CA1225611A - Process and apparatus for waste water purification - Google Patents
Process and apparatus for waste water purificationInfo
- Publication number
- CA1225611A CA1225611A CA000465315A CA465315A CA1225611A CA 1225611 A CA1225611 A CA 1225611A CA 000465315 A CA000465315 A CA 000465315A CA 465315 A CA465315 A CA 465315A CA 1225611 A CA1225611 A CA 1225611A
- Authority
- CA
- Canada
- Prior art keywords
- mixture
- entrainment gas
- water vapor
- waste water
- purification
- Prior art date
- Legal status (The legal status 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 status listed.)
- Expired
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/343—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas
- B01D3/346—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas the gas being used for removing vapours, e.g. transport gas
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Abstract
NHL-KFJ-09 Canada PROCESS AND APPARATUS FOR WASTE WATER PURIFICATION
ABSTRACT OF THE DISCLOSURE
The invention provides a process and an apparatus for effecting that process in which waste water to be cleaned is finely divided into a current of entrainment gas and evaporated.
The water vapor formed is superheated, so that the impurities occur as a solid residue and can be collected. The heat of the purified and compressed mixture of entrainment gas and water vapor is used to superheat the water vapor in the current of entrainment gas.
An optimal separation between water and the substances contaminating it which cannot be evaporated is accomplished with a low expenditure of energy by introducing the water into a current of inert entrainment gas and by heating the mixture of entrainment gas and water vapor thereby formed, before the separation of the solid particles, in the heat exchange with the purified and compressed mixture of entrainment gas and water vapor by cooling it to below the saturation or dew point temperature.
ABSTRACT OF THE DISCLOSURE
The invention provides a process and an apparatus for effecting that process in which waste water to be cleaned is finely divided into a current of entrainment gas and evaporated.
The water vapor formed is superheated, so that the impurities occur as a solid residue and can be collected. The heat of the purified and compressed mixture of entrainment gas and water vapor is used to superheat the water vapor in the current of entrainment gas.
An optimal separation between water and the substances contaminating it which cannot be evaporated is accomplished with a low expenditure of energy by introducing the water into a current of inert entrainment gas and by heating the mixture of entrainment gas and water vapor thereby formed, before the separation of the solid particles, in the heat exchange with the purified and compressed mixture of entrainment gas and water vapor by cooling it to below the saturation or dew point temperature.
Description
NHL-KFJ-09 Canada ~2Z561~
PROCESS AND APPARATUS FOR WASTE WATER PURIFICATION
BACKGROUND OF THE INVENTION
.
1 . F IELD OF THE INVENTION
The in~ention relates to a procesfi and apparatus for waste water purification by evaporation of the water to be purified in an entrainment gas current and removal of the residue which is thereby formed.
PROCESS AND APPARATUS FOR WASTE WATER PURIFICATION
BACKGROUND OF THE INVENTION
.
1 . F IELD OF THE INVENTION
The in~ention relates to a procesfi and apparatus for waste water purification by evaporation of the water to be purified in an entrainment gas current and removal of the residue which is thereby formed.
2 DESCRIPTION OF THE PRIOR ART
-The primary problem~ in the purification of waste water are cau~ed by dissolved impurities and pollutants which, although not dissolved in the waste water, are not sedimentary on account of their fineness. Of special importance are indu~trial waste waters, for which additional purification stages such as chemical precipitations, neutralization of impurities or detoxification by the addition of oxidat~on agents and the u~e of ion exchangers, are necessary even before general purification in clarification installations. In most cases, metallic compounds or salts also occur during the purification of such industrial waste waters, the recovery or recycling of which metallic compound or salts iB
of economic advantage. A qualitatively thorough cleaning of the water up to the purity of distilled water is the ob~ective such processes which include the treatment of brackish water and desalinat-ion of sea water. The latter is of special interest in countries which do not have abundant groundwater or rainwater.
A thorough purification of water can be achieved by distilla-tion. The water is heated in an evaporator up to saturation temperature, the steam formed is extracted and condensed in a cooled condenser. When there is complete evaporation, those substances which cannot be evaporated remain in the evaporator as NHL-KFJ-09 Carlada ~22~6~L
a ~olid residue. With 8U~I ~n open distilla~cion proce~, the wa~er is generally not completely distilled, but a liquid :Eractlon very high in Eial~8 i8 e~tracted ~ro~ the 8~1p of the distillatlon column. In this manner, the open distillation proces~ can be carried out colltinuou~ly, however, t~e high-salc residue i8 generally not xeusable in t~;Le form in which it i~
extracted from the di~tillation apparatus and the residue requires ~urther treatment~
Pervaporation is al~o a know~ separation process (See, for example ) Chemie-Ingenieur Technik, 1982 l No. 3, pp . 22q 224, especially p. 232~. In this proce~s, fluid to be purified i~
conducted along the primsry side of a membra~e to the secondary side of whlch the component~ p~rmea~ing the membrana are ~ran~-ferred in the vapc~r stage and tran~portet away by a carrier ga80 In this proce~s, a high degree of ~electivity i~ achleved in the separ~tion of di~solved componellts. The su~stances which do not pe~meate the membrane remain in khe r~ ue fraction on the primary side of the mem~rane and c~nnot be separated from it without additional measures.
2D OB TS OF T~E I~VE~TIO~
An object of the pre~ent invention i9 to provide a process ~nd apparatus for ~he purificat1on of wa~er by e~aporating the water, in which the non e~aporating ~ub~a~ce3 contained in the water can be recovered without the formatio~ o sludge or a liquid residue fractlon wit:h a ~igh salt content directly as a non-~rolatile pha~e, whereby the degree of puri~y achieved in the vapor to be extracted can be up to the degree of purity of di~tilled water. In ~dditio~, the pro~e~B i8 ~asy to execute with ~ ~mall additional expen~e for che~nical~, even wi~h
-The primary problem~ in the purification of waste water are cau~ed by dissolved impurities and pollutants which, although not dissolved in the waste water, are not sedimentary on account of their fineness. Of special importance are indu~trial waste waters, for which additional purification stages such as chemical precipitations, neutralization of impurities or detoxification by the addition of oxidat~on agents and the u~e of ion exchangers, are necessary even before general purification in clarification installations. In most cases, metallic compounds or salts also occur during the purification of such industrial waste waters, the recovery or recycling of which metallic compound or salts iB
of economic advantage. A qualitatively thorough cleaning of the water up to the purity of distilled water is the ob~ective such processes which include the treatment of brackish water and desalinat-ion of sea water. The latter is of special interest in countries which do not have abundant groundwater or rainwater.
A thorough purification of water can be achieved by distilla-tion. The water is heated in an evaporator up to saturation temperature, the steam formed is extracted and condensed in a cooled condenser. When there is complete evaporation, those substances which cannot be evaporated remain in the evaporator as NHL-KFJ-09 Carlada ~22~6~L
a ~olid residue. With 8U~I ~n open distilla~cion proce~, the wa~er is generally not completely distilled, but a liquid :Eractlon very high in Eial~8 i8 e~tracted ~ro~ the 8~1p of the distillatlon column. In this manner, the open distillation proces~ can be carried out colltinuou~ly, however, t~e high-salc residue i8 generally not xeusable in t~;Le form in which it i~
extracted from the di~tillation apparatus and the residue requires ~urther treatment~
Pervaporation is al~o a know~ separation process (See, for example ) Chemie-Ingenieur Technik, 1982 l No. 3, pp . 22q 224, especially p. 232~. In this proce~s, fluid to be purified i~
conducted along the primsry side of a membra~e to the secondary side of whlch the component~ p~rmea~ing the membrana are ~ran~-ferred in the vapc~r stage and tran~portet away by a carrier ga80 In this proce~s, a high degree of ~electivity i~ achleved in the separ~tion of di~solved componellts. The su~stances which do not pe~meate the membrane remain in khe r~ ue fraction on the primary side of the mem~rane and c~nnot be separated from it without additional measures.
2D OB TS OF T~E I~VE~TIO~
An object of the pre~ent invention i9 to provide a process ~nd apparatus for ~he purificat1on of wa~er by e~aporating the water, in which the non e~aporating ~ub~a~ce3 contained in the water can be recovered without the formatio~ o sludge or a liquid residue fractlon wit:h a ~igh salt content directly as a non-~rolatile pha~e, whereby the degree of puri~y achieved in the vapor to be extracted can be up to the degree of purity of di~tilled water. In ~dditio~, the pro~e~B i8 ~asy to execute with ~ ~mall additional expen~e for che~nical~, even wi~h
3~ ~iffer~nt metal or salt concentra~iotl~ in the waste water.
