The present disclosure generally relates to manufacturing cementitious building products, and more specifically to systems and methods for treating process water used in manufacturing processes.
Manufacturing cementitious building articles, such as fiber cement products, typically requires the use of water as a process aid. During manufacturing, ions such as sulfate, calcium, sodium, and potassium can leach from the cement materials and build up in the process water. High concentrations of such ions in the process water can negatively affect the quality of the cementitious building products as well as the operation of machinery such as sheet machines and other associated manufacturing processes. Process water with high ion concentrations is typically recycled or discharged.
Discharge of spent process water with high ion concentrations can be limited by requirements of discharge permits or other regulations preventing process water from being freely discharged. In some cases, process water effluent may be required to conform to a maximum concentration of certain ion constituents, such as sulfates, before it can be discharged. Existing methods of reducing sulfate concentration in process water include ion exchange and precipitation with barium chloride solution, both of which can be undesirably expensive for reduction of sulfate concentration to acceptable levels. Accordingly, more efficient and/or affordable methods of ion removal from process water are desirable.
The systems, methods, and devices described herein address one or more problems as described above and associated with current process water treatment systems. The systems, methods and devices described herein have innovative aspects, no single one of which is indispensable or solely responsible for their desirable attributes. Without limiting the scope of the claims, the summary below describes some of the advantageous features.
In one embodiment, a method of treating process water from a cementitious article forming process is described. The method includes receiving the process water from the cementitious article forming process, the process water comprising at least sulfate ions and calcium ions in solution, reacting sodium aluminate with the sulfate ions and the calcium ions to form a solid precipitate primarily comprising ettringite, the solid precipitate suspended within the process water in slurry form; clarifying the slurry to produce a clarified process water and a sludge that includes the solid precipitate; and filtering the sludge to produce a liquid filtrate and a solid waste.
In some embodiments, the method further includes adjusting the pH of the liquid filtrate and the clarified process water, and releasing the liquid filtrate and the clarified process water as effluent.
In some embodiments, the process water has an initial concentration of sulfate ions, and the liquid filtrate and the clarified process water each have a concentration of sulfate ions lower than 50% of the initial concentration of sulfate ions.
In some embodiments, the solid precipitate includes ettringite and calcium sulfate.
In some embodiments, the method further includes adding a flocculant to the process water before clarifying the process water and suspended precipitate.
In some embodiments, the method further includes, prior to the reacting, removing a permeate portion of the process water by reverse osmosis to produce a concentrate portion of the process water, wherein the reacting comprises combining the sodium aluminate with the concentrate portion of the process water.
In some embodiments, the quantity of process water and the quantity of sodium aluminate solution arc mixed for a reaction period of less than 20 minutes before the clarifying step.
In some embodiments, the sodium aluminate is not a limiting reagent of the reaction between the sodium aluminate, the sulfate ions, and the calcium ions.
In some embodiments, the sodium aluminate solution contains between 35% and 50% sodium aluminate.
In some embodiments, the volume of sodium aluminate solution is equal to between 0.1% and 0.3% of the volume of the process water.
In another embodiment, a system for treating process water from a cementitious article forming process is described. The system includes a reaction tank in fluid communication with a process water flow path associated with the cementitious forming process, the reaction tank including an agitator; a reagent tank containing a sodium aluminate solution, the reagent tank in fluid communication with the reaction tank; metering equipment including at least one of a valve and a pump, the metering equipment configured to cause a predetermined volume of the sodium aluminate solution to flow from the reagent tank into the reaction tank; a clarifier in fluid communication with the reaction tank; and a filter in fluid communication with the clarifier. The process water flow path is configured to send, to the reaction tank, spent process water including sulfate ions and calcium ions produced by the cementitious article forming process. The sodium aluminate solution reacts with the sulfate ions and calcium ions to form a solid precipitate including ettringite. The clarifier and the filter are configured to at least partially separate the solid precipitate from the process water to produce a volume of treated process water and a quantity of solid waste.
In some embodiments, the predetermined volume of the sodium aluminate solution is determined based at least in part on a concentration of sulfate or calcium ions in the spent process water.
In some embodiments, the predetermined volume of the sodium aluminate solution is between 0.1% and 0.3% of a volume of spent process water in the reaction tank.
