201228939 六、發明說明： 本發明係關^除鹽。更特 碎裂喷射急速汽化注入以用於二：、冑明係闕於使用 (MED)除越，及錄田、〜 其是多重效應蒸餾 …除_，及一種用於此類除 類除鹽之方法。 之裝置及—種用於此 大體上將除鹽稱作自水移除鹽及其他礦物質之過程， 之=除：：準確地描述為自愈加鹽化之鹽水移除較純水 之過程。該過程最常見用以使海水或微咸的水可飲用，作 亦可應用該過程以獲得遠超出 、25飲用水要求之超純水。例 。’此類超純水可用於諸如（例如）&空引擎燃燒室的清 洗之某些工業過程。 用以除鹽之水的鹽度愈大及/或經除鹽的水之純度命 大’則在除鹽過程中所要求之能量愈大。鹽度係、根據總溶 解固體（彻）來Μ的。以毫克每升（mg/1)或百萬分率 (ppm)來量測此TDS。該兩個單位在稀釋溶液中大體上為 可互換的，但在美國更常用ppm。因而將水鹽度之類型及品 質劃分為：海水：15,000_5〇,〇〇〇 mg/1而，微咸的水： 1，500-15,000 mg/1 TDS，河水：5〇〇-3 〇〇〇 mg/l tds，及純 水.小於500 mgn TDS。多數除鹽設備主要使用海水作為 除鹽之水。 除鹽過程旨在將含鹽水分離為兩個水流：一含有低TDS 濃度之淡水流及一濃縮之鹽水流。該過程大體上為能量密 5 201228939 果型的。 在該除鹽過程中使用許多形式之能源（電化學能、核 月卜太陽能、風能等）。該過程可使㈣於此類分離之若^ :同的技#然而’大體上，可將除鹽過程劃分 ::’其涉及加熱水以產生水蒸氣;及⑻膜過程 膜來將水抑或鹽移至兩個區中：一含鹽區及—淡水區。 在該等高脫鹽容量熱技術中’多級急速汽化（聰）及 夕重效應蒸餾（MED) 相對能量密集型的二„ 知-為 市場份額。 -其，、有南產罝且已長時間享有大的 器= mED過程通常涉及將進料水（含鹽水）分佈於汽化 如海水）Γ二道)之表面上。自來源取得該含鹽進料(例 尺）且使其通過敎交拖 ^ yi m λ ^ 初始含鹽進料來… 使用來自該來源之所有 /y、”。經除鹽之蒸氣的同時，其接著經分流 且β玄初始含鹽進料中 除且返…來二 (現具有升高之溫度）被排 設備時=2 Γ’至大海)。在試圖最佳… 亦載有回收成本二此係因為經排除之鹽水 度升 #用熱量。對於水生生物，此類溫 升-之水返回至其來源可為一生態災難。 med歸因於盆盥 宣傳為轉睡之未^ 言的潛在的高熱效能而被 數目所證明，MED，且如由新近正在建造之刪設備的 是以對高品質材料=:咏1然：，當前的MED效率仍 為代價來取得的。若盎適^:化益表面）之高資本支出 Μ適S材料性質，則不可能建立高熱 6 201228939 量及質量傳遞要求。成本亦典 能量之高成本以及增力 =LT:格的排放法規及除鹽 設備容量之需要。響。亦存在増加 _ 所有s剛熱方法均遭受歸因於其 局溫操作範圍之結垢及/或積垢問題之困 ：： 作範圍之高能量要求且亦歸因於所要求之材料的 操作範圍為成本高昂的…卜，源於該高溫操作 範圍之、U后問題亦帶來顯著的財務成纟，此係歸因於用以 清除該結垢之化學物及在執行除垢時所要求之設備操作停 :時間。目此，需要可移位習知熱量及質量傳遞機構而不 曰歸因於結垢不利地影響設備壽命及歸因於設備停工及古 ί量張單而招致巨大成本的技術。在近年來，已對減小I 里使用及增加產量給予注意。 WO 2004/033920 , wo 2006/010949 ^ WO 2008/062218 可為用於理解本發明之適用先前技術。 本發明之一目標為改良除鹽設備，尤其是MED除鹽設 備。可藉由獨立請求項之特徵來達成此目標。進一步之增 強係由附屬請求項來表徵。 在一實施例中，一種裝置包含：一 MED除鹽設備；及 流體移動器，其用於用輸送流體來移動及處理工作流 體’從而提供碎裂噴射急速汽化，其中該流體移動器經配 置以將工作流體提供至該MED除鹽設備之腔室中。 在一實施例中，該流體移動器配置於一 MED腔室之底 邛處，该流體移動器的一出口位於收集在該MED腔室之底 201228939 部處之鹽水上方。較佳地，該流體移動器允許該工作流體 之喷射碎裂及其急速汽化，從而在該流體移動器之出口處 產生實質上純水蒸氣與具有微細大小分佈之含鹽小液滴之 均勻分散混合物。 在一實施例中，該流體移動器充當至一 MED腔室之入 口。較佳地，該流體移動器產生由實質上純水蒸氣及具有 微細大小分佈之含鹽小液滴組成之雙流體急速汽化羽流。 較佳地，該流體移動器自一 MED腔室之底部移動該工作流 體且將該工作流體在自該MED腔室之該底部至頂部的垂直 方向上向上注入至該MED腔室之汽化器表面上。 較佳地，該流體移動器之出口配置於高於該鹽水的高 度b之高度h處。在一實施例中’該工作流體為含鹽進料， 例如海水。 一實施例包含該等MED腔室之實質上純的高給蒸氣之 熱流體壓縮（TFC )以用於將該蒸氣與低體積分率飽和蒸汽 混合及用於使用其來作為用於下一 MED腔室之輸送流體。 較佳地’該TFC過程可回收廢熱及/或可充當真空泵。 在一實施例中，在一除鹽系統（較佳地為MED系統） 中之流體移動器可包含：一中空本體，其具備一具有實質 上恆定橫截面之直通式通道，該直通式通道具有在該通道 之一端處的一入口及在該通道之另一端處的一出口以分別 用於工作流體之進入及排放；一喷嘴，其實質上外接且通 到該通道中，介於該通道之入口及出口端之間；_入口， 其與s玄喷嘴連通以用於輸送流體之引入；及一混合腔室， 201228939 其形成於該喷嘴下游之通道内；其中該喷嘴内部幾何構造 及緊接在該喷嘴排放口上游之該通道之鏜孔構形經如此安 置及建構成最佳化在該輪送流體與工作流體之間的能量傳 遞從而使得在使用中經由輸送流體之引入，工作流體之喷 射流碎裂且經部分地霧化以形成具有局部超音速流動條件 之分散蒸氣/小液滴流動狀態。因為旨在避免形成凝結震 波’所以在十分不同的操作條件下操作該流體移動器，從 而在流體排出該流體移動器時將該等流體保持為分散蒸氣/ 小液滴狀態。 一實施例揭示一種根據一 MED過程之除鹽方法，其包 含以下步驟： 加熱含鹽工作流體； 藉由一流體移動器使用輸送流體來移動該工作流體以 用於將碎裂喷射急速汽化流體提供至一 MED腔室中至一汽 化器表面上；及 將鹽水小液滴與該工作流體蒸氣分離。 在一實施例中，將該等含鹽小液滴收集為鹽水。較佳 地，該含鹽流可歸因於由該流體移動器產生之介穩態熱動 力學或急速汽化現象而降溫同時所得之鹽水增加其鹽度。 此情形為該MED系統可為避免結垢而達成之一關鍵平衡， 但因為根據本發明之急速汽化效應，溫度下降及沈澱積垢 得以避免。 在一實施例中，該流體移動器允許該工作流體之有效 率的噴射碎裂及其急速汽化，從而在該流體移動器之一出 9 201228939 口處產生實質上純水蒸氣與具有微細大小分佈之含鹽小液 滴之均勾分散混合物。較佳％，該流體移動器藉由產生由 實質上純水蒸氣及具有微細大小分佈之含鹽小液滴構成之 雙流體急速汽化羽流來充當至一 MED腔室之入口。較佳 地，該流㈣動n將該切Μ㈣作為錢體急速汽化 羽流自-細腔室之底部遞送且將該含鹽工作流體向上注 入至汽化器表面上。 在-實施例中’該方法提供藉由將該工作流體之實質 上純的高捨蒸氣與低體積分率飽和蒸汽混合及使用該混人 物來作為用於下-MED腔室之輸送流體的該工作流體的實 質上純的高焓蒸氣之熱流體壓縮（TFC)。該TFC過程可分 別藉由回收廢熱及藉由t當真空哀來對能量及資本支出成 本之減小具有顯著影響。 在一實施例中，該方法經由該流體移動器之一出口提 供均句分散的混合物流’其反壓力通常為低於大氣壓的， 從而進纟i纟冑帛渴流及在顯著低於該工作流體的蒸氣 壓或在其標準大氣溫度及壓力（STp)值以下之飽和溫度下 的小液滴之急速汽化。 在實細例中，該分離較佳地藉由提供一除霧器來完 成’該除霧H允許該卫作流體之蒸氣經由該除霧器通過。 較佳地該含鹽工作流體可為海水。 έ根據—實施例，可提供一種在一除鹽系統（較佳為MED 系’先）中移動-工作流體之方法。該方法包含以下步驟： 將/;IL體移動器提供至該工作流體，該移動器具有一具有 10 201228939 實質上值定橫截面之直通式通道以使得該橫截面積決不下 降至小於至該流體移動器的入口之橫截面積；將輸送流體 之實質上外接流通過一環形喷嘴施加至該通道；使用急速 汽化來使該工作流體喷射流碎裂以形成具有局部超音速流 動條件之分散蒸氣及小液滴流動狀態；誘發該工作流體自 通道之一入口流動通過該通道至該通道之一出口來作為在 該流體移動器之出口處的實質上純水蒸氣（實質上純水可 具有小於或等於5_10 ppm之TDS)及具有微細大小分佈之 含鹽小液滴之均勻分散混合物。因此在流體移動器之噴嘴 下游的通道内未產生任何由輸送流體之凝結所致的超音速 凝結震波；亦即，避免了該流動通道中的凝結震波。 一實施例揭示藉由使用輸送流體來使用一用於移動含 鹽工作流體之流體移動器來在一除鹽系統中產生碎裂嘴射 急速汽化。較佳地該除鹽系統可為一多重效應蒸餾（med) 糸統。 實施例包含藉由將該MED系統之所產生的蒸氣與低 積刀率飽和蒸Ά混合及使用該混合物來作為用於下一 MED腔室之輸送流體來使用該med系統之所產生的蒸氣 之熱流體壓縮（TFC )。 實施例可改良除鹽設備（尤其是MED設備）及/或改良 與除鹽設備相關聯之能量消耗及/或成本。由於迫使該含鹽 進料在顯著低於在f知除鹽設備中的飽和溫度之飽和溫度 下π化，所以該等實施例可減小能量使用。實施例可改良 有效性’此係因為歸因於急速霧化所產生之大的表面積， 201228939 熱量及質量傳遞有效性增加且因此該MED蒸氣產量顯著增 加。實施例可歸因於減小結垢及/或減小歸因於設備停工及 高能量消耗的成本而改良設備壽命。實施例可減小結垢， 此係因為該汽化溫度顯著低於該含鹽進料之飽和溫度所 以可較少關注鹽沈澱之結垢。 . 根據本揭示案，熟習此項技術者將易於顯而易見本發 明之其他技術優勢。本申請案之各種實施例僅獲得所闡述 之優勢之-子集。對該等實施例而言，並無任一優勢為關 鍵的。可在技術上將任何所主張之實施例與任何先前所主 張之實施例組合。 併入於本發明中且構成本發明之部分的隨附圖式藉由 實例來說明本發明之當前較佳實施例，且連同上文給出之 大體描述及下文給出之實施方式—起用以藉由實例來解釋 本發明之原理。 實施例係關於使用諸如碎裂喷射急速汽化流體移動器 之流體移動器來將（含鹽）進料水遞送及/或分佈至med系 統的不同腔室之受熱MED汽化器表面（例如管道）上。、 類流體移動器引入作為液體碎裂噴射流匕 堪杆此液體碎 裂噴射流以大表面積（或微細小液滴大 丄广r j刀佈）及在低於 大耽壓的壓力環境中之急速汽化為特性。 田於藉以有效率 地進行汽化之過程係歸因於該流體移動 尸汁展現出之介穩 忍熱力學條件，該過程不同於液體噴霧 史七躺a斑 貝務之過程，此係因為 其^體力學性質顯著不同。在汽化中， 達到液體沸點， 12 201228939 而急速汽化係歸因於蒸氣壓減小所致之沸點減小。為了闡 明該過程之力學特性及其在MED系統内之使用，本發明首 先轉向該流體移動器且接著轉向該MED系統及如何在該 MED系統内使用該流體移動器。該流體移動器可在其他類 型的除鹽系統中使用。 轉向所使用之流體移動器，本發明係關於在MEd過程 中使用體移動來遞送及/或分佈（含鹽）進料水以使得 將該進料作為以大表面積（或微細小液滴大小分佈）及在 低於大氣壓的氣壓環境中之急速汽化為特性之液體碎裂噴 射流來引入。 參看圖1至圖3,流體移動器10包含工作流體通道12, 工作流體通道12具有在工作流體通道12之一端處的入口 14及在工作流體通道12之另一端處的出口 16以分別用於 工作流體18之進入及排放。工作流體丨8為（例如）諸如 海水之含鹽進料且為MED之過程流體。工作流體通道12 為中空本體’其具備如在圖2中所展示之具有實質上恆定 流體動力學橫截面12a之實質上直通式通道，其中通道12 之橫截面積決不降低至小於入口 14之橫截面積。 流體移動器10亦包含通到工作流體通道12中之輸送 流體喷嘴20,其介於工作流體通道12之入口 14與出口 16 中間。在此處所描述之實施例中，輸送流體喷嘴2 〇實質上 外接且通到工作流體通道12中，以使得環形地（亦即，以 環形形式通過環形通道）將高焓及/或高速率輸送流體22引 入至工作流體通道12中。輸送流體22 (亦稱作原動流體 13 201228939 )輸送/移動工作流體1 8。輸送流體喷嘴大體上由同 〜圓錐形筒體形狀製成，從而形成具有輸送流體喷嘴排出 口 26之輪送流體喷嘴20。輸送流體喷嘴2〇具有斂散式内 部幾何播1 再k。如在圖2中所說明，該斂散式幾何構造包含 收斂部分2 ft h1 、 刀ZUb、發散部分2〇c及位於收斂部分2〇b及發散部 20c ^ λ/. 4的喉道部分20a。在由圖1至圖3所說明之三個 實施例中，相同特徵具有相同參考數字。 例如，在圖3中，該流體移動器包含界定一通道之外 殼。該通道I古λ π , 迫/、有入口 14及出口 16且具有實質上恆定直徑。 14形成於一突出物之前端處，該突出物延伸至該外殼 中且在其夕Jx Θ 6 。界疋一增壓空間。該增壓空間具有輸送流體 4大出物在其内部界定該通道之部分。該突出物 之遠離入口丨、告 的還、在其相對外表面上錐形化，且在其與 呑亥外殼的内@ ^ 之對應錐形化部分之間界定輸送流體喷嘴 20 °喷嘴2〇與 、° a聖二間奴體連通且較佳地為環形以使得 其外接該通道。喷 噴嘴2〇具有一噴嘴入口、一噴嘴出口及介 於汲噴嘴入口盥崦 # . 一嘴出口中間的一喉道部分。該喷嘴具有 傲政式内部幾柄堪 口抑該喉道部分具有小於該喷嘴入 〜4通噴嘴出口 5|, y. _ 杈截面積的橫截面積。該喷嘴出口通 王J社该通道内界定 — 心 < 混合腔室中。 在操作中，工你& 通道12中 ^體18流動通過入口 14至工作流體 送流體22(=::輸送流體喷嘴2〇將高焓及/或高速率輸 12中。 =°音速蒸汽或氮氣）注入至工作流體通道 Τ 鞠送流體喑嵴1 Λ 又20之内部幾何構造、混合腔室1 2b、 201228939 緊接在輸送流體噴嘴排出口 26之上游及/或下游的工作流 體通道12之鏜孔構形及輸送流體噴嘴2〇與工作流體通道 12所成之入射角α經安置及建構成最佳化在高焓及/或高速 率輸送流體22與工作流體1 8之間的動量通量及能量傳遞。 高给及/或高速率輸送流體22之注入產生一空氣動力 學弓形震波28 ’空氣動力學弓形震波28之前部30位於穩 定但稀薄化之輸送流體22之周邊處。震波前部3〇以其在 熱力學及流體動力學性質（諸如壓力、速率、溫度及熵） 中的急劇改變為特性。