TW201023960A - System for separation of volatile components from solution and process thereof - Google Patents

Abstract

There is disclosed a separation system for separation of a volatile component from a feed solution such as the separation of water vapor from a saline solution, such as seawater. The separation system includes a plurality of hollow fiber membranes being selectively permeable to allow the volatile component in a volatile phase to pass therethrough while substantially preventing passage of the feed solution. The system also includes a heat source capable of heating the feed solution on one side of the hollow fiber membranes to create the volatile phase that passes through the hollow fiber membranes. A heat exchange means is provided to condense the volatile component and which is configured to capture the heat of condensation, and wherein the heat exchange means are thermally coupled to the heat source to thereby drive or supplement the heat source with the heat of condensation.

Description

201023960 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to a system, method and apparatus for separating volatile components from a feed solution. [Prior Art] Thin film distillation is a film-based process in which water vapor can be driven by a water vapor pressure driven by a difference in temperature, vacuum, and/or solute concentration, and through a pore of a hydrophobic thin crucible. Pass through the film. The main features of the film in a thin film distillation system are that it is porous and resistant to wetting of the treatment liquid, and does not alter the gas-liquid equilibrium of the different components of the treatment liquid. In the ideal case, capillary condensation should not occur in the pores of the film. For each component in the system, the driving force that drives it through the film is the partial pressure gradient present on both sides of the film. In contrast to conventional evaporation processes, thin film distillation processes have the advantage of being able to operate efficiently at lower operating temperatures, thereby saving energy consumption compared to conventional distillation processes. The use of low-grade energy, such as waste heat and solar energy to drive the membrane steaming system, makes it energy efficient and environmentally friendly. However, the big problem with low-level energy is that the heat it provides may change with the Gan. For example, a low-level energy source such as solar energy will provide thermal energy that will change over time and weather conditions. In addition, a low-grade energy source such as waste heat, for example, a chemical production process will vary with the process conditions of the refinery at any given time. Therefore, it is difficult to apply to the thin film distillation process due to the lack of energy output stability of low-grade energy sources.

