WO2018082199A1 - 梯度亚沸蒸馏器 - Google Patents

梯度亚沸蒸馏器 Download PDF

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Publication number
WO2018082199A1
WO2018082199A1 PCT/CN2017/000648 CN2017000648W WO2018082199A1 WO 2018082199 A1 WO2018082199 A1 WO 2018082199A1 CN 2017000648 W CN2017000648 W CN 2017000648W WO 2018082199 A1 WO2018082199 A1 WO 2018082199A1
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WIPO (PCT)
Prior art keywords
liquid
pipe
distiller
evaporation surface
tube
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Application number
PCT/CN2017/000648
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English (en)
French (fr)
Inventor
刘飞
Original Assignee
刘飞
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 刘飞 filed Critical 刘飞
Priority to US16/346,196 priority Critical patent/US20200055745A1/en
Priority to JP2019544955A priority patent/JP2019533578A/ja
Priority to EP17866690.5A priority patent/EP3536390A4/en
Publication of WO2018082199A1 publication Critical patent/WO2018082199A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/06—Evaporators with vertical tubes
    • B01D1/065—Evaporators with vertical tubes by film evaporating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/043—Details
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/30—Accessories for evaporators ; Constructional details thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/007—Energy recuperation; Heat pumps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/008—Liquid distribution
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
    • B01D5/0012—Vertical tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/0075—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with heat exchanging
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/009—Collecting, removing and/or treatment of the condensate
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/045—Treatment of water, waste water, or sewage by heating by distillation or evaporation for obtaining ultra-pure water
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/048—Purification of waste water by evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/08—Thin film evaporation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the invention relates to the field of liquid distillation purification or concentration, in particular to a liquid distillation purification and concentration device and method.
  • a gradient sub-boiling distiller characterized by comprising at least one condensation tube, at least one evaporation surface, a heating device, a liquid distributor, a tail liquid tank, a condensate tank, a tail liquid pipe, a liquid inlet pipe, a condensate pipe,
  • the outer casing wherein one end of the heating device communicates with the liquid distributor, the other end communicates with the condenser tube, one end of the evaporation surface receives the liquid distributor, and the other end is provided with a tail liquid tank, the tail liquid tank communicates with the tail liquid pipe, and one end of the condensation pipe is
  • the inlet pipe communicates with the other end communicating with the heating device, and the condensate tank is located at one end of the condenser pipe and communicates with the condensate pipe.
  • the gradient sub-boiling distiller is characterized in that: the distiller further comprises a pump, and the inlet and the outlet of the pump are respectively communicated with the tail pipe and the inlet pipe through the circulation pipe.
  • the gradient sub-boiling distiller is characterized in that: the distiller further comprises a heat exchanger, and the heat exchanger is disposed on the tail liquid pipe, the condensate pipe and the liquid inlet pipe.
  • the gradient sub-boiling distiller is characterized in that: the circulation pipe further comprises a cooling device.
  • the gradient sub-boiling distiller is characterized in that the inlet pipe is connected to a pipe between the condensing pipe and the heating device or a pipe between the liquid distributor and the heating device.
  • the gradient sub-boiling distiller is characterized in that the distiller further comprises a device for periodically moving the evaporation surface relative to the condensing tube to the evaporation surface.
  • the gradient sub-boiling distiller is characterized in that the distiller further comprises a gas generator, a gas storage tank, an air extractor or a compressor communicating with the outer casing through a pipe.
  • the gradient sub-boiling distiller is characterized in that the distiller further comprises a fan, and the inlet and the outlet of the fan are in communication with the outer casing.
  • the gradient sub-boiling distiller is characterized in that: the condensing tube is made of a polymer material or a composite material thereof, and has a vertical partition inside, and the holes separated by the partitions are connected to the liquid passages at both ends of the condensing tube.
  • the surface of the condensing tube has a protrusion; the evaporation surface is arranged with the condensing tube, and the protrusion of the surface of the condensing tube supports and compresses the evaporation surface; the protrusion of the surface of the condensing tube comprises: a columnar or a tapered protrusion; a columnar tapered protrusion; a longitudinal strip-shaped protrusion; a side surface having a longitudinal strip-shaped projection at one end of the evaporation surface lower than the flow guiding groove at one end of the condensation surface.
  • the gradient sub-boiling distiller is characterized in that the evaporation surface is omitted, and the raw material liquid is dripped or ejected by the liquid dispenser.
  • the raw material liquid enters the condensing pipe and flows from one end of the condensing pipe to the other end.
  • the liquid vapor condenses on the outer surface of the condensing tube, and the heat of condensation causes the temperature of the raw material liquid in the tube to continuously rise, and finally the liquid enters the heating device, is further heated, and the temperature rises.
  • the heated liquid is distributed to the evaporation surface and flows to the other end of the evaporation surface, while continuously evaporating, the temperature is continuously lowered, and the liquid vapor is condensed on the condensation tube, so that the liquid in the condensation tube is continuously heated. Since the water flow rate on the evaporation surface is equal to the water flow rate in the condensation tube, the temperature at which the high temperature liquid flows from one end of the evaporation surface to the other end is the temperature at which the liquid rises after passing through the condensation tube.
  • 20 ° C tap water enters the condensing pipe from the inlet pipe, is preheated to 90 ° C in the condensing pipe, and is finally heated to 100 ° C in the heating device, then distributed to the evaporation surface through the water distributor, and begins to evaporate, with
  • the temperature of the water flowing to the bottom end of the evaporation surface is continuously lower, and the final drop amplitude is basically equal to the increase of the water temperature in the condenser tube (the temperature drop is basically caused by evaporation and heat dissipation, and the contact heat transfer ratio is very small), and the temperature drop is 30 ° C. discharge.
  • the externally supplied heat is to heat the water by 10 ° C, and the corresponding heat of the evaporated (or condensed) water vapor is to lower the water by 70 ° C, so the energy efficiency of the system is about 7 effects. If the influent flow rate is adjusted so that the water is preheated to 95 ° C, and the temperature is lowered to 25 ° C after evaporation from the evaporation surface, the energy efficiency of the device is about 14 effects.
  • the liquid can be evaporated at a higher temperature, so that the final temperature after evaporation of the liquid is increased.
  • a heat exchanger is added to the system for heat exchange between the tail liquid, the condensate and the feed liquid.
  • the tail liquid is recovered into the circulation by the pump, that is, the unvaporized liquid flowing from the evaporation surface is partially collected by the tail liquid tank, and then pumped into the circulation pipeline by the pump, partly by The tail pipe is discharged while the appropriate amount of raw material liquid is replenished by the inlet pipe.