震波前部3〇典型地藉由形成一偽收 縮口或空氣動力學喷嘴34來充當一壁且震波前部30在工 作流體18上展現出法布里阻塞效應（Fabri ch〇]dng effect )。儘官快速稀薄化（或在密度上降低）允許輸送流體 22顯著加速，但其亦在震波前部3〇後產生真空區刊（超 音速流產生低m空區）’其中在法布里阻塞條件下之工 作流體18經錢烈的急速汽化至在輸送流體震波前部3〇 後如此產生之真空36中。在介穩態熱力學條件下存在工作 流體18之劇烈急速汽化或碎裂。在此類過程中歸因於超音 速擴展的輸送流體所產生之真 亦對剪切誘發夾帶 (SIE)現象負貝’ sie現象女砵从士 篆允許工作流體丨8在輸送流體 震波月"3〇處相對於輸送流體22加速。暗 流體22與工作流體18 …輸送201228939 VI. INSTRUCTIONS: The present invention relates to the removal of salts. More special fragmentation jet rapid vaporization injection for use in two:, 胄明阙 使用 in use (MED), 越越, and logging, ~ it is multi-effect distillation... except _, and one for such demineralization The method. The apparatus and apparatus used herein to generally refer to salt removal as a process for removing salt and other minerals from water, except:: accurately describing the process of removing pure water from self-healing and salting brine . This process is most commonly used to make seawater or brackish water drinkable, and the process can be applied to obtain ultrapure water far beyond the 25 drinking water requirements. example . Such ultrapure water can be used in certain industrial processes such as, for example, & empty engine combustion. The greater the salinity of the water used to remove the salt and/or the greater the purity of the desalted water, the greater the energy required in the desalination process. The salinity system is based on the total dissolved solids. The TDS is measured in milligrams per liter (mg/1) or parts per million (ppm). The two units are substantially interchangeable in the dilute solution, but are more commonly used in the United States. Therefore, the type and quality of water salinity are divided into: seawater: 15,000_5〇, 〇〇〇mg/1, brackish water: 1,500-15,000 mg/1 TDS, river water: 5〇〇-3 〇〇 〇mg/l tds, and pure water. Less than 500 mgn TDS. Most desalination plants use seawater as the water for demineralization. The desalination process is designed to separate the brine into two streams: a fresh water stream with a low TDS concentration and a concentrated brine stream. The process is generally energy-sensitive 5 201228939 fruit type. Many forms of energy (electrochemical energy, nuclear energy, wind energy, etc.) are used in this desalination process. This process can (4) be used in such separations. However, in general, the desalination process can be divided:: 'It involves heating water to produce water vapor; and (8) membrane process membrane to water or salt. Moved to two zones: a salt zone and a freshwater zone. In this high-density capacity thermal technology, 'multi-stage rapid vaporization (Cong) and Xihou effect distillation (MED) are relatively energy-intensive two-knowledge--the market share. - It has a long history and has been in the market for a long time. The large-scale = mED process usually involves the distribution of feed water (containing brine) on the surface of vaporized water (such as seawater). The salt feed is taken from the source and passed through ^ yi m λ ^ Initial salt feed to... Use all /y," from this source. At the same time as the desalted vapour, it is then split and the β-Xuan initial salt feed is removed and returned to the second (now elevated temperature) when the equipment is discharged = 2 Γ' to the sea). Attempting to do the best... also contains the cost of recycling. This is due to the elimination of the brine. For aquatic organisms, the return of such warm water to its source can be an ecological disaster. Med is attributed to the number of pots that have been promoted for the potential high heat performance of the sputum, MED, and if the equipment is being built recently, the high quality material =: 咏1: Current MED efficiencies are still at the expense of this. If the high capital expenditure of the ^ 适 ^: 益 益 surface) Μ S S material nature, it is impossible to establish high heat 6 201228939 quantity and quality transfer requirements. The cost is also the high cost of energy and the increase of strength = LT: the emission regulations of the grid and the need for desalination equipment capacity. ring. There are also _ _ all s geothermal methods suffer from scaling and/or fouling problems due to their local temperature operating range:: high energy requirements for the range and also due to the required operating range of the material For the high cost, the post-U problem stems from the high temperature operating range and also brings significant financial success, which is attributed to the chemicals used to remove the scale and required to perform descaling. Equipment operation stop: time. Accordingly, there is a need for a technology that can shift the conventional heat and mass transfer mechanism without inadvertently affecting the life of the equipment due to fouling and incurring significant costs due to equipment downtime and costly billing. In recent years, attention has been paid to reducing the use of I and increasing the output. WO 2004/033920, wo 2006/010949 ^ WO 2008/062218 may be applicable prior art for understanding the present invention. One of the objects of the present invention is to improve desalination equipment, especially MED desalination equipment. This can be achieved by the characteristics of the independent request item. Further enhancements are characterized by an affiliate request. In one embodiment, a device includes: an MED desalination device; and a fluid mover for moving and processing a working fluid with a delivery fluid to provide a fragmentation jet rapid vaporization, wherein the fluid mover is configured to A working fluid is supplied to the chamber of the MED desalination apparatus. In one embodiment, the fluid mover is disposed at the bottom of a MED chamber, and an outlet of the fluid mover is located above the brine collected at the bottom of the MED chamber at 201228939. Preferably, the fluid mover allows the jetting of the working fluid to be fragmented and rapidly vaporized, thereby producing substantially pure water vapor at the outlet of the fluid mover and uniform dispersion of salt droplets having a fine size distribution. mixture. In one embodiment, the fluid mover acts as an inlet to a MED chamber. Preferably, the