JPS5849590B2 - gas purification equipment - Google Patents
gas purification equipmentInfo
- Publication number
- JPS5849590B2 JPS5849590B2 JP54014848A JP1484879A JPS5849590B2 JP S5849590 B2 JPS5849590 B2 JP S5849590B2 JP 54014848 A JP54014848 A JP 54014848A JP 1484879 A JP1484879 A JP 1484879A JP S5849590 B2 JPS5849590 B2 JP S5849590B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- absorption
- liquid
- absorption liquid
- regeneration
- 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
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- Treating Waste Gases (AREA)
- Industrial Gases (AREA)
Description
【発明の詳細な説明】
本発明は、処理ガスとアルカリ性吸収液との接触によっ
てガス中の青酸ガス、硫化水素及びアンモニアを吸収液
に溶解させる吸収装置を設け、前記吸収装置から供給さ
れる吸収液を、酸素ガスを含むガスのパブリングによっ
て再生し、硫化水素を遊離硫黄化として酸化回収した後
の再生吸収液を前記吸収装置に循環供給すべく構戊した
再生装置を設け、かつ、前記吸収装置からの処理ガス中
に残存するアンモニアを除去する装置を設けたガス精製
装置に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention provides an absorption device that dissolves cyanide gas, hydrogen sulfide, and ammonia in the gas into the absorption liquid by contacting the processing gas with an alkaline absorption liquid; A regenerating device configured to regenerate the liquid by bubbling gas containing oxygen gas and oxidize and recover hydrogen sulfide as free sulfide is provided to circulately supply the regenerated absorption liquid to the absorbing device, and The present invention relates to a gas purification device equipped with a device for removing ammonia remaining in processing gas from the device.
上記装置は、例えば石炭乾留により得られる燃料ガスの
ように、大気や水質系外に排出されると公害をまねく青
酸、硫化水素及びアンモニアを含有するガスを対象とし
て、それら有害或分を除去回収するためのものであるが
、従来の装置は第４図に示す構或であり、末だ改善すべ
き点がある。The above equipment is designed to remove and recover harmful components of gases that contain hydrocyanic acid, hydrogen sulfide, and ammonia, which cause pollution when discharged into the atmosphere or water system, such as fuel gas obtained by carbonization of coal. However, the conventional device has the structure shown in FIG. 4, and there are still points to be improved.
つまり、吸収装置５からの吸収液と空気とを別々のノズ
ル２０ａ，２０ｂによって再生装置９の処理液中に供給
する形態を採用していたために、再生装置９における気
液接触効率が悪く、吸収液を十分に再生するためには大
量の空気が必要となり、空気供給に起因する運転経費や
設備費の増大を伴い、その上、再生装置９からの排ガス
が、大量になり、かつ、アンモニア、微量の硫化水素及
び多量の酸素ガスを含むために、吸収装置からの処理ガ
スに対するアンモニア除去装置１２とは別の系２１で処
理する必要があり、設備的にも管理面でも不利であった
。In other words, since the absorption liquid and air from the absorption device 5 were supplied into the processing liquid of the regeneration device 9 through separate nozzles 20a and 20b, the gas-liquid contact efficiency in the regeneration device 9 was poor, and the absorption In order to sufficiently regenerate the liquid, a large amount of air is required, which increases operating costs and equipment costs due to the air supply.Furthermore, the exhaust gas from the regenerator 9 becomes large, and ammonia, Since it contains a small amount of hydrogen sulfide and a large amount of oxygen gas, it is necessary to treat the gas from the absorption device in a system 21 separate from the ammonia removal device 12, which is disadvantageous in terms of equipment and management.
本発明は、上記実情に鑑みて、再生装置への酸素ガスを
含むガスの供給量を少なくできるように、かつ、再生装
置からの排ガスを、吸収装置からの処理ガスと混ぜて、
しかも、有害或分除去能力の低下や爆発の危険性を十分
に回避した状態で処理できるようにし、もって、十分な
有害或分除去を、設備及び運転の経費を少なくした状態
で、かつ、管理が容易な状態で、しかも安全に行えるよ
うにする事を目的とする。In view of the above-mentioned circumstances, the present invention has been developed to reduce the amount of gas containing oxygen gas supplied to the regenerator, and to mix the exhaust gas from the regenerator with the treated gas from the absorber.
