TW201235086A - A method for drying a wet CO2 rich gas stream from an oxy-combustion process - Google Patents
A method for drying a wet CO2 rich gas stream from an oxy-combustion process Download PDFInfo
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- TW201235086A TW201235086A TW101101296A TW101101296A TW201235086A TW 201235086 A TW201235086 A TW 201235086A TW 101101296 A TW101101296 A TW 101101296A TW 101101296 A TW101101296 A TW 101101296A TW 201235086 A TW201235086 A TW 201235086A
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- gas stream
- dryer
- rich
- dry
- regeneration
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- 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
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
- F23L7/007—Supplying oxygen or oxygen-enriched air
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/22—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/102—Nitrogen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/104—Oxygen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/60—Heavy metals or heavy metal compounds
- B01D2257/602—Mercury or mercury compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40043—Purging
- B01D2259/4005—Nature of purge gas
- B01D2259/40052—Recycled product or process gas
- B01D2259/40054—Recycled product or process gas treated before its reuse
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40077—Direction of flow
- B01D2259/40081—Counter-current
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/402—Further details for adsorption processes and devices using two beds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/60—Sorption with dry devices, e.g. beds
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/70—Condensing contaminants with coolers
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Description
201235086 六、發明說明: 【發明所屬之技術領域】 本發明係關於一種用於乾燥來自富氧燃燒製程之富含 c〇2之溼氣體流之方法,特定言之,利用乾燥劑(吸附劑) 實施吸附製程及再生此吸附劑之乾燥方法。 【先前技術】 來自富氧燃燒製程之富含c〇2之溼氣體流需經處理以移 除第一壓縮步驟期間或之後之H2〇。由於需避免固體水合 物或腐蝕物質之形成,使下游分離或注射製程期間不含水 相,故需限制富含c〇2之溼氣體流中之水分。就此乾燥步 驟或製程而言,常使用容納至少一乾燥劑之至少一容器來 吸附來自沿一個方向通過該乾燥劑之富含C02之溼氣體流 之水分。為使乾燥劑再生,沿相反方向提供通過乾燥劑床 之流動。常見裝置係兩個乾燥器,其中一者處於運作,而 另一者待命,且各自處於再生模式。 文獻WO 2009/071816 A2揭示一種於高壓下乾燥富含二 氧化碳之氣體之方法,其中於一吸附乾燥單元中清潔富含 二氧化碳之氣體,該吸附乾燥單元包含以循環方式操作之 至少兩吸附劑瓶中一瓶供應有用於乾燥之富含二氧化 碳之氣體,而另 而另-個瓶藉由乾燥單元所產生之乾氣體流加
乾燥單元之產物之加壓氣體提供至該瓶。 由此已知方法展現之缺點係,將 ’將所產生之富含二氧化碳 】61035.doc 201235086 之乾氣體用作再生氣體及在再生之後將該氣體排放至大 氣。此導致不利之C〇2損失。另一方面,C〇2再循環會不 利地提高用於壓縮之能量需求。 【發明内容】 以上缺點及缺陷係藉由用於乾燥來自富氧燃燒製程之富 含C〇2之溼氣體流之方法克服或減輕,該方法包含:將富 含C〇2之溼氣體流壓縮至乾燥製程操作壓力,於至少一冷 卻器中冷卻富含C〇2之溼氣體流,或於容納至少一乾燥劑 床之至少一乾燥器中乾燥富含CO2之溼氣體流及藉由以與 富含C〇2之溼氣體流之流動方向相反之方向使經加熱之再 生氣體通過該乾燥器來再生該乾燥劑床,於一純化製程中 將备含C〇2之乾氣體流分離為經純化之c〇2氣體流及富含 氮氣及氧氣之廢氣體流,藉此將富含氮氣及氧氣之廢氣體 用作再生軋體,及在再生之後,藉由自壓縮機導出之富 含C〇2之加壓氣體流將乾燥器清洗至少一次,及藉此以自 壓縮機導出之富含co2之加壓氣體流將乾燥器上料至乾燥 製程操作壓力’然後實施各乾燥製程。本發明之其他有利 實施例可參見附接專利申請範圍。 本發明方法提供-種具有低C 〇 2損失且能量上高效率之 乾燥f自富氧燃燒製程之富含C02之座氣體流之方法。更 ^體言之’該用於乾燥來自富氧燃燒製程之富含C02之渔 氣體流之方法提供以下優點: -因將具有低CO,含景夕裔脚m 里之乳體&用於乾燥器中之乾燥劑 再生而具有較低co2損失, 161035.doc 201235086 _減少乾燥及再生製程期間之能量消耗β 【實施方式】 本發明之其他特徵及優點將藉由以上僅以非限制性實例 方式及參照附圖給出之本發明實施例論述得以闡明。 來自富氧燃燒製程之富含eh之溼氣體流需經處理以移 除第一壓縮步驟期間或之後之Η2〇。由於需避免固體水合 物或腐#物質之形《,使叫純化製程之下游分離或注射 製程期f曰1無水才目,㈣限制富含c〇2之溼氣體流中之水 分。 依照圖卜使富含C〇2之溼氣體流1(該氣體流亦可命名為 .來自富氧燃燒製程之熱條件之煙道氣流)經由管線U引導 至一壓縮機2及在該壓縮機中將該氣體壓縮至較佳在丨〇與 60 bar之間之乾燥製程操作壓力。該壓縮機2一般具有多個 壓縮台及因此亦可在一中間壓縮台處安裝乾燥單元6ι、 6.2。最佳地,作為乾燥製程操作壓力之壓力係於乃至η bar範圍内選擇。因此,可藉由壓縮台排放2與乾燥器&^、 6.2之間之一冷凝步驟來最小化乾燥製程之水負載量。於 圖1中所示之本發明實施例中’引導位於壓縮機2下游之熱 氣體流1(經由管線⑴及於至少__冷卻器,較佳於兩個冷卻 器3.1及3.2中冷卻。進一步較佳地,佈置位於冷卻器下 游之一煙道氣處理裝置4用於移除Hg、s〇x、灰塵及類似 物質,及較佳佈置位於冷卻器3.2下游之一蒸氣液體分離 器5用於將冷凝水分自氣體流分離及佈置經由管線μ引向 廢水處理(未顯示)之一液體出口。提供煙道氣處理裝置4延 161035.doc 201235086 長位於乾燥器6」、6·2中之乾燥劑7.卜7.2之使用期限,同 時提供蒸氣液體分離器5將有助於減小乾操器HU之尺 寸。 。,佳將兩乾燥肢!、6 2佈置於冷卻器3卜3 2下游以乾 燥田gC〇2之渔氣體流1。各乾择哭卢仏 合靶岛器谷納用於吸附富含C02 之澄氣體流1中之水分之至少-乾燥劑固定床7」、7_2。根 據本發明,各乾燥器6.