CA1114132A - Process for selective removal of sodium sulfate from an aqueous slurry - Google Patents
Process for selective removal of sodium sulfate from an aqueous slurryInfo
- Publication number
- CA1114132A CA1114132A CA324,172A CA324172A CA1114132A CA 1114132 A CA1114132 A CA 1114132A CA 324172 A CA324172 A CA 324172A CA 1114132 A CA1114132 A CA 1114132A
- Authority
- CA
- Canada
- Prior art keywords
- slurry
- sodium
- wash
- sodium hydroxide
- sodium sulfate
- 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
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/14—Purification
Abstract
ABSTRACT
A process for selectively removing sodium sulfate and sodium hydroxide from an aqueous slurry containing sodium chloride, sodium sulfate and sodium hydroxide, which comprises contacting the slurry in a countercurrent wash step with cool water to remove sodium sulfate and sodium hydroxide therefrom.
A process for selectively removing sodium sulfate and sodium hydroxide from an aqueous slurry containing sodium chloride, sodium sulfate and sodium hydroxide, which comprises contacting the slurry in a countercurrent wash step with cool water to remove sodium sulfate and sodium hydroxide therefrom.
Description
; :
PROCESS FOR SELECTIVE REMOVAL OF
SODIUM SULFATE FROM AN AQUEOUS SLIJRRY
In the electrochemical production of chlorine and sodium hydroxide, brine containing sodium chloride and minor amounts of other salts, such as calcium sulfate, is fed to electrolytic cells. Since the calcium may interfere with cell operation, it is custom-ary practice to precipitate the calcium with a carbonate, such as sodium carbonate. The calcium carbonate precipi-tate is removed from the brine blefore it is fed to the cell, but the sodium sulfate prolduced during such precipitation is carried into thle cell along with the sodium chloride. Chlorine in gaseous form is taken off overhead from the cell and sodiw~ hydroxide in the cell effluent is recovered in more concentrated form rom evaporators. The cell efluent contains substantial amounts of sodium chloride which is customarily returned to the brine fPed and recycled through the electrolytic cells.
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The sodium sulfate has a decreased solubility in concentrated sodium hydroxide solutions, and precipi- -tates out in the evaporators along with the sodium chloride. Sodium sulfate tends to build up on recycle :
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through the evaporators and may cause decreased current efficiency in the electrolytic cell as well as high caustic losses during the separation of the caustic from the cell effluent. Consequently, it is desirable to remove as much of the sodium sulfate as possible from the sodium chloride before it is returned as brine feed to the electrolytic cells. It is also desirable that the sodium sulfate be removed in as concentrated form as possible in order to reduce capital expendi- ~
tures necessary to further process the sulfate stream for discard or for production of a salable chemical.
It is also desirable to remove all but a minor portion of the sodium hydroxide from the sodium chloride that is to be used as brine feed for the cellsrin order to maintain the proper pH level in the cells.
One way of approaching this overall problem, and a suggested process for solving it, is set forth in U. S. Patent No. 4,087,253. This patent proposes using a caustic solution of less than 35% sodium hydroxide to effect separation of the sodium sulfate from the sodium chloride salt. While in theory this problem of separating sodium sulfate and sodium hydroxide from sodium chloride could be resolved by reference to e~lilibrium graphs or charts showing the solubility of these salts in aqueous ~5 solution, there are certain secondary phenomena, such as the formation of the triple salt of sodium hydroxide--sodium sulfate-sodium chloride, that prevent dependable prediction of optimum concentrations, temperatures and flow rat~s for the separation of these salts. Consequently, the solution to this problem of separating the sodium sulfate and sodium hydroxide from highly concentrated solutions or slurries of sodium chloride must depend upon empirical experimentation.
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27,322-F
~ ............. . . .- - - - . .. , --It has now been found that sodium sulfate and sodium hydroxide may be removed from an aqueous slurry containing these compounds and sodium chloride in par-ticulate form, in a saturated aqueous solution thereof, by contacting such a slurry in a countercurrent wash step with cool water.
The present invention particularly resides in a process for selectively removing sodium hydroxide and sodium sulfate from admixture with sodium chloride, `
which comprises making an aqueous slurry of such mixture, contacting the slurry in a countercurrent flow relationship with wash water at a temperature of 45 to 120F, and removing the wash water from the slurry and with it a major portion of the sodium hydroxide and sodium sulfate contained in the slurry.
The present invention also resides in a process for separating sodium hydroxide a~nd sodium sulfate from a slurry containing the -e~a4 in admixture with sodium chloride in particulate form,- which comprises feeding said slurry into an upper portion of a wash column such that the slurry moves downwardly through the wash column, introducing a stream of wash water, at a temperature in the range of 45 to 120F, into the lower portion of the wash column such that the wash water moves upwardly through the column in counter-current flow relationship to the said slurry, removing overflow fluid from the wash column at or near the top of the wash column, said overflow fluid carrying with ~-it most of the sodium hydroxide and sodium sulfate from said slurry, and recovering sodium chloride in the underflow from the lower portion of the wash column.
27,322-F
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-3a-The present invention further resides in a :~
process for removing sodium hydroxide and sodium sulfate from a slurry containing 20 to 45~ by weight sodium chloride, 2 to 7% by weight sodium sulfate and 4 to 16%
by weight of sodium hydroxide, the settled volume of the slurry being within the range of 15 to 30%, which comprises feeding said slurry into the upper portion-of a wash column in such a manner that the slurry moves downwardly through the wash column, sparging a stream of wash water at a temperature in the range `
of from 45 to 80F. into the lower portion of the :`
wash column in such a manner that the wash water moves upwardly through the column in countercurrent relation-ship to said slurry, removing overflow fluid at or:~
near the top of the wash column, said overflow fluid carrying with it a major portion of the sodium hydroxide ~ -and sodium sulfate contained in said slurry, and re-covering the purified sodium chloride in the underflow from the lower portion of the wash column.
