METHOD FOR PREPARING POTASSIUM CHLORIDE FROM CARNALLITE
20230192502 · 2023-06-22
Assignee
Inventors
Cpc classification
Y02A40/20
GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
C01D3/08
CHEMISTRY; METALLURGY
International classification
Abstract
A method for preparing potassium chloride from carnallite includes: carrying out high-temperature water solution mining treatment on carnallite with fresh water to obtain potassium-rich saturated brine; mixing the potassium-rich saturated brine, a sylvine saturated solution, and bittern for mixing brine, evaporation and decomposition to obtain artificial sylvine; and carrying out low-temperature selective dissolution treatment on the artificial sylvine with fresh water to prepare potassium chloride. The carnallite is mined by using hot water, which reduces the content of sodium chloride in the potassium-rich saturated brine; artificial sylvine is only subjected to low-temperature selective dissolution once, which avoids unnecessary energy consumption and impurity accumulation unnecessary for multifold cycles of thermal dissolution-cold crystallization treatment of sylvine while guaranteeing the high yield and high quality of potassium chloride. The method is suitable for different grades of carnallite, has extremely strong adaptability and loose technical conditions, and is conducive to promotion and implementation.
Claims
1. A method for preparing potassium chloride from a carnallite, comprising: (1) contacting a preheated fresh water with the carnallite for a high-temperature water solution mining treatment to obtain a potassium-rich saturated brine, wherein a temperature of the potassium-rich saturated brine is 40° C.-50° C.; wherein the potassium-rich saturated brine comprises the following components in percentage by weight: 7 wt %-11 wt % of NaCl, 7.5 wt %-9.5 wt % of KCl, and 11 wt %-15.5 wt % of MgCl.sub.2; a mass ratio of a fresh water to the carnallite is 0.25:1-1.20:1; in a process of the high-temperature water solution mining treatment, the mass ratio of the fresh water to the carnallite is reduced by 0.15-0.20 when a content of sodium chloride in the carnallite is increased by 10 wt %; (2) mixing the potassium-rich saturated brine, a sylvine saturated solution, and a bittern at 40° C.-50° C. for mixing brine to obtain a carnallite saturated brine and sodium chloride; wherein the carnallite saturated brine comprises the following components in percentage by weight: 1.6 wt %-1.8 wt % of NaCl, 4.0 wt %-4.5 wt % of KCl, and 26.5 wt %-27.0 wt % of MgCl.sub.2; (3) evaporating the carnallite saturated brine at 40° C.-50° C., and then carrying out a solid-liquid separation to obtain a low-sodium carnallite and the bittern; wherein the low-sodium carnallite comprises the following components in percentage by weight: 9 wt %-10 wt % of NaCl, 20 wt %-22 wt % of KCl, and 32 wt %-35 wt % of MgCl.sub.2; (4) carrying out a fresh water decomposition treatment on the low-sodium carnallite at 10° C.-25° C., and then carrying out the solid-liquid separation to obtain an artificial sylvine and a carnallite saturated solution, wherein the artificial sylvine comprises the following components in percentage by weight: 25 wt %-30 wt % of NaCl and 70 wt %-75 wt % of KCl; and (5) carrying out a low-temperature selective dissolution treatment on the artificial sylvine with the fresh water at 10° C.-25° C. to obtain a crude potassium chloride and a statured sylvine solution, and then refining to obtain a potassium chloride; wherein a mass ratio of the fresh water to the artificial sylvine is 0.7:1-1:1.
2. (canceled)
3. (canceled)
4. The method for preparing the potassium chloride from the carnallite according to claim 1, wherein a ratio of a total mass of the potassium-rich saturated brine and the sylvine saturated solution to a mass of the bittern is 1:1.1-1:1.7.
5. The method for preparing the potassium chloride from the carnallite according to claim 1, wherein the bittern in step (3) comprises the following components in percentage by weight: 0.4 wt %-0.5 wt % of NaCl, 0.20 wt %-0.25 wt % of KCl, and 36 wt %-37 wt % of MgCl.sub.2.
6. The method for preparing the potassium chloride from the carnallite according to claim 1, wherein the carnallite saturated solution in step (4) comprises the following components in percentage by weight: 1.5 wt %-2.0 wt % of NaCl, 2.5 wt %-3.5 wt % of KCl, and 25 wt %-27 wt % of MgCl.sub.2.
