TWI334799B - Removing contaminants from natural gas - Google Patents
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- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
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- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
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Description
1334799 玖、發明說明: 【發明所屬之技術領域】 本發明係關於一種藉由形成污染物固體以及後續適當 地炫化此©體㈣’以從天然氣進料物流中移除污染物 的方法與裝置。 當污染物為水時,本發明尤其(但非排除性地)關於 種將天然氣進料物流脫水的方法與裝置。 當π染物為酸性物種,例如硫化氣或二氧化碳時,本 發明尤其(但非排除性地)Μ於一種使天然氣進料物流脫 硫的方法與裝置。 ρ本發明亦尤其(但非排除性地)關於一種依續將天然 氣進料物流脫水與脫硫的方法與裝置。 【先前技術】 不管是來自生產儲槽或健存儲槽的天然氣,其血型地 皆含有水分’以及其它會在生產液化天然氣(lng)的液 化過程中形成固體的物種。一般做法是在液化之前先讓天 然氣接受脫水程序。將水分移除,以防止發生水合物形成 於管路内或液化容器上游的熱交換器内。 / 假使未將水分移除,則固態水合物可能會在管路工件 、熱交換器和/或液化容器内生成。此水合物是含有水分 與具有冰的外觀之天然氣所形成之穩定固態物質,且7天2 氣係位於水合物的晶格内。 ”' 天然水合物的形成以歷史觀點看來被認為是不受歡迎 而應避免的結果。然而,已經發展出來一些促 %大然氣水 1334799 合物生成的方法,像是國際專利申請號〇1/〇〇 755以及 01/12 758。於這些國際專利申請案的第一案中,其描述 一種在一種減低天然氣與水之間的界面張力以促進天然氣 水合物的纟成的試齊j之存在下(昆合天然氣和水#方法與裝 置。於這些國際專利申請案的第二案中,其描述_種生產 工廠,其包含迴旋狀流動路徑,纟用以在降低溫度以生成 天然氣水合物之前引發帛一步料之水與天然…氣的混合。 習知技藝中,將天然氣進料物流脫水的方法包括以乙 二醇吸收水分’或是使用固冑(像是含水氧化鋁、矽溶膠 、石夕石-氧化鋁以及分子篩)吸收水分。 典型地’天然氣亦含有酸性物種,像是硫化氫 與二氧化碳(C02)。此種天然氣被歸類& “酸氣,,。當 H2S與〇)2從天然氣進料物流被移除,則此氣體被歸類為“ 脫硫氣體(sweet)”。因為在即使低濃度下從未經脫硫氣 體中所散發出的臭味,術語“酸氣,,係用於指稱含有H s 的天然氣。H2S是必須被移除以符合法律規定之天秋氣二 染物,…23及其二氧化硫與三氧化硫的燃燒產物亦是 :毒性的。此外,H2",大部分一般與氣體管路相關的金 屬疋有腐#性的’使得酸氣的加工與處理可能導致此種系 如同脫水, 典型地包括使用 分子篩等的吸收 雜與昂貴。 使氣體脫硫的方法亦為習知技藝,此方法 固體吸附程序的吸附,或是使用胺程序、 。現行的脫水與氣體脫硫的方法皆極其複 1334799 【發明内容】 本發明是對國際專利申請公開號〇3/〇62 725中所述的 方法與裝置提出改良。 為此目的,根據本發明之從含有水分的天然氣進料物 流中移除污染物的方法包括以下步驟:於第一容器中將天 然氣進料物流冷卻至水合物生成之第一操作溫度;以及從 第一容器移除脫水氣體物流。 本發明方法之之一基本特徵在於故意形成水合物以移 除水分。-般而言’水合物的生成是要避免的。 $天然氣進料物流進—步包含酸性物種時,根據本發 明之方法適當地更包括於第二容器令將經脫水氣體冷卻至 生成固態酸性物種或該酸性物種溶於液體中的第二操作溫 X及從該第—谷器中移除經脫水、脫硫之氣體物流。 【實施方式】 術°°操作偃度係用以指低於污染物在操作第一或 第二容器之給定麼力下的固體/液體轉移溫度之溫度。 /本說月曰中,》显#液體物流可為任何相容之液 物W #具有南於π染物在第一或第二容器操作的給定 下口體/液體轉移溫度之溫度。因此此溫熱液體物流 或至足以弓|發污染物固體熔化的溫度。