TW559567B

TW559567B - Method and system for desalination sea water by membrane distillation

Info

Publication number: TW559567B
Application number: TW091125147A
Authority: TW
Inventors: Shing-Jung Guo; Jen-Jang Jang
Original assignee: Shing-Jung Guo; Jen-Jang Jang
Priority date: 2002-10-25
Filing date: 2002-10-25
Publication date: 2003-11-01

Abstract

The present invention provides a method and a system for desalination sea water by a membrane distillation where sea water receives a pre-treatment including filtration, forming fine bubbles, pressurization and skimming to remove suspended solid impurities of alge, etc. Then the skimmed feed water receives another treatment of forming fine bubbles so that the sea water and bubbles form a uniform emulsion working fluid in which the bubbles are full of saturated steam. The working fluid is then transported to a desalination device, which contains one or more porous hydrophobic membrane, such that the work fluid permeates easily through the porous hydrophobic membrane to form clean water from condensation of the penetrated steam molecules.

Description

559567 C7 D7 11 五、發明說明（【發明領域】本發明係有關於一種膜蒸餾法與所應用的設備，更詳而言之，特別是指一種可提高海水淡化產水效能，且能提昇膜蒸餾海水淡化分離效率、大幅降低成本的膜蒸餾海水淡化法及其系統。【習知技藝說明】目前全世界應用於海水淡化商業用途之除鹽造水技術，主要可分為蒸餾法（Distillation )及薄膜分離法（ Membrane Desalination)兩大類。蒸餾法又包括：多級閃沸式（Multi-Stage Flash或MSF )、多效蒸顧式（ Multi-Effect Distillation 或 MED )與蒸汽壓縮式（ Vapor Compression或VC)等三種。薄膜分離法主要有逆滲透式（Reverse Osmosis或R〇 ) 與電透析式（ Electro Dialysis 或 ED)兩種方法。海水淡化採用的除鹽造水技術早期以多級閃沸法最並遍’主要應用在中東地區大型的海水淡化廠，並常與火^ 發電廠互相配合運轉’利用火力發電廠汽輪機所使用過的低壓廢蒸汽，作為淡化過程中加熱海水的熱源，其造水量佔全世界淡化總量的48·1 % ( 978萬CMD，1996)。 MSF自195G年即有商業化規模，φ於產能大且應泛，故操作維修技術純熟，其單位模組爭: 取穴造水篁可逵 57,600 CMD。多級閃沸式之原料水若椟 e 右輙一過式（Onc 熱能損失與滷水 through )運轉，將造成加藥成本增加、改採滷水再循所含化學藥品對環境之衝擊等問題。目前多本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐） 559567 C7 ____ D7 五、發明說明（2 ) 環方式運轉。逆滲透法（RO ,其流程如圖一所示）雖開發較晚，但正被世界各國廣泛使用中，主要原因是在薄膜材質及能源回收改良技術已達成熟階段，不但使淡化成本降低且造水率提高’除鹽率高達99.5 〇/〇，而膜管平均使用壽命已延長至5年左右’更可應用在處理工業廢水及冷卻水塔排放水回收再利用等方面，其造水量約佔全世界淡化總量之3 5.9 % ( 729萬CMD，1996 )。逆滲透法雖在1970年代後期開發，但由於興建時程短、佔地面積小與模組化組裝簡易等特性，使得RO成為競爭力最強且快速成長之除鹽造水技術。不過，RO技術發展仍有前處理、操作條件改善（溫度、 pH、耗電）及延長薄膜使用年限之用膜技術等課題仍待持續研究。除了上述方法之外，還有利用膜蒸餾法、太陽能發電、深海水壓差、與液化天然氣（LNG )冷能利用等的海水淡化技術。膜蒸餾法（MD : Membrane Distillation)兼具「傳統蒸餾」與「薄膜分離」之優點，產水水質導電度值小於 10 pS/cm，如第二、三圖所示，是利用只能允許水蒸氣分子通過之多孔疏水性薄膜A ( Hydrophobic Porous Membrane )，將兩種工作水體分隔開來，此種疏水性細小孔洞可以藉由表面張力之限制，防止液相水體通過。若控制此兩種工作水體之溫度不相同，結果將導致兩邊之蒸氣壓不同，致使水蒸氣分子由高溫處（高蒸氣壓）水體經 _本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐） " 第4頁 559567559567 C7 D7 11 V. INTRODUCTION TO THE INVENTION [Field of the Invention] The present invention relates to a membrane distillation method and applied equipment. More specifically, it particularly refers to a method that can improve seawater desalination water production efficiency, and can improve the membrane. Membrane distillation seawater desalination method and system for greatly reducing the cost of distilling seawater desalination. [Description of Known Skills] At present, the desalination and water-making technologies used in commercial desalination in the world can be mainly divided into distillation methods (Distillation). And Membrane Desalination. Distillation methods include: Multi-Stage Flash or MSF, Multi-Effect Distillation or MED, and Vapor Compression. Or VC), etc. There are two main methods of membrane separation: reverse osmosis (Reverse Osmosis or Ro) and electrodialysis (ED). The desalination technology used in seawater desalination uses multiple stages of flash boiling in the early stage. The most common method is 'mainly used in large-scale desalination plants in the Middle East, and often operates in conjunction with thermal power plants' using thermal power plants The low-pressure waste steam used by the turbine, as a heat source for heating seawater during the desalination process, accounts for 48.1% of the world's total desalination (9.87 million CMD, 1996). MSF has been commercialized since 195G. φ is large in production capacity and should be general, so the operation and maintenance technology is proficient, and its unit module contention: the hole making water can be 60057,600 CMD. The multi-stage flash boiling raw water is 椟 e, the right is a one-pass type (Onc thermal energy loss And brine through) will cause problems such as increasing the cost of dosing, changing the use of brine and the impact of chemicals on the environment, etc. At present, many paper standards are applicable to the Chinese National Standard (CNS) A4 specification (210x 297 mm) 559567 C7 ____ D7 V. Description of the invention (2) Ring mode operation. Although the reverse osmosis method (RO, whose process is shown in Figure 1) was developed relatively late, it is being widely used in countries all over the world, mainly due to thin film materials and energy. The recovery and improvement technology has reached the mature stage, which not only reduces the desalination cost and increases the water production rate. 'The salt removal rate is as high as 99.5 〇 / 〇, and the average service life of the membrane tube has been extended to about 5 years.' It can be applied to the treatment of industrial wastewater. In terms of recycling and reuse of the cooling water tower's discharged water, its water production accounts for about 3 5.9% of the world's total desalination (7.29 million CMD, 1996). Although the reverse osmosis method was developed in the late 1970s, due to the short construction time, The small area and easy assembly of the module make RO the most competitive and fast-growing desalination technology. However, the development of RO technology still has pretreatment, improved operating conditions (temperature, pH, power consumption), and Issues such as membrane technology for extending the useful life of thin films remain to be studied. In addition to the above methods, there are seawater desalination technologies using membrane distillation, solar power generation, deep sea water pressure differential, and liquefied natural gas (LNG) cold energy utilization. Membrane Distillation (MD: Membrane Distillation) combines the advantages of "conventional distillation" and "thin film separation". The conductivity value of the produced water is less than 10 pS / cm. The porous hydrophobic membrane A (Hydrophobic Porous Membrane) through which the vapor molecules pass, separates the two types of working water bodies. Such hydrophobic small holes can be prevented by the surface tension to prevent the liquid water body from passing through. If the temperature of the two working water bodies is controlled to be different, the result will be different vapor pressures on both sides, which will cause water vapor molecules to pass through the water body at high temperature (high vapor pressure). _ This paper size applies Chinese National Standard (CNS) A4 specifications (210x 297 mm) " Page 4 559567

