JPH0779942B2 - Air separation device - Google Patents
Air separation deviceInfo
- Publication number
- JPH0779942B2 JPH0779942B2 JP61234656A JP23465686A JPH0779942B2 JP H0779942 B2 JPH0779942 B2 JP H0779942B2 JP 61234656 A JP61234656 A JP 61234656A JP 23465686 A JP23465686 A JP 23465686A JP H0779942 B2 JPH0779942 B2 JP H0779942B2
- Authority
- JP
- Japan
- Prior art keywords
- air
- heat exchanger
- adsorption tower
- separation device
- compressor
- 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 - Fee Related
Links
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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04181—Regenerating the adsorbents
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
- F25J2205/70—Heating the adsorption vessel
-
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation Of Gases By Adsorption (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明は、深冷分離装置の前処理装置として、水分及び
炭酸ガスを吸着除去する装置に係り、特に、エキスパン
ダーコンプレッサーを有する空気分離装置に好適なもの
である。The present invention relates to a device for adsorbing and removing water and carbon dioxide as a pretreatment device for a cryogenic separation device, and more particularly to an air separation device having an expander compressor. It is suitable.
従来の空気分離装置は、特開昭54−83697号に記載のよ
うに、吸着塔の再生ガスを加熱するために、加熱器を配
置し、再生ガスを250℃程度まで昇温していた。しかし
ながら、膨張タービンの制動により生じる高温のガスは
大気放熱しており、熱エネルギの回収については配慮さ
れていなかった。このため、再生ガスの加熱エネルギー
を多く必要とする。この従来技術を第２図により説明す
ると、エキスパンダーコンプレッサー５の圧縮機で圧縮
され、温度上昇（50〜80℃）した原料空気を冷却（５〜
10℃）するため、アフタークーラー９を設けて冷媒又は
冷水により原料空気を冷却していた。また、吸着塔３の
再生用加熱ガスは、再生ガス加熱器８でスチーム又は電
気ヒーター等により加温（150〜250℃）され、吸着塔３
へ供給使用している。このため、アフタークーラー９、
再生ガス加熱器８と個々に動力を必要とするため、プラ
ント全体の消費動力を増加させていた。In the conventional air separation apparatus, as described in JP-A-54-83697, a heater is arranged to heat the regenerated gas in the adsorption tower, and the regenerated gas is heated to about 250 ° C. However, the high temperature gas generated by the braking of the expansion turbine radiates heat to the atmosphere, and no consideration has been given to the recovery of heat energy. For this reason, a large amount of heating gas heating energy is required. This conventional technique will be described with reference to FIG. 2. The raw material air compressed by the compressor of the expander compressor 5 and having a temperature rise (50 to 80 ° C.) is cooled (5 to 5).
Therefore, the after-cooler 9 is provided to cool the raw material air with a refrigerant or cold water. Further, the heating gas for regeneration of the adsorption tower 3 is heated (150 to 250 ° C.) by a steam or an electric heater in the regeneration gas heater 8, and the adsorption tower 3 is heated.
Used to supply. Therefore, aftercooler 9,
Since the regeneration gas heater 8 and individual power are required, the power consumption of the entire plant is increased.
上記従来技術は、エキスパンダーコンプレッサーの圧縮
機出口の高温ガスを単に冷却するのみで、熱回収を行な
っておらず、原単位に問題があった。The above-mentioned conventional technique merely cools the high temperature gas at the compressor outlet of the expander compressor, does not recover heat, and has a problem with the basic unit.
本発明の目的は、従来技術の原単位の問題を改善するこ
とにある。It is an object of the present invention to remedy the prior art intensity problem.
上記目的は、エキスパンダーコンプレッサーの圧縮機出
口の高温のガスと吸着塔再生ガスを熱交換させることに
より、再生ガスを予熱することで達成される。The above object is achieved by preheating the regenerated gas by exchanging heat between the high temperature gas at the compressor outlet of the expander compressor and the regenerated gas in the adsorption tower.
エキスパンダーコンプレッサーの圧縮機出口で昇温して
いる原料空気と、吸着塔再生ガスを熱交換させることに
より、原料空気を冷却すると同時に再生ガスを予熱し
て、アフタークーラー冷熱源の削除と再生ガス加熱機の
消費動力を低減することができる。By exchanging heat between the raw material air heated at the compressor outlet of the expander compressor and the adsorption tower regeneration gas, the raw material air is cooled and at the same time the regeneration gas is preheated, the after-cooler cold heat source is removed and the regeneration gas is heated. The power consumption of the machine can be reduced.