The present invention also resides in an electrolytic process for making ahlorine and sodium hydroxide wherein cell effluent is concentrated to a mixture containing sodium hydroxide, sodium sulfate and composed principally of sodium chloride, the improved process for separating sodium hydroxide and sodium sulfate from said mixture which comprises making an aqueous slurry of such a mixture wherein the sodium chloride is present in particulate form, :
contacting such slurry in a countercurrent relationship with wash water at a temperature in the range of 45 to 120F, removing the wash water from the slurry 27,322-F
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': '' ' '~' -3b-and with it a major portion of the sodium hydroxide and sodium sulfate contained in the slurry, and re-covering sodium chloride from the mixture.
The process of the present invention has been found to be particularly useful in the separation of sodium sulfate and sodiurn hydroxide from the salt cake `
derived from centrifuge or flat bed filters that are downstream from the evaporators employed to concentrate sodium hydroxide in the cell effluent from chloralkali electrolytic cells. Water is added to the salt scrolled from the salt cake to produce a slurry for treatment hereunder. It will be apparent to one skilled in the art that the present invention is equally applicable to the treatment of any slurry having compositions as described herein, regardless of the source of that slurry. The slurries to which the present invention is applicable are those containing sodium hydroxide, sodium sulfate and sodium chloride, the sodium chloride being present in particulate ~orm in a saturated aqueous solution of this salt. These salts may also be present in various complex forms, such as the riple salt ~NaOH-NaCl Na2SO4). It is possible to wash such a slurry in many ways, such as by the use of centrifuges and equilibrium filters where the salt cake is stirred in an aqueous environmen and then the supernatant fluid is passed through a filter bed. Relatively ~ar~
or even hot, process water may be employed. It has been found, however, that a very substantial improvement in .
27,322-F
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the percent of sodium sulfate and sodium hydro~ide removed from such a slurry can be achieved by employing a wash step wherein cool wash water contacts the slurry to be treated in a countercurrent relationship. There are many forms of equipment that may be employed for this countercurrent washing of the slurry, and the particular type of apparatus that is employed does not form a part of the present invention. It is only essential that the slurry be contacted with cool wash water in a countercurrent relationship, so that the sodium sulfate and sodium hydroxide are removed in the overflow stream and the purified sodium chloride is recovered from the underflow stream of the wash column.
In order to more fully describe the present invention, the invention will be discussed in detail in connection with a particular embodiment thereof disclosed in the accompanying drawings, wherein Figure 1 is a flow sheet representing a chloralkali plant; Figure 2 is a diagrammatic drawing of the wash column hereinafter described, and Figure 3 graphically illustrates the ~p P~/`C ~?~ t removal of NaOH and Na2S04 in ~ee~t by weight, plotted against the temperature of the wash water in degrees Farenheit.
Referring now to Figure 1, salt is customarily mined from wells which bring the salt up to the surface in the form o~ aqueous brine. The brine is then pumped to electrolytic cells from which chlorine is recovered in gaseous form and the cell effluent then directed to a series of evaporators from which is obtained caustic in a more concentrated form, such as a 50% solution.
From the evaporators, an aqueous, caustic slurry of inorganic salts is directed to a flat bed filter.
Salt is scrolled off the filter and water added 27,322-F
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which produces a slurry containing varying amounts of sodium chloride as well as sodium hydroxide and sodium sulfate. It will be understood that references herein `
to "percentages", other than those respecting settled volume, are references to percent by weight unless otherwise sta-ted. It is preferred to maintain the amount of sodium hydroxide in such a slurry below about 10%, since sodium hydroxide in excess of this amount suppresses the dissolution of sodium sulfate in the wash water and can cause difficulty in the subsequent production o~ sulfate salts. The present process may be practiced, however, with NaOH levels as high as about 16%. The most effective removal of the sodium sulfate has been found to occur when the amount of sodium sulfate in the slurry is between 4 to 7%. The amount of water in the slurry is regulated in order to obtain a settled volume which will range from 15 to 30%. The term "settled volume" as used herein means that percent of the total volume of the aqueous slurry that is occupied by the insoluble material in suspension.
In the particular type of wash column employed and as described hereafter, a slurry having a settled volume in excess of 22% is preferred. The flow rate at which the slurry is introduced into the wash column and the settled volume of the salt slurry will vary, of course, with the particular size and type of wash column employed.
Settled volumes as high as 40% could be used with some wash columns.
The slurry from the flat bed filter is fed to the wash column, shown in greater detail in Figure 2, at a temperature ranging from 120F to 170F. This slurry is directed onto a feed distribution tray in the wash column which aids in dispersing slurry uniformly ; 27,322-F
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i over the upper portion of the column. As the slurry moves downwardly through the column, a phase designated as "clears" or supernatant liquid is formed above a ~
phase indicated as "solids" composed essentially of -loosely packed, particulate sodium chloride. A conical member designated as a "sputnik" is located near the bottom portion of the wash column and performs the function of preventing or diminishing channeling of more solidly packed, particulate sodium chloride.
As shown in Figure 2, wash water is intro-duced near the bottom portion of the wash column through a plurality of spargers which direct the water upwardly through a series of small holes formed in two radial or ring like spargers and two axial spargers. Since the water enters the wash column under pressure, it helps to prevent or reduce channeling of the particulate ?
sodium chloride in the bottom portion of the wash column. The temperature of the wash water may vary from 45F to 120F. At 120F on:Ly about 70% removal of the Na2SO4 is obtained, so that :it will be necessary to reduce the wash water temperature to about 100F in commercial operations that cannot tolerate this much build-up of sodium sulfate in the recycled cell efflu~nt.
Greatly improved removal of sodium sulfate is achieved, however, when the wash water is below 80F and still more remarkable removal of over 90% of the sodium sulfate from the slurry can be achieved by maintaining the wash water at a temperature of from 45 to 60F.