fluid mover produces a two-fluid rapid vaporization plume consisting of substantially pure water vapor and salty droplets having a fine size distribution. Preferably, the fluid mover moves the working fluid from the bottom of an MED chamber and injects the working fluid upward in a vertical direction from the bottom to the top of the MED chamber onto the vaporizer surface of the MED chamber. . Preferably, the outlet of the fluid mover is disposed at a height h above the height b of the brine. In one embodiment, the working fluid is a salt-containing feed, such as seawater. An embodiment includes substantially pure high vapor-donating hot fluid compression (TFC) of the MED chambers for mixing the vapor with low volume fraction saturated steam and for use as the next MED chamber The chamber transports fluid. Preferably, the TFC process can recover waste heat and/or can function as a vacuum pump. In one embodiment, a fluid mover in a desalination system, preferably an MED system, can comprise: a hollow body having a straight-through passage having a substantially constant cross-section, the straight-through passage having An inlet at one end of the passage and an outlet at the other end of the passage for the entry and discharge of the working fluid, respectively; a nozzle that is substantially circumscribed and opens into the passage, between the passages Between the inlet and the outlet; the inlet, which is in communication with the s-shaped nozzle for the introduction of the fluid; and a mixing chamber, 201228939 which is formed in the passage downstream of the nozzle; wherein the internal geometry of the nozzle is immediately adjacent The pupil configuration of the passage upstream of the nozzle discharge is configured and constructed to optimize energy transfer between the transfer fluid and the working fluid such that, in use, the introduction of the delivery fluid, the working fluid The jet is fragmented and partially atomized to form a dispersed vapor/small droplet flow condition with local supersonic flow conditions. The fluid mover is operated under very different operating conditions because it is intended to avoid the formation of a condensed shock wave, thereby maintaining the fluid in a dispersed vapor/droplet state as the fluid exits the fluid mover. An embodiment discloses a desalination method according to a MED process comprising the steps of: heating a salt-containing working fluid; using a fluid-moving fluid to transport the working fluid for use in a fragmentation jet rapid vaporization fluid by a fluid mover Up to a vaporization surface in a MED chamber; and separating brine droplets from the working fluid vapor. In one embodiment, the salt-containing droplets are collected as brine. Preferably, the salt-containing stream is attributable to the metastable thermodynamics or rapid vaporization produced by the fluid mover to cool down while the resulting brine increases its salinity. This situation is one of the key balances that the MED system can achieve to avoid fouling, but because of the rapid vaporization effect in accordance with the present invention, temperature drops and precipitation fouling are avoided. In one embodiment, the fluid mover allows for efficient jet fragmentation of the working fluid and its rapid vaporization to produce substantially pure water vapor and a fine size distribution at one of the fluid movers 9 201228939 The salt-containing droplets are uniformly dispersed to separate the mixture. Preferably, the fluid mover acts as an inlet to a MED chamber by creating a two-fluid rapid vaporization plume consisting of substantially pure water vapor and a salt-containing droplet having a fine size distribution. Preferably, the stream (four) moves the cut (4) as a body of rapid vaporization plume from the bottom of the thin chamber and injects the salted working fluid upward onto the vaporizer surface. In an embodiment, the method provides for mixing the substantially pure high vapor of the working fluid with a low volume fraction saturated vapor and using the mixed character as the transport fluid for the lower-MED chamber. Substantially pure sorghum vapor thermal fluid compression (TFC) of the working fluid. The TFC process can have a significant impact on the reduction in energy and capital expenditure costs by recovering waste heat and by vacuuming. In one embodiment, the method provides a uniformly dispersed mixture flow through one of the outlets of the fluid mover, the back pressure of which is typically sub-atmospheric, thereby enthalpy flow and is significantly lower than the work The vapor pressure of the fluid or the rapid vaporization of small droplets at a saturation temperature below its standard atmospheric temperature and pressure (STp) value. In a practical example, the separation is preferably accomplished by providing a mist eliminator. The mist removal H allows the vapor of the turbine fluid to pass through the mist eliminator. Preferably, the salt working fluid can be seawater. According to an embodiment, a method of moving a working fluid in a desalination system (preferably MED system) can be provided. The method comprises the steps of: providing an /IL bulk mover to the working fluid, the mover having a straight-through passage having a substantially constant cross-section of 10 201228939 such that the cross-sectional area never drops to less than the fluid a cross-sectional area of the inlet of the mover; a substantially circumfluent flow of the transport fluid is applied to the passage through an annular nozzle; rapid vaporization is used to fracture the working fluid jet to form a dispersed vapor having local supersonic flow conditions and a small droplet flow state; inducing the working fluid to flow from one of the inlets of the passage through the passage to one of the outlets of the passage as substantially pure water vapor at the outlet of the fluid mover (substantially pure water may have less than or A TDS of 5-10 ppm and a homogeneous dispersion of salty droplets with a fine size distribution. Therefore, no supersonic condensed shock wave caused by condensation