COUNTER CIRCULATING LIQUID PROCESSING SYSTEM BY REPEATEDLY RE-USING THERMAL ENERGY

Abstract

A liquid desalination, distillation, disinfection, purification, or concentration system by repeatedly re-using thermal energy is provided. Thermal heat source can be solar, fossil fuel, or low grade heat discharged from industrial systems. Multiple thermally insulated and isolated stages of vaporization-condensation chambers can be connected to enhance production yield. Vapor is generated by direct heating of liquid and flash evaporation. Vapor generated is condensed in condenser cooled by intake liquid. Counter circulating intake liquid will be heated by released latent heat from vapor. Externally provided thermal energy will accumulate and be re-used in the system. Vaporization and condensation process will be continuously re-cycled to enhance production yield. The system can be configured to support flexible deployment in various configurations and in different locations, including direct floating installation on water surface.

Description

FEDERALLY SPONSORED RESEARCH

Not Applicable

SEQUENCE LISTING

Not Applicable

BACKGROUND

Prior Art

Freshwater shortage worldwide has reached crisis level. There is urgent need to provide new freshwater supply worldwide, in addition to conservation effort. With increasingly depleted freshwater sources, the only potentially significant new freshwater source is desalination of seawater. Currently large scale commercially available desalination technology includes Reverse Osmosis (RO), Multi-Effect Distillation (MED), and Multi-Stage Flash Distillation (MSF). However, these desalination methods are expense and consume large amount of fossil fuel as energy source. Only resource-rich or developed nations can afford such technologies. With increasing concern of global climate change, technologies consuming large amount of non-renewable energy to generate freshwater is clearly not an environmentally sustainable long term solution. In addition, energy use efficiency of existing technologies converting saltwater into freshwater is less than ideal. They should and could be improved. Currently, there is no solution to provide new freshwater that can meet all of the long term requirements: environmentally sustainability, price competitiveness, large scale deployment, flexible installation, low cost construction and operation, etc.

Naturally using renewable solar energy to desalinate saltwater is an attractive and environmentally friendly approach. (Other renewable energy sources have not been proven to be adequate to desalinate saltwater on large scale.) Many solar desalination techniques capable of producing freshwater have been proposed. Of all proposed solar desalination technologies, thermal based desalination technology is the most promising. It is based on simple physical principle of using solar energy to heat and vaporize saltwater. Condensed water vapor will provide freshwater. However, solar desalination technology suffers from very low production yield, because of inherent low intensity solar energy. The cost to produce freshwater in turn is very expensive, especially when comparing with current freshwater supplies. Historically freshwater supply is often heavily subsidized by government. Its price typically is not reflection of true cost to produce freshwater. Hence any solar desalination techniques have to be price competitive to current freshwater supply, and can scale up to serve large population freshwater need, in addition to overcome any technical challenges.

Even with current commercially available MSF or MED based thermal desalination technologies using conventional fossil fuel or waste heat vapor from industrial plants, it is not using thermal energy to the fullest extent. Thermal energy re-use is quite limited. A substantial portion of thermal energy enters into the system is discarded. Production yield is limited.

Several other industries and applications use similar thermal distillation techniques and processes as in thermal desalination. They rely on the same physical principle. Original mixed liquid is thermally heated and vaporized. Evaporated vapor is then condensed into separate liquid. If mixed liquid and dissolved content have significant different boiling temperatures, they can be separated by this vaporization-condensation process. This is well-known distillation process to separate or concentrate liquid. This principle is widely used in chemical engineering, food processing, petroleum engineering, and pharmaceutical production to distill, disinfect, purify, or concentrate original liquid. Energy source to heat liquid can be fossil fuel, waste heat, or renewable energy sources like solar energy. Similar to thermal desalination, energy use efficiencies in these applications can be improved to increase production yield.

DEFINITION OF TERMINOLOGY

Important terminologies used in this disclosure are defined as in Table 1.

TABLE 1
Terminology and definition
Terminology    Definition
Original       Water taken from ambience environment to be processed
Water          (desalinated, distilled, purified, concentrated, or treated
               for other purpose). It could be seawater, brackish water,
               agricultural run-off, storm run-off, industrial waste water,
               or any surface or sub-surface water, etc. to be processed.
Original       Liquid to be processed (distilled, disinfected, purified, or
Liquid         concentrated, or treated for other purpose). It could be
               liquid chemical compound mixture, petroleum, or any
               liquid mixture to be treated.
Brine Water    Water circulating in the system after being heated. It
               contains original mixture of liquid components at various
               concentration levels.
Discharged     Brine water discharged from the system after being
Brine Water    processed. It is more concentrated than brine water.
Freshwater     Water condensed from vapor generated through the
               system.
Water Vapor    Freshwater vapor generated from heating brine water.
               It is freshwater vapor that contains very low level of
               salt. Heating at sufficiently high temperature will also
               eliminate living contaminant such as bacteria.
Brine Liquid   Liquid circulating in the system after being heated.
Discharged     Brine liquid discharged from the system after being
Brine Liquid   processed. It is more concentrated than brine liquid.
(also known as In liquid concentration applications brine liquid will
Concentrated   continuously and repeatedly processed till it reaches
Liquid)        certain concentrate level. It is then extracted from
               the system.
Concentrated   See Discharged Brine Liquid
Liquid
Distilled      Liquid condensed from brine liquid vapor generated
Liquid         through the system. If boiling temperatures are
               sufficiently differentiated it can be of pure form
               for one type of liquid component in the original
               liquid mixture.
Distilled      Steam generated from heating brine liquid. Typically,
Vapor          it is highly selectively concentrated with liquid that
               has lower boiling temperature at the same pressure.
Waste Heat     By product of discharge low grade heat from industrial
               plants such as power generation plants or chemical
               processing plants. It is typically carried in the form
               of water vapor. Alternatively, waste heat can be used
               to generate water vapor.
Concentrate    Panel to concentrate low intensity solar energy.
Solar Panel    Its form can be parabolic trough or Fresnel Lens types.
(CSP)          Typically, an evacuated tube is placed near its focal
               line. Heat transfer medium is circulated through the
               evacuated tube and heated to pre-determined temperature.
               Vapor can also be generated directly in the evacuated
               tube if heat transfer medium is the liquid to be
               processed itself.
Concentrated   Parabolic or spherical dish to concentrate low
Solar Dish     intensity solar energy. Typically, a vacuum evacuated
               disk is placed near its focal point. Heat transfer
               medium is circulated through the disk and heated to
               pre-determined temperature. Vapor can also be generated
               directly in the disk if heat transfer medium is the
               liquid to be processed itself.
Thermal        Production of freshwater by heating saltwater to
Desalination   produce freshwater vapor. Vapor is then condensed
               into freshwater.
Multi-stage    In multi-stage configuration each stage pressure
Flash          and temperature are maintained at progressively
Distillation   lower level than the previous stage. Liquid
(MSF)          entering this stage will rapidly evaporate
               (flash evaporation) into vapor in order to adjust
               to new thermal equilibrium within the new stage.
Multi-effect   In multi-stage configuration each stage pressure and
Distillation   temperature are maintained at progressively lower
(MED)          level than the previous stage. Distilled vapor
               and liquid from previous stage is used as heat
               source to heat and vaporize addition liquid.
Reverse        High pressure is applied to a membrane that will
Osmosis        block transfer of salt while allowing pass through
(RO)           of freshwater.
Low Grade      Also known as Waste Heat or Waste Vapor. In industrial
Heat (Also     applications such as power generating plants, some
known as       heat will be released into environment. Typically,
“Waste Heat”)  it is carried away in vapor form and of low intensity.
               It still contains suffcient temperature and thermal
               energy to power distillation or concentration process.

