WO1988004193A1 - Systeme de purification des liquides - Google Patents

Systeme de purification des liquides Download PDF

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Publication number
WO1988004193A1
WO1988004193A1 PCT/US1987/003173 US8703173W WO8804193A1 WO 1988004193 A1 WO1988004193 A1 WO 1988004193A1 US 8703173 W US8703173 W US 8703173W WO 8804193 A1 WO8804193 A1 WO 8804193A1
Authority
WO
WIPO (PCT)
Prior art keywords
liquid
refrigerant
vapor phase
phase
heat exchange
Prior art date
Application number
PCT/US1987/003173
Other languages
English (en)
Inventor
Frank W. Hoffman
Original Assignee
Hoffman Frank W
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hoffman Frank W filed Critical Hoffman Frank W
Publication of WO1988004193A1 publication Critical patent/WO1988004193A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/06—Flash evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/007—Energy recuperation; Heat pumps
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B29/00—Combined heating and refrigeration systems, e.g. operating alternately or simultaneously
    • F25B29/003—Combined heating and refrigeration systems, e.g. operating alternately or simultaneously of the compression type system

Definitions

  • the subject of this invention is the separation of impurities from liquids employing phase changes in the liquid and refrigerative circuits.
  • impurities may be solid, liquid, or gaseous in nature.
  • Materials to be removed may be dissolved as a solute, dispersed as a suspension, emulsified, such as an oil in water, or blended as two or more liquids.
  • Phase changes may include any combination of changes of state between the solid, liquid, and vapor phases and are not limited to a single change of state but may include several phase changes of a mixed variety.
  • any suitable refrigerant may be used such as the freons, ethane, propane, n-butane, ammonia, carbon dioxide, ethylene, propylene, and others. It is also possible to use the same liquid for the refrigerant as the liquid being purified. For example, pure water could be used in the refrigerative circuit when purifying seawater.
  • This invention applies to, but is not limited to, desalination of seawater, ultrapurification of water, purification of industrial wastestreams, drying of numerous chemical residues and sludges, drying of chemicals, processing of raw materials, food preparation, processing, concentration, sterilization, and many others.
  • phase exchange systems of fundamental concern to the end user are capital cost and cost of operation. This invention significantly lowers both the cost of the equipment as well as the expense or running it.
  • inventive aspects are independent of the nature of the refrigerant, type of compression, be it mechanical, electrical, chemical, or thermal, and process application.
  • phase change driving force is provided by a freon refrigeration system compressing a closed circuit with a liquid refrigerant metering device, an evaporative heat exchanger, a refrigerant vapor compressor, and a condensing heat exchanger.
  • the condenser is immersed in the water to be purified and the evaporator located such that it may condense the vapor produced by the boiling water and collect the purified water.
  • the reaction must take place in an environment of suitable pressure such that the water will boil and furthermore appropriate means must be provided to remove the excess heat energy introduced into the system by the refrigeration circuit.
  • the following numerical example illustrates a single stage system using a commercially available compressor with the resultant, capacity expected and energy consumed.
  • a nominally 10 hp discus type piston compressor will provide 261,000 btu/hr of refrigeration when operating between an evaporating temperature of S5°F and a condensing temperature of 70°F with a total power consumption of 4.31 kwh.
  • the amount of heat required to be removed from water vapor to condense it under these conditions is approximately 1056 btu/lb. Calculations show that such a system in simple form would yield 710 gallons per day of purified water at a compressor energy expenditure of approximately 150 kwh/1000 gallons.
  • Commercial data on the compressor also shows the closer the evaporating temperature is to the condensing temperature of the system, the greater the ratio of refrigeration capacity to energy consumption.
  • CAPACITY 710 1420 2130 2840 3550 (GPD)
  • staging can be accomplished directly without the use of a circulating heat transfer liquid and the associated pumping, thereby reducing capital cost and energy. Also, because the heat transfer is accomplished by simultaneous phase changes on either side of the heat exchanger there is a very small sensible heat exchange contribution and therefore each stage can operate over a much smaller temperature difference. For the same operating conditions of the compressor more stages are possible thereby further reducing operating and capital costs.
  • the liquid purification system of the present invention consists of a series of interconnected chambers, each representing one process stage. Within each chamber is a divider to keep the process feed separate from the process product. The arrangement is such that the divider allows free flow of process vapor from the feed region to the product region.
  • the vapor regions are connected in such a manner to each other that the proper pressure equilibrium is established.
  • the feed regions of each chamber are connected such that feed may flow into one chamber and sequentially through each chamber until the concentrated feed is extracted from the last stage. Provision is made to extract the product independently from each chamber and/or combine them if required into a single stream. If required for special separation needs, the product from one chamber may be used as the feed to the next.
  • the invention employs a refrigerative circuit in which gas generated by evaporation of a refrigerant fluid at a low pressure is compressed in the usual way by an appropriate power driven compressor. Compressed gas is then condensed, by giving out heat to evaporate a portion of the feed water to be purified, but according to this invention instead of the usual known single expansion back to the initial low pressure for re-evaporation it is made to cascade through a series of expansions to progressively diminishing pressures before ultimately reaching the initial low pressure.