卜6.2以乾燥模式及再生模式交替 工作。於乾燥模式中,富合Γ 3 C〇2之溼氣體流1係藉由乾燥劑 7.2乾燥及於再生模式中’乾燥劑7卜7.2係藉由再生 氣體流9再生。依照圖卜乾燥器Μ處於乾㈣式及㈣ 盗6」處於再生模式或待命模式。因此,若使用兩或更多 個乾無器 以如上所述般進行使用。間門…、⑽及⑴⑴可相 應地打開及/或關閉。 本發明之另一較佳實施例提供一 種佈局,其具有串聯操 作之兩乾燥器6.1、6·2(圖中並去_、 “ I圆甲1未顯不),其規定係改變富 含C〇2之氣體流1通過乾燥器6 G.2之順序以防止水滲漏 至下游系統中。於此等佈局中,富 . 田3 C〇2之氧體流1首先通 過之乾燥器6.1、6·2亦將隨後先5,丨、去甘 通便无到達其吸附容限。依照改 變之順序藉由使氣體旁通來將此乾燥器6 ι、Μ自操作分 離’隨後實施再生及重置至操作中,彼意指再次使富含 C〇2之氣體流1通過經再生之乾燥器6J6 2。 在乾燥器6.1、6.2下游,富含>妙尸 田S L〇2之乾氣體流(乾煙道氣 流)8會經由一純化製程(未顯示) )其中畐含〇02之乾氣體 161035.doc 201235086 流8分離為幾乎純之c〇2氣體流及含有大量氮氣及氧氣之廢 氣體流。 根據本發明,將含有氮氣及氧氣之廢氣用作再生氣體9 及經由管線12以與富含C〇2之溼氣體流丨之流動方向相反之 流動方向引導至乾燥器61、6 2,及於乾燥器6〖、6 2之再 生模式期間,使乾燥劑7.丨、7 2中之水分脫附。將再生氣 體•·引導至乾燥器6.1、6.2之前,藉由一加熱器1 〇將其加 熱至較佳高於16〇t及低於3〇〇t之溫度。於乾燥模式期 間,再生氣體流9使用較富含c〇2之溼氣體流j更低之壓 力。該再生製程會週期性複現,但循環時間係視乾燥劑 7·1、7.2(吸附劑)及富含eh之溼氣體流1之水分含量而 定。 根據本發明,在乾燥劑7丨、72再生之後以富含c〇2之 氣體流將㈣器6」、6.2清洗或清潔至少—次,且該清洗 氣體流^自壓縮機2之出D獲得。乾燥器61、6.2之清洗係 藉由以富含(:02之氣體流進行部份加壓實施,接著使乾燥 β 6.1、6.2減壓至大氣壓或分別返回至上游製程或乾燥製 程。需進行清洗以減小因再生氣體流9進人乾燥器6ι、Μ 而混入之諸如氮氣之惰性氣體之含量。依照圖i,富含⑺2 之氣體流較佳係直接自壓縮機2之出口(位於冷卻器Η、 3.2上游)經由管線14獲取。m丄 _ 又取根據圖2中所示之另一較佳實施 例,用於清洗乾燥器6 1 , Λ • 、6.2之富含c〇2之氣體流係自冷 钟β 3.1、3.2下游纟^線15獲取及在加熱器财加熱至至 v8〇 C &後使心含叫之氣體流用於清洗乾燥器6 1、 161035.doc 201235086 6 ·2。藉由將富含c〇2之氣體流加熱至上述溫度,可避免因 氣體擴散至具有再生氣體壓力之乾燥容器所導致之固體 C〇2形成。 根據本發明’爲了將乾燥器6.1、6.2重置至操作模式, 在再生製程及/或清洗製程之後’藉由富含C〇2之氣體流使 乾燥器ό. 1、6.2中之壓力提高至乾燥製程操作壓力。依照 圖1,用於提尚乾燥器6.1、6.2中之壓力之富含c〇2之氣體 較佳係直接自壓縮機2之出口(位於冷卻器3 1、3 · 2上游) 經管線14獲取。根據圖2中所示之另一較佳實施例,用於 提高乾燥器6.1、6_2中之壓力之富含c〇2之氣體流係自冷 卻器3.1、3.2下游經管線15獲取及在加熱器1〇中加熱,然 後將該富含c〇2之氣體流引導至乾燥器6 j、6 2。因此, 富含c〇2之熱氣體流(藉由壓縮機2或藉由加熱器1〇加熱)係 用於裝料乾燥器6.1、6.2。 藉由在本發明之乾燥製程之前裝料乾燥器61、6.2,則 可防止在再生製程與乾燥製程之間之變換期間發生壓力波 動,係因壓力波動可導致諸如乾燥器床(乾燥劑床)壓實/粉 碎或床升之破壞,防止上行加壓流動,及壓縮機2可能發 生之關停或製程中斷。因此,提供位於入口中之至少一閥 門16,!、16.2及位於出口管路(或直接接合於乾燥器^.卜 t)·2上)宁之至少 A K冋祀琛器 .1、6.2中之壓力。用於分別減小壓力或緩解乾燥器 6.2之常見方法為經由閥⑽」、18 2將所容納氣體送至大 氣。此亦可藉由裳料再生氣體實施。若正常供料及產物管 161035.doc 201235086 線受阻,則實施此操作。 藉由將本發明之富含c〇2之熱氣體流用於裝料乾燥器 6.1、6.2以替代使用來自乾燥器61、6.2之乾冷C〇2流,可 避免乾燥器6· 1、6.2中所使用之材料及乾燥劑7.1、7.2發生 熱應力。