SUMMARY

The methods and apparatus are based on vaporization of original liquid to produce distilled liquid. If the boiling temperatures of the original liquid components are sufficiently different, liquid vapor generated will be distilled. It is then condensed to produce distilled liquid. In water processing applications, such as saltwater desalination, water boiling temperature is sufficiently high, it can also dis-infect the water undergoing processing. Alternatively, the original liquid can flow through the apparatus repeatedly until pre-determined concentration level is reached. The apparatus, methods, and operation principles are described in the following sections.

1. Physical Principles

Distillation is widely used in many applications and industries. It is based on a simple fact that for a mixed liquid, if different liquid components have different boiling temperatures, when mixed liquid is heated, the vaporization rates for different components will be different. If temperature is set at appropriate temperature, one liquid component will vaporize more rapidly than other liquid components in the original liquid. Vapor generated can then be separated and condensed into liquid to almost pure single liquid component.

1.1 Vaporization and Condensation Cycle:

In thermal desalination process, saltwater is heated to generate freshwater vapor. This is because freshwater and salt have vastly different boiling temperatures. A side benefit is boiling of saltwater will kill organic matters and in effect disinfect the water. Freshwater that produced through thermal desalination can be directly consumed. Using solar thermal desalination as an example, typically temperature difference between saltwater boiling temperature and ambient sea surface is greater than 70° C. Water vapor pressure ratio between these two temperatures can be 25˜40 times. Once generated, water vapor can condense rapidly when exposed to such pressure and temperature difference. However, production yield by relying only on this principle typically is rather low because solar energy intensity at earth surface is low (˜1000 W/m²).

Another physical process can be employed to increase production rate is flash evaporation. For a given liquid mixture in a container, it will be at its thermal equilibrium, i.e. its temperature, pressure, and volume will be at certain level according to thermal dynamic laws. If one parameter is suddenly changed, the mixture will adjust itself to reach new thermal equilibrium state by releasing or absorbing thermal energy. When a liquid at higher temperature is introduced to a region at sufficiently lower pressure and temperature, this liquid is “superheated” in that region. It must release excessive thermal energy to reach new thermal equilibrium state in lower temperature region. Excessive heat is released by vaporizing liquid. Latent heat needed to vaporize liquid will carry away the excessive thermal energy and lower liquid's temperature. This process is called flash evaporation because this type of evaporation can happen rapidly. Multiple of vaporization and condensation stages can be connected together to form a system based on flash vaporization. It is estimated that as much as 13% of saltwater can be “flash” vaporized to generate freshwater vapor between boiling and ambient temperatures. This is in addition to direct vaporization of heating saltwater to boiling temperature.

If only above two physical processes are used to distill or concentrate liquid, production yield typically is still limited. That is why conventional MSF or MED uses large amount of energy to generate distilled liquid. In solar desalination, combined with inherent low intensity of solar energy at earth surface, freshwater production yield will be very low and impractical in commercial applications. This is the physical reason why so many proposed solar desalination techniques have not been able to generate sufficient large amount of freshwater at low cost.

Fortunately, a third physical process can be employed to significantly enhance the distilled liquid production yield. Two counter-flowing heat exchange processes can be designed to further enhance the energy use efficiency and production yield: counter-circulating multi-stage vaporization and multi-stage condensation. Cyclical flash vaporization and condensation can be repeatedly used to vaporize and condense original liquid, provided proper thermal loss is reduced to minimal and thermal isolation between stages is well maintained.

In this design, original liquid serves two purposes. On one flow path it is used to vaporize and generate distilled liquid vapor. External heat will directly vaporize original liquid. Flash vaporization through different stages will vaporize additional liquid. On counter-flowing opposite direction path, original liquid is also used as coolant to condense vapor to generate distilled liquid. When distilled vapor condenses it releases its latent heat to coolant (original liquid). The original liquid as coolant will absorb latent heat and its temperature will gradually rise as it is transported to different stages in the opposite direction. This process can be repeated indefinitely if there is no thermal loss, perfect thermal isolation between stages, and efficient thermal exchanges. In practical situation there will be thermal loss. But if such loss is well controlled and minimized, such repeat vaporization-condensation cycle can be prolonged. As more and more external thermal energy is added to the apparatus, even for low intensity solar energy, total thermal energy available to vaporization-condensation can be drastically increased, i.e. “amplified”. Much higher yield of distilled liquid can then be produced.

In addition, speed of vaporization and condensation cycle can be significantly improved if high efficiency heat exchange devices are used in the apparatus. The amount of vapor generated or condensed depends on not only the amount of thermal energy available, but also thermal energy transfer rate. Faster heat exchange process will produce higher volume of distilled liquid. This will further enhance the production yield of distilled liquid.

This disclosure utilizes all of the above physical processes to present a highly productive apparatus and methods to generate distilled or concentrated liquid. Below sections describe in more details of the apparatus, methods, and operation. The apparatus has multiple stages. Its first stage is direct vaporization stage by using external heat transfer medium. Intermediate stages are used to flash vaporize additional liquid. The last stage is used to pre-heat intake original liquid. External thermal energy will continuously enter into the apparatus and accumulate. Total available thermal energy to vaporize will increase until external thermal energy and thermal loss from the apparatus reaches equilibrium.

1.2 Multi-Stage Vaporization:

• • 1) Solar or fossil thermal energy is used to directly heat and vaporize original liquid in the first stage. Heating can be provided by heat transfer medium, or by vapor produced externally using renewable or conventional heat source.
  • 2) At each stage pressure and temperature are maintained at progressively lower level. Therefore, heated brine liquid from previous stage will be flash vaporized when it enters the next lower pressure and temperature stage. Such flash vaporization will produce additional distilled vapor in addition to direct vaporization.
  • 3) High efficiency vaporization device is employed to speed up heat exchange process during vaporization.

1.3 Multi-Stage Condensation:

• • 1) In each stage vapor will condense on the condenser that is maintained at lower temperature, cooled by intake liquid flowing through it.
  • 2) Liquid condensed is then extracted away to heat brine liquid in next stage.
  • 3) High efficiency condenser and surface treatment is employed to speed up the heat exchange between vapor and condenser.

1.4 Counter Circulating Heat Exchange:

• • 1) Original liquid (from condenser) enters the first stage is heated to boiling temperature to generate vapor. As it enters next stages it will continuously be flash vaporized. Its temperature will be gradually lowered. Thermal energy is transferred to the coolant in condensers.
  • 2) Circulating in opposite direction, coolant used in condenser is the same intake liquid. As it enters a stage, because its temperature is at lower level, it will act as coolant to condense higher temperature vapor in that particular stage. As it moves into next stage, it will absorb thermal energy released by condensed vapor. And its temperature will gradually increase.