The goal of a composite thin film distillation system having a multi-stage cell configuration is to use condensation heat to supplement the thermal energy required to produce a vapor phase of volatile components, which faces certain limitations. Using a limited heat duty at each stage to provide the next stage of the temperature gradient may result in a large number of optimal stage requirements before a reasonable steam liquid yield is achieved. The structure of each ruthenium stage also limits the flexibility of available surfaces and hinders heat exchange. Since the membrane modules and heat exchangers in each stage are the same two units, the control of the heating amount is also limited. An alternative heat exchanger structure optimizes heat flow, but is not acceptable in this case. Traditional thin film steaming systems face the same limitations; the function of the film and heat exchanger cannot be easily individualized, resulting in only a fixed heat exchange surface area. The former requirement is to provide a system, device or device that separates volatile matter from the solution, and has the disadvantage of being installed. The invention is directed to providing a separation system for separating volatile components from the first 5 201023960 of the present invention, the system comprising: a plurality of hollow fiber membranes, Selectively permeable and allowing the passage of volatile components in the volatile phase to substantially prevent the passage of the feed solution; a heat source having the ability to heat the feed solution on one side of the hollow fiber membrane to produce a passage through the hollow fiber membrane a volatile phase; and a heat exchange device condensing the volatile components and configured to obtain heat of condensation, the heat exchange device being thermally coupled to the heat source to thereby drive or supplement the heat source by the heat of condensation. Advantageously, the hollow fiber membrane is used to provide a tightly disposed structure having a relatively high surface area compared to the flat membrane for separating volatile components from the feed solution. Advantageously, the heat exchange device uses the heat of condensation provided by the heat source in the separation process to drive or replenish energy, thereby saving energy input to the overall system. Advantageously, the heat exchange means is a reduction in the consumption of cooling agent to condense volatile constituents. Therefore, the combination of the hollow fiber membrane for recovering heat of condensation and the heat exchanger provides an efficient thermal energy system for separating volatile components from the solution. In one embodiment, a desalination system is provided, comprising: a plurality of hollow fiber membranes that are selectively permeable and allow water vapor to pass therethrough to substantially prevent passage of brine; 201023960 a heat source having a side that heats the hollow fiber membrane The ability of the saline solution to produce a water vapor phase through the hollow fiber membrane; and a heat exchange device for condensing the water vapor phase and configured to obtain heat of condensation, the heat exchange device being thermally coupled to the heat source, thereby Condensation heat drives or supplements the heat source. A second object of the present invention is to provide a separation apparatus for separating volatile components from a feed solution, the apparatus comprising: ® a plurality of hollow fiber membranes having permselectivity and allowing passage of volatile components in the volatile phase, and Substantially preventing the passage of the feed solution; a plurality of hollow fiber modules each having a closed chamber and an inlet for conveying the feed solution to one side of the hollow fiber membrane, and The sealed chamber has a subset of the plurality of hollow fiber membranes extending therethrough; φ a plurality of heat exchangers in communication with the fluid of the volatile component to obtain condensation heat when the volatile components are condensed into a liquid These heat exchange devices have the ability to be thermally coupled to a heat source, thereby driving or supplementing the heat source by the condensation heat described above. A third object of the present invention is to provide a process for separating volatile components from a feed solution, the process comprising the steps of: heating a feed solution with a heat source; when there is a pressure difference between the two sides of the plurality of hollow fiber membranes, 7 201023960 The feed solution is made up of multiple components so that the volatile components in the volatile phase are formed on one side of the hollow fiber membrane, and the volatile components are located on the opposite side of the feed solution, and the volatility in the condensed volatile phase The composition, thus obtaining the heat of condensation, and the use of this heat of condensation, thereby driving or supplementing the heat to the heat source described above. [Embodiment] Definition: The meanings of the words and words used below shall be: "The term "thermal duty" as used in the contents of this manual refers to the passage of a certain period of time. , the heat source, or, the heat sink, ie, the heat sink ', is a heat device that emits heat. For example, the heat load of a heat exchanger refers to a certain The amount of thermal energy required to exchange a heat exchanger from one fluid to another during a particular period. As used herein, the term "variable heat load" means that the heat load will change over time. As referred to in this specification, the term "hollow fiber membrane" means a thin film which has a hollow core surrounded by a closed outer wall. Although some hollow fiber membranes may be substantially circular tubes, the term should not be interpreted to mean that all hollow fiber membranes are circular tubes, and 201023960 is any representative shape. In the present disclosure, the outer wall of the hollow fiber membrane is at least partially permeable to certain chemical species. Thus, physically permeable hollow fibers (eg, due to voids present in the outer wall of the hollow fiber), and/or chemically permeable hollow fibers (eg, through the outer wall of the hollow fiber due to mass transport of chemical species) are included in the definition Within the meaning of. The term "substantially" does not exclude "completely" 'for example', and substantially no composition of ''Y may be completely devoid of gamma. That is to say, the term "substantially" is to be interpreted as, completely, or, or, in part, . If necessary, 'the definition of the invention may be omitted, substantially.' Unless otherwise stated, 'comprising', and 'including (c〇mprise)' and its grammatical changes are mentioned. Shape, is meant to represent, open-ended, or inclusive language that includes not only the recited elements but also additional and unquoted elements. The term "about" as used in the compositional concentrations mentioned in the context generally means the positive/negative five percentages of the set value, and generally more than four percentages of the positive/negative value of the set value, generally more The positive/negative three percentages of the set value are generally more than two percentages of the positive/negative value of the set value. Generally, it can even be a positive/negative percentage of the set value, and generally can even be the zero percentage of the set value. . Throughout the disclosure, certain embodiments may be disclosed in a format 9 201023960. The description of this range format should be understood only for convenience and brevity and should not be construed as limiting the scope of the scope of the unchangeable limitations. Therefore, a range of descriptions should be considered to explicitly disclose all possible sub-ranges and individual values within the scope. For example, a range of 1 to 6 statements should be considered to have explicitly disclosed sub-ranges such as 1 to 3, 〖 to 4, 丨 to 5, 2 to 4, 2 to 6, 3 to 6, etc., and individual ranges within the range Values, such as work, 2, 3, 4, 5, and 6. This applies to a wide range. Disclosure of the Best Embodiment: A typical, non-limiting embodiment of a film module will be disclosed herein. In one embodiment, a separation line for separating a volatile component from a feed solution, such as a self-salt salt solution (eg, a knife exiting water vapor in seawater) is disclosed. The separation system includes a plurality of medium-sized workers with selective permeability. a fibrous membrane that allows the volatility in the volatilized phase to be substantially reduced while substantially preventing the passage of the feed solution. The system also includes a "heat source of the feed solution on one side of the hot hollow fiber membrane to volatilize the empty fibrous membrane. The heat exchange provided is provided with two volatile components' and its configuration can be used to obtain a condensation heat transfer drive or a supplemental heat source. The error is ν. Advantageously, the hydrophobic polymer hollow fiber membrane may be a hydrophobic polymer hydrophobic; Removed from the salt water removal system, 201023960 can not be wetted by the saline solution, but allows water vapor to pass through the polymer, thus increasing the effectiveness of separating water vapor from the brine. Typical hydrophobic polymers include polyalkylacrylic acid. Esters, polydienes, polyolefins, polylactones, polyoxyalkylenes, polyethylene oxides, polypyridines, polycarbonates, polyvinyl acetates, polysulfones, polypropylenes PP), polytetrafluoroethylene (PTFE), polyethylene (PE), polyvinylidene fluoride (PVDF), polydecylpentene (PMP), polydidecyloxane, polybutadiene, polyphenylene Ethylene, polydecyl methacrylate, perfluoropolymer, polydialkyloxazoline or polyphenyloxazoline, derivatives thereof, salts thereof, and combinations thereof. Advantageously, the type of hollow fiber membrane can be Depending on the volatile components separated from the feed solution. For example, in another embodiment, there is disclosed a separation system that separates volatile components from waste oil. The separation system includes a plurality of hydrophobic ones. The tubular stainless steel film has selective permeability and allows the passage of volatile components in the volatile phase to substantially prevent the passage of the feed