of the transport fluid is generated in the passage downstream of the nozzle of the fluid mover; that is, the condensed shock wave in the flow passage is avoided. One embodiment discloses the use of a transport fluid to create a fragmentation nozzle for rapid vaporization in a desalination system using a fluid mover for moving a salt-containing working fluid. Preferably, the desalination system can be a multi-effect distillation (med) system. Embodiments include using the vapor produced by the MED system in a saturated distillation with a low build rate and using the mixture as a transport fluid for the next MED chamber to use the vapor produced by the med system. Hot fluid compression (TFC). Embodiments may improve desalination equipment (especially MED equipment) and/or improve energy consumption and/or cost associated with desalination equipment. These embodiments may reduce energy usage by forcing the salt feed to π at a saturation temperature that is significantly lower than the saturation temperature in the desalination apparatus. The examples may improve the effectiveness' because of the large surface area resulting from rapid atomization, the 201228939 heat and mass transfer effectiveness is increased and thus the MED vapor production is significantly increased. Embodiments may improve equipment life due to reduced fouling and/or reduced costs due to equipment downtime and high energy consumption. Embodiments may reduce fouling because the vaporization temperature is significantly lower than the saturation temperature of the salt-containing feed to less concern for fouling of the salt precipitate. Other technical advantages of the present invention will be readily apparent to those skilled in the art from this disclosure. The various embodiments of the present application achieve only a subset of the advantages described. For each of the embodiments, none of the advantages are critical. Any of the claimed embodiments can be combined technically with any of the previously claimed embodiments. The presently preferred embodiments of the present invention are described by way of example, and are in accordance with the The principles of the invention are explained by way of examples. Embodiments relate to the use of a fluid mover such as a split jet rapid vaporization fluid mover to deliver and/or distribute (salt) feed water to a heated MED vaporizer surface (e.g., a pipe) of a different chamber of a med system. The fluid-like mover is introduced as a liquid fragmentation jet. The liquid fragmentation jet can be sprayed with a large surface area (or a small droplet of large particles) and a rapid flow in a pressure environment below a large pressure. Vaporization is a characteristic. The process by which Tian Yu is efficient in vaporization is attributed to the thermodynamic conditions exhibited by the fluid moving cadaver. This process is different from the process of liquid spray history, which is due to its The mechanical properties are significantly different. In vaporization, the boiling point of the liquid is reached, 12 201228939 and the rapid vaporization is attributed to a decrease in the boiling point due to a decrease in vapor pressure. To illustrate the mechanical properties of the process and its use within the MED system, the present invention first turns to the fluid mover and then turns to the MED system and how the fluid mover is used within the MED system. The fluid mover can be used in other types of desalination systems. Turning to the fluid mover used, the present invention relates to the use of body movement in the MEd process to deliver and/or distribute (salt) feed water such that the feed is distributed as a large surface area (or small droplet size) And the rapid vaporization in a subatmospheric pressure environment is introduced as a characteristic liquid fragmentation jet. Referring to Figures 1 through 3, the fluid mover 10 includes a working fluid passage 12 having an inlet 14 at one end of the working fluid passage 12 and an outlet 16 at the other end of the working fluid passage 12 for respectively Entry and discharge of working fluid 18. The working fluid enthalpy 8 is, for example, a process fluid such as a salty feed to seawater and which is MED. The working fluid channel 12 is a hollow body that is provided with a substantially straight-through channel having a substantially constant hydrodynamic cross-section 12a as shown in Figure 2, wherein the cross-sectional area of the channel 12 is never reduced to less than the inlet 14 Cross-sectional area. The fluid mover 10 also includes a delivery fluid nozzle 20 that opens into the working fluid passage 12 between the inlet 14 and the outlet 16 of the working fluid passage 12. In the embodiment described herein, the delivery fluid nozzle 2 is substantially circumscribed and opens into the working fluid channel 12 such that the sorghum and/or high rate delivery is achieved annularly (ie, in an annular manner through the annular passage) Fluid 22 is introduced into working fluid passage 12. The transport fluid 22 (also known as the motive fluid 13 201228939) transports/moves the working fluid 18 . The delivery fluid nozzle is generally formed in the same shape as the conical cylinder to form a circulating fluid nozzle 20 having a delivery fluid nozzle discharge port 26. The delivery fluid nozzle 2 has a convergent internal geometry 1 again. As illustrated in Fig. 2, the convergent geometry comprises a converging portion 2 ft h1 , a knife ZUb, a diverging portion 2〇c, and a throat portion 20a located at the converging portion 2〇b and the diverging portion 20c ^ λ/. . In the three embodiments illustrated by Figures 1 through 3, the same features have the same reference numerals. For example, in Figure 3, the fluid mover includes a channel defining a channel. The channel I is substantially λ π , forced/, has an inlet 14 and an outlet 16 and has a substantially constant diameter. 