In addition, it is possible to perform treatment while sufficiently avoiding a decrease in the removal capacity of harmful substances and the danger of explosion, thereby achieving sufficient removal of harmful substances while minimizing equipment and operating costs. The purpose is to make it easy and safe to do so.
次に、例示図により本発明の実施態様を説明する。Next, embodiments of the present invention will be described with reference to illustrative drawings.
第１図に示すように、石炭乾留炉１から供給路２を介し
て供給される燃料ガスを密閉型槽３内で上昇流動させな
がら撒布装置４からのアルカリ性吸収液に向流接触させ
るべく構或した吸収装置５を設け、その向流接触によっ
て燃料ガス中の青酸ガス及び硫化水素の全量及びアンモ
ニアの一部を吸収液に吸収させるぺく構威してある。As shown in FIG. 1, the structure is such that the fuel gas supplied from the coal carbonization furnace 1 through the supply path 2 is brought into countercurrent contact with the alkaline absorption liquid from the spreading device 4 while flowing upward in the closed tank 3. An absorber 5 is provided to absorb all of the hydrocyanic acid gas and hydrogen sulfide and part of the ammonia in the fuel gas into the absorbent through countercurrent contact.
循環路６により吸収装置５にかつ再生用空気供給路７に
よりエアーコンプレツサ８に接続された再生装置９を設
け、吸収装置５下部からポンプ１０で送られてくる吸収
液を再生装置９において空気に接触させ、吸収液中の硫
化水素を酸化して遊離硫黄として析出させ、再生された
吸収液を撒布装置４にポンプ１１で送るように構或して
ある。A regenerator 9 is provided which is connected to the absorption device 5 through a circulation path 6 and to an air compressor 8 through a regeneration air supply path 7, and absorbing liquid sent by a pump 10 from the lower part of the absorption device 5 is converted into air in the regeneration device 9. The hydrogen sulfide in the absorption liquid is oxidized and precipitated as free sulfur, and the regenerated absorption liquid is sent to the spraying device 4 by a pump 11.
吸収装置５の上部とアンモニア除去装置１２とを、ミキ
サー１３を備えた一次処理ガス供給路１４を介して接続
すると共に、再生装置９の上部とミキサー１３を排ガス
路１５を介して接続して、吸収装置５からの一次処理燃
料ガスに再生装置９からの排ガスを混合し、その混合ガ
ス中のアンモニアをアンモニア除去装置１２における硫
酸溶液中へのパブリングによって吸収除去すべく構戊し
てある。The upper part of the absorption device 5 and the ammonia removal device 12 are connected via a primary processing gas supply path 14 equipped with a mixer 13, and the upper part of the regenerator 9 and the mixer 13 are connected via an exhaust gas path 15. The primary treatment fuel gas from the absorption device 5 is mixed with the exhaust gas from the regenerator 9, and the ammonia in the mixed gas is absorbed and removed by bubbling into a sulfuric acid solution in the ammonia removal device 12.
そして、適宜、ロダンアンモン濃度が犬になった吸収液
及び遊離硫黄を排出するための弁付排出路１６を循環路
６に接続しである。Then, as appropriate, a valved discharge passage 16 is connected to the circulation passage 6 for discharging the absorbent liquid and free sulfur having a low concentration of rhodanammonium.
前記吸収装置５から再生装置９に吸収液を供給する循環
路６、及び、再生用空気供給路７を、第２図に示すよう
に、再生装置９に設けた複数個のプレミックスノズル１
７に連通させ、吸収液と空気を気液二相流として再生用
密閉型槽１８内に貯留されている吸収液中に吸込ませる
ように構代し、比較的少量の空気供給でもって、吸収液
の十分な再生を確実に行わせるように構或してある。A circulation path 6 for supplying the absorption liquid from the absorption device 5 to the regeneration device 9 and a regeneration air supply path 7 are connected to a plurality of premix nozzles 1 provided in the regeneration device 9, as shown in FIG.