  • the mixed liquid is mixed into the circulating liquid to lower the temperature of the circulating liquid, so that the vapor evaporated on the evaporation surface can be condensed when entering the condenser again.
  • the circulating liquid can be cooled to increase the temperature difference between the evaporation surface and the outer wall of the condenser.
  • the temperature difference between the evaporation surface and the condensation tube wall may be lowered.
  • the tail liquid and the condensate may be exchanged with the raw material liquid entering the apparatus to preheat the raw material liquid entering the apparatus.
  • the newly added raw material liquid can be directly introduced from the pipe between the heating device and the liquid distributor or the pipe between the heating device and the condensation pipe, and the heating device can not heat the circulating liquid.
  • the circulating liquid evaporated from the evaporation surface can be cooled.
  • the evaporation surface is periodically moved relative to the condenser tube to drive the gas movement between the evaporation surface and the condensation tube, thereby promoting the evaporation-condensation process and increasing the yield. It is possible to connect a moving device to the evaporation surface, which moves the evaporation surface periodically. For example: rotation, reciprocating motion in a direction perpendicular to the surface of the condenser, and reciprocating motion in a direction parallel to the surface of the condenser.
  • the evaporation surface is fixed on a shaft, and the shaft is connected with the motor and the crankshaft connecting rod, and the motor drives the evaporation surface to reciprocate;
  • the evaporation surface is formed into a cylindrical shape, the center is provided with a shaft, the shaft is connected to the motor, and the condensation tube is distributed on the evaporation surface.
  • the motor drives the evaporation surface to rotate; at the same time, a plug such as a twist band or a spring can be arranged on the evaporation surface to increase the gas movement.
  • the gradient sub-boiling distiller may be provided with a gas generator, a gas storage tank, an air extractor or a compressor to change the atmosphere or pressure inside the outer casing.
  • a gas generator to generate the required gas or use a gas storage tank to store the required gas, and fill it into the casing through a pipe, and it can be continuously filled or intermittently charged.
  • a tank containing nitrogen is used to communicate with the outer casing, and the outer casing is filled with nitrogen.
  • the device when the raw material liquid is unstable in the air, the device may be filled with an inert gas such as nitrogen, argon or carbon dioxide or a mixed gas thereof; in order to reduce the content of oxygen or carbon dioxide in the condensate, nitrogen may be charged; in order to increase the yield or energy efficiency It can be filled with a gas such as hydrogen or helium.
  • the gas to be charged may be a mixed gas of various gases or a mixed gas containing raw material liquid vapor.
  • the pressure of the gas inside the gradient sub-boiling distiller may be less than atmospheric pressure to accommodate cryogenic distillation or concentration. For example, it can be from 0.01 to 0.9 atm. At this time, on the one hand, it can be realized by adding an air extractor to remove the gas from the system, or by increasing the airtightness of the system, maintaining a lower air pressure after pumping, or both.
  • the gradient sub-boiling distiller may also include a compressor to make the device
  • the partial pressure is greater than atmospheric pressure, which increases the final heating temperature of the liquid to improve energy efficiency. For example, increase the internal pressure of the device so that the water can be heated to 120 ° C
  • the gradient sub-boiling distiller may comprise a fan, preferably a cross-flow fan.
  • the air inlet and outlet of the fan are respectively connected to the outer casing. When the fan is working, the air is sucked from the outer casing and then blown into the outer casing to cause the flow thereof to promote the evaporation and condensation process, thereby improving the output or energy efficiency.
  • the axis of the cross-flow fan impeller is parallel to the evaporation surface, reducing the mixing of the upper layer of high temperature gas and the lower layer of low temperature gas.
  • the evaporation surface of the gradient sub-boiling distiller and the condensation tube may be provided with means for fixing the evaporation surface or separating the evaporation surface from the condensation tube, including a bracket, a pillar, etc., and preferably contacting the condensation tube.
  • the part is higher than the part that is in contact with the evaporation surface.
  • a spring fixed to the evaporation surface or the condensing tube an L-shaped object fixed at one end to the condensing tube, a columnar body, and a cross bar (fixed to the condensing pipe by the struts perpendicular to both ends thereof, the crossbar is parallel to the surface of the condensing pipe
  • the horizontal rod is horizontally disposed and the contact portion with the condensing tube is higher than the crossbar
  • the inverted V-shaped U-shaped bracket (where the V-shaped and U-shaped ends are respectively in contact with the evaporation surface and the condensing tube, respectively)
  • the material is not higher than the contact portion, the raw material liquid does not flow to the surface of the condenser tube, or the strip wire is wound into a V-shaped or U-shaped bracket.
  • the evaporation surface of the gradient sub-boiling distiller can be omitted, the liquid is only distributed, dripped or sprayed by the liquid dispenser, the liquid evaporates during the falling process, and the evaporated tail liquid falls into the tail liquid tank.
  • the liquid distributor is a tube with a plurality of small holes, the liquid drops from the small holes, and evaporates and falls into the tail liquid tank.
  • the gradient sub-boiling distiller may have more than one or only one of the tail liquid tank and the condensate tank, that is, each evaporation surface (condensation tube) may be equipped with a tail liquid tank (condensate tank), or A plurality of evaporation surfaces (condensation tubes) share a tail tank (condensate tank).
  • the condensing tube of the gradient sub-boiling distiller can be made of a polymer material or a composite material thereof, and the inside can have a longitudinal partition plate, and the separator functions to increase the strength of the condensing tube and save materials.
  • the surface of the condensing tube has a convex surface to support and fix the evaporation surface.
  • the protrusions include, but are not limited to, columnar or tapered protrusions; inclined columnar or tapered protrusions; longitudinal rows and rows of protrusions; and longitudinal strip-shaped protrusions with guide grooves on the sides.
  • the protrusions may be columnar, such as a cylinder, a square column, a prism, etc., and the columnar protrusions may be inclined with respect to the surface.
  • the condenser tube When the condenser tube is placed vertically, the top end of the columnar protrusion is lower than the base portion, so that the raw material liquid on the evaporation surface The condensate does not flow upward, and the condensate generated on the columnar projection or the condensate flowing to the columnar projection on the surface of the condensing tube also cleans the columnar projection and finally flows into the raw material liquid without contaminating the condensate.
  • the protrusions may also be longitudinal strips, for example, rectangular, semi-circular, triangular strips, etc., with the top end and The evaporation surface contacts, supports the evaporation surface, and the base is connected to the surface of the condensation tube.
  • the side surface may have a flow guiding groove inclined to the condensation surface, and the one end of the flow guiding groove at the evaporation surface is lower than the end at the condensation surface.