1.5 Accumulation of Thermal Energy:

• • 1) If thermal loss to the environment is reduced to minimal, and there is good thermal isolation between stages to maintain different thermal equilibrium states, heat exchange between these two processes can continue for prolonged time period. In an idea situation this vaporization-condensation cycle can continue indefinitely.
  • 2) As more external thermal energy continuously enters into the system, thermal energy will be accumulated inside the system. Hence more thermal energy is available to vaporize liquid. For low intensity thermal energy such as solar energy, this system in effect “amplifies” available thermal energy to generate more distilled vapor.
  • 3) If properly designed, vaporization and condensation processes can be highly efficient. Thermal energy exchanges can happen rapidly. Increase vaporization and condensation velocity can therefore contribute to increased production yield.

2. System Architecture and Operation

The overall system architecture, apparatus, and operation is described in the following sections.

2.1 Multi-Stage System:

The system is designed to have multiple stages (FIG. 7 or FIG. 8). The first stage (FIG. 1 and FIG. 2) is direct vaporization stage. External thermal energy is used to heat brine liquid and generate vapor directly. External thermal energy can be transferred into this stage either indirectly using heating media, or it can be vapor produced externally. In the first stage, lower temperature intake liquid in condenser will condense the liquid vapor. Once it's heated up to near boiling temperature, it will be released into this stage. It will then be further heated by external heat and generate vapor. Remaining heated brine liquid, at boiling temperature in this stage, will be transferred to next stage for further flash vaporization.

The last stage of the system is the pre-heating stage (FIG. 5 or FIG. 6). Brine liquid (to be discharged) and distilled liquid will flow through this stage at two separate heat exchangers. Intake liquid at ambient temperature enters this stage in opposite direction. Thermal energy remaining in brine liquid and distilled liquid will be transferred to the intake liquid flowing in opposite direction. Brine liquid and distilled liquid temperature will be lowered to near ambient temperature and then released or extracted away for consumption. Intake liquid will absorb thermal energy from the brine liquid and distilled liquid. Its temperature will gradually increase. In effect thermal energy is exchanged between brine liquid and distilled liquid to intake liquid. Minimal thermal energy will be lost. Released liquid (brine liquid and distilled) will be at temperature near ambient temperature.

Between the first and last stages, multiple intermediate stages (FIG. 3 and FIG. 4) are implemented. In these stages, intake liquid will act as coolant in condenser, because its temperature is lower than the stage temperature as it enters the stage. When it leaves the stage, however, it will absorb thermal energy released by the condensed distilled liquid. Its temperature will rise to near stage temperature. Brine liquid and condensed distilled liquid from previous stage will be at higher temperature when just enter this stage. Brine liquid is “superheated” in this stage and it will “flash” evaporate to generate vapor. Condensed distilled liquid is used to heat brine liquid in this stage to generate additional vapor. During the process, condensed distilled liquid will release its excess thermal energy. Its temperature will be lowered to the stage temperature.

2.2 Thermally Shielded and Isolated System:

The system must be thermally shielded to reduce heat loss to the environment. Low thermal conductivity materials can be used in construction of the system. Elements exposed to the environment should be thermally shielded to reduce thermal energy loss. Between stages they should also be thermally shielded to provide thermal isolation. Active heating, by absorbing solar energy or conventional directly controlled heating, can be used to reduce temperature difference between the stage and environment, and therefore reduce thermal loss.

2.3 Dynamically Controlled Operation:

Each stage is dynamically controlled at pre-determined different pressure and temperature. First stage is at highest pressure and temperature. In the second and later stages, temperatures and pressures are progressively lowered to provide pre-determined temperature and pressure differences between stages. At each stage thermal equilibrium temperature and pressure are determined by thermal dynamics.

2.4 Continuous Filtration:

Each stage contains additional filtration to reduce dissolved mineral content. In the last pre-heater stage, original liquid at ambient temperature is first filtered to remove organic and dissolved mineral content. It is then transferred through condenser to provide cooling to condense vapor. In between each stage, addition filtration is added to further remove dissolved mineral content. Original liquid can also be pre-treated chemically and mechanically.

3. Applications

In one embodiment, but not limited to, a solar thermal desalination system can be designed to directly generate freshwater vapor from saltwater, and condense the freshwater vapor into freshwater cooled by ambient saltwater. This system can also be used for saltwater desalination, water purification, and water disinfection near large body of surface water, such as ocean, sea, lake, reservoir, river, etc.

In addition, this method can be applied broadly to any kind of liquid that needs distillation, disinfection, and purification of any water such as brackish water, agricultural runoff, storm runoff water, industrial waste water, or municipal waste water. If it is solar based, it can operate off-grid in remote or less developed areas worldwide. With minor re-configuration, it can also be used to distill, disinfect, purify, or concentrate liquid in other industries such as in chemical engineering, food processing, petroleum engineering, and pharmaceutical production.

3.1 Solar Saltwater Desalination System:

Using solar desalination as an illustrative example, freshwater vapor can be generated from saltwater with Concentrated Solar Panel (CSP). It can include two modes of operation: 1) Direct vapor generation and 2) Indirect vapor generation. In direct vapor generation, saltwater is pumped through thermally evacuated tube directly. Solar energy heat and vaporize saltwater. Pressure and temperature inside evacuated tube is controlled by adjusting the pressure and saltwater flow rate through the tube. In indirect vapor generation, heat transfer medium is heated by CSP solar energy. Heat transfer fluid carries solar energy to each stage to heat up and vaporize saltwater. FIG. 9 or FIG. 10 demonstrate different embodiments of using CSP to desalinate saltwater.

As brine water moves to the next stage it will be heated up by absorbing released latent heat from condensed freshwater vapor. To-be-discharged brine saltwater and condensed freshwater will go through heat exchangers containing intake liquid. Its temperature will be lowered to near ambient temperature and then released. In such counter-circulating heat exchange process, thermal energy will be re-cycled through the system continuously. Minimal thermal energy will be lost to the environment. As more and more thermal energy enters the system, it will be accumulated and intensified. More thermal energy will be available to vaporize and produce freshwater. In effect low intensity or low grade thermal energy such as solar energy or waste energy can be “amplified” to produce larger quantity freshwater.

3.2 Solar Saltwater Desalination Deployment:

Deployment of solar desalination system can be on land near water source, float directly on water surface, or semi-permanently fixed structure near coast. Each CSP and vapor generator/condenser assembly can be connected to form a distributed network. Each unit will operate independent from each. Such distributed system provides additional robustness and reliability. Networked system can be supported on a rigid structure. For water surface installation, the networked system will be floated by flotation devices around the supporting structure to provide buoyancy. For direct installation on seabed, the system will be secured on supporting structure. At opposite corner, a motor powered propeller are connected to the assemble. It is used to control the orientation of each networked assembly to track sun position throughout the day in a floating installation. Angle of CSP is also dynamically adjusted to maximize incident solar energy.

In order to decrease turbulent effect of surface water waves. At the perimeter of the installation, protective buffers are used to reduce wave intensity. As wave pass through such buffers, its energy will be absorbed and reduced by the buffers.

This system can be cascaded into multiple stage water purification system. Previous stage purified water can be sent into next stage water intake pump to provide additional distillation and purification.

Because freshwater is condensed boiling water vapor, if pipelines/condenser/storage tanks are properly sanitized and maintained, purified water can be directly consumed. Portion of the thermal energy can be used to heat freshwater to provide heated freshwater for direct consumption.

