JPS6238080Y2 - - Google Patents
Info
- Publication number
- JPS6238080Y2 JPS6238080Y2 JP14521082U JP14521082U JPS6238080Y2 JP S6238080 Y2 JPS6238080 Y2 JP S6238080Y2 JP 14521082 U JP14521082 U JP 14521082U JP 14521082 U JP14521082 U JP 14521082U JP S6238080 Y2 JPS6238080 Y2 JP S6238080Y2
- Authority
- JP
- Japan
- Prior art keywords
- passage
- liquefied gas
- heat exchanger
- section
- heat
- 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.)
- Expired
Links
- 239000007788 liquid Substances 0.000 claims description 10
- 238000005192 partition Methods 0.000 claims description 5
- 239000007789 gas Substances 0.000 description 22
- 239000003949 liquefied natural gas Substances 0.000 description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 14
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- 238000009835 boiling Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 239000003345 natural gas Substances 0.000 description 5
- 230000008016 vaporization Effects 0.000 description 5
- 239000001294 propane Substances 0.000 description 4
- -1 evaporates Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000001747 exhibiting effect Effects 0.000 description 1
- NBVXSUQYWXRMNV-UHFFFAOYSA-N fluoromethane Chemical compound FC NBVXSUQYWXRMNV-UHFFFAOYSA-N 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000013526 supercooled liquid Substances 0.000 description 1
Landscapes
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Description
【考案の詳細な説明】
利用産業分野
この考案は、液化ガスの冷熱利用プラント、例
えば、空気分離、発電プラント等に使用する熱交
換器の改良に係り、液化ガス中の成分を全て完全
に気化させる共に圧力損失の増加もなく、長期の
連続運転が可能な液化ガス用熱交換器に関する。[Detailed description of the invention] Industrial field of application This invention relates to the improvement of heat exchangers used in plants that use liquefied gas as cold energy, such as air separation and power generation plants. The present invention relates to a heat exchanger for liquefied gas that can be operated continuously for a long period of time without increasing pressure loss.
背景技術
近年、重要なエネルギー源として天然ガスの利
用が盛んであり、天然ガスの輸送に至便なように
液化されているが、省エネルギーに鑑みこれを気
化させる際に放出される膨大な冷熱を積極的に利
用する冷熱利用プラントが各種開発されている。
空気分離、発電プラント等がその代表的なもので
ある。Background technology In recent years, natural gas has been widely used as an important energy source, and it is liquefied for convenient transportation.However, in order to save energy, the enormous amount of cold energy released when vaporizing this gas has been actively used. Various types of cold energy utilization plants have been developed.
Typical examples include air separation and power generation plants.
かかるプラントで熱交換される液化天然ガス
は、過冷液、蒸発、ガスに変化しているが、液化
ガスに含まれる重質成分の影響により、熱交換器
における中間温度が運転時間とともにふらついた
り、圧力損失が増加してプラントの連続運転が短
期間しかできない等の問題があり、運転効率や熱
効率の上で、液化天然ガスの気化用熱交換器の改
善が強く要望されていた。 The liquefied natural gas that is heat exchanged in such plants changes into supercooled liquid, evaporates, and gas, but due to the influence of heavy components contained in the liquefied gas, the intermediate temperature in the heat exchanger fluctuates over the operating time. However, there have been problems such as increased pressure loss and the ability to operate the plant continuously for only a short period of time, and there has been a strong demand for improvements in heat exchangers for vaporizing liquefied natural gas in terms of operating efficiency and thermal efficiency.
従来技術の問題点
上述した熱交換器における中間温度のふらつき
や圧損の増加した問題を調査したところ、液化天
然ガスにはメタン（C1）、エタン（C2）、プロパ
ン（C3）、ブタン（C4）〜（C12）の炭化水素が混
合した状態で含有されているため、これを従来の
熱交換器である液化天然ガスを下注し気化上昇し
て流出させる、所謂アツプ・フロー・パスの熱交
換器に通した場合、液化天然ガスに含有される高
沸点成分（重質成分）は完全に蒸発しきれずに、
熱交換器中に滞留し、また一部は付着し、圧損を
増加させていることが分つた。Problems with the Prior Art When investigating the problems of fluctuations in intermediate temperature and increased pressure loss in the heat exchangers described above, it was found that liquefied natural gas contains a mixture of hydrocarbons, namely methane ( C1 ), ethane ( C2 ), propane ( C3 ), and butane ( C4 ) to ( C12 ), and therefore when this is passed through a conventional heat exchanger, a so-called up-flow path heat exchanger in which liquefied natural gas is poured downward and vaporized and rises before flowing out, the high boiling point components (heavy components) contained in the liquefied natural gas do not completely evaporate, and
It was found that the oil remained in the heat exchanger and some of it adhered to the heat exchanger, causing an increase in pressure loss.