solution. This non-recording steel film can prevent the penetration of waste oil due to its hydrophilic nature, however, the volatile phase The volatile components evaporated in the medium can pass, and thus the volatile components can be separated from the waste oil. The feed solution refers to any liquid solution containing volatile components. That is, the volatile component is one Evaporated matter, so Separated from the liquid solution. For example, the feed solution may be water, and the water includes a volatile organic compound having a lower boiling point than water. Another example is that the feed solution may be an aqueous solution, 11 201023960 which contains One or more solutes are dissolved therein, or the aqueous solution does not substantially contain one or more solutes, but rather a solvent thereof as a volatile component. Further, it should be understood that in some embodiments, the self-feed solution is removed. In addition to volatile components, it may not be to obtain volatile components, but to concentrate the feed solution. For example, in a juice manufacturing process, in order to concentrate juice for transport, it may be an ideal way to remove moisture from the juice. In an embodiment, the separation system includes means for varying the thermal duty of the heat exchange device depending on the heat duty of the heat source. This unit may include a valve system that can be opened and closed. Programmable logic controllers may be used to control the opening and closing of these valves. The heat exchange device can comprise at least one heat exchanger. The heat exchangers can be configured to flow in series or parallel to each other. In one embodiment, the heat exchange device includes a plurality of heat exchangers, and the means for varying the heat load of the heat exchanger is a device that includes a number of heat exchangers for varying the receivable volatile components. Each heat exchanger can have at least one valve for the flow of volatile constituents. When the valve is opened, the heat exchanger can receive volatile components. When the valve of a particular heat exchanger is closed, volatile materials will not enter this particular heat exchanger and the volatile component will then face another heat exchanger with the open valve. In this manner, the number of heat exchangers that can receive volatile components can be controlled. 201023960 Advantageously, the number of heat exchangers used can be chosen to recover as much as possible the latent heat of volatile materials, thus increasing the efficiency of the separation system. More advantageously, the separation system can be used as a power system and can be tailored to process conditions, particularly the amount of heat source heating, and is particularly advantageous when the heat source is variable. The use of customizable heat exchange devices can significantly reduce the total thermal energy consumption of the separation system. • The separation system can include at least one hollow fiber module. In one embodiment, the separation system includes a plurality of hollow fiber modules, each fiber module including a chamber having a subset of a plurality of hollow fiber membranes disposed therein. The plurality of fiber molds can further flow fluidly in series with one another. In the separation system, the heat exchange unit can be disposed between the hollow fiber modules. In one embodiment, the heat exchange device includes a plurality of heat exchangers, wherein at least one of the heat exchangers is disposed between the upstream hollow fiber module and the downstream hollow fiber module that are in fluid communication with each other. Each heat exchanger obtains the heat of condensation of the volatile phase to heat the feed solution in the hollow fiber module. In one embodiment, the heat exchanger disposed between the upper and lower hollow fiber modules is configured to obtain the condensation heat of the volatile phase of the upstream hollow fiber module, and then the heat obtained is used to heat through the downstream hollow. The feed solution of the fiber module. 13 201023960 The heat source is a feed solution configured to heat into a plurality of hollow fiber modules. The heat source can simultaneously heat all of the hollow fiber modules, or simultaneously heat the combination of hollow fiber modules, or individually heat each hollow fiber module. In one embodiment, the configured heat source is a feed solution for individually heating into each hollow fiber module. Advantageously, each hollow fiber module can be operated individually and its operating parameters can be individually controlled. The heat source may include any suitable heat source. The heat source can have a fixed heat load or a variable heat load. In an embodiment, the heat source has a variable thermal load. For example, a heat source having a variable thermal load may be a waste heat source or a solar heat source or a geothermal source. In an embodiment, the heat source may include an exhaust heat source. Typical waste heat sources include waste gas from gas boilers in power plants and incinerators, process gases from chemical and metallurgical operations, and waste heat from other industrial processes. In countries with warm climates, solar energy can be used as a heat source. Solar heat can heat the feed solution from 40 degrees to 95 degrees, from 50 degrees to 95 degrees, from 50 degrees to 75 degrees. In solar heating systems, solar heat is concentrated into a heated fluid, such as water. The heated fluid is then directed to a vacuum tube and its thermal energy is transferred to the feed solution via a heat exchanger, thereby achieving the effect of heating the feed solution. In one embodiment, disclosed is a separation device for separating volatile components from a feed solution 14 201023960, the device comprising: a plurality of hollow fiber membranes having permselectivity and allowing passage of volatile components in the volatile phase, And substantially preventing the passage of the feed solution; a plurality of hollow fiber modules, each module having a closed chamber and an inlet having a subset of a plurality of hollow fiber membranes Extending therethrough, the water inlet is a side for transporting the feed solution to the hollow fiber membrane; a heat source thermally coupled to the feed solution; and a plurality of heat exchangers fluid with the volatile component Coupling, and configured to obtain heat of condensation, wherein the heat exchanger is thermally coupled to the heat source, thereby driving or supplementing the heat source by condensation heat. The plurality of hollow fiber modules may be fluidly connected in series, in parallel, or in series and in parallel with each other. In one embodiment, the plurality of φ hollow fiber modules are fluidly flowing in series with each other. The feed solution can pass through each hollow fiber module or can bypass at least one hollow fiber module. In one embodiment, the feed solution can bypass one or more hollow fiber modules. Each of the hollow fiber modules has a closed chamber having a subset of a plurality of hollow fiber membranes extending therethrough. These hollow fiber membranes may be hydrophobic polymer membranes, and may be selected from the group consisting of polyvinylidene fluoride, polypropylene, polyethylene, and polytetrafluoroethylene 15 201023960 vinyl fluoride. The separation device can further include a monitoring device coupled to the heat source for monitoring the amount of heating of the heat source. The monitoring device can include, for example, at least one or a combination of a thermal sensor coupled to a controller, a temperature transmitter, a temperature sensor, or a thermocouple. The separation device can further include a control device coupled to the monitoring device and the plurality of heat exchangers. The control device is able to determine the number of heat exchangers to be used in accordance with the thermal load in the monitoring. Advantageously, the number of heat exchangers to be used can be customized in accordance with a variable heat source. Further disclosed is a process for separating volatile components from a feed solution, comprising the steps of: heating a feed solution with a heat source; and having a pressure difference between the two sides of the plurality of hollow fiber membranes, allowing the feed solution to pass through the plurality One side of the hollow fiber membrane, the volatile component in a volatile phase is formed on one side of the hollow fiber membrane, and the volatile component is located on the opposite side of the feed solution; the volatile component in the volatile phase is condensed Thereby obtaining a heat of condensation; and using heat of condensation to thereby drive or supplement the heat to the heat source. This process can also include the step of varying the heat source flux. When the heat source flux changes, the process may further comprise the step of utilizing a plurality of heat exchangers to obtain heat of condensation. Then, the heat load of the heat exchanger can be changed as the amount of heating of the heat source changes. The process may further comprise the step (1) of providing a plurality of hollow fiber modules, each hollow fiber module comprising a chamber having a subset of a plurality of hollow fiber membranes disposed therein, wherein the hollow fiber modules are in series with each other Flow, and (ii) individual heating of the feed solution entering each hollow fiber module. • Volatile components can be separated from the liquid by a pressure difference between the lumen side and the shell side of the hollow fiber membrane. This can be achieved by attaching a source of negative pressure to the exit end of the hollow fiber membrane. This negative pressure can be applied to form a vacuum on the lumen side of the hollow fiber membrane. This pressure differential helps to remove volatile components from the liquid and allows volatile components to evaporate at low temperatures, making it possible to use low-grade heat sources for evaporation. Typical volatile components include water, as well as organic compounds such as esters, ethers, aldehydes, alcohols, nitriles, and unsaturated carbohydrates such as terpenes. In one embodiment, the feed solution can be saline, such as brackish water or seawater, and the volatile component can be water evaporated from the brine, which is substantially salt-free water