JPH031592B2 - - Google Patents
Info
- Publication number
- JPH031592B2 JPH031592B2 JP61278111A JP27811186A JPH031592B2 JP H031592 B2 JPH031592 B2 JP H031592B2 JP 61278111 A JP61278111 A JP 61278111A JP 27811186 A JP27811186 A JP 27811186A JP H031592 B2 JPH031592 B2 JP H031592B2
- Authority
- JP
- Japan
- Prior art keywords
- heat exchanger
- tube
- tubes
- exchanger tube
- 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.)
- Expired - Lifetime
Links
Classifications
-
- 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
- F28D1/00—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, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators
- F28D1/02—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, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid
- F28D1/04—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, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits
- F28D1/047—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, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits the conduits being bent, e.g. in a serpentine or zig-zag
- F28D1/0477—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, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits the conduits being bent, e.g. in a serpentine or zig-zag the conduits being bent in a serpentine or zig-zag
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
この発明は空気調和機等の凝縮器や蒸発器とし
て使用されるクロスフインチユーブ式の熱交換器
に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a cross-finch tube heat exchanger used as a condenser or evaporator in an air conditioner or the like.
一般にクロスフインチユーブ式の熱交換器は、
第６図に示されているように、複数の平板状フイ
ンを所定の間隔をもつて互いに平行に配列してな
るフイン群１と、このフイン群１に対してほぼ直
交状に挿通される伝熱管２とで構成され、比較的
小形の空気調和機等においては、同一管径の伝熱
管２を用いた所謂１パス方式が採用されている。
In general, cross-finch tube heat exchangers are
As shown in FIG. 6, there is a fin group 1 formed by arranging a plurality of flat fins parallel to each other at predetermined intervals, and a transmission line inserted approximately perpendicularly to the fin group 1. In relatively small air conditioners and the like, a so-called one-pass method using heat transfer tubes 2 having the same tube diameter is adopted.
ところで、この種の熱交換器を凝縮器とした場
合、冷媒は第７図のように変化する。すなわち、
入口側においては過熱ガスの状態で空気との熱交
換が行なわれて温度T1からT2へ変化し、温度T2
の状態で熱交換とともに相変化が行なわれてガス
は液体となり、液成分の割合が徐々に増加し、出
口側に至ると液体となつて温度がT3にまで低下
する。この相変化に関連して、流体の速度は入口
側ではきわめて速く、出口側で遅くなるととも
に、液溜り状態となる傾向を示す。そこで、一般
に管径を細くすると液体速度が速くなつて熱伝道
率が大きくなるとともに液溜りが少なくなり、し
たがつて熱通過率が大きく熱交換上好ましい反
面、圧力損失が増大して冷凍サイクルの総合効率
を悪くするという面を併せもつことになる。他
方、管径が太い場合には圧力損失は比較的低く抑
えられるが、熱交換器内の冷媒量が増大するとと
もに、特に出口側の流体速度の遅い部分で液溜り
が発生するため、これがコンプレツサを制約しそ
の小形軽量化の妨げとなり、また、熱通過率も悪
くなる。 By the way, when this type of heat exchanger is used as a condenser, the refrigerant changes as shown in FIG. That is,
On the inlet side, the superheated gas exchanges heat with the air, changing the temperature from T 1 to T 2 , and the temperature T 2
In this state, a phase change occurs along with heat exchange, and the gas becomes a liquid, and the proportion of the liquid component gradually increases until it reaches the outlet, where it becomes a liquid and the temperature drops to T 3 . In connection with this phase change, the velocity of the fluid is extremely high on the inlet side, slows down on the outlet side, and tends to form a puddle. Therefore, generally speaking, when the pipe diameter is made smaller, the liquid velocity increases, the heat transfer rate increases, and the amount of liquid pools decreases.Therefore, while the heat transfer rate is high and is favorable for heat exchange, on the other hand, the pressure loss increases and the refrigeration cycle deteriorates. This also has the effect of deteriorating overall efficiency. On the other hand, if the pipe diameter is large, the pressure loss can be kept relatively low, but the amount of refrigerant in the heat exchanger increases and a pool of liquid occurs, especially at the outlet side where the fluid velocity is low. This restricts the size and weight of the product, and also impairs the heat transfer rate.