7, so that the absorption liquid and air are sucked into the absorption liquid stored in the regeneration closed tank 18 as a gas-liquid two-phase flow, and with a relatively small amount of air supply, the absorption It is designed to ensure sufficient regeneration of the liquid.
尚、前記吸収装置５及び再生装置９を構或するに、第３
図に示すように、１個の密閉型槽１９に対して、その上
下中間に前記石炭乾留炉１からの供給路２を、上部に前
記アンモニア除去装置１２に接続した一次処理ガス供給
路１４を、かつ、下部に前記プレミックスノズル１７を
、夫々連通させ、槽１９内下部に貯留された吸収液を槽
１９内上部の前記撒布装置４及び前記プレミックスノズ
ル１７にポンプ輸送する循環路６，６を設け、もって、
槽１９上部を吸収装置５にかつ槽下部を再生装置９に構
威してもよく、このようにすると、ガス精製装置全体の
設置に要する敷地面積を少なくでき、前記ミキサー１３
の省略ができ、かつ、流路構戊を簡略化できる等の利点
が有る。In addition, when configuring the absorption device 5 and the regeneration device 9, a third
As shown in the figure, one closed tank 19 has a supply path 2 from the coal carbonization furnace 1 in the upper and lower middle thereof, and a primary processing gas supply path 14 connected to the ammonia removal device 12 in the upper part. , and a circulation path 6 whose lower part communicates with the premix nozzle 17, and pumps the absorption liquid stored in the lower part of the tank 19 to the spraying device 4 and the premix nozzle 17 in the upper part of the tank 19, 6, and with that,
The upper part of the tank 19 may be used as the absorption device 5 and the lower part of the tank may be used as the regeneration device 9. In this way, the site area required for installing the entire gas purification device can be reduced, and the mixer 13
This has advantages such as omitting the above and simplifying the flow path structure.
処理ガスは、前述のように石炭乾留によって得られる燃
料ガスが主たるものであるが、その他各種使用目的のガ
スから青酸ガス、硫化水素及びアンモニアを除去回収す
るに、本発明による装置を利用できる。As mentioned above, the main gas to be treated is fuel gas obtained by coal carbonization, but the apparatus according to the present invention can be used to remove and recover cyanide gas, hydrogen sulfide, and ammonia from gases for various other purposes.
前記アルカリ性吸収液としては、例えばアンモニア水溶
液や苛性ソーダ溶液等、あるいはそれらに酸化還元触媒
を含ませたもの等を利用できる。As the alkaline absorption liquid, for example, an ammonia aqueous solution, a caustic soda solution, or a mixture thereof containing a redox catalyst can be used.
前記再生装置９に酸素ガスを供給するに、一般的に経済
性の面から大気を利用するが、酸素高濃度ガス等の各種
酸素ガス含有ガスを利用できる。To supply oxygen gas to the regenerator 9, the atmosphere is generally used from the economic point of view, but various oxygen-containing gases such as high oxygen concentration gas can also be used.
前記プレミックスノズル１７の具体構造は各種変形可能
であり、再生用酸素を含むガスが極力徴少気泡化される
ものが望ましい。The specific structure of the premix nozzle 17 can be modified in various ways, and it is desirable that the premix nozzle 17 be able to form as few bubbles as possible in the gas containing oxygen for regeneration.
次に、本発明による装置と、冒記従来タイプの装置との
比較結果の一例を示す。Next, an example of a comparison result between the device according to the present invention and the conventional type device mentioned above will be shown.
硫化水素含有量が６ ｉ ／ Ｎｍ″のガスを３６００
０Ｎｍ／Ｈｒの割で処理する場合、硫化水素の全量を遊
離硫黄にするに必要な空気供給量は、従来タイプで２
５ ０ ０ Ｎｎｉ：／ Ｈｒとなり、本発明タイプで
８ ０ ０ Ｎｒｒｒ：／ Ｈｒとなり、また、再生装
置からの排ガスの酸素ガス濃度は、従来タイプで１７．
３ｖｏｌ％となり、本発明タイプで９．４ｖｏｌ％とな
った。3600 ml of gas with a hydrogen sulfide content of 6 i/Nm"
When processing at a rate of 0Nm/Hr, the amount of air supply required to convert the entire amount of hydrogen sulfide to free sulfur is 2 for the conventional type.