考案の目的
この考案は、液化ガス冷熱利用プラントにおけ
る液化ガスの気化用熱交換器の熱効率を向上させ
ることを目的とし、また、液化ガス成分の完全気
化が可能で、圧力損失の増大がなく、長期の連続
運転が可能な液化ガス用熱交換器を目的としてい
る。Purpose of the invention The purpose of this invention is to improve the thermal efficiency of a heat exchanger for vaporizing liquefied gas in a liquefied gas cold energy utilization plant, and also to completely vaporize the liquefied gas component without increasing pressure loss. The purpose is a heat exchanger for liquefied gas that can be operated continuously for a long period of time.
考案の開示
この考案は、液化ガス成分の完全気化が可能な
構成の熱交換器を目的に種々検討した結果、従来
のアツプ・フロー・パスの熱交換器において、蒸
発ゾーンで残液の中に、ほとんど低沸点成分のメ
タン（C1）がなくなる温度付近でガス流との間に
スリツプ現象を起し、熱交換器の通路中に滞留
し、伝熱面効率が低下し、また、時間と共に蓄積
され圧損を増加させていることに着目し、液化天
然ガスを過冷域及び一部蒸発域については、コー
ルドセクシヨンをアツプ・フローさせて高沸点成
分を液中に含有させたまま流出させ、続いてウオ
ームセクシヨンをダウン・フローさせる構成とす
ることにより、高沸点成分を完全に蒸発させ得る
熱交換器が得られることを知見し、この考案を完
成したものである。Disclosure of the invention As a result of various studies aimed at creating a heat exchanger with a configuration that allows complete vaporization of liquefied gas components, this invention was developed as a result of various studies aimed at creating a heat exchanger with a configuration that allows complete vaporization of liquefied gas components. , near the temperature where methane (C 1 ), a low-boiling point component, almost disappears, a slip phenomenon occurs between the gas flow and the gas flow, which accumulates in the passage of the heat exchanger, reducing the heat transfer surface efficiency, and also increases over time. Focusing on the fact that liquefied natural gas accumulates and increases the pressure drop, in the subcooled region and partial evaporation region, the cold section is made to flow up and the high boiling point components are allowed to flow out while remaining in the liquid. Then, he found that by constructing the worm section to have a down flow, it was possible to obtain a heat exchanger that could completely evaporate high-boiling components, and this idea was completed.
考案の構成
すなわち、この考案は、
液の出入口を除いた周囲をサイドバーで囲い、
その内部に波形フインを挿入した熱媒通路と液化
ガス通路とを仕切板を介して交互に積層したプレ
ートフイン型熱交換器において、
重質成分を含む液化ガスの通路が仕切バーで区
分され、
液化ガスを下から流入させて通路内を上昇させ
ながら隣接通路の熱媒と向流熱交換させて上から
流出するコールドセクシヨンと、
コールドセクシヨンから流出した液化ガスを上
から流入して通路内を降下させながら隣接通路の
熱媒と並流熱交換させて気化させ下方より流出さ
せるウオームセクシヨンとの２セクシヨンから構
成され、
コールドセクシヨンの上部にウオームセクシヨ
ンを配置したことを特徴とする液化ガス用熱交換
器である。Structure of the device In other words, this device surrounds the area except for the liquid inlet and outlet with a side bar,
In a plate-fin type heat exchanger in which heat medium passages with corrugated fins inserted therein and liquefied gas passages are alternately stacked with partition plates interposed in between, the passage for liquefied gas containing heavy components is divided by partition bars. A cold section in which liquefied gas flows in from below and rises in the passage while exchanging countercurrent heat with the heat medium in the adjacent passage and flows out from above; and a cold section in which liquefied gas flowing out from the cold section flows in from above into the passage. It consists of two sections: a worm section, which exchanges heat with the heat medium in an adjacent passage in parallel while descending inside, vaporizes it, and flows out from below.The worm section is located above the cold section. This is a heat exchanger for liquefied gas.
液化天然ガスと熱交換する媒体には、上述の冷
熱利用プラントに応じて選定し、熱交換器内の通
路も向流型あるいは並流型を適宜選定するが、例
えば、熱媒がプロパン、フロン等の単一成分の場
合に、そのクーリングカーブより一部並流型が可
能である場合には、この考案による熱交換器が特
に有効であり、熱交換器を１つのコアより構成で
き、例えば、実施例に示すごとく、１つのコアの
液化天然ガスの通路を上下に２分してコールド、
ウオームの各セクシヨンに構成できる。 The medium for heat exchange with liquefied natural gas is selected depending on the above-mentioned cold energy utilization plant, and the passages in the heat exchanger are appropriately selected from countercurrent type or cocurrent type. For example, if the heating medium is propane or fluorocarbon The heat exchanger according to this invention is particularly effective in the case of a single component such as, for example, when a parallel flow type is possible due to its cooling curve. , As shown in the example, the liquefied natural gas passage of one core is divided into upper and lower halves and cold,
Each section of the worm can be configured.