The flow rate of wash water will, of course, depend upon the amount of slurry being introduced to the wash column as well as the rate of underflow. As a particular example of one embodiment of the invention, however, when the amount of slurry supplied is in the range of , ~
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about 140 gallons per minute, the wash water flow rate may vary from 30 to 45 gallons per minute. The overflow from the wash column shown in Figure 2 amounts ~o the difference between the volume input of the slurry and wash water less the volume of materials removed as underflow. For example, when slurry is supplied at the rate of 140 gallons per minute, the wash column and the wash water input is 40 gallons per minute, an underflow rate of 32 gallons per minute will produce an overflow of approximately 148 gallons per minute. The most efficient removal of sodium hydroxide and sodium sulfate from the slurry occurs when the overflow e~uals or exceeds the rate of flow of the slurry. This overflow carries off a major portion of the sodium sulfate and sodium hydroxide. Under the preferred conditions, with cool wash water of less than 80F, and preferably from ~5 to 60F, approximately 95% of the sodium hydroxide and about 90% of the sodium sulfate can be removed from the slurry being treated. This overflow, which contains relatively large amounts of sodium sul~ate and sodium hydroxide as well as sodium chloride, is sent to the sulfate disposal plant, where it may be further processed into a salable product containing sulfate or some other environmentally acceptable foxm for subse~uent discard.
~he underflow from the wash column contains the purified sodium chloride and typically contains less than 1% each of sodium hydroxide and sodium sulfate. ;
The flow rate of the underflow is regulated by the operation of the wash column and must be sufficiently high to avoid salt build-up which will plug the under-flow pipe lines. In one particular embodiment of the present invention wherein the slurry is introduced at the rate of 140 gallons per minute and wash water was 27,322-F
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,, introduced at the rate of 40 gallons per millute, an underflow of 32 gallons per minute was found to provide satisfactor~ operation of the ~ash column.
This underflow contains a relatively high percentage of particulate sodium chloride, so that the settled volume of the underflow will vary from 40 to 90%. Carrier water is introduced, as shown in Figure 2, in order to dilute the underflow and to better enable it to be pumped ~without plugging of the pipe lines~ to the brine tanks for subsequent recycling through the electrolytic cells.
The following examples are set forth by way of illustration and not by way of limitation, it being understood that the present inv0ntion is limited only as defined in the claims attached hereto.
Example 1 A wash column, as diagrammatically shown in Figure 2, was in-stalled in a chloralkali plant in the manner shown in the flow chart in ~igure 1. The wash column in this particular embodiment was six feet in diameter and twenty-one feet tall. Salt scrolled off flat bed filters downstream from the evaporators was slurried with water and this slurry was then fed to the ~ash column at a temperature in the range of 120F to 170F
and at a flow rate of about 140 gallons per minute, with variations as low as lOQ gallons per minute and as high as 190 gallons per minute. A
ty~ical co~position of t~e slurr~ was about 7% sodium hydroxide, about 5%
sodium sulfa~e and about 35% sodium chloride with the balance being water.
The typical settled yolume of this slurry was about 23%. The composition and settled volume of the slurry feed varied, however, within the ranges aboye set forth.
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The slurry feed coming in at the top of the wash column was direc-ted onto a feed distribution tray which is in -the form of an "X" with slots cut through the arms to disperse the slurry uniformly across a broad cross section of the column. Optimum operation of the wash column was obtained when the bed level of the salt (or "solids" as shown in Figure 2) was about eight feet deep or a 40% level. The bed level is con-trolled by the rate of flow of the underflow, which is preferably maintained at about 32 gallons per minute.
Wash water is introduced at the bottom of the column at a flow rate between 32 and 40 gallons per minute, the higher rate being preferred because it assists in reducing solid salt build-up in the column.
The temperature of the wash water was varied, and the results of such variation are discussed in Examples 2 and 3. The temperature of the wash water is preferably maintained at about 60F.
When the slurry is fed into the wash column at a rate of 140 gallons per mimlte and wash water is introduced at the rate of 40 gal]Lons per minute, and the underflow is removed from th~3 wash column at 30 gallons per minute, the overflow rate is thereby deter-mined as 150 gallons per minute. The overflow from the wash column is removed at the top of the vessel into a launder where it is collected and sent to the sulfate disposal plant. When operating with typical slurry compositions and under preferred conditions, all as described above, the overflow contains approximately 30 6.5% sodium hydroxide, about 4.5% sodium sulfate and -about 21% sodium chloride. It has been found that under the conditions stated in this example, at least 27,322-F
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95% of the sodium hydroxide and at least 90% of the sodium sulfate are removed in the overflow from the slurry that is fed into the wash column.
Example 2 The wash column described in Example 1 was operated at different wash water temperatures to deter-mine the effect of wash water temperature on the per-cent removal of sodium hydroxide and sodium sulfate. ~;~
The results are presented graphically in Figure 3.
Wash water temperature has only a slight effect on the percentage of sodium hydroxide removed from the slurry, - which consistently runs from 95 to 99%. At temperatures above about 80F, the percentage of sodium sulfate removed varies widely even at the same wash water temperature, indicating that a number of factors affect the amount of sodium sulfate removed in the overflow.
However, even here lower ones of these wash temperatures show an increase in the amount of sodium sulfate removed.
At wash water temperatures of about 60F, however, approximately 95% to 98~ removal of the sodium sulfate is consistently attained. ~;
` Example 3 To further illustrate the invention, operating data relating to the operation of the wash column that - 25 has been described and shown in Example 1 is set forth in the iollouing Table:
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It will become apparent from the above detailed description of the invention, as well as the Examples above set forth, that many variations and modifications may be made in the particular embodiments of the inven-tion set forth herein without departing from the invention.For example, the present invention is applicable to the removal of sodium sulfate and sodium hydroxide from admixture with sodium chloride regardless of the source of that particular admixture, and is not restricted to such admixtures occurring in a chloralkali plant.
References herein to "overflow" and "underflow" define relative positioning of these means of removing fluids and/or slurries from the wash column, and should not be interpreted to mean that "overflow" necessarily refers to removal over the top of the column or that "underflow"
means removal at the bottom of the column. Other variations and modifications of the present invention will become apparent to those skilled in the art, and the present invention is to be limited only as set forth in the following claims.