Advantages

This disclosure presents a viable solution to generate freshwater at high volume to meet large scale, low cost desalination need. It can also be generalized into broader applications and industries. Thermal energy is used and re-used repeatedly to generate vapor and condense vapor into distilled (or concentrated) liquid. It can in effect “amplify” low intensity energy source such as solar energy or waste heat to significantly increase production yield. It can also be used in broader applications in other industries to improve liquid processing production yield. Applications can benefit from this technology include liquid distillation, disinfection, purification, and concentration in chemical engineering, food processing, petroleum engineering, and pharmaceutical production, etc. Thermal energy source used to generate distilled or concentrated liquid can be solar, fossil fuel, or waste heat from industrial plants. Summaries of some of the key advantages are listed in the following:

• • 1) Counter-circulating vapor generation and condensation to continuously re-use thermal energy to increase production yield.
  • 2) Dynamic pressure and temperature controlled vapor generation and condensation to maximize yield.
  • 3) Highly efficient heat exchange devices to further enhance production yield.
  • 4) Thermally shielded and isolated steam generation and condensation component to reduce heat loss, and to maintain optimal thermal equilibrium state in each stage.
  • 5) Distributed networked system for increased reliability and robustness.
  • 6) Multi-stage high temperature filtration for dissolved minerals and other organic or particular materials.
  • 7) Direct floating installation at water surface.
  • 8) Propelled solar tracking for floating installation.
  • 9) Perimeter wave reduction devices to reduce water wave turbulence to the system.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 illustrates the side view of one embodiment for the first stage of the apparatus. Pressure and temperature controls are not shown for clarity purpose.

FIG. 2 illustrates the top view of the same embodiment as in FIG. 1 for the first stage of the apparatus. For clarity purpose the bottom portion of the stage (heat exchanger to vaporize brine liquid) non-condensable gas and vapor extraction and regulation, and demister are not shown. They can be inferred from side view in FIG. 1. Pressure and temperature controls are not shown.

FIG. 3 illustrates the side view of one embodiment for intermediate stages. Pressure and temperature controls are not shown for clarity purpose.

FIG. 4 illustrates the side view of the same embodiment as in FIG. 3 for the intermediate stages. For clarity purpose the bottom portion of the stage and demister are not shown. They can be inferred from side view in FIG. 3. Pressure and temperature controls are not shown.

FIG. 5 illustrates one embodiment for the last stage, pre-heater stage, in a distillation or desalination configuration. Pressure and temperature controls are not shown for clarity purpose.

FIG. 6 illustrates another embodiment for the last stage, pre-heater stage, in a concentration configuration. Pressure and temperature controls are not shown for clarity purpose.

FIG. 7 illustrates one embodiment of the apparatus in a horizontally connected multi-stage configuration. Pressure and temperature controls are not shown for clarity purpose.

FIG. 8 illustrates another embodiment of the apparatus in a vertically stacked multi-stage configuration. It operates similarly as in FIG. 7 horizontally connected configuration. Pressure and temperature controls are not shown for clarity purpose.

FIG. 9 illustrates one embodiment of the apparatus configuration and application in floating solar thermal desalination configuration. Anchor of the platform to sea floor is not shown for clarify purpose.

FIG. 10 illustrates another embodiment of the apparatus in a distributed, networked configuration for solar thermal desalination.

FIG. 11 illustrates another embodiment of the apparatus utilizing waste heat from power plant or other industrial systems.

DETAILED DESCRIPTION OF THE DRAWINGS

FIG. 1 illustrates the side view of one embodiment of the first stage in the distillation embodiment. In desalination embodiment intake original liquid will be saltwater. The heating medium can be heat transfer medium heated by external heat source, or can be vapor directly.

External thermal energy (from solar or other heat sources) is pumped in to heat and vaporize brine liquid. Brine liquid is already near boiling temperature when it is released from condenser into this stage, because it has circulated through condensers in other stages as coolant. Vapor generated will condense to form distilled liquid. Distilled liquid and remaining brine liquid will be pumped into next stage to heat and vaporize additional brine liquid. Demister is used to filter brine liquid droplets formed during vaporization.

TABLE 2
Side-view of the first vaporization stage numerals and parts
Numeral	Description	Notes
100	Vaporization
	chamber
102	Vapor condenser.	Condenser is cooled by the intake
		liquid. Intake liquid has been used as
		coolant in condensers and heated by
		previous stages. At discharge point
		(116) its temperature will be near
		boiling temperature.
104	Condenser coolant	Pipeline is connected to the output of
	pump and pipeline.	pervious stage's condenser coolant
		output.
106	Distilled liquid	In desalination embodiment distilled
	collection pan.	liquid will be freshwater.
108	Distilled liquid	It is pumped to next stage as heat
	extraction pipeline	source to heat brine liquid (324).
	and pump.
110	Demister.	Used to filter liquid droplets that may
		form when vaporizing original liquid.
112	Pump to distribute	Brine liquid is near boiling
	heated intake	temperature at this point.
	brine liquid from
	condenser output.
114	Pipeline to transport
	heated intake brine
	liquid from
	condenser to
	distribution nozzle.
116	Nozzle to distribute	Brine liquid is near its boiling
	intake brine	temperature. It is then further heated
	liquid for	and vaporized by external heating
	vaporization.	medium circulating in vaporization
		device (122).
118	Boiling brine liquid.	Its temperature is at boiling
		temperature for this stage equilibrium
		state.
120	Pump and pipeline	Medium can be heat transfer medium
	to supply externally	or vapor directly.
	heated heat
	transfer medium.
122	Vaporization device
	to heat and vaporize
	brine liquid in
	first stage.
124	Pipeline and pumps	Brine liquid temperature is at its
	to transfer brine	thermal equilibrium boiling
	liquid to the next	temperature at this stage. It will be
	intermediate stage.	“superheated” for the next
		intermediate stage since next
		intermediate stage's thermal
		equilibrium temperature will be lower.
126	Stage wall and	Insulation can be either passive
	insulating layer.	insulation or active insulation (heated
		by external heat source such as solar
		energy or conventional heat source.)
128	Heat transfer	Heat transfer medium will return to
	medium return	Concentrated Solar Panel to be re-
	pipeline.	heated.
130	Pipeline and	It will enter next stage to provide
	regulator to	additional heating. At meantime vapor
	extract non-	will condense into distilled liquid to be
	condensable gas	extracted. Pressure regulator will
	and to regulate	dynamically adjust the stage's
	stage pressure.	pressure to pre-determined level.

FIG. 2 illustrates the top view of one embodiment for the first stage. For clarity purpose, bottom half of the chamber (heat exchanger to vaporize brine liquid, and associated pipelines and pumps) is omitted. They have similar structure as the top half and can be inferred from side view illustration.

TABLE 3
Top-view of the first vaporization stage numerals and parts
Numeral	Description	Notes
200	Insulated low thermal conductivity	Insulation can be either passive
	chamber for the first stage.	insulation or active insulation (Heated
		by external heat source such as solar
		energy or conventional heat source.)
202	Apparatus wall.
204	Condenser.	It is cooled by intake brine liquid.
206	Distilled liquid collection pan.
208	Nozzle and pipeline to distribute	Brine liquid is already near its boiling
	brine liquid for vaporization.	temperature. It is then further heated
		and vaporized by external heating
		medium circulating in vaporization
		heat exchanger (122).
210	Apparatus chamber.
212	Condenser output.	Intake liquid at near boiling
		temperature is introduced to the first
		stage to be further heated and
		vaporized. It has been used as coolant
		in previous stages' condensers and in
		the first stage as. Its temperature has
		been rising progressively to near
		boiling temperature near the output
		point of the first stage condenser.
214	Pipeline to extract distilled liquid	In desalination embodiment, distilled
	from collection pan.	liquid is freshwater.
216	Pump to extract distilled liquid.
218	Pump and pipeline to transport intake	Coolant (intake liquid) is already
	liquid as coolant for the condenser to	heated by circulating through previous
	the first stage condenser.	stage condensers as coolant.