Cl _______D7__ 五、發明說明（3 ) 如果在以純化膜應用，可見邱政勳係可用由薄膜孔道滲透至另一低溫處（低蒸氣壓）水體< 低溫處予以冷卻，即可達到將高溫處水體之水份i 分離至低溫處，因此即可用來淡化海水，此亦為堯所習知之技術。在台灣，揭露此種MD之前案技射丨於公告第34 1 523、506944號等專利案（馬哲儒’ 教授等人所提申）。此一因為溫度之差異所導致蒸氣壓差之關Cl _______D7__ V. Description of the invention (3) If it is applied in a purified membrane, it can be seen that Qiu Zhengxun can penetrate from the membrane channel to another low temperature (low vapor pressure) water body < cooling at low temperature can reach the water body at high temperature The water i is separated to a low temperature, so it can be used to desalinate seawater, which is also a technique known to Yao. In Taiwan, the technical shooting of such a pre-MD case was disclosed in Patent Cases No. 34 1 523, 506944 (filed by Professor Ma Zheru 'and others). The relationship between the vapor pressure difference due to the temperature difference

Clausius _ Clapeyron關係式來描述：Clausius _ Clapeyron relation to describe:

InP = + C 而質量傳送之流通量則為下式：山=B · Δ Pi 觸角度由界面化學觀點來看，此一薄膜表面水體之名必須大於9 0。，亦即為疏水性薄膜才有效。 2 r. △ P = -"T"1 c〇s0 (LaPlace方程式） 0 > 90° cos θ < 0 Δ Ρ> 〇雖然，膜蒸餾法有下列優點： 1 ·使用土地小。 2 ·設備費用低。 3 ·操作溫度與壓力低、能源耗用少。 4 ·薄膜所需之機械強度低。本紙張尺度適用中國國家標準（CNS) Α4規格（210χ 297公$--- 第5頁 559567InP = + C and the flux of mass transfer is as follows: Mountain = B · Δ Pi Contact angle From the viewpoint of interface chemistry, the name of the water body on the surface of this film must be greater than 90. That is, it is effective for hydrophobic films. 2 r. △ P =-" T " 1 c0s0 (LaPlace equation) 0 > 90 ° cos θ < 0 ΔP > 〇 However, the membrane distillation method has the following advantages: 1 The use of land is small. 2 · Low equipment cost. 3 · Low operating temperature and pressure, low energy consumption. 4 · The mechanical strength required for the film is low. This paper size applies to China National Standard (CNS) A4 specifications (210 x 297) $ --- page 5 559567

Cl _____D7 五、發明說明（4 ) 5 ·產水純度高。不過，習知之膜蒸餾法有下列缺點： 1 ·需要良好刖處理设備，避免膜表面發生污染 (fouling )。 2 ·在質量傳送過程中’薄膜表面可能發生溫度極象（Temperature Polarization)。亦即當溶液蒸發在薄膜接觸的液體表面產生溫度梯度，造成薄膜兩側效溫度差小於設定溶液之溫度差，使薄膜之有效驅動低，滲透量減少。 3.在質量傳送過程中’薄膜表面還可能發生濃度現象（Concentration Polarization )。當進行薄膜過程中，高溫飼水溶液蒸發成蒸氣，透過薄膜凝結成此時飼水與薄膜界面處因水份散失而使濃度增加，造蒸氣不易蒸發，滲透量隨之減少。 4 ·依水蒸氣之飽和蒸氣壓數據來看，在正常操作下，溫度自25°C提昇至30°C，飽和蒸氣壓自0.461 增加為0 · 6 1 6 p s ί，升溫至3 0 °C，增加5 °C，其產水限，亦即平均每度攝氏升溫，飽和蒸氣壓才增加〇 psi，實在太少了。 5·因為是利用有限溫差來進行液氣平衡之滲透質送，因此質傳速度相對比較緩慢，所以必須保持膜兩體有較大的溫差才能彌補此一問題，可是受限於薄膜操作溫度無法太高與能源耗用效率較差之問題，致使與一般商品化技術競爭。本紙張尺度適用中國國家標準（CNS) A4規格（210χ 297公釐）第6頁堵塞化現時會的有力降極化蒸餾水，成水狀態 psi 量有 • 031 量傳測流材質無法 559567 C7Cl _____D7 V. Description of the invention (4) 5 · High purity of produced water. However, the conventional membrane distillation method has the following disadvantages: 1) Good 刖 treatment equipment is required to avoid fouling of the membrane surface. 2 • Temperature polarization may occur on the surface of the 'film during mass transfer (Temperature Polarization). That is, when the solution evaporates, a temperature gradient is generated on the surface of the liquid in contact with the film, which causes the effective temperature difference between the two sides of the film to be less than the temperature difference of the set solution, which makes the effective driving of the film low and the amount of penetration reduced. 3. During the mass transfer process, a concentration phenomenon may also occur on the surface of the film. During the film process, the high-temperature feed solution evaporates into vapor, and condenses through the film. At this time, the water at the interface between the feed water and the film increases the concentration due to the loss of water, which makes it difficult for the vapor to evaporate and the permeation amount to decrease. 4 · According to the saturated vapor pressure data of water vapor, under normal operation, the temperature is increased from 25 ° C to 30 ° C, the saturated vapor pressure is increased from 0.461 to 0 · 6 1 6 ps ί, and the temperature is increased to 30 ° C When the temperature is increased by 5 ° C, the water production limit, that is, the average temperature rises per degree Celsius, the saturated vapor pressure increases by 0 psi, which is too small. 5. Because the limited temperature difference is used for osmotic mass transfer of liquid-gas balance, the mass transfer speed is relatively slow. Therefore, a large temperature difference between the two membrane bodies must be maintained to compensate for this problem. However, it is impossible to limit the operating temperature of the film. Too high and inefficient energy consumption have led to competition with general commercial technologies. This paper size applies the Chinese National Standard (CNS) A4 specification (210x297 mm). Page 6 Clogging will forcefully reduce the polarization. Distilled water, the state of formation of water. Psi Quantity • 031 Volumetric Flow Measurement Material Not Available 559567 C7