NHL-KFJ-O9 Canada SUMMARY OF THE INVENTION
According to the invention, a finely-divided waste water is introduced into an entrainment gas current and the mixture of entrainment gas and water i8 heated to a temperature which i8 ahove the saturation temperature of the water vapor formed during the heating. The saturation temperature i~ a funct~on of the pressure in the mixture of entrainment gas and wa~er vapor, which is called the total pre6sure Pt below and of the partial pre6sure ratio of the partial pressure of the entrai~ment gas P8Ch to the total pressure Pt, i.e., P~Ch/pt. The lower the total pressure and the higher the partial pressure ratio P8Chlpt~ i.e., the less water per unit of volume contained in the entrainment gas current the lower the saturation temperature. If the entrainment gas mixture, however, is only heated to the saturation temperature, then a separation between the water and the non-evaporating substances contaminating the water cannot be optimally achieved.
The invention, therefore, makes it pos~ible to achieve a condition where the mixture of entrainment ga~ and water vapor formed during the evaporation is free of droplet~ of water, i.e., a ~uperheating of the mixture of entrainment gas and water vapor beyond the saturation temperature. In such a status, the non-evaporating substances are present as electrically neutral solid particles. The finer the division of the water in the entrainment gas stream, the more homogeneous the mixture of entrainment gas and water, which is present in the form of a mist. The fine division of the water in the entrainment ga~
encourages the transfer of heat and accelerates the evaporation.
The solid particles can be filtered out of the superheated mixture of entrainment gas and water vapor as a dry substance and recovered~from the ~eparator.
NHL-KFJ-09 Canada 1~2Z56i~
In another configuration of the in~ention, the proces~
provides for the compression of the purified mixture of entrainment gas and water vapor and then it is used to heat the mixture of entrainment gas and water to be purified, which contains impurities. The compressed mixture of entrainment gas and water vapor is thereby cooled to below the specified saturation or dew point temperature of the water vapor for this pressure, 80 that the evaporation enthalpy which wa6 previously required for the evaporation of the water to be purified in the mixture of entrainment gas and water ~ recovered at a higher pressure levelL The total energy input required for the purification process of the water is thereby sign~ficantly reduced. If, for the execution of the process, heat from outside sources is avallable, e.g., cheap waste heat from physical or chemical processes, or heat from economically-feasible solar energy, it can be used to make up the heat losses in a purification process, and also for the compression of the purified mixture of entrainment gas and water vapor, and to additionally heat the mixture of entrainment gae and water vapor to be purified to the tesired temperature. Another optimization of the thermal balance of the overall process results from the fact that condensate, which is formed during the cooling of the purified mixture of entrainment ga~ and water vapor, is uset to pre-heat the waste water to be purified. The entrainment gas can also be recycled. The pre~sure in the entrainment gas is thereby ad~usted to the pressure at the entrainment gas entrance.
If s~bstances contained in the mixture of entrainment gas and water vapor are recovered as pure salts, then the temperature of the mixture of entrainment gas and water vapor is set before - NHL-KFJ-Og Canada lZZ56~1 the filtration so th~t it is higher than the specified decomposi-tion temperature of the undesirable hydrates contained in the mixture of entrainment gas and water vapor. By selecting the superheating temperature in the mixture of entrainment gafi and water vapor before filtration, it is therefore possible to determine the condition of the solid particles to be recovered, i.e., to determine whether pure salt~ or hydrates will be formed.
To achieve a mixture of entrainment gas and water vapor free of water droplets, a superheating of the mixture of entrainment gas and water vapor by at least about 10 to 20C above the saturation temperature is.necessary. This need not be accomplished solely by the addition of heat, e.g., by a superheater connected ln series behind the evaporator. Rather, it may be appropriate, as an alternative or as a supplementary measure, to reduce the mixture of entrainment gas and water vapor to a pressure at which the mixture of entrainment gas and water vapor flow~ through the ~eparator free of water droplets. In this case, too, the solid particles to be separated can also be recovered dry or as hydrate.
To facilitate the separation, the solid particles are coagulated before the entry of the mixture of entrainment gas and water vapor into the separator.
Favorable working conditions for the overall process can be achieved in the mixture of entrainment gas and water vapor to be purified at partial pressure ratios of entrainment gas partial ~ pressure P8Ch to the total pressure Pt = 0.1 to 0.8. Taking into account the recovery of heat by condensation, depending on the availability of heat from outside sources, it may be appropriate to set the pressure in the compre~sed mixture of entrainment gas and water vapor in the range between 1.5 and 20 bar.
N~IL-KFJ - 0'~ Can~d~
i Zz 56~
One aspect of the invention resides broadly in a process for the purification of waste water comprising the steps of:
introducing finely-divided waste water with solid particles or dissolved substances therein into a current of inert entrain-ment gas to form a mixture of entrainment gas and waste water;
~uperheating said mixture through heat exchange; separating the solid particles from the superheated mixture, there~y rendering a purified m~xture of entrainment gas and water vapori compressing the purified mixture thus cooling the purified mixture below the saturation or dew point temperature thereof; and recovering heat from the cooled purified mlxture for use in the superheating of said mixture through heat exchange.
Another aspect of the invention resides broadly in a process for the purification of waste water which includes the steps of evaporating the water to be purified in a current of entrainment gas and removing the residue formed during the evaporation, the improvement compris'ng the steps of: introducing finely-divided waste water with solid particles therein into the current of entrainment gas to form a mixture of the entrainment gas and the waste water~ heating said mixture to a temperature which i8 above the saturation temperature of water vapor which is formed during the heating of said mixture, wherein the water vapor, solid particles and entrainment gas mixture resulting from said heating is substantially freed of water droplets~ and separating the solid particles from said mixture of water vapor, solid particles and entrainment gas wherein a purified mixture of entrainment gas and water vapor results.
Yet another aspect of the invention resides broadly in a waste water purification apparatus comprising: means for introducing finely-divided waste water having solid particles therein into a current of entrainment gas to form a mixture of entral~ment gas and waste water~ evaporator means for receiving sald mixture and heating said mixture to a temperature which is N~L-KFJ-09 Canada .
lZ25611 above the saturation temperature of water vapor which is formed during the heating of said mixture wherein the water vapor, solid particles and entrainment gas mixture resulting from said heating is substantially free of water droplets; said evaporating means being operably associated wlth said waste water introducing means~ and means for separating the solid particles from the heated m$xture, in communication with the evaporating means wherein a purified mixture of entrainment gas and water vapor is extracted from said separating means.
; Sb i 2 2 56 11 NHL-KFJ-O9 Canada BRIEF DESCRIPTION OF l'HE- DRAWINGS
The above a8 well as other features and advantages of the present invention will become apparent through consideration of the detailed description in con~unction with the accompanying drawings in which:
Figure 1 iB a schematical representation of an installation for the purification of waste water, all accorting to the teachings of this invention; and Figure 2 i8 a graph illustrating the saturation or dew point temperature of water in a mixture of entrainment gas and water vapor as a function of the total pre~sure Pt and the partial pre~sure ratio P8Ch/pt.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
Figure 1 shows an inetallation in which the water to be purified is conducted by means of a fluid pump 1 through a pressure line 2 to the preheater 3 The preheater 3 i8 designed as a counter-current heat exchanger. In the example, the heating metium for the preheater 3 is condensate flowlng in a condensate line 4. The condensate is conveyed by a condensate pump 5 through the preheater 3.
The water to be purified, after its initial heating in the : preheater 3, i8 conducted through a water line 6 to the evaporator 7 and i8 finely divided there by means of an apparatus 8 in an èntrainment gas current; in the example, it i8 8prayed directly by a nozzle into the entrainment gas current. m e : ~ current of antrainment gas flows through an entrainment gas line 9 to the evaporator 7. The location of the nozzle at the inlet 10 of the evaporator 7 is shown only schematically in the illustration. Care mNst be taken that, with the current of entrainment gas, only finely-divided water i8 entered in the i22 S~l~ NHL-KFJ-09 Canada evaporator 7. In place of a spray nozzle, of course, other fluid dividers can be used. A very homogeneous division is achieved with the formation of a mist.