考案の図面に基づく開示
第１図は熱媒にプロパンを使用した熱交換器の
フロー図であり、第２図はコアの要部（Ａ，Ｂ通
路）を示す一部破断斜視図である。第３図は流路
の断面説明図である。Disclosure Based on Drawings of the Invention FIG. 1 is a flow diagram of a heat exchanger using propane as a heat medium, and FIG. 2 is a partially cutaway perspective view showing the main parts of the core (paths A and B). FIG. 3 is a cross-sectional explanatory diagram of the flow path.
ここでは、液の出入口を除いた周囲をサイドバ
ーで囲い、その内部に波形フインを挿入した熱媒
通路と液化ガス通路とを仕切板を介して交互に積
層したアルミ・プレートフイン型熱交換器コア１
を用いて、液化天然ガスが通過するコールドセク
シヨンとウオームセクシヨンを構成してある。 Here, the aluminum plate fin type heat exchanger is surrounded by a side bar except for the liquid inlet/outlet, and a heat medium passage with corrugated fins inserted inside the side bar and a liquefied gas passage are alternately stacked with a partition plate interposed therebetween. core 1
The cold section and warm section, through which liquefied natural gas passes, are constructed using
このコア１には２通路、すなわち、液化天然ガ
ス（LNG）のＡ通路、熱媒（PG）のＢ通路の２
通路を設け、Ａ通路を上下に２分して、上部をウ
オームセクシヨン、下部をコールドセクシヨンに
構成してある。 This core 1 has two passages, namely passage A for liquefied natural gas (LNG) and passage B for heating medium (PG).
A passage is provided, and passage A is divided into upper and lower parts, with the upper section being a warm section and the lower section being a cold section.
作用・効果
まず、液化天然ガスはコア１のコールドセクシ
ヨンのＡ通路に下注されて、気化上昇して中央ヘ
ツダより流出し、ついで連結管を通して上部ヘツ
ダよりウオームセクシヨンのＡ通路に上注され、
気化降下して完全な天然ガス（NG）として他の
中央ヘツダより流出する。Function/Effect First, liquefied natural gas is injected into the A passage of the cold section of core 1, vaporized and rises, and flows out from the central header.Then, it is injected upward from the upper header through the connecting pipe into the A passage of the warm section. is,
It vaporizes and flows out as pure natural gas (NG) from the other central header.
この間、熱媒はコア１のＢ通路に上注され、液
化天然ガスと並流及び向流で熱交換し凝縮されて
下部ヘツダより流出する。 During this time, the heating medium is injected into the B passage of the core 1, exchanges heat with the liquefied natural gas in parallel and countercurrent, is condensed, and flows out from the lower header.
第４図に示すように、この考案の熱交換器では
液化ガスを低沸点成分の残存した液残しの状態
で、中間部のコールドセクシヨン出口から取り出
し、ウオームセクシヨン上端より流入することに
より、下向きの流れとなつて熱媒と熱交換するの
で、熱交換器通路内に高沸点成分（重質分）が滞
留したり、壁に付着することがなく、出口まで気
液混合成分の状態で流れるため、液化ガス中の成
分は全て完全に気化すると共に、圧力損失の増加
もなく、所定の性能を発揮し長期の連続運転が可
能となる。 As shown in Fig. 4, in the heat exchanger of this invention, the liquefied gas is taken out from the outlet of the cold section in the middle section in the form of a liquid residue containing residual low-boiling components, and is introduced from the upper end of the worm section. Since the flow is downward and heat is exchanged with the heating medium, high boiling point components (heavy components) do not remain in the heat exchanger passage or adhere to the walls, and the gas-liquid mixed components remain until the outlet. Because of the flow, all the components in the liquefied gas are completely vaporized, and there is no increase in pressure loss, allowing for long-term continuous operation while exhibiting the desired performance.