  • the guide groove may be: a groove of the convex surface, a groove formed on the side of the protrusion and a groove formed on the side of the protrusion, and a gap formed after the protrusion is cut (or expressed as a gap between the protrusion and the protrusion) ),
  • the liquid dispenser is a device for flowing a liquid to the evaporation surface, and it is preferable to uniformly distribute the liquid on one end of the evaporation surface. It may be only a length of tube and nozzle, the liquid flowing into or falling onto the evaporation surface through the nozzle of the tube, or a tube having a plurality of small holes in the wall, or a tube having a longitudinal slit in the wall.
  • the main function of the condensing pipe according to the present invention is to condense steam by its outer surface, heat transfer of the pipe wall, and at the same time, its internal space allows liquid to pass through, and thus the condensing pipe is not limited to a pipe having a long diameter and a similar diameter.
  • the shape of the tube wall may be any shape as long as it can be used for heat transfer and condensation, and may be irregular or various shapes such as a curved surface, a flat surface or a surface having fins.
  • the cross section of the tube may be a circular tube, a rectangular shape, a long strip shape (longer than a wide rectangle), an oblate shape (a length larger than a wide circle or an ellipse), and the like, for example, a circular tube, a rectangular tube, or the like.
  • a tube having a flat cross section is preferable, for example, a tube having a cross section of 2 to 10 mm in width and 20 to 1000 mm in length or elliptical.
  • the material of the pipe wall may be metal, polymer material, inorganic material or the like.
  • the outer surface of the condensing tube can be properly treated to infiltrate or not wet with the condensate, such as hydrophilization, so that the condensate flows down in a film, reducing the possibility that the condensed droplets mix with the raw material liquid to contaminate the condensate. Sex, it can also reduce the distance between the evaporation surface and the condenser tube to save space, increase production or energy efficiency.
  • the evaporation surface of the present invention is a device for expanding the liquid distribution and maximizing the surface area thereof to facilitate evaporation, while the liquid flows through the surface and the pores thereof, and at the same time, it is preferred that the evaporation surface is in good affinity with the liquid to be treated. Sex to facilitate the expansion of the liquid on the surface of the evaporation surface. For softer materials, the skeleton and or the outer frame can be used to tension and level it.
  • Evaporation surfaces include, but are not limited to, the following materials (or consist of skeletons or frames):
  • Fiber braid such as fiberglass cloth or felt, silicone cloth or felt, rock wool cloth or felt or board, stainless steel fiber cloth Felt
  • a mesh made of filaments or fibers made of various materials such as one or more layers of 40 mesh-150 mesh hydrophilized stainless steel mesh;
  • a plate or a perforated plate such as a hydrophilically treated stainless steel plate, a glass plate, a ceramic plate, or the like.
  • the evaporation surface is made up of 2 layers of treated degreased fiberglass cloth (the inter-layer pores of the fiberglass cloth can make the liquid diffuse better) and the outer frame is made, and a V-shaped groove is arranged at the top of the evaporation surface (or Then, the outer wall of the tank is covered with the fiberglass cloth, and the liquid enters the tank through the water distributor, and then overflows from the slot and falls into the evaporation surface (or enters the evaporation surface by the fiberglass cloth of the groove wall).
  • the shape of the evaporation surface is the same as the shape of the condensation surface of the condenser tube and the area is equal, and the evaporation surface is disposed in parallel with the condensation tube.
  • the evaporation surface and the condensation tube are preferably arranged in phase, and both surfaces of the evaporation surface are distributed with liquid, and both function as evaporation.
  • the heating device is a device for raising the temperature of the liquid, and may be an electrothermal method or a steam heating or waste heat recovery method.
  • electrothermal method for example, electric heating plates, electric heating pipes, heat exchangers, and the like.
  • electrical heating for smaller throughput distillation equipment, it is preferred to use electrical heating, while for larger throughput equipment it is preferred to use steam heating.
  • the heating device is placed in the housing or outside the housing to heat the liquid, and the liquid is heated to a certain temperature, for example, the heating device is an electric heating tube and is placed inside or outside the pipeline of the raw material liquid in the housing, or placed in a material outside the housing. The raw material liquid is heated inside or outside the liquid pipe section.
  • the condensation tube is disposed opposite the evaporation surface, and preferably the outer surface of the condensation tube is parallel to the evaporation surface to facilitate the evaporation-condensation process.
  • the evaporation surface and the condensation tube may be at an angle to the vertical surface, preferably placed vertically to facilitate flow of liquid from the evaporation surface and condensate flow from the outer surface of the condensation tube without accumulation.
  • the distance between the evaporation surface and the surface of the condensing tube is adjusted (both surfaces are flat surfaces and arranged in parallel), when the distances are respectively 3 mm, 7 mm, 20 mm,
  • the yield and energy efficiency at 7mm is slightly smaller than that at 3mm, while at 20mm, the yield and energy efficiency are much smaller.
  • the gradient distiller also includes other auxiliary facilities, such as a power source, a temperature controller, an outer casing insulation layer, a raw material liquid processing facility, a regulating instrument, a valve, etc., which are not described in detail in the prior art.
  • auxiliary facilities such as a power source, a temperature controller, an outer casing insulation layer, a raw material liquid processing facility, a regulating instrument, a valve, etc., which are not described in detail in the prior art.
  • the distiller and the distillation method of the present invention are mainly used for distillation purification or concentration of liquids, such as production of distilled water, seawater desalination, salting of seawater, and concentration of extracts.
  • Distillation apparatus according to the present invention due to comparison
  • the heat of condensation is completely recovered, and the heat of the preheated raw material liquid mainly comes from the heat of condensation, and thus the heat of vaporization of the liquid is basically derived from the heat of condensation, so that a large amount of energy is saved, and the distillation apparatus of the present invention has no need to cool water or reduce cooling water.
  • the advantage of the amount of use For example, according to the data of Example 2, the energy efficiency is 10 effects, and the yield is 1 L/m2h.
  • the distiller of the present invention can be operated under normal pressure, not only the safety is greatly improved, but also an inexpensive, corrosion-resistant polymer material or a composite material thereof can be used instead of the alloy material, which greatly reduces the cost.
  • Figure 1 is a schematic view showing the structure of the distiller at the level of the evaporation surface.
  • Figure 2 is a schematic view showing the structure of a gradient distiller having a heat exchanger.
  • Figure 3 is a schematic view showing the structure of a distiller having a cooling device.
  • Figure 4 is a schematic view showing the structure of a retort of a plurality of evaporation faces and a condenser.
  • Figure 5 is a schematic view showing the structure of a distiller for treating a high temperature liquid.
  • Figure 6 is a schematic view showing the structure of a condenser tube made of a polymer material.
  • Figure 7 is a schematic view showing the structure of a condenser tube made of a polymer material.