7. The method for preparing the potassium chloride from the carnallite according to claim 1, further comprising: recovering the carnallite saturated solution obtained in step (4) for preparing the low-sodium carnallite by an evaporation in step (3).
8. The method for preparing the potassium chloride from the carnallite according to claim 1, wherein a content of the potassium chloride in the crude potassium chloride in step (5) is 85 wt %-90 wt %.
9. The method for preparing the potassium chloride from the carnallite according to claim 1, wherein the refining treatment in step (5) comprises: washing and drying the crude potassium chloride.
10. The method for preparing the potassium chloride from the carnallite according to claim 9, wherein a washing solution used by the washing is selected from the fresh water; a liquid-to-solid mass ratio of the washing solution to the crude potassium chloride is 0.20:1-0.25:1; a temperature of the washing is 10° C.-25° C.
11. The method for preparing the potassium chloride from the carnallite according to claim 10, further comprising: recovering a refined potassium mother liquor generated by the washing for the low-temperature selective dissolution treatment of the artificial sylvine in step (5).
12. The method for preparing the potassium chloride from the carnallite according to claim 1, further comprising: recovering the bittern obtained in step (3) for mixing brine in step (2).
13. The method for preparing the potassium chloride from the carnallite according to claim 1, wherein an amount of the fresh water in step (4) is 1.1-1.2 times of an amount calculated by a phase diagram.
14. The method for preparing the potassium chloride from the carnallite according to claim 1, wherein the sylvine saturated solution in step (5) comprises the following components in percentage by weight: 18 wt %-20 wt % of NaCl and 7 wt %-11 wt % of KCl.
15. The method for preparing the potassium chloride from the carnallite according to claim 1, further comprising: recovering the sylvine saturated solution obtained in step (5) for mixing brine in step (2).
Description
BRIEF DESCRIPTION OF THE DRAWINGS
[0032] For more clearly illustrating the embodiments of the present application or technical solution in the prior art, drawings required to be used in the embodiments or the prior art will be simply discussed below. Obviously, the drawings described below are only some embodiments in the present application, and other drawings can be obtained according to these drawings by persons of ordinary skill in the art without creative efforts.
[0033]
[0034]
[0035]
[0036]
[0037]
[0038]
DETAILED DESCRIPTION OF THE EMBODIMENTS
[0039] In view of the defects in the prior art, after long-term research and a lot of practice, the inventor of the present application puts forward the technical scheme of the present application, which adopts the high-temperature water-soluble method to mine carnallite, and combines the brine mixing, evaporation and other processes to produce potassium chloride with high efficiency and quality, so as to realize the development and utilization of potassium resources in various kinds of carnallite.
[0040] Next, the technical solution of the present application will be clearly and completely described, obviously, the described embodiments are some embodiments of the present application but not all the embodiments. Based on the embodiments of the present application, other embodiments obtained by persons of ordinary skill in the art without creative efforts all fall within the protective scope of the present application.
[0041] One aspect of the embodiments of the present application provides a method for preparing potassium chloride from carnallite, comprising:
[0042] carrying out high-temperature water solution mining treatment on carnallite with fresh water to obtain potassium-rich saturated brine;
[0043] mixing the potassium-rich saturated brine, a sylvine saturated solution and bittern for mixing brine, evaporation and decomposition to obtain artificial sylvine; and
[0044] carrying out low-temperature selective dissolution treatment on the artificial sylvine with fresh water to prepare potassium chloride.
[0045] In some specific embodiments, the method for preparing potassium chloride from carnallite specifically comprises:
[0046] (1) contacting preheated fresh water with carnallite for high-temperature water solution mining treatment to obtain potassium-rich saturated brine, wherein the temperature of the potassium-rich saturated brine is 40° C.-50° C.; through hot water preheating treatment, the temperature of the obtained potassium-rich saturated brine reaches 40° C.-50° C.;
[0047] (2) mixing the potassium-rich saturated brine, the sylvine saturated solution and the bittern at 40° C.-50° C. for mixing brine to obtain carnallite saturated brine and sodium chloride;
[0048] (3) evaporating the carnallite saturated brine at 40° C.-50° C., and then carrying out solid-liquid separation to obtain low-sodium carnallite and bittern;
[0049] (4) carrying out fresh water decomposition treatment on the low-sodium carnallite at 10° C.-25° C., and then carrying out solid-liquid separation to obtain artificial sylvine and a carnallite saturated solution; and
[0050] (5) carrying out low-temperature selective dissolution treatment on the artificial sylvine with fresh water at 10° C.-25° C. to obtain crude potassium chloride and a sylvine saturated solution, and then refining to obtain potassium chloride.
