201211375 六、發明說明： 【發明所屬之技術領域】 本發明大體上係關於製程流之冷卻或冷凝中之能量轉 換。自製程流之廢熱可在有機郎肯循環系統中轉化為機械 - 能而產生電能》 * 本申請案主張2010年8月27曰申請之美國申請案第 12/870,036號之優先權。 【先前技術】 悉知郎肯循環系統為一種將熱能轉化為機械軸功率之簡 單且》丁靠設備。在遭遇低位熱能時，有機工作流體係用於 代替水/蒸汽。利用低位熱能（一般地，275<>c及更低）操作 之水/蒸汽系統會具有相關之高體積及低壓。因此，使用 低壓蒸汽作為工作流體之蒸汽郎肯循環導致大型汽輪機具 有2發電效率。為維持系統尺寸小且效率高，採用滞點接 近至溫之有機工作流體。相較於低操作溫度下之水，該等 流體具有賦予較高容量之較高氣體密度及賦予較高效率之 有利運輸及傳熱性質。在工業生產環境中，有更多的機會 來使用諸如甲苯及戊燒之可燃性工作流體，特定言之工業 生產* &之工業生產或儲存現場具有大量可燃物時。然 • ❿’理想的有機工作流體應係環境可接受、不可燃，且具 有低毒性’並在正壓下操作。該等流體揭示於以引用其全 文的方式併入本文中之仍7 428 816 82中。 有機郎肯循環（「0RC」）系統常用以回收自工業生產之 廢熱。該等系統在潛熱輸出為變量及直接負載匹配變得困 155228.doc 201211375 難’而混淆熱電聯合彳、統之有效操作時❹在此實 例中，可藉由使用有機郎肯循環系統將廢熱轉化為轴功 率。此軸功率可用以（例如）操作泵，或其可用以發電。藉 由採用此方法’總生產效率更高且燃料利用率降低。可減 少發電之氣體排放，因為產生電能之絕大部分需求係由廢 熱提供》 【發明内容】 本發明之-主要實施例為一種由有機郎肯循環系統中之 具有不同溫度之兩或更多種製程流發電裝 括-或多個用於交換至少一種低溫製程流與液態郎= 工作流體t間的熱量以獲得-種經加熱之卫作流體之低溫 交換器；—或多個用於交換至少—種高溫冑程流與該經加 熱的工作流體之間的熱量以獲得一種經汽化的工作流體之 高溫交換器；一個由該經汽化的工作流體驅動以發電給輸 出軸及減壓工作流體之膨脹器；一個用於降低該減壓工作 流體之溫度以獲得一種液態工作流體之工作流體冷凝器； 一個使該液態工作流體於循環系統中循環之泵；將一或多 個低/JUL父換器、尚溫乂換器、膨脹器、冷凝器、泵及該等 交換器中之一或兩者周圍之工作流體旁道連接之導管； 及 個用於監測兩或更多種製程流及工作流體之流速、 溫度及壓力及用於提供控制信號給泵及膨脹器之控制器。 一更特定實施例為一種藉由有機郎肯循環系統中之具有 不同溫度之兩或更多種製程流發電之裝置，該裝置包括： 一個藉由加熱液態郎肯循環工作流體獲得經加熱的工作流 155228.doc -4- 201211375 體而使至少一種低溫製程流冷凝之低溫冷凝器；一個藉由 加熱該經加熱的工作流體獲得經汽化的工作流體而使至少 一種尚溫製程流冷凝之高溫冷凝器；一個藉由該經汽化的 工作流體驅動而發電給輸出軸及減壓工作流體之膨服器，· -個用於If低該減壓工作流體之溫度以獲得一種液態工作 流體之工作流體冷凝器；一個使該液態工作流體於循環系 統中循環之栗’將低溫冷凝器、高溫冷凝器、膨脹器、冷 凝器、系及該等冷凝器中之—或兩者之卫作流體旁道 連接之導管，及-個用於監測S或更多種製程流及工作流 免速狐度及壓力及用於提供控制信號給泵及膨脹器 之控制器。 -替代性實施例為—種藉由有機郎肯循環系統中之具有 不同溫度之兩種製程流發電之方法，該方法包括：藉：加 熱液態郎肯循環卫作流體獲得經加熱的卫作流體而使低溫 製程流冷卻；藉由加熱該經加熱的工作流體獲得經汽化的 工作流體而使高溫製程流冷卻；使該經汽化的工作流體擴 張以發電給輸出轴及減壓卫作流體使該減壓工作流 體冷凝以獲得液態郎肯循環工作流體。 :從^發明之以下詳細描述中獲得及推斷本發明之其他 目才示、貫施例及細節。 【實施方式】 二更充分地理解有機郎肯循環設備可如何組態以利用 将α顧塔之廢熱，圖中提供基礎設備組態圖。高溫塔⑺ 用於措由蒸館分離饋送流11中之兩或更多種組分，利用 155228.doc 201211375 再沸器12對該塔提供熱量。導管13中之塔頂蒸汽通過郎肯 循環交換器100之區段1〇〇B，其中至少部分冷凝為液體且 經導管14送至接收器15。平行地，低溫塔2〇係用於藉由蒸 傭分離饋送流21中之兩或更多種組分，利用再沸器22對該 塔提供熱量。導管23中之塔頂蒸汽通過郎肯循環交換器 100之區段100A，其中至少部分冷凝為液體且經導管24送 至接收器25。低溫塔塔頂傳熱至經由導管1〇1進入交換器 的郎肯流體，然後高溫塔塔頂傳熱至郎肯流體，因為此階 段之轉移更有效地增加經加熱的郎肯流體1〇2之溫度。離 開交換器之兩製程流（24及14)之溫差較佳為至少1〇β(：，然 而，無意由此限制本發明。 以框5 0體現之郎肯循環系統並不受限於冷凝氣流（諸如 13及23)。在交換器100之兩或更多區段中與郎肯循環工作 流體交換熱量之任何製程流（諸如冷卻之混合相或液流）係 在本發明範圍内。本發明可更爲有效地冷凝，因為製程流 之入口與出口間之溫度範圍較小。個別交換器可用於交換 器1〇〇中所示之兩或更多個服務而非該交換器之區段，即201211375 VI. Description of the Invention: TECHNICAL FIELD OF THE INVENTION The present invention generally relates to energy conversion in cooling or condensation of process streams. The waste heat of the self-contained process can be converted into a mechanical-energy-generating electric energy in the organic Rankine cycle system. * This application claims priority to U.S. Application Serial No. 12/870,036, filed on August 27, 2010. [Prior Art] The known Langken cycle system is a simple and stable device that converts thermal energy into mechanical shaft power. In the case of low heat, an organic workflow system is used instead of water/steam. Water/steam systems operating with low thermal energy (generally, 275 <>c and lower) will have associated high volume and low pressure. Therefore, the use of low-pressure steam as the working fluid's steam Rankine