In the evaporator 7, the mixture of entrainment gas and water flowing in through the entrance 10 is heated to a temperature which i8 higher than the saturation temperature of the water vapor in the mixture of entrainment gas and water vapor. The saturation temperature i8 a function of the total pressure Pt in the mixture of entrainment gas and water vapor, and of the partial pressure ratio between the partial pressure of the entrainment gas P8Ch and the total pressure Pt. Figure 2 illustrates the dependence of the saturation or dew point temperature on the total pressure Pt and the partial pre~sure ratio P8Ch/~t. The higher the total pressure Pt and the lower the partial pressure ratio P8Ch/pt~ the more water will therefore be sprayed into the entrainment gas at the same total pressure Pt, the higher the saturation temperature.
For the achievement of a condition free of water droplets, the mixture of entrainment gas and water vapor must be heated to at least about 19 to 20C hlgher than the saturation temperature, If the heat available in the evaporator 7 i8 insufficient for the superheating, then the mixture of entrainment gas and water vapor can al~o be heated to the desired temperature in a superheater 7a in series behind the evaporator 7.
. .
The superheater 7a is accessible by means of a bypass, which runs parallel to the feed line 14 leading from the outlet 12 of the evaporator 7 to the separator 13. The bypass 11 and thus the superheater 7a carry the flow of the mixture of entrainment gas and water vapor aftex the opening or closing of the cutoff cock~
15 (in the bypass 11) and 14a (in the feed line 14).
NHL-KFJ-O9 Canada The ~uperheated mixture o~ entrai~ment gas and water vapor i~ co~duet~d via the feed llne 14 to the ~eparator 13. The sep~rator 13 i~ capable o reta~ning those ~ub~tance~ which remain unevaporated dur~ng the evaporation of th~ water portion in the current of entrainment ga~ ~nd w~lich are pre~ent as ~olid particles in the mixture of entrainment gas and water vapor free of water droplets. The separator i~ therefor~ to be 6elec~ed on the ba~l~ of the ~peclf~d degree o purity and it exhi~its a flltra~ion qual~ty which satisfiQ~ the applica~le r~quirements.
Such separators are known ln them~elve~. They are described~ for ~xample, in F.A. H~ngl~in, "Grundri~s d~r Chemi~chen Tech~ik"
~"Outline o Chemical Technology"), Verlag Chemie GmbH, Weinheim, 1963, pp.74 ff., espec~ally p..125, ~he con~ents of which are incorporated herein by reference wi~h regard ~o the impuriSie~
~ which remain as ~olid particle~ ln the mlxture of entrai~ment ga~
and water vapor after the evaporation, a very h~gh purity of thP
mixture of en~rai~m~nt ga~ and water vapor ca~ b~ achieved which corr~sponds to the filter qual~ty used.
The installation lllustrated schemat~cally in the figure has, par~llel to the feed line 14l another bypa~s lla, which lead~ to a prea~ure re~uc~r 16. The pre~sure re~ucer 16 can be act~Yated by ope~ing snd clo~ing cutoff valves 17, 17a in the bypa~ lla and feed line 14. Thi8 i~ for ca~es where the fiuper heating of the mixture of entrainm~t ga~ and water vapor in the evaporator i8 not ~uicient to achieve a mixture of entrainment gas and w~ter vapor ree of water droplets and if a cheap ~ource o heat i8 not avail~ble to provide supplemen~ary heat to ~he superhea~er 7 , making po~ible an economical implementa~on of the proce~. In the flowchart shown in Figure 1, the pre~6ure reducer 16 i~ represented only ~chematically a~ a throttle me~hanism.
NHL-KFJ-09 Canada ~ Z Z S 6 ~ ~
In the illustrated exEmple, the separator 13 i8 a chæmber in which the entrainment ga~ current is reversed. The solid particles which are thereby separated from the mixture of entrainment gas and water vapor accumulate on the floor 18 of the separator 13 and are continuously removed by means of a suction device 19.
The purified mixture of entrainment gas and water vapor flowing out of the separator 13 via ~he ~eparator outlet 13a, for recovery of the heat carried along with the mixture of entrainment gas and water vapor as a heating medium, flows in heating lines 7' back into the evaporator 7. The mixture of entrainment gas and water vapor i8 extracted from the separator 13 for this purpose by means of a compressor 20, via its suction line 21, and COmpre88ed 80 that the water portion i8 condenset during cooling and give~ up its heat to the mixture of entrainment gas and water to be purified, at a dew point temperature which 18 above the saturation temperature of the water vapor in the mixture of entrainment ga~ and water vapor to be purified. The heat recovered during the condensation of the purified water portion is thereby transferred to the mixture of entrainment gas and water or water vapor to be purified.
If the temperature difference between the dew point temperature on the one hand ant the saturation temperature in the evaporator on the other hand by compression alone is not sufficient to make the mixture of entrainment gas and water vapor to be purified free of water droplets, then the compressed mixture of entrainment gas and water vapor can be heated in a supplementary heater 22. The heater 22 in the example is connected in a bypass llb to the pressure line 23 of the compressor 20. The mixture of entrainment gas and water vapor, or a portion of it, can be NHL-KFJ-O9 Canada 1 2 2 56 ~ 1 conducted into the heater 22 by controlling the cutoff valves 24, 25 in the pressure line 23 and bypass llb. The hea~ ~ource for the superheater 7a for the mixture of entrainment gas and water vapor to be purified can, for ex~mple, be waste heat or heat obtained by the conversion of ~olar energy. The more the purified mixture of entrainment gas ant water vapor i8 compre~sed, the less additional heating of the mixture of entrainment gas and water vapor is necessary in the heater 22, to achieve a condition where the mixture of entrainment gas and water vapor to be purified is free of water droplets.
From the heater 22, a connection line 26 leads to the evaporator 7. In the example, the evaporator 7 is designed as a tubular boiler with tubes as the heating medium lines 7'. The compressed mixture of entrainment gas ant water vapor in the evaporator 7 flows in the tubes. The compressed m~xture of entrainment gas and water vapor is cooled below the dew point temperature of the water vapor in the mixture of entrainment gas and water vapor. The contensate which is thereby formed travels through the condensate line 4 to the preheater 3, while the rèmaining compressed entrainment gae is réturned via an outlet 27 to the input 10 of the evaporator 7 in the circuit. The pressure in the entrainment gas i8 hereby set by means of a pres6ure controller 28 at the pressure in the entrainment gas line 9. At the entrance 10 of the evaporator 7, the entrainment gas current is then again charged with water to be purified.
If waste water containing NiS04, for example, is purified in the installation described above, then NiS04 can be recovered either as a dry salt or a8 a hydrate, NiS04 . 6 H20. For the hydrate, the free reaction enthalpy ~H and the entropy ~S of the reaction are:
NHL-KFJ-09 Canada lZ256~1 NiS04 + 6 H20 _m~Nis04 . 6 H20 H = -85.80 Cal/Mol S = 213.23 Cal/Mol K.
With these values, the required partial pressure of the water vapor P~ 0 for the formation of hydrate from the equation:
~S 1 ~IJ
P = e~ ~~ . e ~ ~ bar ~2 is:
P~ 0 ~ 2.42 bar at T ~ 150C
P~20 - 5.17 bar at T ~ 170C.
If the mixture of entrainment gas ant water vapor to be purified is set at a total pressure Pt ~ 8 bar and Pinely-divided waste water containing NiS04 is in3ected into the entrain-ment gas up to a partial pressure ratio P6Ch/pt ~ 0.5, then there i~ a partial pressure of PH2o 4 b Corresponding to this partlal pres~ure, considering the above-mentioned values as the formation temperature for NiS04 . 6 H20 i8 a temperature of T ~ 165C. For temperatures in the mixture of entrainment gas and water vapor above this tempera-ture, ice., for ~ ~165C, solid particles which consist of dry salt NiS04 remain in the mixture of entrainment gas and water vapor.
NHL-KFJ-09 Canada lZZ5611 If wa~te water containing NiC12 iB to be purified, ~hen either the dry salt NiC12 or a hydrate NiC12 . 2 H20 can be recovered. For the hydrate formation, a water vapor partial pressure of:
- 6958.5 P~ 0 = 5.1806 . 107 . e T bar is nece~sary. From this, it follows that:
P~20 z 3.716 bar at T = 150C
P~20 ~ 6.529 bar at T e 165C.
