘッダ−８から窒素室６に導入され、酸
素室５の液体酸素ＬＯと熱交換して凝縮液化し、出口ヘ
ッダ−１０に集められて下部配管３７から導出される。Nitrogen gas GN is introduced into the nitrogen chamber 6 from each inlet header 8 through the nitrogen gas main pipe 34 from the top of the lower column 32, and is condensed and liquefied by exchanging heat with the liquid oxygen LO in the oxygen chamber 5, and then transferred to the outlet header 10. is collected and led out from the lower piping 37.
一方、上部塔３１の精留板３８最下段から導入管３６を
通って、凝縮蒸発器１の最上段の液溜７に流入した液体
酸素ＬＯは、前述のごとく一部が酸素室５の流路１４に
流入し、窒素室６の窒素ガスＧＮと熱交換して蒸発し、
酸素ガスＧＯとなり流路１４を流れて端部１４ａから流
出し、上部塔３１の上昇ガスとなるとともに、一部は製
品酸素ガスＧｏとして配管３８から採取される。On the other hand, as described above, part of the liquid oxygen LO that has flowed from the bottom of the rectifying plate 38 of the upper column 31 through the introduction pipe 36 into the liquid reservoir 7 at the top of the condensing evaporator 1 flows into the oxygen chamber 5. It flows into the passage 14, exchanges heat with the nitrogen gas GN in the nitrogen chamber 6, and evaporates.
The oxygen gas GO becomes oxygen gas GO, flows through the channel 14, flows out from the end 14a, becomes the ascending gas in the upper column 31, and a portion is collected from the pipe 38 as the product oxygen gas Go.
蒸発しない過剰の液体酸素ＬＯは流路１４の端部１４ａ
から流下し、隔板３３上に溜まり配管３９から導出され
、その一部は製品として採取され、他は液体酸素ポンプ
、あるいはサーモサイフオンリボイラー等によって揚上
され、上部の配管４０から再び液Ｍ７に循環される。Excess liquid oxygen LO that does not evaporate is stored at the end 14a of the flow path 14.
It flows down from the pipe 39 and accumulates on the partition plate 33, and is led out from the pipe 39. A part of it is collected as a product, and the other part is lifted up by a liquid oxygen pump or a thermosiphon-only boiler, and is returned to the liquid M7 from the pipe 40 at the top. is circulated.
前述のごとく液体酸素ＬＯは各液溜７から各流路１４に
流入して熱交換を行ない、それ以上の液体酸素ＬＯがオ
ーバーフロー管１６により順次下段の液溜７に流下する
もので、最下段の液溜７ａからは隔板３３上に流下する
。As mentioned above, liquid oxygen LO flows into each flow path 14 from each liquid reservoir 7 and undergoes heat exchange, and further liquid oxygen LO flows down to the lower liquid reservoir 7 through the overflow pipe 16, The liquid flows down onto the partition plate 33 from the liquid reservoir 7a.
また、液体酸素ＬＯが酸素室５内で完全に蒸発して、流
路１４にアチセレンが析出しないように、過剰な液体酸
素ＬＯを流して常時流路１４を液体酸素ＬＯで洗うこと
が好ましく、過剰の液体酸素ＬＯが流下していることを
知るために、隔板３３上に溜まっている液体酸素１０の
量を液面計４１により計測する。Further, in order to prevent liquid oxygen LO from completely evaporating in the oxygen chamber 5 and atyselene from precipitating in the flow path 14, it is preferable to constantly wash the flow path 14 with liquid oxygen LO by flowing an excess of liquid oxygen LO. In order to know that excess liquid oxygen LO is flowing down, the amount of liquid oxygen 10 accumulated on the partition plate 33 is measured by the liquid level gauge 41.
このように、液体酸素を流下させるので、液圧による液
温上昇がなく、窒素ガスの凝縮温度を低下させて下部塔
の運転圧力を低減でき、原料空気圧縮機の動力費を低減
する。In this way, since the liquid oxygen is allowed to flow down, there is no rise in liquid temperature due to liquid pressure, and the condensation temperature of nitrogen gas can be lowered to reduce the operating pressure of the lower column, reducing the power cost of the raw air compressor.
また凝縮蒸発器の高さを高くし、伝熱面積を大ぎくでき
るので、より能力の高いものを精留塔の径内に納めるこ
とができ、複精留塔の製作を容易にする。Furthermore, since the height of the condensing evaporator can be increased and the heat transfer area can be increased, a device with higher capacity can be accommodated within the diameter of the rectifying column, making it easier to manufacture a double rectifying column.
さらにまた起動時上部塔を流下してきた液化ガスを流入
させると同時に凝縮と蒸発を生じるので、起動時間が大
幅に短縮され、この間の動力費を削減できる。Furthermore, since condensation and evaporation occur at the same time as the liquefied gas that has flowed down the upper column is introduced at the time of startup, startup time is significantly shortened and power costs during this time can be reduced.