In some embodiments, the sodium aluminate solution comprises between 35% and 50% sodium aluminate.
In some embodiments, the clarifier includes a slant plate clarifier configured to output a clarified liquid and a sludge.
In some embodiments, the filter is configured to receive the sludge and output a solid waste and a liquid filtrate.
In some embodiments, the system further includes at least one additional reaction tank in fluid communication with the process water flow path, the reagent tank, and the clarifier, wherein the metering equipment is configured to independently control a first flow of sodium aluminate into the reaction tank and a second flow of sodium aluminate into the at least one additional reaction tank.
In another embodiment, a cementitious shaped article manufacturing system is described. The system includes a forming unit configured to form a cementitious shaped article, such as a fiber cement board, wherein the forming unit discharges spent process water containing at least sulfate ions and calcium ions; a wastewater treatment unit configured to treat at least a portion of the spent process water by mixing the spent process water with sodium aluminate to form a solid precipitate, and removing the solid precipitate from the spent process water to produce a treated process water having a concentration of sulfate ions relatively lower than an initial concentration of sulfate ions in the spent process water; and a discharge unit configured to adjust the pH of the treated process water.
In some embodiments, the wastewater treatment unit includes a clarifier and a filter for removing the solid precipitate from the spent process water.
In some embodiments, the treated process water is substantially free of the solid precipitate.
Certain embodiments of the present disclosure will now be described, by way of example only, with reference to the accompanying drawings. From figure to figure, the same or similar reference numerals are used to designate similar components of an illustrated embodiment.
Although the present disclosure is described with reference to specific examples, it will be appreciated by those skilled in the art that the present disclosure may be embodied in many other forms. The embodiments discussed herein are merely illustrative and do not limit the scope of the present disclosure.
In the description which follows, like parts may be marked throughout the specification and drawings with the same reference numerals. The drawing figures are not necessarily to scale and certain features may be shown exaggerated in scale or in somewhat generalized or schematic form in the interest of clarity and conciseness.
The present disclosure describes water treatment processes for removing ions leached from cement in process water and/or wastewater generated in connection with the manufacture of cementitious building articles, such as fiber cement or the like.
As shown in
When the recycle stream 120a of the process water 120 is retained, the remaining portion forms the waste stream 120b to be discharged as effluent. The quantities and/or concentrations of various residues, impurities, ions, and the like contained within effluent may be subject to discharge permit or contract restrictions, or other regulation. Thus, the waste stream 120b is sent to the treatment unit 130 for removal of at least a portion of the constituent materials in the waste stream 120b. Components and processes of the treatment unit 130, such as those for removal of sulfate and/or calcium ions, will be discussed in greater detail with reference to
Generally described, the novel treatment processes described herein include combining the waste stream 120b of process water 120, which contains sulfate (SO42−) and calcium (Ca2+) ions, with a solution containing sodium aluminate (NaAlO2) to produce a solid precipitate comprising at least a substantial portion of the sulfate and calcium ions. The resultant precipitate is composed primarily of ettringite, and may further include a smaller quantity of calcium sulfate (gypsum). The primary chemical reaction between the sulfate ions, calcium ions, and sodium aluminate in water to produce ettringite is generally characterized by:
2/3NaAlO2+SO4−2+2Ca+2=1/3(Ca6Al2(SO4)3(OH)12.26H2O), (1)
as 2/3 mole of sodium aluminate react with 1 mole of sulfate ions and 2 moles of calcium ions to produce 1/3 mole of ettringite. In addition, a smaller quantity of calcium sulfate (CaSO4) may be formed by the reaction of calcium (Ca2+) ions with sulfate (SO42−) ions in solution.
The novel sodium aluminate wastewater treatment processes described herein may provide various advantages over existing water treatment processes for removal of sulfate and/or calcium ions. For example, the sodium aluminate treatment described herein may be relatively less expensive than existing methods, such as ion exchange or treatment with barium chloride. In addition, the reaction between sodium aluminate, sulfate and calcium ions is relatively rapid, especially under moderate agitation, such that each batch of wastewater may be treated quickly (e.g., less than 15-20 minutes of reaction time).