If the total pre~sure of the mixture of entrainment gas and water vapor i8 set at 8 bar and if P~Ch/pt = 0.5, then the formation temperature for the hydrate NiC12 . 2 H20 i8 a tempera-ture T - 153C. For temperature~ in the mixture of entrainment gas and water vapor above this temperature, i.e., for T >153C, according to this equation, dry salt particles NiC12 can therefore be separated from the mixture of entrainment gas and water vapor.
The preheater 3 can, for example, be ad3usted ~o that the quantity pf waste water to be purified can be sprayed at a -`~ temperature of approximately 60C or even higher into the current20 of entrainment gas. The current of entrainment gas and the quality of waste water sprayed in are ad~usted to one another so that in the mixture of entrainment gas and water vaporj there is a partial pressure ratio of the entrainment gas partial pressure PSCh to the total pressure Pt in the range between 0.1 and 0.8.
NHL-KFJ-09 Canada lZ~5~11 At a partial pressure ratio P8Ch/pt 8 0.4 and a total pre~sure of Pt - 5 bar, the saturation temperature for the water vapor i8 approximately 130C. To achieve a condition free of water droplet6, a superheating of the mixture of entrainment gas and water vapor of at least lo to 20C above the saturation temperature is necessary. If it is assumed that for this superheating in the evaporator 7, there i8 a temperature difference of 20C between the compressed purified mixture o~ entrainment ga~ and water vapor u~ed as the heating medlum and the mixture of entrainment gas and water vapor to be purifled, then the purified mixture of entrainment gas and water vapor at the same partial pressure ratio P8Ch/Pt is to be compressed wlthout additional superheating in the heater 22 to an approximate total pressure of 14 bar.
Taking into account the transfer of heat in the evaporator 7, a total pressure is generally to be set in the range between 1. 5 and 20 bar. At a lower compres6ion, for the achievement of a mixture of entrainment gas and water vapor free of water droplets, an additional heating of the compressed mixture of entrainment gas and water vapor in the heater 22 is necessary. Alternatively, or in combination with all the other measures mentioned above, for the secure achievement of a condition free of water droplets, it is also possible to reduce the total pressure in the mixture of entrainment gas and water vapor in the pressure relief apparatus 16 before the separation of the solid particles. In the example, the pressure reducer 16 is designed as a swirl chamber, to coagulate the solid particles, taking advantage of adhesion. The ~ solid particles are separated from the superheated mixture of entrainment gas and water vapor in the separator 13. A purified mixture of entrainment gas and water vapor flows into the separator 13.
NHL-KFJ-09 Canada lZ256~1 U~able entrainment gases include helium, argon, nitrogen, air or other gases which react neither with the water nor with the substances to be removed which are contained in the wa6te water.
To consume as little energy as possible in the compres~ion and heating of the purified mixture of entrainment gas and water vapor, the working range must be optimized. At partial pressure ratios P8Ch/pt between 0.1 and 0.8, at total pre~sures between 1.5 and 20 bar at the compressor outlet, and at temperatures below 220C, favorable working conditlons can be establi~hed for the execution of the proces~.
What has been described is a unique process and apparatus for the purification of waste water. The invention is not to be taken as limited to all the details that are de6cribed herein-above, since difications and variations thereof may be made without departing from the spirit or scope of the invention.
NHL-KFJ-O9 Canada SUMMARY OF THE INVENTION
According to the invention, a finely-divided waste water is introduced into an entrainment gas current and the mixture of entrainment gas and water i8 heated to a temperature which i8 ahove the saturation temperature of the water vapor formed during the heating. The saturation temperature i~ a funct~on of the pressure in the mixture of entrainment gas and wa~er vapor, which is called the total pre6sure Pt below and of the partial pre6sure ratio of the partial pressure of the entrai~ment gas P8Ch to the total pressure Pt, i.e., P~Ch/pt. The lower the total pressure and the higher the partial pressure ratio P8Chlpt~ i.e., the less water per unit of volume contained in the entrainment gas current the lower the saturation temperature. If the entrainment gas mixture, however, is only heated to the saturation temperature, then a separation between the water and the non-evaporating substances contaminating the water cannot be optimally achieved.
The invention, therefore, makes it pos~ible to achieve a condition where the mixture of entrainment ga~ and water vapor formed during the evaporation is free of droplet~ of water, i.e., a ~uperheating of the mixture of entrainment gas and water vapor beyond the saturation temperature. In such a status, the non-evaporating substances are present as electrically neutral solid particles. The finer the division of the water in the entrainment gas stream, the more homogeneous the mixture of entrainment gas and water, which is present in the form of a mist. The fine division of the water in the entrainment ga~
encourages the transfer of heat and accelerates the evaporation.
The solid particles can be filtered out of the superheated mixture of entrainment gas and water vapor as a dry substance and recovered~from the ~eparator.
NHL-KFJ-09 Canada 1~2Z56i~
In another configuration of the in~ention, the proces~
provides for the compression of the purified mixture of entrainment gas and water vapor and then it is used to heat the mixture of entrainment gas and water to be purified, which contains impurities. The compressed mixture of entrainment gas and water vapor is thereby cooled to below the specified saturation or dew point temperature of the water vapor for this pressure, 80 that the evaporation enthalpy which wa6 previously required for the evaporation of the water to be purified in the mixture of entrainment gas and water ~ recovered at a higher pressure levelL The total energy input required for the purification process of the water is thereby sign~ficantly reduced. If, for the execution of the process, heat from outside sources is avallable, e.g., cheap waste heat from physical or chemical processes, or heat from economically-feasible solar energy, it can be used to make up the heat losses in a purification process, and also for the compression of the purified mixture of entrainment gas and water vapor, and to additionally heat the mixture of entrainment gae and water vapor to be purified to the tesired temperature. Another optimization of the thermal balance of the overall process results from the fact that condensate, which is formed during the cooling of the purified mixture of entrainment ga~ and water vapor, is uset to pre-heat the waste water to be purified. The entrainment gas can also be recycled. The pre~sure in the entrainment gas is thereby ad~usted to the pressure at the entrainment gas entrance.
If s~bstances contained in the mixture of entrainment gas and water vapor are recovered as pure salts, then the temperature of the mixture of entrainment gas and water vapor is set before - NHL-KFJ-Og Canada lZZ56~1 the filtration so th~t it is higher than the specified decomposi-tion temperature of the undesirable hydrates contained in the mixture of entrainment gas and water vapor. By selecting the superheating temperature in the mixture of entrainment gafi and water vapor before filtration, it is therefore possible to determine the condition of the solid particles to be recovered, i.e., to determine whether pure salt~ or hydrates will be formed.
To achieve a mixture of entrainment gas and water vapor free of water droplets, a superheating of the mixture of entrainment gas and water vapor by at least about 10 to 20C above the saturation temperature is.necessary. This need not be accomplished solely by the addition of heat, e.g., by a superheater connected ln series behind the evaporator. Rather, it may be appropriate, as an alternative or as a supplementary measure, to reduce the mixture of entrainment gas and water vapor to a pressure at which the mixture of entrainment gas and water vapor flow~ through the ~eparator free of water droplets. In this case, too, the solid particles to be separated can also be recovered dry or as hydrate.
To facilitate the separation, the solid particles are coagulated before the entry of the mixture of entrainment gas and water vapor into the separator.
Favorable working conditions for the overall process can be achieved in the mixture of entrainment gas and water vapor to be purified at partial pressure ratios of entrainment gas partial ~ pressure P8Ch to the total pressure Pt = 0.1 to 0.8. Taking into account the recovery of heat by condensation, depending on the availability of heat from outside sources, it may be appropriate to set the pressure in the compre~sed mixture of entrainment gas and water vapor in the range between 1.5 and 20 bar.
N~IL-KFJ - 0'~ Can~d~
i Zz 56~
One aspect of the invention resides broadly in a process for the purification of waste water comprising the steps of:
introducing finely-divided waste water with solid particles or dissolved substances therein into a current of inert entrain-ment gas to form a mixture of entrainment gas and waste water;
~uperheating said mixture through heat exchange; separating the solid particles from the superheated mixture, there~y rendering a purified m~xture of entrainment gas and water vapori compressing the purified mixture thus cooling the purified mixture below the saturation or dew point temperature thereof; and recovering heat from the cooled purified mlxture for use in the superheating of said mixture through heat exchange.