  • refrigerant fluid in the downwards cascade is condensed, evaporated, recondensed and re-evaporated and so on for several stages until finally it reaches the bottom pressure and temperature where the final evaporation occurs for return to the compressor.
  • each stage the refrigerant fluid is first condensed and then evaporated, heat being extracted from the refrigerant in the first half-stage and supplied to the refrigerant in the second half-stage.
  • the heat extracted in the first half stage is celivered to feed water to be purified, the boiling temperature of the feed water being below the condensing temperature of the refrigerant.
  • condensing refrigerant causes pure water vapor to boil off.
  • the pure water vapor is free to pass to the second half-stage, where the refrigerant fluid has been expanded to a lower pressure and temperature than it was in the first half-stage, and where the refrigerant coil is not submerged.
  • the water vapor condenses on the outside surface of the refrigerant coil, re-evaporating refrigerant for conveying to the coil in the next first half stage.
  • thermodynamic principles It is achieved in this invention by the appropriate arranging of control passages and heat exchangers provided for the refrigerant fluid and processed liquid by the invention.
  • the invention also includes a separate secondary heat transfer circuit which rejects energy from the main refrigerant and process fluid circuits so as to maintain the operation at a desired steady condition.
  • the drawing is a schematic illustration of the essential components of the apparatus and process of the present invention.
  • the liquid purification system 70 comprising chambers 5, 14, and 25 arranged as stages in the system 70.
  • Each chamber is divided by a barrier 6, 16, and 59, respectively, thus dividing the chambers into two half-stage regions.
  • the first half of each chamber will be referred to as feed regions 4, 13, and 21, while the other halves of each chamber will be referred to as product regions 8, 19, and 24.
  • Each chamber 5, 14 and 25 has the feed and product regions connected by a vapor passage 7,16a , and 22, respectively.
  • Each chamber is operatively connected to the atrrosphere via passage 29, a pressure regulating device 28, a passage 27, and passages 26, 20 and 11.
  • the device 28 is a vacuum pump.
  • Passages 11, 20 and 26 are sized so as to allow removal of non-condensable gases from the system yet allow the three chambers to maintain their individual thermodynamic balance.
  • the refrigerative circuit in this example consists of a suction line 3, a compressor 2, a discharge line 1, an initial stage feed heat exchanger 31, a restrictive passage 33, initial stage product heat exchanger 35, a passage 37, a middle stage feed heat exchanger 38, a restrictive passage 40, a middle stage product heat exchanger 41, a passage 43, a final stage feed heat exchanger 44, a restrictive passage 46, a final stage product heat exchanger 48, and a passage 60.
  • Suction line 3-suitable metal tubing Suction line 3-suitable metal tubing, compressor 2-conventional piston type refrigeration compressor, discharge line 1 - suitable metal tubing, heat exchangers 31, 35, 28, 41, 44 and 43 - conventional metal coils of adequate size and surface area, restrictive passages 33, 40 and 46 - orifice plates, and passages 37, 43, 61 and 60 - a metal pipe.
  • Raw process feed enters through passage 30 and accumulates to an appropriate level in feed region 4 as feed pool 32.
  • the partially concentrated feed continues through connector passage 52 to form feed pool 39 in feed region 13 where it is further concentrated and then proceeds through connector passage 53 to become feed pool 45 in the last stage feed region 21.
  • the process fluid is withdrawn from the system by passage 57, pump 56, and passage 55.
  • the product portion of the process fluid circuit is the purified product which accumulates in the product regions 8, 19 and 24 as product pools 36, 42 and 47. Product may be withdrawn through passages 58, 54 and 51 into a common passage 62, pump 50, and passage 49.
  • auxiliary heat rejection circuit To thermodynamically balance the system an auxiliary heat rejection circuit must be employed. It need not be a refrigeration unit as shown here but could be a heat exchanger using cooled liquid circulation, air exchange to the atmosphere or some other means of either condensing or removing excess vapor generated. One could even use a vapor pump to remove the excess vapor directly.
  • the auxiliary system here consists of a refrigeration compressor 15 discharging compressed gas through line 17 to a condensor 23 where the commercial refrigerant condenses to a liquid.
  • This liquid refrigerant passes through line 18 and is metered through the refrigerant expansion valve 12 into the auxiliary heat exchanger 9 to be evaporated to a gas and returned to compressor 15 through gas line 10.
  • the heat to evaporate the refrigerant in the auxiliary heat exchanger 9 is supplied by condensing product vapor 34.
  • the general operation of the liquid purification process is as follows: a compressed gaseous refrigerant in feed heat exchanger 31 condenses and rejects heat to feed pool 32 causing some feed to vaporize because of the lowered pressure in the chamber.
  • the now liquid refrigerant is metered through the orifice plate 33 into the product heat exhanger 35 which is at a reduced pressure being connected through the remainder of the circuit to the suction line 3 of the compressor 2. Because of the reduced pressure the refrigerant evaporates, taking in heat by condensing the vapor produced from the feed pool 32.
  • the refrigerant vapor then passes through passage 37 into feed exchanger 38.
  • the gaseous refrigerant condenses again rejecting its heat to the feed pool 39.
  • the process repeats itself through successive stages until the final stage where the gaseous refrigerant is directed to the compressor 2 by suction line 3.
  • Below is an example of typical operating conditions for processing impure water using an R-22 refrigerant fluid.