5 0 0 Nni:/Hr, and 8 0 0 Nrrr:/Hr for the inventive type, and the oxygen gas concentration of the exhaust gas from the regenerator was 17.
3 vol%, and 9.4 vol% for the type of the present invention.
すなわち、本発明による装置を用いると、再生装置に供
給すべき空気量は従来の％以下になり、また、吸収装置
及び再生装置からのガス量の和は従来に比して３０％程
度減少し、設備の小型化によるイニシャルコストの低減
を効果的に行えると共に、ガス輸送に要する動力費節約
によるランニングコストの大巾な低減を図れるのである
。That is, when the device according to the present invention is used, the amount of air to be supplied to the regenerator will be less than 30% of the conventional amount, and the sum of the gas amounts from the absorption device and the regenerator will be reduced by about 30% compared to the conventional method. In addition to effectively reducing the initial cost by downsizing the equipment, it is also possible to significantly reduce running costs by saving power costs required for gas transportation.
ちなみに、上述の量のガスを処理するに際しての、空気
供給用コンプレツサや吸収液循環ポンプ等に要する電気
代を試算したところ、本発明装置を利用すると、従来装
置を利用する場合に比して年間２４００万円程度の巨額
の節約を図れる事が判った。Incidentally, when we calculated the electricity costs required for the air supply compressor, absorption liquid circulation pump, etc. when processing the amount of gas mentioned above, we found that using the device of the present invention costs less per year than when using the conventional device. It was found that a huge savings of approximately 24 million yen could be achieved.
また、従来タイプのように再生装置からの排ガス中に１
７．３ｖｏｌ％もの犬量の酸素ガスが含有されると、吸
収装置からの一次処理ガスが可燃性であれば、一次処理
ガスと再生装置からの排ガス混合に伴って局部的燃焼を
生じる危険性が犬であるが、本発明タイプのように排ガ
ス中の酸素ガス濃度が低いと、そのような局部的燃焼を
生じず、安全性においても有効である。In addition, unlike the conventional type, 1
If as much as 7.3 vol% of oxygen gas is contained, if the primary treatment gas from the absorption device is flammable, there is a risk of local combustion occurring due to the mixing of the primary treatment gas and the exhaust gas from the regeneration device. However, when the concentration of oxygen gas in the exhaust gas is low as in the type of the present invention, such local combustion does not occur, which is effective in terms of safety.
以上要するに、本発明は、冒記した装置において、前記
再生装置９に、前記吸収装置５からの吸収液と前記酸素
ガスを含むガスを気液二相流として槽内貯留吸収液中に
吹込むプレミックスノズル１７を設け、前記再生装置９
の排ガス路１５を、前記吸収装置５からアンモニア除去
装置１２への一次処理ガス供給路１４に連通させてある
事を特徴とする。In summary, in the above-mentioned apparatus, the present invention causes the regenerator 9 to blow gas containing the absorbent liquid from the absorber 5 and the oxygen gas into the absorbent liquid stored in the tank as a gas-liquid two-phase flow. A premix nozzle 17 is provided, and the regeneration device 9
The exhaust gas passage 15 is connected to the primary processing gas supply passage 14 from the absorption device 5 to the ammonia removal device 12.
すなわち、プレミックスノズル１７によって再生装置９
に吸収液と再生のための酸素ガスを供給する事によって
、吸収液と酸素ガスの接触効率が顕著に高くなり、その
結果、十分な吸収液再生を確実に行わせるに必要な再生
装置９への酸素ガス供給量を著しく少なくできて、再生
装置９への酸素ガス供給に起因する設備面及び運転面で
の経済的負担を顕著に減少できるようになった。That is, the premix nozzle 17
By supplying the absorbing liquid and oxygen gas for regeneration to the regenerating device 9, the contact efficiency between the absorbing liquid and the oxygen gas is significantly increased. The amount of oxygen gas supplied to the regenerator 9 can be significantly reduced, and the economic burden on equipment and operation caused by the supply of oxygen gas to the regenerator 9 can be significantly reduced.