6·液體蒸氣化過，實際產水量不大。 7 ·右要大量生產濟效益。程（相變化）僅發生於少量孔隙内部 ’必需提供大量能源與膜管，不符經但是因為產出之本發明即是針對际上，雖然習知膜蒸鶴法理論可行蒸氣量太少’戶斤以—直未能順利商品化上述缺失提出改善方法。【發明概要】 ’即在提供一種可提昇海水淡膜蒸餾海水淡化法。在於提供一種膜蒸餾海水淡化因此，本發明之一目的化效率並能降低造水成本之本發明之另一目的，即糸統。於疋’本發明之膜蒸餾海水淡化法及其系、统，包含有下列步驟·一、供給海水：取一容器盛裝預定容量之-海 Κ並將海水經過過濾前處理以去除部份雜質；二、加壓孚除刖處s •將過濾後海水進行微細氣泡化加壓浮除前處 [以去除藻類等懸浮固體雜質；三、微細氣泡化注氣處理·將浮除後之飼水經過微細氣泡化氣水混合再次處理，使海水與氣體混合成均勻白霧乳化狀態之工作液體，其氣泡内為飽和水蒸氣；四、淡化處理：再將均勻氣水混合狀態之工作液體輸送至一淡化裝置，該淡化裝置内部具有一個或一個以上的疏水性多孔薄膜，使含有大量飽和水蒸氣的高含氣量工作液體，可輕易透過多孔疏水性薄膜；五、冷凝構件：對透過薄膜之水蒸氣分子予以凝結生成淡水。用中國國家標準（CNS) A4規格（210χ 297公爱）一' " 頁第 559567 C7 ^_ _D7 五、發明說明（6 ) 【圖示之簡單說明】本發明之其他特徵及優點，在以下配合參考圖示之較佳實施例的詳細說明中，將可清處的明白，在圖示中：第一圖是一方塊流程圖’說明現有RO薄膜海水淡化法的處理流程；第二圖是一方塊流程圖，說明習知膜蒸餾法（MD ) 的處理流程；第三圖是一局部結構放大示意圖，說明習知海水淡化裝置利用加熱的海水滲透生成淡水的情形；第四圖是一方塊流程圖，說明本發明膜蒸餾海水淡化法一較佳實施例的處理流程；第五圖是一系統構造圖，說明本發明的膜蒸餾海水淡化系統各組成裝置以及管路的佈線情形；第六圖是一對應示意圖，說明本發明在吹氣加熱後可大幅提昇水蒸氣量的情形；以及第七圖是一比對示意圖，說明本發明經過奈米級微細氣泡化而呈飽合狀態的工作液體，可大量釋放水蒸氣透入多孔性有機膜生成淡水的狀態，以及與習知膜蒸餾法的生成淡水量的差異情形。【較佳實施例之詳細說明】參閱第四、五圖，本發明一種膜蒸餾海水淡化法及其系統，包含有下列步驟：一、供給海水•·取一容器20盛裝預定容量之海水本紙張尺度適用中國國家標準（CNS) A4規格（210χ 297公釐）第8頁 5595676. The liquid has been vaporized, and the actual water production is not large. 7 · Right to mass production economic benefits. The process (phase change) only occurs in a small amount of pores. 'A lot of energy and membrane tubes must be provided, which is inconsistent, but because the invention of the output is aimed at the world. The above-mentioned shortcomings have not been successfully commercialized, and improvement methods have been proposed. [Summary of the Invention] 'It is to provide a seawater desalination method which can enhance seawater desalination membrane distillation. It is to provide a membrane distillation seawater desalination. Therefore, one object of the present invention is to improve the efficiency and reduce the cost of water production. Another object of the present invention is the system. The membrane distillation seawater desalination method of the present invention and its system and system include the following steps: 1. Supplying seawater: take a container containing a predetermined volume of seawater and subject the seawater to pre-filtration to remove some impurities; Second, the pressurized fouling removal s • The filtered seawater is micro-bubbled before being pressurized to float [to remove suspended solid impurities such as algae; III. Micro-bubble gas injection treatment. Pass the floated feed water through The micro-bubble gas-water mixture is processed again to make the seawater and gas mixed into a uniform white mist emulsified working liquid, and the bubbles are saturated with water vapor; 4. Desalination treatment: The working liquid in a uniform gas-water mixed state is sent to a Desalination device, the desalination device has one or more hydrophobic porous film inside, so that the high-gas content working liquid containing a large amount of saturated water vapor can easily pass through the porous hydrophobic film; 5. Condensing component: the water vapor passing through the film The molecules are coagulated to produce fresh water. Use Chinese National Standard (CNS) A4 specification (210χ 297 public love)-"Page 559567 C7 ^ _ _D7 V. Description of the invention (6) [Simplified description of the diagram] Other features and advantages of the present invention are as follows In the detailed description of the preferred embodiment with reference to the figure, it can be clearly understood that in the figure: The first figure is a block flow chart illustrating the processing flow of the existing RO thin film desalination method; the second figure is A block flow diagram illustrating the processing flow of the conventional membrane distillation method (MD); the third figure is an enlarged schematic diagram of a partial structure illustrating a situation in which a conventional seawater desalination device uses heated seawater to generate fresh water; the fourth figure is a block The flow chart illustrates the processing flow of a preferred embodiment of the membrane distillation seawater desalination method of the present invention. The fifth diagram is a system configuration diagram illustrating the components of the membrane distillation seawater desalination system of the present invention and the wiring of the pipeline; the sixth The figure is a corresponding schematic diagram illustrating the situation that the present invention can greatly increase the amount of water vapor after blowing and heating; and the seventh diagram is a comparison schematic diagram illustrating that the invention passes through nanometers. Fine bubbles to saturation state of the working fluid, can be massive release of water vapor penetration into the porous film-forming organic fresh state, and the difference in the amount of fresh water into the case with conventional raw film distillation process. [Detailed description of the preferred embodiment] Referring to the fourth and fifth figures, a membrane distillation seawater desalination method and system thereof according to the present invention include the following steps: 1. Supplying seawater • Take a container 20 containing a predetermined volume of seawater paper Standards apply to Chinese National Standard (CNS) A4 specifications (210 x 297 mm) Page 8 559567