cycle results in a large steam turbine with 2 power generation efficiencies. In order to maintain a small system size and high efficiency, an organic working fluid with a hysteresis approaching to temperature is used. These fluids have a higher gas density that imparts higher capacity and a favorable transport and heat transfer property that imparts higher efficiency than water at low operating temperatures. In an industrial production environment, there are more opportunities to use flammable working fluids such as toluene and pentane, especially when industrial production or storage sites in industrial production or storage sites have large amounts of combustibles. However, 理想' ideal organic working fluids should be environmentally acceptable, non-flammable, and have low toxicity and operate under positive pressure. Such fluids are disclosed in still incorporated herein by reference in its entirety. The Organic Rankine Cycle (“0RC”) system is commonly used to recover waste heat from industrial production. These systems become trapped in the latent heat output as variables and direct load matching becomes 155228.doc 201211375 Difficult to confuse the combined heat and power of the combined heat and power, in this example, the waste heat can be transformed by using the organic Langken cycle system For the shaft power. This shaft power can be used, for example, to operate a pump, or it can be used to generate electricity. By adopting this method, the total production efficiency is higher and the fuel utilization rate is lowered. The gas emission of power generation can be reduced, because most of the demand for generating electric energy is provided by waste heat. SUMMARY OF THE INVENTION The main embodiment of the present invention is a two or more different temperatures in an organic Rankine cycle system. The process flow power generation includes - or a plurality of low temperature exchangers for exchanging heat between at least one low temperature process stream and liquid lang = working fluid t to obtain a heated working fluid; or a plurality of a high temperature process stream and heat between the heated working fluid to obtain a vaporized working fluid high temperature exchanger; a driven by the vaporized working fluid to generate electricity to the output shaft and the reduced pressure working fluid An expander; a working fluid condenser for reducing the temperature of the decompressed working fluid to obtain a liquid working fluid; a pump for circulating the liquid working fluid in the circulation system; replacing one or more low/JUL parent a conduit, a temperature converter, an expander, a condenser, a pump, and a conduit connecting the working fluid bypasses around one or both of the exchangers; Measuring the flow rate of the process fluid stream and the working of two or more, and the temperature and pressure of the pump and for providing a control signal to the controller of the expander. A more specific embodiment is a device for generating electricity by two or more process streams having different temperatures