そこで、少し大きな空気調和機においては、第
８図に示されているように、気体および気相成分
の多い入口側に例えば２つの伝熱管２ａ，２ｂを
並列配管し、液体および液相成分が多くなるその
途中部位で１本の伝熱管２ｃにするという所謂２
パス−１パス方式を採用するようにしている。 Therefore, in a slightly larger air conditioner, for example, two heat transfer tubes 2a and 2b are installed in parallel on the inlet side where there are many gases and gas phase components, as shown in FIG. The so-called 2 process in which a single heat exchanger tube 2c is used at the middle part where the number of tubes increases
A pass-one pass method is adopted.
この２パス−１パス方式によれば、理論的には
管径が細い場合と太い場合の各利点が引出される
ことになるが、実際の設計段階において既存の管
径のものの中から適正な管径のものを組合せるこ
とが難しい許りでなく、途中で１パスにするため
の配慮が必要であり、したがつて配管の自由度が
制約されるとともに、コストアツプは免れない。
また、第６図に示した従来例をも含めて言えるこ
とであるが、同一径の伝熱管を２列配置する関係
上、フイン巾もそれなりに大きくなり熱交換器の
小形化を図るにも自ずた限界があつた。
According to this 2-pass - 1-pass method, the advantages of small and large pipe diameters can be theoretically brought out, but in the actual design stage, it is necessary to choose the appropriate diameter from among the existing pipe diameters. It is difficult to combine pipe diameters, and consideration must be given to one pass along the way, which limits the freedom of piping and inevitably increases costs.
In addition, this also applies to the conventional example shown in Fig. 6, but since two rows of heat exchanger tubes of the same diameter are arranged, the fin width becomes relatively large, making it difficult to downsize the heat exchanger. There was a natural limit.
上記した従来の欠点を解決するため、この発明
においては、冷媒中の液体および気液二相流の液
相成分が多い部分には比較的管径の細い伝熱管を
使用し、他方、冷媒の気体および気液二相流の気
相成分の多い部分にはそれよりも管径の太い伝熱
管を用いるようにしている。
In order to solve the above-mentioned conventional drawbacks, in the present invention, a heat transfer tube with a relatively small diameter is used for the liquid in the refrigerant and the liquid phase component of the gas-liquid two-phase flow. Heat exchanger tubes with larger diameters are used in portions of the gas and gas-liquid two-phase flow where the gas phase component is large.
上記のように伝熱管の管径をその途中から変化
させることにより、圧力損失による影響は非常に
小さくなる一方、液溜りも減少し、冷凍サイクル
の全体の冷媒量も少なくし得るため、熱交換率の
大幅な向上が図れるとともに、コンプレツサの小
形軽量化が可能となる。また、液体および液相成
分の多い部分の管径を細くしたことにより、それ
に応じてフイン巾をより狭くすることができる。
By changing the diameter of the heat transfer tube midway through the heat transfer tube as described above, the effect of pressure loss becomes extremely small, while also reducing liquid pooling and reducing the total amount of refrigerant in the refrigeration cycle. In addition to significantly improving the efficiency, it is also possible to make the compressor smaller and lighter. Furthermore, by reducing the diameter of the tube in the portion containing a large amount of liquid and liquid phase components, the fin width can be made narrower accordingly.
以下、この発明の実施例を第１図ないし第４図
を参照しながら詳細に説明する。
Hereinafter, embodiments of the present invention will be described in detail with reference to FIGS. 1 to 4.
第１図はこの発明を凝縮器に適用した第１の実
施例を示す要部斜視図、第２図は同実施例の側面
図である。これらの図において、１０は複数の例
えばアルミニウムからなる平板状フイン１０ａを
所定の間隔、すなわちそれらの間に空気が流動し
得るように所定の間隔をもつて互いに配列してな
るフイン群であつて、これは先に説明した従来の
フイン群１とほぼ同様な構成である。 FIG. 1 is a perspective view of a main part showing a first embodiment in which the present invention is applied to a condenser, and FIG. 2 is a side view of the same embodiment. In these figures, 10 is a fin group in which a plurality of flat fins 10a made of, for example, aluminum are arranged at predetermined intervals, that is, at predetermined intervals so that air can flow between them. , which has almost the same configuration as the conventional fin group 1 described above.