The processed wastewater and precipitated solids produced by the present processes may have further advantageous qualities. In one example, the low calcium concentration in the treated wastewater produced by the processes described herein may significantly improve the functionality of other downstream treatment processes, for example, reverse osmosis or other treatment processes, that may be used to further treat the wastewater before release as effluent. In another example, the precipitated ettringite and/or gypsum solids may have a relatively large particle size, allowing them to be separated during sludge dewatering by traditional filtration methods that may not be effective with existing treatment processes. The addition of a flocculant, coagulating, dewatering, or settling agent such as, for example, a polyacrylamide, may further increase the particle size and improve filtration efficiency.
As will be described in greater detail, the chemical reactions between sodium aluminate and wastewater containing ion contaminants can be carried out in one or more treatment tanks. The resulting suspension of liquid and precipitate can be clarified, such as by a settling tank, slant plate clarifier, or other clarifying apparatus, to produce a clarified process water and a sludge. The sludge can further be dewatered to yield a solid waste that can be disposed of conveniently, such as in a landfill or other waste disposal site. The clarified process water can be further treated, such as by pH adjustment or other final treatment processes, and released as effluent, for example, to a municipal wastewater system or the like.
Turning now to
The one or more process water tanks 205a, 205b are in fluid communication with a process water flow path of a manufacturing apparatus and configured to receive wastewater streams 202a, 202b comprising waste or excess process water from the manufacturing apparatus. For example, the one or more process water tanks 205a, 205b may be configured to receive the waste stream 120b from the forming unit 105 depicted in
Wastewater that has been collected in process water tanks 205a, 205b is transferred to the common wastewater transfer tank 215 by process water tank pumps 210a, 210b. Process water tank pumps 210a, 210b can be centrifugal pumps or any other suitable pump for moving wastewater in a pipe. The flow of wastewater between process water tanks 205a, 205b and the wastewater transfer tank 215 is further controllable by the position of valves 212a, 212b. Valves 212a, 212b can be opened, closed, partially opened, and/or partially closed as desired to provide an appropriate flow rate from each process water tank 205a, 205b to the wastewater transfer tank 215. Valves 212a, 212b can be operable automatically, manually, and/or remotely. Wastewater in the wastewater transfer tank can then be transferred to the wastewater feed tank 225 by the transfer tank pump 220. The transfer tank pump 220 can be a centrifugal pump or any other suitable pump for moving wastewater in a pipe.
In some embodiments, the configuration of process water tanks 205a, 205b, wastewater transfer tank 215, and wastewater feed tank 225 may be advantageous by providing added temporary storage capacity. As will be described with reference to
Turning to
The flow of wastewater 302 from the wastewater feed tank 305 to the agitated tanks 310a, 310b, 310c, 310d can be induced and precisely metered by a feed tank pump 307 and wastewater valves 308a, 308b, 308c, 308d. Similarly, the flow of sodium aluminate solution to the agitated tanks 310a, 310b, 310c, 310d can be induced and precisely metered by a sodium aluminate supply pump 317 and sodium aluminate valves 318a, 318b, 318c, 318d. Once the desired quantities of wastewater 302 and sodium aluminate solution are combined in one of the agitated tanks 310a, 310b, 310c, 310d, the mixture can be agitated for an appropriate reaction period, such as 5 minutes, 10 minutes, 15 minutes, or longer, to achieve thorough mixing and/or a more complete reaction of the wastewater 302 and the sodium aluminate solution.
The volumetric ratio of sodium aluminate solution to wastewater can be determined based on stoichiometric principles so as to provide sufficient sodium aluminate to achieve the precipitation reaction and/or to avoid wasting excess sodium aluminate solution that will not be consumed. In some embodiments, the concentration of sulfate and calcium ions in the wastewater can be determined from a sample of the wastewater taken prior to treatment. Once the quantity of sulfate and calcium within the wastewater are known, the quantity of sodium aluminate can preferably be determined such that calcium and/or sulfate is a limiting reagent of the reaction. For example, a quantity of spent process wastewater may include approximately 1600 ppm of sulfate and approximately 900 ppm of calcium. As shown in equation 1 above, the reaction of sulfate and calcium to form each ettringite molecule consumes 2 sodium aluminate molecules, 3 sulfate ions, and 6 calcium ions. Thus, calcium can be a limiting reagent, and the quantity of sodium aluminate solution to be added to the wastewater can be selected such that sufficient sodium aluminate is present to consume all of the ionic calcium present in the wastewater.