溫熱液體可能 或可能不會使污染物全部形成溶液。 現將參照隨附圖式更詳細說明本發明,其中 圖1為本發明第一具體實例之程序流程圖;以及 圖2為本發明另一具體實例之程序流程圖。 1334799 。::照圖1。圖i顯示進行本發明之方法之裝置ι〇 染物θ 〇包含有第—容器12。在第—容器12中移除的污 砝广因此離開第一容器12的氣體是乾燥的。重質 虱化合物被移除亦是纟方法之結果,故離開第一 的氣體物流為由m 12内之條件決定之程度的 :合物的露滴。然而’離開第一容器12 i體的水露點, 由於水合物的形成,所以較其平衡露點低。 #如圖1所示之具體實例,來自水源的漫進料氣體由導 官15進料到第一閃蒸槽16,其中冷凝液從進料氣體中分 離。第-閃蒸槽16内的壓力與溫度條件典型上是在75至 ⑽bar的等級及介於25 i价之間(約高於水合物形 成溫度5至urc)。經由導管17離開第—閃蒸槽的冷 凝液物流為如前所定義溫熱液體,,。此冷凝液是由與 天^氣起生成之液態碳氫化合物所組成。在第一閃蒸槽 16中與酸渥進料氣體分離的氣體物流經由渥酸氣體進料^ 流入口 20進入第一容器12。中間熱交換器22可用來冷卻 介於第-閃蒸槽16與第一容器12間的澄酸氣體。中間熱 交換器22使溼酸氣體的溫度降低的溫度為正好高於在進 料物流之肖定壓力下水合物生成溫度。纟進料物流之特定 壓力下水合物生成溫度為第一操作溫度之最大值,第一操 作溫度為第一容器12内之操作溫度。 可使用Joule-Thompson閥24或其它適當膨脹裝置來 膨脹供給入第一容器12的溼氣體進料物流,以在該物流 進入第一容器12時進一步冷卻之。J〇ule_Th〇mps〇n閥24 1334799 另可定義進入第一容器12的入口 20。在膨脹進入第一容 器1 2的溼酸氣體進料物流之後,容器1 2内的氣體壓力_ 溫度條件便容許水合物形成。必要的冷卻程度可藉由流經 J〇ule-Th〇mpson閥24的溼酸氣體進料物流的膨脹度來達 成。 將第- m 2 π的第一操作溫度與壓力維持在水合物 可藉以形成的程度。進入Joule_Thomps〇n閥24下游而至 第一容器1 2的天然氣進料物流是處於第一操作溫度。 假使天然氣進料物流亦含有酸性物種,第一容器丨2内 的進料氣體被冷卻到的第一操作溫度為低於水合物生成的 溫度,但高於固態酸性物種(像是Μ與c〇2)生成的溫度 。這是用來產生水合物及避免酸性物種的固態物於第一容 器12内生成。 乾燥的酸性氣體經由乾燥酸性氣體出口離開第一容器 12。典型上,離開第一容器12的乾燥酸性氣體具有介於 10至30 bar、且低於膨脹裝置24上游壓力的標稱壓力, 以及介於10至25°C、且低於膨脹裝置24上游溫度之溫度 。術語乾燥氣體”是指不含水的氣體。 含有水合物的液體物流經由水冷凝液出口 28移出第一 容器12,並經導管29流至分離器30。水是在水冷凝液分 離器30中從冷凝液中分離。此分離器例如可以是帶有擋 板的重力分離單元《由於水比冷凝液重,故任何適當的重 力分離技術都可使用《所分離出的冷凝液經由導管31移 出’而分離出的水經由導管33移出。 1334799 將進入第一容器12的天然氣進料物流被冷卻至第一操 作溫度。或者,可使用經由經由過冷卻液體入口 μ導入 的一或多個過冷卻液體喷射液來冷卻天然氣進料物流。於 另-替代具體實例中’天然氣進料物流是肖j〇uie_ Thompson間24與經由入口 26提供的過冷卻液體兩者來冷 卻。在喷射液冷卻的例子中,天然氣進料物流可於水合物 生成溫度或高於水合物生成溫度進入第一容器丨2。
過冷卻液體入口 26應置於第一容器12内、高於澄酸 亂體進料物流的人α 2Q上。於所述具體實例中,過冷卻 液體入σ 26 4複數個喷嘴。特別的過冷卻液體為從本程 序回收與噴麗入第一容器12的冷凝液。使用喷射液是要 使過冷卻液體與氣體的接觸面積最大化’並因而使過冷卻 液體與溼酸氣體接觸的冷卻效果最大化。