フイン群１０には銅管からなる伝熱管がそれと
直交するように挿通されるのであるが、この発明
においては、図示しないコンプレツサ側に接続さ
れ、同コンプレツサから過熱ガスが供給されると
ともに、気体および気相成分の多いとされる冷媒
流入側領域の管部分には管径の比較的太い、例え
ば直径9.52mmの第１の伝熱管１１ａが用いられ、
熱交換とともに相変化が進行して液体および液相
成分の多いとされる冷媒出口側領域の部分にはそ
れよりも管径が細い、例えば直径7.94mmの第２の
伝熱管１１ｂが用いられている。なお、図示され
ていないが、第１の伝熱管１１ａと第２の伝熱管
１１ｂは継手部材により接続されている。また、
この実施例においては、フイン群１０に対して第
１の伝熱管１１ａと第２の伝熱管１１ｂは２列状
態となるように挿通されているが、３列配管の場
合には第３図に示されているように、例えば冷媒
流入側の気体および気相成分の多いとされる２列
を太い第１の伝熱管１１ａとし、冷媒出口側の液
体および液相成分の多いとされる残りの１列を細
い第２の伝熱管１１ｂとすればよい。同様に４列
配管の場合には第４図に示されているように、例
えば２列を管径の太い第１の伝熱管１１ａとし、
残りの２列を管径の細い第２の伝熱管１１ｂとす
る。なお、一般に熱交換器用の銅管としては、
6.35mm、7.94mm、9.52mm、12.7mm、15.9mm、19.05
mmの各サイズのものが使用されているが、上記の
太管と細管は隣り同士のサイズであることがバラ
ンス的に最も好ましい。 A heat exchanger tube made of a copper tube is inserted through the fin group 10 so as to be perpendicular to it, but in this invention, it is connected to the compressor side (not shown), and superheated gas is supplied from the compressor, and gas and The first heat transfer tube 11a having a relatively large tube diameter, for example, 9.52 mm in diameter, is used in the tube portion of the refrigerant inflow side region where the gaseous phase components are considered to be large.
A second heat transfer tube 11b with a smaller tube diameter, for example, 7.94 mm in diameter, is used in the region on the refrigerant outlet side where phase change progresses with heat exchange and there is a large amount of liquid and liquid phase components. There is. Although not shown, the first heat exchanger tube 11a and the second heat exchanger tube 11b are connected by a joint member. Also,
In this embodiment, the first heat exchanger tube 11a and the second heat exchanger tube 11b are inserted into the fin group 10 in two rows, but in the case of three rows of piping, as shown in FIG. As shown, for example, the two rows on the refrigerant inflow side, which are said to have a large amount of gas and gas phase components, are set as the thick first heat transfer tubes 11a, and the remaining rows on the refrigerant outlet side, which are said to have a large amount of liquid and liquid phase components, are set as the thick first heat transfer tubes 11a. One row may be the thin second heat exchanger tubes 11b. Similarly, in the case of four rows of piping, as shown in FIG. 4, for example, the second row is the first heat exchanger tube 11a with a larger pipe diameter,
The remaining two rows are made into second heat exchanger tubes 11b having a smaller tube diameter. In general, copper pipes for heat exchangers are:
6.35mm, 7.94mm, 9.52mm, 12.7mm, 15.9mm, 19.05
Although various sizes of mm are used, it is most preferable for the above-mentioned thick tube and thin tube to be of the same size as each other in terms of balance.
上記各実施例は凝縮器についてのものである
が、蒸発器の場合でも全く同様に適用することが
できる。これを第５図に示されている蒸発器にお
ける冷媒の状態変化図を参照しながら説明する。 Although each of the above embodiments relates to a condenser, it can be applied to an evaporator in exactly the same way. This will be explained with reference to the state change diagram of the refrigerant in the evaporator shown in FIG.
すなわち、蒸発器の場合においはて、図示しな
い膨張弁側に接続される冷媒流入口が気液二相流
となつており、通常乾き度0.2程度で蒸発が始ま
り温度T2のまま蒸発をつづけ、ガス状態となつ
てから顕熱変化で熱交換とともに温度T2からT3
へと温度上昇する。このように凝縮器と対称的な
変化であるため、蒸発器の場合は凝縮器と異なり
その冷媒流入側と冷媒出口側とが逆にするが、こ
の場合においても気体および気相成分の多い領域
に管径の太い第１の伝熱管を利用し、液体および
液相成分の多い領域に管径の細い第２の伝熱管を
用いることになる。 In other words, in the case of an evaporator, the refrigerant inlet connected to the expansion valve side (not shown) is a gas-liquid two-phase flow, and evaporation usually starts at a dryness of about 0.2 and continues at a temperature of T 2 . , after becoming a gas, the temperature increases from T 2 to T 3 with heat exchange due to sensible heat change.
The temperature rises to . In this way, the change is symmetrical to that of the condenser, so in the case of the evaporator, unlike the condenser, the refrigerant inlet side and the refrigerant outlet side are reversed, but even in this case, the area with a large amount of gas and gas phase components is A first heat exchanger tube with a larger diameter is used in this region, and a second heat exchanger tube with a smaller diameter is used in an area containing a large amount of liquid and liquid phase components.