尚、空気液化分離における液体酸素と窒素ガスとの熱交
換による蒸発と凝縮以外の、他の液媒と流体を用いた場
合も同様の作用効果を得られるものである。Note that similar effects can be obtained when using other liquid media and fluids than evaporation and condensation through heat exchange between liquid oxygen and nitrogen gas in air liquefaction separation.
本発明は以上説明したように第一流体室の液媒と第二流
体室の流体とで熱交換を行なう凝縮蒸発器の第一流体室
に、上下多段に流路を設け、該流路の一端側に前記流路
と連通する液溜を上下多段に設けるとともに、液媒を各
段の液溜に供給させながら前記流路に導入して熱交換さ
せるので、液媒の液深が僅少となり液圧による温度上昇
がなくなり、凝縮蒸発器の効率を向上させ、第二流体室
側の流体の凝縮温度を低下させて運転圧力を低減するこ
とにより、動力費を削減できる。As explained above, the present invention provides a first fluid chamber of a condensing evaporator in which heat exchange is performed between a liquid medium in a first fluid chamber and a fluid in a second fluid chamber, and a flow path is provided in upper and lower stages in multiple stages. At one end side, liquid reservoirs communicating with the flow path are provided in multiple stages above and below, and the liquid medium is introduced into the flow path and heat exchanged while being supplied to the liquid reservoirs at each stage, so that the liquid depth of the liquid medium is small. There is no temperature rise due to liquid pressure, the efficiency of the condensing evaporator is improved, the condensing temperature of the fluid in the second fluid chamber is lowered, and the operating pressure is reduced, thereby reducing power costs.
また凝縮蒸発器の高さ方向の形状的制限が無くなり長尺
にすることで処理能力増加が可能になつた。その結果凝
縮蒸発器を収納する容器径を精留塔と同一とすることが
可能となり大型空気分離装置用精留塔でも上下部塔を上
下一体構造で製作することが可能となった。In addition, there are no restrictions on the shape of the condenser-evaporator in the height direction, making it possible to increase the throughput by making it longer. As a result, it became possible to make the diameter of the container housing the condensing evaporator the same as that of the rectification column, and even in the case of a rectification column for large-scale air separation equipment, it became possible to manufacture the upper and lower columns in an integrated structure.
さらに、液媒中に浸漬する必要がないため、起動時間を
短縮できる。Furthermore, since there is no need to immerse the device in a liquid medium, startup time can be shortened.
第１図及び第２図は本発明の一実滴例を示すもので、第
１図は凝縮蒸発器の一部を切欠いて示す斜視図、第２図
は第一流体室である酸素室の断面図、第３図及び第４図
は本発明の他の実施例を示すもので、第３図は酸素室の
断面図、第４図は第３図の■−ＩＶ矢視図、第５図は本
発明の更に他の実施例を示す酸素室の断面図、第６図及
び第７図は本発明の凝縮蒸発器を複精留塔に用いた例を
示すもので、第６図は精留塔の要部断面図、第７図は第
６図のＶｌ −Ｖｌ断面図である。
１・・・凝縮蒸発器 ４・・・仕切板 ５・・・酸
素室（第一流体室） ６・・・窒素室（第二流体室）
７・・・液溜 １４・・・流路 １５・・・伝熱
板１６・・・オーバーフロー管 ２４・・・マニホー
ルド管 ＧＮ・・・窒素ガス Ｇｏ・・・酸素ガス
ＬＮ・・・液体窒素 ＬＯ・・・液体酸素特 許 出
願 人 日本酸素株式会社溌１園
第６区
憩
秀７因
並Figures 1 and 2 show an example of an actual droplet of the present invention. Figure 1 is a partially cutaway perspective view of the condenser evaporator, and Figure 2 is a perspective view of the oxygen chamber, which is the first fluid chamber. 3 and 4 show other embodiments of the present invention, in which FIG. 3 is a sectional view of the oxygen chamber, FIG. The figure is a sectional view of an oxygen chamber showing still another embodiment of the present invention, and Figures 6 and 7 are examples of using the condensing evaporator of the present invention in a double rectification column. FIG. 7 is a sectional view of the main part of the rectification column, and is a sectional view taken along the line Vl--Vl in FIG. 6. 1... Condensing evaporator 4... Partition plate 5... Oxygen chamber (first fluid chamber) 6... Nitrogen chamber (second fluid chamber)
7...Liquid reservoir 14...Flow path 15...Heat exchange plate 16...Overflow tube 24...Manifold tube GN...Nitrogen gas Go...Oxygen gas LN...Liquid nitrogen LO ...Liquid oxygen patent applicant Nihon Sanso Co., Ltd.