將處於介於10至30 bar的壓力(低於膨脹裝置24之 上游壓力)以及第一容器丨2的操作溫度下的乾燥酸氣體 ,經由位於導管35的第二熱交換器36導入第二閃蒸槽4〇 。其於第二熱交換器36中冷卻而形成高於_56()(:之溫度的 氣體與冷凝液的兩相混合物。未顯示的是可藉由與經外部 冷束循環(如東循環)循環的^東劑間接熱交換提 供額外的冷卻。於第二閃蒸槽4〇中,將冷凝液與乾酸氣 體物流分離。液體物流經由液體出口 42離開第二閃蒸槽 40,且被充分冷卻以滿足可能被送入第一容器丨2内的過 冷卻液體入口 26的過冷卻液體所需的標準。過冷卻液體 經由設有幫浦44的導管43供應至過冷卻液體入口 26。 12 丄 乾燥酸氣體經由氣體七口 轴: 轧骽出口 47離開第二閃蒸槽40,並 A由導管45進入中間埶交換琴2 …、乂俠态以,並由此至終端使用者 (未顯示)。 如同較早所觀察到的’本發明係關於藉由形成水合物 將天然氣脫水。為防止水合物阻塞出σ 28料管Μ, 較佳為將存在於第一容器12底部的冷凝液加熱。此可適· 當地藉由使溫熱液體導入低於進料物流被導入的高度下來 導入第一容器12中。 t於第- 洛槽i 6分離的一部份溫熱冷凝液物流係經由籲 導b 17與入口 18供給入第一容器12。該溫熱冷凝液足夠 熱’以至於可液化於第一"12的第一區内形成的水合 物s水合物熔化時,在水合物晶格内捕捉的氣體被釋放 出,而水跑到含有冷凝液的溶液中。此外,至少一部分於 水/冷凝液分離器30中分離的冷凝液可(於加熱後,未顯 不)經由導管37被回收,而當作用以加熱第一容器12内 的可冷凍物種之固體物的溫熱液體來使用。 任何存在於水冷凝液分離器内的氣體皆可被回收至第 籲 谷裔12。或者或是另外地,於水/冷凝液分離器3〇分離 的—部份氣體可被回收至經由入口 2〇進入第一容器12的 漫酸氣體進料物流。 適當地’經由入口 26噴灑入第一容器的液體為天然氣 液體’此天然氣液體是C2,液化石油氣成份,qq與 Cs +碳氫化合物成份之混合物。 適當地,經由入口 18導入第一容器的溫熱液體亦為天 13 然氣液體。 現清參照冑2,其顯示本發明之另一具體實例。於此 體實你丨rfe —β 中處理已脫水氣體以使其酸成份移除。脫 7八%序已來昭固 _ …,'、圖1詳述,故於此將不再重複。具有與圖i 二元件相同功能之元件則具有相同之參考符號。 乾酸氣體經由氣體出口 47離開第二閃蒸;ft 40,並經 乾馱氣體入口 46進入第二容器14。就如同第一容器12 ,’’σ 乐二谷器14的乾酸氣體可用joule —Th〇mps〇n閥 8或其他適當的膨脹裝置(像是渦輪膨脹機),以進一步 ^卻,氣體。如同先前之第一容器12, J〇ule_Th〇mps〇n 閃可定義乾酸氣體入口 46。進入第二容器14的乾燥氣體 皿度處於第二操作溫度。第二操作溫度是酸性物種固體物 生成的最南溫度’或是酸性物種溶於液體之溫度。
备由出口 62離開第二容器14的氣體是經脫水與脫硫 的乾燥的經脫硫氣體典型上會是處於壓力介於20至 5〇bar之間以及溫度不低於-85X:的狀態。此經脫硫乾燥氣 體的產物流典型上是於室溫下送至終端使用者。 可藉由使乾燥經脫硫氣體於膨脹裝置63膨脹而進一步 冷卻乾燥經脫硫氣體的產物流,而進一步冷卻的乾燥經脫 硫氣體係在一或多個熱交換器38, 36或22中使用,以影 響裝置10内一或多個其它處理物流的冷卻。請注意到乾 燥氣體於熱交換器36内冷卻之溫度係高於在給定管線壓 力下酸性物種固體物形成之溫度。 從出口 52移出的液體含有酸性物種。 14 1334799 藉由使乾燥酸性氣《I*认 體於Joule-Thompson閱48膨脹而 將乾燥酸性氣體冷卻5 @ u & 至第—操作溫度。或者,可使用經由 入口 49提供的一或容伽、、 固過冷卻液體喷射液來冷卻乾燥酸 性氣體。於另一具體眘/丨a 、體實例中,天然氣進料物流同時為 Joule-Thompson 閥 aq λ, , 8與經由入口 49提供的過冷卻液體所 冷卻。在喷灑冷卻的例早Φ 社β_ J子中,乾综軋體可以處於或高於酸 性物種固體物形成之溫声出缺ω + 又或馱性物種浴於液體之溫度進入 第二容器14。
過冷卻液體入口 49廡σ 應位於第二谷|§ 14内且高於乾燥 酸性氣體入口 46之上。匕丄 Λ ^ 在所述具體實例中,過冷卻液體 入口 49為複數個噴霧噴喈 、務Τ嘴。可調整第二容器14内的溫度 與壓力狀態,以形成可冷;* & 凡J令凍物種之固體物。對於氣體之脫 硫’其溫度-壓力狀雜P带抽44_ ^ *調整為形成硫化氫(H2S)與二氧 化碳(C02)的固體。妷而,货 — 2 …、而第二容器内的程序狀態已足以導 致其他碳氫化合物,像异絮 . 1豕疋本、甲苯、乙基笨與二甲苯的可 冷凉·物種之固體物形成。
