Counter circulating liquid processing system by repeatedly re-using thermal energy

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims the benefit of provisional patent application Ser. No. 62/175,358, filed Jun. 14, 2015 by the present inventor.

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) Direct Heating and Vaporization Stage: Solar, fossil fuel, or industrial waste heat is used to directly heat and vaporize original liquid in the first stage. Heating can be provided by heat transfer medium flow through heat exchanger in the first direct heating stage, or by vapor, or by liquid produced externally using renewable energy, industrial waste heat, or conventional heat source.
- 2) Flash Vaporization Stages: Middle section of intermediate stages rely on flash vaporization to produce additional distilled vapor. At each stage saturation pressure and temperature are maintained at progressively lower level. Therefore, heated original liquid (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 occurring in the first directing heating stage.
- 3) High thermal efficiency vaporization device can be 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 can be employed to increase heat exchange between vapor and condenser. Different techniques include: (a) Increase condenser heat exchange surface area; (b) Design different geometric configuration of heat exchanger; (c) Apply hydrophobic coating to exchanger exterior surface; (d) Use higher thermal conductivity materials to construct thermal exchanger.
  
  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. Thermal insulation and isolation can be accomplished by the combination of: a) using low thermal conductivity materials for stage exterior wall; b) adding thermal shield to the exterior wall and other components (pipelines, valves, regulators, and pumps) of the stage; c) applying surface coating to increase heat absorption from the environment, d) enclosing the stage in a vacuum chamber to reduce convective heat loss to the environment; e) adding active heating to the exterior of the stage to reduce temperature difference between stage exterior wall and the environment.

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.

Number	Name	Date	Kind
4475988	Tsumura	Oct 1984	A
6391162	Kamiya	May 2002	B1
6607639	Longer	Aug 2003	B1
9834454	Frolov	Dec 2017	B2
20060272933	Domen	Dec 2006	A1
20150158740	Hurtado	Jun 2015	A1
20150329378	Polk, Jr.	Nov 2015	A1
20170275182	Alshahrani	Sep 2017	A1

Counter circulating liquid processing system by repeatedly re-using thermal energy

Information

Patent Number

Date Filed

Date Issued

Inventors

Original Assignees

Examiners

CPC

Field of Search

US

CPC

International Classifications

Term Extension

Abstract

Description

Claims

US Referenced Citations (8)

Related Publications (1)