vapor. The coolant used to condense the volatile components that have evaporated in the final stage can be any type of coolant. In one embodiment, the cooling liquid at room temperature (about 20 ° C) is water. Advantageously, room temperature water is readily available in the factory and can be easily recycled or disposed of. 17 201023960 Detailed description: Figure 1 is an energy-saving thin film distillation process 100 comprising stages A, B, C, ..., η, where A represents the first stage, B represents the second stage, and η represents the nth stage. Each stage includes a storage tank containing seawater (1〇Α, 10Β, 10C, ..., 1〇η), heat exchangers (12Α, 12Β, 12C, ..., 12η), and a membrane module (14Α, 14Β, 14C, ..., 14η). A plurality of hollow fiber films (not shown) having a subset of each of the film modules (14, 14, 14, C, ..., 14n) are disposed therein. Referring to the stage A of the thin film distillation process, the seawater liquid stored in the storage tank 10A flows to the heat exchanger 12A via the feed stream 11A. The seawater feed stream 11A is heated by the following method and exits the heat exchanger 12A via the hot seawater stream 13A. The temperature of the hot fluid is higher than the temperature of the seawater in feed stream 11A, and the hot fluid flows into heat exchanger 12A via hot fluid stream 16A. The hot fluid passing through stream 16 A has been heated by a solar heat source, wherein the solar energy is used to heat the hot fluid. The hot fluid acts as a heat source for heating the seawater passing through the heat exchanger 12A. When the thermal energy present in the hot fluid is transferred to the seawater passing through the heat exchanger 12A, the hot fluid in 16A is cooled to a lower temperature and exits the heat exchanger 12A via the cooling fluid stream 18A. After passing through the heat exchanger 12A, the hot seawater 13A flows into the membrane module 14A under a negative pressure state (i.e., vacuum) at 201023960. The membrane module 14A and the other membrane modules (14B, 14C, ..., 14n) include a chamber having a water inlet conduit for receiving seawater and for allowing seawater to be self-contained Remove the discharge pipe. As described above, the chamber of the module 14A is composed of a plurality of hollow fiber membranes (not shown), each hollow fiber membrane having an open end at one end of the tube and a closed end at the other end of the tube. The hollow fiber membrane is made of a hydrophobic polymer (polypropylene, polyethylene, polyvinylidene fluoride, or polytetrafluoroethylene) that allows water vapor to pass through but is generally impermeable to aqueous liquids. Applying a vacuum state to the inner cavity side or the outer casing side of the hollow fiber membrane can also create a vacuum state in the chamber 14A. When the hot seawater stream 13A enters the chamber of the membrane module 14A, most of the water contained in the seawater evaporates into water vapor substantially free of salt. The water vapor passes through the wall of the hollow fiber membrane, enters the inner cavity of the hollow fiber membrane disposed in the membrane module 14A, and then exits through the open end of the hollow fiber membrane as the vapor stream 17A. Most of the seawater rich in salt at this point remains in the chamber of membrane module 14A and is removed from membrane module 14A via product stream 15A. The vapor stream 17A is insulated to prevent heat loss and maintained in a negative pressure state to ensure that water can be maintained in a vapor state prior to entering the downstream heat exchanger 12B, as will be described further below. It must be understood that other film modules (14B, 14C, ..., 19 201023960 14n) have the same operational principle as the film module 14A described above. At the same time as the operation, in order to evaporate the water substantially from the seawater liquid, the seawater may need to be subjected to the above distillation process more than once. Therefore, most of the seawater passing through the membrane chamber may be returned to the storage tank 10 via the product stream 15 to further perform the above treatment until all of the moisture has been substantially removed from the seawater. When the water vapor in the vapor stream 17 is condensed into a water liquid, the latent heat of condensation in the downstream heat exchanger 12 is given off. This © heat of condensation is exchanged with the seawater entering the stage 由 from the storage tank 10 through the feed stream 11Β. The condensed water, which is condensed from the water liquid stream 28, is substantially water-free. The function of the vapor stream 17 is similar to the hot fluid stream 16 Α, i.e., the vapor stream 17 Α provides thermal energy to heat the seawater passing through the heat exchanger 10. For the sake of convenience, by heating seawater to evaporate water to g water vapor, and subsequently obtaining a plurality of repeated condensation heats, the other stages B, C, ..., η are not described. However, it should be understood that the stages C, C, ..., η have the same operational principles as the above stages. It should further be understood that the process of obtaining condensing heat from the upstream heat exchange module and then heating the obtained condensing heat into another downstream seawater feed of the hollow fiber module can be repeated any number of times until the last downstream repeat Is the display phase η. 20 201023960 In stage η, vapor stream 17n is a by-product of the thin film steaming process 100 referred to herein and may be further processed or utilized for other uses (not depicted herein). Please refer to Fig. 2, which is a second embodiment of the present invention. Fig. 2 has the same technical features as those of Fig. 1, and is denoted by the same numeral, but with a symbol. Figure 2 is an energy-saving film steaming process 100', including stages A, B, C, ..., n, and then ❹ Α > represents the first stage, Β, represents the second stage, and η , representing the nth stage. Each stage includes a storage tank containing seawater (10Α', 10Β'' 10C', ..., ι〇η,), heat exchangers (12Α, 12Bf, 12Cf, ..., 12η') and membrane modules. (14α, 14Β, 14C', ..., 14η'). Each of the film modules (ΐ4Α, 14Β, 14C, ..., 14n) has a subset of a plurality of hollow fiber membranes (not shown) disposed therein. Stages A', Β, C, ... , η, and its constituent members are the same as the process 100 shown in Fig. 1. _ In the process 100', water is evaporated from the seawater liquid, and then the obtained heat of condensation is used to heat the seawater in the downstream stage, The process is the same as described in Stage 第 in Figure 1. In addition to the heat of condensation, additional heat sources are provided to each stage (B, C7, ..., ι〇) (12Β, 12CT,...,12ι 〇, as described below. Referring to the stage, the temperature of the hot fluid is higher than the temperature of the seawater in the feed stream 11Β', and the hot fluid flows into the heat exchanger 12 via the hot fluid stream 16Β4. The hot fluid stream is 16 Β, as a supplement The heat source 'is used for 21 201023960 to heat the seawater flow 11B through the heat exchanger 12B<~ When the thermal energy present in the hot fluid stream 16Bf is transferred to the seawater flow 11B4, the hot fluid in 16B< is cooled to a lower temperature, and Leaving the heat exchanger via cooling fluid stream 18B' 12B% Referring now to the seawater liquid remaining in the membrane chamber 14A' after evaporation of the water, it may be returned to the storage tank 10A' via the product stream 15A' for the next process. The conduit 20A' allows the seawater in the storage tank 10A' to communicate. To the storage tank 10B^ in this way, the seawater in the thin film distillation process 1〇 (the stage A' of the seawater can be further distilled in the stage K. Similarly for the stage Β, ..., (n-iy, Each storage tank (10B, ..., 10 (n-iy) is fluidly coupled to its downstream storage tanks (10CT, ..., 1〇1〇) so that the seawater in each stage can be further distilled in the downstream stage. Referring to Fig. 3, which is a third embodiment of the present invention, which has the same technical features as those of Fig. 1, and is shown by the same numeral table, but with a symbol (〃). Stage A" is an alternative embodiment of Stage V in Figure 2. Stage A includes a storage tank 10A containing seawater, heat exchangers 12A and 12B, and membrane modules (14A"-1, 14A "-2, ..., 14A"-n). The elements in stage A are the same as those in stage V of Figure 2 above. The components used herein are denoted by the same reference numerals, but with a symbol Γ). 22 201023960 In this embodiment, a plurality of thin film modules (14A"-1, 14A";-2,...,14A"-n). In addition, the film chamber in the thin film module (14A"-1, 14A, -2, ..., 14A, '-n) further comprises at least one additional discharge tube With the bypass tube (26Α"-1, 26Α, '·2, 26A,,, 3,...)' to allow any of the film modules (14A"-1, 14A"-2,...,14A'fn) The seawater bypasses any of the downstream modules. The advantage of this setup is that if any of the membrane modules fails, the seawater can still bypass the faulty module and continue the steaming process. The seawater leaving from the heat exchanger 12A enters the first film module 14A via the conduit 24A. It must be understood that the film module 14A〃-1 has the same operation as the film module 14A in Fig. 1 above. principle. After distillation through the membrane module 14A〃-1, the remaining seawater flows through the conduit 24A〃-1 to the membrane module 14A〃-2 for further steaming. Q It should be understood that this process can be repeated any number of times until the last downstream module 14A 〃-η, where the remaining seawater can be collected via conduit 24Α〃-η or via a recycle stream 15Α〃 to the feed stream 11Α Carry out further processes. Figure 4 is a thin film distillation process 400, which corresponds to the stages Α, Β' and C' of the thin film distillation process of Figure 2, and further includes programmable logic controllers (PLCs) (30 Å, 30 Å). The components of Fig. 4 are the same as those of Fig. 2 except for the components marked with the asterisk 23 201023960 (*). These programmable logic controllers (30A, 30B) are respectively connected to the vapor streams (17A*, 17B*) of the respective stages, and the temperature inside them is measured. The temperatures of the vapor streams (17A*, 17B*) are indicated below by T17A and Ti7B, respectively.

