TW204305B - - Google Patents
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- Publication number
- TW204305B TW204305B TW081103266A TW81103266A TW204305B TW 204305 B TW204305 B TW 204305B TW 081103266 A TW081103266 A TW 081103266A TW 81103266 A TW81103266 A TW 81103266A TW 204305 B TW204305 B TW 204305B
- Authority
- TW
- Taiwan
- Prior art keywords
- catalyst
- gas
- catalyst particles
- nozzle
- reactor
- Prior art date
Links
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
- B01J38/12—Treating with free oxygen-containing gas
- B01J38/30—Treating with free oxygen-containing gas in gaseous suspension, e.g. fluidised bed
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/386—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only internally, i.e. the particles rotate within the vessel
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/215—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/31—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation of cyclic compounds with ring-splitting
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00654—Controlling the process by measures relating to the particulate material
- B01J2208/00681—Agglomeration
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S502/00—Catalyst, solid sorbent, or support therefor: product or process of making
- Y10S502/515—Specific contaminant removal
- Y10S502/518—Carbonaceous contaminant
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Catalysts (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Description
0430b A 6 Π 6 經濟部屮央桴準而Μ工消"合作社印製 五、發明説明() 本發明偽有朗一種加強流體化床催化劑性質的方法 ,其偽在催化劑表面上因污染物或其他物理或化學變化而 失去活性或流醱化性質。更明確地説,本發明係有關於一 種在使用中磨掉催化劑的表面以除去催化劑表面的k薄層 使得新鮮的催化劑得以暴露出來的方法。此外,本發明是 有關一種使催化粒子去黏聚的方法。 在一個流體床催化反應器中,經過撤細分割的固態催 化粒子典型上與蒸氣的反竈媒介接觸。這些催化粒子由一 處理氣賭之上升氣流抬起且攪動以使其看起來是懸浮在氣 流中而似一沸騰掖龌,所以叫做「流醱床」。 最廣為人知也是最早應用流體床反應器技術是油的催 化裂解製造汽油及其它輕烴類。其它的用途包括殘餘物之 煉焦;煤焦氣化;苯或丁烷催化氣化成順丁烯二酸醉;丙 烯之氨氣化成丙烯丨S :以及氮化氫氣化成氣。 本發明著重在使用於流體床反應器的催化劑。經過使 用及一段時間後,因催化劑表面被污染物或反鼴生成的副 産物堵塞,或因催化劑的表面進行一種物理或化學的變化 而成一種較不具催化性的形式,流體床催化劑會失掉活性 。