Abstract

Système de purification des liquides (70) comprenant une cuve (4) destinée à recevoir un premier liquide (92) contenant des impuretés, un appareil de réfrigération (1) en communication avec la cuve (4) pourvu d'un dispositif (2) de compression du réfrigérant et deux jeux au moins d'échangeurs de chaleur (31, 35) et (38, 41) montés en série et adaptés pour recevoir le réfrigérant du dispositif de compression (2). Chaque jeu d'échangeurs de chaleur (31, 35) et (38, 41) possède un dispositif d'évaporation du liquide (31, 38), en communication avec le liquide (32, 39) contenant des impuretés, qui sert à induire un changement de phase dans le liquide, changement comportant une phase vapeur (8) pratiquement débarrasée des impuretés, un dispositif de condensation de la phase vapeur (35, 41), relié au dispositif d'évaporation du liquide (31, 38), pour condenser la phase vapeur (8), avec lequel celle-ci est en communication pour produire un liquide pratiquement pur (36, 42), enfin un dispositif de détente (33, 40) entre le dispositif d'évaporation du liquide (31, 38) et le dispositif de condensation (35, 40), destiné à entraîner la détente du réfrigérant à mesure que celui-ci passe dans le dispositif d'évaporation du liquide (31, 38) et dans le dispositif de condensation de la phase vapeur (35, 41). Le système (70) comporte également un dispositif (3) de retour du réfrigérant depuis le dispositif échangeur de chaleur (31, 35) et (38, 41) jusqu'au dispositif de compression (2).
PCT/US1987/003173 1986-12-03 1987-12-02 Systeme de purification des liquides WO1988004193A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US93722786A 1986-12-03 1986-12-03
US937,227 1986-12-03

Publications (1)

Publication Number Publication Date
WO1988004193A1 true WO1988004193A1 (fr) 1988-06-16

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ID=25469648

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1987/003173 WO1988004193A1 (fr) 1986-12-03 1987-12-02 Systeme de purification des liquides

Country Status (2)