  • a condensing pipe 2 is disposed in the outer casing 9, and the condensing pipe 2 is composed of 20 round pipes of 10 mm in length and 500 mm in length, and the evaporating surface 1 is a stainless steel plate, and the distance between the evaporating surface and the condensing pipe is 30 mm.
  • the raw material liquid enters the condensing pipe 2 from the inlet port 10 and flows along the condensing pipe 2, and the liquid vapor condenses on the lower surface of the condensing pipe 2, while the condensing heat preheats the liquid in the condensing pipe 2.
  • the preheated liquid enters the heating device 3 via the liquid dispenser 4, and is further heated in the heating device 3, and the heated liquid enters the evaporation surface 1, and is distributed and flows on the evaporation surface 1 while continuously evaporating.
  • the temperature of the liquid is also continuously lowered, eventually entering the tail tank 6, and being discharged by the tail pipe 12.
  • the liquid vapor condenses on the surface of the condensing pipe 2, and the condensate flows along the condensing pipe 2 to one end and falls into the condensate tank 7 (the left end of the condensing pipe is higher than the right end), and is discharged through the condensate pipe 11.
  • the evaporation surface 1 is two layers of treated and degreased fiberglass cloth (the pores between the fiberglass cloth layers can make the liquid spread better) and the outer frame is made, and the evaporation surface is 7 mm away from the condensation tube.
  • the top of the evaporation surface is provided with a V-shaped groove (or the outer wall of the groove is covered with the fiberglass cloth), and the liquid enters the groove through the water distributor, and then overflows from the groove and falls into the evaporation surface (or by the groove wall)
  • the fiberglass cloth enters the evaporation surface), and the condensation tube 2 is 20 10mm ⁇ 10mm
  • the stainless steel square tubes are juxtaposed.
  • the raw material liquid enters the heat exchanger 5 from the inlet port 10, enters the condenser tube 2, flows along the condenser tube 2, is preheated in the condenser tube 2, and simultaneously condenses liquid vapor on the outer surface of the condenser tube 2.
  • the preheated liquid enters the heating device 3, is further heated in the heating device 3, and the heated liquid enters the liquid distributor 4, is distributed by the liquid distributor 4 to the evaporation surface 1, and is distributed on the evaporation surface 1 in a film shape. And flowing, while continuously evaporating, and the temperature of the liquid is continuously lowered, finally entering the tail water tank 6, entering the heat exchanger 5 from the pipeline, exchanging heat with the raw material liquid in the heat exchanger 5, and finally discharging it from the tail liquid pipe 12.
  • the liquid vapor evaporated by the evaporation surface is condensed on the surface of the condensing pipe 2, and the condensate flows along the condensing pipe 2 to one end and falls into the condensate tank 7, and enters the heat exchanger 5 through the pipe, and carries out the raw material liquid in the heat exchanger 5.
  • the heat exchange is finally discharged from the condensate pipe 11.
  • the heating device 3 is a liquid storage tank at the top end of the condensation tube, and has a built-in heater, and the heating device is located in the outer casing 9.
  • a liquid cooling device 13 is provided on the liquid circulation pipe 14 to appropriately cool the circulating liquid to increase the temperature difference between the evaporation surface and the condensation pipe, thereby increasing the evaporation and condensation speed.
  • the liquid in the cooling device 13 exchanges heat with outside air, cooling water, and the like.
  • the replenished raw material liquid enters the liquid circulation pipe 14 from the inlet port 10, and enters the condensing pipe 2 with the circulating liquid, flows along the condensing pipe 2, is preheated in the condensing pipe 2, and liquid vapor occurs on the outer surface of the condensing pipe 2 Condensation,.
  • the preheated liquid enters the heating device 3, is further heated in the heating device 3, and the heated liquid enters the liquid distributor 4, is distributed by the liquid distributor 4 to the evaporation surface 1, and is distributed on the evaporation surface 1 in a film shape.
  • the finally unvaporized liquid enters the tail water tank 6, partially discharged from the tail liquid pipe 12, and part of the circulation is continuously evaporated and moderately cooled in the cooling device.
  • the liquid vapor evaporated from the evaporation surface is condensed on the surface of the condensing pipe 2, and the condensate flows along the condensing pipe 2 to one end and falls into the condensate tank 7, and finally discharged from the condensate pipe 11.
  • the apparatus in this embodiment comprises a plurality of condensing tubes 2 having a rectangular cross section of 5 mm ⁇ 250 mm and a length of 600 mm, that is, each condensing tube contains two condensing surfaces of 250 mm ⁇ 600 mm.
  • the evaporation surface 250mm ⁇ 600mm is a hydrophilized 150 mesh stainless steel mesh.
  • the screen is fixed and tensioned by a frame, and the top of the evaporation surface is a V-shaped groove covered with a mesh.
  • the evaporation surface 1 is parallel to the condensation tube 2, arranged one on another and at a distance of 3 mm.
  • the heat exchanger 5 is used for heat exchange between the raw material liquid and the condensate and the tail liquid.
  • the technical scheme of the embodiment is suitable for concentrating the high temperature extract or distilling the high temperature wastewater. Pure water.
  • the high temperature liquid is introduced from the top and can be operated without heating the circulating liquid, or the heating energy is less. Concentration of high temperature extracts such as traditional Chinese medicine aqueous extracts (usually high temperature extraction) is particularly advantageous.
  • the replenished raw material liquid is mixed into the circulating liquid through the liquid inlet pipe 10, enters the heating device 3 with the circulating liquid, is heated and heated (or not heated) in the heating device 3, and then enters the liquid discharging device 4, and is distributed to the evaporation surface 1, Evaporating and cooling on the evaporation surface 1, and then flowing into the tail liquid tank 6, partially discharged from the tail liquid pipe 12, partially transported by the circulation pump 8 and the circulation pipe 14 through the cooling device 13, and moderately cooled in the cooling device 13, after which Each condensing pipe 2 is distributed through a pipe, preheated in the condensing pipe 2, and then collected by the pipe, and then the raw material liquid is added.
  • a gradient sub-boiling distiller made of a polymer material or a composite material thereof (for example, polypropylene which is thermally conductive to enhance thermal conductivity).
  • the condensation tube is shown in Figures 6 and 7.
  • the condensing tube has a length of 1200 mm and a rectangular shape with a length of 1000 mm and a width of 5 mm.
  • the two ends of the condensing tube are provided with a liquid passage 23, and the longitudinal partition 15 functions to increase the strength.
  • the partitions formed by the longitudinal partition 15 are connected to the ends of the condensing tube.
  • the liquid passages 23 are in communication.