Tset-30A is the temperature input to the programmable logic controller 30A, where Tset_30A is the minimum temperature required to heat the seawater passing through the heat exchanger 12B*. After comparing the measured temperature T17A with the © set temperature Tset-3QA, the programmable logic controller 30A controls the valves (V17A, V32A, and V16B) located in the vapor stream 17A*, the bypass stream 32A, and the hot fluid stream 16B*, respectively. ) on and off. Detailed control will be further described below. Because the heat source is solar, the heat that the heat source provides every day may change over time. For example, the heat in the morning and evening is less than at noon. Thus, the thermal energy provided by the solar source varies over time, meaning that during each stage of process 400, its thermal load needs to be varied depending on the particular energy load obtained at any particular time. For example, the higher the temperature of the vapor stream 17A* (i.e., typically during noon), the more heat energy is used to condense the water vapor therein. Therefore, if the temperature T17A is higher than the temperature Tset-30A', it is not necessary to provide a supplemental heat source via the hot fluid stream 16B*. Thus, when the measured temperature T17A is higher than the set temperature Tset_30A, the valve V 7A is opened, and the valves V32A and V16B are closed, and 24 201023960 flows to the heat exchanger 12B* in the stage with the water vapor in the vapor stream 17A*. . On the other hand, when the measured temperature T17A is lower than the set temperature Tset-3〇A (i.e., usually during morning or evening), it is indicated that the heat energy in the vapor stream 17A* is insufficient. Therefore, the valve ν17 Α is closed and the valve V32A is opened, so the water vapor in the vapor stream 17A* does not flow to the heat exchanger 12B* in the stage K. The water vapor at the vapor φ flow of 17 Α* is a by-product which leaves the membrane module 14 Α* via the bypass flow 32 。. In addition, valve V16B is opened to provide a supplemental heat source introduced through hot fluid stream 16B* into heat exchanger 12B* to enable it to heat the seawater passing through feed stream 11B*. Similarly, the programmable logic controller 30B is connected to the vapor stream 17Β* of stage K and controls the opening and closing of the valves (V17B, V32B and Vi6C) after determining the temperature of the vapor stream 17Β* (denoted as Τΐ7Β). Figure 5 is a calculus diagram detailing the operation of the programmable logic controller (30A) of Figure 4.