Cl D7 五、發明說明（7 ) 二、加壓浮除、氣水混合：在一管路上設置一抽水馬達30，對該容器20進行海水抽取動作，該管路另一旁支設有一氣體供應器40，該氣體供應器40可對管路送入_ 預定氣體4，在本實施例中，該氣體4是採用一般的空氣，在混合之前，該氣體4預先作加壓加熱，再與海水1混合成帶有氣體的工作液體5，加溫之目的主要是讓混合後的工作液體5帶有一定高溫，可加速工作液體5水蒸氣的產生，而且對氣體加溫所需的能量遠小於對液體加溫，具有節省成本的功效；另外，氣體4與海水1混合成工作液體5以後，高壓的工作液體5再輸送至一減壓筒5〇内作儲置減壓，減壓筒50 —側設有一洩壓閥5 1，該洩壓閥 5 1再連接至氣體供應器40，使工作液體5得以在管路内作循環。三、微細氣泡化處理：將工作液體5由減壓筒50再輸送至一奈米級微細氣泡化裝置60，其主要作用是對工作液體5進行碎解乳化，使工作液體5内的水分子可因為大量曝氣而變得微細化，相對的所產生的蒸氣量增加，如第六圖所示，此種原理就如將壺中的水進行吹氣加熱後，其產生出的蒸氣量，會遠多於單純將壺中水正常加熱的狀態 :至於微細化水分子的手段可運用多種不同技術完成，在本實施例中’該奈米級微細氣泡化裝置6 〇乃採用*一種泡洙產生機（圖未示），將開關打開後’工作液體5即可被打成具有大量超微細泡沫的液體’此種泡沫產生機的構造原理皆已為習知（如台灣第215 5 8 5號、美國第本紙張尺度適財_家標準（CNS) A4規格（雇^^麓）第9頁 559567 C7 D7 五、發明說明（8 ) 6,293,529 !虎等專利），故在此即不再多加贊述。四、淡化處理··再將工作液體5輸送至一淡化裝置 70内’同時參閱第七圖，該淡化裝置7()内部設置有複數個疏水性的多孔性有機膜71，且在一側接設有一排水管路 73及/火水&路74，該等多孔性有機膜7 i可採用串聯或是並聯方式設置，由於本發明工作液體5在經過超微细化處理後，濃度已達飽合狀態，0此，可大量地生成水基氣2透入多孔性有機膜7 1。 … 五、冷凝構件：將透過多孔性有機Μ 71❿到達其另側的冷凝構件72施以冷凝，在本實施例中，該淡化裝置7〇乃通入空氣以對冷凝構件72進行冷卻，如此一來，水瘵氣2即可被凝結而生成淡水3 ,處理過後的工作液體 5可輸送至排水管路73 ,該排水管路73可再與另一淡化裝置（圖未不）作成銜接，如此工作液體5可重覆循環使用，而淡水3可輸送至淡水管路74，此外，在淡水管路 74上接设有一負壓元件80，該負壓元件80通常採用真空幫浦’如此即可抽取淡水3到達另一容器9〇内作儲置利用。在上述系統中，本發明除了增加奈米級微細氣泡化加壓洋除之前處理裝置，以加強原有膜蒸餾法之前處理效果外’關鍵處在於本發明將膜表面原先被不能直接擴散之液相所佔有之空間，改由飽和水蒸氣直接取代。這樣一來’原先類似Arnold擴散裝置之蒸氣擴散模式’改成部份為氣相強制對流（f〇rced convective mass 本紙張尺度適用標準（CNS) A4規格（21Gx 297公楚)---- 第10頁 559567Cl D7 V. Description of the invention (7) 2. Pressurized floatation and gas-water mixing: a pumping motor 30 is installed on a pipeline to perform seawater extraction on the container 20, and a gas supplier is provided on the other side of the pipeline. 40. The gas supplier 40 can send _ predetermined gas 4 to the pipeline. In this embodiment, the gas 4 is general air. Before mixing, the gas 4 is pre-heated under pressure and then mixed with seawater 1 Mixed into a working liquid 5 with gas, the purpose of heating is to make the mixed working liquid 5 with a certain high temperature, which can accelerate the production of water vapor in the working liquid 5, and the energy required to heat the gas is much less than The heating of the liquid has the effect of saving costs. In addition, after the gas 4 and the seawater 1 are mixed into the working liquid 5, the high-pressure working liquid 5 is sent to a decompression cylinder 50 for decompression storage. The decompression cylinder 50 — A pressure relief valve 51 is provided on the side, and the pressure relief valve 51 is connected to the gas supplier 40 so that the working fluid 5 can be circulated in the pipeline. 3. Micro-bubble treatment: The working liquid 5 is transferred from the decompression cylinder 50 to a nanometer-level micro-bubble device 60, and its main function is to disintegrate and emulsify the working liquid 5 to make water molecules in the working liquid 5 It can be miniaturized due to a large amount of aeration, and the relative amount of steam generated is increased. As shown in the sixth figure, this principle is like the amount of steam generated after the water in the pot is blown and heated. Far more than simply heating the water in the pot normally: As for the means of miniaturizing water molecules, a variety of different technologies can be used. In this embodiment, 'the nano-level micro-bubble device 6 〇 uses * a bubble Generator (not shown), the working principle of this kind of foam generator is known (such as Taiwan No. 215 5 8 5) No., the first paper size of the United States _Home Standard (CNS) A4 specification (employment ^^ foot) Page 9 559567 C7 D7 V. Description of the invention (8) 6,293,529! Tigers and other patents), so it will not be added here Praise. 4. Desalination process: The working liquid 5 is then transferred to a desalination device 70. At the same time, referring to the seventh figure, the desalination device 7 () is provided with a plurality of hydrophobic porous organic membranes 71, and is connected on one side. A drainage pipe 73 and / or fire water & road 74 are provided. The porous organic membranes 7 i can be arranged in series or in parallel. Since the working liquid 5 of the present invention has undergone ultra-fine processing, the concentration has reached a saturated level. In this state, a large amount of water-based gas 2 can be generated to penetrate the porous organic film 71. … 5. Condensing component: The condensing component 72 that reaches the other side through the porous organic M 71❿ is condensed. In this embodiment, the desalination device 70 is ventilated to cool the condensing component 72. In the future, the water radon gas 2 can be condensed to generate fresh water 3, and the processed working liquid 5 can be transported to the drainage pipe 73, which can be connected with another desalination device (not shown in the figure). The working liquid 5 can be repeatedly used, and the fresh water 3 can be transported to the fresh water pipeline 74. In addition, a negative pressure element 80 is connected to the fresh water pipeline 74. The negative pressure element 80 is usually a vacuum pump. The fresh water 3 is drawn to another container 90 for storage. In the above system, in addition to adding nano-scale micro-bubble pressurized pre-treatment equipment to enhance the pre-treatment effect of the original membrane distillation method, the key point of the present invention is that the membrane surface of the present invention was originally liquid that could not be directly diffused. The space occupied by the phase is directly replaced by saturated water vapor. In this way, 'the original vapor diffusion mode similar to the Arnold diffusion device' was changed to forced convection in gas phase (f0rced convective mass (CNS) A4 specification (21Gx 297)) 10 pages 559567

Cl ___D7_ 五、發明說明（9 ) transfer)模式，其質傳模式由擴散（diffUSi〇n)變成部份對流（partially convective)，擴散量大幅增加。在以下將透過各種不同條件的實驗，對發明作所能達成之目的作進一步的證驗解說：【應用範例說明】原有薄膜蒸餾操作範例：範例一：以Liqui-Cel® l〇-inch X-40脫氣膜2支串聯為例（25 C );此膜為疏水性聚丙稀中空纖維材質，代表孔徑0·03 μιη，採真空模式操作。以傳統膜蒸顧法方式操作，流量為1 〇〇 gpm，產水中之含水量35.6 %，每小時產水166克，流通量相當於 0.00064 L/hr m2 或 0.00038 GFD。若採用此種薄膜來進行海水淡化，產水量太少。Cl ___D7_ 5. Description of the invention (9) Transfer) mode, its mass transfer mode is changed from diffUSion to partial convective, and the amount of diffusion is greatly increased. In the following, experiments under various conditions will be used to further verify the purpose that the invention can achieve: [Application example description] The original thin film distillation operation example: Example 1: Liqui-Cel® 10-inch X- An example of 40 degassing membranes connected in series (25 C); this membrane is made of hydrophobic polypropylene hollow fiber material, representing a pore size of 0.03 μm, and operates in vacuum mode. Operated by the traditional membrane evaporation method, the flow rate is 100 gpm, the water content in the produced water is 35.6%, and the produced water is 166 grams per hour, and the flow rate is equivalent to 0.00064 L / hr m2 or 0.00038 GFD. If such a film is used for desalination, the amount of water produced is too small.