[0051] In some specific embodiments, the potassium-rich brine in step (1) comprises the following components in percentage by weight: 7 wt %-11 wt % of NaCl, 7.5 wt %-9.5 wt % of KCl, and 11 wt %-15.5 wt % of MgCl.sub.2.
[0052] Further, a mass ratio of the fresh water to the carnallite is 0.25:1-1.20:1.
[0053] Further, the mass ratio of the fresh water to the carnallite decreases with the increase of the content of sodium chloride in carnallite.
[0054] Still further, in the process of water solution mining, the mass ratio of the fresh water to the carnallite is reduced by 0.15-0.20 when the content of sodium chloride in carnallite increases by 10 wt %. In some specific embodiments, the carnallite saturated brine in step (2) comprises the following components in percentage by weight: 1.6 wt %-1.8 wt % of NaCl, 4.0 wt %-4.5 wt % of KCl, and 26.5 wt %-27.0 wt % of MgCl.sub.2.
[0055] Further, a ratio of a total mass of the potassium-rich saturated brine and the sylvine saturated solution to a mass of bittern is 1:1.1-1:1.7.
[0056] Still further, the higher the content of sodium chloride in the potassium-rich saturated brine and the sylvine saturated solution, the more the amount of the bittern.
[0057] In some specific embodiments, the low-sodium carnallite in step (3) comprises the following components in percentage by weight: 9 wt %-10 wt % of NaCl, 20 wt %-22 wt % of KCl, and 32 wt %-35 wt % of MgCl.sub.2.
[0058] Further, the bittern in step (3) comprises the following components in percentage by weight: 0.4 wt %-0.5 wt % of NaCl, 0.20 wt %-0.25 wt % of KCl, and 36 wt %-37 wt % of MgCl.sub.2.
[0059] Further, the method also comprises: recovering the bittern obtained in step (3) for mixing brine in step (2).
[0060] In some specific embodiments, the method also comprises: the artificial sylvine in step (4) comprises the following components in percentage by weight: 25 wt %-30 wt % of NaCl and 70 wt %-75 wt % of KCl.
[0061] Further, the carnallite saturated solution comprises the following components in percentage by weight: 1.5 wt %-2.0 wt % of NaCl, 2.5 wt %-3.5 wt % of KCl, and 25 wt %-27 wt % of MgCl.sub.2.
[0062] In some specific embodiments, the method also comprises: recovering the carnallite saturated solution obtained in step (4) for preparing low-sodium carnallite by evaporation in step (3).
[0063] Further, the amount of the fresh water in step (4) is 1.1-1.2 times of the amount calculated by a phase diagram.
[0064] In some specific embodiments, a mass ratio of the fresh water to the artificial sylvine in step (5) is 0.7:1-1:1.
[0065] Further, the crude potassium chloride contains 85 wt %-90 wt % potassium chloride.
[0066] Further, the sylvine saturated solution comprises the following components in percentage by weight: 18 wt %-20 wt % of NaCl and 7 wt %-11 wt % of KCl.
[0067] Further, the method also comprises: recovering the sylvine saturated solution obtained in step (5) for mixing brine in step (2).
[0068] In some specific embodiments, the refining treatment in step (5) comprises washing and drying the obtained crude potassium chloride.
[0069] Further, a washing solution used by the washing treatment comprises fresh water.
[0070] Further, a liquid-to-solid mass ratio of the washing solution to the crude potassium chloride is 0.20:1-0.25:1.
[0071] Further, the temperature of the washing treatment is 10° C.-25° C.
[0072] Further, the method also comprises: recovering refined potassium mother liquor generated by the washing treatment for low-temperature selective dissolution treatment of artificial sylvine in step (5).
[0073] Where, as one of more specific embodiments of the present application, as shown in
[0074] (1) stage I: carnallite is mined by using a fresh water solution method to obtain potassium-rich saturated brine. In order to improve the mining speed, mining is conducted with hot water, the temperature of the dissolved brine is controlled at 40° C.-50° C.; the mass ratio of fresh water to carnallite is controlled to 0.25:1-1.20:1, the fresh water mass ratio decreases with the increase of the content of sodium chloride in carnallite, and the ratio is reduced to (0.15-0.20 fresh water mass ratio)/(10 wt % NaCl). The potassium-rich saturated brine comprises 7 wt %-11 wt % of NaCl, 7.5 wt %-9.5 wt % of KCl and 11 wt %-15.5 wt % of MgCl.sub.2.