実施例
前述した第２図から第４図に示す構成からなる
この考案による熱交換器において、液化天然ガス
と熱媒の気液状態を分析した結果、
液化天然ガスは
コールドセクシヨン入口で−157℃、
液体率（液体／全量wt％）100％、
コールドセクシヨンとウオームセクシヨンとの中
間点で−70℃、12％、
そしてウオームセクシヨン出口で−31℃、0.1％
であつた。Example As a result of analyzing the gas-liquid state of the liquefied natural gas and the heating medium in the heat exchanger according to this invention having the configuration shown in FIGS. 2 to 4 described above, it was found that the liquefied natural gas is -157 °C, liquid percentage (liquid/total wt%) 100%, -70 °C, 12% at the midpoint between the cold and warm sections, and -31 °C, 0.1% at the warm section exit.
It was hot.
一方、熱媒は、 Ｂ通路の上部ヘツダ前で−21℃のガスであり、 Ｂ通路出口で−29℃、液体率100％であつた。 On the other hand, the heating medium is The gas is at -21℃ in front of the upper header of passage B. At the exit of passage B, the temperature was -29°C and the liquid content was 100%.
また、液化天然ガスと熱媒とのＴ−ｉ線図を第
３図に示す。 Moreover, a Ti diagram of liquefied natural gas and a heat medium is shown in FIG.
上記結果より明らかなように、この考案の熱交
換器によつて液化天然ガスが完全に気化され、熱
交換器の圧損を発生させることなく、プラントの
連続運転が可能なことが分る。 As is clear from the above results, the liquefied natural gas is completely vaporized by the heat exchanger of this invention, and the plant can be operated continuously without causing pressure loss in the heat exchanger.
第１図はこの考案による実施例を示すフロー図
てあり、第２図はコアのＡ，Ｂ通路を示す一部破
断斜視図で、第３図はコアのＡ，Ｂ通路の流路断
面図である。第４図は実施例における液化天然ガ
スと熱媒とのエンタルピー（ｉ）と温度（℃）と
の関係を示すＴ−ｉ線図である。
図中、１……コア、Ａ，Ｂ……通路、LNG…
…液化天然ガス、PG……熱媒、NG……天然ガ
ス、LPG……プロパン。
Fig. 1 is a flowchart showing an embodiment of this invention, Fig. 2 is a partially cutaway perspective view showing passages A and B of the core, and Fig. 3 is a sectional view of passages A and B of the core. It is. FIG. 4 is a T-i diagram showing the relationship between enthalpy (i) and temperature (° C.) of liquefied natural gas and heat medium in the example. In the diagram, 1... Core, A, B... Passage, LNG...
...Liquefied natural gas, PG...Heating medium, NG...Natural gas, LPG...Propane.
Claims (1)
その内部に波形フインを挿入した熱媒通路と液化
ガス通路とを仕切板を介して交互に積層したプレ
ートフイン型熱交換器において、 重質成分を含む液化ガスの通路が仕切バーで区
分され、 液化ガスを下から流入させて通路内を上昇させ
ながら隣接通路の熱媒と向流熱交換させて上から
流出するコールドセクシヨンと、 コールドセクシヨンから流出した液化ガスを上
から流入して通路内を降下させながら隣接通路の
熱媒と並流熱交換させて気化させ下方より流出さ
せるウオームセクシヨンとの２セクシヨンから構
成され、 コールドセクシヨンの上部にウオームセクシヨ
ンを配置したことを特徴とする液化ガス用熱交換
器。[Scope of claim for utility model registration] Surrounding the area excluding the liquid entrance and exit with a side bar,
In a plate-fin type heat exchanger in which heat medium passages with corrugated fins inserted therein and liquefied gas passages are alternately stacked with partition plates interposed in between, the passage for liquefied gas containing heavy components is divided by partition bars. A cold section in which liquefied gas flows in from below and rises in the passage while exchanging countercurrent heat with the heat medium in the adjacent passage and flows out from above; and a cold section in which liquefied gas flowing out from the cold section flows in from above into the passage. It consists of two sections: a worm section, which exchanges heat with the heat medium in an adjacent passage in parallel while descending inside, vaporizes it, and flows out from below.The worm section is located above the cold section. A heat exchanger for liquefied gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14521082U JPS5955272U (en) | 1982-09-25 | 1982-09-25 | Heat exchanger for liquefied gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14521082U JPS5955272U (en) | 1982-09-25 | 1982-09-25 | Heat exchanger for liquefied gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5955272U JPS5955272U (en) | 1984-04-11 |
| JPS6238080Y2 true JPS6238080Y2 (en) | 1987-09-29 |
Family
ID=30323588
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP14521082U Granted JPS5955272U (en) | 1982-09-25 | 1982-09-25 | Heat exchanger for liquefied gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5955272U (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6839975B2 (en) * | 2015-12-28 | 2021-03-10 | 株式会社神戸製鋼所 | Intermediate medium vaporizer |
-
1982
- 1982-09-25 JP JP14521082U patent/JPS5955272U/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5955272U (en) | 1984-04-11 |
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