FIG. 3 illustrates the side view of one embodiment for the intermediate stage in the distillation embodiment. In desalination embodiment intake original liquid will be saltwater. At each of the intermediate stage, equilibrium temperature and pressure of that stage are set at pre-determined, progressively lower level than the temperature and pressure at previous stage. Brine liquid from previous stage will become “superheated” upon entering this stage. It will immediately flash vaporize into distilled vapor in order to maintain proper thermal equilibrium at this stage.

Distilled liquid collected from previous stage will also enter this stage and is used as heating medium to heat brine liquid. Distilled liquid temperature will decrease to reach thermal equilibrium temperature at this stage. In addition, as pipeline containing non-condensable gas, vapor, and distilled liquid flow through intermediate and final stage, it will provide additional heating to brine liquid in each stage.

TABLE 4
Side-view of intermediate stage numerals and parts
Numeral	Description	Notes
300	Output of condenser coolant (intake	Coolant temperature at this stage is
	liquid) into next stage condenser.	lower than the temperature at next
		stage. Hence it can be served as
		coolant to condense liquid vapor.
302	Brine liquid input from previous	Input brine liquid is “superheated”
	stage. It is pumped and distributed	when entering this stage because
	into this stage (318 & 320).	previous stage thermal equilibrium
		temperature is higher.
304	Intermediate stage walls and	Insulation can be either passive
	insulating layer.	insulation or active insulation (Heated
		by external heat source such as solar
		energy or conventional heat source.)
306	Condenser.	It is cooled by intake liquid.
308	Pipeline and pump to transport
	intake liquid (coolant) through
	condenser.
310	Distilled liquid collection pan.
312	Distilled liquid transport pipeline to	In desalination embodiment distilled
	merge into main distilled liquid	liquid will be freshwater.
	pipeline.
314	Demister to filter out brine droplets
	may form during vaporization.
316	Intermediate stage chamber.
318	Pipeline, pump, and spray nozzle to	“Superheated” liquid will quickly
	distribute brine liquid from previous	vaporize (“flash vaporize”) when
	stage.	entering a lower pressure and
		temperature region.
320	Spray nozzle to “flash” vaporize part	“Superheated” liquid will quickly
	of brine liquid.	vaporize (“flash vaporize”) when
		entering a lower pressure and
		temperature region.
322	Brine liquid.	It is at boiling point for this stage's
		pressure and temperature. It is being
		further heated by the distilled liquid
		transported from previous stage.
		Distilled liquid from previous stage is
		at higher temperature than brine liquid
		at this stage. Hence it can further
		vaporize some of the brine liquid in
		this stage.
324	Main pipeline and pump to combine	Distilled liquid temperature will
	and transport collected distilled	gradually be lowered as it circulates
	liquid.	through each intermediate stage to
		heat brine liquid and release its
		thermal energy to vaporize brine
		liquid.
326	Combiner to combine distilled liquid
	generated in this stage and from
	previous stage.
328	Heat exchanger to heat and vaporize	Distilled liquid from previous stage is
	brine liquid.	at higher temperature than the
		equilibrium temperature at this stage.
		Therefore, it can be used to further
		heat and vaporize brine liquid.
330	Pipeline and regulator to transport	It will enter next stage to provide
	non-condensable gas, vapor, and	additional heating. At meantime vapor
	distilled liquid to next stage.	will condense into distilled liquid to be
		extracted. Pressure regulator will
		dynamically adjust the stage's
		pressure to pre-determined level.
332	Pipeline and pump to transport
	distilled liquid to next stage.
334	Combiner, pipeline, and stage	Intake pipeline takes in current stage
	gas/vapor intake line.	non-condensable gas and vapor. They
		are combined in combiner with
		previous stage's non-condensable gas,
		distilled liquid, and vapor.

FIG. 4 illustrates the top view of one embodiment for the intermediate stage. For clarity purpose, bottom half of the chamber (distilled liquid heat exchanger, demister, pipelines, and pumps) is omitted. They have similar structure as the top half and can be inferred from the side view illustration.

TABLE 5
Top-view of intermediate stage numerals and parts
Numeral	Description	Notes
400	Apparatus wall
402	Apparatus insulation layer.	Insulation can be either passive
		insulation or active insulation (Heated
		by external heat source such as solar
		energy or conventional heat source.)
404	Distilled liquid collection pan.
406	Condenser.
408	Pipeline and pump to transport and
	distribute brine liquid from previous
	stage to this stage.
410	Apparatus chamber.
412	Output of condenser coolant (intake	Coolant is the intake liquid from
	liquid) to next stage condenser.	previous stage condenser. At output its
		temperature will be at thermal
		equilibrium boiling temperature for
		this stage.
414	Main condenser pipeline and pump	When distilled liquid leaving this stage
	to collect and transport distilled	its temperature will be at equilibrium
	liquid.	temperature of this stage.
416	Pipeline and pump to transport	Entering intake liquid will have lower
	condenser coolant (intake liquid).	temperature than the equilibrium
		temperature at this stage.

FIG. 5 illustrates the side view of one embodiment for the last stage (pre-heater stage) in distillation embodiment. In desalination embodiment intake original liquid will be saltwater and distilled liquid will be freshwater.

Intake original liquid is pumped to this stage from the environment or external storage at ambient temperature. Discharged brine liquid and distilled liquid are pumped through this stage in opposite direction in heat exchangers. Remaining heat from discharged brine liquid and condensed distilled liquid are transferred to intake original liquid. Discharged liquid and condensed liquid will be pumped away at near ambient temperature. At this stage essentially all remaining thermal energy above ambient thermal energy level in distilled and discharged brine liquid is recovered.

Pipeline and pump transporting non-condensable gas will also flow through this stage.

For clarity purpose it is not shown in the drawing. Distilled liquid from previous stage extracted through this path is combined with other distilled liquid before entering the last pre-heater stage. It is also not shown for clarity purpose.

TABLE 6
Side-view of the last stage (pre-heater) numerals and parts descriptions
Numeral	Description	Notes
500	Pump and pipeline to extract heated	Intake liquid has absorbed heat from
	intake original liquid,	distilled and brine liquid. Its
		temperature has risen from ambient
		temperature.
502	Pipeline to transfer distilled liquid	In desalination configuration distilled
	from previous intermediate stage to	liquid will be freshwater and original
	the last pre-heater stage,	liquid will be saltwater.
504	Thermal insulating layer.	Insulation can be either passive
		insulation or active insulation (Heated
		by external heat source such as solar
		energy or conventional heat source.)
506	Pre-heater last stage wall.
508	Heat exchanger containing distilled
	liquid.
510	Pre-heater (last stage) heat	Colder intake liquid will be near the
	exchange chamber holding intake	bottom while warmed up intake liquid
	original liquid,	will rise to the top of the chamber.
512	Heat exchanger containing distilled
	liquid.
514	Pipeline to introduce intake original
	liquid into pre-heater stage.
516	Pump and pipeline to transport
	distilled liquid.
518	Pipeline and pump for intake liquid.
520	Pump and pipeline for discharged	Discharged brine liquid temperature
	brine liquid,	will be near ambient temperature.
522	Re-mixer to mix brine liquid with	At pre-determined level part of the
	intake liquid.	brine liquid can be re-introduced into
		intake liquid circulation flow.
524	Pipeline to transport to be
	discharged brine liquid from
	previous intermediate stage.