表一膜蒸餾法計算例/25°CTable 1 Calculation example of membrane distillation method / 25 ° C

Flows 進水 (Inlet) 出水 (Outlet ) 產水 (Perm ) Volume flow (容積流量），gpm 100.00 100.00 0.360 Mass flow (流量）， lb/hr 50,050.13 50,048.68 1.453 Mol flow, lb-mole/hr (莫耳流量） 2,778.07 2,778.0 1 0.057 Mole Percent (莫耳濃度） — Oxygen (氧） 0.0004798% 0.0000306% 21.89% Nitrogen (氮） 0.0009 1 05% 0.000058 1% 41.54% Water (水） 99.998589% 99.9999 10% 3 5.63〇/〇 Carbon Dioxide (二氧化碳） 0.0000206% 0.00000 1 3% 0.94% 本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐）第11頁 559567Flows Inlet Outlet Perm Volume flow, gpm 100.00 100.00 0.360 Mass flow, lb / hr 50,050.13 50,048.68 1.453 Mol flow, lb-mole / hr ) 2,778.07 2,778.0 1 0.057 Mole Percent — Oxygen 0.0004798% 0.0000306% 21.89% Nitrogen 0.0009 1 05% 0.000058 1% 41.54% Water 99.998589% 99.9999 10% 3 5.63〇 / 〇 Carbon Dioxide (carbon dioxide) 0.0000206% 0.00000 1 3% 0.94% This paper size applies to China National Standard (CNS) A4 (210x 297 mm) Page 11 559567

Avg MW (平均分子量） 18.016 1 8 η 1 25.475 Approximate Vapor Load (lb-mole/hr) (氣體負載量） 0.057 Approx. Vapor Molar Comp. (氣體莫耳成份） lb-mole/hr g/hr Oxygen (氧） 21.89% 0.012 181 Nitrogen (氮） 41.54% 0.024 301 Water (水） 3 5.63% 0.020 166 Carbon Dioxide (二氧化碳） 0.94% 0.001 11 範例二：使用脫氣膜（30°C ) 同上，以傳統膜蒸餾法方式操作，溫度提高5艽，流量為100 gpm’產水中之含水量47.7 %,每小時產水258克，流通量相當於0.00099 L/hr m2或000058 GFD，仍然太低Avg MW (average molecular weight) 18.016 1 8 η 1 25.475 Approximate Vapor Load (lb-mole / hr) 0.057 Approx. Vapor Molar Comp. Lb-mole / hr g / hr Oxygen ( Oxygen) 21.89% 0.012 181 Nitrogen (nitrogen) 41.54% 0.024 301 Water (water) 3 5.63% 0.020 166 Carbon Dioxide (carbon dioxide) 0.94% 0.001 11 Example 2: Using a degassing membrane (30 ° C) Same as above, using traditional membrane distillation The temperature is increased by 5 ° C, the flow rate is 100% of the water content in the produced water is 47.7%, the water produced per hour is 258 grams, and the flow rate is equivalent to 0.00099 L / hr m2 or 000058 GFD, which is still too low.

表二膜蒸餾法計算例/30°CTable 2 Calculation example of membrane distillation method / 30 ° C

Flows Inlet (進水） Outlet (出水） Perm (產水） Volume flow, gpm 100.00 100.00 0.418 Mass flow, lb/hr 50,050.13 50,048.54 1.592 Mol flow, lb-mole/hr 2,778.07 2,778.00 0.066 Mole Percent Oxygen 〇.〇〇〇4449〇/0 0.0000234% 17.70% Nitrogen 0.0008502% 0.0000447% 3 3.8 3 % Water 99.998686% 99.99993 1 % 47.74% Carbon Dioxide 0.00001 82% 0.0000010% 0.72% 本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐）第12頁 559567 C7 D7 五、發明說明（11 )Flows Inlet Outlet Perm Volume flow, gpm 100.00 100.00 0.418 Mass flow, lb / hr 50,050.13 50,048.54 1.592 Mol flow, lb-mole / hr 2,778.07 2,778.00 0.066 Mole Percent Oxygen 〇.〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇〇 4449〇 / 0 0.0000234% 17.70% Nitrogen 0.0008502% 0.0000447% 3 3.8 3% Water 99.998686% 99.99993 1% 47.74% Carbon Dioxide 0.00001 82% 0.0000010% 0.72% This paper size applies to China National Standard (CNS) A4 specifications (210x 297 mm) PCT) Page 12 559567 C7 D7 V. Description of the invention (11)

Avg MW 18.016 18.016 24.063 Approximate Vapor Load (lb-mole/hr) 0.066 Approx. Vapor Molar Comp. lb-mole/hr g/hr Oxygen 17.70% 0.012 170 Nitrogen 3 3.83% 0.022 284 Water 47.74% 0.032 258 Carbon Dioxide 0.72% 0.000 10 範例三：使用脫氣膜（43°c ) 同上，以傳統膜蒸餾法方式操作，溫度提高43 °C，流量為100 gpm，產水中之含水量97.2 〇/〇，每小時產水8,986克，流通量相當於34.6 L/hr m2或20.3 GFD。Avg MW 18.016 18.016 24.063 Approximate Vapor Load (lb-mole / hr) 0.066 Approx. Vapor Molar Comp. Lb-mole / hr g / hr Oxygen 17.70% 0.012 170 Nitrogen 3 3.83% 0.022 284 Water 47.74% 0.032 258 Carbon Dioxide 0.72% 0.000 10 Example 3: Using a degassing membrane (43 ° c) Same as above, operated by the traditional membrane distillation method, the temperature is increased by 43 ° C, the flow rate is 100 gpm, the water content in the produced water is 97.2 〇 / 〇, and the water produced per hour is 8,986 G, with a flow rate equivalent to 34.6 L / hr m2 or 20.3 GFD.

表三膜蒸餾法計算例/43cCTable 3 Example of membrane distillation method calculation / 43cC

Flows Inlet Outlet Perm Volume flow，gpm 100.00 99.96 7.145 Mass flow, lb/hr 50,050.13 50,029.39 20.740 Mol flow，lb-mole/hr 2,778.07 2,776.94 1.131 Mole Percent Oxygen 0.0003803% 0.0000001% 0.93% Nitrogen 0.0007390% 〇.〇〇〇〇〇〇2% 1.8 1 % Water 99.998867% 99.999999% 97.22% Carbon Dioxide 0.0000 136% 0.0000000% 0.0 3 % Avg MW 18.016 18.016 18.337 Approximate Vapor Load (lb-mole/hr) 1.131 Approx. Vapor Molar Comp. (lb-mole/hr) g/hr 本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐）第13頁 559567 C7 D7 五、發明說明（12)Flows Inlet Outlet Perm Volume flow, gpm 100.00 99.96 7.145 Mass flow, lb / hr 50,050.13 50,029.39 20.740 Mol flow, lb-mole / hr 2,778.07 2,776.94 1.131 Mole Percent Oxygen 0.0003803% 0.0000001% 0.93% Nitrogen 0.0007390% 0.000790%. 〇2% 1.8 1% Water 99.998867% 99.999999% 97.22% Carbon Dioxide 0.0000 136% 0.0000000% 0.0 3% Avg MW 18.016 18.016 18.337 Approximate Vapor Load (lb-mole / hr) 1.131 Approx. Vapor Molar Comp. (Lb-mole / hr) g / hr This paper size is applicable to China National Standard (CNS) A4 (210x 297 mm) Page 13 559567 C7 D7 V. Description of the invention (12)

