SEPARATION OF OXYGENATED COMPOUND USING A METALLIC SALT

Abstract

A process, system, and apparatus are provided for separating an oxygenated compound from a stream. More specifically, a stream comprising the oxygenated compound is fed into a cooling tower along with a caustic outlet stream comprising a metallic salt. Contact between the oxygenated compound and the metallic salt results in the conversion of a portion of the oxygenated compound into a derivative salt. The derivative salt and the unconverted oxygenated compound material are condensed by cooling and substantially removed from the cooling tower as an oxygenated compound outlet stream. The gaseous components of the stream, less a substantial portion of the oxygenated compound, are removed from the cooling tower as a cooling outlet stream.

Description

Field of Invention The present description refers in general to the separation of oxygenated compounds from lower alkanes using caustic waste. Background of the Invention Olefins such as ethylene, propylene, and butylene can be building blocks for a variety of commercially valuable polymers. Since natural sources of olefins may not exist in commercial quantities, polymer producers can rely on methods to convert the more abundant lower alkanes into olefins. Typically, a polymer producer can use steam cracking to produce alkenes from lower alkanes. Steam cracking is a highly endothermic process in which lower alkanes diluted with steam are subjected very briefly to a high temperature of at least 700°C, requiring a large energy input. In addition, steam cracking can lead to coke formation in the reactor, which can result in higher maintenance costs and lower profitability. Oxidative dehydrogenation (OD) is an alternative to steam cracking that can be exothermic, can have a low energy demand, and can produce little or no coke. Ref. 316256 In hydrocarbon dehydration (HD), a lower alkane is mixed with oxygen in the presence of a catalyst and optionally an inert diluent at low temperatures, such as 300°C, to produce the corresponding alkene. In some examples, other byproducts such as carbon monoxide, carbon dioxide, and an oxygenated compound may also be produced in the HD process. These byproducts may undergo further processing before becoming a marketable product or may be discarded. Further processing to separate byproducts from the marketable product can increase the complexity of a chemical complex and the associated energy demands. Further downstream processing of the DHO process includes the removal of oxygenated compounds, such as acetic acid, using a cooling tower, followed by the removal of carbon oxides, particularly carbon dioxide, using an amine tower or caustic scrubbing, or both. Oxygenated compounds removed from the cooling tower result in dilute solutions of the oxygenated compound that may require further processing before they can be marketed. The use of a caustic scrubbing to remove carbon oxides produces spent caustics or metallic salts such as sodium carbonate or sodium hydrogen sulfide, which must be removed by deep well injection, humid air oxidation, or incineration.This description refers to the use of metallic salts to simplify the separation and concentration of oxygenated compounds present in and removed from a gas stream. Summary of the Invention In one aspect, a method is provided for separating an oxygenated compound from a stream. More specifically, the stream comprising the oxygenated compound is fed into a cooling tower along with a caustic outlet stream comprising a metallic salt. The streams are cooled by the addition of water, and contact between the oxygenated compound and the metallic salt during cooling facilitates the conversion of the oxygenated compound into a derived salt. An outlet stream of oxygenated compound comprising a substantial portion of the derived salt and at least a substantial portion of unconverted oxygenated compound is removed from the cooling tower. A cooling outlet stream, comprising gaseous components present in the stream, is also removed from the cooling tower. In another aspect, an apparatus is provided for separating an oxygenated compound from a stream. More specifically, the apparatus comprises a cooling tower comprising a cooling inlet, a cooling outlet, a metal salt inlet, and an oxygenated compound outlet. The cooling inlet is configured to receive the stream comprising the oxygenated compound. The metal salt inlet is configured to receive a caustic outlet stream comprising a metal salt from the cooling tower, thereby enabling contact between the caustic outlet stream and the oxygenated compound stream.The cooling outlet is suitable for removing a cooled outlet stream and the oxygenated compound outlet is suitable for removing an oxygenated compound outlet stream comprising at least a substantial portion of a derived salt formed by contact of the oxygenated compound with the metal salt and at least a substantial portion of the unconverted oxygenated compound. In another aspect, a system is provided for the separation of an oxygenated compound from a stream. More specifically, the system comprises a cooling tower configured to receive a stream comprising the oxygenated compound and a caustic outlet stream comprising a metallic salt, resulting in contact of the oxygenated compound with the metallic salt and the conversion of a portion of the oxygenated compound into a derivative salt; cooling the incoming stream and the caustic outlet stream; removing at least a substantial portion of a derivative salt and at least a substantial portion of the unconverted oxygenated compound; and removing a cooling outlet stream comprising gaseous components from the stream. In one aspect, a method is provided for converting a lower alkane into an alkene. More specifically, an inlet stream comprising oxygen and the lower alkane is fed into an oxidative dehydrogenation (OD) reactor. At least a portion of the lower alkane is converted to the alkene in the OD reactor, and an OD outlet stream comprising the alkene, an oxygenated compound, and a carbon-based oxide is produced. The OD outlet stream and a caustic outlet stream comprising a metal salt are fed into a cooling tower and cooled. Contact in the cooling tower between the oxygenated compound and the metal salt facilitates the conversion of a portion of the oxygenated compound into a derived salt.A cooling outlet stream comprising at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide is removed from the cooling tower, as is an oxygenated compound outlet stream comprising at least a substantial portion of the unconverted oxygenate and at least a substantial portion of the derived salt. The cooling outlet stream is fed into a caustic scrubbing tower and contacted with a caustic agent to form a metallic salt that is removed from the caustic tower and can be recycled and used as part of the caustic outlet stream fed into the cooling tower with the DHO outlet stream. In another aspect, an apparatus for the oxidative dehydrogenation (DHO) of a lower alkane to an alkene is provided. More specifically, the apparatus comprises a DHO reactor, a cooling tower, a caustic scrubbing tower, and a return line. The DHO reactor comprises a DHO inlet and a DHO outlet. The DHO inlet is suitable for conveying a DHO inlet stream comprising the lower alkane to the DHO reactor. The DHO outlet is suitable for conveying a DHO outlet stream comprising the alkene, an oxygenated compound, and a carbon-based oxide. The cooling tower comprises a cooling inlet, a cooling outlet, a metal salt inlet, and an oxygenated compound outlet. The cooling inlet is in fluid communication with the DHO outlet to receive the DHO outlet stream.The cooling outlet is suitable for conveying a cooling outlet stream comprising at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide. The oxygenated compound outlet is suitable for conveying an oxygenated compound outlet stream comprising at least a substantial portion of the oxygenated compound and a derived salt. The caustic scrubbing tower comprises a scrubbing inlet, a scrubbing outlet, a caustic agent inlet, and a caustic agent outlet. The scrubbing inlet is in fluid communication with the cooling outlet to receive the cooling outlet stream. The caustic agent outlet is suitable for conveying a caustic agent outlet stream comprising a metallic salt.The return line is in fluid communication with the caustic agent outlet to receive the caustic agent outlet stream and carry the caustic agent outlet stream to the metallic salt inlet of the cooling tower. In another aspect, a system for the oxidative dehydrogenation (OD) of a lower alkane is provided. More specifically, the system comprises an OD reactor, a cooling tower, a caustic scrubbing tower, and a return line. The OD reactor is configured to receive an inlet stream comprising oxygen and the lower alkane. The OD reactor is configured to produce an outlet stream comprising an alkene, an oxygenated compound, and a carbon-based oxide.The cooling tower is configured to receive and cool the DHO outlet stream and a caustic outlet stream comprising a metallic salt, to contact the oxygenated compound with the metallic salt to convert a portion of the oxygenated compound into a derivative salt, to remove an oxygenated compound outlet stream comprising at least a substantial portion of the unconverted oxygenated compound and at least a substantial portion of the derivative salt, and to produce a cooling outlet stream comprising at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide. The caustic scrubbing tower is configured to receive the cooling outlet stream and contact a substantial portion of the carbon-based oxide from the cooling outlet stream with a caustic agent to form a caustic outlet stream comprising a metallic salt.The return line is configured to direct the caustic outlet stream to the cooling tower and bring it into contact with the DHO outlet stream to form a salt derived from the metallic salt and the oxygenated compound. The oxygenated compound outlet stream comprises a substantial portion of the derived salt. It is understood that the inventions described herein are not limited to the examples summarized in this summary. Several other aspects are described and exemplified herein. / uu jo io Brief Description of the Figures The features and advantages of the examples, and how to achieve them, will become clearer and the examples better understood with reference to the following description of examples taken together with the accompanying figures, in which: FIGURE 1 is a flow diagram illustrating a non-limiting example of a system for converting an alkane into an alkene; FIGURE 2 is a flow diagram illustrating a non-limiting example of a system for separating an oxygenated compound from a stream that includes a cooling tower with a primary stage and a secondary stage; FIGURE 3 is a flow diagram illustrating a non-limiting example of a system comprising a separation vessel; FIGURE 4 is a flow diagram illustrating a non-limiting example of a system comprising an oxygen eliminator; FIGURE 5 is a flow diagram illustrating a non-limiting example of a system comprising an amine tower; and FIGURE 6 is a flow diagram illustrating a non-limiting example of a system comprising a polymerization reactor. / uuoo io Detailed Description of the Invention The examples set forth in this document illustrate certain examples, in one way, and such examples should not be interpreted as limiting the scope of the examples in any way. Certain exemplary aspects of the present description will now be described to provide a general understanding of the principles of structure, function, manufacture, and use of the systems, apparatus, and methods described herein. One or more examples of these aspects are illustrated in the accompanying figures. Persons skilled in the art will understand that the systems and methods specifically described herein and illustrated in the accompanying figures are non-limiting exemplary aspects and that the scope of the various examples of the present invention is defined solely by the claims. The features illustrated or described in connection with one exemplary aspect may be combined with the features of other aspects. Such modifications and variations are intended to be included within the scope of the present invention. References throughout the description to several examples, some examples, one example, or similar phrases mean that a particular feature, structure, or characteristic described in relation to the example is included in at least one example. Therefore, occurrences of the phrases "in several examples," "in some examples," "in one example," or "in one example," or similar phrases, in places throughout the description do not necessarily refer to the same example. Furthermore, the particular features, structures, or characteristics may be combined in any appropriate way in one or more examples. Thus, the particular features, structures, or characteristics illustrated or described in relation to one example may be combined, in whole or in part, with the feature structures or characteristics of one or more examples without limitation.It is intended that such modifications and variations be included within the scope of the present examples. Apart from operational examples or where otherwise stated, all numbers or expressions referring to quantities of ingredients, reaction conditions, etc., used in the description and claims shall be understood to be modified in all cases by the term "approximately." Accordingly, unless otherwise stated, the numerical parameters stated in the following description and appended claims are approximations that may vary depending on the desired properties that the present description seeks to achieve. At a minimum, and not as an attempt to limit the application of the doctrine of equivalents to the scope of the claims, each numerical parameter shall be interpreted at least in light of the number of significant digits reported and by applying ordinary rounding techniques. Although the numerical ranges and parameters that define the broad scope of the description are approximations, the numerical values ​​stated in the specific examples are reported as accurately as possible. However, any numerical value inherently contains certain errors that necessarily result from the standard deviation found in its respective test measurements. Furthermore, it should be understood that any numerical interval listed herein is intended to include all subintervals contained within it. For example, an interval from 1 to 10 is intended to include all subintervals between and including the stated minimum value of 1 and the stated maximum value of 10; that is, having a minimum value equal to or greater than 1 and a maximum value equal to or less than 10. Because the numerical intervals described are continuous, they include all values ​​between the minimum and maximum values. Unless expressly stated otherwise, the various numerical intervals specified in this application are approximations. The grammatical articles *a*, *una*, and *el*, as used in this document, are intended to include at least one or one or more, unless otherwise indicated, even if *at least one* or *one or more* is expressly used in certain cases. Therefore, the above grammatical articles are used herein to refer to one or more of one (i.e., at least one) of the particular identified items. Furthermore, the use of a singular noun includes the plural, and the use of a plural noun includes the singular, unless the context of use requires otherwise. As used in this document, the term substantial portion means at least 50 percent by weight. A substantial portion may be from 50% to 100% by weight, such as, for example, at least 60% by weight, at least 70% by weight, at least 80% by weight, at least 90% by weight, or at least 95% by weight. As used in this document, the term alkane refers to an acyclic saturated hydrocarbon. In several examples, an alkane consists of hydrogen and carbon atoms arranged in a linear structure in which all carbon-carbon bonds are single bonds. An alkane has the general chemical formula CnH2n+2, and in several examples, for a lower alkane, 'n' is in the range of 2 to 4. In several examples, an alkane refers to one or more of the following: ethane, propane, butane, pentane, hexane, octane, decane, and dodecane. In several examples, a lower alkane refers to one or more of the following: ethane, propane, and butane. As used in this document, the term alkene refers to an unsaturated hydrocarbon containing at least one carbon-carbon double bond. In several examples, alkene refers to alpha-definites. For example, alkene may refer to one or more of ethylene, propylene, 1-butene, butadiene, pentene, pentadiene, hexene, octene, decene, and dodecene. As used in this document, the terms alpha olefin or α-olefin refer to a family of organic compounds that are alkenes (also known as olefins) with the chemical formula CxH2x, distinguished by having a double bond in the primary or alpha (α) position. In several examples, alpha olefin refers to one or more of ethylene, propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, 1-decene, and 1-dodecene. As used in this document, the term fixed-bed reactor refers to one or more reactors, in series or in parallel, that often include a cylindrical tube filled with catalyst granules, with reactants flowing through the bed and being converted into products. The catalyst in the reactor may have multiple configurations, including, for example, one large bed, several horizontal beds, several tubes packed in parallel, multiple beds in their own casings, and / or combinations thereof. As used in this document, the term fluidized bed reactor refers to one or more reactors, in series or in parallel, that often include a fluid (e.g., gas or liquid) that can pass through a solid granular catalyst, which may be shaped like tiny spheres, at a speed high enough to suspend the solid granular catalyst and cause the solid granular catalyst to behave like a fluid. As used in this document, the term HDPE refers to high-density polyethylene, which typically has a density greater than or equal to 0.941 g / cm³. HDPE has a low degree of branching. HDPE can often be produced using chromium / silica catalysts, Ziegler-Natta catalysts, or metallocene catalysts. As used in this document, the term LDPE refers to low-density polyethylene, which can be a highly branched polyethylene with long chains. The density of LDPE often ranges from 0.910 to 0.940 g / cm³. LDPE can be created by free-radical polymerization. As used in this document, the term LLDPE refers to linear low-density polyethylene, which can be a polyethylene with a significant number of short branches resulting from the copolymerization of ethylene with at least one α-olefin comonomer. In some examples, LLDPE has a density in the range of 0.915 to 0.925 g / cm³. In some examples, the LLDPE may be an ethylene-hexene copolymer, an ethylene-octene copolymer, or an ethylene-butene copolymer. The amount of comonomer incorporated can be from 0.5 mol% to 12 mol% with respect to ethylene, in some examples from 1.5 mol% to 10 mol%, and in other examples from 2 mol% to 8 mol%. As used herein, the term MDPE refers to medium-density polyethylene, which may be a polyethylene with some short and / or long chain branching and a density in the range of 0.926 to 0.940 g / cm3. MDPE can be produced using chromium / silica catalysts, Ziegler-Natta catalysts, or metallocene catalysts. As used in this document, the term VLDPE refers to very low-density polyethylene, which can be a polyethylene with high levels of short-chain branching and a typical density in the range of 0.880–0.915 g / cc. In some examples, VLDPE can be a substantially linear polymer. VLDPE is typically produced by the copolymerization of ethylene with α-olefins. It can also be produced using metallocene catalysts. As used in this document, the term gas-phase polyethylene process refers to a process in which a mixture of ethylene, optional alpha-olefin comonomers, and hydrogen is passed over a catalyst in a fixed-bed or fluidized-bed reactor. The ethylene and optional alpha-olefins polymerize to form polyethylene granules, suspended in the flowing gas, which can exit the reactor. In several examples, two or more of the individual reactors are placed in parallel or in series, each operating under slightly different conditions, so that the properties of the different polyethylenes from the reactors are present in the resulting polyethylene mixture. In some examples, the catalyst system includes, for instance, chromium