上記した実施例の説明から明らかなように、こ
の発明によれば、フイン群に挿通される伝熱管の
うち、冷媒の気体および気相成分が多い部分には
管径の太い伝熱管を用い、他方、冷媒の液体およ
び液相成分の多い部分には管径の細い伝熱管を用
いたことにより、圧力損失の増大を可及的に少な
くし得るとともに、液溜り現象も少なくなの、か
つ、冷媒サイクル全体の許容冷媒充填量が少なく
てよいことからコンプレツサの小形軽量化を図り
得る熱交換器が提供される。また、この発明によ
れば、従来の２パス−１パス方式の如く途中で２
本の伝熱管を１本にまとめる必要がなく、ただ単
に管径の異なる伝熱管を接続すればよいため、設
計の自由度が高められるとともに組立作業性が格
段と向上される。これに関連してフイン巾をより
小さくることができる。例えば管径9.25mmに対し
そのフイン巾を25mm、管径7.94mmに対するフイン
巾を22mmとすれば、２列熱交換器とした場合のフ
イン巾は47mmとなり、管径9.52mmの２列配管とし
た場合のフイン幅50mmより３mm程フイン巾を小さ
くすることができる。また、同一管径の伝熱管を
使用している従来例と比べて、この発明において
は途中から管径の細い伝熱管を使用するものであ
るため、若干配管長が長くなるにしてもその分コ
スト低減を図ることができる。因みに、熱交換器
はアルミニウムのフインと銅管とから構成されて
いるが、そのコスト比率は約１：２で、銅管の占
めるコスト割合がきわめて大きい。
As is clear from the description of the embodiments described above, according to the present invention, among the heat exchanger tubes inserted into the fin group, heat exchanger tubes with a large diameter are used in the portions where the gas and gas phase components of the refrigerant are large. On the other hand, by using heat transfer tubes with a small diameter in areas where there is a large amount of liquid and liquid phase components of the refrigerant, it is possible to minimize the increase in pressure loss, and also to minimize the phenomenon of liquid accumulation. A heat exchanger is provided that allows the compressor to be made smaller and lighter because the allowable amount of refrigerant charged in the entire cycle is small. Further, according to the present invention, unlike the conventional 2-pass-1-pass method, 2 passes
There is no need to combine heat exchanger tubes into one tube, and it is only necessary to connect heat exchanger tubes with different diameters, which increases the degree of freedom in design and greatly improves the ease of assembly. In connection with this, the fin width can be made smaller. For example, if the fin width is 25 mm for a pipe diameter of 9.25 mm, and the fin width is 22 mm for a pipe diameter of 7.94 mm, the fin width for a two-row heat exchanger will be 47 mm, which means that the fin width for a two-row heat exchanger will be 47 mm. The fin width can be reduced by about 3 mm from the fin width of 50 mm in that case. Furthermore, compared to the conventional example that uses heat transfer tubes with the same diameter, this invention uses heat transfer tubes with a narrower diameter from the middle, so even if the length of the pipe becomes slightly longer, the Cost reduction can be achieved. Incidentally, the heat exchanger is composed of aluminum fins and copper tubes, and the cost ratio is approximately 1:2, with the copper tubes accounting for an extremely large proportion of the cost.
さらには、管径の太い伝熱管と管径の細い伝熱
管の組合せにより、熱交換器自体の通風抵抗が減
少する。この効果はフイン群を流れる空気の流動
方向からみて細い方の管を上流側、太い方の管を
下流側に配置した場合により顕著であつて、これ
により送風機能力および騒音対策上有利になる。 Furthermore, the combination of heat exchanger tubes with a large diameter and heat exchanger tubes with a small diameter reduces the ventilation resistance of the heat exchanger itself. This effect is more noticeable when the thinner tube is placed on the upstream side and the thicker tube is placed on the downstream side when viewed from the flow direction of the air flowing through the fin group, and this is advantageous in terms of blowing function and noise control.