Oxygen 0.93% 0.011 153 Nitrogen 1.8 1 % 0.021 261 Water 97.22% 1.100 8,986 Carbon Dioxide 0.03% 0.000 8 範例四：使用PTFE微濾膜（20°C ) mean pore size (平均孑匕隙大小）：0.2 μηι mean thickness (平均厚度）:60 μηι mass of water vapor in saturated air (飽和空氣水蒸氣含量） 20°C ： 17.24 g/m3 > mean bubble point (平均泡點）：19 psi Patm (大氣壓力）：14.7 psi typical air flow rate (空氣流率）：6 L/min cm2Oxygen 0.93% 0.011 153 Nitrogen 1.8 1% 0.021 261 Water 97.22% 1.100 8,986 Carbon Dioxide 0.03% 0.000 8 Example 4: Using a PTFE microfiltration membrane (20 ° C) mean pore size (average 隙 size): 0.2 μηι mean thickness (Average thickness): 60 μηι mass of water vapor in saturated air 20 ° C: 17.24 g / m3 > mean bubble point: 19 psi Patm (atmospheric pressure): 14.7 psi typical air flow rate: 6 L / min cm2

= 0.36m3/hr cm2 = 6.21 g/hr cm2 = 62.1 L/hr m2 = 36.5 GFD 為一般海水淡化膜之3-6倍。此為20°C完全飽和氣體之特例。若將溫度提高至43 °C， typical air flow rate超過 12 L/min cm2 43〇C ·· 59.24 g/m3= 0.36m3 / hr cm2 = 6.21 g / hr cm2 = 62.1 L / hr m2 = 36.5 GFD is 3-6 times that of ordinary seawater desalination membranes. This is a special case of a fully saturated gas at 20 ° C. If the temperature is increased to 43 ° C, the typical air flow rate exceeds 12 L / min cm2 43〇C ·· 59.24 g / m3

所以流通量將超過 12*0.06*59.24 = 42.7 g/hr em2 = 427 L/hr cm2 = 25 1 GFD 本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐) ~一第14頁 559567Therefore, the circulation volume will exceed 12 * 0.06 * 59.24 = 42.7 g / hr em2 = 427 L / hr cm2 = 25 1 GFD This paper size applies the Chinese National Standard (CNS) A4 specification (210x 297 mm) ~ one page 14 559567

Cl D7 五、發明說明（13 ) 為一般海水淡化膜之2 5 - 3 6倍。此為43 °C完全飽和氣體之特例。【結論】表四膜蒸餾法計算比較結果溫度（°c) 25 30 43 43 (奈米級微細氣泡化氣液比1:5) 43 完全氣泡化 Vapor Load (lb-mole/hr) 0.057 0.066 1.131 >2 相對倍數關係 1.00 1.16 19.84 >40 Vapor Load For Water (%) 35.63 47.74 97.22 相對倍數關係 1.00 1.34 2.73 Vapor Load For Water (lb-mole/hr) 0.020 0.032 1.100 >2 相對倍數關係 1.00 1.60 55 Vapor Load For Water (g/hr) 166 258 8,986 > 18000 相對倍數關係 1.00 1.55 54.13 > 100 Flux (GFD) 0.00038 0.00058 20.3 >40 251 相對倍數關係 1.00 1.53 53421 > 100000 660526 由上述結果可以發現溫度高低強烈影響膜蒸餾法之產水量。以43 °C的數據來看，比MSF方法的操作溫度低，其熱量可由循環pump做功所放出之能量即可維持供應無虞，不需另外增設加熱裝置。此時之流通量為25 °C之50000多倍，實在驚人。過去未能深入探討膜蒸餾海水淡化法之操作條件，我們發現在良好設計條件下，其流通量已比傳統RO高2-3倍，若加上本發明方法，其流通量將以倍數方式增加，經濟效益更顯著。以上即為本發明膜蒸餾海水淡化法及其系統的處理過程及相關聯系統構造之概述；接著，再將本發明預期所能達成本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐）第15頁 559567 五、發明說明（14 之功效陳述如后： (1 )·淡水生成效率快速本發明主要改良重點是將海水1與氣體4混人仃奈米級微細氣泡化處理，因 A η後，再進，内部將生成大量且肉眼無法看男Π處理過程的海水1 度幾近到達飽合狀態，海水地微氣泡，使海水1濃 2(液相—氣相），在易地即可相轉變成為水蒸氣可大量且快…/二有機M 71接觸後，水蒸氣2 J人2：且陝迷地滲透至冷凝構戌…丄吐ΑΦ曰ΑΛ ; 上’使仔本發明可快速生成的大置的决水，生產效率奇佳。 (2) ·製造成本便宜Cl D7 V. Description of the invention (13) It is 2 5-3 6 times of ordinary seawater desalination membrane. This is a special case of fully saturated gas at 43 ° C. [Conclusion] Table 4 Calculation and comparison results of membrane distillation method Temperature (° c) 25 30 43 43 (nano-scale micro-bubble gas-liquid ratio 1: 5) 43 Fully-bubble Vapor Load (lb-mole / hr) 0.057 0.066 1.131 > 2 Relative multiple relationship 1.00 1.16 19.84 > 40 Vapor Load For Water (%) 35.63 47.74 97.22 Relative multiple relationship 1.00 1.34 2.73 Vapor Load For Water (lb-mole / hr) 0.020 0.032 1.100 > 2 Relative multiple relationship 1.00 1.60 55 Vapor Load For Water (g / hr) 166 258 8,986 > 18000 relative multiple relationship 1.00 1.55 54.13 > 100 Flux (GFD) 0.00038 0.00058 20.3 > 40 251 relative multiple relationship 1.00 1.53 53421 > 100000 660526 From the above results it is possible It was found that the temperature strongly affected the water yield of the membrane distillation method. According to the data of 43 ° C, the operating temperature is lower than that of the MSF method, and the heat can be maintained by the energy released by the circulating pump work, and no additional heating device is required. The circulation at this time is more than 50,000 times 25 ° C, which is amazing. The operating conditions of the membrane distillation seawater desalination method have not been thoroughly explored in the past. We have found that under good design conditions, the flow rate is already 2-3 times higher than that of traditional RO. If the method of the present invention is added, the flow rate will be increased in multiples. The economic benefits are more significant. The above is an overview of the membrane distillation seawater desalination method of the present invention, the processing process of the system and the structure of the associated system; then, the paper size expected to be achieved by the present invention is adapted to the Chinese National Standard (CNS) A4 specification (210x 297) (Principle) Page 15 559567 V. Description of the invention (14 The effect of the statement is as follows: (1). The fresh water generation efficiency is fast. The main improvement of the present invention is to mix seawater 1 and gas 4 into the nano-scale microbubble treatment. After A η, re-enter, a large amount of seawater will be generated in the interior and cannot be seen by the naked eye. The seawater is almost saturated at 1 degree, and the microbubbles of the seawater make the seawater 1 thick and 2 (liquid phase-gas phase). The phase change from ground to water vapor can be large and fast ... / After the two organic M 71 are contacted, the water vapor 2 J person 2: and the shame penetrates into the condensed structure ... spitting ΑΦ 曰 ΑΛ; the above makes the present invention Large set of water can be generated quickly, and the production efficiency is very good. (2) · Cheap manufacturing cost