  • the surface of the condensing tube is provided with a columnar protrusion 16, a strip-shaped protrusion 17 having a rectangular cross section or a strip-shaped protrusion 21 having a triangular cross section, and the height of the protrusion is 3 mm to 15 mm.
  • On the surface of the strip-shaped projections there are respectively a flow guiding groove: a gap 19 and 20 between the groove 18 and the strip-shaped projection, and a guide groove 22 formed by the convex side and the male pattern on the side.
  • the columnar protrusion may be inclined with respect to the surface.
  • the top end of the columnar protrusion When the condenser tube is placed vertically, the top end of the columnar protrusion is lower than the base portion, so that the raw material liquid on the evaporation surface does not flow upward into the condensate, and the condensate or condensation generated on the columnar protrusion
  • the condensate flowing on the surface of the tube to the columnar projections also cleans the columnar projections and eventually flows into the raw material liquid without contaminating the condensate.
  • the protrusions may also be longitudinal strips, for example, strips having a rectangular, semi-circular, triangular shape, etc., the top end of which is in contact with the evaporation surface, supports the evaporation surface, and the base is connected to the surface of the condensation tube.
  • the side surface may have a flow guiding groove inclined to the condensation surface, and the one end of the flow guiding groove at the evaporation surface is lower than the end at the condensation surface.

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Abstract

一种梯度亚沸蒸馏器，包括冷凝管（2）、蒸发面（1）、加热装置（3）、布液器（4）、尾液槽（6）、冷凝液槽（7）、尾液管（12）、进液管（10）、冷凝液管（11）、外壳（9），原料液体经过冷凝管（2）被预热，在加热装置（3）内被进一步加热之后在蒸发面（1）上流下，并不断蒸发，温度不断降低，蒸汽在冷凝管（2）表面冷凝，其冷凝热对冷凝管（2）内的原料液体预热，原料液体在冷凝管（2）内的流向与在蒸发面（1）上相反。

Description

梯度亚沸蒸馏器 技术领域
本发明涉及液体蒸馏纯化或浓缩领域，具体是一种液体蒸馏纯化、浓缩设备及方法。
背景技术
现有的蒸馏技术，包括蒸馏水生产、海水淡化、液体浓缩为了节约能源常使用多效蒸馏技术。需要高温及高压，同时设备复杂，能效受设备的级数限制，而蒸馏浓缩通常只能达到2-3效。亚沸蒸馏具有冷凝水杂质少的优点，所以用于对水质要求较高的场合的用水制备。目前的亚沸蒸馏器，首先产量小只能用于实验室用水的制备，其次能效低，是远低于一效的，能源浪费严重，同时冷凝浪费大量水资源。
发明内容
本发明的目的是提供一种液体蒸馏设备及蒸馏方法，以解决现有技术存在的问题。
为了达到上述目的，本发明所采用的技术方案为：
一种梯度亚沸蒸馏器，其特征在于：包括至少一个冷凝管、至少一个蒸发面、加热装置、布液器、尾液槽、冷凝液槽、尾液管、进液管、冷凝液管、外壳，其中加热装置的一端与布液器相通，另一端与冷凝管相通，蒸发面一端承接布液器，另一端设有尾液槽，尾液槽与尾液管相通，冷凝管的一端与进液管相通，另一端与加热装置相通，冷凝液槽位于冷凝管的一端且与冷凝液管相通。
所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括一个泵，泵的进口和出口通过循环管道分别与尾液管、进液管相通。
所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括换热器，换热器设置于尾液管、冷凝液管和进液管上。
所述的梯度亚沸蒸馏器，其特征在于：所述的循环管道上还包括一个冷却装置。
所述的梯度亚沸蒸馏器，其特征在于：所述的进液管连接于冷凝管与加热装置之间的管道上或布液器与加热装置之间的管道上。
所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括一个使蒸发面相对于冷凝管做周期运动的装置连接于蒸发面上。