適當地,過冷卻液體為流經導管43的一部份液體。為 了降低溫度,此液體流經導f 5Q而後到達熱交換器38, 在此處’ T與乾燥脫硫氣體進行間接熱交換而冷卻。之後 ’乾燥脫硫氣體流經導f 65❿至熱交換g 36,以冷卻來 自第一容器12的乾燥酸性氣體。 申清人已發現到’特別的I q — q碳氫化合物成份於 液體中之濃度為當進料氣體中之每一莫耳c〇2具有〇 5到 1.5莫耳的範圍。第二容器14中的液體是從人口 49喷麗 15 1334799 入容器的液體。因此’ c2-c4碳氫化合物成份於過冷卻液體 的濃度應該介於指定範圍内。吾人應當瞭解到,假使在導 管50中q-C4碳氫化合物成份於液體物流中的濃度太低的 5貝丨了將額外的C2_C4碳氫化合物成份加入此物流中。 為防止酸性物種阻塞出口 52,存在於第二容器14底 部的冷凝液較佳為加熱的。此可藉由將溫熱液體經由低於 進料物流導入之高度的溫熱冷凝液入口 56導入第二容器 14而適當地被進行。適當的液體為流經導管50的液體。 或者亦可使用流經導管31的液體。 上述流程圖之進一步最佳化以改善熱整合是有可能的 。例如,部分經由出口 π雜 筮— * 52離開第一谷益14的碳氫化合物 液體物流可被回收至第-容器12之入口 26。為了這樣做 ,於是使用分離容器(未顯示)來將富含醆性物種的液體 物流與回收的碳氫化合物物流分離。 【圖式簡單說明】 (一) 圖式部分 圖1為本發明第-具體實例之程序流程圖;以及 圖一2為本發明另一具體實例之程序流程圖。 (二) 元件代表符號 10用於進行本發明方法之裝置 12第一容器 14第二容器 15 導管 1334799 17 導管 18 入口 20 濕酸性氣體進料物流之入口 22 中間熱交換器 24 膨脹裝置 26 過冷卻液體入口 28 水冷凝液出口 29 導管 30 分離器 31 導管 33 導管 34 乾燥酸性出口 35 導管 36 第二熱交換器 37 導管 38 熱交換器 40 第二閃蒸器 42 液體出口 43 導管 44 幫浦 45 導管 46 乾燥酸性氣體入口 47 氣體出口 48 膨脹裝置 17 1334799 49 過冷卻液體入口 50 導管 52 出口 56 溫熱冷凝液入口 62 乾燥酸性氣體出口 63 膨脹裝置 65 導管
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Claims (1)
1334799 外年丨^月^/曰修(更)正本 拾、申請專利範圍: l一種從含有水分及酸性物種的天然氣進料物流中移 除巧染物的方法,該方法包括以下步驟: 於第一容器内將該天然 中移除經脫水的氣體物流; 冷卻至酸性物種之固體物形 第二操作溫度;以及從該第 物流。 氣進料物流脫水;從第一容器 在第二容器中將經脫水的氣體 成或該酸性物種溶於液體中之 二容器移除脫水、脫硫之氣體 :2.如申請專利範圍帛!項之方法,其中將該天然氣進 料物机脫纟包括|該天然氣進料物流冷卻到形&水合物之 第—操作溫度。 3·如申請專利範圍第2項之方法,其中於第一容器中 將該天然氣進料物流冷卻至第一操作溫度之步驟包含於低 於4第一担作溫度之溫度下將該天然氣進料物流導入該第 一容器。 4·如申請專利範圍第1或2項之方法,其中於第二容 器了將該脫水氣體冷卻至第二操作溫度之步驟包含於低於 該第二操作溫度之溫度下將該脫水氣體導入該第二容器。 5.如申請專利範圍第1或2項之方法,其中於第一容 器中將該天然氣進料物流冷卻至第一操作溫度之步驟包含 於低於該第一操作溫度之溫度下將該天然氣進料物流導入 該第一容器,以及其中於第二容器中將該脫水氣體冷卻至 第二操作溫度 < ㈣包含於低於該第二操作溫度之溫度下 將該脫水氣體導入該第二容器。 1334799 6.如申請專利範圍第1項之方法,其中於第—容器中 將該天然氣進料物流冷卻至第一操作溫度之步驟包含將該 天然氣進料物流導入該第一容器,以及於低於該第—操作 溫度之溫度下將液體物流導入該第一容器,以與水合物形 成漿料。 ‘ 7·如申請專利範圍第1或2項之方法,其中於第二容 * 器中將該脫水氣體冷卻至第二操作溫度之步驟包含將該脫 水氣體導入該第二容器’以及於低於該第二操作溫度之溫 度下將液體物流導入該第二容器,以與酸性污染物形成漿參 料或混合物。 8. 如申請專利範圍第1或2項之方法,其中於第一容 器中將该天然氣進料物流冷卻至第一操作溫度之步驟包含 將該天然氣進料物流導入該第一容器,以及於低於該第一 才市作諷度之溫度下將液體物流導入該第一容器以與水合 物形成漿料,以及其中於第二容器中將該脫水氣體冷卻至 第二操作溫度之步驟包含將該脫水氣體導入該第二容器, 以及於低於該第二操作溫度之溫度下將液體物流導入該第攀 一谷器,以與酸性污染物形成漿料或混合物。 