Claims (1)
とを交互に形成し、前記第一流体室の液媒と、前記第二
流体室の流体とで熱交換を行なう凝縮蒸発器において、
前記第一流体室に上下多段に複数の伝熱板を配置して液
媒の流路を形成し、該流路の一端は開放とし、他端側に
該流路と連通し、上部を開放した複数の液溜を上下多段
に設けるとともに、液媒を各段の液溜に供給させながら
前記流路に導入して熱交換させるように構成したことを
特徴とする凝縮蒸発器。 ２、前記液媒の流路は、液溜側の一端から他端先端に向
って昇り勾配を有していることを特徴とする特許請求の
範囲第１項記載の凝縮蒸発器。[Claims] 1. First fluid chambers and second fluid chambers are formed alternately by a large number of vertical partition plates, and the liquid medium in the first fluid chamber and the fluid in the second fluid chamber are formed alternately. In a condensing evaporator that performs heat exchange,
A plurality of heat transfer plates are arranged in upper and lower stages in the first fluid chamber to form a flow path for the liquid medium, one end of the flow path is open, the other end communicates with the flow path, and the upper part is open. A condensing evaporator characterized in that a plurality of liquid reservoirs are provided in upper and lower stages, and a liquid medium is introduced into the flow path while being supplied to the liquid reservoirs in each stage for heat exchange. 2. The condensing evaporator according to claim 1, wherein the liquid medium flow path has an upward slope from one end on the liquid reservoir side to the tip of the other end.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP32904987A JPH0668434B2 (en) | 1986-12-26 | 1987-12-24 | Evaporator |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61-314781 | 1986-12-26 | ||
| JP31478186 | 1986-12-26 | ||
| JP32904987A JPH0668434B2 (en) | 1986-12-26 | 1987-12-24 | Evaporator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63267877A true JPS63267877A (en) | 1988-11-04 |
| JPH0668434B2 JPH0668434B2 (en) | 1994-08-31 |
Family
ID=26568072
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP32904987A Expired - Lifetime JPH0668434B2 (en) | 1986-12-26 | 1987-12-24 | Evaporator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0668434B2 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1990000243A1 (en) * | 1988-07-04 | 1990-01-11 | Japan Oxygen Co., Ltd. | Condenser/evaporator |
| EP0607006B1 (en) * | 1993-01-11 | 1996-12-11 | KABUSHIKI KAISHA KOBE SEIKO SHO also known as Kobe Steel Ltd. | Plate fin heat exchanger built-in type multi-stage thermosiphon |
| JP2003535301A (en) * | 2000-05-31 | 2003-11-25 | リンデ アクチエンゲゼルシヤフト | Multi-stage condenser |
| CN104390428A (en) * | 2014-12-01 | 2015-03-04 | 杭州福斯达实业集团有限公司 | Large efficient condensation evaporator |
| WO2020045662A1 (en) * | 2018-08-30 | 2020-03-05 | 国立大学法人佐賀大学 | Heat exchanger |
| JP2021096028A (en) * | 2019-12-17 | 2021-06-24 | 大陽日酸株式会社 | Multistage liquid reservoir type condensation evaporator, and air separation device with the multistage liquid reservoir type condensation evaporator |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08182714A (en) * | 1994-12-28 | 1996-07-16 | Mutsumi Tekunika:Kk | Coffin for burying small animal |
-
1987
- 1987-12-24 JP JP32904987A patent/JPH0668434B2/en not_active Expired - Lifetime
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1990000243A1 (en) * | 1988-07-04 | 1990-01-11 | Japan Oxygen Co., Ltd. | Condenser/evaporator |
| US5222549A (en) * | 1988-07-04 | 1993-06-29 | Japan Oxygen Co., Ltd. | Condenser/evaporator |
| EP0607006B1 (en) * | 1993-01-11 | 1996-12-11 | KABUSHIKI KAISHA KOBE SEIKO SHO also known as Kobe Steel Ltd. | Plate fin heat exchanger built-in type multi-stage thermosiphon |
| JP2003535301A (en) * | 2000-05-31 | 2003-11-25 | リンデ アクチエンゲゼルシヤフト | Multi-stage condenser |
| CN104390428A (en) * | 2014-12-01 | 2015-03-04 | 杭州福斯达实业集团有限公司 | Large efficient condensation evaporator |
| WO2020045662A1 (en) * | 2018-08-30 | 2020-03-05 | 国立大学法人佐賀大学 | Heat exchanger |
| JP2020034234A (en) * | 2018-08-30 | 2020-03-05 | 国立大学法人佐賀大学 | Heat exchanger |
| JP2021096028A (en) * | 2019-12-17 | 2021-06-24 | 大陽日酸株式会社 | Multistage liquid reservoir type condensation evaporator, and air separation device with the multistage liquid reservoir type condensation evaporator |
| WO2021125224A1 (en) * | 2019-12-17 | 2021-06-24 | 大陽日酸株式会社 | Multi-level liquid reservoir-type condensation evaporator, and air separation device equipped with multi-level liquid reservoir-type condensation evaporator |
| CN114787570A (en) * | 2019-12-17 | 2022-07-22 | 大阳日酸株式会社 | Multi-stage liquid storage type condensation evaporator and air separation device with same |
| CN114787570B (en) * | 2019-12-17 | 2024-05-24 | 大阳日酸株式会社 | Multistage liquid storage type condensation evaporator and air separation device with same |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0668434B2 (en) | 1994-08-31 |
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