in an organic Rankine cycle system, the apparatus comprising: a heated work obtained by heating a liquid Rankine cycle working fluid Stream 155228.doc -4- 201211375 a cryogenic condenser that condenses at least one low temperature process stream; a high temperature condensation that condenses at least one still temperature process stream by heating the heated working fluid to obtain a vaporized working fluid a sweller that is driven by the vaporized working fluid to generate electricity to the output shaft and the decompressing working fluid, a working fluid for if the temperature of the decompressing working fluid is lower to obtain a liquid working fluid a condenser; a pumping fluid that circulates the liquid working fluid in the circulation system - a cryogenic condenser, a high temperature condenser, an expander, a condenser, a system, and the like Connected conduits, and a control for S or more process flows and workflows for speed-free fox and pressure and for providing control signals to the pump and expander . An alternative embodiment is a method of generating electricity by two process streams having different temperatures in an organic Rankine cycle system, the method comprising: heating a liquid Langken cycle fluid to obtain a heated service fluid Cooling the low temperature process stream; cooling the high temperature process stream by heating the heated working fluid to obtain a vaporized working fluid; expanding the vaporized working fluid to generate electricity to the output shaft and the pressure reducing fluid The reduced pressure working fluid is condensed to obtain a liquid Rankine cycle working fluid. Other details, embodiments, and details of the invention are obtained and derived from the following detailed description of the invention. [Embodiment] Second, it is more fully understood how the organic Rankine cycle device can be configured to utilize the waste heat of the α Guta, and the basic device configuration diagram is provided in the figure. The high temperature column (7) is used to separate the two or more components of the feed stream 11 from the steaming chamber, and the column is supplied with heat using a 155228.doc 201211375 reboiler 12. The overhead vapor in conduit 13 passes through section 1 B of Rankine cycle exchanger 100 where it is at least partially condensed to liquid and sent to receiver 15 via conduit 14. In parallel, the cryogenic column 2 is used to separate two or more components of the feed stream 21 by steaming, and the reboiler 22 is used to provide heat to the column. The overhead vapor in conduit 23 passes through section 100A of Rankine cycle exchanger 100 where it is at least partially condensed to liquid and sent via conduit 24 to receiver 25. The top of the cryogenic tower heats up to the Rankine fluid entering the exchanger via conduit 1〇1, and then the top of the high temperature tower heats up to the Rankine fluid, as the transfer at this stage more effectively increases the heated Rankine fluid 1〇2 temperature. The temperature difference between the two process