9. 如申睛專利範圍第5項之方法,其中該液體為天然 氣液體。 ▲ 1 〇·如申請專利範圍第1或2項之方法,其更包括於 e令器中加熱水合物至高於該第一操作溫度之溫度以 獲得含水液體之步驟。 U·如申請專利範圍第卜戈2項之方法,其更包括於 20 :第,容器中加熱該酸性物種至高於該第二操作溫度之溫 X以獲得含酸性物種液體之步驟。 ㈣12二申請專利範圍第1或2項之方法,其更包括於 =w中加熱該水合物以獲得含水液體,以及於該第 …中加熱該酸性物種以獲得含酸性物種液體之步驟。 13·如中請專利範圍第1()項之方法,其中於該第一容 ’、’、該水合物包含加入—種溫熱的液體至水合物中。 器中力1 如”專利制帛12項之方法,其中於該第一容 …該水合物包含加入_種溫熱的液體至水合物中。 器中力.二申請專利範圍第11項之方法,其中於該第二容 〒加熱該酸性物錄6 中。 種3加入一種溫熱液體至該酸性物種 12項之方法’其中於該第二容 入一種溫熱液體至該酸性物種 16.如申請專利範圍第 益中加熱該酸性物種包含加 中。 丨7·如申請專利範圍第 為天然氣液體。 18 ·如申請專利範圍第 為天然氣液體。 19. 如申請專利範圍第 為天然氣液體。 20. 如申請專利範圍第 為天然氣液體。
項之方法,其中該溫熱液體 14項之方法,其中該溫熱液體 15項之方法,其中該溫熱液體 16項之方法,纟中該溫熱液體 21
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NO952241D0 (no) * | 1995-06-07 | 1995-06-07 | Jon Steinar Gudmundsson | Framgangsmåte for transport og lagring av olje og gass |
US5819555A (en) * | 1995-09-08 | 1998-10-13 | Engdahl; Gerald | Removal of carbon dioxide from a feed stream by carbon dioxide solids separation |
US5783082A (en) | 1995-11-03 | 1998-07-21 | University Of North Carolina | Cleaning process using carbon dioxide as a solvent and employing molecularly engineered surfactants |
GB9601030D0 (en) * | 1996-01-18 | 1996-03-20 | British Gas Plc | a method of producing gas hydrate |
TW366409B (en) | 1997-07-01 | 1999-08-11 | Exxon Production Research Co | Process for liquefying a natural gas stream containing at least one freezable component |
CA2294742C (en) * | 1997-07-01 | 2005-04-05 | Exxon Production Research Company | Process for separating a multi-component gas stream containing at least one freezable component |
AUPQ118899A0 (en) | 1999-06-24 | 1999-07-22 | Woodside Energy Limited | Natural gas hydrate and method for producing same |
AUPQ228399A0 (en) | 1999-08-17 | 1999-09-09 | Woodside Energy Limited | Production plant |