藉由使用本發明之熱氣體流,可避免絕熱膨脹至 乾燥器6.1、6·2中之後因低溫而導致乾冰形成(最壞情 況)’係因膨脹之熱氣體流亦具有較低但不太冷之溫度。 富含C〇2之熱氣體流之溫度係由壓縮機2之壓縮關係決定且 較佳係於80與140。(:之間。於其他情況中,當在加熱器1〇 中加熱富含C〇2之氣體流時,較佳先將其加熱至至少 80 c ’然後將富含c〇2之氣體流用於裝料乾燥器61、 6.2。 就乾燥器6· 1、6.2之第一次加壓或裝料而言,在系統建 立之後便無需特殊裝置。此較佳係藉由保證在壓縮機啟動 ^用於吸附操作所需之所有乾燥器.6.1、6.2中之所有乾燥 4床7.1、7.2對壓縮機2打開而得以實現,彼意指使適當的 閥門打開。 6.2之操作模式(乾燥、再生、清洗、裝 16_1 、 16.2 、 17.1 、 17_2 、 18.1 、 18.2 、 根據乾燥器6.1、 料或待命),使閥門 19-1 ' 19.2 ' 20 1 . • 、20,2、21及22打開或關閉。例如,於乾 燥製程期間,鉍、降 乾知益6.2之閥門20.2及17·2(或乾燥器6丨之 协^ .1及丨7·1)打開,乾燥器6.2之所有其他閥門關閉。 62之19期間,閥門21(僅存在於圖2之實例)、乾燥器 及18.2(或乾燥器6_1之閥門19丨及18丨)打開,乾 161035.doc 201235086 燥器ό·2之所有其他閥門關閉(包括僅存在於圖2之實例中之 閥門22)。於清洗製程期間,閥門22(僅存在於圖2之實例 中)及乾燥器6.2之16.2(或乾燥器6.1之閥門16.1)打開且在 達到特定壓力水準,較佳10至丨5 bar之壓力之後關閉。隨 後打開閥門18.2(或乾燥器6.1之閥門18.1)以對系統再次減 壓。可重複此順序以防止雜質含量過高。於其他情況中, 乾燥器6.1、6.2之裝料可藉由打開閥門22(僅存在於圖2之 實例中)及乾燥器6.2之閥門16.2(或乾燥器6.1之閥門16.1) 來啟動’乾燥器6.2之所有其他閥門關閉(包括僅存在於圖2 之貫例中之閥門2 1)。當乾燥器6.1、6.2中之壓力水準達到 乾燥製程操作壓力水準時,可打開管線丨丨2及其製程閥門 20.2及乾燥器6.2之閥門17.2(或管線u」及其閥門2〇」及乾 燥器6.1之閥門17.1:)以將各乾燥器重置為吸附操作,彼意 指乾燥操作。 本發明之乾燥及再生製程提供針對能量消耗及低c〇2損 失之最佳解決方式。 雖然本發明已參照各示例性實施例進行描述,然而熟習 本項技術者將琿解,可在不脫離本發明範圍下進行各種變 化及其元件可經等效物替代。此外,可實施許多修改以使 本發明教義適應具體情況或材料而不脫離本發明之實質範 圍。因此,本發明並非限制於作為實施本發明之最佳模式 而揭不之具體實施例,本發明將包括屬於附接專利申請範 圍内之所有貫施例。 【圖式簡單說明】 161035.doc 12 201235086 富氧燃燒製程之 富氧燃燒製程之 圖1係根據第一實施例之用於乾燥來 富含C〇2之溼氣體流之方法之示意圖, 圖2係根據第二實施例之用於乾燥來 富含C〇2之溼氣體流之方法之示意圖。 " 【主要元件符號說明】 1 富含co2之溼氣體流 2 壓縮機 3.1 冷卻器 3.2 冷卻器 4 煙道氣處理裝置 5 蒸氣液體分離器 6.1 乾燥器 6.2 乾燥器 7.1 乾燥劑床 7.2 乾燥劑床 8 昌含c〇2之乾氣體流 9 再生氣體 10 加熱器 11 管線 11.1 管線 11.2 管線 12 管線 13 管線 14 管線 161035.doc -13- 201235086 15 管線 16.1 閥門 16.2 閥門 17.1 閥門 17.2 閥門 18.1 閥門 18.2 閥門 19.1 閥門 19.2 閥門 20.1 閥門 20.2 閥門 21 闊門 22 閥門 161035.doc
Claims (1)