As described above, the programmable logic controller 30A is programmed to control the opening and closing of the valves (V! 7A 'V32A and V16B). When temperature T

When 17A is higher than Tset_3〇A, the programmable logic controller 30A transmits an electronic signal that opens the valve Vi7A and closes the valves V32A and Vi6B. On the other hand, when the temperature T17A is lower than Tset_3〇A, the programmable logic controller 30A transmits an electronic signal for closing the valve V 17A and opening the valves V32A and Vi6B. 25 201023960 , 6 ® — Controlled film evaporation process, which corresponds to phase A and phase B of the steaming process shown in Figure 1, and the progress includes a programmable logic controller (pLc) (shed) and a plurality of Heat exchangers connected in series (12B*-1, 12B_2, ··· ' 12B*-N). Except for the components marked with a double asterisk (**), all other components in Figure 6 are identical to the i-th image. During operation, one or more heat exchangers, 12B-2, ..., 12B*-N) may be used to heat the seawater feed UB*. The programmable logic controller 40B measures the flow (38-1, 38-2, liquid water) leaving the heat exchanger (12BM, l2B*-2, ..., 12B*-N), respectively.

Water vapor of the mixture in ···, 38-(N-l))

The temperature ' thus controls the seawater feed 11B* to flow through these heat exchangers (12BSIM, 12B*_2, ..., 12B*_N) via the open valve v11B' or via a bypass flow (5 (M, 50-2, ..., 50·(Ν·1)) Bypassing one or more heat exchangers (12Β*-1, 12Β*-2,..., 12Β,Ν). Liquid flow (38-b 38-2,... The temperature of 38-(Ν-1)) is represented by Ding 38-1, Τ38-2, ..., Τ38-(Ν-1) in the following. Controlling the flow of seawater feed 11Β** is based on the measured The temperature y ..., T38_(ni). The measured temperature T3W, 26 201023960 Τ 38-2, ..., the paw (7) - is the individual set temperature Tset_4 〇 B input into the programmable logic controller 40B. Compared. The set temperature Tset-40B is the minimum temperature required to heat the seawater passing through each heat exchanger (12B*-1, 12B*_2, ..., 12B*-N). The opening and closing of the valves (Viib, V50-I, V50-2, ..., V5〇-(Nl)) can help the seawater feed 11B** flow through the heat exchanger (12Β*·1, 12Β*· Control of 2,..., 12B*-N), and the valves φ are respectively fed along the seawater 11B** and the bypass flow (50-1, 50-2, ..., 50(N-1) ), which will be further explained below. All valves (V11B, V5M, V5O-2, ..., V5〇-(N-1)) are closed unless otherwise stated below. During operation, the programmable logic controller 40B measures the temperature of the liquid stream 38-1 exiting the heat exchanger 12B*-1. If the measured temperature does not exceed the set temperature Tset_4GB, the programmable logic controller 40B transmits an electronic signal that opens the valve V5 (M) because φ is that there is not enough heat in the flow 38-1 to operate the remaining heat exchanger ( 12Β*·2,...,12B*-N). Therefore, the feed 11B** flows directly into the heat exchanger 12B*-1, bypassing the remaining heat exchanger via the feed stream 50-1 (12B*-2) On the other hand, if the measured temperature T3H is higher than the set temperature Tset-4〇B, the programmable logic controller 40B transmits an electronic signal that opens the valve V11B, and the programmable logic controller 40B The temperature of the fluid leaving the next heat exchanger 12B*-2 is measured. 27 201023960 Similarly, if the measured temperature Τ38_2 does not exceed the set temperature Tset-4〇B, the programmable logic controller 40 transmits the electrons that open the valve V50-2. The seawater feed 11B** flows directly into the next heat exchanger 12B*-2 via the feed stream 50-2 and then flows into the heat exchanger. Similarly, if the measured temperature T38_2 is higher than the set temperature Tset-40B , the programmable logic controller 40B transmits an electronic signal that opens the valve V11B. And the programmable logic controller 40B measures the temperature of the fluid leaving the next heat exchanger (12B*-3, not shown). As described above, if the flow enters the heat exchanger 12B*-N 38-(Ν-1 When the temperature is not higher than the set temperature Tset_4〇B, the programmable logic controller 40B transmits an electronic signal that opens the valve V 50-(Ν-1). This is to make the seawater feed 11B** via the feed stream 50- (Ν-1) flows directly into the heat exchanger 12B*-(N-1) (not shown), and then flows into the heat exchanger (12B*-(N-2) (not shown), ..., 12B*- 2, 12B*-1), but bypassing the heat exchanger 12B*-N. If the measured temperature T 38-(Ν-1) is higher than the set temperature Tset_4〇B, the programmable logic controller 40B transmits the opening valve V11B. The electronic signal, that is, the seawater feed 11B* continuously flows through all the heat exchangers (12B*-N, ..., 12B*-2, 12Β*·1) connected in series to each other. Therefore, the series are connected in series with each other. The number of heat exchangers can be changed according to whether there is enough heat energy (such as temperature as an indicator) 201023960 to heat the seawater feed. Figure 7 is the calculation of Figure 7 of Figure 7 in Figure 6. Unless otherwise stated, the valve Μν11Β, ν5_ν5... 乂 关闭 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 50 3" temperature: 38: two 1! η is Bu 2, ........ If the measured temperature is back; Also, the floppy Tset_4〇B, the programmable logic controller 4〇β transmits the electronic signal of the valve V11B. On the other hand, if the measured temperature is lower than the set temperature Tset_4 (10), the programmable logic controller 40B transmits an electronic signal that turns on the valve V5", where η is 1, 2, ..., Nd. According to the above figure 6 and In the description of Figure 7, it is understood that the programmable logic controller 40B is capable of adjusting the total surface area of the heat exchanger 'this is required for the thin film distillation process 600. Example 1: Concentration by a multi-stage thin film distillation process using the above separation system Sodium chloride solution. Each stage of the thin film distillation process comprises a film evaporation module and a heat exchanger unit. The feed liquid is a sodium chloride solution 'the sodium carbonate solution to be concentrated and initially 6% concentrated The flow rate is 1000 kg / day. 29 201023960 The external heat source is only for the feed liquid in the first stage of the thin film distillation module. In this example, the external heat source is the heat energy converted from the power consumption. The thermal energy provided is 5x108 Joules/day. . . . The deserted sodium chloride solution passes through the heat exchanger and is heated by an external heat source. This solution then enters the thin film distillation module, the solution. The water in the form is evaporated to form water vapor. The thin film distillation module comprises the film chamber as described in Fig. 1 above. The film is made of polypropylene, which has a diameter of 0.4 to 0.6 mm. An® is provided with approximately 60,000 to 80,000 fibers. The vapor evaporated from the first stage of the membrane steam module is removed via a heat exchanger unit for heating the feed liquid in the second stage of the membrane distillation module to A temperature of about 65 ° C. The feed liquid in the second stage is the residual solution that has not evaporated in the first stage. After heating the feed liquid, the water vapor is condensed into a water liquid. The amount of water evaporated from the first stage is 19〇kg. ❹ Similarly, the water vapor evaporated from the second stage of the thin film distillation module is taken out via the heat exchanger assembly to heat the feed liquid in the third stage of the film evaporation module to about 55 art. The temperature of the water evaporating from the second stage is 18 〇 kg. The water vapor evaporated from the third stage of the thin film distillation module is taken out to 'heat the feed liquid in the fourth stage of the thin film distillation module to Temperature of about 45 ° C The amount of water evaporated from the third stage is 30 201023960 170 kg. The water vapor evaporated in the fourth stage is cooled by room temperature water. The amount of water evaporated from the fourth stage is 160 kg. The post-drunk concentration of the gasified sodium solution is 20 %. In a single-stage process, the thermal energy consumption per ton of moisture is 2.63x106 joules, the two-stage process is 135xl 〇6 joules, the three-stage process is 〇.93X106 joules, and the four-stage process is 0.71x106 joules. Therefore, the four-stage process can reduce the heat consumption of the separation system by 73% compared to a single process. Applicability: It will be understood that the system disclosed in the present invention separates the feed by thin f?, Volatile components in solution. Advantageous: The hollow fiber thinner used for degassing is compared to the polymer plate, and the surface area is much larger. This increases the throughput of the thin film distillation to achieve - better process efficiency and lower cost. The individual stages of the operation of the group are different. It is advantageous that the operating parameters of the line can be individually controlled. It is to be understood that the 'separation of the evaporation system from the feed solution is::, the fork-changing device allows the borrowing of the mileage. energy. The advantageous 31 201023960 is 'to greatly reduce the overall thermal energy consumption of the separation system. It will be appreciated that the heat exchange device comprises at least one heat exchanger. Advantageously, the number of heat exchangers can be selected to recover as much as possible the latent heat of the vaporized volatile constituents, thereby increasing the efficiency of the separation system. More advantageously, the energy efficiency design of the disclosed separation system overcomes the major problems of conventional thin film distillation processes. While a reasonable effort has been made to describe an equivalent embodiment of the present invention, it will be apparent to those skilled in the art after reading the above disclosure. Therefore, any equivalent modifications or alterations to the spirit and scope of the invention are intended to be included in the scope of the appended claims. BRIEF DESCRIPTION OF THE DRAWINGS The accompanying drawings illustrate a disclosed embodiment and are intended to explain the principles of the disclosure. However, it is to be understood that the drawings are only intended to be illustrative, and are intended to limit the invention. A schematic diagram of a thin film evaporation process for exposing the embodiment; a second schematic diagram of a thin film distillation process of another disclosed embodiment; the first figure is a stage of the film evaporation process shown in FIG. - Example; Fig. 4 is a diagram of the control of the thin film distillation process shown in Fig. 2, 201023960, and Fig. 5 is the programmable logic controller shown in Fig. 4. (calculation diagram of (PLC); Figure 6 is a control diagram for controlling the thin film distillation process shown in Fig. 1; and Fig. 7 is a programmable logic controller (PLC) shown in Fig. 6 A calculation chart. [Main component symbol description] 100: Energy-saving thin film distillation process; 10A, 10B, 10C, 10n: storage tank; 11A, 11B, 11C, 11n: feed stream; 12A, 12B, 12C, 12n: heat exchanger; 13Β, 13C, 13η: hot sea water flow; 14Α, 14Β, 14C, 14η: thin film module; 15Α, 15Β, 15C, 15η: product flow; 16Α: hot fluid flow; 17Α, 17Β, 17C, 17η: vapor flow; : cooling fluid flow; 28Α, 28Β, 28C: water liquid flow; 1〇 (Τ: energy-saving thin film distillation process; 10Α', 10Bf, 10CT, 10nf: storage tank; llAf, 11B', llCf, llnf: feed stream; 12Af, 12Bf, 12CT, heat exchanger; 33 201023960 13A, 13B, 13C, 14A, 14B, 14C, 15A, 15B, 15C, 16A, 16B, 16C, 17A , 17B, 17C, 18A, 18B, 18C, 20A, 20B, 20C, 28A, 28B, 28C,: 10A 〃: storage tank; 11A": feed stream;