FIG. 6 illustrates the side-view for the last stage (pre-heater stage) in concentration embodiment.

Intake original liquid is pumped to this stage from the environment or external storage at ambient temperature. Distilled liquid is pumped through this stage in opposite direction in heat exchanger. Remaining heat from condensed distilled liquid is transferred to intake original liquid. Condensed distilled liquid will be pumped away at near ambient temperature. Brine liquid will be re-circulated back into condenser as coolant. Brine liquid may also be mixed with intake liquid to be introduced into condenser as coolant. Once pre-determined concentration level is reached, brine liquid will be pumped away. At this stage essentially all remaining thermal energy above ambient thermal energy level in distilled is recovered.

Pipeline and pump transporting non-condensable gas will also flow through this stage. For clarity purpose it is not shown in the drawing. Distilled liquid from previous stage extracted through this path is combined with other distilled liquid before entering the last pre-heater stage. It is also not shown for clarity purpose.

TABLE 7
Side-view of the last (pre-heater) stage numerals and parts descriptions in
liquid concentration embodiment
Numeral	Description	Notes
600	Pump and pipeline to transport	Brine liquid and intake liquid mixing
	heated intake original liquid from	ratio can be pre-determined.
	pre-heater. It can also combine
	brine liquid with intake liquid back
	to condenser (616).
602	Pipeline to transfer distilled liquid
	from previous intermediate stage to
	the last, pre-heater stage.
604	Thermal insulating layer.	Insulation can be either passive
		insulation or active insulation (Heated
		by external heat source such as solar
		energy or conventional heat source.)
606	Last, pre-heater stage wall.
608	Pre-heater chamber holding intake	Colder intake liquid will be near the
	original liquid,	bottom while warmed up intake liquid
		will rise to the top of the chamber.
610	Heat exchanger.	Distilled liquid in the exchanger will
		transfer its thermal energy to intake
		original liquid. Its temperature will be
		lowered to near ambient temperature
		near exit.
612	Pipeline and pump to transport
	distilled liquid.
614	Pipeline and pump to transport	Intake original liquid is at ambient
	intake original liquid.	temperature.
616	Pipeline to transport brine liquid	Brine liquid and intake liquid ratio can
	from intermediate stage back into	vary according to pre-determined
	mixing with intake liquid (600).	ratio.

FIG. 7 illustrates multiple stage horizontally connected embodiment. Different stages can be connected physically together or connected through insulated pipelines and pumps. Temperature and pressure controller for each stage are not shown for clarity purpose.

Intake liquid will be pumped into the last (pre-heater) stage. It will be filtered for organic, particular, and dissolved contents through a series of filtration devices. Intake liquid will enter into condenser circulation as coolant. As it moves through different stages it will absorb latent heat released by condensing vapor. At the first stage condenser output, its temperature will be close to boiling temperature and released into first stage. Once the liquid enters into first stage, it will be heated and vaporized partially by thermal energy provided by external sources such as solar, conventional fossil heat, or waste heat.

Distilled liquid will be pumped into next stages as heat source. As it moves through different stages and release its thermal energy, its temperature will gradually drop. At the last stage, most remaining thermal energy in distilled liquid will be transferred to intake liquid. Distilled liquid will be pumped away at near ambient temperature.

Brine liquid, as it moves into the next stage, will be partially flash evaporated. Its thermal energy will be gradually transferred to coolant in condenser (i.e. intake liquid). Its temperature will be progressively lowered. At the last stage, remaining thermal energy above ambient thermal energy level will be mostly transferred to intake liquid. It will be released at near ambient temperature.

TABLE 8
Multi-stage connected embodiment numerals and parts descriptions
Numeral	Description	Notes
700	Distilled liquid collection pan.
702	Stage walls and thermal insulating	Insulation can be either passive
	layer for each stage.	insulation or active insulation (Heated
		by external heat source such as solar
		energy or conventional heat source.)
704	Stage chamber.	Thermal equilibrium temperature and
		pressure at each stage are controlled at
		pre-determined. progressively lowered
		levels. Temperature and pressure
		controller for each stage are not shown
		for clarity purpose.
706	Condensers.	Condenser coolant (intake liquid) will
		absorb latent heat released by vapor as
		it condenses vapor at different stages.
		Its temperature will progressively rise.
708	Filtration devices.
710	Pump and pipeline to extract brine
	liquid from the last intermediate
	stage to the last, pre-heater stage.
712	Additional intermediate stages can
	be added according to different pre-
	determined operating parameters.
714	Pump and pipeline for intake liquid.	Intake liquid circulates through
		condensers as each stage as coolant to
		condense distilled vapor. Between
		stages it will undergo further filtration
		(708).
716	Last (pre-heater) stage wall and	Insulation can be either passive
	insulating layer.	insulation or active insulation (Heated
		by external heat source such as solar
		energy or conventional heat source.)
718	Heat exchanger containing to-be-
	discharged brine liquid.
720	Last, pre-heater stage chamber	Colder intake liquid will be near the
	holding intake liquid.	bottom while warmed up intake liquid
		will rise to the top of the chamber.
722	Pump and pipeline to transport
	discharged brine liquid.
724	Pump and pipeline for intake
	original liquid.
726	Pump and pipeline to extract	Discharged brine liquid temperature is
	distilled liquid.	near ambient temperature.
728	Heat exchanger containing distilled
	liquid.
730	Pump to extract distilled liquid.
732	Combiner to combine distilled
	liquid from current stage collection
	pan and distilled liquid from
	previous stages.
734	Heat exchanger containing distilled	Distilled liquid from previous stage
	liquid.	has higher temperature than current
		stage's brine liquid temperature.
		Therefore, it can be used to heat and
		vaporize additional vapor.
736	Demister to filter brine liquid
	droplet.
738	Brine liquid.	At each stage its temperature is at
		stage's boiling temperature.
740	Pipeline and pump for transferring	Pump omitted in drawing to aid
	of distilled liquid between stages.	clarity.
742	Pipeline and pump for transferring	Pump omitted in drawing to aid
	of brine liquid between stages.	clarity.
744	Pipeline and pump for external	Heating medium can be heat transfer
	heating medium entering heat	medium or vapor. Pump omitted in
	exchanger.	drawing to aid clarity.
746	Pipeline and pump for external	Heating medium can be heat transfer
	heating medium returning to	medium or vapor. Pump omitted in
	external heating source.	drawing to aid clarity.
748	Pipeline and nozzle to distribute	Dispenser omitted in drawing to aid
	intake liquid from condenser.	clarity. Intake brine liquid has been
		heated to near boiling temperature
		when entering the first stage.

FIG. 8 illustrates another embodiment of the apparatus in vertically stacked multi-stage configuration. Pipelines and pumps can be either internal to the stacks or on the exterior of the chamber walls. It operates similarly to the embodiment illustrated in FIG. 7.