本發明一改習知董+ I 對海水加熱的做法，而是改採海水1混合氣體4的手段，如果兮盏胁又如果4軋體4採用熱空氣將更佳，此種手 ί又所需的能置不會太高，麵讲杳、，&過貫驗數據證貫，本發明整個系統所需的能量遠較習知者要來得低’而淡水3的產能卻可有效提升’故本發明確實可降低淡水3的製造成本，利用本發明即可生產出符合經濟成本的淡水3。 (3) .延長薄膜使用壽命奈米級微細氣泡化加壓浮除裝置具有良好前處理效果，可去除海水中懸浮固體、藻類、膠質固體等雜質，有效降低污/尼#度指數（SDI : Silt Density Index )，加上高含氣量之工作水體有強烈擾動效果（Turbulent Effect )，可有效減少薄膜表面污染堵塞之現象。 (4) ·降低對流質量傳送阻力奈米級的微細氣泡化注氣處理裝置可將空氣氣泡微細化本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐）第16頁 559567 C7 _________D7__ 五、發明說明（15) --- ，使大部份氣泡大小比薄膜表面孔洞之開口還小，陝有效懸浮分散於待處理飼水水體中，還可克 =了可以，降低對流質量傳送阻力。札^包表面張力 (5) ·產水量大高含氣量之工作水體，改變了疏水性薄膜表面孔口處之質傳模式，薄膜孔口之氣液比例提高，使f傳阻力大幅;降，由原先液體於孔隙内蒸發成蒸氣，變成部份液體已=行氣化，大幅增加蒸氣流通量，打破需要液氣平衡之限制，同時減少了溫度極化與濃度極化現象，有效提昇造水量。值得一提的是，此一改良方法，除了可應用於上述的海水淡化（Sea Water Desalination )、半鹹水淡化（ Brackish Water Desalination)處理外，亦可運用於污水淨化（Effluent Reclamation)、廢水回收（Waste Water Reclamation )與含鹽酒精脫鹽處理（saited Rice Wine Desalination )等工業製程。惟以上所述者，僅為本發明之較佳實施例而已，當不能以此限定本發明實施之範圍，即大凡依本發明申請專利範圍及發明說明書内容所作之簡單的等效變化與修飾，皆應仍屬本發明專利涵蓋之範圍内。本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐）第17頁 559567 C7 D7 五、發明說明 (16) [ 元件標號對照】卜. 海水 2·· •水蒸氣 3"· 淡水 4·· •氣體 5··· 工作液體 10 …淡化裝置 11" •多孔有機膜 11 1…孑L隙 12·· •冷凝構件 20 …容器 30" •抽水馬達 40 …氣體供應器 50.· •減壓筒 5 1 …泡壓閥 60·· •奈米級微細氣泡化裝置 70 …淡化裝置 7卜 •多孔性有機膜 72 …冷凝構件 73·· •排水管路 74 …淡水管路 80·· •負壓元件 90 …另一容器本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐）第18頁The present invention changes the method of heating the seawater by Zhi Dong + I, but changes the method of extracting the mixed gas 4 of seawater 1. It is better to use hot air if the rolling body 4 is used. The required energy capacity will not be too high. It is proved that the energy required by the entire system of the present invention is much lower than that of a conventional person, but the capacity of fresh water 3 can be effectively increased. Therefore, the present invention can indeed reduce the manufacturing cost of the fresh water 3, and the fresh water 3 can be produced in accordance with the economic cost by using the present invention. (3) Nano-grade micro-bubble pressure floatation device with long film life has good pre-treatment effect. It can remove impurities such as suspended solids, algae, colloidal solids in seawater, and effectively reduce the pollution / Ni # degree index (SDI: Silt Density Index), coupled with the high water content of the working water body has a strong disturbance effect (Turbulent Effect), which can effectively reduce the phenomenon of film surface pollution and clogging. (4) · Nano-level micro-bubble gas injection processing device to reduce the convective mass transmission resistance. The air bubbles can be miniaturized. The paper size is applicable to China National Standard (CNS) A4 (210x 297 mm). Page 16 559567 C7 _________D7__ V. Description of the invention (15) ---, making most of the bubbles smaller than the openings of the holes on the surface of the film. Shaanxi effectively suspends and disperses in the feed water to be treated. It can also reduce the resistance of convective mass transmission. . The surface tension of the package (5) · The working water body with large water production and high gas content has changed the mass transfer mode at the orifice of the surface of the hydrophobic membrane, and the gas-liquid ratio of the membrane orifice is increased, which makes the f-transmission resistance greatly reduced; The original liquid evaporates into vapor in the pores, and becomes a part of the liquid has been vaporized, which greatly increases the vapor flow, breaks the restriction of liquid-gas balance, and reduces the phenomenon of temperature polarization and concentration polarization, effectively increasing the amount of water produced. . It is worth mentioning that this improved method can be used in addition to the aforementioned Sea Water Desalination and Brackish Water Desalination treatment, as well as Effluent Reclamation and Wastewater Recovery ( Waste Water Reclamation) and Said Rice Wine Desalination. However, the above are only the preferred embodiments of the present invention. When the scope of implementation of the present invention cannot be limited by this, that is, the simple equivalent changes and modifications made according to the scope of the patent application and the content of the invention specification, All should still fall within the scope of the invention patent. This paper size applies the Chinese National Standard (CNS) A4 specification (210x 297 mm) Page 17 559567 C7 D7 V. Description of the invention (16) [Comparison of component numbers] B. Sea water 2 ·· • Water vapor 3 " · Fresh water 4 ·· • Gas 5 ··· Working liquid 10… Desalination device 11 " • Porous organic membrane 11 1… 孑 L gap 12 ·· • Condensation member 20… Container 30 " • Pumping motor 40… Gas supply 50. · • Cylinder 5 1… Bubble pressure valve 60 ·· • Nano-level micro-bubble device 70… Desalination device 7 • Porous organic membrane 72… Condensing member 73 ·· • Drain line 74… Fresh water line 80 ·· • • Negative pressure element 90… another container This paper size applies to China National Standard (CNS) A4 (210x 297 mm) Page 18