streams (24 and 14) leaving the exchanger is preferably at least 1 〇 β (:, however, it is not intended to limit the invention thereby. The Langken cycle system embodied in block 50 is not limited to the condensed gas stream. (such as 13 and 23) Any process stream (such as a cooled mixed phase or liquid stream) that exchanges heat with a Rankine cycle working fluid in two or more sections of the exchanger 100 is within the scope of the invention. Condensation can be more efficient because the temperature range between the inlet and outlet of the process stream is small. Individual exchangers can be used for two or more services shown in the exchanger 1〇〇 instead of the section of the exchanger. which is
交換器100A及100B可為〇RC回路中呈串聯形式之 D 田單獨 的交換器。 郎肯循環系統之工作流體循環通過熱量回收 〜…、又換器 100，其溫度增加並轉化為蒸汽。工作流體蒸汽係經由導 管102送至膨脹器1〇3 ,膨脹過程使熱能轉化為機械軸功 率。此軸功率可藉由採用帶、輪、齒輪、傳送或類似裝置 之習知配置，根據所期速度及所需轉矩來進行任何機械工 155228.doc 201211375 作。重要地，可將該軸連接至諸如感應發電機之電功率產 生裝置。所產生之電流可就地使用或傳遞至柵極。離開膨 脹器之工作流體繼續送至冷凝器104，使用水（如所示）或空 氣作為冷卻介質之適當熱量排放使該流體冷凝為液體。亦 需冷凝器與泵間具有一液體緩衝罐105以確保一直並足夠 地供應液體給泵吸。該液體流至泵丨〇6，該泵使流體壓力 增至可將其回引入熱量回收熱交換器中之壓力，因此，完 成郎肯循環回路。 在郎肯循環膨脹器103為離線或處於瞬間狀態（諸如啟動 及關閉）時’熱量因工作流體持續循環而排放於冷凝器1 〇4 中之空氣或水。膨脹器中回收之能量則排放於工作流體冷 凝器104中。熱交換器設計可為熟習此項相關技術者明暸 之翼板/板、板/板、殼/管、翼板/管、微管道（包括雙壁）或 其他設計。 *涉及製程流間之溫差接近之根據本發明之能量回收係 藉由使用具有增強泡核沸騰面之交換器而加以改良。此增 強彿騰面可以（例如）US 3,384，154 ; US 3,821,018 ; US 4,064,914 ； US 4,060,125 ； US 3,906,604 ； US 4,216,826 ； US 3,454,〇81 ; US 4,769,51 1 及 US 5,091，075 中所述之多種 方式發揮作用；其等均係以引用的方式併入本文中。此等 增強管道特別適於與塔再沸器之熱交換及適於將熱量自塔 冷凝器排放至其他再沸器或蒸汽發生器。 一般，將該等增強泡核沸騰面併於殼·與-管型熱交換器 之官上。該等增強管係以熟習此項相關技術者習知之多種 155228.doc 201211375 不同方法製造。例如，該等管可包括沿由管機械加工製得 之管表面延伸之環狀或螺旋狀空腔。或者，表面上可提= 翼板。此外，該等管可經刻痕以提供肋條、凹槽、多孔層 及類似物。 一般，更有效之增強管為於管之沸騰面上具有—多孔層 之彼等者。該多孔層可以熟習此項相關技術者習知之眾多 不同方法提供。該等多孔表面中之最有效者具有藉由受限 空腔開口將蒸汽收集於層空腔内之所謂的凹形空腔。在一 此方法中，如US 4,064,914所述，多孔沸腾層係結合至導 熱壁之一側。多孔表面層之本質特徵為具毛細管尺寸之互 連孔，其中一些係與外表面連通。待沸騰之液體係經由外 孔及表面下互連1進入表面下空腔’ i經空腔之金屬所形 成之壁受熱。該液體之至少一部分係在空腔内汽化且所得 氣泡靠著空腔壁生長。其一部分最終經由外孔自空腔出來 及然後上升經過多孔層上方之液膜而脫離進入液膜上方之 氣體空間中ϋ體自互連孔流人空腔中且連續地重複 此機制。包含多孔沸騰層之此等增強管係以*u〇p，Du Plaines，Illinois製造之商品名 High Flux Tubing購得。爲通 過交換器100之溫度差最小且因此改良郎肯循環的效率， 以於本發明中用以汽化交換器丨00中之工作流體之增強泡 核滞騰表面為較佳。 增強冷凝面亦用於具有小溫差之實際熱交換器設計。於 本發明中針對於1〇〇中之塔頂冷凝器或1〇5中之工作流體冷 凝器’以增強冷凝面為較佳。 155228.doc 201211375 裝置包括一種用於監測兩或更多種製程流及工作流體之 流速、溫度及壓力及用於提供控制信號給泵及膨脹器之控 制器。熟習者悉知之電子控制器係連接至能量轉化系統之 多個組件以一般根據控制器内之記憶或電子裝置之設定點 或操作點來監測及/或控制組件操作。電子控制器特定言 之係連接至膨脹器、冷凝器、泵及冷凝器中之一或兩者周 圍之工作流旁道。當然，電子控制器可使用多個控制器實 施，關鍵在於即使在變化的輸入流體溫度或其他操作參數 變化期間保持相對穩定的操作。 有機化合物通常具有超出則發生熱分解之溫度上限。熱 分解之起始係關於化學品之特定結構及因此隨不同化合物 變化。爲了利用與工作流體之直接熱交換而接近高溫源， 可利用上述之熱通量及質量流量之設計考慮以利於熱交 換，同時使工作流體低於其熱分解起始溫度。此種情況之 直接換熱-般需求導致成本提高之其他卫程及機械特徵 件。在此等情況下，二次回路設計可藉由控制溫度同時規 避針對直接換熱實例列舉之問題而利於接近高溫熱源。此 方法亦可在無須影響或改變工藝排熱封裝下提供對郎肯循 環系統中未來經改良之工作流體更大之改進自由度。通常 進行成本風險/效益分析以確定用於特定應用之最好方法 (直接或間接熱交換）。 流體選擇取決於多種因素，包括溫度匹配性、熱動力性 質、傳熱性質、成本、安全問題、環境可接受性及可用 性。合適之工作流體包括水、聚石夕氧、脂族煙、環煙、芳 155228.doc 201211375 族烴、烯烴、含氟烴（包括烷烴及烯烴、環狀化合物）、氣 氟醚、全氟醚、醇、酮、氟化酮、氟化醇、酯、磷酸酯。 合適之其他流體描述於以引用的方式併入本文中之仍 7,428,816 B2* »除了用於本發明製程之上述流體之外， 已確定用於本發明製程之多種較佳流體。用於本發明製程 之流體包含如下結構之較佳化合物。 X z y m 其中X、y、Z及m各選自由以下組成之群：氟、氫、及 R，其中R及1各為具有1至6個碳原子之烷基、芳基或烷芳 基，且其中Rf係經部分或完全氟化。