所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括气体发生器、气体储罐、抽气机或压气机通过管道与外壳相通。
所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括一个风机，风机的进口和出口与外壳相通。
所述的梯度亚沸蒸馏器，其特征在于：所述的冷凝管由高分子材料或其复合材料制成，内部有纵向隔板，隔板隔开的孔道均与冷凝管两端的液体通道相通，冷凝管表面有凸起；蒸发面与冷凝管相间排列，冷凝管表面的凸起将蒸发面支撑、压紧；所述的冷凝管表面的凸起包括：柱状或锥状凸起；倾斜的柱状锥状凸起；纵向条形凸起；侧面有处于蒸发面的一端低于处于冷凝面的一端的导流槽的纵向条形凸起。
所述的梯度亚沸蒸馏器，其特征在于：所述的蒸发面省去，原料液体由布液器滴落或喷出。
根据本发明的技术方案，原料液体进入冷凝管，从冷凝管的一端流向另一端。同时，液体的蒸汽在冷凝管的外表面冷凝，冷凝热使管内的原料液体温度不断的升高，最终液体进入加热装置，被进一步加热，温度升高。被加热后的液体，分布到蒸发面上，流向蒸发面的另一端，同时不断的蒸发，温度不断降低，液体蒸汽在冷凝管上冷凝，使冷凝管内液体不断被加热。由于蒸发面上的水流量与冷凝管内的水流量相等，所以高温液体自蒸发面一端流至另一端所下降的温度就是液体经冷凝管后上升的温度。
例如20℃的自来水由进水管进入冷凝管，在冷凝管内被预热至90℃，最后在加热装置内被加热至100℃，之后经布水器分布到蒸发面上，并开始蒸发，随着水流向蒸发面底端温度不断下，其最终下降幅度基本与冷凝管内水温升高幅度相等(其温降基本为蒸发散热所致，接触传热占比极少)，温度降为30℃，排出。在此过程中外界提供的热量为将水加热10℃，而蒸发(或冷凝)的水蒸气对应的热量为使水降低70℃，所以系统的能效约为7效。如果进行调节进水流速使水预热后为95℃，从蒸发面蒸发后温度降为25℃，则设备能效约为14效。
为了增加产量，可以使液体在较高的温度下蒸发，所以提高液体蒸发后的最终温度。因而在系统内加入换热器，用于尾液、冷凝液与进液之间进行热交换。
为了节约用水或用于提取液的浓缩，用泵将尾液回收进入循环，即从蒸发面上流下的未蒸发完的液体，部分经尾液槽汇集，再由泵泵入循环管道，部分由尾液管排出，同时由进液管补充适量的原料液体。循环液体中混入原料液体使循环液体温度降低，因而再次进入冷凝管时可以对蒸发面上蒸发的蒸汽进行冷凝。为了增加产量，可以对循环液体进行冷却，以增加蒸发面和冷凝管外壁的温差。另外，也可以为了增加热效降低蒸发面与冷凝管壁的温差，例如将排出尾液、冷凝液与进入设备的原料液体进行热交换，对进入设备的原料液体进行预热。
对于原料液体温度较高需要蒸馏纯化或浓缩的，新补充的原料液体可以自加热装置与布液器之间的管道或加热装置与冷凝管之间的管道直接引入，加热装置可以不对循环液体加热，同时可以对从蒸发面蒸发后的的循环液体进行冷却。
使蒸发面相对于冷凝管进行周期运动，以带动蒸发面和冷凝管之间的气体运动，从而促进蒸发-冷凝过程进行，提高产量。可以使一个运动装置与蒸发面相连接，该运动装置使蒸发面做周期运动。例如：转动，与冷凝管表面垂直方向的往复运动，与冷凝管的面平行方向的往复运动。例如将蒸发面固定于一个轴上，轴与电机和曲轴连杆相连，则电机带动蒸发面往复运动；蒸发面制成圆筒状，中心设有一轴，轴连接电机，冷凝管分布于蒸发面周围，电机带动蒸发面旋转；同时可以在蒸发面设置扭带、弹簧等插件以增加气体运动。
所述的梯度亚沸蒸馏器可以设有气体发生器、气体储罐、抽气机或压气机，以改变外壳内部的气氛或压力。使用气体发生器产生所需要的气体或者使用气体储罐储存所需要的气体，通过管道充入外壳内，可以连续充入也可以间断充入。例如使用一储有氮气的储罐与外壳相通，对外壳内充入氮气。例如当原料液体在空气中不稳定时可以对设备内充以氮气、氩气、二氧化碳等惰性气体或其混合气体；为降低冷凝液中氧气或二氧化碳的含量可以充以氮气；为了提高产量或能效可以充以氢气、氦气等气体。所充入的气体也可以是各种气体的混合气体或含有原料液体蒸汽的混合气体。
所述的梯度亚沸蒸馏器内部气体的压力可以小于大气压力，以适应低温蒸馏或浓缩。例如可以为0.01-0.9个大气压。此时，一方面可以靠增加抽气机将气体从系统抽去来实现，也可以通过提高系统的气密性，在抽气后维持较低气压运行，或者同时采用这两种方法。另外，所述的梯度亚沸蒸馏器也可以包括压气机，使设备内 部压力大于大气压，这样提高液体最终可加热温度，以提高能效。例如增加设备内部气压使水可以加热至120℃
所述的梯度亚沸蒸馏器可以包括风机，优选贯流风机。风机的空气入口和出口分别与外壳相连，风机工作时从外壳内吸入空气，再吹入外壳内，造成其流动，促进蒸发和冷凝过程进行，提高产量或能效。贯流风机叶轮轴心与蒸发面平行，减少上层高温气体与下层低温气体的混合。
所述的梯度亚沸蒸馏器的蒸发面和冷凝管之间可以设置有将蒸发面固定或将蒸发面与冷凝管隔开一定距离的装置，包括支架、支柱等，且优选其与冷凝管接触部位高于与蒸发面接触部位。例如：固定于蒸发面或冷凝管上的弹簧、一端固定于冷凝管上的L形物体、柱状物体、横杆(通过两端与其垂直的支柱固定于冷凝管上，横杆平行于冷凝管表面且相隔一定距离，优选横杆水平设置且与冷凝管接触部位高于横杆)、倒置的V形U形支架(其中V形和U形的两端分别与蒸发面和冷凝管接触，因其中间高于接触部位，原料液体不会流到冷凝管表面)或条形丝网卷成截面为V形或U形的支架。
所述的梯度亚沸蒸馏器的蒸发面可以省去，液体仅由布液器分布、滴落或喷出，液体在下落的过程中发生蒸发，蒸发后的尾液落入尾液槽。例如布液器为一段开有多个小孔的管，液体从小孔滴落，蒸发后落入尾液槽。
所述的梯度亚沸蒸馏器的尾液槽和冷凝液槽可以有多个也可以仅有一个，即可以每个蒸发面(冷凝管)均配备一个尾液槽(冷凝液槽)，也可以多个蒸发面(冷凝管)共用一个尾液槽(冷凝液槽)。
所述的梯度亚沸蒸馏器的冷凝管可以由高分子材料或其复合材料制成，内部可以有纵向隔板，隔板起到增加冷凝管强度、节约材料的作用。冷凝管表面有凸起，起到支撑、固定蒸发面的作用。所述的凸起包括但不限于：柱状或锥状凸起；倾斜的柱状或锥状凸起；纵向条行凸起；侧面有导流槽的纵向条形凸起。