13η, hot sea water flow; 14η, thin film module; 15η, product flow, 16nf hot fluid flow; 17η, vapor flow; 18η, cooling fluid flow 20η, conduit water liquid flow; 12A", 12B": heat exchanger; 13A〃 : hot sea water flow; 14A"-1, 14A"-2, 14A,, -n: thin film module; 15 A〃: product flow; Ιό A": hot fluid flow; 17A"-1, 17A"-2, 17A "-n: vapor flow;

18A〃: cooling fluid flow; 24A", 24A"·24Α”·2, 24Α"-(η-1), 24Α”·η: conduit; 26Α"-1,26Α”-2,26Α"-3 : Bypass tube; 28Α〃: water liquid flow; 400: thin film distillation process; storage tank; feed stream; heat exchanger; hot sea water flow; 10Α*, 10Β*, 10C*: 11Α*, 11Β*, 11C*: 12Α* , 12Β*, 12C* : 13Α* ' 13Β* > 13C* : 34 201023960 Thin film module; product flow, hot fluid flow, vapor flow; cooling fluid flow; 14A*, 14B*, 14C* 15A*, 15B* , 15C* 16A*, 16B*, 16C* 17A*, 17B*, 17C* 18A*, 18B*, 18C* 28C*: water liquid flow; 30A, 30B: programmable logic controller; 32A, 32B: bypass flow ;