再者，其中之較佳者 為藉由使前述化合物與HF反應及經氫氣還原得到之彼等化 合物得到的飽和化合物。 最佳為式CxFyHz化合物，其中x=j2-b，其中b為〇至6 , y-2x-z，且對於x/2及2x/3 =整數則z=2x/3 ;對於\/2及3"4= 整數則Ζ=3χ/4 ;對於χ/2不等於整數則ζ=χ_2 ;對於χ/2及 x/5 =整數則ζ=χ-3。再者，最佳者為藉由使HF與前述化合 物反應及經氫氣還原得到之彼等化合物得到的飽和化合 物。Genetron 245fa(HFC-245fa)為特有利的工作流體。 實例： 以下實例說明芳族錯合物使用0RC生產9〇〇 〇〇〇噸/年之 對二曱苯之本發明之益處。該芳族錯合物之態樣描述於以 155228.doc •10· 201211375 引用的方式併入本文中之US 6,740,788中。本申請案圖中 所述之欄10及20分別為在吸附分離單元中自解吸附劑分離 出C8-芳族萃餘物及自解吸附劑分離出富含對二曱苯之萃 取物之蒸餾塔。相對地，萃餘物塔為高溫塔及萃取物塔為 低溫塔。爲比較ORC與空氣冷卻及水冷卻，熱負荷如下： 排放之熱量 (MW) T-入口 (0C) τ-出口 (oc) 萃取物塔塔頂 34.0 151.1 128.9 萃餘物塔塔頂 90.6 152.6 140.8 總計 124.6 - 相對於空氣及水冷凝器實例，使用ORC之淨功率效益係 採用以下等式計算： 水冷卻： 淨功率效益（MW)=渦輪生成功率（MW)-泵功率（MW)-冷 卻水泵功率（MW)-冷卻塔風機功率（MW)+基礎實例空氣冷 卻器風機功率（MW) 空氣冷卻： 淨功率效益（MW)=渦輪生成功率（MW)-泵功率（MW)-空 氣冷卻器風機功率（MW)+基礎實例空氣冷卻器風機功率 (MW) 水冷凝器 空氣冷凝器 淨功率效益（MW) 13.2 12.4 155228.doc -11 - 201211375The exchangers 100A and 100B may be separate converters of the D field in series in the 〇RC loop. The working fluid of the Rankine cycle system is circulated through heat recovery ~..., and the converter 100 is heated and converted to steam. The working fluid vapor is sent via conduit 102 to expander 1〇3, which expands the thermal energy into mechanical shaft power. This shaft power can be performed by any conventional mechanism using belts, wheels, gears, transmissions or the like, depending on the speed and torque required. 155228.doc 201211375. Importantly, the shaft can be connected to an electric power generating device such as an induction generator. The generated current can be used locally or transferred to the grid. The working fluid exiting the expander is then sent to the condenser 104 where it is condensed into a liquid using appropriate heat discharge of water (as shown) or air as a cooling medium. It is also desirable to have a liquid buffer tank 105 between the condenser and the pump to ensure that liquid is supplied and pumped continuously and adequately. The liquid flows to pump 丨〇6, which increases the fluid pressure to the pressure that can be introduced back into the heat recovery heat exchanger, thus completing the Rankine loop. When the Rankine cycle expander 103 is off-line or in an instantaneous state (such as starting and closing), the heat or the air discharged into the condenser 1 〇 4 due to the continuous circulation of the working fluid. The energy recovered in the expander is then discharged into the working fluid condenser 104. The heat exchanger design can be known to those skilled in the art for flaps/boards, plates/boards, shells/tubes, wings/tubes, micro-pipes (including double walls) or other designs. * The energy recovery according to the present invention, which relates to the temperature difference between process streams, is improved by using an exchanger having an enhanced nucleate boiling surface. Such augmentation can be as described in, for example, US 3,384,154; US 3,821,018; US 4,064,914; US 4,060,125; US 3,906,604; US 4,216,826; US 3,454, 〇81; US 4,769,51 1 and US 5,091,075 Modes play a role; they are all incorporated herein by reference. These enhanced conduits are particularly suitable for heat exchange with