catalysts, Ziegler-Natta catalysts, zirconium catalysts, and metallocene catalysts, and combinations thereof. As used in this document, the term high-pressure polyethylene process refers to converting ethylene gas into a white solid by heating it to very high pressures in the presence of minute amounts of oxygen (less than 10 ppm oxygen) at 1000 bar - 3000 bar and 80°C - 300°C. In some examples, the high-pressure polyethylene process produces LDPE. As used in this document, the term low-pressure polyethylene process refers to polymerizing ethylene using a catalyst, which in some examples includes aluminum, at generally lower pressures than the high-pressure polyethylene process. In some examples, the low-pressure polyethylene process can be carried out at 10 bar–80 bar and 70°C–300°C. In several examples, the low-pressure polyethylene process yields HDPE. In several examples, an α-olefin comonomer can be included in the low-pressure polyethylene process to yield LLDPE. As used in this document, the term solution polyethylene process refers to processes that polymerize ethylene and one or more optional α-olefins in a lower alkane hydrocarbon mixture in the presence of one or more catalysts. In several examples, two or more of the individual reactors may be placed in parallel or in series, each of which may be under slightly different conditions, so that the properties of different polyethylenes from the reactors are present in the resulting polyethylene mixture. In some examples, the catalysts include, but are not limited to, chromium catalysts, Ziegler-Natta catalysts, zirconocene catalysts, hafnocene catalysts, phosphinimine catalysts, metallocene catalysts, and combinations thereof. As used in this document, the term polyethylene suspension process refers to single-tube loop reactors, double-tube loop reactors, or autoclaves (stirred tank reactors) used to polymerize ethylene and optional α-olefins in the presence of a catalyst system and a diluent. Non-limiting examples of diluents include isobutane, n-hexane, or n-heptane. In some examples, two or more of the individual reactors are placed in parallel or in series, each of which may be under slightly different conditions, so that the properties of different polyethylenes from the reactors are present in the resulting polyethylene blend. In some examples, the catalyst system includes, for instance, chromium catalysts, Ziegler-Natta catalysts, zirconocene catalysts, hafnocene catalysts, phosphinimine catalysts, metallocene catalysts, and combinations thereof. As used in this document, the term long-chain branching refers to a situation in which, during α-olefin polymerization, a vinyl-terminated polymer chain can be incorporated into a growing polymer chain. Long branches often have a length that can be longer than the average critical entanglement distance of a linear polymer chain (e.g., without long-chain branching). In some cases, the effects of long-chain branching disrupt the rheological behavior. As used in this document, the term short-chain branching refers to an ethylene copolymer with an α-olefin or branches of fewer than 40 carbon atoms. In some examples, the α-olefin or branches are present in less than 20% by weight of the polyethylene, and in some examples, less than 15% by weight. In some cases, the presence of short-chain branches can interfere with the formation of the polyethylene crystal structure and may be observed as a lower density compared to a linear polyethylene (without short-chain branching) of the same molecular weight. As used in this document, the term monomer refers to small molecules containing at least one double bond that can react in the presence of a free-radical polymerization initiator to chemically bond to other monomers to form a polymer. As used herein, the term olefinic monomer includes, without limitation, α-olefins and, in some examples, ethylene, propylene, 1-butene, 1-hexene, 1-octene and combinations thereof. As used in this document, the term polyolefin refers to a material, which is prepared by polymerizing a monomer composition containing at least one olefinic monomer. As used in this document, the term polyethylene may include, for example, an ethylene homopolymer, an ethylene copolymer, and an α-olefin. As used in this document, the term polypropylene / uuoo io may include a propylene homopolymer such as, for example, isotactic polypropylene and syndiotactic polypropylene, a propylene copolymer, and an α-olefin. As used in this document, the term polymer refers to macromolecules composed of repeating structural units connected by covalent chemical bonds and may include, for example, a homopolymer, a random copolymer, a block copolymer, and a graft copolymer. As used in this document, the term thermoplastic refers to a class of polymers that can soften or become liquid when heated and harden when cooled. In some examples, a thermoplastic may be a high-molecular-weight polymer that can be repeatedly heated and reshaped. In several examples, a thermoplastic resin may include a polyolefin and an elastomer that has thermoplastic properties. As used in this document, the terms thermoplastic elastomers and TPE refer to a class of copolymers or a mixture of polymers (in some examples a mixture of a thermoplastic and a rubber) that includes materials that have both thermoplastic and elastomeric properties. As used in this document, the terms thermoplastic olefin or TPO refer to polymer / filler blends containing some fraction of polyethylene, polypropylene, polypropylene block copolymers, rubber, and a reinforcing filler. Fillers may include, for example, talc, fiberglass, carbon fiber, wollastonite, metal oxysulfate, and combinations thereof. Rubber may include, for example, ethylene-propylene rubber, EPDM (ethylene-propylene-diene rubber), ethylene-butadiene copolymer, styrene-ethylene-butadiene-styrene block copolymers, styrene-butadiene copolymers, ethylene-vinyl acetate copolymers, ethylene-alkyl (meth)acrylate copolymers, and VLDPE such as those available under the trade name Flexomer® resin from Dow Chemical Co., Midland, MI, styrene-ethylene-ethylene-propylene-styrene (SEEPS).These can also be used as materials that the interpolymer will modify to adapt their rheological properties. Unless otherwise specified, all molecular weight values ​​are determined using gel permeation chromatography (GPC). Molecular weights are expressed as polyethylene equivalents with a relative standard deviation of 2.9% for number-average molecular weight (Mn) and 5.0% for weight-average molecular weight (Mw). Unless otherwise stated, the molecular weight values ​​reported here are weight-average molecular weights (Mw). Unless otherwise specified, all / uu jo io pressure values ​​are gauge pressure values. As used in this document, the term apparatus refers to at least one of a suitable device, machine, structure, or other equipment capable of performing the functions of the method, apparatus, and system as described herein. For example, the term apparatus may refer to a chemical complex, and the terms are interchangeable. Many chemical production processes can produce oxygenated compounds as co-products, such as acetic acid, acrylic acid, maleic acid, and maleic anhydride. A cooling tower is typically used to remove these compounds from a process stream. In the cooling tower, a cooling agent condenses the oxygenated compound in the process stream, leaving unreacted hydrocarbons and carbon- or sulfur-based oxides in the gaseous state. This allows for the separation of the condensed oxygenated compound from the gaseous components. In some cooling processes, the oxygenated compound may be diluted to a low concentration, which may be insufficient for downstream applications. The oxygenated compound may require further purification and / or processing to generate a product sufficient for downstream applications. For example, it may be necessary to remove water from the oxygenated compound to increase its concentration. Separating the oxygenated compound from water can increase the complexity of a cooling tower and / or separation vessel due to the small thermal separation (e.g., boiling point) between the oxygenated compound and water. In some cases, a mixture of oxygenated compound and water may be azeotropic. The separation vessel may employ a large column, a large number of stages, a high reflux ratio, and a high energy demand to separate an azeotropic mixture of oxygenated compound and water. In the petrochemical industry, a process stream can be treated with a caustic agent to remove a contaminant. For example, during the processing of gasoline, kerosene, and liquefied petroleum gas (LPG), sulfides and organic acids are removed by treatment with a caustic agent such as sodium hydroxide. In an ethane cracking process, carbon dioxide can be removed using a caustic agent. The treatment may involve reacting the caustic agent with the contaminant to form a different product that can be removed from the process stream. For example, the reaction of gaseous hydrogen sulfide with a caustic sodium hydroxide solution can produce water and hydrogen sulfide, which can be removed in liquid form with the water.In the case of an ethane cracker, carbon dioxide can be removed from the process stream by converting the carbon dioxide into sodium bicarbonate in the caustic tower. When the caustic agent reacts with the contaminant, the caustic agent is consumed (i.e., spent). Spent caustic agent may be undesirable and may require disposal, which can be costly and increase the complexity of the chemical production process. For example, spent caustic agent may be sold to pulp and paper manufacturers who may require its transport to a different facility. Spent caustic agent can also be disposed of by deep well injection, incineration, and / or neutralization by humid air oxidation. These disposal processes may require additional energy, costs, and complexity in the chemical production process. Converting spent caustic agent into a marketable product capable of removing oxygenated compounds from process streams can reduce energy requirements, costs, and the complexity of chemical production processes. Therefore, a method, system, and apparatus are provided that can improve the purification of oxygenated compounds and reduce energy requirements for purification. More specifically, a stream comprising the oxygenated compound can be introduced into a cooling tower, and the oxygenated compound can be removed from the stream. A caustic outlet stream comprising a metallic salt can be introduced into the cooling tower. The stream can be contacted with the caustic outlet stream to form a salt derived from the metallic salt and the oxygenated compound.A cooling outlet stream can be produced in the cooling tower and an oxygenated compound outlet stream comprising at least a substantial portion of the oxygenated compound and at least a substantial portion of the derived salt can be produced in the cooling tower. Oxidative dehydrogenation (DHO) can couple the endothermic dehydrogenation of an alkane with the strongly exothermic oxidation of hydrogen. For example, the DHO of an alkane might involve contacting an alkane and oxygen in a DHO reactor with a DHO catalyst under reaction conditions (e.g., temperature, pressure, flow rate, etc.) that promote the oxidation of the alkane to the corresponding alkene. The corresponding alkene includes hydrocarbons with the same number of carbon atoms as the alkane used in the DHO reactor, but with the addition of a carbon-carbon double bond. For example, using DHO, ethane can be converted to ethylene, propane can be converted to propylene, and butane can be converted to butylene. Any known DHO catalyst can be suitable for use with the present description. For example, a DHO catalyst containing a mixed metal oxide can be used. Furthermore, the reaction conditions can be controlled to adjust the selectivity and yield of the DHO reactor products. As is known in the art, the conditions will vary and can be optimized for a particular alkane, a specific catalyst, a selected product, and / or a particular inert diluent. A byproduct of a DHO reaction can be an oxygenated compound that may need to be removed from the process stream, and the DHO process can generate spent caustic agent. Therefore, in several examples, a method, a system, and an apparatus for converting a lower alkane into an alkene are provided. An inlet stream comprising oxygen and the lower alkane can be introduced into a DHO reactor. At least a portion of the lower alkane can be converted into the alkene in the DHO reactor, and an outlet DHO stream comprising the alkene, an oxygenated compound, and a carbon-based oxide can be produced. The outlet DHO stream can be introduced into a cooling tower, and the oxygenated compound can be removed from the outlet DHO stream. In the cooling tower, an outlet cooling stream comprising at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide can be produced.Furthermore, an oxygenated compound outlet stream comprising at least a substantial portion of the oxygenated compound can be produced in the cooling tower. This cooling outlet stream can be fed into a caustic scrubbing tower. In the caustic scrubbing tower, the cooling outlet stream can be contacted with a caustic agent to form a caustic outlet stream comprising a metallic salt. This caustic outlet stream can then be fed back into the cooling tower. The oxygenated compound outlet stream can be contacted with the caustic outlet stream to form a salt derived from the metallic salt and the oxygenated compound. This oxygenated compound outlet stream can also comprise a substantial portion of the derived salt. With reference to FIGURE 1, a flow diagram of a non-limiting example of a system 100 for converting an alkane to an alkene is illustrated. As illustrated, a DHO reactor 102 and a cooling tower 104 can be in operational communication. For example, a DHO outlet 102b of the DHO reactor 102 can be in fluid communication with a cooling inlet 104a of the cooling tower 104 through a DHO outlet line 110. In addition, a cooling outlet 104c of the cooling tower 104 can be in fluid communication with a scrubbing inlet 106a of the caustic scrubbing tower 106 through a cooling outlet line 114. Consequently, the DHO reactor 102 can be in fluid communication with the caustic scrubbing tower 106 through the cooling tower 104. The DHO reactor 102 may comprise a DHO inlet 102a that can be configured to receive a DHO inlet stream from a DHO inlet line 108 and may be suitable for conveying the DHO inlet stream to the DHO reactor 102. The DHO inlet stream may comprise a gaseous mixture of a lower alkane and oxygen. In several examples, the DHO inlet stream may further include at least one of a carbon-based oxide, a sulfide, steam, and an inert diluent. In several examples, the DHO inlet stream may comprise another hydrocarbon, such as methane. The inert diluent may comprise, for example, nitrogen. In several examples, the carbon oxide may comprise at least one of carbon dioxide and carbon monoxide.The concentration of oxygen and the lower alkane within the mixture in the DHO inlet stream, as well as the temperature and pressure of the DHO inlet stream, can be adjusted so that the mixture remains within the flammability limits. In several examples, the lower alkane is in a gaseous state. In several examples, the carbon monoxide is in a gaseous state. In several examples, the sulfide is in a gaseous state. In several examples, multiple DHO inlet lines may be configured to introduce the DHO inlet stream to the DHO 102 reactor. For example, each reactant (e.g., lower alkane, oxygen, steam, carbon-based oxide, and inert diluent) may be added directly to the DHO 102 reactor, each in separate inlet lines (not shown). Alternatively, one or more reactants may be premixed and added in more than one inlet line. In several examples, reactants may be premixed before entering the DHO 102 reactor and subsequently introduced into the DHO reactor through a common DHO inlet. In several examples, steam may be added indirectly as water mixed with an additional reactant, and the resulting mixture may be preheated before entering the DHO 102 reactor.When steam is added indirectly as water, the preheating process can raise the temperature of the mixture so that the water can be substantially converted, and in several examples, completely converted to steam before entering the DHO 102 reactor. The DHO 102 reactor may include a catalyst capable of catalyzing the conversion of reactants within the DHO inlet stream into products such as, for example, an alkene and an oxygenated compound, and in several examples, a carbon-based oxide. The catalyst may be, for example, a mixed metal oxide catalyst, many varieties of which have been described in the art. In several examples, the products may additionally include water. As is known in the art, the catalyst composition, the composition of the DHO feed stream, and the reaction conditions within the DHO 102 reactor, such as temperature and pressure, can be adjusted to promote the desired selectivity of a product. For example, the ratio of the lower alkane to oxygen can be outside the upper flammability limit of the mixture. In several examples, the oxygen concentration in the DHO feed stream can range from 0.1% to 30% by weight of the DHO feed stream, and in some examples, it varies from 0.1% to less than 30% by weight, less than 25% by weight, or less than 20% by weight. In several examples, the lower alkane concentration in the DHO feed stream can range from 0.1% to 50% by weight of the DHO feed stream, and in some examples, it varies from 0.1% to less than 50% by weight or less than 40% by weight. In several examples, increasing the steam concentration in the DHO inlet stream can increase the amount of oxygenated compound produced relative to the alkene produced in DHO reactor 102. In several examples, reducing the steam concentration in the DHO inlet stream can decrease the amount of oxygenated compound produced relative to the alkene produced in DHO reactor 102. The steam concentration in the DHO inlet stream can range from 0.1% to 40% by weight of the total DHO inlet stream 108, and in some examples, it varies from 0.1% to less than 40% by weight or less than 25% by weight. In several examples, the steam concentration in the DHO inlet stream can be at least 1% by weight. In several examples, the DHO inlet stream may comprise 20% oxygen by weight, 40% lower alkane by weight, and the remainder is steam, carbon dioxide, and / or an inert diluent. In several examples, the DHO process has a selectivity for the corresponding alkene (e.g., ethylene in the case of ethane DHO) of over 95%, such as, for example, over 98%. The gas space-hour velocity (GHSV) within the DHO reactor 102 can range from 500 to 30,000 tr1, and in some examples, the GHSV within the DHO reactor 102 can exceed 1000 tu1. In several examples, the space-time yield of the corresponding alkene (e.g., productivity) in grams per hour (g) per kilogram (kg) of catalyst can be at least 900, such as, for example, greater than 1500, greater than 3000, or greater than 3500, at a DHO reactor temperature of, for example, 350°C to 400°C. In several examples, the productivity of the catalyst can be increased by increasing the temperature in the DHO 102 reactor until the selectivity of the alkene decreases. The use of a DHO reactor to carry out a DHO reaction according to the description falls within the knowledge of a person experienced in the art. In several examples, the reaction can be carried out at temperatures in the range of 300°C to 450°C, such as 300°C to 425°C, or 330°C to 400°C. In several examples, the reaction can be carried out at pressures in the range of 3.447 to 689.47 kPa (0.5 pounds per square inch (psi) to 100 psi), such as 103.4 to 344.73 kPa (15 psi to 50 psi). In several examples, the lower alkane can have a residence time in the DHO reactor ranging from 0.002 seconds to 30 seconds, or from 1 second to 10 seconds. The products of the DHO reaction can exit the DHO reactor 102 through the outlet of DHO 102b in a DHO outlet stream. The outlet of DHO 102b can be configured to receive the DHO outlet stream and can be suitable for conveying the DHO 110 outlet stream from the DHO reactor 102 into the DHO 110 outlet line. In several examples, in addition to the products, the DHO outlet stream may include unreacted components from the DHO inlet stream such as, for example, lower alkane, carbon-based oxide, oxygen, steam, inert diluent, and combinations thereof. In several examples, the temperature of the DHO outlet stream