此外,當污染物或一種物理或化學的變化發生在催化劑 的表面時,有些催化劑變成“黏性”而小流體床粒子開始 凝聚成較大粒子。凝聚的粒子導致催化表面積的減少,因 此影《到流體床催化劑的總體性質。更甚者,凝聚的粒子 阻礙了催化劑床的自然循琛及流體化。 上述問題的代表性的解決方法是在流體床反窸器中更 (請先閲誚背而之注意事項#蜞窍本頁) 裝· 訂_ 線_ 本紙尺度逍用中國81家楳準仰5)甲4規格(210父297公;《:> -3- 81. 4. 10,000¾ (II) 經濟部屮央#準局ex工消赀合作杜印3i Λ (5 _I5J_ 五、發明説明() 換全部或部分的催化劃。這方法花费很大,不僅在於催化 劑成本.且因鼷掉流腰床反應器以進行催化薄交換;時造成 的生産損失的成本也是很大。 在此所敘述的發明的目的是提供一可解決因凝聚、污 染物或催化劑表面上的物理或化學變化所帶來的問題及延 長催化劑的壽命的方法。 已發現一種使流髏床催化劑去凝聚及因催化劑表面上 之污染作用或物理或化學變化而失去活性或流$化性質的 流體床催化劑再暴露其表面的方法。此方法^^在操作 ' & 的流體床反匾器内部實行,但也可随意地在反籯絮外被實 行,用一種連鑛或非連鑛的方式。 在一個較好的實施例中,此方法包含了在一流體床反 應器設置至少一噴嘴,經其可自反應器外部之源將氣e供 應至此反應器中。此噴嘴是設置在反應器内部使得噴嘴没 於催化床中以使逸出管口的氣體立即與催化劑接觸。從噴 嘴出來的氣體之逃脱速度為足以接觸流體化的流體床催化 劑粒子並且在谙些催化劑粒子中産生許多的碰撞。催化劑 粒子多重碰撞之衝擊力磨掉了催化劑表面,因此移去了催 化劑表面上任何的污染物或較不具催化性的物質而暴s出 新鮮的催化劑。 圖示為一簡化的流體床反應器横截面圖.説明本發明 的實施例。 流體床反應器是任何可發生氣一固或液一固接觸過程 之反應瓶。在反應瓶中.微細分割的固態粒子床(即流體 (請先間誚背而之注意事項冉場寫本頁) 裝· 本紙尺度边用中S國家標準(CNS)T4規格(210x297公;《:) —4 — 81. 4. 10,000¾ (|[) Λ 6 Π6 eft 1305 五、發明説明() (請先W1讀背而之注意事項-?!-填窍本頁) 床催化劑)藉利用處理之氣體或掖體流抬起且分開。流鱧 床反窸器可以是各種形狀及大小。典型的反應器是在反應 器底部設置一雄檷,其可容許處理之進料通過時支撑催化 劑床。本敘述的其餘部分著重在本發明的氣-固相接觸製 法的實施上。但是.此«所述的方法也同樣可應用在掖一 '固相接觭製程。 在氣一固相接觸製程中,處理産物氣體在反應器頂端 逸出。因産物氣雔通常撝帶催化劑粒子,將産物氣體流經 一分離器以移去催化劑粒子,而這些粒子經由一浸漬座回 到催化劑床上。此分離器可以是任何固體回收裝置,如抽 氣過濾器。 流體床催化劑為細撖分割的固體粒子,視其應用之不 同在大小、重量、形狀及組成不間。具觀來看,流觼床催 化劑常類似一種粉末,但是也可能為小珠狀。典型的流體 床催化粒子大小從10至200撤米不等。 經濟部屮央標準灼β工消赀合作社印¾ 在某些醮用上,流腥床催化劑的效果會因催化劑表面 上污染物的形成或物理或化學變化而降低。這種狀況會導 致催化劑活性的降低或造成催化劑變成《黏性”,因此使 催化粒子易凝聚,而失掉了流動性及/或催化活性。 在本發明的實際操作上,流體床反應器的内部設置了 一個或更多噴嘴.而一高速流動的氣體會經由此噴嘴送至 催化劑床。在本發明的實際操作的過程中,催化劑是保持 在流體化狀態(即被流體化),而這是導因於處理氣體或 其它氣體的上升氣流將催化劑粒子抬升、擾亂、及懸浮於 本紙尺度遑用中a S家標毕(CNS> Y4規格(210x297公龙) -5- 81. 4. 10,000張⑻ δ 五、發明説明() 上升氣鼸中。氣髏流的力量造成許多流體化催化》粒子間 的碰撞,而埴些碰撞的衝量會磨掉催化劑的表面Μ移去表 面上的任何汚染物,因而顯露出新鮮的催化劑。此外.催 化劑粒子碰撞造成的衝擊力將會去凝聚(即斷開)任何凝 聚的催化劑粒子。本發明也可在備有任何可使高速氣體流 與流髏化催化剤粒子接觸的裝備(如噴_或氣體分布鐵柵 或單或多孔金颶板)的任何反應器内操作。 本發明在裝備有多於一値噴嘴的流體床反應器内操作 較受偏好。此«所用的噴嘴可以是任何形狀或大小.做任 何形式的噴射。此电.廒可以簡如一開口管子或一端有燭心 或窳縮器用來加速或導引氣體逸出的短試管。管口的大小 -------- 對本發明的實際操作並不重要。管口小到直徑只有0.016 英吋的曾被使用過(在氣醱分布鐵栅中含有三個直徑0,016 英吋的鑲嵌的洞)。典型的管口大小是直徑0.0625英吋到 0.25英吋。