14 is formed at the front end of a projection that extends into the outer casing and at its eve Jx Θ 6 . The boundary is a pressurized space. The plenum has a portion of the transport fluid 4 that defines the passage therein. The protrusion is further away from the inlet, and is tapered on its opposite outer surface, and defines a conveying fluid nozzle 20 ° between the conical portion of the inner casing and the inner portion of the outer casing. It is in communication with, and preferably annular, such that it circumscribes the channel. The spray nozzle 2 has a nozzle inlet, a nozzle outlet, and a throat portion intermediate the nozzle inlet .. The nozzle has a plurality of handles inside the arrogant type. The throat portion has a cross-sectional area that is smaller than the nozzle opening into the nozzle outlet 5|, y. _ 杈. The nozzle outlet is defined in the channel - the heart < mixing chamber. In operation, the flow 18 of the passage 12 flows through the inlet 14 to the working fluid to deliver the fluid 22 (=:: the delivery fluid nozzle 2 〇 will be sorghum and/or at a high rate of 12%. = ° sonic steam or Nitrogen) is injected into the working fluid channel 鞠 喑嵴 喑嵴 Λ Λ 20 internal geometry, mixing chamber 1 2b, 201228939 next to the working fluid channel 12 upstream and/or downstream of the delivery fluid nozzle outlet 26 The pupil configuration and the angle of incidence α of the fluid delivery nozzle 2 and the working fluid channel 12 are optimized for placement and construction of the momentum between the turbid and/or high rate transport fluid 22 and the working fluid 18. Quantity and energy transfer. Injection of high and/or high rate delivery fluid 22 produces an aerodynamic arcuate shock 28' aerodynamic arcuate shock 28 front portion 30 is located at the periphery of the steady but thinned transport fluid 22. The front part of the seismic wave is characterized by its sharp changes in thermodynamic and hydrodynamic properties such as pressure, velocity, temperature and entropy. The front portion of the shock wave typically acts as a wall by forming a pseudo-retractor or aerodynamic nozzle 34 and the front portion 30 of the shock wave exhibits a Fabri effect on the working fluid 18. Rapid thinning (or reduced density) allows for a significant acceleration of the transport fluid 22, but it also creates a vacuum zone after the front of the shock wave (supersonic flow produces a low m-space) where the Fabri blockage The working fluid 18 under conditions is rapidly vaporized to a vacuum 36 thus produced after the front portion of the fluid wave is delivered. There is severe rapid vaporization or fragmentation of the working fluid 18 under metastable thermodynamic conditions. In this type of process, the true nature of the transport fluid due to supersonic expansion is also negative for the shear-induced entrainment (SIE) phenomenon. The 砵ie phenomenon from the gentry allows the working fluid 丨8 in the transport fluid shock wave month" The 3 turns are accelerated relative to the transport fluid 22. Dark fluid 22 and working fluid 18 ... transport
仙訂迷率的減小及因此在令 流體中的橫向剪切應力之減彡 〇X 切應力有助於該工作流體之 杈〇男 ⑼”夕古〇㈣ 叉射碎裂。另外，歸因於輸送 體22之直接接觸凝結及工作流體U之直接接觸汽化， 201228939 層化蒸氣流區產生且充當一強烈混合層及/或（在可凝結 輸送流體22之狀況中）潤滑媒體以減小該橫向剪切應力同 時增強渦流剪切應力。 根據一實施例，該流體移動器可包含：一中空本體， 其具備一具有實質上怪定橫截面之直通式通道，該直通式 通道具有在該通道之一端處的一入口及在該通道之另一端 處的一出口以分別用於工作流體之進入及排放；其中該通 道之橫截面積決不減小至小於該入口之橫截面積；一喷 嘴’其實質上外接且通到該通道中，介於該通道之入口端 與出口端中間；一入口 ’其與該噴嘴連通以用於引入輸送 流體；及一混合腔室，其形成於該噴嘴下游之通道内；其 中該噴嘴内部幾何構造及緊接在該噴嘴排出口上游之通道 的鏜孔構形經如此安置及建構成最佳化在該輸送流體與工 作流體之間的能量傳遞從而使得在❹中㈣輸送流體之 引入來誘發該（該等）工作流體自該入口流動通過該通道 至該通道之出°，且該工作流體噴射流歸因於急速汽化及 部分霧化而碎裂以形成實質上純的水蒸氣與具有微細大小 分佈的含鹽小液滴之具有局部超音速流動條件的均勻分散 混合物，其在該流體移動器之出口 地徘出至MED腔室中。 根據一實施例’可提供一種稃叙 徑移動工作流體之方法。該 方法包含以下步驊：將一流體移 π邱森杈供至該工作流體， 該移動器具有一具有實質上恆定橫 、截•面之直通式通道；通 過一％形嘴嘴將輸送流體之實質 ^ 員貞上外接流施加至該通道； 在该偽收縮口 （空氣動力學喷嘴 負1 )之邊界處部分地霧化及 201228939 化該工作流體及在緊接在該收縮口之空氣動力學喉道後 的該擬收縮管的核心處急速汽化該工作流體以形成具有乃 超音速流動條件之分散蒸氣及小液滴流動狀態；誘發該 工作流體自該通道之入口通過該通道流至出口；藉此避免 由於該輸送流體的凝結而在該喷嘴下游的通道内產生超音 速凝結震波，以及避免該凝結震波之調變而改變工作流體 自該出口之排放。 上述過程之組合效應產生通過出口 16之均勻分散或混 合物流24,其背壓力通常為低於大氣壓的；從而進一步產 生強烈渦流及在比標準大氣溫度及壓力下的飽和溫度顯著 更低之飽和溫度下的小液滴之急速汽化。此流出物饋入該 MED系統的腔室。 在習知MED系統中的除鹽過程可涉及將進料（含鹽） 水分佈於在若干不同的腔室（亦稱作效應或小室）中$汽 化器之表面上而形成一薄膜以促進在每一腔室的上部區段 中將進料（含鹽）水預熱之後的汽化。圖4描繪具有該等 不同的腔室之習知MED應用之主要過程。含鹽進料Η^例 如：水）㈣其來源且被允許通過—熱交換器，通常將該 熱交換器稱作在圖5中的預熱器5〇(凝結器），在預埶器 5〇中含鹽進料18a的溫度歸因於來自經除鹽蒸氣_的孰 傳遞而上升，而經除鹽蒸氣_又凝結叫盡管使用來自該來 源之所有初始含鹽進料來凝結經除鹽蒸氣Μ，但接著將該 初始含鹽進料分流且將該初始含鹽進料中之大部分（現且 M k溫度）作為含鹽排除物6而排除线回至來源⑼ 17 201228939 如，至大海h在試圖最佳化MED設備時含鹽排除物6的 量為要害，此係因為含鹽排除物6亦攜載耗成本方可回收 之有用熱量。此外，已知對於水生生物，此類溫度升高之 水返回至其來源為一生態災難。 在％知系統中’接著允許該含鹽進料（工作流體丄8) 之剩餘較小。p分隨著其通過MED系統而獲取更多熱量， 其在最終腔室（效應）處開始m該MED過程路線行進 至第一效應。注意到該MED過程的關鍵優勢中之一者為僅 在第一效應中供應能量（以汽化器、外部熱量之形式），通 常將第-效應之壓力維持在顯著低於大氣壓的條件下。在 該等效應的其餘者中之所有過程作為此熱力學過程之級聯 來執行。 在本發明之過程的實施例中，該等效應可具有根據流 體熱傳遞表面的類型（例如. 直管道下降膜、垂直管道 上升膜纟平s道下降膜 '平板熱交換器）及鹽水流相 於蒸氣流之方肖（例如：正向、逆向或平行進給）之若干 :同的組態。在所有該等技術中，—種用以最佳化 !量傳遞之方法可為增加液體表面積。然而，在本發明之 貫施例中’流體並非作*键 乍為4膜而疋以含鹽小液滴及急迷汽 化喷射流之形式與該等流體熱傳遞表面相遇。 轉向圖5 ’說明本發明之初始MED腔室或效應之例示 性、且態之實施例。工作汽@R Y , ”體（例如諸如海水之含鹽進料 通過如^ 4中所展示之各種預熱器（凝結器）且到達最 終預熱裔5〇 ’工作流體18接著自最終預熱器50進入入口 201228939 Η作為流體移動器1G之工作流體18。在初始效應中可提 供某種开/式之泵以幫助工作流體i 8移動通過該流體移動 器由銷爐5 1所產生之輸送流體22 (例如蒸汽）進入輸送 机體喷嘴20 ’通過輸送流體喷嘴喉道—且隨著其排出輸 送流體喷嘴排出口 26而與工作流體1"目互作用。輸送流 體22之上游壓力可小於4巴。如上文描述，該流體力學特 性包括複雜的流體動力學及熱力學現象且允許工作流體18 之有效率的噴射碎裂及其急速汽化，從而在流體移動器】〇 之出口 16(其隨後充當至第-MED腔冑52之入口）處產 ^為雙流II急速汽化羽流53之實f上純水蒸氣與具有微 、田大小刀佈之含鹽小液滴之均句分散混合物24，雙流體急 ^汽化羽流53由實質上純水蒸氣及具有微細大小分佈之含 J液滴構成。不目於傳、统MED系统，將該含鹽進料自第 MED腔至52之底部作為雙流體急速汽化羽流μ來遞送 且向上注入至汽化器表面54 (諸如管道束）中。儘管傳統 MED腔至52之顯著體積及/或表面積填充有管道纟54以增 =、、傳遞效率’但本發明顯著地減少了汽化器材料使用及 A後的、、σ垢維3蔓成本。替代地，具有其微細大小含鹽小液 雙视體急速汽化羽流53增強了熱傳遞且因此增強汽化 六率$步產生實質上純的水蒸t 6〇，實質上純水蒸氣 Μ被:：通過除霧器55而進入蒸氣腔室56中。 ED腔至52處於低於大氣壓的壓力或真空條件下，且 因此：無實質上壓力恢復之情況下，在流體移動器1〇中產 生之心逮 >又化流歸因於其自身之流體動力學真空條件而繼 19 201228939 續。例如，參看圖！ ’該收縮口下游之壓力P23可小於在該 流體移動器之排出口處的壓力p24，其中P24較佳地小於或 等於0.35巴。同時，參看圖5，雙流體急速汽化羽流53演 變意s胃著咼渦流耗散及歸因於汽化之該等含鹽小液滴的密 度之增加產生易於導致小液滴聚結之環境。隨著該等小液 滴變得更大且歸因於增加的鹽度而更緻密，該等小液滴傾 向於沈降於MED腔室52之底部且形成鹽水流57，又將該 鹽水流5 7作為含鹽進料或工作流體18來遞送用於下一 MED腔室。 在蒸氣腔室56中的實質上純的水蒸氣6〇可具有兩個 組分。第一組分可為歸因於與預熱器5〇的熱交換之凝結蒸 氣60a，而第二組分可為剩餘高焓蒸氣6〇b。在蒸氣腔室％ 中的顯著純的凝結水蒸氣60a經驅動至下一凝結物混合器 59且形成所有經除鹽水之部分。在傳統med過程令，通常 將實質上純的高給蒸氣60b作為用於下一腔室汽化器之熱 源來遞送。針對本發明，亦可遵循彼過程。然而，一更有 效率的過程為藉由將實質上純的高给蒸氣_與低體積分 率飽和蒸汽混合且使㈣混合物來作為用於下—細腔室 =送流體22來使用實質上純的高 ^TFC)61。該TFC過程基本上為_蒸汽混合過程，例 二由：用中央或環形蒸汽喷出器來遞送具有高壓力值之 蒸π以產生所要求之輸送流體Tf 收廢熱及藉由充當真空果而對能量及資/ 61分別藉由回 具有顯著影響。在傳統MED系統中 出成本之減少 具二泵形成總設備成 20 201228939 本之高百分率。 