may be in the range of 100°C to 450°C, for example, 300°C to 425°C, and in certain examples, 330°C to 400°C. Any of the known reactor types applicable to the hydrochemical oxidation (HO) of an alkane may be used with the present description. For example, a fixed-bed reactor, a fluidized-bed reactor, or combinations thereof may be used for the HOD reactor 102. In a typical fixed-bed reactor, the reactants are introduced into the reactor at an inlet and flow through an immobilized catalyst. The products are formed and exit through the reactor outlet. A person skilled in the art will understand what features are required with respect to the reactor's shape and dimensions, reactant inlets, product outlets, temperature and pressure control, and means for immobilizing the catalyst. In a typical fluidized bed reactor, the catalyst bed may be supported by a porous structure or a spreader plate and located near a lower end of the reactor. Reactants flow through the fluidized bed reactor at a velocity sufficient to fluidize the bed (e.g., the catalyst rises and begins to rotate in a fluidized manner). The reactants can be converted into products upon contact with the fluidized catalyst, and the reactants are subsequently removed from an upper end of the reactor. A person skilled in the art would understand the required characteristics regarding the reactor shape and dimensions, the shape and size of the spreader plate, the inlet temperature, the outlet temperature, the reactor temperature and pressure, the reactor inlets, the reactant outlets, and the velocities necessary to achieve fluidization. In several examples, there may be multiple DHO reactors connected in series or in parallel. Each DHO reactor may be identical or different. For example, each DHO reactor may contain the same or different DHO catalysts. In several examples, the multiple DHO reactors may each be a fixed-bed reactor, each a fluidized-bed reactor, or combinations of fixed-bed and fluidized-bed reactors. Regardless of the configuration of the DHO reactor 102, the DHO outlet 102b can be in fluid communication with the cooling inlet 104a of cooling tower 104 via the DHO outlet line 110 to direct the DHO outlet stream to cooling tower 104. The cooling inlet 104a can be configured to receive the DHO outlet stream from the DHO outlet line 110 and can be suitable for conveying the DHO outlet stream to cooling tower 104. In several instances, the cooling inlet 104a can be configured to receive a product stream and can be suitable for conveying the product stream to cooling tower 104. The product stream can comprise at least one of a hydrocarbon, such as an alkane or alkene, and one of an organic alcohol, such as ethanol. Cooling tower 104 may comprise a flash drum, an oxygenated compound scrubber, or similar components or combinations thereof. Cooling tower 104 may be configured to cool the components in the DHO outlet stream and remove at least a substantial portion of the alkene from the DHO outlet stream. In several examples, cooling tower 104 may facilitate the removal of oxygenated compound and water from the DHO outlet stream. Cooling tower 104 may produce a cooling outlet stream comprising at least a substantial portion of the alkene from the DHO outlet stream and, in several examples, at least a substantial portion of the carbon-based oxide from the DHO outlet stream.In several examples, the cooling outlet stream may include additional components of the DHO outlet stream, such as a portion of the oxygen, a portion of the oxygenated compound, a portion of the inert diluent, a portion of the vapor, and a portion of the unreacted alkane. In several examples, the cooling outlet stream is in a gaseous state. The cooling outlet stream exits cooling tower 104 through cooling outlet 104c. Cooling outlet 104c may be configured to receive the cooling outlet stream and may be suitable for conveying the cooling outlet stream from cooling tower 104 to cooling outlet line 114. Cooling tower 104 can produce an oxygenated compound outlet stream comprising at least a substantial portion of the oxygenated compound from the DHO outlet stream and, in some instances, a derived salt as described herein. In several instances, the oxygenated compound outlet stream may comprise additional components from the DHO outlet stream such as, for example, a substantial portion of water (e.g., steam), a lower alkane, an alkene, oxygen, and a carbon-based oxide. The oxygenated compound outlet stream can exit cooling tower 104 through an oxygenated compound outlet 104b of cooling tower 104.The oxygenated compound outlet 104b can be configured to receive the oxygenated compound outlet stream and can be suitable for conveying the oxygenated compound outlet stream out of the cooling tower 104 on the oxygenated compound outlet line 112. In several examples, cooling tower 104 can be in operational communication with a caustic scrubbing tower 106. Cooling outlet 104c can be in seamless communication with the scrubbing inlet 106a of the caustic scrubbing tower 106 via cooling outlet line 114 to direct the cooling outlet stream to the caustic scrubbing tower 106. Scrubbing inlet 106a can be configured to receive the cooling outlet stream from cooling outlet line 114 and can be suitable for conveying the cooling outlet stream to the caustic scrubbing tower 106. The caustic scrubbing tower 106 may comprise a scrubbing inlet 106a, a scrubbing outlet 106c, a caustic inlet 106d, and a caustic outlet 106b. The caustic inlet 106d may be configured to receive a caustic agent stream comprising a caustic agent from a caustic agent line 120 and may be suitable for conveying the caustic agent stream to the caustic scrubbing tower 106. The caustic agent may comprise a hydroxide, such as, for example, at least one of sodium hydroxide, potassium hydroxide, and ammonium hydroxide. In several instances, the caustic agent stream includes water or any other suitable component. The caustic scrubber 106 can be configured to contact the caustic agent stream with the cooling outlet stream. In several examples involving a carbon-based oxide comprising carbon dioxide, the caustic agent can react with carbon dioxide and / or sulfide in the cooling outlet stream to form a metallic salt. The metallic salt can be, for example, at least one of a sulfide and one of a carbonate. The carbonate can comprise at least one of sodium bicarbonate, potassium carbonate, and ammonium bicarbonate. The sulfide can comprise hydrogen sulfide. In several examples, the metallic salt can be water-soluble.The reaction can remove at least a substantial portion of the carbon-based oxide (e.g., carbon dioxide) and, in several examples, the sulfide (e.g., hydrogen sulfide) from the cooling outlet stream and produce a scrubbing outlet stream and a caustic outlet stream. For example, the reaction of sodium hydroxide and carbon dioxide is shown in the reaction scheme 1. Reaction scheme 1 CO2 + NaOH « NaHCO3 The scrubbing outlet stream may include unreacted components from the cooling outlet stream. The 106c scrubbing outlet can be configured to receive the scrubbing outlet stream and may be suitable for conveying the scrubbing outlet stream from the 106 caustic scrubbing tower to the 116 scrubbing outlet line. The caustic outlet stream may comprise a substantial portion of the metal salt and, in some examples, at least some water, caustic agent, and oxygenate. In several examples, the caustic agent outlet 106b may be configured to receive the caustic agent outlet stream and may be suitable for conveying the caustic outlet stream to a return line 118. The return line 118 may be configured to receive the caustic agent outlet stream and discharge the caustic outlet stream to a metal salt inlet 104d of the cooling tower 104. In several examples, the caustic outlet stream may comprise a spent caustic stream. In several examples, the caustic effluent stream can be produced by various suitable processes. For example, the caustic effluent stream can be produced by a cracking process such as ethylene cracking, a refining process such as mercaptan oxidation, a papermaking process, a soapmaking process, a detergentmaking process, a food manufacturing process, any other suitable caustic production process, and combinations thereof. In several examples, a storage vessel can store caustic waste, and the storage vessel can include a storage vessel outlet (not shown) suitable for conveying the caustic agent effluent stream to the metal salt inlet 104d.Therefore, the method, system, and apparatus according to the present description are not limited to DHO processes, and the method, system, and apparatus according to the present description may be used with other suitable processes. In several examples, the caustic waste stream and the DHO outlet stream can be introduced separately and / or simultaneously into cooling tower 104. Cooling tower 104 can be configured to contact the caustic outlet stream with the DHO outlet stream. In several instances, cooling tower 104 can be configured to react the caustic outlet stream with the DHO outlet stream to form a derivative salt and, in several instances, a carbon-based oxide and / or sulfide from the metal salt and the oxygenated compound. In several instances, cooling tower 104 can react the metal salt with the oxygenated compound and, in some instances, with water and a caustic agent to form the derivative salt and the carbon-based oxide and / or sulfide. The derivative salt can comprise an acetate, an acrylate, and a malonate. For example, the acetate can comprise at least one of sodium acetate, potassium acetate, and ammonium acetate. The acrylate can comprise at least one of sodium acrylate, potassium acrylate, and ammonium acrylate.Malonate may comprise at least one of the following: sodium malonate, potassium malonate, and ammonium malonate. In several instances, the resulting salt may be soluble in water. For example, the reaction of sodium bicarbonate and the oxygenated compound to form sodium acetate, carbon dioxide, and water is illustrated in Reaction Scheme 2. Reaction scheme 2 NaHCOa + CH3COOH θ CO2+ H2O + NaC2H3O2 In several examples, the molar ratio of the metal salt in the caustic outlet stream to be oxygenated in the DHO outlet stream may be in the range of 0.8:1 to 1.2:1, such as 1:1. In several examples, the molar ratio of the metal salt in the caustic outlet stream to be oxygenated in the DHO outlet stream may be greater than 1:1, such as 2:1. In several examples, cooling tower 104 can be configured to maintain a pH within a range of 2 to 12, such as 4 to 11, 4 to 7, or 7 to 11. In several examples, cooling tower 104 can be configured to maintain a pH within a range of the pKa of the oxygenated compound to the pKa of the metal salt in order to facilitate the formation of the derived salt. In several examples, the oxygenated compound comprises acetic acid, which has a pKa of 4.7, and sodium bicarbonate, which has a pKa of 10.3. In several examples, the pH is measured in a mixture of water, oxygenated compound, and metal salt. The cooling outlet stream may comprise a substantial portion of the carbon-based oxide from the DHO outlet stream in cooling tower 104. In several instances, the carbon-based oxide from the DHO outlet stream may pass through cooling tower 104 without substantially reacting. The oxygenated compound outlet stream may comprise the oxygenated compound, the derived salt, and water. The addition of the caustic outlet stream to the cooling tower may decrease the amount of oxygenated compound and increase the amount of derived salt in the cooling outlet stream. The decrease in oxygenated compound in the cooling outlet stream may result from the conversion of the oxygenated compound into the derived salt.Converting the oxygenated compound into the derived salt can facilitate the removal of the oxygenated compound from the DHO outlet stream and limit the oxygenated compound from exiting cooling tower 104 in the alkene outlet stream. The cooling tower 104 can be single-stage or multi-stage. For example, with reference to Figure 2, a flow diagram of a non-limiting example of a system 200 comprising a multi-stage cooling tower is illustrated. As illustrated, the DHO outlet line 110 can be in fluid communication with a first inlet of the heat exchanger (HX) 222a of a first HX 222. The first inlet of HX 222a can be configured to receive the DHO outlet stream from the DHO outlet line 110 and can be suitable for conveying the DHO outlet stream to the first HX 222. The first HX 222 can be configured to adjust the temperature of the DHO outlet stream.For example, the first HX 222 can cool the DHO outlet stream to a temperature below 200°C, such as below 100°C, below 50°C, below 40°C, and in some examples, the first HX 222 can cool the DHO outlet stream to a temperature between 20°C and 80°C. In several examples, the first HX 222 can cool the DHO outlet stream to a temperature that induces condensation of the oxygenated compound, such as a temperature below or equal to the boiling point of the oxygenated compound and / or a temperature that reduces the vapor pressure of the oxygenated compound. The first HX 222 can be any HX known in the art. For example, the first HX 222 can be a standalone HX separate from a cooling tower. In several examples, the first HX 222 may be an integrated HX that is part of a cooling tower. The temperature-adjusted DHO output current can exit the first HX 222 through a first HX 222b output as a first HX output current. The first HX 222b output can be configured to receive the first HX output current and can be used to carry the first HX output current from the first HX 222 to the first HX 236 output line. The first outlet of HX 222b can be in fluid communication with a separator inlet 238a of a separator 238 via the first outlet line of HX 236 to direct the first outlet stream of HX to the separator 238. The separator 238 can comprise a vapor-liquid separator such as, for example, a flash drum. The inlet of separator 238a can be configured to receive the first outlet stream of HX from the first outlet line of HX 236 and can be suitable for conveying the first outlet stream of HX to the separator 238. / uu jo io The separator 238 can be configured to condense the oxygenated compound and produce a condensate outlet stream substantially composed of liquid and an alkene outlet stream substantially composed of gas. The condensate outlet stream may comprise oxygenated compound material from the first HX outlet stream. In several examples, the condensate outlet stream may comprise at least 80% oxygenated compound by weight, such as, for example, at least 90% oxygenated compound by weight, at least 95% oxygenated compound by weight, or 80% to 100% oxygenated compound by weight. In several examples, the condensate outlet stream may additionally comprise water from the first HX outlet stream. A condensate outlet 238b of the separator 238 can be configured to receive the condensate outlet stream and may be suitable for conveying the condensate outlet stream out of the separator 238 and into the condensate line 242. An alkene outlet 238c of the separator 238 can be configured to receive the alkene outlet stream and may be suitable for conveying the alkene outlet stream out of the separator 238 to the alkene outlet line 240. In several examples, a second HX 224 can be provided in seamless communication with the separator 238. For example, the alkene outlet line 240 can be in seamless communication with a second HX 224a input of the second HX 224. The second HX 224a input can be configured to receive the alkene outlet stream from the alkene outlet line 240 and can be suitable for conveying the DHO outlet stream to the second HX 224. The second HX 224 can be configured to adjust the temperature of the alkene outlet stream. For example, the second HX 224 can cool the alkene outlet stream to a temperature of less than 170°C, such as less than 100°C, less than 50°C, less than 40°C, and in some examples, the second HX 224 can cool the alkene outlet stream to a temperature of 20°C to 80°C.In several examples, the second HX 224 can cool the DHO outlet stream to a temperature that induces condensation of the oxygenated compound, such as a temperature lower than or equal to the boiling point of the oxygenated compound and / or a temperature that reduces the vapor pressure of the oxygenated compound. The second HX 224 can be any HX known in the art. For example, the second HX 224 can be a standalone HX separate from a cooling tower. In several examples, the second HX 224 can be an integrated HX that is part of a cooling tower. The temperature-adjusted DHO output stream can exit the second HX 224 through a second HX 224b output as a second HX output stream. The second HX 224b output can be configured to receive the second HX output stream and can be used to carry the second HX output stream from the second HX 224 to the second output line of the HX 256. The second output of HX 224b can be in seamless communication with a cooling inlet 204a of a cooling tower 204 via the second output line of HX 256 to direct the second output stream of HX to the cooling tower 204. The cooling inlet 204a can be configured to receive the second output stream of HX from the second output line of HX 256 and can be suitable for conveying the second output stream of HX to the cooling tower 204. A metal salt inlet 204d of cooling tower 204 can be configured to receive the caustic outlet stream from return line 118 and can be suitable for conveying the caustic outlet stream to cooling tower 204. Cooling tower 204 can be configured to contact the caustic outlet stream with the second HX outlet stream. In several instances, cooling tower 204 can be configured to react the caustic outlet stream with the second HX outlet stream to form a derivative salt and, in several instances, a carbon-based oxide and / or sulfide. / uu jo io In several instances, cooling tower 204 can react the metallic salt with the oxygenated compound and, in some instances, with water and a caustic agent, to form the derivative salt and the carbon and / or sulfide-based oxide. The caustic outlet stream can enable more effective removal of the oxygenated compound from the alkene outlet stream. Removing more of the oxygenated compound from the alkene outlet stream can extend the operating life of downstream equipment that may become fouled by the formation of a derivative salt of the oxygenated compound. Cooling tower 204 can be configured to quench components in the second HX outlet stream and remove at least a substantial portion of the alkene from the second HX outlet stream. In several examples, cooling tower 204 can facilitate the removal of oxygenated compound and water from the second HX outlet stream. Cooling tower 204 can produce a cooling outlet stream comprising at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide from the second HX outlet stream. In several examples, the cooling outlet stream can comprise additional components from the second HX outlet stream such as, for example, oxygen, oxygenated compound, inert diluent, water (e.g., steam), and unreacted alkane. The cooling outlet stream exits cooling tower 204 through cooling outlet 204c.Cooling outlet 204c can be configured to receive the cooling outlet stream and may be suitable for conveying the cooling outlet flow from cooling tower 204 to cooling outlet line 114. Cooling tower 204 can produce a derived salt outlet stream comprising at least a substantial portion of the oxygenated compound from the second HX outlet stream and / or at least a substantial portion of the derived salt formed by cooling tower 204. In several instances, the derived salt outlet stream may comprise additional components from the second HX outlet stream, such as, for example, a substantial portion of water, lower alkane, alkene, oxygen, and carbon-based oxide. The derived salt outlet stream exits cooling tower 204 through an oxygenated compound outlet 204b of cooling tower 204. The oxygenated compound outlet 204b can be configured to receive the derived salt outlet stream and can be suitable for conveying the derived salt outlet stream out of cooling tower 204 in the oxygenated compound outlet line 212. In several examples, the oxygenated compound in the oxygenated compound outlet stream, the condensate outlet stream, or the byproduct salt outlet stream may undergo further processing. For example, with reference to FIGURE 3, the oxygenated compound may be separated from the byproduct salt in a separation vessel 326. FIGURE 3 is a flow diagram of a non-limiting example of a system 300 comprising the separation vessel 