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:
PROCESS FOR SELECTIVE REMOVAL OF
SODIUM SULFATE FROM AN AQUEOUS SLIJRRY
In the electrochemical production of chlorine and sodium hydroxide, brine containing sodium chloride and minor amounts of other salts, such as calcium sulfate, is fed to electrolytic cells. Since the calcium may interfere with cell operation, it is custom-ary practice to precipitate the calcium with a carbonate, such as sodium carbonate. The calcium carbonate precipi-tate is removed from the brine blefore it is fed to the cell, but the sodium sulfate prolduced during such precipitation is carried into thle cell along with the sodium chloride. Chlorine in gaseous form is taken off overhead from the cell and sodiw~ hydroxide in the cell effluent is recovered in more concentrated form rom evaporators. The cell efluent contains substantial amounts of sodium chloride which is customarily returned to the brine fPed and recycled through the electrolytic cells.
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The sodium sulfate has a decreased solubility in concentrated sodium hydroxide solutions, and precipi- -tates out in the evaporators along with the sodium chloride. Sodium sulfate tends to build up on recycle :
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through the evaporators and may cause decreased current efficiency in the electrolytic cell as well as high caustic losses during the separation of the caustic from the cell effluent. Consequently, it is desirable to remove as much of the sodium sulfate as possible from the sodium chloride before it is returned as brine feed to the electrolytic cells. It is also desirable that the sodium sulfate be removed in as concentrated form as possible in order to reduce capital expendi- ~
tures necessary to further process the sulfate stream for discard or for production of a salable chemical.
It is also desirable to remove all but a minor portion of the sodium hydroxide from the sodium chloride that is to be used as brine feed for the cellsrin order to maintain the proper pH level in the cells.
One way of approaching this overall problem, and a suggested process for solving it, is set forth in U. S. Patent No. 4,087,253. This patent proposes using a caustic solution of less than 35% sodium hydroxide to effect separation of the sodium sulfate from the sodium chloride salt. While in theory this problem of separating sodium sulfate and sodium hydroxide from sodium chloride could be resolved by reference to e~lilibrium graphs or charts showing the solubility of these salts in aqueous ~5 solution, there are certain secondary phenomena, such as the formation of the triple salt of sodium hydroxide--sodium sulfate-sodium chloride, that prevent dependable prediction of optimum concentrations, temperatures and flow rat~s for the separation of these salts. Consequently, the solution to this problem of separating the sodium sulfate and sodium hydroxide from highly concentrated solutions or slurries of sodium chloride must depend upon empirical experimentation.
`;
27,322-F
~ ............. . . .- - - - . .. , --It has now been found that sodium sulfate and sodium hydroxide may be removed from an aqueous slurry containing these compounds and sodium chloride in par-ticulate form, in a saturated aqueous solution thereof, by contacting such a slurry in a countercurrent wash step with cool water.
The present invention particularly resides in a process for selectively removing sodium hydroxide and sodium sulfate from admixture with sodium chloride, `
which comprises making an aqueous slurry of such mixture, contacting the slurry in a countercurrent flow relationship with wash water at a temperature of 45 to 120F, and removing the wash water from the slurry and with it a major portion of the sodium hydroxide and sodium sulfate contained in the slurry.
The present invention also resides in a process for separating sodium hydroxide a~nd sodium sulfate from a slurry containing the -e~a4 in admixture with sodium chloride in particulate form,- which comprises feeding said slurry into an upper portion of a wash column such that the slurry moves downwardly through the wash column, introducing a stream of wash water, at a temperature in the range of 45 to 120F, into the lower portion of the wash column such that the wash water moves upwardly through the column in counter-current flow relationship to the said slurry, removing overflow fluid from the wash column at or near the top of the wash column, said overflow fluid carrying with ~-it most of the sodium hydroxide and sodium sulfate from said slurry, and recovering sodium chloride in the underflow from the lower portion of the wash column.
27,322-F
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-3a-The present invention further resides in a :~
process for removing sodium hydroxide and sodium sulfate from a slurry containing 20 to 45~ by weight sodium chloride, 2 to 7% by weight sodium sulfate and 4 to 16%
by weight of sodium hydroxide, the settled volume of the slurry being within the range of 15 to 30%, which comprises feeding said slurry into the upper portion-of a wash column in such a manner that the slurry moves downwardly through the wash column, sparging a stream of wash water at a temperature in the range `
of from 45 to 80F. into the lower portion of the :`
wash column in such a manner that the wash water moves upwardly through the column in countercurrent relation-ship to said slurry, removing overflow fluid at or:~
near the top of the wash column, said overflow fluid carrying with it a major portion of the sodium hydroxide ~ -and sodium sulfate contained in said slurry, and re-covering the purified sodium chloride in the underflow from the lower portion of the wash column.
The present invention also resides in an electrolytic process for making ahlorine and sodium hydroxide wherein cell effluent is concentrated to a mixture containing sodium hydroxide, sodium sulfate and composed principally of sodium chloride, the improved process for separating sodium hydroxide and sodium sulfate from said mixture which comprises making an aqueous slurry of such a mixture wherein the sodium chloride is present in particulate form, :
contacting such slurry in a countercurrent relationship with wash water at a temperature in the range of 45 to 120F, removing the wash water from the slurry 27,322-F
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:: , . ', . .
': '' ' '~' -3b-and with it a major portion of the sodium hydroxide and sodium sulfate contained in the slurry, and re-covering sodium chloride from the mixture.