所述的凸起可以为柱状，例如圆柱、方柱、棱柱等，柱状凸起可以相对于表面倾斜，当冷凝管竖直放置时柱状凸起的顶端低于基部，这样蒸发面上的原料液体不会向上流入冷凝液，而柱状凸起上产生的冷凝液或者冷凝管表面流到柱状凸起上的冷凝液也对柱状凸起产生清洗并最终流入原料液体，不会对冷凝液产生污染。所述的凸起也可以为纵向条形，例如截面为矩形、半圆形、三角形的条形等，其顶端与 蒸发面接触，支撑蒸发面，基部连接于冷凝管表面。其侧面可以有与冷凝面成倾斜的导流槽，导流槽处于蒸发面的一端低于处于冷凝面的一端。这样，蒸发面上的液体流向冷凝面时会汇入导流槽，并沿导流槽流回蒸发面，而凸起上产生的冷凝液也会沿导流槽，同时对凸起进行清洗，使原料液体不会污染冷凝液。见图6和图7
所述的导流槽可以为：凸起表面的凹槽、凸起侧面的阳纹与凸起侧面形成的槽、凸起剪断后形成的间隙(或者表述为凸起与凸起之间的间隙)、
所述的布液器为使液体流至蒸发面的装置，最好使液体均匀的分布于蒸发面的一端。可以仅为一段管及管口，液体经由该管的管口流入或落入蒸发面上，或者为一段壁上开有多个小孔的管，或在壁上有纵向狭缝的管。
本发明所述的冷凝管主要作用是利用其外表面对蒸汽冷凝，管壁传热，同时其内部空间容许液体通过，因而所述的冷凝管并非限于截面长径和宽径相近的管。管壁的形状只要可用于传热、冷凝即可，其形状可以是规则的，也可以是不规则的多种形状，例如弧形、平面或表面有翅片的面等。
优选较大的、平整的外表面制成的，同时相对较小的内部空间的管状物，以使内部蓄积较少的液体。管的截面可以为圆形、矩形、长条形(长远大于宽的矩形)、扁圆形(长大于宽的圆或椭圆)等，例如为圆管、矩形管等。优选截面扁平的管，例如截面为宽2-10mm、长20-1000mm矩形或椭圆形的管。
也可以使用多个圆管或方管排列而成，例如多个10mm×20mm的不锈钢方管并列。
管壁的材料可以是金属、高分子材料、无机材料等。
可以对冷凝管的外表面进行适当的处理，使之与冷凝液浸润或不浸润，比如亲水化处理，使冷凝液成膜状流下，减少冷凝液滴与原料液体混合而污染冷凝液的可能性，同时也可以减小蒸发面与冷凝管之间的距离，以节约空间、增加产量或能效。
本发明所述的蒸发面为使液体分布扩展，最大的增加其表面积以利于蒸发的装置，同时液体从其表面和孔隙流过，同时最好使蒸发面与其所处理的液体由良好的亲和性，以利于液体在蒸发面表面的扩展。对于较软的材料，可以使用骨架和或外框将其张紧、平整。
蒸发面包括但不限于以下材料构成(或者包含骨架或外框)：
纤维编织物，例如玻纤布或毡、硅氧布或毡、岩棉布或毡或板、不锈钢纤维布 或毡；
由各种材料制成的细丝或纤维制成的网，例如一层或多层40目-150目的经亲水化处理的不锈钢丝网；
板或多孔板，例如亲水处理的不锈钢板、玻璃板、陶瓷板等。
例如蒸发面为2层经处理去油的玻纤布(玻纤布层间孔隙可使液体更好的扩散)和外框制成，在蒸发面的顶部设置有截面为V形的槽(或者再在槽内外壁覆盖玻纤布)，液体经布水器进入槽内，再由槽口溢出，落入蒸发面(或由槽壁的玻纤布进入蒸发面)。
优选蒸发面形状与冷凝管的冷凝面形状相同且面积相等，且蒸发面与冷凝管平行设置。
当系统包括多个冷凝管和蒸发面时，蒸发面和冷凝管优选相间排列，且蒸发面的两个表面均分布有液体，均起到蒸发的作用。
本发明所述的加热装置为一个使液体温度升高的装置，可以使用电热方式，也可以使用蒸汽加热、废热回收等方式。例如电热板、电热管、换热器等。对于较小产量的蒸馏设备，优选使用电加热，而对于较大产量的设备优选使用水蒸汽加热。
另外，加热装置置于壳体内或壳体外对液体进行加热，将液体加热至一定温度，例如加热装置为电热管且置于壳体内原料液体的管道内或外侧，或者置于处于壳体外的原料液体管段的内或外对原料液体进行加热。
冷凝管与蒸发面相对设置，优选冷凝管的外表面与蒸发面平行，以促进蒸发-冷凝过程的进行。蒸发面及冷凝管可以与竖直面成一定的角度，优选竖直放置以利于液体从蒸发面流下及冷凝液从冷凝管外表面流下而不会蓄积。
对于根据本发明技术方案制作的一台蒸馏器，调节其蒸发面与冷凝管的表面之间距离(两个面均为平整表面且平行排列)，当其距离分别为3mm、7mm、20mm时，7mm时的产量与能效略微比3mm时小，而为20mm时则产量和能效小很多。另外，可以通过调节液体流量、加热温度等在产量和能效之间进行调节。
所述的梯度蒸馏器还包括其他辅助设施，例如电源、温控仪、外壳保温层、原料液体处理设施、调节仪器仪表、阀门等属于现有技术未做详述。
本发明的蒸馏器及蒸馏方法主要用于液体的蒸馏纯化或浓缩，例如蒸馏水的生产、海水淡化、海水浓缩制盐、提取液的浓缩等。根据本发明的蒸馏设备由于比较 完全的回收了冷凝热，预热原料液体的热量主要来自冷凝热，因而液体的蒸发热也基本来自冷凝热，所以节约了大量的能源，同时本发明的蒸馏设备具有无需冷却水或减少冷却水的用量的优点。例如根据实施例2的数据，能效达到10效，产量为1L/m2h。
另外，由于本发明的蒸馏器可以在常压下运行，不光安全性大幅度提高，还可以使用便宜、耐腐蚀的高分子材料或其复合材料代替合金材料，大幅度降低了造价。
附图说明
图1蒸发面水平的蒸馏器结构示意图。
图2设有换热器的梯度蒸馏器结构示意图。
图3设有冷却装置的蒸馏器结构示意图。
图4多个蒸发面和冷凝管的蒸馏器结构示意图。
图5处理高温液体的蒸馏器结构示意图。
图6一种高分子材料制成的冷凝管的结构示意图。
图7一种高分子材料制成的冷凝管的结构示意图。
具体实施方式
实施例1
如图1所示，外壳9内设有冷凝管2，冷凝管2为20根直径10mm长500mm的圆管并列组成，蒸发面1为不锈钢板，蒸发面与冷凝管距离为30mm。原料液体由进液口10进入冷凝管2，并沿冷凝管2流动，在冷凝管2的下表面液体蒸汽发生冷凝，同时冷凝热对冷凝管2内的液体进行预热。被预热后的液体经由布液器4进入加热装置3，在加热装置3内被进一步加热，被加热后的液体进入蒸发面1，在蒸发面1上呈膜状分布且流动，同时不断蒸发，而液体的温度也不断降低，最终进入尾液槽6，由尾液管12排出。液体蒸汽在在冷凝管2的表面冷凝，冷凝液沿冷凝管2流向一端并落入冷凝液槽7(冷凝管的左端比右端高)，经由冷凝液管11排出。
实施例2
如图2所示，蒸发面1为两层经处理去油的玻纤布(玻纤布层间孔隙可使液体更好的扩散)和外框制成，蒸发面与冷凝管相距7mm，在蒸发面的顶部设置有截面为V形的槽(或者再在槽内外壁覆盖玻纤布)，液体经布水器进入槽内，再由槽口溢出，落入蒸发面(或由槽壁的玻纤布进入蒸发面)，冷凝管2为20根10mm×10mm 的不锈钢方管并列组成。原料液体由进液口10进入换热器5，再进入冷凝管2，并沿冷凝管2流动，在冷凝管2内被预热，同时在冷凝管2外表面液体蒸汽发生冷凝。被预热后的液体进入加热装置3，在加热装置3内被进一步加热，被加热后的液体进入布液器4，被布液器4分布至蒸发面1，在蒸发面1上呈膜状分布且流动，同时不断蒸发，而液体的温度也不断降低，最终进入尾水槽6，由管道进入换热器5，在换热器5内与原料液体进行热交换，最终由尾液管12排出。由蒸发面蒸发的液体蒸汽在在冷凝管2的表面冷凝，冷凝液沿冷凝管2流向一端并落入冷凝液槽7，由管道进入换热器5，在换热器5内与原料液体进行热交换，最终由冷凝液管11排出。其中加热装置3为冷凝管顶端的蓄液池，内置加热器，加热装置处于外壳9内。