326. As illustrated, the separation vessel 326 has a separation inlet 326a, a first separation outlet 326b, and a second separation outlet 326c. The separation inlet 326a may be configured to receive the oxygenated compound outlet stream from the oxygenated compound outlet line 112 and may be suitable for conveying the oxygenated compound outlet stream to the separation vessel 326.In several examples, the separation inlet 326a can be configured to receive at least one of the salt outlet stream derived from the oxygenated compound outlet line 212 and the condensate outlet stream from the condensate line 242 and can be suitable for conveying the respective stream or streams to the separation vessel 326. Separation vessel 326 can separate the oxygenated compound from the derived salt, and in several examples, separation vessel 326 can separate the oxygenated compound from water. The presence of the derived salt in separation vessel 326 can enhance the separation of the oxygenated compound from water. For example, the derived salt and the oxygenated compound can dissociate and / or react with water to form a salt derivative ion (e.g., CH3COO) and an acid (e.g., H3O+, Na+). Since the derived salt and the oxygenated compound can form a common ion, an increase in the concentration of one of the salt derivatives and the oxygenated compound can affect the other. For example, the reactions of sodium acetate (C2H3NaO2), acetic acid (CH3COOH), bicarbonate ion (HCO3~), carbon dioxide (CO2) and water (H2O) are illustrated in reaction scheme 3. Reaction scheme 3 CH3COOH + H2O θ CH3COO- + H3O+ h2o + hco3~ « CO32~ + H30+ 2H2O + CO2θ HCO3- + H3O+ C2H3NaO2θ (or CH3COO- + Na+ As illustrated in Reaction Scheme 3, sodium acetate can form an acetate ion that can affect the equilibrium reaction of acetic acid and water. For example, sodium acetate can cause the equilibrium reaction of acetic acid and water to favor the separate species of acetic acid and water over an acetate ion and an acid, compared to the reaction without the presence of acetate. The separation vessel 326 may comprise various pieces of equipment familiar to those experienced in the field. For example, the separation vessel 326 may comprise an extraction tower, a packed column, a screening tray column, a spray column, a KARR column, a rotating disc contactor, a stirred cell extractor, a rectification tower, a separator, and combinations thereof. In some instances, the separation vessel 326 may include a liquid-liquid extractor. Consequently, the addition of a salt to the oxygenated compound inlet stream can increase the efficiency of the separation vessel 326 and facilitate the effective separation of the oxygenated compound from water. The separation vessel 326 can produce a second separation outlet stream comprising a substantial portion of the oxygenated compound from the oxygenated compound outlet stream. In some instances, the second separation outlet stream may comprise additional components of the oxygenated compound outlet stream, such as, for example, water. In some instances, the second separation outlet stream may comprise at least 80% oxygenated compound by weight, such as, for example, at least 90% oxygenated compound by weight, at least 95% oxygenated compound by weight, or from 80% to 100% oxygenated compound by weight. The second separation outlet stream can exit the separation vessel 326 through the second separation outlet 326c of the separation vessel 326.The second separation outlet 326c can be configured to receive the second separation outlet stream and may be suitable for conveying the second separation outlet stream from the separation vessel 326 into the second separation outlet line 328. The separation vessel 326 can produce a first separation outlet stream comprising a substantial portion of the salt derived from the oxygenated compound outlet stream and, in several instances, a substantial portion of the water from the oxygenated compound outlet stream. In several instances, the first separation outlet stream can comprise at least 10% salt derived by weight, such as, for example, at least 30% salt derived by weight, at least 50% salt derived by weight, or 30% to 70% salt derived by weight. In several instances, the first separation outlet stream can comprise at least 5% water by weight, such as, for example, at least 10% water by weight, at least 25% water by weight, or 15% to 50% water by weight. The first separation outlet stream can exit the separation vessel 326 through the first separation outlet 326b of the separation vessel 326.The first separation outlet 326b can be configured to receive the first separation outlet stream and may be suitable for transporting the first separation outlet stream from the separation vessel 326 into the first separation outlet line 330. The separation vessel 326 can be configured with a recycling line 332 in seamless communication with the first separation outlet line 330 and / or the first separation outlet 326b. The recycling line 332 can be configured to recycle a portion of the salt from the first separation outlet stream to the separation vessel 326 via the recycling inlet 326d. The recycling line 332 can be configured to receive a portion of the first separation outlet stream and can be suitable for conveying a recycling stream to a recycling inlet 326d of the separation vessel 326. The recycling inlet 326d can be configured to receive the recycling stream and can be suitable for conveying the recycling stream to the separation vessel 326.For example, the recycling stream may comprise a portion of the salt derived from the first separation outlet stream and, in several examples, a portion of the water from the first separation outlet stream. The recycling line 332 can be configured to recycle the derived salt from the outlet stream of the first separation vessel until a selected concentration of derived salt is achieved in the separation vessel 326. In several examples and with reference to FIGURES 1 and 3, the return line 118 can allow the additional generation of derived salt in the cooling tower 104, which would flow to the separation vessel 326 through the oxygenated compound outlet line 112 to increase the concentration of derived salt in the separation vessel 326. In several examples, a supplementary salt stream can be added to the separation vessel 326. In several examples, the supplementary salt may comprise ethyl acetate. With reference to FIGURE 4, in several examples, an oxygen scavenger 444 can be arranged between the DUO reactor 102 and the cooling tower 104. FIGURE 4 is a flow diagram of a non-limiting embodiment of a system 400 comprising an oxygen scavenger 444. As illustrated, the oxygen scavenger 444, comprising a scavenger inlet 444a and a scavenger outlet 444b, can be provided in fluid communication with the DHO reactor 102 (Figure 1) through the DHO outlet line 110 and with the cooling tower 104 through the scavenger outlet line 446. The scavenger inlet 444a can be configured to receive the DHO outlet stream and can be suitable for conveying the DHO outlet stream to the oxygen scavenger 444.The oxygen scavenger 444 can remove a substantial portion of the oxygen in the DHO outlet stream and produce a scavenger outlet stream comprising the DHO outlet stream with the substantial portion of oxygen removed. The oxygen scavenger 444 can have various designs as known in the art. The outlet of the scavenger 444b can be configured to receive the scavenger outlet stream and can be suitable for conveying the scavenger outlet stream from the oxygen scavenger 444 to the outlet line of the scavenger 446. The cooling inlet 104a of the cooling tower 104 can be configured to receive the scavenger outlet stream. With reference to Figure 5, in several examples, an amine tower 548 can be arranged between the cooling tower 104 and the caustic scrubbing tower 106. Figure 5 is a flow diagram of a non-limiting example of a system 500 comprising an amine tower 548. As illustrated, the amine tower 548, comprising an amine tower inlet 548a and an amine tower outlet 548b, can be provided in fluid communication with the cooling tower 104 (Figure 1) through the cooling outlet line 114 and with the caustic scrubbing tower 106 through the amine tower outlet line 550. The inlet of the amine tower 548a can be configured to receive the cooling outlet stream and can be suitable for conveying the cooling outlet stream to the amine tower 548.The 548 amine tower can remove a substantial portion of carbon dioxide from the cooling outlet stream and produce an amine tower outlet stream comprising the cooling outlet stream with the substantial portion of carbon dioxide removed. The 548 amine tower can have various designs as known in the art. The outlet of the amine tower 548b can be configured to receive the outlet stream from the amine tower and can be suitable for conveying the amine tower outlet stream from the amine tower 548 to the outlet line of the amine tower 550. The wash inlet 106a of the caustic wash tower 106 can be configured to receive the amine tower outlet stream from the outlet line of the amine tower 550. Having a high-efficiency oxygenated compound removal system upstream of the amine tower 548 can limit, and in some cases prevent, amine degradation in the presence of the oxygenated compound in the amine tower 548. For example, the oxygenated compound can form thermostable salts with the amine in the amine tower 548, which can degrade efficiency and shorten the operating life of the amine tower 548. With reference to FIGURE 6, in several examples, a polymerization reactor 652 can be in fluid communication with the caustic scrubbing tower 106 via the scrubbing outlet line 116. FIGURE 6 is a flow diagram of a non-limiting example of a system 600 comprising a polymerization reactor 652. As illustrated, the polymerization reactor 652, comprising a polymerization inlet 652a and a polymerization outlet 652b, can be provided in fluid communication with the caustic scrubbing tower 106 via the scrubbing outlet line 116. In several examples, a demethanizer (not shown) can be arranged in the scrubbing outlet line 116 between the caustic scrubbing tower 106 and the polymerization reactor 652. The polymerization inlet 652a can be configured to receive the DHO outlet stream. and may be suitable for transporting the DHO outlet stream to the polymerization reactor 652.The polymerization reactor 652 can produce a polymer from the alkene and generate a polymerization outlet stream comprising the polymer. In several examples, the polymer comprises at least one of polyethylene, polypropylene, and polybutylene. The polymerization reactor 652 can have various designs as known in the art. The polymerization outlet 652b can be configured to receive the polymerization outlet stream and can be suitable for conveying the polymerization outlet stream from the polymerization reactor 652 to the polymerization outlet line 654. The concentrations of the components within the system can be measured at any point in the process using any means known in the art. For example, a detector such as a gas chromatograph, an infrared spectrometer, and a Raman spectrometer can be placed downstream or upstream of the DHO reactor 102, the cooling tower 104, the caustic scrubbing tower 106, the separator 238, the separation vessel 326, the oxygen scavenger 444, the amine tower 548, and the polymerization reactor 652. In several examples, the inlet stream of DHO 108 may comprise mixtures that fall within the flammability limits of the components. For example, the mixture may exist under conditions that prevent the propagation of an explosive event. In these examples, the flammable mixture may be created within a medium where ignition can be immediately quelled. In several examples, oxygen and lower alkanes may be mixed at a point where they are surrounded by a flame-retardant material. Therefore, the surrounding material can quell any ignition. The flame-retardant material includes, for example, metallic or ceramic components, such as stainless steel walls or ceramic supports.In several examples, oxygen and lower alkanes can be mixed at low temperatures, where an ignition event may not lead to an explosion. The mixture can then be introduced into the DHO reactor before the temperature is increased. Therefore, flammable conditions may not exist until the mixture is surrounded by flame-stopping material within the reactor. In several examples, olefins produced using a DHO reactor, or any of the processes or complexes described in this document, can be used to prepare various olefin derivatives using a polymerization reactor. Olefin derivatives include, but are not limited to, polyethylene, polypropylene, ethylene oxide, propylene oxide, polyethylene oxide, polypropylene oxide, vinyl acetate, vinyl chloride, acrylic esters (e.g., methyl methacrylate), thermoplastic elastomers, thermoplastic olefins, mixtures thereof, and combinations thereof. In several examples, ethylene and optionally α-olefins can be produced in a DHO reactor, or any of the processes or complexes described herein, and used to manufacture polyethylene using a polymerization reactor. The polyethylene produced from the ethylene and optional α-olefins described herein may include ethylene homopolymers, ethylene-α-olefin copolymers, resulting in HDPE, MDPE, LDPE, LLDPE, and VLDPE. The polyethylene produced using ethylene and optional α-olefins described herein can be produced using any suitable polymerization process and equipment. Suitable ethylene polymerization processes include, but are not limited to, gas-phase polyethylene processes, high-pressure polyethylene processes, low-pressure polyethylene processes, solution polyethylene processes, suspension polyethylene processes, and suitable combinations thereof arranged in parallel or in series.A process for converting a lower alkane to an alkene according to the present description may include introducing an inlet stream comprising oxygen and the lower alkane into a DHO 102 reactor. In several examples, the inlet stream may further include at least one carbon-based oxide, steam, and an inert diluent. At least a portion of the lower alkane may be converted to the alkene in the DHO 102 reactor. In several examples, the alkane may comprise ethane and the alkene comprises ethylene. In several examples, the alkane may comprise propane and the alkene comprises propylene. In several examples, the alkane comprises butane and the alkene may comprise butylene. An DHO outlet stream comprising the alkene, an oxygenated compound, and a carbon-based oxide may be produced.In several examples, the DHO outlet stream may comprise at least one of a sulfide, water, an unreacted alkane, oxygen, and an inert diluent. The DHO outlet stream can be fed into a cooling tower 104, and the oxygenated compound can be removed from the DHO outlet stream in the cooling tower 104 to produce a cooling outlet stream comprising at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide. Furthermore, the cooling tower 104 can produce an oxygenated compound outlet stream comprising at least a substantial portion of the oxygenated compound. In several examples, the DHO outlet stream can be fed into an oxygen eliminator 444 before the cooling tower 104. Oxygen can be removed from the DHO outlet stream in the oxygen eliminator 444 and the DHO outlet stream can be fed into the cooling tower 104 after the oxygen eliminator 444. The cooling outlet stream can be fed into a caustic scrubbing tower 106. The cooling outlet stream can be contacted with a caustic agent to form a caustic outlet stream comprising a metallic salt. In several examples, the cooling outlet stream is contacted with the caustic agent in the caustic scrubbing tower 106. / uu jo io In several examples, the cooling outlet stream can be fed into an amine scrubbing tower 548 before the caustic scrubbing tower 106. A substantial portion of the carbon-based oxide can be removed from the cooling outlet stream. The cooling outlet stream with the substantial portion of carbon oxide removed can then be fed into the caustic scrubbing tower 106. The caustic outlet stream can be introduced into cooling tower 104, and the DHO outlet stream can be contacted with the caustic outlet stream to form a derived salt and, in several instances, a carbon-based oxide and sulfide. In several instances, the DHO outlet stream is contacted with the caustic outlet stream in cooling tower 104. The oxygenated compound outlet stream can comprise a substantial portion of the derived salt. In several instances, the pH of cooling tower 104 can be maintained within a range of 2 to 12, such as 4 to 11, 4 to 7, or 7 to 11. In several instances, the pH of cooling tower 104 can be maintained within a range of the pKa of the oxygenated compound to the pKa of the metallic salt. In several examples, the oxygenated compound outlet stream can be fed into a separation vessel 326. The oxygenated compound can be separated from the derived salt within the oxygenated compound outlet stream. A second oxygenated compound outlet stream can be produced comprising a substantial portion of the oxygenated compound from the oxygenated compound outlet stream. A separation outlet stream can be produced comprising a substantial portion of the derived salt from the oxygenated compound outlet stream. In several examples, a portion of the separation outlet stream can be recycled to the separation vessel 326. In several examples, a supplementary salt, such as ethyl acetate, can be introduced into the separation vessel 326. In several examples, the DHO outlet stream can be separated into a first intermediate stream and a second intermediate stream. The first intermediate stream may comprise at least a substantial portion of the oxygenated compound from the DHO outlet stream. The second intermediate stream may comprise at least a substantial portion of the alkene from the DHO outlet stream. The second intermediate stream may come into contact with the caustic outlet stream to form the derived salt and, in several examples, a carbon-based oxide and / or a sulfide. In several examples, olefin derivatives can be produced from the alkene. This description may introduce an alternative use for the caustic waste stream, and in some examples, may eliminate the need to dispose of the caustic waste stream altogether. Furthermore, reusing the caustic waste stream can yield a useful byproduct salt that can aid in the separation of the oxygenated compound from the cooling outlet stream and the purification of the oxygenated compound in the separation vessel. Efficient removal of the oxygenated compound from the cooling outlet stream can extend the operating life of downstream equipment, such as protecting the amine tower from fouling and degradation of the amine solution. Additionally, the byproduct salt can be sold. Furthermore, effective purification of the oxygenated compound can create a marketable product such as glacial acetic acid. The method, system, and apparatus according to the present description may include other suitable process equipment such as, for example, a compressor and a pump. EXAMPLES Computational modeling of a liquid-liquid separation vessel was used with ASPEN Plus® chemical process simulation software version 8.6, commercially available from Aspen Technology, Inc., Bedford, Massachusetts, to demonstrate the increase in concentration of a dilute oxygenated compound stream using the described method. The model simulates the effect of temperature, mass flow rate, and oxygenated compound outlet stream composition on the composition of the separation outlet stream and the second oxygenated compound outlet stream. The compositions chosen for each example reflect compositions that may be present in an oxygenated compound outlet stream produced from a cooling tower downstream of an oxidative dehydrogenation process of ethane.The oxygen exhaust streams from an ethane DHO process typically comprise dilute acetic acid, where the mass fraction of acetic acid ranges from 1 to 5%, but in some cases can reach 25%. The oxygenated compound exhaust stream may also contain trace levels of carbon oxides, such as carbon dioxide. The addition of a caustic exhaust stream comprising a metallic salt in the cooling tower can reduce the mass fraction of acetic acid in the oxygenated compound exhaust stream. Example 1 For Example 1, the inlet levels represent compositions of carbon dioxide, water, acetic acid, and sodium acetate (as sodium ion and acetate ion) representative of an oxygenated compound outlet stream coming directly from the cooling tower without any additional sodium acetate added (via a recycle line). The total mass flow rate was set at 6980 kg / h, at a gauge pressure of 185.7 kPa and a temperature of 40°C. The simulation results revealed a mass flow rate of 5436 kg / h for the first separation outlet stream and a mass flow rate of 1545 kg / h for the second separation outlet stream. Example 2 For Example 2, the inlet levels represent compositions of carbon dioxide, water, acetic acid, and sodium acetate (as sodium ion and acetate ion) for the oxygenated compound outlet stream, which includes additional sodium acetate (added via a recycle line). The total mass flow rate was set at 55,982 kg / h, at a gauge pressure of 465 kPa and a temperature of 65°C. The simulation results revealed a mass flow rate of 54,917 kg / h for the first separation outlet stream and a mass flow rate of 975 kg / h for the second separation outlet stream. Example 3 For Example 3, the inlet levels represent compositions of carbon dioxide, water, acetic acid, and sodium acetate (as sodium ion and acetate ion) for the oxygenated compound outlet stream, which includes additional sodium acetate ion (added via a recycle line). The total mass flow rate was set at 61,014 kg / hr, a gauge pressure of 465 kPa, and a temperature of 52°C. The simulation results revealed a mass flow rate for the first separation outlet stream of 60,537 kg / hr and a mass flow rate for the second separation outlet stream of 477 kg / hr. TABLE 1 Oxygen Outlet Stream Separation Outlet Stream Second Oxygenated Compound Outlet Stream Example 1 2 3 1 2 3 1 2 3 Temp (°C) 40 65 52 40 64 53 40 64 53 Mass Flow (kg / hr) 6980 55982 61014 5436 54917 60537 1545 975 477 Mass Fraction CO2 0.001 0.000 0.000 0.000 0.000 0.000 0.006 0.000 0.000 H2O 0.235 0.162 0.233 7 0.287 0.164 0.235 0.052 0.046 0.074 CH3OOH 0.219 0.024 0.026 0.013 0.024 0.019 0.942 0.954 0.925 Na+ 0.153 0.228 0.208 0.196 0.232 0.210 0.000 0.000 0.000 CH3COO~ 0.392 0.586 0.533 0.504 0.596 0.537 0.000 0.000 0.000 As shown in Table 1, all examples demonstrate significant separation of sodium acetate from acetic acid, resulting in a much more concentrated and pure acetic acid solution. The second oxygenated compound outlet stream in each example shows no detectable sodium acetate. Adding excess sodium acetate to the oxygenated compound outlet stream by recycling the separation outlet stream increased the mass flow rate without increasing the mass fraction of acetic acid in the second oxygenated compound outlet stream. However, in both Example 2 and Example 3, the mass fraction of acetic acid in the oxygen outlet stream was significantly lower compared to Example 1.This demonstrates that recycling the separation outlet stream would be beneficial for oxygenated compound outlet streams where oxygenated compound levels are lower, such as in cases where the cooling tower comprises a first and a second stage. Removing a substantial portion of the acetic acid in the first stage results in the stream entering the second stage having a significantly lower acetic acid mass fraction. These results show that even in this case, the acetic acid level in the second oxygenated compound outlet stream is above 90% (mass fraction). ADDITIONAL OPTIONS The present invention provides the following exemplary forms, the numbering of which should not be interpreted as a designation of levels of importance. Mode 1 provides a method for the separation of an oxygenated compound from a stream. The method includes introducing the stream containing the oxygenated compound and a caustic outlet stream containing a metallic salt into a cooling tower, contacting the oxygenated compound with the metallic salt in the cooling tower to convert a portion of the oxygenated compound into a derived salt, and removing from the cooling tower a cooling outlet stream and an oxygenated compound outlet stream that includes at least a substantial portion of the unconverted oxygenated compound and at least a substantial portion of the derived salt. Mode 2 provides the method of mode 1, where the current and caustic outlet stream are introduced separately into the cooling tower. Mode 3 provides the method of either mode 1-2, wherein the introduction of the current into the cooling tower occurs concomitantly with the introduction of the caustic outlet current into the cooling tower. Mode 4 provides the method of any of modes 1-3, wherein the oxygenated compound outlet stream is introduced into a separation vessel to separate the unconverted oxygenated compound from the derived salt, producing a second oxygenated compound outlet stream that includes a substantial portion of the unconverted oxygenated compound from the oxygenated compound outlet stream and a separation outlet stream that includes a substantial portion of the derived salt from the oxygenated compound outlet stream. Mode 5 provides the method of mode 4 where a portion of the separation outlet stream is recycled back to the separation vessel. Mode 6 provides the method of any of modes 4-5, wherein ethyl acetate is introduced into the separation vessel. Mode 7 provides the method of any of modes 1-6, wherein the stream includes at least one of a carbon-based oxide, a sulfide, an unreacted alkane, an alkene, and oxygen, and the quenching outlet stream includes at least a substantial portion of at least one of a carbon-based oxide, a sulfide, an unreacted alkane, an alkene, and oxygen that are present in the stream. Mode 8 provides the method of any of modes 1-7, wherein the current includes a carbon-based oxide selected from at least one of carbon monoxide and carbon dioxide. Mode 9 provides the method of any of modes 7-8, wherein the carbon-based oxide includes carbon dioxide and further includes introducing the cooling outlet stream into an amine scrubbing tower and removing a substantial portion of the carbon-based oxide from the cooling outlet stream. Mode 10 provides the method of any of modes 1-9, wherein the stream is introduced into an oxygen eliminator and oxygen is removed from the stream, if present, before introducing the stream into the cooling tower. Mode 11 provides the method of any of modes 1 to 10, wherein the pH of the cooling tower is maintained in a range of one pKa of the oxygenated compound to one pKa of the metallic salt. Modality 12 provides the method of any of modalities 1-11, wherein the oxygenated compound includes acetic acid which has a pKa of 4.7 and the metal salt includes sodium bicarbonate which has a pKa of 10.3. Mode 13 provides the method of any of modes 1-12, wherein a substantial portion of the oxygenated compound is removed from the stream before introducing the stream into the cooling tower. Mode 14 provides the method of any of modes 1-13, wherein the cooling outlet stream is introduced into a caustic scrubbing tower and brought into contact with a caustic agent selected from at least one of sodium hydroxide, potassium hydroxide, and ammonium hydroxide, to form the metallic salt that is removed from the caustic scrubbing tower. Mode 15 provides the method of mode 14 where the metallic salt removed from the caustic scrubbing tower is recycled back to the cooling tower as a component of the caustic outlet stream. Modality 16 provides the method of any of modalities 1-15, wherein the metal salt includes at least one of sodium hydrogen sulfide, sodium bicarbonate, potassium carbonate, and ammonium bicarbonate. Modality 17 provides the method of any of modalities 1-16, wherein the oxygenated compound includes at least one of acetic acid, acrylic acid, maleic acid, and maleic anhydride. Mode 18 provides the method of any of modes 1-17, wherein the derived salt includes at least one of the following: sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate, and ammonium malonate. Mode 19 provides the method of any of modes 1-18, wherein the caustic outlet stream is produced by at least one process selected from an oxidative dehydrogenation process, a cracking process, a refining process, a papermaking process, a soapmaking process, a detergentmaking process, and a food manufacturing process. Mode 20 provides the method of any of modes 1-19, wherein the stream includes an alkene that includes at least one of ethylene and propylene. Modality 21 provides the method of modality 20, wherein olefin derivatives are produced from the alkene. Modality 22 provides the method of modality 21, wherein the olefin derivatives include at least one of the following: polyethylene, polypropylene, ethylene oxide, propylene oxide, polyethylene oxide, polypropylene oxide, thermoplastic elastomers, and thermoplastic olefins. Modality 23 provides the method of modality 22, wherein the olefin derivative is a polyethylene and includes at least one of ethylene homopolymers, ethylene and α-olefin copolymers, high-density polyethylene (HDPE), medium-density polyethylene (MDPE), low-density polyethylene (LDPE), linear low-density polyethylene (LLDPE), and very low-density polyethylene (VLDPE). Mode 24 provides an apparatus for separating an oxygenated compound from a stream. The apparatus includes a cooling tower comprising a cooling inlet for receiving the stream containing the oxygenated compound, a cooling outlet for removing a cooling outlet stream, a metal salt inlet for introducing a caustic outlet stream containing a metal salt, and an oxygenated compound outlet for removing an oxygenated compound outlet stream. The oxygenated compound may come into contact with the metal salt in the cooling tower to convert a portion of the oxygenated compound into a derived salt, a substantial portion of which is removed together with a substantial portion of unconverted oxygenated compound as a component of the oxygenated compound outlet stream. Mode 25 provides the apparatus of mode 23, which further includes a separation vessel including a separation inlet in fluid communication with the oxygenated compound outlet and configured to receive the oxygenated compound outlet stream, a derived salt outlet for removing a derived salt outlet stream that includes a derived salt, and a separation outlet configured to remove a separation outlet stream that includes a substantial portion of the unconverted oxygenated compound present in the oxygenated compound outlet stream. Mode 26 provides the apparatus of mode 25, wherein the separation vessel further includes a recycling line in fluid communication with the bypass salt outlet to receive the bypass salt outlet stream and direct at least a portion of the bypass salt outlet stream to the separation inlet of the separation vessel. Modality 27 provides the apparatus of any of Modalities 25-26, wherein the separation vessel further includes a supplementary salt inlet suitable for introducing ethyl acetate into the separation vessel. Mode 28 provides the apparatus of any of modes 24-27, wherein the current includes at least one of a carbon-based oxide, a sulfide, water, an unreacted alkane, an alkene, and oxygen. Mode 29 provides the apparatus of mode 28, wherein the carbon-based oxide includes at least one of either carbon monoxide or carbon dioxide. Mode 30 provides the apparatus of mode 29, wherein the carbon-based oxide includes carbon dioxide and further includes an amine scrubbing tower comprising an amine inlet and an amine outlet, the amine inlet being in fluid communication with the cooling outlet to receive the cooling outlet stream, and the amine scrubbing tower configured to remove at least a portion of the carbon-based oxide from the cooling outlet stream. Mode 31 provides the apparatus of any of the modes 24-30, which further includes an oxygen eliminator comprising an eliminator inlet and an eliminator outlet, the oxygen eliminator suitable for removing oxygen from the stream and the eliminator outlet in fluid communication with the cooling tower inlet to direct the stream towards the cooling inlet. Mode 32 provides the apparatus of any of modes 24-31, wherein the cooling tower is configured for a pH in a range of one pKa of the oxygenated compound to one pKa of the metallic salt. Modality 33 provides the apparatus of any of modalities 24-32, wherein the oxygenated compound includes acetic acid which has a pKa of 4.7 and the metal salt includes sodium bicarbonate which has a pKa of 10.3. Mode 34 provides the apparatus of any of modes 24-33, wherein the cooling tower includes a primary stage and a secondary stage, wherein the primary stage is configured to remove a substantial portion of oxygenated compound from the stream and includes the cooling inlet, a first intermediate outlet, and a second intermediate outlet, the first intermediate outlet being configured for removal from the stream of the primary stage and being in fluid communication with an intermediate inlet of the secondary stage, the second intermediate outlet being suitable for removing the substantial portion of oxygenated compound removed from the stream, and the second stage including the cooling outlet, the metal salt inlet, and the oxygenated compound outlet. Mode 35 provides the apparatus of any of modes 24-34, which further includes a caustic scrubbing tower comprising a scrubbing inlet, a scrubbing outlet, a scrubbing inlet and a caustic outlet, the scrubbing inlet being fluidly connected with the cooling outlet to receive the cooling outlet stream, the caustic outlet configured to remove the caustic outlet stream, the caustic inlet configured to introduce at least one of sodium hydroxide, potassium hydroxide and ammonium hydroxide into the caustic scrubbing tower and wherein the caustic scrubbing tower further includes a return line in fluidly connected with the caustic outlet to receive the caustic outlet stream and remove the caustic outlet stream to the metallic salt inlet of the cooling tower. Modality 36 provides the apparatus of any of modalities 24-35, wherein the metallic salt includes at least one of sodium hydrogen sulfide, sodium bicarbonate, potassium carbonate, and ammonium bicarbonate. Modality 37 provides the apparatus of any of modalities 24 to 36, wherein the oxygenated compound / uu jo io includes at least one of acetic acid, acrylic acid, maleic acid, and maleic anhydride. Modality 38 provides the apparatus of any of modalities 24-37, wherein the derived salt includes at least one of the following: sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate, and ammonium malonate. Mode 39 provides the apparatus of any of modes 24-38, wherein the caustic outlet stream is produced by at least one process selected from an oxidative dehydrogenation process, a cracking process, a refining process, a papermaking process, a soapmaking process, a detergentmaking process, and a food manufacturing process. Mode 40 provides the apparatus of any of modes 24-39, wherein the current includes an alkene that includes at least one of ethylene and propylene. Modality 41 provides the apparatus of modality 40, which further includes a polymerization reactor suitable for preparing olefin derivatives from the alkene. Modality 42 provides the apparatus of modality 41, wherein the olefin derivatives include at least one of polyethylene, polypropylene, ethylene oxide, propylene oxide, polyethylene oxide, polypropylene oxide, thermoplastic elastomers, and thermoplastic olefins. Modality 43 provides the apparatus of modality 42, wherein the olefin derivative is polyethylene and includes at least one of ethylene homopolymers, ethylene and α-olefin copolymers, high-density polyethylene (HDPE), medium-density polyethylene (MDPE), low-density polyethylene (LDPE), linear low-density polyethylene (LLDPE), and very low-density polyethylene (VLDPE). Mode 44 provides a system for separating an oxygenated compound from a stream. The system includes a cooling tower configured to receive the stream containing the oxygenated compound and a caustic outlet stream containing a metallic salt, contacting the oxygenated compound with the metallic salt to convert a portion of the oxygenated compound to a derivative salt, cooling the derivative salt and the unconverted oxygenated compound, producing a cooling outlet stream containing the stream with a substantial portion of the oxygenated compound removed, and producing an oxygenated compound outlet stream containing at least a substantial portion of the unconverted oxygenated compound and at least a substantial portion of the derivative salt. Mode 45 provides the system of mode 44 which further includes a separation vessel configured to receive the oxygenated compound outlet stream, separate the unconverted oxygenated compound from the derived salt within the first oxygenated compound outlet stream, produce a second oxygenated compound outlet stream which includes a substantial portion of the unconverted oxygenated compound from the oxygenated compound outlet stream, and produce a separation outlet stream which includes a substantial portion of the derived salt from the oxygenated compound outlet stream. Mode 46 provides the system of mode 45, wherein the separation vessel also includes a recycling line configured to recycle a portion of the separation outlet stream to the separation vessel. Mode 47 provides the system of any of modes 45-46, wherein the separation vessel is further configured to receive ethyl acetate. Mode 48 provides the system of any of modes 44-47, wherein the stream includes at least one of a carbon-based oxide, a sulfide, an unreacted alkane, an alkene, and oxygen. Mode 49 provides the system of mode 48, wherein the carbon-based oxide includes at least one of carbon monoxide and carbon dioxide. Mode 50 provides the system of mode 49, wherein the carbon-based oxide includes carbon dioxide and further includes an amine scrubbing tower configured to receive the cooling outlet stream and remove at least a portion of the carbon-based oxide from the cooling outlet stream. Mode 51 provides the system of any of the modes 44-50, which also includes an oxygen eliminator configured to remove oxygen from the stream and direct the stream to the cooling tower. Mode 52 provides the system of any of modes 44-51, where the cooling tower is configured to maintain a pH in a range of one pKa of the oxygenated compound to one pKa of the metallic salt. Mode 53 provides the system of any of modes 44-52, where the cooling tower is configured to maintain a pH in a range of 2 to 12. Mode 54 provides the system of any of modes 44-53 where the cooling tower includes two stages, the first stage configured to remove a substantial portion of the oxygenated compound from the stream, and the second stage configured to receive the stream with a substantial portion of the oxygenated compound removed. Mode 55 provides the system of any of modes 44-54, which further includes a caustic scrubbing tower configured to receive the cooling outlet stream and a caustic agent selected from at least one of sodium hydroxide, potassium hydroxide, and ammonium hydroxide, in contact with a substantial portion of the carbon-based oxide from the cooling outlet stream with the caustic agent to form a metallic salt and produce the caustic outlet stream, and includes a return line configured to direct the caustic outlet stream from the caustic scrubbing tower to the cooling tower. Modality 56 provides the system of any of modalities 44-55, wherein the metal salt includes at least one of sodium hydrogen sulfide, sodium bicarbonate, potassium carbonate, and ammonium bicarbonate. Modality 57 provides the system of any of modalities 44-56, wherein the oxygenated compound includes at least one of acetic acid, acrylic acid, maleic acid, and maleic anhydride. Modality 58 provides the system of any of modalities 44-57, wherein the derived salt includes at least one of the following: sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate, and ammonium malonate. Mode 59 provides the system of any of modes 44-58, wherein the caustic outlet stream is produced by at least one process selected from an oxidative dehydrogenation process, a cracking process, a refining process, a papermaking process, a soapmaking process, a detergentmaking process, and a food manufacturing process. Mode 60 provides the system of any of modes 44-59, wherein the stream further includes an alkene that includes at least one of ethylene and propylene. Mode 61 provides the system of mode 60, which further includes a polymerization reactor configured to produce olefin derivatives from the alkene. Modality 62 provides the system of modality 61, wherein the olefin derivatives include at least one of polyethylene, polypropylene, ethylene oxide, propylene oxide, polyethylene oxide, polypropylene oxide, thermoplastic elastomers, and thermoplastic olefins. Modality 63 provides the system of modality 62, wherein the olefin