Claims

559567 A8 B8 C8 申請專利範圍 •一種膜蒸餾海水淡化法，、供給海水：取一容器水經過過濾前處理以去除部份雜質；包含有下列步驟：盛裝預定容量之一海水，並將海一加壓浮除前處理：將過濾後海水進行微細氣泡化加壓洋除前處理，以去除藻類等懸浮固體雜質；一微細氣泡化注氣處理：將浮除後之飼水經過微細氣泡化氣水混合再次處理，使海水與氣體混合成均句白霧礼化狀態之工作液體，其氣泡内為飽和水蒸氣；四、淡化處理：再將均勻氣水混合狀態之工作液體輸送至一淡化裝置，該淡化裝置内部具有一個或一個以上的疏水性多孔薄膜，使含有大量飽和水蒸氣的高含氣量工作液體，可輕易透過多孔疏水性薄膜；及五、冷凝構件：對透過薄膜之水蒸氣分子予以凝結生成淡水。 2 ·依據申請專利範圍第丄項所述之膜蒸餾海水淡化法，其中，在步驟二時，加壓入海水内的該氣體為空氣。 3 ·依據申請專利範圍第2項所述之膜蒸餾海水淡化法，其中，該氣體尚未與海水混合之前，可以預先以高溫進行加熱，使混合後的工作液體具有一定溫度。 4 ·依據申請專利範圍第2項所述之膜蒸餾海水淡化法，其中 ’該氣體是以負壓吸入方式與海水混合處理。 5 ·依據申請專利範圍第1項所述之膜蒸餾海水淡化法，其中’該工作液體之操作溫度建議為3 〇 ~ 6 01：。 6 ·依據申請專利範圍第1項所述之膜蒸餾海水淡化法，其本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公餐）第19頁 559567 a8 C8 _-_______D8__ 六、申請專利範圍中’在步驟二時’可以添加界面活性劑於飼水内，以穩定或增加氣泡數量。 7 · —種膜蒸餾海水淡化系統，包含：一容器，用以盛裝預定容量之海水，該容器一側設有一供抽送海水的管路；一氣體供應裝置’是連結於該管路上，其具有一氣體供應器，以對該管路上的海水泵送入加壓氣體，使海水成為帶有氣體的工作液體；一微細氣泡化裝置，是連結於該氣體供應裝置一側，可對工作液體進行碎解乳化；一淡化裝置，是連結於該微細氣泡化裝置一側，具有一個或一個以上的多孔疏水性薄膜；一冷凝裝置，是與該淡化裝置連結，以對通過該等多孔疏水性薄膜的水蒸氣施以凝結而生成淡水。 8 ·依據申请專利範圍第7項所述之膜蒸餾海水淡化系統，其中，更包含有一減壓筒，該減壓筒是設置於該氣體供應器一側，供儲置氣體與海水混合成的工作液體，該減壓筒具有一洩壓閥，該洩壓閥是連結於該氣體供應器，使工作液體得以在該管路内循環。 9 ·依據申請專利範圍第7項所述之膜蒸餾海水淡化系統，其中，該淡化裝置是通入空氣對冷凝裝置進行冷卻。 1 0 ·依據申請專利範圍第7項所述之膜蒸餾海水淡化系統，其中，該淡化裝置接設有一排水管路及一淡水管路，該淡水管路並接設有一負壓元件，以將成品淡水抽送至另一本紙張尺度適用中國國家標準（CNS) A4規格（210χ 297公釐）第20頁 559567 六、申請專利範圍容器儲置。 1 1 ·依據申請專利 ’其中，該淡 0 · 0 0 1 〜0 · 0 5 μχη，水性材質薄膜不 wound)、中空键 frame) 〇 1 2 ·依據申請專利其中’該等多孔3 A8 B8 C8 D8 範圍第7項所述之膜蒸餾海水淡化系統 .化裝置所使用薄膜孔隙大小約屬於習稱之微過濾（MF)或超過濾（UF)疏限外型是管式（tubular)、捲式（spiral i* 維（hollow fiber)或板框式（plate and 範圍第7項所述之膜蒸餾海水淡化系統，范性薄膜之膜管可以串聯或並聯方式操作本紙張尺度適用中國國家標準（CNS) A4規格（210x 297公釐）第21頁559567 A8 B8 C8 Patent Application Scope • A membrane distillation seawater desalination method to supply seawater: take a container of water and treat it before filtering to remove some impurities; it contains the following steps: hold one of the seawater of a predetermined capacity, and add one to the sea Pre-float removal treatment: The filtered seawater is subjected to micro-bubble pressure and pre-sealing treatment to remove suspended solid impurities such as algae; a micro-bubble gas injection treatment: the floated feed water is subjected to micro-bubble gas water Mixing and reprocessing, so that seawater and gas are mixed into a homogeneous white mist etiquette working liquid, whose bubbles are saturated with water vapor; 4. Desalination treatment: The working liquid in a uniform gas-water mixed state is sent to a desalination device. The desalination device has one or more hydrophobic porous membranes inside, so that high gas content working liquids containing a large amount of saturated water vapor can easily pass through the porous hydrophobic membranes; and 5. Condensing component: The water vapor molecules that pass through the membranes are applied. Condensation produces fresh water. 2 · According to the membrane distillation seawater desalination method described in item 申请 of the patent application scope, wherein in step two, the gas pressurized into the seawater is air. 3. According to the membrane distillation seawater desalination method described in item 2 of the scope of the patent application, before the gas is mixed with seawater, it can be heated at high temperature in advance to make the mixed working liquid have a certain temperature. 4 · According to the membrane distillation seawater desalination method described in item 2 of the scope of the patent application, wherein the gas is mixed with seawater in a negative pressure suction method. 5 • According to the membrane distillation seawater desalination method described in item 1 of the scope of the patent application, ‘the operating temperature of the working liquid is recommended to be 30 to 60: 1. 6 · According to the membrane distillation seawater desalination method described in item 1 of the scope of patent application, the paper size of this paper applies the Chinese National Standard (CNS) A4 specification (210x 297 meals) Page 19 559567 a8 C8 _-_______ D8__ VI. Patent Application In the range 'in step two', a surfactant can be added to the feed water to stabilize or increase the number of bubbles. 7 · — Seed membrane distillation seawater desalination system, including: a container for containing seawater of a predetermined capacity, a side of the container is provided with a pipeline for pumping seawater; a gas supply device is connected to the pipeline, which has A gas supplier to pump pressurized gas into the seawater on the pipeline to make the seawater a working liquid with gas; a micro-bubble device is connected to one side of the gas supply device and can carry out working liquid Fragmentation and emulsification; a desalination device is connected to one side of the micro-bubble device and has one or more porous hydrophobic films; a condensation device is connected to the desalination device to pass through the porous hydrophobic films The water vapor is condensed to produce fresh water. 8. The membrane distillation seawater desalination system according to item 7 of the scope of the patent application, which further includes a pressure reducing cylinder, which is arranged on the side of the gas supplier for mixing the storage gas with the seawater. For the working fluid, the pressure reducing cylinder has a pressure relief valve, which is connected to the gas supplier, so that the working fluid can be circulated in the pipeline. 9. The membrane distillation seawater desalination system according to item 7 of the scope of the patent application, wherein the desalination device is cooled by passing air into the condensation device. 10 · The membrane distillation seawater desalination system according to item 7 of the scope of the patent application, wherein the desalination device is connected with a drainage pipe and a fresh water pipe, and the fresh water pipe is connected with a negative pressure element in parallel to The fresh water of the finished product is pumped to another paper size which is applicable to the Chinese National Standard (CNS) A4 specification (210 x 297 mm). Page 20 559567 6. The scope of patent application container storage. 1 1 · According to the patent application, where the light is 0 · 0 0 1 ～ 0 · 0 5 μχη, the water-based material film does not wound), hollow bond frame) 〇1 2 · According to the patent application, which includes these porous 3 A8 B8 C8 D8 The membrane distillation seawater desalination system described in item 7 of the scope. The pore size of the membrane used in the desalination device is about the microfiltration (MF) or ultrafiltration (UF). (Spiral i * dimension (hollow fiber) or plate-and-frame (plate and range of the membrane distillation seawater desalination system described in item 7), the membrane film tube of the general thin film can be operated in series or in parallel. This paper is applicable to Chinese national standards (CNS ) A4 size (210x 297 mm) page 21