实施例3
本实施方案中，在液体循环管道14上设有液体冷却装置13对循环液体进行适当的冷却，以增加蒸发面与冷凝管之间的温差，从而增加蒸发和冷凝速度。在冷却装置13内液体与外界的空气或冷却水等进行热交换。
补充的原料液体由进液口10进入液体循环管道14中，并随循环液体进入冷凝管2，沿冷凝管2流动，在冷凝管2内被预热，同时在冷凝管2外表面液体蒸汽发生冷凝，。被预热后的液体进入加热装置3，在加热装置3内被进一步加热，被加热后的液体进入布液器4，被布液器4分布至蒸发面1，在蒸发面1上呈膜状分布且流动，同时不断蒸发，而液体的温度也不断降低，最终未蒸发的液体进入尾水槽6，部分由尾液管12排出，部分继续进行循环蒸发并在冷却装置内被适度降温。由蒸发面蒸发的液体蒸汽在在冷凝管2的表面冷凝，冷凝液沿冷凝管2流向一端并落入冷凝液槽7，最终由冷凝液管11排出。
实施例4
本实施例中设备包含多根冷凝管2，冷凝管的横截面为5mm×250mm的矩形，长600mm，即每根冷凝管含有2个250mm×600mm的冷凝面。蒸发面250mm×600mm为经亲水化处理的150目不锈钢丝网，丝网用边框固定、张紧，蒸发面的顶部为覆有丝网的V形槽。蒸发面1与冷凝管2平行、相间布置且相距3mm距离。换热器5用于原料液体与冷凝液、尾液之间进行热交换。
实施例5
本实施例的技术方案适合于对高温提取液进行浓缩或对高温废水进行蒸馏制取 纯水。高温液体由顶端引入，可以在不对循环液体加热的情况下工作，或者加热耗能较少。对于高温提取液如中药水提液(通常是高温提取)的浓缩尤为有利。
补充的原料液体通过进液管10混入循环液体，随循环液体进入加热装置3，在加热装置3内被加热升温(或者不进行加热)，再进入布液器4，被分布至蒸发面1，在蒸发面1上蒸发、降温，之后流入尾液槽6，部分由尾液管道12排出，部分由循环泵8和循环管道14输送流经冷却装置13，在冷却装置13内被适度冷却，之后通过管道分配进入每个冷凝管2，在冷凝管2内被预热，再由管道汇集，再加入原料液体。
实施例6
一种由高分子材料或其复合材料(例如加导热材料增强导热性的聚丙烯)制成冷凝管的梯度亚沸蒸馏器。为了节省篇幅，本节不对整体结构详述，仅叙述其所使用的冷凝管。所述的冷凝管见图6和图7。冷凝管长1200mm，截面为长1000mm宽5mm的矩形，冷凝管两端设有液体通道23，纵向隔板15起到增加强度的作用，纵向隔板15所分隔成的孔道均与冷凝管两端的液体通道23相通。冷凝管表面设有柱状凸起16、截面为矩形的条形凸起17或截面为三角形的条形凸起21，凸起高度为3mm-15mm。在条形凸起的表面分别有导流槽：凹槽18和条形凸起之间的间隙19和20以及凸起侧面与侧面上的阳纹形成的导流槽22。柱状凸起可以相对于表面倾斜，当冷凝管竖直放置时柱状凸起的顶端低于基部，这样蒸发面上的原料液体不会向上流入冷凝液，而柱状凸起上产生的冷凝液或者冷凝管表面流到柱状凸起上的冷凝液也对柱状凸起产生清洗并最终流入原料液体，不会对冷凝液产生污染。所述的凸起也可以为纵向条形，例如截面为矩形、半圆形、三角形的条形等，其顶端与蒸发面接触，支撑蒸发面，基部连接于冷凝管表面。其侧面可以有与冷凝面成倾斜的导流槽，导流槽处于蒸发面的一端低于处于冷凝面的一端。这样，蒸发面上的液体流向冷凝面时会汇入导流槽，并沿导流槽流回蒸发面，而凸起上产生的冷凝液也会沿导流槽流动，同时对凸起进行清洗，使原料液体不会污染冷凝液。

Claims (10)

  1. 一种梯度亚沸蒸馏器，其特征在于：包括至少一个冷凝管、至少一个蒸发面、加热装置、布液器、尾液槽、冷凝液槽、尾液管、进液管、冷凝液管、外壳，其中加热装置的一端与布液器相通，另一端与冷凝管相通，蒸发面一端承接布液器，另一端设有尾液槽，尾液槽与尾液管相通，冷凝管的一端与进液管相通，另一端与加热装置相通，冷凝液槽位于冷凝管的一端且与冷凝液管相通。
  2. 根据权利要求1所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括一个泵，泵的进口和出口通过循环管道分别与尾液管、进液管相通。
  3. 根据权利要求1或2所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括换热器，换热器设置于尾液管、冷凝液管和进液管上。
  4. 根据权利要求2所述的梯度亚沸蒸馏器，其特征在于：所述的循环管道上还包括一个冷却装置。
  5. 根据权利要求4所述的梯度亚沸蒸馏器，其特征在于：所述的进液管连接于冷凝管与加热装置之间的管道上或布液器与加热装置之间的管道上。
  6. 根据权利要求1所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括一个使蒸发面相对于冷凝管做周期运动的装置连接于蒸发面上。
  7. 根据权利要求1所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括气体发生器、气体储罐、抽气机或压气机通过管道与外壳相通。
  8. 根据权利要求1所述的梯度亚沸蒸馏器，其特征在于：所述的蒸馏器还包括一个风机，风机的进口和出口与外壳相通。
  9. 根据权利要求1或2、4、5、7任一项所述的梯度亚沸蒸馏器，其特征在于：所述的冷凝管由高分子材料或其复合材料制成，内部有纵向隔板，隔板隔开的孔道均与冷凝管两端的液体通道相通，冷凝管表面有凸起；蒸发面与冷凝管相间排列，冷凝管表面的凸起将蒸发面支撑、压紧；所述的冷凝管表面的凸起包括：柱状或锥状凸起；倾斜的柱状锥状凸起；纵向条形凸起；侧面有处于蒸发面的一端低于处于冷凝面的一端的导流槽的纵向条形凸起。
  10. 根据权利要求1或2所述的梯度亚沸蒸馏器，其特征在于：所述的蒸发面省去，原料液体由布液器滴落或喷出。
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EP3536390A1 (en) 2019-09-11

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