derivative is polyethylene and includes at least one of the ethylene homopolymers, ethylene and α-olefin copolymers, high-density polyethylene (HDPE), medium-density polyethylene (MDPE), low-density polyethylene (LDPE), linear low-density polyethylene (LLDPE), and very low-density polyethylene (VLDPE). Motif 64 provides a method for converting a lower alkane into an alkene comprising introducing an inlet stream comprising oxygen and the lower alkane into an oxidative dehydrogenation (ODD) reactor and converting at least a portion of the lower alkane into the alkene in the ODD reactor and producing an ODD outlet stream comprising the alkene, unconverted lower alkane, an oxygenated compound, and a carbon-based oxide, introducing the ODD outlet stream and a caustic outlet stream comprising a metallic salt into a cooling tower, contacting the oxygenated compound with the metallic salt within the cooling tower to convert a portion of the oxygenated compound into a derived salt, cooling a substantial portion of the unconverted oxygenated compound and a substantial portion of the derived salt, and removing a cooling outlet stream comprising the alkene.the unconverted lower alkane and carbon-based oxide from the cooling tower, and remove an oxygenated compound outlet stream that includes the cooled derivative salt and the cooled unconverted oxygenated compound from the cooling tower. Mode 65 provides the method of mode 64, which further includes introducing the cooling outlet stream into a caustic scrubbing tower that includes a caustic agent, contacting the carbon-based oxide from the cooling outlet stream with the caustic agent in the caustic scrubbing tower to form a metallic salt, removing a caustic outlet stream that includes the metallic salt from the caustic scrubbing tower, and introducing the caustic outlet stream into the cooling tower with the DHO outlet stream. Mode 66 provides the method of any of modes 64-65, which further includes introducing the oxygenated compound outlet stream into a separation vessel and separating the unconverted oxygenated compound from the derived salt in the separation vessel to produce a second oxygenated compound outlet stream that includes a substantial portion of the unconverted oxygenated compound from the oxygenated compound outlet stream and a separation outlet stream that includes a substantial portion of the derived salt from the oxygenated compound outlet stream. Mode 67 provides the method of mode 66, which further includes recycling a portion of the separation outlet stream that includes the diverted salt to the separation vessel. Mode 68 provides the method of any of modes 66-67, which also includes introducing ethyl acetate into the separation vessel. Mode 69 provides the method of any of modes 64-68, wherein the carbon-based oxide includes carbon dioxide and further includes introducing the cooling outlet stream to an amine scrubbing tower and removing a substantial portion of the carbon-based oxide from the cooling outlet stream before introducing the cooling outlet stream to the caustic scrubbing tower. Mode 70 provides the method of any of modes 64-69, wherein the DHO outlet stream also includes at least one of a sulfide, water, and oxygen. Mode 71 provides the method of any of modes 64-70, which further includes introducing the DHO outlet stream into an oxygen eliminator and removing the oxygen from the DHO outlet stream in the oxygen eliminator before introducing the DHO outlet stream into the cooling tower. Mode 72 provides the method of any of modes 64-71, which further includes maintaining a cooling tower pH in a range of one pKa of the oxygenated compound to one pKa of the metallic salt. Modality 73 provides the method of any of modalities 64-72, wherein the oxygenated compound includes acetic acid having a pKa of 4.7 and the metal salt includes sodium bicarbonate having a pKa of 10.3. Mode 74 provides the method of any of modes 64-73, which further includes removing a substantial portion of the oxygenated compound within the DHO outlet stream before introducing the DHO outlet stream into the cooling tower. Modality 75 provides the method of any of modalities 65-74, wherein the caustic agent includes at least one of sodium hydroxide, potassium hydroxide, and ammonium hydroxide. Modality 76 provides the method of any of modalities 64-75, wherein the metallic salt includes at least one of sodium bicarbonate, potassium carbonate, and ammonium bicarbonate. Modality 77 provides the method of any of modalities 64-7 6, wherein the carbon-based oxide includes at least one of carbon monoxide and carbon dioxide. Modality 78 provides the method of any of Modalities 64-77, wherein the oxygenated compound includes at least one of acetic acid, acrylic acid, maleic acid, and maleic anhydride. Modality 79 provides the method of any of Modalities 64-78, wherein the derived salt includes at least one of the following: sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate, and ammonium malonate. Mode 80 provides the method of any of modes 64-79, wherein the lower alkane includes ethane and the alkene includes ethylene. Mode 81 provides the method of any of modes 64-79, wherein the lower alkane includes propane and the alkene includes propylene. Modality 82 provides the method of any of modalities 64-81, which further includes the production of olefin derivatives from the alkene. Modality 83 provides the method of modality 82, wherein the olefin derivatives include at least one of polyethylene, polypropylene, ethylene oxide, propylene oxide, polyethylene oxide, polypropylene oxide, thermoplastic elastomers, and thermoplastic olefins. Modality 84 provides the method of modality 83, wherein the olefin derivative includes polyethylene and includes at least one of ethylene homopolymers, ethylene and α-olefin copolymers, high-density polyethylene (HDPE), medium-density polyethylene (MDPE), low-density polyethylene (LDPE), linear low-density polyethylene (LLDPE), and very low-density polyethylene (VLDPE). Modality 85 provides an apparatus for the oxidative dehydrogenation (DHO) of a lower alkane to an alkene. The apparatus includes a DHO reactor comprising a DHO inlet and a DHO outlet. The DHO inlet is configured to receive an inlet stream of DHO comprising the lower alkane in the DHO reactor. The DHO outlet is suitable for removing an outlet stream of DHO comprising the alkene, the unconverted lower alkane, an oxygenated compound, and a carbon-based oxide from the DHO reactor. A cooling tower includes a cooling inlet, a cooling outlet, a metal salt inlet, and an oxygenated compound outlet. The cooling inlet is in fluid communication with the DHO outlet to receive the outlet stream of DHO.the cooling outlet configured to remove a cooling outlet stream that includes at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide from the cooling tower, the metal salt inlet configured to receive a caustic outlet stream that includes a metal salt, the oxygenated compound outlet suitable for removing an oxygenated compound outlet stream that includes at least a substantial portion of the oxygenated compound and a derived salt, a caustic scrubbing tower that includes a scrubbing inlet, a scrubbing outlet, a caustic inlet, and a caustic outlet, the scrubbing inlet in fluid communication with the cooling outlet to receive the cooling outlet stream, the caustic outlet suitable for carrying a caustic outlet stream that includes a metal salt,and a return line in fluid communication with the caustic outlet to receive the caustic outlet stream and direct the caustic outlet stream to the metallic salt inlet of the cooling tower. Mode 86 provides the apparatus of mode 85, which further includes a separation vessel comprising a separation inlet, a derivative salt outlet, and a separation outlet, the separation inlet being fluidly connected with the oxygenated compound outlet to receive the oxygenated compound outlet stream, the derivative salt outlet suitable for carrying a separation outlet stream comprising a derivative salt, and the separation outlet suitable for carrying a second oxygenated compound outlet stream comprising a substantial portion of the oxygenated compound. Mode 87 provides the apparatus of mode 86, wherein the separation vessel further includes a recycling line in fluid communication with the outlet of the diverted salt to receive the separation outlet stream and to release at least a portion of the separation outlet stream to the inlet of the separation vessel. Modality 88 provides the apparatus of modality 87, wherein the separation vessel further includes a supplementary salt inlet suitable for introducing ethyl acetate into the separation vessel. / uuoo io Modality 89 provides the apparatus of any of Modalities 85-88, further comprising an amine washing tower comprising an amine inlet and an amine outlet, the amine inlet being fluidly connected with the cooling outlet to receive the cooling outlet stream, the amine washing tower suitable for removing at least a portion of the carbon-based oxide from the cooling outlet stream, and the amine outlet being fluidly connected with the washing inlet of the caustic washing tower to deliver the cooling outlet stream to the washing inlet. Mode 90 provides the apparatus of any of modes 85-89, wherein the DHO outlet stream further includes at least one of a sulfide, water, an unreacted alkane, and oxygen. Modality 91 provides the apparatus of any of the modalities 85-90, which further includes an oxygen eliminator comprising an eliminator inlet and an eliminator outlet, the eliminator inlet in fluid communication with the DHO outlet to receive the DHO outlet stream, the oxygen eliminator suitable for removing oxygen from the DHO outlet stream, and the eliminator outlet in fluid communication with the cooling tower inlet to deliver the DHO outlet stream to the cooling inlet. Mode 92 provides the apparatus of any of modes 85-91, wherein the cooling tower is suitable for a pH in a range of one pKa of the oxygenated compound to one pKa of the metallic salt. Modality 93 provides the apparatus of any of modalities 85-92, wherein the oxygenated compound includes acetic acid which has a pKa of 4.7 and the metal salt includes sodium bicarbonate which has a pKa of 10.3. Mode 94 provides the apparatus of any of modes 85-93, wherein the cooling tower further includes a primary stage and a secondary stage, the primary stage configured to remove a substantial portion of the oxygenated compound from the DHO outlet stream and includes the cooling inlet, a first intermediate outlet and a second intermediate outlet, the first intermediate outlet in fluid communication with an intermediate inlet of the secondary stage, the second intermediate outlet suitable for removing the oxygenated compound extracted from the DHO outlet stream, and the second stage including the cooling outlet, the metal salt inlet and the oxygenated compound outlet. Modality 95 provides the apparatus of any of Modalities 85-94, wherein the caustic agent inlet is suitable for conveying at least one of sodium hydroxide, potassium hydroxide, and ammonium hydroxide to the caustic washing tower. Modality 96 provides the device of any of the 85-95 modalities, wherein the metallic salt includes at least one of sodium bicarbonate, potassium carbonate, and ammonium bicarbonate. Modality 97 provides the apparatus of any of modalities 85-96, wherein the carbon-based oxide includes at least one of carbon monoxide and carbon dioxide. Modality 98 provides the apparatus of any of Modalities 85-97, wherein the oxygenated compound includes at least one of acetic acid, acrylic acid, maleic acid, and maleic anhydride. Modality 99 provides the apparatus of any of Modalities 85-99, wherein the derived salt includes at least one of the following: sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate, and ammonium malonate. Modality 100 provides the apparatus of any of modality 85-99, wherein the lower alkane includes ethane and the alkene includes ethylene. Modality 101 provides the apparatus of any of modality 85-99, wherein the lower alkane includes propane and the alkene includes propylene. Modality 102 provides the apparatus of any of Modalities 85-101, which further includes a polymerization reactor suitable for preparing olefin derivatives from the alkene. Modality 103 provides the apparatus of modality 102, wherein the olefin derivatives include at least one of the following: polyethylene, polypropylene, ethylene oxide, propylene oxide, polyethylene oxide, polypropylene oxide, thermoplastic elastomers, and thermoplastic olefins. Modality 104 provides the apparatus of modality 103, wherein the olefin derivative includes polyethylene and includes at least one of ethylene homopolymers, ethylene and α-olefin copolymers, high-density polyethylene (HDPE), medium-density polyethylene (MDPE), low-density polyethylene (LDPE), linear low-density polyethylene (LLDPE), and very low-density polyethylene (VLDPE). Modality 105 provides a system for the oxidative dehydrogenation (DHO) of a lower alkane. The system includes a DHO reactor configured to receive an inlet stream that includes oxygen and the lower alkane and to produce a DHO outlet stream that includes an alkene, an oxygenated compound, and a carbon-based oxide; a cooling tower configured to receive the DHO outlet stream and a caustic outlet stream that includes a metal salt; contacting the oxygenated compound with the metal salt to convert a portion of the oxygenated compound into a derivative salt; cooling the DHO outlet stream; substantially removing the unconverted oxygenated compound and the derivative salt from the DHO outlet stream; and producing a cooling outlet stream that includes at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide.and producing an oxygenated compound outlet stream that includes at least a substantial portion of the unconverted oxygenated compound and at least a substantial portion of the derived salt, a caustic scrubbing tower configured to receive the cooling outlet stream and contact a substantial portion of the carbon-based oxide from the cooling outlet stream with a caustic agent to form a caustic outlet stream that includes a metallic salt, and a return line configured to direct the caustic outlet stream to the cooling tower and contact the caustic outlet stream with the DHO outlet stream to form the derived salt from the metallic salt and the oxygenated compound, wherein the oxygenated compound outlet stream includes a substantial portion of the derived salt. Mode 106 provides the system of mode 105, which further includes a separation vessel configured to receive the oxygenated compound outlet stream and separate the oxygenated compound from the derived salt within the oxygenated compound outlet stream to produce a second oxygenated compound outlet stream that includes a substantial portion of the oxygenated compound from the oxygenated compound outlet stream and a separation outlet stream that includes a substantial portion of the derived salt from the first oxygenated compound stream. Mode 107 provides the system of mode 106, wherein the separation vessel also includes a recycling line configured to recycle a portion of the separation outlet stream that includes the salt diverted to the separation vessel. Mode 108 provides the system of any of modes 106-107, wherein the separation vessel is configured to receive ethyl acetate. Mode 109 provides the system of any of modes 105-108, which further includes an amine scrubbing tower configured to receive the cooling outlet stream, remove at least a portion of the carbon-based oxide from the cooling outlet stream, and draw the cooling outlet stream into the caustic scrubbing tower. Mode 110 provides the system of any of modes 105-109, wherein the DHO outlet stream further includes at least one of a sulfide, water, an unreacted alkane, and oxygen. The 111 modality provides the system of any of the 105-110 modalities, which also includes an oxygen eliminator configured to remove oxygen from the DHO outlet stream and suitable for taking the DHO outlet stream to the cooling tower. Mode 112 provides the system of any of modes 105-111, where the cooling tower is configured to maintain a pH in a range of one pKa of the oxygenated compound to one pKa of the metallic salt. Mode 113 provides the system of any of modes 105-112, where the cooling tower is configured to maintain a pH in a range of 2 to 12. Mode 114 provides the system of any of modes 105-113, wherein the cooling tower includes a primary stage and a second stage, the primary stage configured to remove a substantial portion of the oxygenated compound from the DHO outlet stream before directing the DHO outlet stream to the second stage, the second stage configured to contact the DHO outlet stream with the caustic outlet stream to form a salt derived from the metallic salt and the compound / uu jo io 100% oxygenated. Mode 115 provides the system of any of modes 105-114, wherein the caustic agent includes at least one of sodium hydroxide, potassium hydroxide, and ammonium hydroxide in the caustic scrubbing tower. Modality 116 provides the system of any of modalities 105-115, wherein the metallic salt includes at least one of sodium bicarbonate, potassium carbonate, and ammonium bicarbonate. Modality 117 provides the system of any of modalities 105-116, wherein the carbon-based oxide includes at least one of carbon monoxide and carbon dioxide. Modality 118 provides the system of any of modalities 105-117, wherein the oxygenated compound includes at least one of acetic acid, acrylic acid, maleic acid, and maleic anhydride. Modality 119 provides the system of any of modalities 105-118, wherein the derived salt includes at least one of the following: sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate, and ammonium malonate. Mode 120 provides the system of any of modes 105-119, wherein the lower alkane includes / uu jo io 101 ethane and the alkene includes ethylene. Mode 121 provides the system of any of modes 105-119, wherein the lower alkane includes propane and the alkene includes propylene. Modality 122 provides the system of any of modalities 105-121, which further includes a polymerization reactor configured to produce olefin derivatives from the alkene. Modality 123 provides the system of modality 122, wherein the olefin derivatives include at least one of polyethylene, polypropylene, ethylene oxide, propylene oxide, polyethylene oxide, polypropylene oxide, thermoplastic elastomers, and thermoplastic olefins. Modality 124 provides the system of modality 123, wherein the olefin derivative includes polyethylene and includes at least one of the ethylene homopolymers, ethylene and α-olefin copolymers, high-density polyethylene (HDPE), medium-density polyethylene (MDPE), low-density polyethylene (LDPE), linear low-density polyethylene (LLDPE), and very low-density polyethylene (VLDPE). A person experienced in the technique will recognize that the components, devices, operations / actions, and objects described in this document, and the discussion that the / uu jo io The examples in section 102 are used for conceptual clarity and contemplate various configuration modifications. Consequently, as used in this document, the specific examples / modalities presented and the accompanying discussion are intended to be representative of their more general classes. In general, the use of any specific instance is intended to be representative of its class, and the omission of specific components, devices, operations / actions, and objects should not be considered a limitation. Although the present description provides descriptions of several specific aspects to illustrate various points of the description and / or its potential applications, it is understood that persons skilled in the art will occur to them with variations and modifications. Accordingly, the invention or inventions described herein should be understood to be at least as broad as claimed, and not as narrowly defined by the particular illustrative aspects provided herein. INDUSTRIAL APPLICABILITY The process is applicable to the separation of oxygenated compounds from gas streams. The process is applicable to facilitate the removal of oxygenated compounds from gas streams by converting a portion of the gas. 103 oxygenated compound in a derived salt before removal, allowing simplified concentration of the removed oxygenated compounds by liquid-liquid separation. It is hereby stated that, as of this date, the best method known to the applicant for putting the aforementioned invention into practice is the one that is clear from the present description of the invention.