Another aspect of the invention resides broadly in a process for the purification of waste water which includes the steps of evaporating the water to be purified in a current of entrainment gas and removing the residue formed during the evaporation, the improvement compris'ng the steps of: introducing finely-divided waste water with solid particles therein into the current of entrainment gas to form a mixture of the entrainment gas and the waste water~ heating said mixture to a temperature which i8 above the saturation temperature of water vapor which is formed during the heating of said mixture, wherein the water vapor, solid particles and entrainment gas mixture resulting from said heating is substantially freed of water droplets~ and separating the solid particles from said mixture of water vapor, solid particles and entrainment gas wherein a purified mixture of entrainment gas and water vapor results.
Yet another aspect of the invention resides broadly in a waste water purification apparatus comprising: means for introducing finely-divided waste water having solid particles therein into a current of entrainment gas to form a mixture of entral~ment gas and waste water~ evaporator means for receiving sald mixture and heating said mixture to a temperature which is N~L-KFJ-09 Canada .
lZ25611 above the saturation temperature of water vapor which is formed during the heating of said mixture wherein the water vapor, solid particles and entrainment gas mixture resulting from said heating is substantially free of water droplets; said evaporating means being operably associated wlth said waste water introducing means~ and means for separating the solid particles from the heated m$xture, in communication with the evaporating means wherein a purified mixture of entrainment gas and water vapor is extracted from said separating means.
; Sb i 2 2 56 11 NHL-KFJ-O9 Canada BRIEF DESCRIPTION OF l'HE- DRAWINGS
The above a8 well as other features and advantages of the present invention will become apparent through consideration of the detailed description in con~unction with the accompanying drawings in which:
Figure 1 iB a schematical representation of an installation for the purification of waste water, all accorting to the teachings of this invention; and Figure 2 i8 a graph illustrating the saturation or dew point temperature of water in a mixture of entrainment gas and water vapor as a function of the total pre~sure Pt and the partial pre~sure ratio P8Ch/pt.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS
Figure 1 shows an inetallation in which the water to be purified is conducted by means of a fluid pump 1 through a pressure line 2 to the preheater 3 The preheater 3 i8 designed as a counter-current heat exchanger. In the example, the heating metium for the preheater 3 is condensate flowlng in a condensate line 4. The condensate is conveyed by a condensate pump 5 through the preheater 3.
The water to be purified, after its initial heating in the : preheater 3, i8 conducted through a water line 6 to the evaporator 7 and i8 finely divided there by means of an apparatus 8 in an èntrainment gas current; in the example, it i8 8prayed directly by a nozzle into the entrainment gas current. m e : ~ current of antrainment gas flows through an entrainment gas line 9 to the evaporator 7. The location of the nozzle at the inlet 10 of the evaporator 7 is shown only schematically in the illustration. Care mNst be taken that, with the current of entrainment gas, only finely-divided water i8 entered in the i22 S~l~ NHL-KFJ-09 Canada evaporator 7. In place of a spray nozzle, of course, other fluid dividers can be used. A very homogeneous division is achieved with the formation of a mist.
In the evaporator 7, the mixture of entrainment gas and water flowing in through the entrance 10 is heated to a temperature which i8 higher than the saturation temperature of the water vapor in the mixture of entrainment gas and water vapor. The saturation temperature i8 a function of the total pressure Pt in the mixture of entrainment gas and water vapor, and of the partial pressure ratio between the partial pressure of the entrainment gas P8Ch and the total pressure Pt. Figure 2 illustrates the dependence of the saturation or dew point temperature on the total pressure Pt and the partial pre~sure ratio P8Ch/~t. The higher the total pressure Pt and the lower the partial pressure ratio P8Ch/pt~ the more water will therefore be sprayed into the entrainment gas at the same total pressure Pt, the higher the saturation temperature.
For the achievement of a condition free of water droplets, the mixture of entrainment gas and water vapor must be heated to at least about 19 to 20C hlgher than the saturation temperature, If the heat available in the evaporator 7 i8 insufficient for the superheating, then the mixture of entrainment gas and water vapor can al~o be heated to the desired temperature in a superheater 7a in series behind the evaporator 7.
. .
The superheater 7a is accessible by means of a bypass, which runs parallel to the feed line 14 leading from the outlet 12 of the evaporator 7 to the separator 13. The bypass 11 and thus the superheater 7a carry the flow of the mixture of entrainment gas and water vapor aftex the opening or closing of the cutoff cock~
15 (in the bypass 11) and 14a (in the feed line 14).
NHL-KFJ-O9 Canada The ~uperheated mixture o~ entrai~ment gas and water vapor i~ co~duet~d via the feed llne 14 to the ~eparator 13. The sep~rator 13 i~ capable o reta~ning those ~ub~tance~ which remain unevaporated dur~ng the evaporation of th~ water portion in the current of entrainment ga~ ~nd w~lich are pre~ent as ~olid particles in the mixture of entrainment gas and water vapor free of water droplets. The separator i~ therefor~ to be 6elec~ed on the ba~l~ of the ~peclf~d degree o purity and it exhi~its a flltra~ion qual~ty which satisfiQ~ the applica~le r~quirements.
Such separators are known ln them~elve~. They are described~ for ~xample, in F.A. H~ngl~in, "Grundri~s d~r Chemi~chen Tech~ik"
~"Outline o Chemical Technology"), Verlag Chemie GmbH, Weinheim, 1963, pp.74 ff., espec~ally p..125, ~he con~ents of which are incorporated herein by reference wi~h regard ~o the impuriSie~
~ which remain as ~olid particle~ ln the mlxture of entrai~ment ga~
and water vapor after the evaporation, a very h~gh purity of thP
mixture of en~rai~m~nt ga~ and water vapor ca~ b~ achieved which corr~sponds to the filter qual~ty used.
The installation lllustrated schemat~cally in the figure has, par~llel to the feed line 14l another bypa~s lla, which lead~ to a prea~ure re~uc~r 16. The pre~sure re~ucer 16 can be act~Yated by ope~ing snd clo~ing cutoff valves 17, 17a in the bypa~ lla and feed line 14. Thi8 i~ for ca~es where the fiuper heating of the mixture of entrainm~t ga~ and water vapor in the evaporator i8 not ~uicient to achieve a mixture of entrainment gas and w~ter vapor ree of water droplets and if a cheap ~ource o heat i8 not avail~ble to provide supplemen~ary heat to ~he superhea~er 7 , making po~ible an economical implementa~on of the proce~. In the flowchart shown in Figure 1, the pre~6ure reducer 16 i~ represented only ~chematically a~ a throttle me~hanism.
NHL-KFJ-09 Canada ~ Z Z S 6 ~ ~
In the illustrated exEmple, the separator 13 i8 a chæmber in which the entrainment ga~ current is reversed. The solid particles which are thereby separated from the mixture of entrainment gas and water vapor accumulate on the floor 18 of the separator 13 and are continuously removed by means of a suction device 19.
The purified mixture of entrainment gas and water vapor flowing out of the separator 13 via ~he ~eparator outlet 13a, for recovery of the heat carried along with the mixture of entrainment gas and water vapor as a heating medium, flows in heating lines 7' back into the evaporator 7. The mixture of entrainment gas and water vapor i8 extracted from the separator 13 for this purpose by means of a compressor 20, via its suction line 21, and COmpre88ed 80 that the water portion i8 condenset during cooling and give~ up its heat to the mixture of entrainment gas and water to be purified, at a dew point temperature which 18 above the saturation temperature of the water vapor in the mixture of entrainment ga~ and water vapor to be purified. The heat recovered during the condensation of the purified water portion is thereby transferred to the mixture of entrainment gas and water or water vapor to be purified.
If the temperature difference between the dew point temperature on the one hand ant the saturation temperature in the evaporator on the other hand by compression alone is not sufficient to make the mixture of entrainment gas and water vapor to be purified free of water droplets, then the compressed mixture of entrainment gas and water vapor can be heated in a supplementary heater 22. The heater 22 in the example is connected in a bypass llb to the pressure line 23 of the compressor 20. The mixture of entrainment gas and water vapor, or a portion of it, can be NHL-KFJ-O9 Canada 1 2 2 56 ~ 1 conducted into the heater 22 by controlling the cutoff valves 24, 25 in the pressure line 23 and bypass llb. The hea~ ~ource for the superheater 7a for the mixture of entrainment gas and water vapor to be purified can, for ex~mple, be waste heat or heat obtained by the conversion of ~olar energy. The more the purified mixture of entrainment gas ant water vapor i8 compre~sed, the less additional heating of the mixture of entrainment gas and water vapor is necessary in the heater 22, to achieve a condition where the mixture of entrainment gas and water vapor to be purified is free of water droplets.