[0075] (2) Stage II: the potassium-rich saturated brine, the sylvine saturated solution and bittern are mixed to precipitate out sodium chloride, and the carnallite saturated brine is remained. The temperature of mixing brine is the same as that of the potassium-rich saturated brine; a mass ratio of (potassium-rich saturated brine+sylvine saturated solution) to bittern is controlled to 1:1.1-1:1.7, and the higher the content of sodium chloride in potassium-rich brine, the larger the amount of bittern; the bittern can be obtained by evaporating the brine in the later stage without separate preparation. The obtained carnallite saturated brine comprises 1.6 wt %-1.8 wt % of NaCl, 4.0 wt %-4.5 wt % of KCl and 26.5 wt %-27.0 wt % of MgCl.sub.2.
[0076] Stage III: the carnallite saturated brine is evaporated to obtain low-sodium carnallite and bittern. The evaporation temperature is controlled to be the same as that of the carnallite saturated brine; when the residual solution comprises 0.4 wt %-0.5 wt % of NaCl, 0.20 wt %-0.25 wt % of KCl and 36 wt %-37 wt % of MgCl.sub.2, evaporation stops. Solid-liquid separation is conducted, the residual solution at this time is bittern, and all of the bittern is recycled to stage II for mixing brine; the precipitated solid phase comprises 9 wt %-10 wt % of NaCl, 20 wt %-22 wt % of KCl and 32 wt %-35 wt % of MgCl.sub.2, which is low-sodium carnallite.
[0077] (4) Stage IV: the low-sodium carnallite is decomposed with fresh water to obtain artificial sylvine and the carnallite saturated solution. The decomposition temperature is controlled at 10° C.-25° C., and the addition amount of fresh water is 1.1-1.2 times of the theoretical fresh water amount (the theoretical fresh water amount is calculated by a phase diagram). After solid-liquid separation, the obtained solid phase is artificial sylvine comprising 25 wt %-30 wt % of NaCl and 70 wt %-75 wt % of KCl; the liquid phase is the carnallite saturated solution comprising 1.5 wt %-2.0 wt % of NaCl, 2.5 wt %-3.5 wt % of KCl and 25 wt %-27 wt % of MgCl.sub.2. The carnallite saturated solution is returned back to stage III for reuse.
[0078] (5) Stage V: the artificial sylvine is selectively dissolved with fresh water and refined potassium mother liquor to obtain crude potassium chloride. The dissolution temperature is controlled to be the same as the decomposition temperature in stage IV; a liquid-solid mass ratio of fresh water (or refined potassium mother liquor) to artificial sylvine is 0.7:1-1.0:1, in which all of sodium chloride and a part of potassium chloride enter the liquid phase, and the solid phase remained after solid-liquid separation is crude potassium chloride with a potassium chloride content of 85 wt %-90 wt %; the liquid phase is a sylvine saturated solution comprising 18 wt %-20 wt % of NaCl and 7 wt %-11 wt % of KCl. The sylvine saturated solution is returned to stage II for reuse.
[0079] (6) The crude potassium chloride is refined to produce a potassium chloride product. The crude potassium chloride is washed with fresh water and dried to finally obtain the potassium chloride product, wherein the liquid-solid mass ratio of fresh water added for washing to crude potassium chloride is 0.20:1-0.25:1, and the washing temperature is the same as the dissolution temperature in stage V. The refined potassium mother liquor obtained by washing is returned back to stage V for reuse.
[0080] In the present application, when actual conditions are allowable, water solution mining, mixing brine and evaporation processes in this technical solution are all conducted at higher temperatures; decomposition of carnallite, selective dissolution of artificial sylvine and refining of potassium chloride are still controlled to be conducted at low temperatures. Similarly, this replacement solution can achieve water solution mining of various carnallites and preparation of potassium chloride products.