The process of the present invention has been found to be particularly useful in the separation of sodium sulfate and sodiurn hydroxide from the salt cake `
derived from centrifuge or flat bed filters that are downstream from the evaporators employed to concentrate sodium hydroxide in the cell effluent from chloralkali electrolytic cells. Water is added to the salt scrolled from the salt cake to produce a slurry for treatment hereunder. It will be apparent to one skilled in the art that the present invention is equally applicable to the treatment of any slurry having compositions as described herein, regardless of the source of that slurry. The slurries to which the present invention is applicable are those containing sodium hydroxide, sodium sulfate and sodium chloride, the sodium chloride being present in particulate ~orm in a saturated aqueous solution of this salt. These salts may also be present in various complex forms, such as the riple salt ~NaOH-NaCl Na2SO4). It is possible to wash such a slurry in many ways, such as by the use of centrifuges and equilibrium filters where the salt cake is stirred in an aqueous environmen and then the supernatant fluid is passed through a filter bed. Relatively ~ar~
or even hot, process water may be employed. It has been found, however, that a very substantial improvement in .
27,322-F
::
: ' ' .: ' ' ~ ' , .
the percent of sodium sulfate and sodium hydro~ide removed from such a slurry can be achieved by employing a wash step wherein cool wash water contacts the slurry to be treated in a countercurrent relationship. There are many forms of equipment that may be employed for this countercurrent washing of the slurry, and the particular type of apparatus that is employed does not form a part of the present invention. It is only essential that the slurry be contacted with cool wash water in a countercurrent relationship, so that the sodium sulfate and sodium hydroxide are removed in the overflow stream and the purified sodium chloride is recovered from the underflow stream of the wash column.
In order to more fully describe the present invention, the invention will be discussed in detail in connection with a particular embodiment thereof disclosed in the accompanying drawings, wherein Figure 1 is a flow sheet representing a chloralkali plant; Figure 2 is a diagrammatic drawing of the wash column hereinafter described, and Figure 3 graphically illustrates the ~p P~/`C ~?~ t removal of NaOH and Na2S04 in ~ee~t by weight, plotted against the temperature of the wash water in degrees Farenheit.
Referring now to Figure 1, salt is customarily mined from wells which bring the salt up to the surface in the form o~ aqueous brine. The brine is then pumped to electrolytic cells from which chlorine is recovered in gaseous form and the cell effluent then directed to a series of evaporators from which is obtained caustic in a more concentrated form, such as a 50% solution.
From the evaporators, an aqueous, caustic slurry of inorganic salts is directed to a flat bed filter.
Salt is scrolled off the filter and water added 27,322-F
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which produces a slurry containing varying amounts of sodium chloride as well as sodium hydroxide and sodium sulfate. It will be understood that references herein `
to "percentages", other than those respecting settled volume, are references to percent by weight unless otherwise sta-ted. It is preferred to maintain the amount of sodium hydroxide in such a slurry below about 10%, since sodium hydroxide in excess of this amount suppresses the dissolution of sodium sulfate in the wash water and can cause difficulty in the subsequent production o~ sulfate salts. The present process may be practiced, however, with NaOH levels as high as about 16%. The most effective removal of the sodium sulfate has been found to occur when the amount of sodium sulfate in the slurry is between 4 to 7%. The amount of water in the slurry is regulated in order to obtain a settled volume which will range from 15 to 30%. The term "settled volume" as used herein means that percent of the total volume of the aqueous slurry that is occupied by the insoluble material in suspension.
In the particular type of wash column employed and as described hereafter, a slurry having a settled volume in excess of 22% is preferred. The flow rate at which the slurry is introduced into the wash column and the settled volume of the salt slurry will vary, of course, with the particular size and type of wash column employed.
Settled volumes as high as 40% could be used with some wash columns.
The slurry from the flat bed filter is fed to the wash column, shown in greater detail in Figure 2, at a temperature ranging from 120F to 170F. This slurry is directed onto a feed distribution tray in the wash column which aids in dispersing slurry uniformly ; 27,322-F
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, ' , .
'~ . , ' :, . : . .
i over the upper portion of the column. As the slurry moves downwardly through the column, a phase designated as "clears" or supernatant liquid is formed above a ~
phase indicated as "solids" composed essentially of -loosely packed, particulate sodium chloride. A conical member designated as a "sputnik" is located near the bottom portion of the wash column and performs the function of preventing or diminishing channeling of more solidly packed, particulate sodium chloride.
As shown in Figure 2, wash water is intro-duced near the bottom portion of the wash column through a plurality of spargers which direct the water upwardly through a series of small holes formed in two radial or ring like spargers and two axial spargers. Since the water enters the wash column under pressure, it helps to prevent or reduce channeling of the particulate ?
sodium chloride in the bottom portion of the wash column. The temperature of the wash water may vary from 45F to 120F. At 120F on:Ly about 70% removal of the Na2SO4 is obtained, so that :it will be necessary to reduce the wash water temperature to about 100F in commercial operations that cannot tolerate this much build-up of sodium sulfate in the recycled cell efflu~nt.
Greatly improved removal of sodium sulfate is achieved, however, when the wash water is below 80F and still more remarkable removal of over 90% of the sodium sulfate from the slurry can be achieved by maintaining the wash water at a temperature of from 45 to 60F.
The flow rate of wash water will, of course, depend upon the amount of slurry being introduced to the wash column as well as the rate of underflow. As a particular example of one embodiment of the invention, however, when the amount of slurry supplied is in the range of , ~
27,322-F
. . ' .a~
about 140 gallons per minute, the wash water flow rate may vary from 30 to 45 gallons per minute. The overflow from the wash column shown in Figure 2 amounts ~o the difference between the volume input of the slurry and wash water less the volume of materials removed as underflow. For example, when slurry is supplied at the rate of 140 gallons per minute, the wash column and the wash water input is 40 gallons per minute, an underflow rate of 32 gallons per minute will produce an overflow of approximately 148 gallons per minute. The most efficient removal of sodium hydroxide and sodium sulfate from the slurry occurs when the overflow e~uals or exceeds the rate of flow of the slurry. This overflow carries off a major portion of the sodium sulfate and sodium hydroxide. Under the preferred conditions, with cool wash water of less than 80F, and preferably from ~5 to 60F, approximately 95% of the sodium hydroxide and about 90% of the sodium sulfate can be removed from the slurry being treated. This overflow, which contains relatively large amounts of sodium sul~ate and sodium hydroxide as well as sodium chloride, is sent to the sulfate disposal plant, where it may be further processed into a salable product containing sulfate or some other environmentally acceptable foxm for subse~uent discard.