第１図はこの発明を凝縮器に適用した場合の一
実施例を示す要部斜視図、第２図は同実施例の側
面図、第３図および第４図はこの発明の他の実施
例を示す第２図と同様な側面図、第５図は蒸発器
における冷媒の状態変化を示す説明図、第６図は
一般的な従来例を示す側面図、第７図は凝縮器に
おける冷媒の状態変化を示す説明図、第８図は２
パス−１パス方式の従来例を示す側面図である。
図中、１０はフイン群、１０ａは平板状フイ
ン、１１ａは第１の伝熱管（太管）、１１ｂは第
２の伝熱管（細管）である。
Fig. 1 is a perspective view of essential parts showing an embodiment in which the present invention is applied to a condenser, Fig. 2 is a side view of the same embodiment, and Figs. 3 and 4 are other embodiments of the invention. Figure 5 is an explanatory diagram showing changes in the state of refrigerant in the evaporator, Figure 6 is a side view showing a general conventional example, and Figure 7 is a diagram showing changes in the state of refrigerant in the condenser. An explanatory diagram showing state changes, Figure 8 is 2
FIG. 2 is a side view showing a conventional example of a pass-1 pass method. In the figure, 10 is a fin group, 10a is a flat fin, 11a is a first heat exchanger tube (thick tube), and 11b is a second heat exchanger tube (thin tube).
Claims (1)
動し得るように所定の間隔をもつて互いに平行に
配列してなるフイン群を有し、該フイン群に対し
て伝熱管をほぼ直交状に挿通してなる熱交換器に
おいて、 上記伝熱管をその中を通される冷媒中の気体お
よび気液二相流の気相成分が多い部分と、液体お
よび気液二相液の液相成分の多い部分とに区分け
し、前者の部分に管径の太い第１の伝熱管を用い
るとともに、後者の部分に該第１の伝熱管よりも
実質的に管径の細い第２の伝熱管を用いたことを
特徴とする熱交換器。 ２ 特許請求の範囲１において、上記フイン群を
通過する気流方向を基準として上記第２の伝熱管
はその上流側に配置され、他方上記第１の伝熱管
はその下流側に配置されることを特徴とする熱交
換器。 ３ 特許請求の範囲１または２において、上記第
１の伝熱管と第２の伝熱管は継手部材を介して互
いに連通されていることを特徴とする熱交換器。[Scope of Claims] 1. A fin group including a plurality of flat fins arranged in parallel with each other at a predetermined interval so that airflow can flow between them, and airflow is transmitted to the fin group. In a heat exchanger formed by inserting heat tubes almost orthogonally, the heat exchanger tubes are used to connect a portion of the refrigerant passed through the heat exchanger tubes to a portion containing a large amount of gas phase component of the gas and gas-liquid two-phase flow, and a portion of the refrigerant that is passed through the heat exchanger tubes in a substantially orthogonal manner. A first heat exchanger tube with a larger diameter is used in the former part, and a first heat exchanger tube with a substantially smaller diameter than the first heat exchanger tube is used in the latter part. A heat exchanger characterized by using the heat exchanger tubes of No. 2. 2. In claim 1, the second heat exchanger tube is arranged on the upstream side of the airflow direction passing through the fin group, and the first heat exchanger tube is arranged on the downstream side thereof. Features of heat exchanger. 3. The heat exchanger according to claim 1 or 2, wherein the first heat exchanger tube and the second heat exchanger tube are communicated with each other via a joint member.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP27811186A JPS63131989A (en) | 1986-11-21 | 1986-11-21 | Heat exchanger |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP27811186A JPS63131989A (en) | 1986-11-21 | 1986-11-21 | Heat exchanger |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63131989A JPS63131989A (en) | 1988-06-03 |
| JPH031592B2 true JPH031592B2 (en) | 1991-01-10 |
Family
ID=17592775
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP27811186A Granted JPS63131989A (en) | 1986-11-21 | 1986-11-21 | Heat exchanger |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63131989A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4995453A (en) * | 1989-07-05 | 1991-02-26 | Signet Systems, Inc. | Multiple tube diameter heat exchanger circuit |
| BR0303172A (en) * | 2003-07-21 | 2005-04-05 | Multibras Eletrodomesticos Sa | Evaporator for refrigerator |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS432682Y1 (en) * | 1964-12-28 | 1968-02-03 | ||
| JPS5183854U (en) * | 1974-12-27 | 1976-07-06 | ||
| JPS5345564U (en) * | 1976-09-22 | 1978-04-18 | ||
| JPS57127732A (en) * | 1981-02-02 | 1982-08-09 | Hitachi Ltd | Air conditioner |
| JPS6127493A (en) * | 1984-07-16 | 1986-02-06 | Matsushita Electric Ind Co Ltd | Heat exchanger with fins |
-
1986
- 1986-11-21 JP JP27811186A patent/JPS63131989A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS63131989A (en) | 1988-06-03 |
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