[0081] In the present application, (1) by mining with hot water, the mass ratio of fresh water to carnallite is controlled to 0.25:1-1.20:1, the fresh water mass ratio decreases with the increase of the content of sodium chloride in carnallite, the ratio is reduced to (0.15-0.20 fresh water mass ratio)/(10 wt % NaCl), and the content of sodium chloride in potassium-rich saturated brine is reduced to the greatest extent while rapidly mining carnallite; (2) in the process of mixing brine, the mass ratio of (potassium-rich saturated brine+sylvine saturated solution) to bittern is controlled to 1:1.1-1:1.7, which not only rapidly obtains the low-sodium carnallite saturated brine and omits the halite and sylvine sections in the process of evaporation but also realizes the full utilization of bittern in the later stage, thereby avoiding the environment hazard caused by discharge of bittern; (3) the artificial sylvine is subjected to low-temperature selective dissolution only once to prepare potassium chloride, so that the yield of potassium chloride in this stage is up to 70%-80% without using cyclic thermal dissolution-cold crystallization treatment again.
[0082] Next, the technical solution of the present application will be further illustrated in detail in combination with several preferred embodiments and drawings. This example will be conducted in the premise of the technical solution of the present application and gives detailed implementation modes and specific operation processes, however, the protective scope of the present application is not limited to the following examples.
[0083] Experimental materials used in the following examples, unless specially stated, are all purchased by conventional biochemical reagent companies.
[0084] The following examples (examples 1-3) are all obtained by the following steps:
[0085] (1) carnallite was mined with a fresh water solution method to obtain potassium-rich saturated brine.
[0086] (2) The potassium-rich saturated brine, a sylvine saturated solution and bittern were mixed to precipitate out sodium chloride and remain carnallite saturated brine. The brine mixing temperature was the same as that of the potassium-rich saturated brine; the mass ratio of (potassium-rich saturated brine+sylvine saturated solution) to bittern was controlled, and the higher the content of sodium chloride in potassium-rich brine, the larger the amount of bittern; the bittern was obtained by evaporating the brine in the later stage without separate preparation.
[0087] (3) The carnallite saturated brine was evaporated to obtain low-sodium carnallite and bittern. The evaporation temperature was controlled to be the same as that of the carnallite saturated brine; solid-liquid separation was conducted, and the remained solution at this moment was bittern all of which was reused to step (2) for mixing brine.
[0088] (4) The low-sodium carnallite was decomposed with fresh water to obtain artificial sylvine and a carnallite saturated solution. The carnallite saturated solution was returned back to step (3) for reuse.
[0089] (5) The artificial sylvine was selectively dissolved with fresh water and refined potassium mother liquor to obtain crude potassium chloride. The sylvine saturated solution was returned back to step (2) for reuse.
[0090] (6) The crude potassium chloride was refined to produce a potassium chloride product. The crude potassium chloride was washed with fresh water and dried to finally obtain the potassium chloride product. The washing temperature was the same as the dissolution temperature in step (5). The refined potassium mother liquor obtained by washing was returned back to step (5) for reuse.
Example 1
[0091]
TABLE-US-00001 Mass composition/% Stage Name NaCl KCl MgCl.sub.2 H.sub.2O Water solution Carnallite 48 10.5 19.5 22 mining Liquid-solid mass ratio of water solution 0.25:1 mining fresh water to carnallite Temperature of potassium-rich saturated 50° C. brine Composition of potassium-rich saturated 7 8.4 15.5 69.1 brine Mixing brine Mass ratio of potassium-rich saturated 1:1.1 brine to bittern Brine mixing temperature 50° C. Carnallite saturated brine 1.8 4.5 27 66.7 Evaporation of Evaporation temperature 50° C. carnallite saturated Bittern 0.5 0.25 37 62.25 brine Low-sodium carnallite 10 22 35 33 Decomposition of Decomposition temperature 25° C. low-sodium Addition amount of fresh water 1.2 times of theoretical fresh carnallite water amount Artificial sylvine 30 70 0 0 Carnallite saturated solution 2 3.5 27 67.5 Selective Dissolution temperature 25° C. dissolution of Mass ratio of fresh water to artificial 0.7:1 artificial sylvine sylvine Crude potassium chloride 10 90 0 0 Sylvine saturated solution 20 11 0 69 Refining of crude Washing temperature 25° C. potassium chloride Mass ratio of fresh water to crude 0.2:1 potassium chloride Potassium chloride product 2 96 0 2 Total yield of potassium chloride 90%
Example 2
[0092]