From the heater 22, a connection line 26 leads to the evaporator 7. In the example, the evaporator 7 is designed as a tubular boiler with tubes as the heating medium lines 7'. The compressed mixture of entrainment gas ant water vapor in the evaporator 7 flows in the tubes. The compressed m~xture of entrainment gas and water vapor is cooled below the dew point temperature of the water vapor in the mixture of entrainment gas and water vapor. The contensate which is thereby formed travels through the condensate line 4 to the preheater 3, while the rèmaining compressed entrainment gae is réturned via an outlet 27 to the input 10 of the evaporator 7 in the circuit. The pressure in the entrainment gas i8 hereby set by means of a pres6ure controller 28 at the pressure in the entrainment gas line 9. At the entrance 10 of the evaporator 7, the entrainment gas current is then again charged with water to be purified.
If waste water containing NiS04, for example, is purified in the installation described above, then NiS04 can be recovered either as a dry salt or a8 a hydrate, NiS04 . 6 H20. For the hydrate, the free reaction enthalpy ~H and the entropy ~S of the reaction are:
NHL-KFJ-09 Canada lZ256~1 NiS04 + 6 H20 _m~Nis04 . 6 H20 H = -85.80 Cal/Mol S = 213.23 Cal/Mol K.
With these values, the required partial pressure of the water vapor P~ 0 for the formation of hydrate from the equation:
~S 1 ~IJ
P = e~ ~~ . e ~ ~ bar ~2 is:
P~ 0 ~ 2.42 bar at T ~ 150C
P~20 - 5.17 bar at T ~ 170C.
If the mixture of entrainment gas ant water vapor to be purified is set at a total pressure Pt ~ 8 bar and Pinely-divided waste water containing NiS04 is in3ected into the entrain-ment gas up to a partial pressure ratio P6Ch/pt ~ 0.5, then there i~ a partial pressure of PH2o 4 b Corresponding to this partlal pres~ure, considering the above-mentioned values as the formation temperature for NiS04 . 6 H20 i8 a temperature of T ~ 165C. For temperatures in the mixture of entrainment gas and water vapor above this tempera-ture, ice., for ~ ~165C, solid particles which consist of dry salt NiS04 remain in the mixture of entrainment gas and water vapor.
NHL-KFJ-09 Canada lZZ5611 If wa~te water containing NiC12 iB to be purified, ~hen either the dry salt NiC12 or a hydrate NiC12 . 2 H20 can be recovered. For the hydrate formation, a water vapor partial pressure of:
- 6958.5 P~ 0 = 5.1806 . 107 . e T bar is nece~sary. From this, it follows that:
P~20 z 3.716 bar at T = 150C
P~20 ~ 6.529 bar at T e 165C.
If the total pre~sure of the mixture of entrainment gas and water vapor i8 set at 8 bar and if P~Ch/pt = 0.5, then the formation temperature for the hydrate NiC12 . 2 H20 i8 a tempera-ture T - 153C. For temperature~ in the mixture of entrainment gas and water vapor above this temperature, i.e., for T >153C, according to this equation, dry salt particles NiC12 can therefore be separated from the mixture of entrainment gas and water vapor.
The preheater 3 can, for example, be ad3usted ~o that the quantity pf waste water to be purified can be sprayed at a -`~ temperature of approximately 60C or even higher into the current20 of entrainment gas. The current of entrainment gas and the quality of waste water sprayed in are ad~usted to one another so that in the mixture of entrainment gas and water vaporj there is a partial pressure ratio of the entrainment gas partial pressure PSCh to the total pressure Pt in the range between 0.1 and 0.8.
NHL-KFJ-09 Canada lZ~5~11 At a partial pressure ratio P8Ch/pt 8 0.4 and a total pre~sure of Pt - 5 bar, the saturation temperature for the water vapor i8 approximately 130C. To achieve a condition free of water droplet6, a superheating of the mixture of entrainment gas and water vapor of at least lo to 20C above the saturation temperature is necessary. If it is assumed that for this superheating in the evaporator 7, there i8 a temperature difference of 20C between the compressed purified mixture o~ entrainment ga~ and water vapor u~ed as the heating medlum and the mixture of entrainment gas and water vapor to be purifled, then the purified mixture of entrainment gas and water vapor at the same partial pressure ratio P8Ch/Pt is to be compressed wlthout additional superheating in the heater 22 to an approximate total pressure of 14 bar.
Taking into account the transfer of heat in the evaporator 7, a total pressure is generally to be set in the range between 1. 5 and 20 bar. At a lower compres6ion, for the achievement of a mixture of entrainment gas and water vapor free of water droplets, an additional heating of the compressed mixture of entrainment gas and water vapor in the heater 22 is necessary. Alternatively, or in combination with all the other measures mentioned above, for the secure achievement of a condition free of water droplets, it is also possible to reduce the total pressure in the mixture of entrainment gas and water vapor in the pressure relief apparatus 16 before the separation of the solid particles. In the example, the pressure reducer 16 is designed as a swirl chamber, to coagulate the solid particles, taking advantage of adhesion. The ~ solid particles are separated from the superheated mixture of entrainment gas and water vapor in the separator 13. A purified mixture of entrainment gas and water vapor flows into the separator 13.
NHL-KFJ-09 Canada lZ256~1 U~able entrainment gases include helium, argon, nitrogen, air or other gases which react neither with the water nor with the substances to be removed which are contained in the wa6te water.
To consume as little energy as possible in the compres~ion and heating of the purified mixture of entrainment gas and water vapor, the working range must be optimized. At partial pressure ratios P8Ch/pt between 0.1 and 0.8, at total pre~sures between 1.5 and 20 bar at the compressor outlet, and at temperatures below 220C, favorable working conditlons can be establi~hed for the execution of the proces~.
What has been described is a unique process and apparatus for the purification of waste water. The invention is not to be taken as limited to all the details that are de6cribed herein-above, since difications and variations thereof may be made without departing from the spirit or scope of the invention.
Claims (26)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for the purification of waste water comprising the steps of:
introducing finely-divided waste water with solid particles or dissolved substances therein into a current of inert entrain-ment gas to form a mixture of entrainment gas and waste water;
superheating said mixture through heat exchange;
separating the solid particles from the superheated mixture, thereby rendering a purified mixture of entrainment gas and water vapor;
compressing the purified mixture thus cooling the purified mixture below the saturation or dew point temperature thereof;
and recovering heat from the cooled purified mixture for use in the superheating of said mixture through heat exchange.
introducing finely-divided waste water with solid particles or dissolved substances therein into a current of inert entrain-ment gas to form a mixture of entrainment gas and waste water;
superheating said mixture through heat exchange;
separating the solid particles from the superheated mixture, thereby rendering a purified mixture of entrainment gas and water vapor;
compressing the purified mixture thus cooling the purified mixture below the saturation or dew point temperature thereof;
and recovering heat from the cooled purified mixture for use in the superheating of said mixture through heat exchange.
2. The process for the purification of waste water according to Claim 1 including the steps of preheating the waste water to be purified prior to the formation of the mixture of entrainment gas and waste water.
3. The process for the purification of waste water according to Claim 2 further including the steps of separating the entrain-ment gas from the purified mixture of entrainment gas and water vapor and recycling the separated entrainment gas for use in the current of entrainment gas into which waste water is introduced.
4. The process for the purification of waste water according to Claim 3 including the step of controlling the pressure of the recycled separated entrainment gas during the water purification process.
NHL-KFJ-09 Canada
NHL-KFJ-09 Canada
5. The process for the purification of waste water according to Claim 1 wherein the mixture of entrainment gas and water vapor includes at least one hydrate therein and wherein the step of superheating the mixture elevates the mixture to a temperature which is above the decomposition temperature of at least one of the hydrates.