象二=水流”歸因於介穩態熱力學或急速汽化現 增加。此為該系統為避免結垢而要 .. # ’右鹽水流溫度增加則原本會發生结 垢。但由於根據本發明之各 '° 殿結垢得到避免。 效應’溫度已下降且沈 轉向圖6，說明中間MED腔宮忐蚪庙 - 至戈效應之例示性組態之 實施例。該實施例與上 _ 、文所揭不之初始腔室的實施例相似 且相似特徵具有相似參考數 淮λ/ΓΕΤΛ 子儘g該佈局可使人想起標 準MED組態，但存在其★至 一此類差異為（例如）使 用上文所揭示的藉由將實 八 貝負上純的回知蒸軋00b與低體積 刀率飽和蒸汽混合且使用兮 使用该混合物作為用於下一 MED腔室 之輸送流體22之實曾卜M Α β Μ 貫質上，，屯的间蒸氣60b之TFC概念0卜 :了建立針對質量、能量及鹽度平衡之守怪方程式，開發 f擬凝結物混合器接合，點…此器件用於模型化目的。該 盗件自蒸氣腔室56之内側收集凝結物60a，且在所要求的 、'衡方程式的產生中允許該三個守恆變數。將與來自該預 熱器的凝結物組合的來自該混合器的凝結物朝向下一凝结 物混合器導引。 假定（例如）在MED設備中有14個效應或腔室，效 應η之凝結物混合器接合點59遵循—索引規則而自先前效 …接收凝結物’且遵循該索引規則而將凝結物提供至下一 效應。在圖6中之項目59揭示「自η·3,其中⑽哪，⑴) 及「接下來59混合η+3，其中（轮2 ;衫（3,4,5,6 7 9,1〇))」； 21 201228939 實施：，說明最終卿腔室或效應之例示性組態之 儘官存在與標準MED系統之相似性，但存在基本 列如，在最終腔室或效應中，不存在預熱器5。且因 實質上純的凝結水蒸氣端口 6〇a可用。替代地將該 … 至初始蒸汽凝結器單元67。然而，TFC技術61可 =縮蒸汽及將該蒸汽發送至一凝結器抑或在效… 推動輸送流體2 2。 轉向圖8,說明MED過程之腔室52中的流體移動器 之例不14實施例。在此實施例中，在MED腔室之底 部處提供流體移動器10。此_腔室52與上文所揭示之 彼：相似相_52_腔室56之間為除霧器55。 可提供真空栗71以將在刪腔室52内之壓力減小至低於 大氣壓的壓力或真空條件。 一可在MED腔t52巾提供汽化器表&54 (較佳地諸如 管道束54)。汽化器表面54可（例如）為垂直管道下降膜、 垂直管道上升膜、水平管道下降膜及/或平板熱交換器。與 不具有流體移動器10之MED系統的汽化器表面相比在 本實施例中該汽化器表面54減小’且因此汽化器材料及隨 後的結垢維護成本減小。 可提供鹽水收集器72以收集該鹽水及轉遞鹽水流57。 在圖8中之液位b指示在MED腔室52之底部處的鹽水量。 鹽水收集器72經如此配置以使得該鹽水不觸及流體移動器 10之出口 16。高度h指示流體移動器1〇之出口 16的高度。 出口 16因而位於咼度h處，該高度11在MED腔室中的 22 201228939 鹽水液位b上方。傳4触么土 流耗散及歸因於气二…化羽流53演變意謂著高渦 導致小液滴聚結之環液滴的密度之增加產生易於 於增加的鹽度而更緻密 …更大且歸因 —^ + 在这等小液滴傾向於沈降於MED腔 至5 2之底部且形成越欢勺 進料或工作㈣^ / 鹽水流57作為含鹽 吱氣诵、“愈 來遞送用於下-小室。羽流53之純水 蒸氣通過除霧器55;在 在圖8中由自羽流53至除霧器55之 箭頭60來說明此情形。 旦 文所，述之系統、方法及使用允許與除鹽有關之能 里及或成本之減小。因此本發明十分適於實行該等目標且 達成所提及之目的及優勢’以及本發明固有之其他目的及 優勢。儘官藉由參考本發明之特定較佳實施例來描述及定 義本七明’但此類參考不暗示對本發明之限制且不應推斷 任何此類限制。如一般熟習此項技術者所想到，本發明能 夠在形態及功能方面具有相#大的修改、變更及等效物。 本發明之所描述的較佳實施例僅為例示性，且未詳盡列舉 本發明之料。因&，在完全認識到在所有方面中的等效 物的情況下，意欲本發明僅受附加之申請專利範圍之範疇 限制。 圖1展示流體移動器之示意例示性實施例。 圖2展示流體移動器之例示性實施例之示意細節。 圖3展示流體移動器之進一步例示性實施例。 圖4展示MED過程之習知實施例的示意佈局。 23 201228939 圖5展示MED過程之第一腔室（第一效應）的例示性 實施例之示意佈局。 圖6展示MED過程之中間腔室（中間效應）的例示性 實施例之示意佈局。 圖7展示MED過程之最終腔室（最終效應）的例示性 實施例之示意佈局。 圖8展示在MED過程的腔室中之流體移動器之例示性 實施例。 【主要元件符號說明】 無 24The reduction in the rate of the singularity and thus the reduction of the transverse shear stress in the fluid 彡〇X shear stress contributes to the fragmentation of the working fluid (杈〇) (夕) 四古〇(四). Direct contact condensation of the transport body 22 and direct contact vaporization of the working fluid U, 201228939 The stratified vapor flow zone is created and acts as an intense mixing layer and/or (in the condition of the condensable transport fluid 22) to lubricate the medium to reduce The transverse shear stress simultaneously enhances the eddy shear stress. According to an embodiment, the fluid mover can comprise: a hollow body having a straight-through passage having a substantially ambiguous cross-section, the straight-through passage having the passage An inlet at one end and an outlet at the other end of the passage for respectively entering and discharging the working fluid; wherein the cross-sectional area of the passage is never reduced to less than the cross-sectional area of the inlet; 'It is substantially circumscribed and passes into the passage between the inlet end and the outlet end of the passage; an inlet 'which communicates with the nozzle for introducing a transfer fluid; and a mixing chamber, Formed in a passage downstream of the nozzle; wherein the internal geometry of the nozzle and the pupil configuration of the passage immediately upstream of the nozzle discharge port are so placed and constructed to optimize between the transport fluid and the working fluid The energy transfer thereby causes the introduction of a fluid in the crucible (4) to induce the flow of the working fluid from the inlet through the passage to the passage, and the working fluid jet is attributed to rapid vaporization and partial atomization. And splitting to form a substantially pure water vapor with a finely distributed salt-containing droplets of a uniformly dispersed mixture having a local supersonic flow condition, which is scooped out into the MED chamber at the outlet of the fluid mover According to an embodiment, a method for moving a working fluid can be provided. The method comprises the steps of: moving a fluid to a working fluid, the moving device having a substantially constant transverse, truncated • a straight-through passage of the face; a substantial flow of the fluid to be delivered to the passage through a %-shaped nozzle; at the pseudo-shrinkage (air The mechanical nozzle is partially atomized at the boundary of the negative 1) and the working fluid is rapidly vaporized at the core of the pseudo-shrink tube immediately after the aerodynamic throat of the shrinkage port to form a Dispersing vapor and droplet flow state of sonic flow conditions; inducing the working fluid to flow from the inlet of the passage through the passage to the outlet; thereby avoiding supersonic condensation in the passage downstream of the nozzle due to condensation of the transport fluid Seismic waves, and avoiding the modulation of the condensed shock wave to change the discharge of the working fluid from the outlet. The combined effect of the above process produces a uniform dispersion or mixture flow 24 through the outlet 16, the back pressure of which is typically subatmospheric; Intense vortexing and rapid vaporization of small droplets at a saturation temperature significantly lower than the saturation temperature at standard atmospheric temperatures and pressures. This effluent is fed into the chamber of the MED system. Desalination processes in conventional MED systems may involve distributing feed (salt) water over a surface of a vaporizer in a number of different chambers (also known as effects or chambers) to form a film to facilitate The vaporization of the feed (salt) water after preheating is carried out in the upper section of a chamber. Figure 4 depicts the main process of a conventional MED application with such different chambers. The salt-containing feed Η^, for example: water) (iv) is of its origin and is allowed to pass through the heat exchanger, which is usually referred to as the preheater 5〇 (condenser) in Fig. 5, in the preheater 5 The temperature of the salt-containing feed 18a in the crucible is attributed to the rise in the