a column reboiler and for discharging heat from the tower condenser to other reboilers or steam generators. Typically, the nucleate boiling surfaces are enhanced and applied to the shell and tube heat exchanger. These enhanced tubing are manufactured in a variety of ways 155228.doc 201211375, which is well known to those skilled in the art. For example, the tubes can include an annular or helical cavity extending along the surface of the tube machined by the tube. Alternatively, the surface can be raised = wing. In addition, the tubes can be scored to provide ribs, grooves, porous layers and the like. In general, more effective reinforced tubes are those having a porous layer on the boiling surface of the tube. The porous layer can be provided by a number of different methods known to those skilled in the art. The most effective of these porous surfaces has a so-called concave cavity that collects vapor within the layer cavity by a restricted cavity opening. In one such method, as described in U.S. Patent 4,064,914, the porous boiling layer is bonded to one side of the heat conducting wall. The essential feature of the porous surface layer is interconnected pores having capillary dimensions, some of which are in communication with the outer surface. The liquid system to be boiled enters the subsurface cavity via the outer and subsurface interconnects 1 i is heated by the wall formed by the metal of the cavity. At least a portion of the liquid vaporizes within the cavity and the resulting bubbles grow against the walls of the cavity. A portion thereof eventually exits the cavity through the outer hole and then rises through the liquid film above the porous layer to detach from the gas space above the liquid film into the body cavity from the interconnected pores and continuously repeats this mechanism. Such reinforced tubing comprising a porous boiling layer is commercially available under the trade name High Flux Tubing manufactured by Du Plaines, Illinois. In order to minimize the temperature difference through the exchanger 100 and thus improve the efficiency of the Rankine cycle, it is preferred in the present invention to enhance the nucleate stagnation surface of the working fluid in the exchanger 00. The enhanced condensation surface is also used in actual heat exchanger designs with small temperature differences. In the present invention, it is preferred to use a top condenser in the top or a working fluid condenser in the first to enhance the condensation surface. 155228.doc 201211375 The device includes a controller for monitoring the flow rate, temperature and pressure of two or more process streams and working fluids and for providing control signals to the pump and expander. The electronic controller known to those skilled in the art is coupled to a plurality of components of the energy conversion system to generally monitor and/or control component operation based on memory or electronic device setpoints or operating points within the controller. The electronic controller is specifically connected to the working