TW573112B (en) * | 2001-01-31 | 2004-01-21 | Exxonmobil Upstream Res Co | Process of manufacturing pressurized liquid natural gas containing heavy hydrocarbons |
FR2824492B1 (fr) * | 2001-05-11 | 2003-06-27 | Inst Francais Du Petrole | Procede de pretraitement d'un gaz naturel contenant des composes acides |
CA2383283C (fr) * | 2001-05-11 | 2010-09-07 | Institut Francais Du Petrole | Procede de pretraitement d'un gaz naturel contenant des composes acides |
WO2003062725A1 (en) * | 2002-01-18 | 2003-07-31 | Curtin University Of Technology | Process and device for production of lng by removal of freezable solids |
AU2002951005A0 (en) | 2002-08-27 | 2002-09-12 | Shell Internationale Research Maatschappij B.V. | Method of removing carbon dioxide fouling from cryogenic equipment |
AU2003900534A0 (en) * | 2003-02-07 | 2003-02-20 | Shell Internationale Research Maatschappij B.V. | Process and apparatus for removal of a contaminant from a natural gas feed stream |
US6946017B2 (en) * | 2003-12-04 | 2005-09-20 | Gas Technology Institute | Process for separating carbon dioxide and methane |
-
2003
- 2003-02-07 AU AU2003900534A patent/AU2003900534A0/en not_active Abandoned
-
2004
- 2004-02-04 EA EA200501263A patent/EA009248B1/ru not_active IP Right Cessation
- 2004-02-04 CN CNA2006101685815A patent/CN1990836A/zh active Pending
- 2004-02-04 WO PCT/EP2004/050077 patent/WO2004070297A1/en active Search and Examination
- 2004-02-04 CN CN2004800036332A patent/CN1950657B/zh not_active Expired - Fee Related
- 2004-02-04 EP EP06124321A patent/EP1790927A3/en not_active Withdrawn
- 2004-02-04 AU AU2004209623A patent/AU2004209623C1/en not_active Revoked
- 2004-02-04 EP EP04707945A patent/EP1601918A1/en not_active Withdrawn
- 2004-02-04 CA CA002515139A patent/CA2515139A1/en not_active Abandoned
- 2004-02-04 OA OA1200500224A patent/OA13101A/en unknown
- 2004-02-04 EA EA200601957A patent/EA009563B1/ru not_active IP Right Cessation