In some embodiments, the sodium aluminate is provided in a solution containing between 30% and 60% sodium aluminate. In some embodiments, the solution contains between 35% and 40%, such as 38%, sodium aluminate. In some embodiments, the solution contains between 40% and 50%, such as 45%, sodium aluminate. In one embodiment, a 38% solution of sodium aluminate with sodium hydroxide as a buffering agent is used as a reagent to react with the calcium and sulfate ions in the process water. In some embodiments, the quantity of sodium aluminate solution is between 0.5 and 5 gallons for each 1000 gallons of wastewater, for example, between 1 gallon and 5 gallons, between 1 gallon and 2 gallons, or other suitable quantity. In one example implementation, the volumetric ratio is approximately 1.62 gallons of 38% sodium aluminate solution per 1000 gallons of wastewater. Thus, the volume of the sodium aluminate solution can be in the range of 0.05% to 0.5% of the volume of wastewater to which the sodium aluminate solution is added. In various embodiments, the volumetric ratio of sodium aluminate to wastewater can be adjusted for each treatment batch based on a detected concentration of calcium and/or sulfate ions in the wastewater.
Preferably, because the agitated reaction is a batch process, each tank 310a, 310b, 310c, 310d is closed during the reaction period. For example, the feed tank pump 307 can be activated with valve 308a open and valves 308b, 308c, and 308d closed, such that the wastewater 302 flows only into tank 310a. When the desired reaction volume of wastewater 302 has been pumped into tank 310a, valve 308a is closed and valve 308b is opened such that the wastewater 302 can begin filling tank 310b, or the feed tank pump 307 can be deactivated. During or after the filling of tank 310a, the sodium aluminate supply pump 317 is activated with valve 318a open and valves 318b, 318c, and 318d closed, such that calcium aluminate solution flows into tank 310a. When the desired volume of sodium aluminate solution has been pumped into tank 310a, valve 318a is closed and the sodium aluminate supply pump 317 is deactivated. After a first tank 310a has been filled with the appropriate quantities of wastewater 302 and sodium aluminate solution, the treatment system 300 can proceed to fill a second tank 310b, 310c, or 310d.
During the reaction period, the sodium aluminate in the tank 310a reacts with the sulfate and calcium ions in the wastewater 302 according to chemical equation (1) above, producing a solid precipitate of ettringite suspended in the wastewater 302. In addition, a portion of the calcium and sulfate ions in the wastewater 302 may interact during the reaction to form a relatively small quantity of calcium sulfate (e.g., 10% or less of the total volume of solid precipitate). Thus, the result of the mixing and agitation in tank 310a is a colloidal suspension of solid precipitate suspended in wastewater 302, which may be in the form of a dilute slurry of ettringite, gypsum, and process water. A further result of the reaction period is that the liquid portion of the precipitate-laden wastewater 302 has a lower concentration of sulfate and calcium ions relative to the wastewater 302 that was pumped into the tank 310a.
At the end of the reaction period, each tank 310a, 310b, 310c, 310d can be emptied independently by activation of a tank outlet pump 312a, 312b, 312c, 312d. Tank outlet pumps 312a, 312b, 312c, and 312d can be centrifugal pumps or other suitable liquid pumps capable of transferring a suspension or slurry. Each tank outlet pump 312a, 312b, 312c, 312d is in fluid communication with its respective tank 310a, 310b, 310c, 310d and the clarifier 320 so as to pump the contents of the tank 310a, 310b, 310c, 310d to the clarifier 320.
The clarifier 320 can comprise one or more of a settling tank, rectangular clarifier, tube settler, slant plate clarifier, or the like. At the clarifier, solid precipitate matter produced in one of tanks 310a, 310b, 310c, 310d is removed from the wastewater 302 by settling or other suitable clarifying process. After clarifying, the clarifier 320 outputs clarified wastewater 325, which can be substantially free of precipitate, and sludge 335 comprising the solid precipitate and a portion of the liquid wastewater 302. A clarified wastewater pump 327 transfers the clarified wastewater 325 from the clarifier 320 to the treated wastewater storage 330. A sludge pump 337 transfers the sludge 335 from the clarifier 320 to the sludge dewatering unit 340.