transport of the deuterium from the desalted vapour, while the desalted vapour_coagulation is said to coagulate the desalted using all of the initial salt-containing feed from the source. Steam hydrazine, but then the initial salt feed is split and most of the initial salt feed (now Mk temperature) is removed as a salt rejection 6 to the source (9) 17 201228939 The amount of salt-containing excretion 6 is critical when attempting to optimize MED equipment, because the salt-containing excretion 6 also carries a useful amount of heat that can be recovered. Furthermore, it is known that for aquatic organisms, such elevated temperature water is returned to its source as an ecological disaster. In the %-aware system, the remainder of the salt-containing feed (working fluid 丄8) is then allowed to be smaller. The p-score gets more heat as it passes through the MED system, which begins at the final chamber (effect) and the MED process route travels to the first effect. It is noted that one of the key advantages of the MED process is to supply energy only in the first effect (in the form of a vaporizer, external heat), and typically maintain the pressure of the first effect at a significantly lower than atmospheric pressure. All processes in the remainder of these effects are performed as a cascade of this thermodynamic process. In embodiments of the process of the present invention, the effects may be based on the type of fluid heat transfer surface (eg, straight pipe descending film, vertical pipe ascending film, flattening sigma falling film 'plate heat exchanger), and brine flow phase Several of the steam flow (for example: forward, reverse or parallel feed): the same configuration. In all of these techniques, a method for optimizing the amount of delivery can be to increase the surface area of the liquid. However, in the present embodiment of the invention, the fluid is not a * bond 乍 4 film and the salt heat droplets and the vaporization jets meet the fluid heat transfer surfaces. Turning to Figure 5', an exemplary embodiment of an initial MED chamber or effect of the present invention is illustrated. Working steam @RY , "body (for example, salty feed such as seawater passes through various preheaters (condensers) as shown in ^ 4 and reaches the final preheated 5 〇 'working fluid 18 followed by the final preheater 50 enters the inlet 201228939 Η as the working fluid 18 of the fluid mover 1G. An open/type pump may be provided in the initial effect to assist the working fluid i 8 to move through the fluid transporter to produce the fluid produced by the pin furnace 51 22 (e.g., steam) enters the conveyor body nozzle 20' by transporting the fluid nozzle throat - and interacts with the working fluid 1" as it exits the delivery fluid nozzle discharge port 26. The upstream pressure of the delivery fluid 22 can be less than 4 bar As described above, the hydrodynamic properties include complex hydrodynamic and thermodynamic phenomena and allow for efficient jet fragmentation of the working fluid 18 and its rapid vaporization, thereby at the outlet of the fluid mover 16 (which subsequently acts as The inlet of the first-MED chamber 52 is produced as a double-flow II rapid vaporization plume 53. The pure water vapor on the solid f and the salt-distributed mixture of the small droplets of the micro- and large-sized knife cloth 24 The two-fluid emergency vaporization plume 53 is composed of substantially pure water vapor and a J-containing droplet having a fine size distribution. The salt-containing feed is taken from the bottom of the MED chamber to the bottom of 52 without the MED system. The dual fluid rapid vaporization plume μ is delivered and injected upward into the vaporizer surface 54 (such as a tube bundle). Although the significant volume and/or surface area of the conventional MED chamber 52 is filled with the conduit 54 to increase the transmission efficiency, The invention significantly reduces the use of the vaporizer material and the post-A, σ scale dimension 3 vine cost. Alternatively, the micro-sized salt-containing small liquid double-viewing rapid vaporization plume 53 enhances heat transfer and thus enhances vaporization The rate of $ produces a substantially pure water vapor t 6 〇, substantially pure water vapor enthalpy:: passes through the demister 55 into the vapor chamber 56. The ED chamber to 52 is under subatmospheric pressure or vacuum And, therefore, in the absence of substantial pressure recovery, the resulting force in the fluid mover 1 又 re-flow is attributed to its own hydrodynamic vacuum conditions continued 19 201228939. For example, see the figure ! 'Under the shrinkage mouth The pressure P23 may be less than the pressure p24 at the discharge port of the fluid mover, wherein P24 is preferably less than or equal to 0.35 bar. Meanwhile, referring to Fig. 5, the two-fluid rapid vaporization plume 53 evolves to mean sinus turbulent flow The increase in density of such salt-containing droplets attributed to vaporization creates an environment that tends to cause small droplets to coalesce. As these droplets become larger and attributed to increased salinity, Dense, the droplets tend to settle at the bottom of the MED chamber 52 and form a brine stream 57, which in turn is delivered as a salt feed or working fluid 18 for the next MED chamber. The substantially pure water vapor 6 in the vapor chamber 56 can have two components. The first component may be the condensed vapor 60a due to heat exchange with the preheater 5, and the second component may be the remaining sorghum vapor 6〇b. The substantially pure condensed water vapor 60a in the vapor chamber % is driven to the next condensate mixer 59 and forms all of the desalinated portion. In a conventional med process, substantially pure high feed steam 60b is typically delivered as a heat source for the next chamber vaporizer. For the present invention, the process can also be followed. However, a more efficient process is to use substantially pure by mixing substantially pure high steam to low volume fraction saturated steam and (4) mixture as the lower-thin chamber = feed fluid 22. High ^TFC) 61. The TFC process is essentially a steam mixing process, and the second is performed by: using a central or annular steam ejector to deliver steam π having a high pressure value to produce the desired transport fluid Tf waste heat and by acting as a vacuum Energy and capital / 61 have significant effects by back. The cost reduction in the traditional MED system has a total percentage of the two pumps forming a total of 20 201228939.