TABLE 9
Multi-stage vertically “stacked” embodiment numerals and parts descriptions
Numeral	Description	Notes
800	Apparatus exterior walls and	Insulation can be passive or actively
	insulating layers.	heated insulation by either solar or
		conventional heating.
802	Condenser.	Heated intake brine liquid is
		distributed to the first stage when it is
		near boiling temperature (842).
804	Continuous filtration devices	To continuously remove particular
		materials and dissolved mineral
		contents.
806	Heat transfer medium input into	Heat transfer medium can be indirect
	vaporization device.	heating using heat transfer medium or
		direct vapor heating.
808	Distilled liquid collection pan.	In desalination distilled liquid is
		freshwater.
810	Demister.	To filter out brine liquid droplets
		formed during vaporization.
812	Brine liquid.	Its temperature is at stage's thermal
		equilibrium temperature.
814	Pipelines and pumps to extract and	Distilled liquid is used in each
	transport distilled liquid.	intermediate stage to further heat the
		brine liquid until its temperature is
		near ambient environment temperature
		near exit outlet.
816	Additional filtration devices can be
	connected to additional
	intermediate stages.
818	Additional intermediate stages can
	be connected to add more stages at
	pre-determined operating
	parameters.
820	Pipeline and pump to transport	Intake brine liquid is pre-heated from
	intake liquid to next stage	ambient temperature by to be
	condenser.	discharged brine liquid and distilled
		liquid.
822	Heat exchanger for brine liquid.
824	Last Pre-heater stage walls and
	insulating layer.
826	Pump to transport brine liquid to	Discharged brine liquid temperature
	discharge.	will be near ambient temperature when
		exiting the last stage.
828	Pipeline and pump to transport
	intake liquid into the last pre-heater
	stage.
830	Pipeline and pump to transport
	distilled liquid pre-heater stage.
832	Heat exchanger for distilled liquid.
	Pipeline and pump (830) will
	transport distilled liquid to the last
	pre-heater stage.
834	Combiner, pipeline, and pump to
	combine and transport distilled
	liquid.
836	Pipeline, pump, & brine liquid	Details of pump and spray nozzle are
	spray nozzle to distribute brine	not shown for clarify.
	liquid to the next intermediate
	stage.
838	Heat transfer medium return
	(output) pipeline and pump.
840	Vaporization device to generate	Vaporization device is heated by
	distilled liquid vapor.	externally heated heat transfer
		medium.
842	Pipeline, pump, and spray nozzle to	Intake brine liquid, after being used as
	distribute intake brine liquid from	coolant at different stages' condensers,
	condenser in the first stage.	its temperature will be near boiling
		temperature when exit the condenser.

FIG. 9 illustrates one embodiment of using Concentrated Solar Panel (CSP) to heat saltwater to generate distilled freshwater. The unit is mounted on a floating platform that can be deployed directly on water surface.

Solar energy is concentrated by Concentrating Solar Panel (CSP). One embodiment of using parabolic reflective panel is used as example. Heated heat transfer medium is pumped into the apparatus as heat source. It will vaporize saltwater and produce freshwater. Floatation devices can be attached to the system to provide buoyancy at water surface. The platform can also be constructed to provide buoyancy. CSP and the apparatus are secured on rigid structure to the platform. The floating platform can also track intraday sun movement through motorized propelling devices attached to the platform on opposite sides.

TABLE 10
Concentrated Solar Panel (CSP) desalination embodiment numerals and
parts descriptions
Numeral	Description	Notes
900	Supporting and solar tracking	Solar tracking structure and
	structure for CSP.	mechanism are not shown in the
		illustration for clarity purpose.
902	Concentrated Solar Panel (CSP).	CSP can be parabolic or flat Fresnel
		types CSP panel.
904	Evacuated solar tube to collect solar	Solar heat is concentrated and used to
	energy.	heat transfer medium in the evacuated
		tube.
906	Pipeline and pump to transfer	Pump and pipeline details are not
	heated heat transfer medium into	shown.
	the apparatus to generate distilled
	vapor and liquid.
908	Return pipeline and pump to
	transfer heat transfer medium back
	to evacuated solar tube.
910	Apparatus to generate distilled
	vapor and liquid, or concentrated
	liquid.
912	Multiple CSP can be connected to
	form a larger system.
914	Pipeline and pump to transfer	Distilled liquid is at near ambient
	distilled liquid.	temperature after transferring
		remaining excessive heat above
		ambient thermal energy level back to
		intake liquid.
916	Pipeline and pump to supply intake
	liquid
918	Floatation devices and motorized	Discharged brine liquid is at near
	propelling devices attached to the	ambient temperature. Motorized
	platform to provide buoyancy.	propellers can be added to rotate the
		platform in order to track sun
		trajectory throughout the day.
920	Floating platforms can be extended
	to accommodate multiple units.
922	Platform to provide structure	Itself can serve as floatation or liquid
	support for all the CSP, apparatus,	storage device.
	pipeline, pumps, and other devices.
924	Storage tanks to hold distilled	Storage tank can also provide
	liquid.	additional buoyancy to the platform.
926	Pipeline and pump to discharge	Discharged brine liquid is at near
	brine liquid.	ambient temperature.
928	Anchor to hold platform and	In floating installation the platform
	structure in position.	can be rotated.
930	Supporting structure for CSP.

FIG. 10 illustrates one embodiment of using multiple CSP panels to desalinate saltwater. CSP panels are connected to provide concentrated heat transfer medium to heat and vaporize salt water in an apparatus. The number of CSP panels is flexible. It can be as large as a CSP field in centralized desalination plant. Or it can be assembled into sub unit to provide distributed, but networked desalination system.

Multiple CSPs can be combined to form a sub-system. Heated heat transfer medium from each unit is combined and then pumped into the apparatus to produce freshwater from saltwater. It can also be used for other liquid processing using solar energy.

TABLE 11
Distributed solar desalination system numerals and parts descriptions
Numeral	Description	Notes
1000	Concentrated Solar Panel (CSP).
1002	Evacuated solar tube to heat heat
	transfer medium.
1004	Pipeline and pumps to collect and	Details and pumps are not shown for
	transport heated heat transfer	clarity purpose.
	medium.
1006	Pipeline and pumps for return and	Details and pumps are not shown for
	re-distribute of heat transfer	clarity purpose.
	medium from the apparatus.
1008	Apparatus to generate distilled
	liquid or concentrated liquid.
1010	Pipeline and pump to extract	In desalination embodiment distilled
	distilled liquid.	liquid is freshwater. Details and
		pumps are not shown for clarity
		purpose.
1012	Pipeline and pump to supply intake	In desalination embodiment intake
	liquid.	liquid is saltwater. Details and pumps
		are not shown for clarity purpose.
1014	Pipeline and pump to discharge	Discharged brine liquid will be at near
	brine liquid.	ambient temperature. Details and
		pumps are not shown for clarity
		purpose.

FIG. 11 illustrates one embodiment of using waste heat discharged from industrial plant to power the apparatus to generate distilled liquid.

Waste heat is used to heat and vaporize brine liquid or saltwater to generate distilled liquid or freshwater respectively.

TABLE 12
Desalination system using waste vapor numerals and parts descriptions
Numeral	Description	Notes
1100	Pipeline and pump to extract	Generally, liquid condensed from
	condensed distilled waste vapor	waste vapor from power plant should
	liquid for further processing.	be separated from the distilled liquid
		produced by the apparatus. Pump is
		not shown for clarity purpose.
1102	Pipeline to supply vapor from
	discharged waste vapor from
	industrial plant.
1104	Regulator to control the pressure
	and flow rate of waste vapor.
1106	Water supply to steam generator
	(1108).
1108	Steam generator.
1110	High pressure steam to drive
	generator.
1112	Power generator or other industrial
	equipment.
1114	Waste steam (vapor) pipeline and
	pump.
1116	Distilled liquid output pipeline and
	pump for consumption.
1118	Intake liquid input pipeline and	Intake liquid will be at ambient
	pump.	temperature.
1120	Pipeline and pump to transport to-
	be-discharged brine liquid.
1122	The apparatus to generate distilled
	liquid or concentrate liquid.