また、上述のような再生装置９へのガス供給量減少に伴
って、再生装置９からの排ガス量も著しく減少する事、
並びに、上述のような効率良い吸収液と酸素ガスとの接
触に伴って、再生装置９からの排ガス中の硫化水素が皆
無あるいはそれに近い状態になると共に、排ガスの酸素
ガス濃度が著しく低下する事を利用して、再生装置９か
らの排ガスを吸収装置５からの処理ガスと混合処理させ
るから、有害戊分除去能力低下や可燃性処理ガスの燃焼
という問題を回避しながら、精製装置全体の簡略化を図
る事ができ、その結果、一層経済面で有利にできると共
に、管理面においても有利になった。Furthermore, as the amount of gas supplied to the regenerator 9 decreases as described above, the amount of exhaust gas from the regenerator 9 also decreases significantly.
In addition, due to the contact between the efficient absorbing liquid and oxygen gas as described above, hydrogen sulfide in the exhaust gas from the regenerator 9 becomes completely or almost completely absent, and the oxygen gas concentration in the exhaust gas decreases significantly. Since the exhaust gas from the regenerator 9 is mixed with the treated gas from the absorber 5 using the As a result, it was not only economically advantageous, but also administratively advantageous.
図面は本発明に係るガス精製装置の実施の態様を例示し
、第１図はフローシ一ト、第２図は要部の縦断面図、第
３図は別の実施態様を示すフローシ一ト、第４図は従来
例を示すフローシ一トである。
２・・・・・・処理ガス供給路、４・・・・・・撒布装
置、５・・・・・・吸収装置、６・・・・・・循環路、
９・・・・・・再生装置、１２・・・・・・アンモニア
除去装置。
１４・・・・・・一次処理ガス供給路、１５・・・・・
・排ガス路、１７・・・・・・プレミックスノズル、１
９・・・・・・密閉型槽。The drawings illustrate embodiments of the gas purification apparatus according to the present invention, FIG. 1 is a flow sheet, FIG. 2 is a longitudinal sectional view of the main part, and FIG. 3 is a flow sheet showing another embodiment. FIG. 4 is a flowchart showing a conventional example. 2...Processing gas supply path, 4...Spraying device, 5...Absorption device, 6...Circulation path,
9... Regeneration device, 12... Ammonia removal device. 14...Primary processing gas supply path, 15...
・Exhaust gas path, 17...Premix nozzle, 1
9... Closed tank.
Claims (1)
中の青酸ガス、硫化水素及びアンモニアを吸収液に溶解
させる吸収装置５を設け、前記吸収装置５から供給され
る吸収液を、酸素ガスを含むガスのパブリングによって
再生し、硫化水素を遊離硫黄化として酸化回収した後の
再生吸収液を前記吸収装置５に循環供給すべく構威した
再生装置９を設け、かつ、前記吸収装置５からの処理ガ
ス中に残存するアンモニアを除去する装置１２を設けた
ガス精製装置であって、前記再生装置９に、前記吸収装
置５からの吸収液と前記酸素ガスを含むガスを気液二相
流として槽内貯留吸収液中に吹込むプレミックスノズル
１７を設け、前記再生装置９の排ガス路１５を、前記吸
収装置５からアンモニア除去装置１２への一次処理ガス
供給路１４に連通させてある事を特徴とするガス精製装
置。 ２ 前記吸収装置５及び再生装置９を構或するに、密閉
型槽１９に対して、その上下中間部に処理ガス供給路２
を、上部に前記一次処理ガス供給路１４を、かつ、下部
に前記プレミックスノズル１７を、夫々連通させると共
に、前記密閉型槽１９内下部に貯留された吸収液を、槽
１９内上部に設けた撒布装置４及び前記プレミックスノ
ズル１７に供給する循環路６を設けてある事を特徴とす
る特許請求の範囲第１項に記載の装置。 ３ 前記処理ガスが、石炭乾留により得られる燃料ガス
である事を特徴とする特許請求の範囲第１項又は第２項
に記載の装置。[Scope of Claims] 1. An absorption device 5 is provided that dissolves cyanide gas, hydrogen sulfide, and ammonia in the gas into the absorption liquid by contacting the processing gas with the alkaline absorption liquid, and the absorption liquid supplied from the absorption device 5 is , a regenerator 9 configured to circulately supply the regenerated absorption liquid to the absorption device 5 after regeneration by bubbling of a gas containing oxygen gas and oxidation recovery of hydrogen sulfide as free sulfur is provided; A gas purification device is provided with a device 12 for removing ammonia remaining in the processing gas from the device 5, and the gas purification device 12 is provided with a device 12 for removing ammonia remaining in the processing gas from the device 5, and the gas containing the absorption