以下、本発明の一実施例を第１図により説明する。 An embodiment of the present invention will be described below with reference to FIG.
原料空気圧縮機１で約6Kg/cm2Gに圧縮された原料空気
は、空気冷却器２で約10℃に冷却され、吸着塔３へ送ら
れる。ここで、後述の深冷分離装置内で固化する水分及
び炭酸ガスを吸着除去し、精製空気として後流のエキス
パンダーコンプレッサー５及び空気熱交換器４へ送られ
る。エキスパンダーコンプレッサー５へ送られた原料空
気は、約７〜8Kg/cm2Gに圧縮され、50〜80℃まで昇温す
る。この圧縮空気は、空気熱交換器４への入口温度を原
料空気とそろえるために、再生ガス予熱器７で深冷分離
装置の廃ガスと熱交換して約10℃に冷却され、空気熱交
換器４へ送られる。一方、深冷分離装置から出てくる廃
ガスは、空気熱交換器４で常温（６℃程度）まで温度回
復した後、再生ガス予熱器７へ送られ、圧縮空気と熱交
換して約40℃まで昇温される。The raw material air compressed by the raw material air compressor 1 to about 6 kg / cm 2 G is cooled to about 10 ° C. by the air cooler 2 and sent to the adsorption tower 3. Here, the water and carbon dioxide gas that solidify in the later-described cryogenic separation device are adsorbed and removed, and sent as purified air to the expander compressor 5 and the air heat exchanger 4 in the downstream. The raw material air sent to the expander compressor 5 is compressed to about 7-8 Kg / cm 2 G and heated up to 50-80 ° C. This compressed air is heat-exchanged with the waste gas of the cryogenic separation device in the regeneration gas preheater 7 in order to make the inlet temperature to the air heat exchanger 4 equal to the feed air, and is cooled to about 10 ° C. Sent to container 4. On the other hand, the waste gas discharged from the cryogenic separation device is returned to room temperature (about 6 ° C) by the air heat exchanger 4 and then sent to the regenerated gas preheater 7 to exchange heat with the compressed air to about 40 ° C. The temperature is raised to ℃.
吸着塔３の再生工程時には、約40℃に昇温した廃ガスを
再生ガス加熱器８で約150℃まで昇温した後、吸着塔３
へ供給し、吸着塔３の再生に使用される。During the regeneration process of the adsorption tower 3, the temperature of the waste gas heated to about 40 ° C is raised to about 150 ° C by the regeneration gas heater 8, and then the adsorption tower 3 is heated.
And is used to regenerate the adsorption tower 3.
吸着塔３の冷却工程時には、再生ガス予熱器7,再生ガス
加熱器８をバイパスした再生ガスが吸着塔３へ常温のま
ま供給される。また、再生ガスの余剰分を再生ガス予熱
器７へ供給し、再生ガス予熱器７出口で大気放出するこ
とにより、エキスパンダーコンプレッサー５の圧縮機出
口の圧縮空気を冷却する。During the cooling process of the adsorption tower 3, the regeneration gas bypassing the regeneration gas preheater 7 and the regeneration gas heater 8 is supplied to the adsorption tower 3 at room temperature. Further, the surplus of the regenerated gas is supplied to the regenerated gas preheater 7 and discharged to the atmosphere at the outlet of the regenerated gas preheater 7 to cool the compressed air at the compressor outlet of the expander compressor 5.
本実施例によれば、エキスパンダーコンプレッサーのア
フタークーラーがなくなるため、冷媒又は冷水が不要に
なる。また、再生ガス加熱機の容量を次式（１）で示す
如く、約3/4に低減することができる。According to this embodiment, since the aftercooler of the expander compressor is eliminated, the refrigerant or cold water becomes unnecessary. Further, the capacity of the regenerative gas heater can be reduced to about 3/4 as shown in the following equation (1).
〔発明の効果〕 本発明によれば、再生ガス加熱器の消費動力を約25％程
度低減することができ、また、エキスパンダーコンプレ
ッサーのアフタークーラーに冷媒等を使用しないため、
消費動力を低減することができ、原単位を向上させるこ
とができる効果がある。 [Advantages of the Invention] According to the present invention, the power consumption of the regenerative gas heater can be reduced by about 25%, and since no refrigerant or the like is used in the aftercooler of the expander compressor,
The power consumption can be reduced and the basic unit can be improved.