6. The process for the purification of waste water according to Claim 1 wherein the step of separating the solid particles from the mixture of water vapor, solid particles and entrainment gas is effected at a pressure at which the mixture is free of water droplets.
7, The process for the purification of waste water according to Claim l including the step of coagulating the solid particles prior to the separation thereof from the mixture of water vapor, solid particles and entrainment gas.
8. The process for the purification of waste water according to Claim 1 wherein the water to be purified is added to the current of entrainment gas in a predetermined quantity such that a partial pressure ratio is established in the mixture of entrainment gas and water vapor prior to the step of separating such that the entrainment gas partial pressure Psch and the total pressure of the mixture of entrainment gas and water vapor Pt in the range Psch/Pt = 0.1 to 0.8.
9. The process for the purification of waste water according to Claim 1 the purified mixture of entrainment gas and water vapor is compressed at a total pressure in the range between 1.5 and 20 bar.
NHL-KFJ-09 Canada
NHL-KFJ-09 Canada
10. In a process for the purification of waste water which includes the steps of evaporating the water to be purified in a current of entrainment gas and removing the residue formed during the evaporation, the improvement comprising the steps of:
introducing finely-divided waste water with solid particles wherein into the current of entrainment gas to form a mixture of the entrainment gas and the waste water;
heating said mixture to a temperature which is above the saturation temperature of water vapor which is formed during the heating of said mixture, wherein the water vapor, solid particles and entrainment gas mixture resulting from said heating is substantially freed of water droplets; and separating the solid particles from said mixture of water vapor, solid particles and entrainment gas wherein a purified mixture of entrainment gas and water vapor results.
introducing finely-divided waste water with solid particles wherein into the current of entrainment gas to form a mixture of the entrainment gas and the waste water;
heating said mixture to a temperature which is above the saturation temperature of water vapor which is formed during the heating of said mixture, wherein the water vapor, solid particles and entrainment gas mixture resulting from said heating is substantially freed of water droplets; and separating the solid particles from said mixture of water vapor, solid particles and entrainment gas wherein a purified mixture of entrainment gas and water vapor results.
11. The improved process for the purification of waste water according to Claim 10 including the steps of separating the water vapor from the purified mixture of entrainment gas and water results; compressing the separated water vapor to cool the separated water vapor below the saturation or dew point temperature of the water vapor in the mixture of entrainment gas and water vapor; and recovering heat generated during the cooling of the separated water vapor to heat the mixture of entrainment gas and water or water vapor to be purified by evaporation.
12. The improved process for the purification of waste water according to Claim 10 including the step of preheating the waste water to be purified prior to evaporation thereof.
13. The improved process for the purification of waste water according to Claim 11 wherein the entrainment gas separated NHL-KFJ-09 Canada from the purified mixture of entrainment gas and water vapor is recycled for use in the current of entrainment gas into which waste water is introduced.
14. The improved process for the purification of waste water according to Claim 13 including the step of controlling the pressure of the recycled entrainment gas during the water purification process.
15. The improved process for the purification of waste water according to Claim 10 wherein the mixture of entrainment gas and water vapor includes at least one hydrate therein and wherein the step of heating the mixture elevates the mixture to a temperature which is above the decomposition temperature of at least one of the hydrates.
16. The improved process for the purification of waste water according to Claim 10 wherein the step of separating the solid particles from the mixture of water vapor, solid particles and entrainment gas is effected at a pressure at which the mixture is free of water droplets.
17. The improved process for the purification of waste water according to Claim 10 including the step of coagulating the solid particles prior to the separation thereof from the mixture of water vapor, solid particles and entrainment gas.
18. The improved process for the purification of waste water according to Claim 10 wherein the water to be purified is added to the current of entrainment gas in a predetermined quantity such that a partial pressure ratio is established in the mixture of entrainment gas and water vapor prior to the step of NHL-KFJ-09 Canada separating such that the entrainment gas partial pressure Psch and the total pressure of the mixture of entrainment gas and water vapor Pt in the range Psch/Pt = 0.1 to 0.8.
19. The improved process for the purification of waste water according to Claim 11 the purified mixture of entrainment gas and water vapor is compressed at a total pressure in the range between 1.5 and 20 bar.
20. A waste water purification apparatus comprising:
means for introducing finely-divided waste water having solid particles therein into a current of entrainment gas to form a mixture of entrainment gas and waste water;
evaporator means for receiving said mixture and heating said mixture to a temperature which is above the saturation temperature of water vapor which is formed during the heating of said mixture wherein the water vapor, solid particles and entrainment gas mixture resulting from said heating is substantially free of water droplets; said evaporating means being operably associated with said waste water introducing means; and means for separating the solid particles from the heated mixture, in communication with the evaporating means wherein a purified mixture of entrainment gas and water vapor is extracted from said separating means.
means for introducing finely-divided waste water having solid particles therein into a current of entrainment gas to form a mixture of entrainment gas and waste water;
evaporator means for receiving said mixture and heating said mixture to a temperature which is above the saturation temperature of water vapor which is formed during the heating of said mixture wherein the water vapor, solid particles and entrainment gas mixture resulting from said heating is substantially free of water droplets; said evaporating means being operably associated with said waste water introducing means; and means for separating the solid particles from the heated mixture, in communication with the evaporating means wherein a purified mixture of entrainment gas and water vapor is extracted from said separating means.
21. The improved apparatus for the purification of waste water according to Claim 20 wherein the separator means includes an outlet, and a compressor means is in communication with said separator outlet wherein the purified mixture of entrainment gas and water vapor is compressed, said compressor means including a pressure line which leads to the entrance of a heating medium NHL-KFJ-09 Canada line of the evaporator means and wherein connected to the end of the heating medium line there is a condensate line for the removal of the condensate formed in the evaporator and an outlet for compressed entrainment gas.
22. The improved apparatus for the purification of waste water according to Claim 21 including a heater means in communication with the heating medium in communication with the heating medium line of the evaporation, wherein the purified mixture of entrainment gas and water vapor is heated prior to entry into the heating medium line of the evaporator.
23. The improved apparatus for the purification of waste water according to Claim 22 including an outlet means for the entrainment gas located at the end of the heating medium line of the evaporation which empties into an entrainment gas line leading to the entrance of the evaporator.
24. The improved apparatus for the purification of waste water according to Claim 23 including a pressure regulator means disposed at a location where the outlet empties into the entrainment gas line.
25. The improved apparatus for the purification of waste water according to Claim 24 wherein a pressure reduction means is disposed between the evaporator means and the separator means.