- 201235086 七、申請專利範圍: 1. 一種乾燥來自富氧燃燒製程之富含eh之溼氣體流之方 法,該方法包含: 將該田3 C〇2之屋氣體流(1 )壓縮至乾燥製程操作壓 力, ' 於至少—冷卻器(3.1、3.2)中冷卻該富含(:02之涯氣體 流(1), 或於容納至少一乾燥劑床(7.1、7.2)之至少一乾燥器 (6.1、6.2)中乾燥該富含c〇2之渔氣體流⑴及藉由以與該 富含C02之渔氣體流⑴之流動方向相反之方向使經加熱 之再生氣體(9)通過該乾燥器(61、6 2)來再生該乾燥劑 床(7.1 、 7.2), 於純化製程中將富含c〇2之乾氣體流⑴分離為經純 化之C02氣體流及富含氮氣及氧氣之廢氣體流, 藉此將該富含氮氣及氧氣之廢氣體流㈣再生氣體 (9), 及在再生之後,藉由自壓縮機(2)導出之富含c〇2之永 壓氣體流將該乾燥器(6」、6.2)清洗至少一次’ f藉此以自該壓縮機(2)導出之富含C〇2之加壓氣體流 將。亥乾燥裔(6· 1、6.2)裝料至乾燥製程操作麗力,然後實 施各乾燥製程。 2.如請求们之方法’其中該乾燥製程操作壓力係於_ 60 bar之間。 月长項1之方法’其中在該再生製程期間該再生氣體 16I035.doc 201235086 (9)之壓力低於該乾燥製程操作壓力。 4.如請求項1之方法,其中用於清洗該乾燥器(6」、6 2)之 富含C〇2之加壓氣體流係直接自該壓縮機(2)不游獲取並 直接供料至該乾燥器(6.1、6.2)。 5·如請求項1之方法,其中用於清洗該乾燥器(6丨、6 2)之 富含c〇2之加壓氣體流係自該冷卻器(31、3 2)下游獲取 及藉由一加熱器(10)加熱至至少8〇t,然後供料至該乾 燥器(6.1 、 6.2)。 6. 如請求項丨之方法,其中用於在各乾燥製程之前裝料該 乾燥器(6」、6.2)之富含C〇2之加壓氣體流係直接自該壓 縮機(2)下游獲取並直接供料至該乾燥器(61、6 2)。 7. 如請求項丨之方法,其中用於在各乾燥製程之前裝料該 乾燥器⑹、6.2)之富含C〇2之加壓氣體流係自該冷卻器 (3·。1、3·2)下游獲取及藉由一加熱器(10)加熱至至少 80°C ’然後供料至該乾燥器(6.丨、6 2)。 8. :請求項i之方法’其中包含於該富含c〇2之渔氣體流⑴ 中之Hg及/或处及/或灰塵係藉由位於該乾燥器⑹、 6.2)上游之一煙道處理裝置(4)移除。 9. 如清求項丨之方法, a ^ 3於〇哀田含C〇2之溼氣體流(1) ^ 邛份蒸氣係藉由位於該乾燥器(6.1、6,2)上游之一 蒸氣液體分離器(5)冷凝及排出。 ' 10. 如請求項1之方法, .哭n〇h 其中°亥再生乳體流(9)係藉由一加孰 〇)加熱至160至3〇〇t之溫度。 ‘, 11. 女响求項i之方法,其中為了乾 田3 之溼氣體流 16I035.doc 201235086 ⑴,使用兩或更多個乾燥器(6·1、6.2)及使其等彼此平 行佈置及藉此一乾燥器處於乾燥模式及其他者則處於再 生模式或待命模式。 ' 12. 如請求項1之方法,其中爲了乾燥該富含c〇2之溼氣體流 (1),使用兩乾燥器(6」、6 2)及將其等以串聯方式佈置 及藉此使該兩乾燥器(6〗、6 2)處於乾燥模式,或藉由使 該富含C〇2之溼氣體流(丨)旁通該經再生之乾燥器(6 1 6.2)而使該兩乾燥器(6·ι、6 2)中之一者處於再生模气 同時使另一乾燥器(6.1、6.2)處於乾燥模式。 13. 如請求項12之方法,其中在再生之後’將該經再生之乾 燥器(6.1、6.2)設定為該等乾燥器(6.1、6,2)备 ^承列中之第 -一乾燥器(6.1、6.2)。 161035.doc
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US20150362187A1 (en) | 2014-06-16 | 2015-12-17 | Alstom Technology Ltd | Gas processing unit and method of operating the same |
US9791852B2 (en) | 2014-08-21 | 2017-10-17 | General Electric Technology Gmbh | Apparatus and method for controlling at least one operational parameter of a plant |
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US7666251B2 (en) * | 2006-04-03 | 2010-02-23 | Praxair Technology, Inc. | Carbon dioxide purification method |
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