更典型的管口大小是直徑介於0.125英吋到 ...........··'·. 經濟部屮央標準而A工消"合作社印^ (請先閲讀背而之注意事項再蜞寫本頁) 0,1875英吋。管口直徑為9/64”及5/32”者較受偏好。氣體 之逃脱速度必須足以驅使催化劑粒子産生許多力量足以磨 去催化剤表面的碰撞。通常較硬的催化劑需要較大的逃脱 速度。可以用大到轚速的逃脱速度。管口及氣體流速大小 之測定是為了決定所要使用的氣體的速度。受偏好的氣體 速度是介於200至1200fps。而氣體速度600到llOOfps更受 偏好。較合宜地,造樣的氣體速度使得氣體一催化劑的“ 接觸區域”伸展到噴嘴前數英吋而進入催化劑床。此噴嘴 可被導向以提供一値與流體化處理氣體成同流、反流或交 本紙張尺度边用中B國家標準(CNS) Ή規格(210X297公;¢) 一 6- 81. 4. 10,000張(f[) 05 Λ 6 Η 6 經洧部屮央標準而员工消伢合作杜印製 五、發明説明() 叉流向的高速氣饅流。而較合宜的是將此管嘴導向提供一 值舆流體化處理氣腥同流向的高速度氣體流。 噴嘴可放置於催化Μ床的任何地方,在此噴射的氣髖 將可接觸到流體化催化劑粒子。例如,噴嘴可放在反應器 壁之内或反慝器中間。為了使本發明的效果達到最大,噴 嘴鼴位於反窸器内部,此處催化劑的循環最好。這樣增大 了與氣匾接觸的催化劑總量。因此,噴嘴較適宜位於與浸 潰座開口相鄰或在其附近(浸潰座開口即催化劑從分離器 回到反應器的入口點)。應小心以確保自噴嘴逸出的氣醱 不會驅使催化劑進入反_器的任何内部組成,因為催化劑 與反應器組成間的碰撞將更可能摧毀催化劑,而重覆的碰 撞將損壊反窸器組成。 此高速氣體可以是任何氣鳢或液醱蒸氣,該氣體對反 應過程是羥鈍或是有助益的。典型地,此氣體是從反醮器 外部之源供應到噴嘴。當流體床反應器被用於一氧化反應 時,氣體通常是用空氣。但是,活性較差的氣體如氮氣或 反醢進料氣體也可使用。在本發明的實際操作中(卽生産 中),商用刻度的反應器以及氣體總産量的增加可被忽略 〇 將摧化劑去凝聚及再暴霉其表面的過程可以斷鑛地或 連續地被操作,其決定於催化劑與噴嘴特色之需要如噴嘴 數目、噴嘴位置及維開噴喊的氣體逃脱速度。 從催化朗表面上磨掉的污染或催化性較差的物質通常 随著反醮器的廢料移走,然後經由適當的分離方法(如抽 (請先間讀背而之注意事項再塥裒木頁) 裝- 線· 本紙尺度边用中國Β家標準(CNS) Ή規格(210x297公:《:) —Π — 81. 4. 10,000張⑻ 經濟部屮央榀準杓β工消赀合作社印製 --- 五、發明説明() 氣裝置、過濾器等)將其與反應産物分開。本發明的操作 .的一餡重要闢鍵在於控制氣體流速及噴嘴的放置使得再暴 露催化劑的表面及將催化劑去凝聚的效益增至最大,而另 一方面減少催化剤表面磨去的量以使催化劑的損失減至最小。 本發明的實施例以圓示説明。流體床反應器1#是流 流體床催化劑2。反進料氣體經由管線3進入反應器並 且通遇氣體分布檷4到達催化劑床。攜帶著催化粒子的氣 相反應産物進人抽氣裝置6,反應産物與催化劑即在此處 分離。氣相反窸産物經由管線5移出反器。催化劑經由 浸潰座7回到催化劑床2。高速氣體經由管線8供應至反 應器而經由噴嘴9導引至催化劑床。 本發明可用於任何催化性流醱床操作中,當其催化劑 表面被反應副産物或催化劑組成的物理或化學爱化所污染 時。在這種狀況下催化劑將會失去活性及/或流動性。經 由磨去催化劑表面以再暴露新鮮催化劑或將催化劑去凝聚 化,活性及/或流動性將會恢復.而催化劑的赛命就可延 長。本發明可被鼴用的代表性反應有油之催化裂解生成石 油及其他輕烴,殘餘物之煉焦.煤焦汽化,苯或正丁烷氣 化成順丁烯二酸酐,丙烯之氨氣化成丙烯丨S,及氛化氳氣 化成氣。 如本處所述,操作時高速氣體與流體化催化劑在反應 器内部接觭。本發明也可將噴嘴放置在浸潰座内部來操作 。再者,流體床反應器附有再生器,該再生器排除經過處 (請先閲讀背而之注意事項孙塡寫本頁) 本紙張尺度边用中a Η家楳準(CNS)>P4規怙(2丨0x297公¢) 81. 4. 10,000¾ (II) Λ 6 η 6 ^04305_ 五、發明説明() 理及再活化然後返回反軀器的催化劑,催化劑表面可被再 暴露且/或催化劑被去凝聚化於再生器之内或於反應器舆 再生器之間的催化劑轉移管線中。最後一點,本發明可被 «施經由從反褰器移走催化劑、再暴露催化劑表面、及/或 催化劑去凝聚化如本處所述,然後使催化劑回到反鼴器。 前面的敍述並非意欲完全包括_或限制此發明於所發 表之精確的形式,而且根據上述發表的觀點,顯然許多的 修正和變異是可能的。本叙述的目的是要解釋本發明的原 則及其實際應用,並且因之使他人熟習利用此發明於其不 同的實施例中之技術及適用於其所構思之特殊用途的不同 修正。本發明只打算定義於以下的範圍。 (請先閲請背而之注意事項再塥寫本頁) 經濟部屮央槛準而β工消"合作社印製 81. 4. 10,000¾ (II) 本紙張尺度逍用中a國家樣準(CNS)lM規怙(210x297公;tt)