CONCLUSION, RAMIFICATIONS, AND SCOPE

As demonstrated in this disclosure, the apparatus and methods can be used broadly in many different types of applications, including solar thermal desalination. It is based on solid physical principles. It can significantly increase energy use efficiency and production yield. With retro-fitting, systems and applications in use today can be upgraded to drastically improve its energy use efficiency and production yield, including many currently deployed thermal desalination plants based on MED and MSF.

In summary, the said apparatus and methods can provide many significant advantages over current best available technologies to desalinate, distill, disinfect, purify, or concentrate liquid:

• • 1) It can significantly increase energy use efficiency and production yield in liquid processing. In current MED or MSF systems, thermal energy re-use is limited. With continuous re-use and accumulation of thermal energy, their efficiency can increase significantly. Production yield using the same amount of thermal energy will also be significantly increased.
  • 2) It can use renewable energy source such as solar energy or low grade waste heat to power liquid processing.
  • 3) When combined with concentrated solar energy, it can provide virtually unlimited supply of freshwater worldwide at high production yield. Because of high production yield, and low cost construction, maintenance, and operation, it can provide unlimited amount of freshwater at highly competitive price to current municipal water supply.
  • 4) When combined with solar energy, it is very environmentally friendly and sustainable. It does not release harmful chemicals to the environment. Disturbance to the environment is minimal. In solar desalination released brine water is near ambient temperature. Released brine water is broadly distributed to large areas. Its intake of saltwater is small “sip”. Its released brine water just has slightly more salt concentration than ambient saltwater. Released brine water temperature is near ambient temperature.
  • 5) Its construction and deployment is simple and reliable.
  • 6) It offers option to install and deploy in different locations, even include direct water surface installation. With water surface installation, it can be deployed in less intrusive or environmentally impactful locations. Because of its modular, distributed design, units can be installed at different types of locations to meet local requirement.
  • 7) With solar energy as thermal energy source, it can operate “off-grid” in remote and un-developed locations. There is minimal dependency or pre-requirement to infrastructure such as electrical grid.
  • 8) With boiling of water to generate freshwater vapor, freshwater produced is already sanitized. It can be directly consumed, if the system and pipelines are properly maintained.
  • 9) Because of the simple design and construction, the system is high reliable and robust. Materials used can be long lasting. In turn it will significantly reduce long term operation and maintenance cost.
  • 10) Its modular, distributed, networked design can scale to different requirement. They can be custom tailored to local needs. As need changes, they can be scaled up or down quickly. Investment can be re-deployed.

Although the descriptions above contain many specificities, these should not be construed as limiting the scope of the embodiments but as merely providing illustrations of some of several embodiments. For example, the apparatus could be designed and constructed using different configurations in addition to illustrated horizontally connected or vertically stacked configurations. The apparatus could be designed and constructed using widely available different materials, shapes, configurations, or techniques, not limited to the above described materials, shapes, configurations or techniques. Heat source could be of many different types and generated through different means, in addition to solar energy or waste heat. Liquid to be processed could be of many different types and for different applications, not just limited to desalination, disinfection, purification, or concentration purposes. Thus the scope of the embodiments should be determined by the appended claims and their legal equivalents, rather by the examples given.

Claims

1. A method to desalinate, distill, disinfect, purify, or concentrate original liquid by repeatedly re-using thermal energy, comprising

2. A multi-staged apparatus in claim 1 further including heating original liquid to generate vapor and condensing vapor into separated liquid. It further comprises of plurality of vaporization devices, condensers, tanks, and means to control pressure, temperature, vapor and liquid flow rates, etc. at each stage.

3. A method in claim 1 further including re-using thermal energy by means of counter-circulating condensed liquid, brine liquid, and vapor in opposite direction of original liquid in plurality of stages.

4. A method in claim 1 further including reducing thermal loss to the environment and increasing thermal isolation between stages by means of method or plurality of methods selected from a group of the following methods: 1) Using low thermal conductivity materials2) Thermal shielding3) Solar energy absorbing coating applied to the apparatus4) Vacuum shielding5) Controlled heating of the apparatus.

5. A method in claim 1 further including generating vapor by means of externally heated heat transfer medium circulating through brine liquid in the first stage. A demister is used to separate brine liquid droplets in the stage from mixing with distilled vapor.

6. A method in claim 1 further including generating additional vapor by means of plurality of vapor generation stages. At each stage, pressure and temperature is controlled to provide progressively lower temperature and pressure at each stage from the first stage to the last stage. At each stage A demister is used to separate brine liquid droplets in the stage from mixing with distilled vapor.

7. A method in claim 1 further including optimally maintained pressure and temperature at each stage by means of dynamically adjusting predetermined pressure and temperature.

8. An apparatus in claim 1 further including high heat transfer efficiency vaporization devices and condensers in plurality of stages, with or without device surface treatment.

9. A method in claim 1 further including removing non-condensable vapor in each stage by means of extraction. Condensable distilled vapor extracted together with non-condensable gas will be condensed into distilled liquid in the next stages.

10. A method in claim 1 further including pre-heating intake original liquid by means of heat extracted from condensed distilled liquid, discharged brine liquid, and vapor.

11. A method in claim 1 further including continuously removing organic, particular, and dissolved mineral content in original liquid at plurality of stages by means of filtration.

12. A method in claim 1 further including desalinating or disinfecting original water into consumable freshwater. In one exemplary embodiment intake water can be drawn from ocean, sea, bay, river, lake, waste water, or runoff water that require desalination or disinfection.

13. A method in claim 1 further including concentrating original liquid. In one exemplary embodiment, brine liquid is mixed with intake original liquid or continuously re-introduced as intake liquid to continue the concentration process till reaching predetermined concentration level.

14. An apparatus in claim 1 further including using concentrated solar energy as heat source. In one exemplary embodiment concentrated solar energy is used to heat transfer medium to be used to heat and vaporize original liquid. In another exemplary embodiment concentrated solar energy is used to heat original liquid directly to generate distilled vapor to be used to heat and further vaporize original liquid.

15. A method in claim 1 further including using fossil fuel, low grade heat, or released steam from industrial plants to provide thermal energy to vaporization liquid for desalination, distillation, disinfection, purification, or concentration.

16. A distributed and networked system to deploy liquid desalination, disinfection, distillation, purification, or concentration system on land or at water surface, comprising

17. An apparatus in claim 16 further including a networked system with inter-connected module to form a larger network.

18. A method in claim 16 further including floating the system at water surface by means of attaching flotation devices, or directly using pipelines and storage devices in the apparatus as flotation devices.

19. An apparatus in claim 16 further including a solar tracking mechanism for intra-day solar movement. Motorized propellers attached to opposite side of the system can rotate the system floating at water surface to track intra-day sun movement by means of predetermined program and plurality of sensors.

20. An apparatus in claim 16 further including water wave reduction by means of a perimeter wave reducing devices around the deployed system at water surface.