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AU (1) AU1052688A (fr)
WO (1) WO1988004193A1 (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0768278A1 (fr) * 1995-10-11 1997-04-16 Jeffrey A. White Méthode pour le traitement des eaux polluées par atomisation et congélation
WO1999061125A1 (fr) * 1998-05-22 1999-12-02 Auspac Technology Pty. Ltd. Procede et appareil de distillation hybride
WO2008155436A3 (fr) * 2007-06-19 2009-02-26 Beeb Bioenergias S A Installation pour la production de biodiesel
ES2313839A1 (es) * 2007-06-19 2009-03-01 Guillermo Perez Celada Destilador condensador de una mezcla a destilar.
WO2013112060A1 (fr) 2012-01-27 2013-08-01 Columbeanu Ion Liant hydraulique à base de sulfate de calcium, procédé de production de ce dernier et applications spécifiques associées
US10334828B2 (en) 2013-03-15 2019-07-02 Deepwater Desal Llc Co-location of a heat source cooling subsystem and aquaculture
US10662084B2 (en) 2012-06-07 2020-05-26 Deepwater Desal Llc Systems and methods for data center cooling and water desalination
US11214498B2 (en) 2013-03-15 2022-01-04 Deepwater Desal Llc Refrigeration facility cooling and water desalination

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1466670A (en) * 1919-11-19 1923-09-04 Monti Eudo Process for concentrating solutions and evaporating fluids
US3869351A (en) * 1973-11-09 1975-03-04 Everett H Schwartzman Evaporation system as for the conversion of salt water
US4014751A (en) * 1975-06-13 1977-03-29 Mccord James W Vapor generating and recovering apparatus
US4181577A (en) * 1974-07-18 1980-01-01 Auscoteng Pty. Ltd. Refrigeration type water desalinisation units
US4278502A (en) * 1977-05-30 1981-07-14 Christopher Stevens Chemical recovery apparatus
US4308106A (en) * 1980-08-01 1981-12-29 Mannfeld Robert L Process for removing substantially all water from an alcohol-containing solution for use as a motor fuel or motor fuel additive
US4472948A (en) * 1981-10-23 1984-09-25 Alsthom-Atlantique Heat pump installation operating from a cold source constituted by a turbid or corrosive solution

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1466670A (en) * 1919-11-19 1923-09-04 Monti Eudo Process for concentrating solutions and evaporating fluids
US3869351A (en) * 1973-11-09 1975-03-04 Everett H Schwartzman Evaporation system as for the conversion of salt water
US4181577A (en) * 1974-07-18 1980-01-01 Auscoteng Pty. Ltd. Refrigeration type water desalinisation units
US4014751A (en) * 1975-06-13 1977-03-29 Mccord James W Vapor generating and recovering apparatus
US4278502A (en) * 1977-05-30 1981-07-14 Christopher Stevens Chemical recovery apparatus
US4308106A (en) * 1980-08-01 1981-12-29 Mannfeld Robert L Process for removing substantially all water from an alcohol-containing solution for use as a motor fuel or motor fuel additive
US4472948A (en) * 1981-10-23 1984-09-25 Alsthom-Atlantique Heat pump installation operating from a cold source constituted by a turbid or corrosive solution

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0768278A1 (fr) * 1995-10-11 1997-04-16 Jeffrey A. White Méthode pour le traitement des eaux polluées par atomisation et congélation
WO1999061125A1 (fr) * 1998-05-22 1999-12-02 Auspac Technology Pty. Ltd. Procede et appareil de distillation hybride
WO2008155436A3 (fr) * 2007-06-19 2009-02-26 Beeb Bioenergias S A Installation pour la production de biodiesel
ES2313839A1 (es) * 2007-06-19 2009-03-01 Guillermo Perez Celada Destilador condensador de una mezcla a destilar.
WO2013112060A1 (fr) 2012-01-27 2013-08-01 Columbeanu Ion Liant hydraulique à base de sulfate de calcium, procédé de production de ce dernier et applications spécifiques associées
US10662084B2 (en) 2012-06-07 2020-05-26 Deepwater Desal Llc Systems and methods for data center cooling and water desalination
US11377372B2 (en) 2012-06-07 2022-07-05 Deepwater Desal Llc Systems and methods for data center cooling and water desalination
US10334828B2 (en) 2013-03-15 2019-07-02 Deepwater Desal Llc Co-location of a heat source cooling subsystem and aquaculture
US11134662B2 (en) 2013-03-15 2021-10-05 Deepwater Desal Llc Co-location of a heat source cooling subsystem and aquaculture
US11214498B2 (en) 2013-03-15 2022-01-04 Deepwater Desal Llc Refrigeration facility cooling and water desalination

Also Published As

Publication number Publication date
AU1052688A (en) 1988-06-30

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