【図面の簡単な説明】 第１図は本発明の一実施例を示す空気分離装置の系統
図、第２図は従来の空気分離装置の系統図である。 １……原料空気圧縮機、２……空気冷却器、３……吸着
塔、４……空気熱交換器、５……エキスパンダーコンプ
レッサー、６……精留塔、７……再生ガス予熱器、８…
…再生ガス加熱器、９……アフタークーラー。BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a system diagram of an air separation device showing an embodiment of the present invention, and FIG. 2 is a system diagram of a conventional air separation device. 1 ... Raw material air compressor, 2 ... Air cooler, 3 ... Adsorption tower, 4 ... Air heat exchanger, 5 ... Expander compressor, 6 ... Fractionation tower, 7 ... Regeneration gas preheater, 8 ...
… Regeneration gas heater, 9… Aftercooler.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 岡部 道昌 山口県下松市大字東豊井794番地 株式会 社日立製作所笠戸工場内 (56)参考文献 特開 昭57−6282（ＪＰ，Ａ) ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Michimasa Okabe 794 Azuma Higashitoyo, Shimomatsu City, Yamaguchi Prefecture Inside the Kasado Plant, Hitachi Ltd. (56) References JP-A-57-6282 (JP, A)
Claims (1)
ング式吸着法により除去する吸着塔と、 上記水分及び炭酸ガスが除去された原料空気より窒素，
酸素，アルゴン等を採取する深冷分離装置と、 上記吸着塔を通過した後の原料空気の一分流を冷却し
て、上記深冷分離装置に原料空気として供給する空気熱
交換器と、 上記吸着塔を通過した後の原料空気の他の分流を圧縮す
る圧縮機と、上記深冷分離装置に膨張空気を供給する膨
張タービンとからなるエキスパンダーコンプレッサー
と、 上記圧縮機から吐出される圧縮空気を、上記深冷分離装
置から上記空気熱交換器を通して送出される廃ガスと熱
交換する再生ガス予熱用熱交換器と、 上記再生ガス予熱用熱交換器および上記空気熱交換器に
より上記圧縮空気を冷却して、上記膨張タービンに供給
する冷却流路と、 上記冷却流路を流れる上記圧縮空気との熱交換により加
熱された上記廃ガスを、上記吸着塔の再生ガスとして上
記吸着塔に供給する再生ガス流路と からなることを特徴とする空気分離装置。1. An adsorption tower for removing moisture and carbon dioxide in raw air by a temperature swing adsorption method, and nitrogen from raw air from which the moisture and carbon dioxide have been removed,
A cryogenic separation device that collects oxygen, argon, etc., an air heat exchanger that cools a partial flow of the raw material air that has passed through the adsorption tower and supplies it as raw material air to the cryogenic separation device, and the adsorption A compressor for compressing another split stream of the feed air after passing through the tower, an expander compressor consisting of an expansion turbine for supplying expansion air to the deep-chill separator, and compressed air discharged from the compressor, A regeneration gas preheating heat exchanger for exchanging heat with waste gas sent from the deep-separation device through the air heat exchanger, and cooling the compressed air by the regeneration gas preheating heat exchanger and the air heat exchanger. The cooling gas supplied to the expansion turbine, and the waste gas heated by heat exchange with the compressed air flowing through the cooling flow path, are reused as regeneration gas for the adsorption tower in the adsorption tower. Air separation apparatus characterized by comprising a sheet for regeneration gas flow path.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61234656A JPH0779942B2 (en) | 1986-10-03 | 1986-10-03 | Air separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61234656A JPH0779942B2 (en) | 1986-10-03 | 1986-10-03 | Air separation device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6391121A JPS6391121A (en) | 1988-04-21 |
| JPH0779942B2 true JPH0779942B2 (en) | 1995-08-30 |
Family
ID=16974427
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61234656A Expired - Fee Related JPH0779942B2 (en) | 1986-10-03 | 1986-10-03 | Air separation device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0779942B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH029791U (en) * | 1988-07-04 | 1990-01-22 | ||
| FR2930330B1 (en) * | 2008-04-22 | 2013-09-13 | Air Liquide | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS576282A (en) * | 1980-06-14 | 1982-01-13 | Kobe Steel Ltd | Air separator |
-
1986
- 1986-10-03 JP JP61234656A patent/JPH0779942B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6391121A (en) | 1988-04-21 |
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| Date | Code | Title | Description |
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| LAPS | Cancellation because of no payment of annual fees |