38: liquid flow; 500: algorithm; 600: thin film distillation process;

Vl7A, V32A, Vi6B, V17B, V32B, Vi6C: valve;

Tl7A, Ti7B: temperature of the vapor stream; 10A**, 10B**: storage tank; 11A**: feed stream; 12A*, 12B*-2, 12B*-N: heat exchanger; 13A**, 13B**: hot sea water flow; 14A**, 14B**: thin film module; 15A**, 15B**: product flow; 16A**: hot fluid flow; 17A**, 17B**: vapor flow; A**: cooling fluid flow; 40B: programmable logic controller; 38-1, 38-2, 38-(Ν-1): liquid flow; 50-1, 50_2, 50_(N_1): bypass flow; 201023960 Τ38_ι, T38-2, T38-(n-1): measured temperature; V50-I, V50-2, V5〇-(Nl): valve; and 700: algorithm.

36

Claims (1)

201023960 VII. Patent application scope: 1. A separation system for separating volatile components from a feed solution, comprising: a plurality of hollow fiber membranes having selective permeability and allowing the volatile components in a volatile phase to pass And substantially preventing the passage of the feed solution; a heat source having the ability to heat the feed solution on one side of the hollow fiber membrane to produce the volatile phase through the hollow fiber membrane; and a heat exchange device, It condenses the volatile component and is configured to obtain a heat of condensation that is thermally coupled to the heat source, thereby driving or supplementing the heat source by the heat of condensation. 2. The separation system of claim 1, wherein the hollow fiber membrane is hydrophobic. 3. The separation system according to claim 2, wherein the hydrophobic aqueous hollow fiber membrane is composed of a hydrophobic polymer. 4. The separation system of claim 1, further comprising means for varying the thermal duty of the heat exchange device based on the heat duty of the heat source. 5. The separation system of claim 4, wherein the heat exchange device comprises a plurality of heat exchangers, and wherein the means for varying the heat load of the heat exchanger comprises changing the heat exchanger The number of devices that have the ability to receive this volatile 37 201023960 component. 6. The separation system of claim 1, further comprising a plurality of hollow fiber modules, each of the hollow fiber modules including a chamber having a subset of the plurality A hollow fiber membrane is disposed therein. 7. The separation system of claim 6, wherein the plurality of hollow fiber modules are in fluid flow in series with one another. 8. The separation system of claim 6, wherein the thermal switching device comprises a plurality of heat exchangers, wherein at least one of the heat exchangers is disposed in an upstream hollow cavity module in fluid flow in series with each other A downstream hollow fiber module. 9. The separation system of claim 8, wherein the heat exchanger disposed between the upstream hollow fiber module and the downstream hollow fiber module is configured to obtain the upstream hollow fiber module. The heat of condensation of the volatile phase and the resulting heat of condensation are used to heat the feed solution into the downstream hollow fiber module. </ RTI> </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> </ RTI> <RTIgt; The separation system of claim 1, wherein the heat source is the separation system described in item 1, wherein the source of heat is caused by the heat source. The heat source comprises at least one of (1) a waste source, (8) a solar heat source, and (iii) a geothermal source. A separation system for separating volatile components from the feed solution, comprising: a plurality of hollow fiber membranes, Selecting permeability and allowing passage of the volatile component in a volatile phase to substantially prevent passage of the feed solution; a plurality of hollow fiber modules each having a closed chamber and a water inlet ( Inlet), the chamber has a subset of the plurality of hollow fiber membranes extending therethrough, the water inlet is a side of the feed solution to the plurality of hollow fiber membranes; and a plurality of heat exchangers a condensing heat in fluid communication with the volatile component to obtain a condensed heat of the volatile component, the plurality of heat exchangers having the ability to be thermally coupled to a heat source, thereby utilizing the cold Driving the heat source or supplement. 14. The separation system of claim 13, wherein the plurality of hollow fiber modules are in fluid flow in series with one another. The separation system of claim 14, wherein the feed solution is capable of bypassing one or more of the plurality of hollow fiber modules. 16. The separation system of claim 13, wherein the plurality of hollow fiber membranes consist of a hydrophobic polymer membrane. 17. The separation system of claim 16, wherein the hydrophobic polymer membrane is selected from the group consisting of polyvinylidene chloride, polypropylene, polytetrafluoroethylene, and polyethylene. 39 201023960 18. The separation system described in the patent application _13 further includes a monitoring device that is coupled with the heat source to monitor the heat duty. 19. The separation system of claim 18, further comprising: a control device in combination with the monitoring device and the plurality of exchangers 2 wherein the control device has a determination based on the monitored amount of heating The ability to use the number of heat exchangers. 2〇. A process for separating volatile components from a feed solution, the step of heating the feed solution by a heat source; and when there is a pressure difference between the two sides of the plurality of hollow fiber membranes, passing the feed solution One side of the plurality of hollow fiber membranes, wherein the volatile component in a volatile phase is formed on one side of the hollow fiber membrane, and the volatile component is located on the opposite side of the feed solution; condensing the volatile phase The volatile component therein, thereby obtaining a heat of condensation; and using the heat of condensation, thereby driving or supplementing the heat to the heat source. 21. The process of claim 20, further comprising a step of varying the flux of the heat source. 22. The process of claim 21, further comprising the steps of: using a plurality of heat exchangers to obtain the heat of condensation; and 201023960 changing the plurality of heats according to a variable amount of heat of the heat source The thermal duty of the exchanger. 23. The process of claim 20, further comprising the steps of: providing a plurality of hollow fiber modules, each of the hollow fiber modules including a chamber having a sub-chamber The plurality of hollow fiber membranes are disposed therein, the plurality of hollow fiber modules are fluidly flowing in series with each other; and the feed solution is heated individually into each of the plurality of hollow fiber modules. 41