~he underflow from the wash column contains the purified sodium chloride and typically contains less than 1% each of sodium hydroxide and sodium sulfate. ;
The flow rate of the underflow is regulated by the operation of the wash column and must be sufficiently high to avoid salt build-up which will plug the under-flow pipe lines. In one particular embodiment of the present invention wherein the slurry is introduced at the rate of 140 gallons per minute and wash water was 27,322-F
' ` ' ' ' `' ' ' ' ' ' ' ` ' ' .
,, ,: .. . . ' .' , . :
.
- ~ :
- ,. . : . .
.
,, introduced at the rate of 40 gallons per millute, an underflow of 32 gallons per minute was found to provide satisfactor~ operation of the ~ash column.
This underflow contains a relatively high percentage of particulate sodium chloride, so that the settled volume of the underflow will vary from 40 to 90%. Carrier water is introduced, as shown in Figure 2, in order to dilute the underflow and to better enable it to be pumped ~without plugging of the pipe lines~ to the brine tanks for subsequent recycling through the electrolytic cells.
The following examples are set forth by way of illustration and not by way of limitation, it being understood that the present inv0ntion is limited only as defined in the claims attached hereto.
Example 1 A wash column, as diagrammatically shown in Figure 2, was in-stalled in a chloralkali plant in the manner shown in the flow chart in ~igure 1. The wash column in this particular embodiment was six feet in diameter and twenty-one feet tall. Salt scrolled off flat bed filters downstream from the evaporators was slurried with water and this slurry was then fed to the ~ash column at a temperature in the range of 120F to 170F
and at a flow rate of about 140 gallons per minute, with variations as low as lOQ gallons per minute and as high as 190 gallons per minute. A
ty~ical co~position of t~e slurr~ was about 7% sodium hydroxide, about 5%
sodium sulfa~e and about 35% sodium chloride with the balance being water.
The typical settled yolume of this slurry was about 23%. The composition and settled volume of the slurry feed varied, however, within the ranges aboye set forth.
'` ., ',.
~ .
.. ' ~, . . . . .. . .
-: ~ ' ,~ ' ' ; ' . `
- . :. -: . . ., ~ ,- ,.' :
.
The slurry feed coming in at the top of the wash column was direc-ted onto a feed distribution tray which is in -the form of an "X" with slots cut through the arms to disperse the slurry uniformly across a broad cross section of the column. Optimum operation of the wash column was obtained when the bed level of the salt (or "solids" as shown in Figure 2) was about eight feet deep or a 40% level. The bed level is con-trolled by the rate of flow of the underflow, which is preferably maintained at about 32 gallons per minute.
Wash water is introduced at the bottom of the column at a flow rate between 32 and 40 gallons per minute, the higher rate being preferred because it assists in reducing solid salt build-up in the column.
The temperature of the wash water was varied, and the results of such variation are discussed in Examples 2 and 3. The temperature of the wash water is preferably maintained at about 60F.
When the slurry is fed into the wash column at a rate of 140 gallons per mimlte and wash water is introduced at the rate of 40 gal]Lons per minute, and the underflow is removed from th~3 wash column at 30 gallons per minute, the overflow rate is thereby deter-mined as 150 gallons per minute. The overflow from the wash column is removed at the top of the vessel into a launder where it is collected and sent to the sulfate disposal plant. When operating with typical slurry compositions and under preferred conditions, all as described above, the overflow contains approximately 30 6.5% sodium hydroxide, about 4.5% sodium sulfate and -about 21% sodium chloride. It has been found that under the conditions stated in this example, at least 27,322-F
- . .
. . .
- , , ~ , .
95% of the sodium hydroxide and at least 90% of the sodium sulfate are removed in the overflow from the slurry that is fed into the wash column.
Example 2 The wash column described in Example 1 was operated at different wash water temperatures to deter-mine the effect of wash water temperature on the per-cent removal of sodium hydroxide and sodium sulfate. ~;~
The results are presented graphically in Figure 3.
Wash water temperature has only a slight effect on the percentage of sodium hydroxide removed from the slurry, - which consistently runs from 95 to 99%. At temperatures above about 80F, the percentage of sodium sulfate removed varies widely even at the same wash water temperature, indicating that a number of factors affect the amount of sodium sulfate removed in the overflow.
However, even here lower ones of these wash temperatures show an increase in the amount of sodium sulfate removed.
At wash water temperatures of about 60F, however, approximately 95% to 98~ removal of the sodium sulfate is consistently attained. ~;
` Example 3 To further illustrate the invention, operating data relating to the operation of the wash column that - 25 has been described and shown in Example 1 is set forth in the iollouing Table:
. .
~: ' 27,322-F
,~
`' ' : ` . . :.
: , : ' ` `. ~:
-.
.
~LiL`~
U~
~1 t` ~ ~ ~ Lr~ ~1 U~
Z :, .
~o h ~1 ~:1 ~ ~ Il~ 0 ~ ~ 1` ~ ~ ~:
~ P~ O ~ ~1 ~ O Ln ~1 0 ~1 ~1 ~ ~ Z .........
3 0 ~ ` o o ,1 ,~
O ~ ~ ~ (~
,1 ~
~ ~ _ ~ ~ ~ ~ ~ 0 C~ o~ o~ CO 1`
~ 3 ~ Ll~ Ln In U~ Lt~ L~ .r) ul E~ .
_~
1¢ ~: 3 ~: o o o o o o o U~ ~R O ~:4 d~ d1 ~ ~ ~ di d~
3 1~ ~
~ ~ :.`
,~ O o In ~D ~1 0 0 U~ ';~'. .
:~ ~ . . . . . . . ..
~ Z d' ~1 ~ ~ ~ ~ IY) .