Claims

1. A method for separating an oxygenated compound from a stream, characterized in that it comprises: introducing the stream comprising the oxygenated compound and a caustic outlet stream comprising a metallic salt into a cooling tower; contacting the oxygenated compound with the metallic salt in the cooling tower to convert a portion of the oxygenated compound into a derived salt; removing from the cooling tower; a cooling outlet stream; and an oxygenated compound outlet stream comprising at least a substantial portion of the unconverted oxygenated compound and at least a substantial portion of the derived salt.

2. The method according to claim 1, characterized in that the current and the caustic outlet current are introduced separately into the cooling tower.

3. The method according to claim 1, characterized in that the introduction of the current into the cooling tower occurs concomitantly with the introduction of the caustic outlet current into the cooling tower.

4. The method according to claim 1, characterized in that it further comprises: introducing the oxygenated compound outlet stream into a separation vessel and separating the unconverted oxygenated compound from the derived salt to produce: a second oxygenated compound outlet stream comprising a substantial portion of the oxygenated compound from the oxygenated compound outlet stream; and a separation outlet stream comprising a substantial portion of the derived salt from the oxygenated compound outlet stream.

5. The method according to claim 4, characterized in that it further comprises recycling a portion of the separation outlet stream to the separation vessel.

6. The method according to claim 4, characterized in that it further comprises introducing ethyl acetate into the separation vessel.

7. The method according to claim 1, characterized in that: the stream further comprises at least one of a carbon-based oxide, a sulfide, an unreacted alkane, an alkene, or oxygen; and 106 the cooling outlet stream comprises at least a substantial portion of at least one of a carbon-based oxide, a sulfide, an unreacted alkane, an alkene, or oxygen that are present in the stream.

8. The method according to claim 7, characterized in that the stream comprises a carbon-based oxide selected from at least one of carbon monoxide and carbon dioxide.

9. The method according to claim 8, characterized in that the carbon-based oxide comprises carbon dioxide and further comprises introducing the cooling outlet stream into an amine scrubbing tower and removing a substantial portion of the carbon-based oxide from the cooling outlet stream.

10. The method according to claim 7, characterized in that it further comprises introducing the stream into an oxygen eliminator and removing oxygen, if present, from the stream in the oxygen eliminator before introducing the stream into the cooling tower.

11. The method according to claim 1, characterized in that it further comprises maintaining the pH of the cooling tower in a range of the pKa of the oxygenated compound to the pKa of the metallic salt.

12. The method according to claim 11, characterized in that the oxygenated compound comprises acetic acid having a pKa of 4.7 and the metal salt comprises sodium bicarbonate having a pKa of 10.

3.

13. The method according to claim 1, characterized in that it further comprises removing a portion of the oxygenated compound from the stream before introducing the stream into the cooling tower.

14. The method according to claim 7, characterized in that it further comprises: introducing into a caustic scrubbing tower: the cooling outlet stream; and a caustic agent selected from at least one of sodium hydroxide, potassium hydroxide, or ammonium hydroxide; wherein the carbon-based oxide present in the cooling outlet stream is brought into contact with the caustic agent in the caustic scrubbing tower to form the metallic salt, which can be removed from the caustic scrubbing tower and introduced into the cooling tower as part of the caustic outlet stream.

15. The method according to claim 1, characterized in that the metallic salt comprises at least one of the following: sodium hydrogen sulfide, sodium bicarbonate, potassium carbonate, or ammonium bicarbonate.

16. The method according to claim 1, characterized in that the oxygenated compound comprises at least one of acetic acid, acullic acid, maleic acid or maleic anhydride.

17. The method according to claim 1, characterized in that the derived salt comprises at least one of sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate or ammonium malonate.

18. The method according to claim 1, characterized in that it further comprises producing the caustic outlet stream by at least one process selected from an oxidative dehydrogenation process, a cracking process, a refining process, a papermaking process, a soapmaking process, a detergentmaking process, or a food manufacturing process.

19. The method according to claim 1, characterized in that the stream further comprises an alkene comprising ethylene, propylene or a mixture thereof.

20. The method according to claim 19, characterized in that it further comprises producing olefin derivatives from the alkene.

21. The method according to claim 20, characterized in that the olefin derivative comprises at least one of a polyethylene, a polypropylene, an ethylene oxide, a propylene oxide, a polyethylene oxide, a polypropylene oxide, a thermoplastic elastomer or a thermoplastic olefin.

22. The method according to claim 21, characterized in that the polyethylene comprises at least one of an ethylene homopolymer, an ethylene and aolefin copolymer, a high-density polyethylene (HDPE), a medium-density polyethylene (MDPE), a low-density polyethylene (LDPE), a linear low-density polyethylene (LLDPE), or a very low-density polyethylene (VLDPE).

23. An apparatus for separating an oxygenated compound from a stream, characterized in that it comprises a cooling tower comprising: a cooling inlet for receiving the stream comprising the oxygenated compound; a cooling outlet for removing a cooling outlet stream; a metal salt inlet for introducing a caustic outlet stream comprising a metal salt; and an oxygenated compound outlet for removing an oxygenated compound outlet stream; and wherein the oxygenated compound can come into contact with the metal salt in the cooling tower to convert a portion of the oxygenated compound into a derivative salt, a substantial portion of which is removed together with a substantial portion of the unconverted oxygenated compound as a component of the oxygenated compound outlet stream.