liquid and the oxygen gas from the absorption device 5 is transferred to the regeneration device 9 into a gas-liquid state. A premix nozzle 17 is provided to blow a two-phase flow into the absorbent liquid stored in the tank, and the exhaust gas path 15 of the regenerator 9 is communicated with the primary processing gas supply path 14 from the absorber 5 to the ammonia removal device 12. A gas purification device characterized by: 2. When configuring the absorption device 5 and the regeneration device 9, a process gas supply path 2 is provided in the upper and lower intermediate portions of the closed tank 19.
The upper part communicates with the primary processing gas supply path 14 and the lower part communicates with the premix nozzle 17, and the absorption liquid stored in the lower part of the closed tank 19 is provided in the upper part of the tank 19. 2. The device according to claim 1, further comprising a circulation path 6 for supplying the spraying device 4 and the premix nozzle 17. 3. The apparatus according to claim 1 or 2, wherein the processing gas is a fuel gas obtained by carbonization of coal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP54014848A JPS5849590B2 (en) | 1979-02-09 | 1979-02-09 | gas purification equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP54014848A JPS5849590B2 (en) | 1979-02-09 | 1979-02-09 | gas purification equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS55106293A JPS55106293A (en) | 1980-08-14 |
| JPS5849590B2 true JPS5849590B2 (en) | 1983-11-05 |
Family
ID=11872447
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP54014848A Expired JPS5849590B2 (en) | 1979-02-09 | 1979-02-09 | gas purification equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5849590B2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5959465U (en) * | 1982-10-12 | 1984-04-18 | 三洋電機株式会社 | battery storage device |
| JPS6042261U (en) * | 1983-08-31 | 1985-03-25 | キヤノン株式会社 | Battery case holding structure |
| JPS6148564U (en) * | 1984-07-30 | 1986-04-01 | ||
| JPH0145083Y2 (en) * | 1984-06-01 | 1989-12-26 | ||
| JP2009114233A (en) * | 2007-11-01 | 2009-05-28 | Nippon Steel Engineering Co Ltd | Liquid phase oxidation wet type desulphurization apparatus |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62201623A (en) * | 1986-02-28 | 1987-09-05 | Nippon Kokan Kk <Nkk> | Desulfurizer for hydrogen sulfide-containing gas |
| JP5573460B2 (en) * | 2010-07-27 | 2014-08-20 | Ｊｆｅスチール株式会社 | Coke oven gas desulfurization equipment |
-
1979
- 1979-02-09 JP JP54014848A patent/JPS5849590B2/en not_active Expired
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5959465U (en) * | 1982-10-12 | 1984-04-18 | 三洋電機株式会社 | battery storage device |
| JPS6042261U (en) * | 1983-08-31 | 1985-03-25 | キヤノン株式会社 | Battery case holding structure |
| JPH0145083Y2 (en) * | 1984-06-01 | 1989-12-26 | ||
| JPS6148564U (en) * | 1984-07-30 | 1986-04-01 | ||
| JP2009114233A (en) * | 2007-11-01 | 2009-05-28 | Nippon Steel Engineering Co Ltd | Liquid phase oxidation wet type desulphurization apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS55106293A (en) | 1980-08-14 |
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