Claims (1)
- 六、申請專利範面 補充 A7 B7 C7 D7 第81 103266號ffi請案申請專利範圍修正本 修正日期:82年1月 1 ..一種將流體床催化劑粒乎去凝聚或再暴露流體床催化 劑粒子的表的.方法’其表面在用於製造丙铺睛或丨噴 丁烯二酸酐時産生污染或物理或化學變化,該方法& 含在流體化狀態下使粒子大小為1 0至20 0 « m的流|| 床催化劑粒子與一速度介於β〇 · 98至366公尺/毎秒( 200到1 200吳呎/每秒)的氣體接觸,其足以使催化 劑粒子間産生充分碰撞,而去凝聚流體床催化劑粒子 ,或磨去催化劑粒子表面以除去污染或已變化的表面 (請先聞讀背面之注意事項再硯寫本頁 / .裝. 經濟部屮央標準局貝工消费合作社印製 2.如申誚專利範園第1項的方法,其中該氣體為空氣或 m*5$=r 氣° 3 .如申請專利範圍第1項的方法,其中該方法可在任何 設置使氣流與流體化催化劑接觸之装置的容器中進行 0 4. 一種將流體床催化劑粒子去凝聚或再暴露流體床催化 劑粒子表面的方法,該表面在用於製造丙烯請或順丁 烯二酸酐時産生污染或物理或化學變化,該方法包含 (a )在流體化狀態下維持催化劑粒子在流體床反 應器之内,Η中該催化_粒子大小為自1 〇至200 w m ’該流體床反應器附設至少-噴嘴,氣體從反應器夕卜 之源供應至此’而此噴嘴放置在反應器内部使得噴嘴 -10 - •訂· 本紙張尺度適用中Β國家櫺毕(CNS)甲4規格(210x297公釐) A7 C7 六、申請專利範圊 沈浸於催化劑粒子間.巨從噴嘴出來的氣體ώ:即與催化 劑粒子接觸; (bi ·氣體以60.98至366公尺/每秒( 200到12 00英呎/每# i的逃脫速度自噴嘴通過,在此處該氣 體在催化劑粒f間引起許多碰撞,其衝量足以使流體 床催化劑粒F去凝聚,或磨去催化劑粒子的表面以除 去受污染的戎己變化的表面。 5 .如申請專利範圍第4項之方法,其中該氣體為空氣或 6.如申請專利範圍第4項之法,其中流體床反應器設 有一抽氣装置以fif氣體排出物中分離催化劑,U其中 該抽氣裝置備有…浸潰座以使催化劑回到反應器a該 噴嘴就位於催化劑離開浸凟座的出口附近… 7 .如申請專利範圍第4項之方法,其中再暴露催化劑表 面的方法是W於當流體床反應器在製造順丁烯二酸酐 成丙烯睛的過程中' 8 .如申請專利範圍第4項之方法 > 其屮噴嘴管Π開口大 小為介於Μ择〇. 75公分(0.125英时)與0.47625 (請先聞請背面之注意事頊再填寫本頁 k. 經濟部屮央標準局貝工消费合作社印製 分 ι·-χ 寸 Π 11 11 本紙張尺度逋用中闺Η家標準(CNS)甲4規格(210x297公釐)
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DE (1) | DE69217650T2 (zh) |
ES (1) | ES2097870T3 (zh) |
TW (1) | TW204305B (zh) |
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SG11201500218VA (en) | 2012-07-12 | 2015-03-30 | Mannkind Corp | Dry powder drug delivery systems and methods |
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BR122019026637B1 (pt) | 2013-07-18 | 2023-09-26 | Mannkind Corporation | Formulações farmacêuticas de pó seco e método para a fabricação de uma formulação de pó seco |
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WO2015148905A1 (en) | 2014-03-28 | 2015-10-01 | Mannkind Corporation | Use of ultrarapid acting insulin |
CN103897744B (zh) * | 2014-03-28 | 2015-11-11 | 新奥科技发展有限公司 | 一种改善流化床设备内流化状况的方法 |