象二 = water flow" is attributed to the increase in metastable thermodynamics or rapid vaporization. This is the system to avoid scaling. # 'The right brine flow temperature increase will cause scaling. However, due to the invention according to the invention The fouling of each '° hall is avoided. The effect 'temperature has dropped and sinks to Figure 6, which illustrates an example of an exemplary configuration of the intermediate MED cavity Gongji Temple-togo effect. This example and the above _, the text Embodiments of the initial chamber are similar and similar features have similar reference numbers. This layout can be recalled as a standard MED configuration, but there is a difference of (such as) The present disclosure discloses the use of a mixture of sulphide 00b and a low volume sulphur saturated steam, and the use of the mixture as a transport fluid 22 for the next MED chamber. Α β Μ 贯 , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , The purpose of the pirate The condensate 60a is collected on the inside of the 56 and allowed to be in the required generation of the 'equation equation'. The condensate from the mixer, which is combined with the condensate from the preheater, is directed toward the next condensation. The mixer is guided. Assuming, for example, that there are 14 effects or chambers in the MED device, the condensate mixer junction 59 of the effect η follows the index rule and receives the condensate from the previous effect and follows the indexing rule. The condensate is supplied to the next effect. Item 59 in Figure 6 reveals "from η·3, where (10), (1)) and "Next 59 is mixed η+3, where (round 2; shirt (3, 4) , 5,6 7 9,1〇))"; 21 201228939 Implementation: Explain that the exemplary configuration of the final chamber or effect is similar to the standard MED system, but there are basic columns such as In the chamber or effect, there is no preheater 5. And because the substantially pure condensate vapor port 6〇a is available. Alternatively, the ... to the initial steam condenser unit 67. However, the TFC technique 61 can = reduce steam and send the steam to a condenser or push the fluid 2 2 . Turning to Figure 8, an embodiment of a fluid mover in chamber 52 of the MED process is illustrated. In this embodiment, a fluid mover 10 is provided at the bottom of the MED chamber. This _chamber 52 is a demister 55 between the similar phase _52_chamber 56 and the one disclosed above. A vacuum pump 71 can be provided to reduce the pressure within the purge chamber 52 to subatmospheric pressure or vacuum conditions. A vaporizer table & 54 (preferably such as tube bundle 54) may be provided in the MED chamber t52. The carburetor surface 54 can be, for example, a vertical duct descending membrane, a vertical duct riser membrane, a horizontal duct descending membrane, and/or a plate heat exchanger. The carburetor surface 54 is reduced in this embodiment as compared to the carburetor surface of the MED system without the fluid mover 10 and thus the carburetor material and subsequent fouling maintenance costs are reduced. A brine collector 72 can be provided to collect the brine and transfer the brine stream 57. The level b in Figure 8 indicates the amount of brine at the bottom of the MED chamber 52. The brine collector 72 is configured such that the brine does not touch the outlet 16 of the fluid mover 10. The height h indicates the height of the outlet 16 of the fluid mover 1 . The outlet 16 is thus located at a temperature h above the 22 201228939 brine level b in the MED chamber. It is said that the increase of the density of the ring droplets caused by the high vortex causes the droplets to coalesce to produce an easy increase in salinity and is more dense... Larger and attributable—^ + in these small droplets tend to settle in the MED cavity to the bottom of the 5 2 and form a more funneling feed or work (four) ^ / brine flow 57 as a salty helium gas, "more and more Delivered for the lower-cell. The pure water vapor of the plume 53 passes through the demister 55; this is illustrated in Figure 8 by the arrow 60 from the plume 53 to the demister 55. , methods, and uses that allow for a reduction in the amount of energy associated with the desalination and/or the cost reductions. The present invention is therefore well adapted to carry out the objects and at the The present invention is described and defined by reference to the particular preferred embodiments of the invention, which are not intended to limit the invention and should not be construed as a limitation. The invention can be modified and changed in terms of form and function. The preferred embodiments of the present invention are intended to be illustrative only, and not to be exhaustively enumerated. The present invention is intended to be fully recognized in all respects. The invention is only limited by the scope of the appended claims. Figure 1 shows a schematic exemplary embodiment of a fluid mover. Figure 2 shows a schematic detail of an exemplary embodiment of a fluid mover. Figure 3 shows a further exemplary implementation of a fluid mover. Figure 4 shows a schematic layout of a conventional embodiment of a MED process. 23 201228939 Figure 5 shows a schematic layout of an exemplary embodiment of a first chamber (first effect) of a MED process. Figure 6 shows an intermediate cavity of a MED process. Schematic layout of an exemplary embodiment of a chamber (intermediate effect) Figure 7 shows a schematic layout of an exemplary embodiment of the final chamber (final effect) of the MED process. Figure 8 shows a fluid mover in a chamber of a MED process Illustrative embodiment. [Main component symbol description] No 24