26. The improved apparatus for the purification of waste water according to Claim 25 wherein the pressure reduction means is a swirl chamber for the coagulation of solid particles contained in the mixture of solid particles, entrainment gas and water vapor.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3337360.4-43 | 1983-10-14 | ||
| DE19833337360 DE3337360A1 (en) | 1983-10-14 | 1983-10-14 | METHOD AND DEVICE FOR WASTE WATER TREATMENT |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1225611A true CA1225611A (en) | 1987-08-18 |
Family
ID=6211798
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000465315A Expired CA1225611A (en) | 1983-10-14 | 1984-10-12 | Process and apparatus for waste water purification |
Country Status (10)
| Country | Link |
|---|---|
| US (2) | US4643832A (en) |
| EP (1) | EP0142018B1 (en) |
| JP (1) | JPS6097086A (en) |
| AT (1) | ATE26820T1 (en) |
| CA (1) | CA1225611A (en) |
| DE (2) | DE3337360A1 (en) |
| DK (1) | DK160084C (en) |
| GR (1) | GR80493B (en) |
| IL (1) | IL73202A (en) |
| SU (1) | SU1743352A3 (en) |
Families Citing this family (34)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3627477A1 (en) * | 1986-08-13 | 1988-02-25 | Extraktionstechnik Gmbh | METHOD FOR SEPARATING WATER-INSOLUBLE DISTILLATES FROM WATER STEAM |
| DE3834319A1 (en) * | 1988-10-08 | 1990-04-12 | Kernforschungsanlage Juelich | METHOD AND DEVICE FOR PRODUCING PURE WATER AND SUBSTANCES SOLVED IN WATER |
| US5376262A (en) * | 1993-06-08 | 1994-12-27 | Exxon Research And Engineering Company | Concentration and/disposal of non-volatile inorganic contaminants from refinery waste water streams |
| KR0119766B1 (en) * | 1993-11-23 | 1997-10-29 | 신호근 | Vaporizing and concentration drying apparatus and method |
| US5810977A (en) * | 1994-11-21 | 1998-09-22 | Aqua Health International Ltd. | Purifying water by superheated steam |
| DE19741806A1 (en) * | 1997-09-22 | 1999-03-25 | Nicolaos Dipl Phys Iniotakis | Purifying hot waste water containing a high organic or inorganic load of impurities by evaporation and compressing vapor |
| DE19833739C1 (en) * | 1998-07-27 | 2000-03-30 | Siemens Ag | Method and device for separating a neutron absorbing absorber from a coolant |
| US6497794B1 (en) | 1999-07-12 | 2002-12-24 | Marine Desalination Systems L.L.C. | Desalination using positively buoyant or negatively buoyant/assisted buoyancy hydrate |
| US6969467B1 (en) * | 1999-07-12 | 2005-11-29 | Marine Desalination Systems, L.L.C. | Hydrate-based desalination with hydrate-elevating density-driven circulation |
| US6673249B2 (en) | 2000-11-22 | 2004-01-06 | Marine Desalination Systems, L.L.C. | Efficiency water desalination/purification |
| US6890444B1 (en) | 2003-04-01 | 2005-05-10 | Marine Desalination Systems, L.L.C. | Hydrate formation and growth for hydrate-based desalination by means of enriching water to be treated |
| US6475460B1 (en) | 1999-07-12 | 2002-11-05 | Marine Desalination Systems Llc | Desalination and concomitant carbon dioxide capture yielding liquid carbon dioxide |
| US20040195160A1 (en) * | 1999-07-12 | 2004-10-07 | Marine Desalination Systems, L.L.C. | Hydrate-based reduction of fluid inventories and concentration of aqueous and other water-containing products |
| US6767471B2 (en) * | 1999-07-12 | 2004-07-27 | Marine Desalination Systems, L.L.C. | Hydrate desalination or water purification |
| US6565715B1 (en) | 1999-07-12 | 2003-05-20 | Marine Desalination Systems Llc | Land-based desalination using buoyant hydrate |
| AU2001270061A1 (en) * | 2000-06-26 | 2002-01-08 | Marine Desalination Systems, L.L.C. | Controlled cooling of input water by dissociation of hydrate in an artificially pressurized assisted desalination fractionation apparatus |
| US6635149B1 (en) * | 2000-10-26 | 2003-10-21 | Norman Campbell | Water purification system |
| DE10108528C1 (en) * | 2001-02-22 | 2002-06-13 | Neubert Susanne | Process for treating liquids e.g. seawater, brackish water, wastewater and effluent comprises using preheating/removal unit for preheating and pre-cleaning the liquid |
| US7008544B2 (en) * | 2002-05-08 | 2006-03-07 | Marine Desalination Systems, L.L.C. | Hydrate-based desalination/purification using permeable support member |
| JP2005270888A (en) * | 2004-03-25 | 2005-10-06 | Choonpa Jozosho Kk | Solution concentration method and concentrator to be used therein |
| RU2470869C2 (en) * | 2005-11-22 | 2012-12-27 | Острейлиан Криэйтив Текнолоджиз Пти Лтд | System of pipelines |
| DE102006042501B4 (en) * | 2006-09-07 | 2010-11-25 | Eisenmann Anlagenbau Gmbh & Co. Kg | Method and installation for drying objects |
| WO2009132327A1 (en) * | 2008-04-25 | 2009-10-29 | Jepson W Paul | Desalination method and apparatus |
| EA201000640A1 (en) * | 2010-04-05 | 2011-04-29 | Владимир Борисович ДУДИН | INSTALLATION FOR WATER CLEANING |
| US8709257B2 (en) * | 2010-04-20 | 2014-04-29 | King Abdulaziz City for Science and Technology (KACST) | Method and system for purifying liquid using waste heat |
| CN102887557B (en) * | 2011-07-18 | 2015-04-15 | 赵凤宇 | Equipment for desalination by glass ceramics dilutor and direct salt manufacturing and technology thereof |
| DE102013223837A1 (en) * | 2013-11-21 | 2015-05-21 | Siemens Aktiengesellschaft | Process for dewatering a suspension-like substance mixture |
| US9783431B2 (en) * | 2014-05-28 | 2017-10-10 | Katz Water Tech, Llc | Apparatus and method to remove contaminates from a fluid |
| RU2673841C2 (en) * | 2014-11-11 | 2018-11-30 | Юрий Михайлович Примазон | Cleaning device for draining of waste liquid |
| JP6566876B2 (en) | 2016-01-26 | 2019-08-28 | 東洋エンジニアリング株式会社 | Heat exchange amount adjustment method for internal heat exchange distillation column |
| RU2642560C2 (en) * | 2016-04-26 | 2018-01-25 | Общество с ограниченной ответственностью "НПО Пылеочистка" | Method of distilling liquids in inert gas environment |
| US10864482B2 (en) | 2017-08-24 | 2020-12-15 | Katz Water Tech, Llc | Apparatus system and method to separate brine from water |
| US11713258B2 (en) | 2017-08-24 | 2023-08-01 | Katz Water Tech, Llc | Apparatus system and method to extract minerals and metals from water |
| US11034605B2 (en) | 2018-03-29 | 2021-06-15 | Katz Water Tech, Llc | Apparatus system and method to extract minerals and metals from water |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE377747C (en) * | 1921-04-21 | 1923-06-26 | Otto Gutzwiller | Method and device for drying solid bodies in solution or in suspension within a liquid |
| US3306236A (en) * | 1964-09-11 | 1967-02-28 | Exxon Research Engineering Co | Burner for waste materials and method of burning waste materials |
| US3305091A (en) * | 1965-04-20 | 1967-02-21 | George A Brady | Method of separating liquid-solid suspensions into individual phases |
| CH493435A (en) * | 1969-01-13 | 1970-07-15 | Sutter Ernst | Process for the odor-free removal of waste water and / or sludge, installation for carrying out the process and application of the process |
| US4097378A (en) * | 1975-09-30 | 1978-06-27 | St Clair John Craig | Multiple effect evaporation of water from water containing combustible sludges |
| CH605428A5 (en) * | 1976-05-17 | 1978-09-29 | Von Roll Ag | |
| JPS601077B2 (en) * | 1981-03-28 | 1985-01-11 | 日本フア−ネス工業株式会社 | Sewage sludge evaporative concentrator |
-
1983
- 1983-10-14 DE DE19833337360 patent/DE3337360A1/en active Granted
-
1984
- 1984-09-27 GR GR80493A patent/GR80493B/en unknown
- 1984-10-09 DE DE8484112074T patent/DE3463365D1/en not_active Expired
- 1984-10-09 EP EP19840112074 patent/EP0142018B1/en not_active Expired
- 1984-10-09 AT AT84112074T patent/ATE26820T1/en not_active IP Right Cessation
- 1984-10-09 IL IL7320284A patent/IL73202A/en not_active IP Right Cessation
- 1984-10-10 DK DK485084A patent/DK160084C/en active
- 1984-10-12 SU SU843805259A patent/SU1743352A3/en active
- 1984-10-12 CA CA000465315A patent/CA1225611A/en not_active Expired
- 1984-10-13 JP JP59213295A patent/JPS6097086A/en active Pending
- 1984-10-15 US US06/660,942 patent/US4643832A/en not_active Expired - Fee Related
-
1986
- 1986-10-20 US US06/921,591 patent/US4767527A/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| IL73202A0 (en) | 1985-01-31 |
| GR80493B (en) | 1985-02-11 |
| DK485084D0 (en) | 1984-10-10 |
| DE3463365D1 (en) | 1987-06-04 |
| DK160084C (en) | 1991-06-10 |
| EP0142018B1 (en) | 1987-04-29 |
| EP0142018A1 (en) | 1985-05-22 |
| IL73202A (en) | 1987-09-16 |
| DK160084B (en) | 1991-01-28 |
| ATE26820T1 (en) | 1987-05-15 |
| US4767527A (en) | 1988-08-30 |
| DK485084A (en) | 1985-04-15 |
| DE3337360C2 (en) | 1989-10-26 |
| US4643832A (en) | 1987-02-17 |
| SU1743352A3 (en) | 1992-06-23 |
| JPS6097086A (en) | 1985-05-30 |
| DE3337360A1 (en) | 1985-05-02 |
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