- 2004-02-05 TW TW093102630A patent/TWI334799B/zh not_active IP Right Cessation
- 2004-02-05 US US10/772,621 patent/US7152431B2/en not_active Expired - Lifetime
- 2004-02-05 TW TW095146983A patent/TW200724835A/zh unknown
- 2004-02-06 MY MYPI20040360A patent/MY138913A/en unknown
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2005
- 2005-09-06 NO NO20054132A patent/NO20054132L/no not_active Application Discontinuation
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2006
- 2006-11-06 US US11/556,869 patent/US20070056317A1/en not_active Abandoned
- 2006-11-20 NO NO20065318A patent/NO20065318L/no not_active Application Discontinuation
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2009
- 2009-10-08 US US12/575,846 patent/US20100024472A1/en not_active Abandoned
- 2009-12-24 AU AU2009251211A patent/AU2009251211A1/en not_active Abandoned
Also Published As
Publication number | Publication date |
---|---|
OA13101A (en) | 2006-11-10 |
WO2004070297A1 (en) | 2004-08-19 |
US20070056317A1 (en) | 2007-03-15 |
AU2003900534A0 (en) | 2003-02-20 |
CN1950657B (zh) | 2010-06-16 |
TW200418563A (en) | 2004-10-01 |
NO20054132D0 (no) | 2005-09-06 |
EA009248B1 (ru) | 2007-12-28 |
AU2004209623B2 (en) | 2007-07-12 |
AU2004209623A1 (en) | 2004-08-19 |
AU2009251211A1 (en) | 2010-01-28 |
US7152431B2 (en) | 2006-12-26 |
US20100024472A1 (en) | 2010-02-04 |
EP1790927A3 (en) | 2008-01-16 |
EP1601918A1 (en) | 2005-12-07 |
CA2515139A1 (en) | 2004-08-19 |
TW200724835A (en) | 2007-07-01 |
EA200501263A1 (ru) | 2006-04-28 |
EA009563B1 (ru) | 2008-02-28 |
EP1790927A2 (en) | 2007-05-30 |
EA200601957A1 (ru) | 2007-02-27 |
US20040187686A1 (en) | 2004-09-30 |
NO20054132L (no) | 2005-10-11 |
CN1990836A (zh) | 2007-07-04 |
MY138913A (en) | 2009-08-28 |
CN1950657A (zh) | 2007-04-18 |
AU2004209623C1 (en) | 2009-10-08 |
NO20065318L (no) | 2005-10-11 |
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