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CN109999729B (zh) * | 2019-04-26 | 2022-08-02 | 上海华畅环保设备发展有限公司 | 沸腾床加氢反应器中催化剂原位在线旋流活性恢复方法和装置 |
CN110052226B (zh) * | 2019-04-26 | 2022-08-02 | 上海华畅环保设备发展有限公司 | 沸腾床加氢反应器中催化剂原位在线旋流活性恢复方法和装置 |
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Publication number | Priority date | Publication date | Assignee | Title |
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US2605234A (en) * | 1947-12-01 | 1952-07-29 | Phillips Petroleum Co | Regeneration of a carbonized fischer-tropsch catalyst |
US2651600A (en) * | 1950-02-21 | 1953-09-08 | Standard Oil Dev Co | Method of reducing contaminants on finely divided catalyst |
US2958650A (en) * | 1955-07-28 | 1960-11-01 | Houdry Process Corp | Removing contaminants from catalyst particles |
US3050469A (en) * | 1959-05-25 | 1962-08-21 | Phillips Petroleum Co | Catalyst regeneration process and apparatus |
JPS61263646A (ja) * | 1985-05-17 | 1986-11-21 | Mitsubishi Heavy Ind Ltd | 石炭焚脱硝触媒の再生方法 |
-
1990
- 1990-11-15 US US07/614,311 patent/US5124291A/en not_active Expired - Lifetime
-
1992
- 1992-04-16 CN CN92103676A patent/CN1046639C/zh not_active Expired - Lifetime
- 1992-04-21 ES ES92303546T patent/ES2097870T3/es not_active Expired - Lifetime
- 1992-04-21 DE DE69217650T patent/DE69217650T2/de not_active Expired - Fee Related
- 1992-04-21 AT AT92303546T patent/ATE149099T1/de not_active IP Right Cessation
- 1992-04-21 EP EP92303546A patent/EP0566785B1/en not_active Expired - Lifetime
- 1992-04-25 TW TW081103266A patent/TW204305B/zh not_active IP Right Cessation
Also Published As
Publication number | Publication date |
---|---|
ES2097870T3 (es) | 1997-04-16 |
US5124291A (en) | 1992-06-23 |
EP0566785B1 (en) | 1997-02-26 |
DE69217650D1 (de) | 1997-04-03 |
DE69217650T2 (de) | 1997-06-12 |
CN1046639C (zh) | 1999-11-24 |
ATE149099T1 (de) | 1997-03-15 |
EP0566785A1 (en) | 1993-10-27 |
CN1077399A (zh) | 1993-10-20 |
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