TABLE-US-00002 Mass composition/% Stage Name NaCl KCl MgCl.sub.2 H.sub.2O Water solution Carnallite 19.5 16.5 30 34 mining Liquid-solid mass ratio of water solution 1.2:1 mining fresh water to carnallite Temperature of potassium-rich saturated 40° C. brine Composition of potassium-rich saturated 10 7.5 13.5 69 brine Mixing brine Mass ratio of potassium-rich saturated 1:1.3 brine to bittern Brine mixing temperature 40° C. Carnallite saturated brine 1.6 4 26.5 67.9 Evaporation of Evaporation temperature 40° C. carnallite saturated Bittern 0.4 0.2 36 63.4 brine Low-sodium carnallite 9 20 32 39 Decomposition of Decomposition temperature 10° C. low-sodium Addition amount of fresh water 1.1 times of theoretical fresh carnallite water amount Artificial sylvine 25 75 0 0 Carnallite saturated solution 1.5 2.5 25 71 Selective Dissolution temperature 10° C. dissolution of Mass ratio of fresh water to artificial .sup. 1:1 artificial sylvine sylvine Crude potassium chloride 15 85 0 0 Sylvine saturated solution 18 7 0 75 Refining of crude Washing temperature 10° C. potassium chloride Mass ratio of fresh water to crude 0.25:1 potassium chloride Potassium chloride product 4 92 0 4 Total yield of potassium chloride 92%
Example 3
[0093]
TABLE-US-00003 Mass composition/% Stage Name NaCl KCl MgCl.sub.2 H.sub.2O Water solution Carnallite 31.5 19.5 23 26 mining Liquid-solid mass ratio of water solution .sup. 1:1 mining fresh water to carnallite Temperature of potassium-rich saturated 45° C. brine Composition of potassium-rich saturated 9.5 9.5 11 70 brine Mixing brine Mass ratio of potassium-rich saturated 1:1.7 brine to bittern Brine mixing temperature 45° C. Carnallite saturated brine 1.7 4.2 26.8 67.3 Evaporation of Evaporation temperature 45° C. carnallite saturated Bittern 0.45 0.23 36.5 62.82 brine Low-sodium carnallite 9.5 21 34 35.5 Decomposition of Decomposition temperature 15° C. low-sodium Addition amount of fresh water 1.15 times of theoretical fresh carnallite water amount Artificial sylvine 27 73 0 0 Carnallite saturated solution 1.7 3 26 69.3 Selective Dissolution temperature 15° C. dissolution of Mass ratio of fresh water to artificial 0.9:1 artificial sylvine sylvine Crude potassium chloride 12 88 0 0 Sylvine saturated solution 19 8.5 0 72.5 Refining of crude Washing temperature 15° C. potassium chloride Mass ratio of fresh water to crude 0.23:1 potassium chloride Potassium chloride product 3 94 0 3 Total yield of potassium chloride 95%
[0094] In addition, the inventors of this case also conduct tests with other raw materials, technological operations and technological conditions mentioned in this specification with reference to the foregoing examples, and relatively ideal results are obtained.
[0095] Various aspects, embodiments, features and examples of the present application should be deemed as be illustrative in all aspects, and are not intended to limit the present application, and the scope of the present application is defined by claims. Those skilled in the art will understand other samples, amendments and uses without departing from the spirit and scope of the present application.
[0096] The use of the title and sections in the present application is not meant to limit the present application; each section can be applied to any aspects, embodiments or features of the present application.
[0097] Throughout the present application, where a composition is described as having, comprising or including particular components, or where a process is described as having, comprising or including particular process steps, it is contemplated that the processes taught herein also essentially consist of or consist of the described process steps.
[0098] It should be understood that the order of steps or order in which particular actions are performed is not extremely important, so long as the teachings of the present application remain operable. Furthermore, two or more two steps or actions can be simultaneously performed.
[0099] Although the present application has been described with reference to illustrative embodiments, those skilled in the art will understand that various other changes, omissions and/or additions can be made without departing from the spirit and scope of the present application, and substantive equivalents can be used to replace elements in embodiments. In addition, many amendments can be made without departing from the scope of the present application so that specific situations or materials are suitable for the teachings of the present application. Therefore, it is intended herein to include all the embodiments within the scope of the appended claims of the present application but not limit the present application to implement the particular embodiments disclosed by the present application. Furthermore, unless specifically stated, any use of terms first, second and the like does not denote any order or importance, but rather the terms first, second and the like are used to distinguish one element from another element.