flow bypass around one or both of the expander, condenser, pump, and condenser. Of course, the electronic controller can be implemented using multiple controllers, the key being to maintain a relatively stable operation even during varying input fluid temperatures or other operating parameter changes. Organic compounds usually have an upper temperature limit above which thermal decomposition occurs. The origin of thermal decomposition is related to the specific structure of the chemical and thus to the different compounds. In order to utilize a direct heat exchange with a working fluid to access a high temperature source, the above design considerations of heat flux and mass flow may be utilized to facilitate heat exchange while at the same time lowering the working fluid below its thermal decomposition onset temperature. The direct heat transfer in this case - the general demand and other mechanical and mechanical features that lead to increased costs. In such cases, the secondary loop design facilitates access to the high temperature heat source by controlling the temperature while avoiding the problems listed for the direct heat exchange example. This method also provides greater freedom of improvement for future improved working fluids in the Rankine cycle system without affecting or changing the process heat rejection package. A cost risk/benefit analysis is usually performed to determine the best method (direct or indirect heat exchange) for a particular application. Fluid selection depends on a variety of factors including temperature matching, thermodynamic properties, heat transfer properties, cost, safety issues, environmental acceptability, and availability. Suitable working fluids include water, polyox, oxygen, smog, aromatic 155228.doc 201211375 hydrocarbons, olefins, fluorinated hydrocarbons (including alkanes and alkenes, cyclic compounds), fluoroethers, perfluoroethers , alcohol, ketone, fluorinated ketone, fluorinated alcohol, ester, phosphate ester. Other suitable fluids are described herein by reference in their entirety. 7,428,816 B2* » In addition to the fluids described above for use in the process of the present invention, a number of preferred fluids for use in the process of the present invention have been identified. The fluids used in the process of the present invention comprise preferred compounds of the structure described below. X zym wherein each of X, y, Z and m is selected from the group consisting of fluorine, hydrogen, and R, wherein R and 1 are each an alkyl group, an aryl group or an alkylaryl group having 1 to 6 carbon atoms, and Wherein Rf is partially or fully fluorinated. Further, preferred among them are saturated compounds obtained by reacting the above compounds with HF and hydrogen compounds obtained by hydrogen reduction. Most preferred is a compound of the formula CxFyHz, where x = j2-b, where b is 〇 to 6, y-2x-z, and for x/2 and 2x/3 = integers z = 2x/3; for \/2 and 3"4= Integer Ζ=3χ/4; χ/2 is not equal to integer ζ=χ_2; for χ/2 and x/5 = integer ζ=χ-3. Further, the most preferred