The sludge dewatering unit 340, described in greater detail below with reference to
In some embodiments, a flocculant, clarifying, coagulating, dewatering, or settling agent such as, for example, a polyacrylamide, can further be added in the wastewater treatment system 300 to facilitate the clarification process. In some embodiments, the flocculant can be added to the mixture of wastewater 302 and sodium aluminate in a tank 310a, 310b, 310c, 310d, at any time during the reaction period. In other embodiments, the flocculant can be added after the reaction period, for example, by being metered into the fluid flow path between a tank 310a, 310b, 310c, 310d and the clarifier 320. Preferably, the flocculant is incorporated into the treated wastewater 302 before the wastewater 302 and precipitate reach the clarifier 320.
Turning now to
As described above with reference to
The sludge 420 is transferred for dewatering by a sludge pump 422. The sludge pump 422 can be a centrifugal pump or the like. The sludge pump 422 transfers the sludge 420 to the filter 425. The filter 425 can be any filter suitable for retaining solid precipitate particles, such as a rotary filter, a drum filter, a vacuum drum filter, a bag filter, an inertial separator, or the like. The filter 425 allows a filtrate 440 portion of the sludge 420 to pass, while removing from the sludge 420 a solid waste 430 containing relatively little or none of the liquid treated wastewater 402. The solid waste 430 is removed from the filter 425 and transported by a conveyor 432 or other transport apparatus to a solid waste receptacle 435, such as a dumpster or other waste container, for disposal. The filtrate 440 is transferred to the filtrate tank 445, where it is stored and/or sent by a filtrate pump 447 to the treated wastewater storage 415.
At the treated wastewater storage 415, the filtrate 440 is combined with the clarified wastewater 410 output from the clarifier 405. After having the solid waste 430 removed, the filtrate 440 portion of the sludge 420 may have a substantially similar or identical composition to the clarified wastewater 410. The filtrate 440 and clarified wastewater 410 as combined in the treated wastewater storage 415 typically have a significantly reduced concentration of sulfate and calcium ions relative to the original output of the cementitious article forming units described herein. The sulfate and calcium ions removed from the treated wastewater stream 402 are generally contained within the solid waste 430, which may be disposed of safely (e.g., in a landfill, etc.) without releasing its components into a water system such as a municipal wastewater system, ground water, or the like.
Preferably, the sulfate and calcium ion concentration of the treated wastewater in the treated Wastewater storage 415 are low enough to comply with any regulations and/or other limits on effluent sulfate and/or calcium concentration, such that the contents of the treated wastewater storage 415 can be discharged as effluent without requiring further treatment for removal of calcium or sulfate. The treated wastewater in the treated wastewater storage 415 is transferred to discharge equipment 450 for final treatment and/or release. In some implementations, further treatment may be required to treat aspects of the wastewater other than calcium and sulfate ion concentration. For example, the discharge equipment 450 can include known treatment systems such as ion exchange for removal of other ionic constituents, a final filtration or clarifying stage, reverse osmosis, or the like. In another example, the discharge equipment 450 can include a carbonation tank or other pH adjustment apparatus configured to raise or lower the pH of the treated wastewater into an acceptable pH range for discharge as effluent.
With reference to
As shown in
The reverse osmosis input stream 502 comprises the solution produced by the treatment processes depicted in
At the reverse osmosis system 505, the reverse osmosis input stream 502 is treated by known reverse osmosis methods using a semi-permeable membrane. A portion of the reverse osmosis input stream 502 passes through the semi-permeable membrane, emerging from the reverse osmosis system 505 as the reverse osmosis permeate 507 containing a lower concentration of sulfate, calcium, sodium, and potassium ions relative to the reverse osmosis input stream 502. The remaining portion of the reverse osmosis input stream 502 does not pass through the semi-permeable membrane, and is released as the reverse osmosis concentrate 509 containing a higher concentration of sulfate, calcium, sodium, and potassium ions relative to the reverse osmosis input stream 502. Generally, the volume of the reverse osmosis permeate 507 is larger than or similar to the volume of the reverse osmosis concentrate 509 (e.g., 50% permeate and 50% concentrate, 60% permeate and 40% concentrate, 70% permeate and 30% concentrate, 80% permeate and 20% concentrate, 90% permeate and 10% concentrate, etc.). Thus, the reverse osmosis concentrate 509 may have significantly higher concentrations of sulfate, calcium, sodium, and/or potassium ions.