~ \
:' 0~ ~ d' ~ ~ 0 ~
~; l` co ~ ~ 0 ~l o ~a ~ ~ . .
- ~ . .
o~ o o o ~ o o o o : ;
~1 ~ U ~ ~ ~ ~ ~ d1 Lr) ~` : .
27, 322-F
:i. ` . : : : . : :
` .
'~ o~ ~
o ~ ~
~) ~ ~d ~ U) ~` ~ ~ t` `
P z; ~ cr~
~ S~ ' i - "
P: ~
~; C~
~ '`
rl od' ~Q U~ ~ `
~ ~d~ OD ~ ~ ~ ~ ~ ~ ' ~: .
3 ~ ~Z ~
O ~ $ r~
:` ~ u~ SS ~
o~
~1 rd ~ ~ ~ c~
~1 '`
` 27, 322-F
.` :, .. ` ...... . . . . . . . . . ~ . ` , q~
It will become apparent from the above detailed description of the invention, as well as the Examples above set forth, that many variations and modifications may be made in the particular embodiments of the inven-tion set forth herein without departing from the invention.For example, the present invention is applicable to the removal of sodium sulfate and sodium hydroxide from admixture with sodium chloride regardless of the source of that particular admixture, and is not restricted to such admixtures occurring in a chloralkali plant.
References herein to "overflow" and "underflow" define relative positioning of these means of removing fluids and/or slurries from the wash column, and should not be interpreted to mean that "overflow" necessarily refers to removal over the top of the column or that "underflow"
means removal at the bottom of the column. Other variations and modifications of the present invention will become apparent to those skilled in the art, and the present invention is to be limited only as set forth in the following claims.
27,322-F
:
Claims (12)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A process for selectively removing sodium hydroxide and sodium sulfate from admixture with sodium chloride, which comprises making an aqueous slurry of such mixture, contacting the slurry in a countercurrent flow relationship with wash water at a temperature of 45° to 120°F, and removing the wash water from the slurry and with it a major portion of the sodium hydroxide and sodium sulfate contained in the slurry.
2. The process as defined in Claim 1 wherein the wash water is introduced at a temperature of from 45° to 80°F.
3. The process as defined in Claim 1 wherein the wash water is introduced at a temperature of from 45° to 60°F.
4. A process for separating sodium hydroxide and sodium sulfate from a slurry containing the same in admixture with sodium chloride in particulate form, which comprises feeding said slurry into an upper portion of a wash column such that the slurry moves downwardly through the wash column, introducing a stream of wash water, at a temperature in the range of 45° to 120°F, into the lower portion of the wash column such that the wash water moves upwardly through the column in counter-current flow relationship to the said slurry, removing overflow fluid from the wash column at or near the top of the wash column, said over-flow fluid carrying with it most of the sodium hydroxide and sodium sul-fate from said slurry, and recovering sodium chloride in the underflow from the lower portion of the wash column.
5. The process as defined in Claim 4, wherein the slurry contains from 20 to 45% by weight of sodium chloride, from 2 to 7% by weight of sodium sulfate, and from 4 to 16% by weight of sodium hydroxide, the settled volume of the slurry being within the range of from 15 to 30%
by weight.
by weight.
6. A process as defined in Claim 4 wherein the wash water is sparged into the wash column at a temperature of from 45° to 80°F.
7. The process as defined in Claim 4 wherein the overflow is removed from the wash column at a rate at least equal to the rate at which the slurry is fed into the wash column.
8. The process as defined in Claim 4 wherein the overflow fluid contains at least about 95% by weight of sodium hydroxide and at least about 90% by weight of sodium sulfate, of the slurry fed into the wash column and wherein the underflow contains less than 1% by weight of sodium hydroxide and less than 1% by weight of sodium sulfate.
9. A process for removing sodium hydroxide and sodium sulfate from a slurry containing 20 to 45% by weight sodium chloride, 2 to 7% by weight sodium sulfate and 4 to 16% by weight of sodium hydroxide, the settled volume of the slurry being within the range of 15 to 30%, which comprises feeding said slurry into the upper portion of a wash column in such a manner that the slurry moves downwardly through the wash column, sparging a stream of wash water at a temperature in the range of from 45° to 80°F. into the lower portion of the wash column in such a manner that the wash water moves upwardly through the column in countercurrent relationship to said slurry, removing overflow fluid at or near the top of the wash column, said overflow fluid carrying with it a major portion of the sodium hydroxide and sodium sulfate contained in said slurry, and recovering the purified sodium chloride in the underflow from the lower portion of the wash column.
10. A process as defined in Claim 9 wherein the overflow is removed from the wash column at a rate at least equal to the rate at which the slurry is fed into the wash column.
11. In an electrolytic process for making chlorine and sodium hydroxide wherein cell effluent is concentrated to a mixture containing sodium hydroxide, sodium sulfate and composed principally of sodium chloride, the improved process for separating sodium hydroxide and sodium sulfate from said mixture which comprises making an aqueous slurry of such a mixture wherein the sodium chloride is present in particulate form, contacting such slurry in a countercurrent rela-tionship with wash water at a temperature in the range of 45° to 120°F, removing the wash water from the slurry and with it a major portion of the sodium hydroxide and sodium sulfate contained in the slurry, and re-covering sodium chloride from the mixture.