one is a saturated compound obtained by reacting HF with the above compound and hydrogen sulfide. Genetron 245fa (HFC-245fa) is a particularly advantageous working fluid. EXAMPLES The following examples illustrate the benefits of the present invention in which an aromatic complex is produced using 0RC to produce 9 〇〇〇 ton/year of p-terphenyl. The aspect of the aromatic complex is described in US 6,740,788, which is incorporated herein by reference in its entirety. Columns 10 and 20 described in the drawings of the present application respectively separate the C8-aromatic raffinate from the desorbent in the adsorption separation unit and separate the diphenylbenzene-rich extract from the desorbent. tower. In contrast, the raffinate column is a high temperature column and the extract column is a cryogenic column. To compare ORC with air cooling and water cooling, the thermal load is as follows: Emission of heat (MW) T-inlet (0C) τ-outlet (oc) Extract tower top 34.0 151.1 128.9 Residue tower top 90.6 152.6 140.8 Total 124.6 - Relative to air and water condenser examples, the net power efficiency using ORC is calculated using the following equation: Water Cooling: Net Power Benefit (MW) = Turbine Power (MW) - Pump Power (MW) - Cooling Pump Power (MW) - Cooling Tower Fan Power (MW) + Basic Example Air Cooler Fan Power (MW) Air Cooling: Net Power Benefit (MW) = Turbine Power (MW) - Pump Power (MW) - Air Cooler Fan Power (MW)+Basic Example Air Cooler Fan Power (MW) Water Condenser Air Condenser Net Power Benefit (MW) 13.2 12.4 155228.doc -11 - 201211375
實例 年效益($MM/年） 水冷凝器 空氣冷凝器 功率=$0.07/kWh 無C02權 $7.4 MM $6.9 MM 功率=$0.10/kWh 無C02權 $10.6 MM $9.9 MM 功率=$0.07/kWh 30$/MT C02 權 $9.1 MM $8.4 MM 功率=$0.10/kWh $30/MT C02 權 $12.3 MM $11.3 MMExample Year Benefit ($MM/year) Water Condenser Air Condenser Power = $0.07/kWh No C02 Right $7.4 MM $6.9 MM Power = $0.10/kWh No C02 Right $10.6 MM $9.9 MM Power = $0.07/kWh 30$/MT C02 Right $9.1 MM $8.4 MM Power=$0.10/kWh $30/MT C02 Right $12.3 MM $11.3 MM
功率生成計算值 渦輪/發電機效率 0.80/0.95 冷卻塔風機 7 kW/1000 gpm 冷卻水泵ΔΡ 50 psi 功率燃料當量 9,090 Btu/kWh co2排放量 56.2 kg/GJ 【圖式簡單說明】 圖為顯示使用ORC自兩蒸餾塔回收熱量之簡化工藝流程 圖。 【主要元件符號說明】 10 南溫塔 11 饋送流 12 再沸器 13 導管 14 導管 155228.doc 201211375 15 接收器 20 低溫塔 21 饋送流 22 再沸器 23 導管 24 導管 25 接受器 50 框 100 交換器 100A 100之區段 100B 100之區段 101 導管 102 導管 103 膨脹器 104 工作流體冷凝器 105 液體緩衝罐 106 泵 155228.doc 13-Power generation calculated value Turbine/generator efficiency 0.80/0.95 Cooling tower fan 7 kW/1000 gpm Cooling water pump ΔΡ 50 psi Power fuel equivalent 9,090 Btu/kWh co2 emissions 56.2 kg/GJ [Simple diagram] The picture shows the use of ORC A simplified process flow diagram for recovering heat from two distillation columns. [Main component symbol description] 10 South Wenta 11 Feed stream 12 Reboiler 13 Catheter 14 Catheter 155228.doc 201211375 15 Receiver 20 Cryogenic tower 21 Feed stream 22 Reboiler 23 Catheter 24 Catheter 25 Receiver 50 Box 100 Exchanger Section 100 of 100A 100 Section 100B 100 Catheter 102 Catheter 103 Expander 104 Working Fluid Condenser 105 Liquid Buffer Tank 106 Pump 155228.doc 13-