The reverse osmosis concentrate 509 may be treated by similar processes to those described with reference to
The reverse osmosis concentrate 509 can be pretreated, for example, in the concentrate pretreatment tank 510. In some embodiments, the pretreatment can be accomplished without a tank by adding components to the reverse osmosis concentrate 509 traveling in a pipe or other conduit. In some embodiments, the concentrate pretreatment tank 510 can be an agitated tank to facilitate mixing of the reverse osmosis concentrate 509 with added components.
The example concentrate treatment process begins with pH adjustment. Calcium hydroxide (e.g., lime) from the calcium hydroxide supply 515 is added to the reverse osmosis concentrate 509 in the concentrate pretreatment tank 510. Additional calcium may further be added to the reverse osmosis concentrate 509 from the calcium supply 520. Quantities of calcium hydroxide and calcium can be determined, for example, based on a desired pH range. In one example, calcium hydroxide and calcium are added to control the pH of the reverse osmosis concentrate 509 within a range such as between 11.5 and 12.5 or other suitable range for ettringite formation.
After the pH is adjusted in the concentrate pretreatment tank 510, calcium chloride is added to the concentrate pretreatment tank 510 from the calcium chloride supply 525. Calcium chloride may be desirable as an additional component in order to provide sufficient calcium for the formation of ettringite. As shown in equation (1) above, a relatively large quantity of calcium is required for the formation of ettringite. Moreover, because the reverse osmosis input stream 502 has already been treated by ettringite formation, the reverse osmosis concentrate 509 may have relatively high concentrations of sulfate, sodium, and potassium, and a relatively lower concentration of calcium. Accordingly, the addition of calcium hydroxide, calcium, and calcium chloride may advantageously provide sufficient calcium for further ettringite formation from the reverse osmosis concentrate.
After the calcium hydroxide, calcium, and calcium chloride are added to the reverse osmosis concentrate 509 in the concentrate pretreatment tank 510, the pretreatment process terminates, producing a pretreated concentrate 512 suitable for treatment with sodium aluminate. Sodium aluminate can then be reacted with the sulfate and calcium ions in the pretreated concentrate 512 to produce a precipitate primarily comprising ettringite, as well as other components such as calcium sulfate or the like. In some embodiments, the sodium aluminate reaction may be achieved within the discharge equipment 450 (
As described above, the reverse osmosis and concentrate pretreatment process of
A series of tests were carried out to determine the effectiveness of ion removal using various doses of sodium aluminate with spent process water. Wastewater containing approximately 1611 ppm of sulfate ions and approximately 897 ppm of calcium ions was combined with a 38% sodium aluminate solution. Three dosages of sodium aluminate solution were tested. The three tested dosages were 75%, 100%, and 125% of a proposed dosage of 1.62 gallons of sodium aluminate solution per 1000 gallons of wastewater. Thus, the three tested dosages correspond to 1.215, 1.62, and 2.025 gallons of sodium aluminate solution per 1000 gallons of wastewater, respectively. Each test dosage of 38% sodium aluminate solution was combined with sample of the wastewater, and the sulfate and calcium ion concentrations were sampled at 5 minute intervals for 25 minutes, and sampled again after total reaction times of 35 minutes and 45 minutes.
A series of tests were carried out to evaluate the effect of a flocculant on the settling time of the precipitate produced by the reaction of sodium aluminate with sulfate and calcium ions in wastewater. A polyacrylamide flocculant was combined with two samples of sodium aluminate treated wastewater in concentrations of 0.66 ppm and 3.9 ppm. A third sample of the sodium aluminate treated wastewater was allowed to settle as a control sample without the addition of flocculant. The flocculation testing was carried out in three graduated settling cones. The volume within each cone occupied by the settling solids was measured repeatedly between 0 and 30 minutes of settling time.
Particle size testing was carried out to evaluate the size of solid precipitate particles produced by the wastewater treatment processes described herein. After the sample wastewater was treated with sodium aluminate, the resulting precipitate was analyzed using a conventional laser particle size analyzer.