12. A process as defined in Claim 11 wherein the wash water is at a temperature of from 45° to 80°F.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA324,172A CA1114132A (en) | 1979-03-26 | 1979-03-26 | Process for selective removal of sodium sulfate from an aqueous slurry |
| US06/057,916 US4246241A (en) | 1979-03-26 | 1979-07-16 | Process for selective removal of sodium sulfate from an aqueous slurry |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA324,172A CA1114132A (en) | 1979-03-26 | 1979-03-26 | Process for selective removal of sodium sulfate from an aqueous slurry |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1114132A true CA1114132A (en) | 1981-12-15 |
Family
ID=4113825
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA324,172A Expired CA1114132A (en) | 1979-03-26 | 1979-03-26 | Process for selective removal of sodium sulfate from an aqueous slurry |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US4246241A (en) |
| CA (1) | CA1114132A (en) |
Families Citing this family (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57191226A (en) * | 1981-05-21 | 1982-11-25 | Dow Chemical Canada | Selective removal of sodium sulfate from aqueous slurry |
| US4645512A (en) * | 1985-05-06 | 1987-02-24 | The Dow Chemical Company | Continuous process for removing water-soluble particles from organic liquids |
| US5023803A (en) * | 1989-04-10 | 1991-06-11 | Olin Corporation | Process to control the addition of carbonate to electrolytic cell brine systems |
| DE69124497T2 (en) * | 1990-12-28 | 1997-07-10 | Akzo Nobel Nv | Process for the production of sodium chloride |
| US6652603B2 (en) | 2001-06-29 | 2003-11-25 | Inco Limited | Process for removing sodium sulfate from nickel hydroxide effluent streams |
| US20060289003A1 (en) * | 2004-08-20 | 2006-12-28 | Lackner Klaus S | Laminar scrubber apparatus for capturing carbon dioxide from air and methods of use |
| US20060051274A1 (en) * | 2004-08-23 | 2006-03-09 | Wright Allen B | Removal of carbon dioxide from air |
| WO2007018558A2 (en) * | 2005-07-20 | 2007-02-15 | The Trustees Of Columbia University In The City Of New York | Electrochemical recovery of carbon dioxide from alkaline solvents |
| JP2009502483A (en) * | 2005-07-28 | 2009-01-29 | グローバル リサーチ テクノロジーズ，エルエルシー | Carbon dioxide removal from the air |
| US9266051B2 (en) | 2005-07-28 | 2016-02-23 | Carbon Sink, Inc. | Removal of carbon dioxide from air |
| EP2668992A3 (en) | 2006-03-08 | 2014-04-02 | Kilimanjaro Energy, Inc. | Air collector with functionalized ion exchange membrane for capturing ambient CO2 |
| MX2009003500A (en) * | 2006-10-02 | 2009-04-16 | Global Res Technologies Llc | Method and apparatus for extracting carbon dioxide from air. |
| EP2139584A4 (en) | 2007-04-17 | 2011-05-18 | Global Res Technologies Llc | Capture of carbon dioxide (co2) from air |
| CA2703617A1 (en) | 2007-11-05 | 2009-05-14 | Global Research Technologies, Llc | Removal of carbon dioxide from air |
| EP2212008A1 (en) | 2007-11-20 | 2010-08-04 | Global Research Technologies, LLC | Air collector with functionalized ion exchange membrane for capturing ambient co2 |
| CA2715874C (en) | 2008-02-19 | 2019-06-25 | Global Research Technologies, Llc | Extraction and sequestration of carbon dioxide |
| WO2009149292A1 (en) * | 2008-06-04 | 2009-12-10 | Global Research Technologies, Llc | Laminar flow air collector with solid sorbent materials for capturing ambient co2 |
| WO2010019608A1 (en) * | 2008-08-11 | 2010-02-18 | Global Research Technologies, Llc | Method and apparatus for removing ammonia from a gas stream |
| US9085477B2 (en) | 2010-06-23 | 2015-07-21 | Veolia Water Solutions & Technologies Support | Process for reducing the sulfate concentration in a wastewater stream |
| WO2019161114A1 (en) | 2018-02-16 | 2019-08-22 | Carbon Sink, Inc. | Fluidized bed extractors for capture of co2 from ambient air |
Family Cites Families (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3168379A (en) * | 1957-12-27 | 1965-02-02 | Morton Salt Co | Apparatus and method of producing brine |
| US3130016A (en) * | 1961-05-09 | 1964-04-21 | Pennsalt Chemicals Corp | Process for brine manufacture |
| US3236609A (en) * | 1963-04-11 | 1966-02-22 | Int Salt Co | Production of high purity sodium chloride brine by multistage leaching |
| US3363995A (en) * | 1964-02-10 | 1968-01-16 | Morton Int Inc | Brine production process |
| US3395098A (en) * | 1964-11-19 | 1968-07-30 | Texaco Inc | Recovery of fresh water from brine |
| US3385674A (en) * | 1965-10-07 | 1968-05-28 | Diamond Crystal Salt Co | Lateral flow rock salt dissolver and method |
| US3800026A (en) * | 1971-04-06 | 1974-03-26 | Stauffer Chemical Co | Method for preparing sodium chloride brine |
| US4029744A (en) * | 1973-07-25 | 1977-06-14 | Exxon Research And Engineering Company | Process for removing the salt of a weak acid and a weak base from solution |
| US3983032A (en) * | 1975-01-30 | 1976-09-28 | Texaco Inc. | Brine desalination process with phase-breaking by cold hydrocarbon injection |
| US4151261A (en) * | 1975-06-17 | 1979-04-24 | Allied Chemical Corporation | Method of preparing sodium liquors low in calcium |
| US4119508A (en) * | 1975-12-10 | 1978-10-10 | Osaka Soda Co. Ltd. | Method of purifying the raw brine used in alkali salt electrolysis |
| DE2609673C3 (en) * | 1976-03-09 | 1979-01-11 | Braunschweigische Maschinenbauanstalt, 3300 Braunschweig | Extraction tower for countercurrent leaching of sugar beet pulp |
| JPS53113299A (en) * | 1977-03-15 | 1978-10-03 | Asahi Glass Co Ltd | Method of concentrating caustic alkaline sulution for ion exchange membrane electrolysis |
| US4094956A (en) * | 1977-08-12 | 1978-06-13 | The Dow Chemical Company | Method of reducing the sodium sulfate content of halite |
-
1979
- 1979-03-26 CA CA324,172A patent/CA1114132A/en not_active Expired
- 1979-07-16 US US06/057,916 patent/US4246241A/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| US4246241A (en) | 1981-01-20 |
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