The particles produced in the example process generally exhibited a normal distribution of particle sizes, ranging between approximately 5 microns and 200 microns. The normal distribution was centered on a mean particle size of approximately 49 microns. Conveniently, particles of an average size of 49 microns may readily be removed from process water by traditional means of solid-liquid separation, such as centrifugal separation, filtration means including bag filtration or rotary filtration, or the like.
Sulfate ion removal testing was additionally performed on a sample of pretreated reverse osmosis concentrate using various doses of sodium aluminate. Pretreated reverse osmosis concentrate having a measured concentration of sulfate ions was treated with four dosages of 38% sodium aluminate solution. The four tested dosages were 100%, 125%, 150%, and 175% of a proposed dosage of 1.62 gallons of sodium aluminate solution per 1000 gallons of pretreated reverse osmosis concentrate. The calcium dosage in pretreatment was 125% of the theoretical value.
In addition, the precipitated solids from the trials described above were analyzed by x-ray diffraction to determine constituent materials.
Certain features that are described in this disclosure in the context of separate implementations can also be implemented in combination in a single implementation. Conversely, various features that are described in the context of a single implementation can also be implemented in multiple implementations separately or in any suitable subcombination. Moreover, although features may be described above as acting in certain combinations, one or more features from a claimed combination can, in some cases, be excised from the combination, and the combination may be claimed as any subcombination or variation of any subcombination.
Moreover, while methods may be depicted in the drawings or described in the specification in a particular order, such methods need not be performed in the particular order shown or in sequential order, and that all methods need not be performed, to achieve desirable results. Other methods that are not depicted or described can be incorporated in the example methods and processes. For example, one or more additional methods can be performed before, after, simultaneously, or between any of the described methods. Further, the methods may be rearranged or reordered in other implementations. Also, the separation of various system components in the implementations described above should not be understood as requiring such separation in all implementations, and it should be understood that the described components and systems can generally be integrated together in a single product or packaged into multiple products. Additionally, other implementations are within the scope of this disclosure.
Conditional language, such as “can,” “could,” “might,” or “may,” unless specifically stated otherwise, or otherwise understood within the context as used, is generally intended to convey that certain embodiments include or do not include, certain features, elements, and/or steps. Thus, such conditional language is not generally intended to imply that features, elements, and/or steps are in any way required for one or more embodiments.
Conjunctive language such as the phrase “at least one of X, Y, and Z,” unless specifically stated otherwise, is otherwise understood with the context as used in general to convey that an item, term, etc. may be either X, Y, or Z. Thus, such conjunctive language is not generally intended to imply that certain embodiments require the presence of at least one of X, at least one of Y, and at least one of Z.
Although making and using various embodiments are discussed in detail below, it should be appreciated that the description provides many inventive concepts that may be embodied in a wide variety of contexts. The specific aspects and embodiments discussed herein are merely illustrative of ways to make and use the systems and methods disclosed herein and do not limit the scope of the disclosure. The systems and methods described herein may be used for treatment of process water from cementitious and/or fiber cement building articles and are described herein with reference to this application. However, it will be appreciated that the disclosure is not limited to this particular field of use.
Some embodiments have been described in connection with the accompanying drawings. The figures are drawn to scale, but such scale should not be limiting, since dimensions and proportions other than what are shown are contemplated and are within the scope of the disclosed inventions. Distances, angles, etc. are merely illustrative and do not necessarily bear an exact relationship to actual dimensions and layout of the devices illustrated. Components can be added, removed, and/or rearranged. Further, the disclosure herein of any particular feature, aspect, method, property, characteristic, quality, attribute, element, or the like in connection with various embodiments can be used in all other embodiments set forth herein. Additionally, it will be recognized that any methods described herein may be practiced using any device suitable for performing the recited steps.
While a number of embodiments and variations thereof have been described in detail, other modifications and methods of using the same will be apparent to those of skill in the art. Accordingly, it should be understood that various applications, modifications, materials, and substitutions can be made of equivalents without departing from the unique and inventive disclosure herein or the scope of the claims.
This application claims the benefit of U.S. Provisional Application Ser. No. 62/460,662, filed Feb. 17, 2017, entitled “SYSTEMS AND METHODS FOR TREATING CEMENTITIOUS ARTICLE FORMING PROCESS WATER,” which is hereby incorporated by reference in its entirety and for all purposes.
Number | Date | Country | |
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62460662 | Feb 2017 | US |