24. The apparatus according to claim 23, characterized in that it further comprises a separation vessel comprising: a separation inlet in fluid communication with the oxygenated compound outlet and configured to receive the oxygenated compound outlet stream; a derivative salt outlet removing a derivative salt outlet stream comprising a derivative salt; and a separation outlet configured to remove a separation outlet stream comprising a substantial portion of the unconverted oxygenated compound present in the oxygenated compound outlet stream.

25. The apparatus according to claim 24, characterized in that the separation vessel further comprises a recycling line in fluid communication with the outlet of the diverted salt to receive the outlet stream of the diverted salt and to direct at least a portion of the outlet stream of the diverted salt to the separation inlet of the separation vessel.

26. The apparatus according to claim 24, characterized in that the separation vessel further comprises a supplementary salt inlet suitable for transporting ethyl acetate to the separation vessel.

27. The apparatus according to claim 23, characterized in that the stream further comprises at least one of a carbon-based oxide, a sulfide, water, an unreacted alkane, an alkene, or oxygen.

28. The apparatus according to claim 27, characterized in that the carbon-based oxide comprises at least one of either carbon monoxide or carbon dioxide.

29. The apparatus according to claim 27, characterized in that the carbon-based oxide comprises carbon dioxide and further comprises an amine scrubbing tower comprising an amine inlet and an amine outlet, the amine inlet being in fluid communication with the cooling outlet to receive the cooling outlet stream, and the amine scrubbing tower being suitable for removing at least a portion of the carbon-based oxide from the cooling outlet stream.

30. The apparatus according to claim 27, characterized in that it further comprises an oxygen eliminator comprising an eliminator inlet and an eliminator outlet, the oxygen eliminator being suitable for removing oxygen from the stream and the eliminator outlet being in fluid communication with the cooling inlet of the cooling tower for directing the stream into the cooling inlet.

31. The apparatus according to claim 23, characterized in that the cooling tower is suitable for / uu jo io 112 a pH in a range of a pKa of the oxygenated compound to a pKa of the metallic salt.

32. The apparatus according to claim 31, characterized in that the oxygenated compound comprises acetic acid having a pKa of 4.7 and the metallic salt comprises sodium bicarbonate having a pKa of 10.

3.

33. The apparatus according to claim 23, characterized in that the cooling tower comprises a primary stage and a secondary stage, wherein: the primary stage comprises the cooling inlet, a first intermediate outlet and a second intermediate outlet, the first intermediate outlet being in fluid communication with an intermediate inlet of the secondary stage, the second intermediate outlet being adapted to remove a second outlet stream of oxygenated compound, and the second stage comprising the cooling outlet, the metal salt inlet and the oxygenated compound outlet, wherein the primary stage is configured to remove a substantial portion of the oxygenated compound in the stream before introducing the stream into the second stage.

34. The apparatus according to claim 23, characterized in that it further comprises: a caustic washing tower comprising a washing inlet, a washing outlet, a caustic agent inlet and a caustic agent outlet, the washing inlet being in fluid communication with the cooling outlet to receive the cooling outlet stream, the caustic agent outlet configured to remove the caustic outlet stream, the caustic agent inlet configured to introduce at least one of sodium hydroxide, potassium hydroxide or ammonium hydroxide into the caustic washing tower; and a return line in fluid communication with the caustic agent outlet to receive the caustic outlet stream and discharge the caustic outlet stream to the metallic salt inlet of the cooling tower.

35. The apparatus according to claim 23, characterized in that the metallic salt comprises at least one of the following: sodium hydrogen sulfide, sodium bicarbonate, potassium carbonate, or ammonium bicarbonate.

36. The apparatus according to claim 23, characterized in that the oxygenated compound comprises at least one of the following: acetic acid, acrylic acid, maleic acid, or maleic anhydride.

37. The apparatus according to claim 23, characterized in that the derived salt comprises at least one of sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate or ammonium malonate.

38. The apparatus according to claim 23, / uu jo io 114 characterized in that the caustic outlet stream is produced by at least one process selected from an oxidative dehydrogenation process, a cracking process, a refining process, a papermaking process, a soapmaking process, a detergentmaking process, or a food manufacturing process.

39. The apparatus according to claim 23, characterized in that the stream further comprises an alkene comprising ethylene, propylene or a mixture thereof.

40. The apparatus according to claim 39, characterized in that it further comprises a polymerization reactor suitable for preparing an olefin derivative from the alkene.

41. The apparatus according to claim 40, characterized in that the olefin derivative comprises at least one of a polyethylene, a polypropylene, an ethylene oxide, a propylene oxide, a polyethylene oxide, a polypropylene oxide, a thermoplastic elastomer or a thermoplastic olefin.

42. The apparatus according to claim 41, characterized in that the polyethylene comprises at least one of an ethylene homopolymer, an ethylene copolymer and an aolefin, a high-density polyethylene (HDPE), a medium-density polyethylene (MDPE), a low-density polyethylene (LDPE), a linear low-density polyethylene (LLDPE) or a very low-density polyethylene (VLDPE).

43. A system for separating an oxygenated compound from a stream, characterized in that it comprises a cooling tower configured: to receive the stream comprising the oxygenated compound and a caustic outlet stream comprising a metallic salt, and to contact the oxygenated compound with the metallic salt to convert a portion of the oxygenated compound into a derivative salt; to cool the derivative salt and the unconverted oxygenated compound; to produce a cooling outlet stream comprising the stream with a substantial portion of the oxygenated compound removed; and to produce an oxygenated compound outlet stream comprising at least a substantial portion of the unconverted oxygenated compound and at least a substantial portion of the derivative salt.

44. The system according to claim 43, characterized in that it further comprises a separation vessel configured: to receive the outlet stream of the oxygenated compound; to separate the unconverted oxygenated compound from the derived salt within the first outlet stream of the oxygenated compound; to produce a second outlet stream of oxygenated compound comprising a substantial portion of the unconverted oxygenated compound from the outlet stream of the oxygenated compound; and a separation outlet stream comprising a substantial portion of the derived salt from the outlet stream of the oxygenated compound.

45. The system according to claim 44, characterized in that the separation vessel further comprises a recycling line configured to recycle a portion of the outlet stream from the separation to the separation vessel.

46. ​​The system according to claim 44, characterized in that the separation vessel is further configured to receive ethyl acetate.

47. The system according to claim 43, characterized in that the stream further comprises at least one of a carbon-based oxide, a sulfide, an unreacted alkane, an alkene, or oxygen.

48. The system according to claim 47, characterized in that the carbon-based oxide comprises at least one of either carbon monoxide or carbon dioxide.

49. The system according to claim 47, characterized in that the carbon-based oxide comprises carbon dioxide and further comprises an amine scrubbing tower configured: to receive the cooling outlet stream; and to remove at least a portion of the carbon-based oxide from the cooling outlet stream.

50. The system according to claim 47, characterized in that it further comprises an oxygen eliminator configured to remove oxygen from the stream and direct the stream towards the cooling tower.

51. The system of claim 43, characterized in that the cooling tower is configured to maintain a pH in a range of a pKa of the oxygenated compound to a pKa of the metallic salt.

52. The system according to claim 43, characterized in that the cooling tower is configured to maintain a pH in a range of 2 to 12.

53. The system according to claim 43, characterized in that the cooling tower comprises two stages, the first stage configured to remove a substantial portion of the oxygenated compound from the stream and the second stage configured to receive the stream with a substantial portion of the oxygenated compound removed.

54. The system according to claim 43, characterized in that it further comprises a caustic scrubbing tower configured: to receive the cooling outlet stream; to receive a caustic agent selected from at least one of sodium hydroxide, potassium hydroxide, or ammonium hydroxide; to contact a substantial portion of the carbon-based oxide from the cooling outlet stream with the caustic agent to form a metallic salt; and to produce the caustic outlet stream; and a return line configured to direct the caustic outlet stream from the caustic scrubbing tower to the cooling tower.

55. The system according to claim 43, characterized in that the metallic salt comprises at least one of the following: sodium hydrogen sulfide, sodium bicarbonate, potassium carbonate, or ammonium bicarbonate.

56. The system according to claim 43, characterized in that the oxygenated compound comprises at least one of the following: acetic acid, acrylic acid, maleic acid, or maleic anhydride.

57. The system according to claim 43, characterized in that the derived salt comprises at least one of sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate, or ammonium malonate. / uu jo io 119 58. The system according to claim 43, characterized in that the caustic outlet stream is produced by at least one process selected from an oxidative dehydrogenation process, a cracking process, a refining process, a papermaking process, a soapmaking process, a detergentmaking process, or a food manufacturing process.

59. The system according to claim 43, characterized in that the stream further comprises an alkene comprising ethylene, propylene or a mixture thereof.

60. The system according to claim 59, characterized in that it further comprises a polymerization reactor configured to produce an olefin derivative from the alkene.

61. The system according to claim 60, characterized in that the olefin derivative comprises at least one of a polyethylene, a polypropylene, an ethylene oxide, a propylene oxide, a polyethylene oxide, a polypropylene oxide, a thermoplastic elastomer, or a thermoplastic olefin.

62. The system according to claim 61, characterized in that the polyethylene comprises at least one of an ethylene homopolymer, an ethylene copolymer and an aolefin, a high-density polyethylene (HDPE), a medium-density polyethylene (MDPE), a low-density polyethylene (LDPE), a linear low-density polyethylene (LLDPE), or a very low-density polyethylene (VLDPE).

63. A method for converting a lower alkane into an alkene, characterized in that it comprises: introducing an inlet stream comprising oxygen and the lower alkane into an oxidative dehydrogenation (ODD) reactor; converting at least a portion of the lower alkane into the alkene in the ODD reactor and producing an ODD outlet stream comprising the alkene, the unconverted lower alkane, an oxygenated compound, and a carbon-based oxide; introducing the ODD outlet stream and a caustic outlet stream comprising a metallic salt into a cooling tower; contacting the oxygenated compound with the metallic salt within the cooling tower to convert a portion of the oxygenated compound into a derived salt; and cooling a substantial portion of the unconverted oxygenated compound and a substantial portion of the derived salt.removing a cooling outlet stream comprising the alkene, the unconverted lower alkane, and the carbon-based oxide from the cooling tower; and removing an oxygenated compound outlet stream comprising the cooled derived salt and the cooled unconverted oxygenated compound from the cooling tower.

64. The method according to claim 63, characterized in that it further comprises: introducing the cooling outlet stream into a caustic scrubbing tower comprising a caustic agent; contacting the carbon-based oxide of the cooling outlet stream with the caustic agent in the caustic scrubbing tower to form a metallic salt; removing a caustic outlet stream comprising the metallic salt from the caustic scrubbing tower; and introducing the caustic outlet stream to the cooling tower with the DHO outlet stream.

65. The method according to claim 63, characterized in that it further comprises: introducing the oxygenated compound outlet stream into a separation vessel; separating the unconverted oxygenated compound from the derived salt to produce a second oxygenated compound outlet stream comprising a substantial portion of the unconverted oxygenated compound from the oxygenated compound outlet stream and a separation outlet stream comprising a substantial portion of the derived salt from the oxygenated compound outlet stream.

66. The method according to claim 65, / uu jo io 122 characterized in that it further comprises recycling a portion of the separation outlet stream comprising the salt diverted to the separation vessel.

67. The method according to claim 65, characterized in that it further comprises introducing ethyl acetate into the separation vessel.

68. The method according to claim 64, characterized in that the carbon-based oxide comprises carbon dioxide and further comprises introducing the cooling outlet stream into an amine scrubbing tower and removing a substantial portion of the carbon-based oxide from the cooling outlet stream before introducing the cooling outlet stream into the caustic scrubbing tower.

69. The method according to claim 63, characterized in that the DHO outlet stream further comprises at least one of a sulfide, water, or oxygen.

70. The method according to claim 68, characterized in that it further comprises introducing the DHO outlet stream into an oxygen eliminator and removing the oxygen from the DHO outlet stream in the oxygen eliminator before introducing the DHO outlet stream into the cooling tower.

71. The method according to claim 63, characterized in that it further comprises maintaining a pH of the CLornn / Lznz / E / Yi 123 cooling tower in a range of a pKa of the oxygenated compound to a pKa of the metallic salt.

72. The method according to claim 70, characterized in that the oxygenated compound comprises acetic acid having a pKa of 4.7 and the metal salt comprises sodium bicarbonate having a pKa of 10.

3.

73. The method according to claim 63, characterized in that it further comprises removing a substantial portion of the oxygenated compound within the DHO outlet stream before introducing the DHO outlet stream into the cooling tower.

74. The method according to claim 64, characterized in that the caustic agent comprises at least one of sodium hydroxide, potassium hydroxide or ammonium hydroxide.

75. The method according to claim 63, characterized in that the metallic salt comprises at least one of the following: sodium bicarbonate, potassium carbonate, or ammonium bicarbonate.

76. The method according to claim 63, characterized in that the carbon-based oxide comprises at least one of either carbon monoxide or carbon dioxide.

77. The method according to claim 63, characterized in that the oxygenated compound comprises at least one of the following: acetic acid, acrylic acid, maleic acid or maleic anhydride.

78. The method according to claim 63, characterized in that the derived salt comprises at least one of sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate or ammonium malonate.

79. The method according to claim 63, characterized in that the lower alkane comprises ethane and the alkene comprises ethylene.

80. The method according to claim 63, characterized in that the lower alkane comprises propane and the alkene comprises propylene.

81. The method according to claim 63, characterized in that it further comprises producing olefin derivatives from the alkene.

82. The method according to claim 80, characterized in that the olefin derivatives comprise at least one of a polyethylene, a polypropylene, an ethylene oxide, a propylene oxide, a polyethylene oxide, a polypropylene oxide, a thermoplastic elastomer, or a thermoplastic olefin.

83. The method according to claim 81, characterized in that the polyethylene comprises at least one of an ethylene homopolymer, an ethylene copolymer and an α-olefin, a high-density polyethylene (HDPE), a medium-density polyethylene (MDPE), a low-density polyethylene (LDPE), a linear low-density polyethylene (LLDPE), and very low-density polyethylene (VLDPE).

84. An apparatus for the oxidative dehydrogenation (DHO) of a lower alkane to an alkene, characterized in that it comprises: a DHO reactor comprising a DHO inlet and a DHO outlet, the DHO inlet configured to receive an inlet stream of DHO comprising the lower alkane into the DHO reactor, the DHO outlet suitable for removing an outlet stream of DHO comprising the alkene, an unconverted lower alkane, an oxygenated compound, and a carbon-based oxide from the DHO reactor;a cooling tower comprising a cooling inlet, a cooling outlet, a metal salt inlet, and an oxygenated compound outlet, the cooling inlet being fluidly connected with the DHO outlet to receive the DHO outlet stream, the cooling outlet configured to remove a cooling outlet stream comprising at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide from the cooling tower, the metal salt inlet configured to receive a caustic outlet stream comprising a metal salt, the oxygenated compound outlet being suitable for removing an oxygenated compound outlet stream comprising at least a substantial portion of the oxygenated compound and a derived salt;A caustic scrubbing tower comprising a scrubbing inlet, a scrubbing outlet, a caustic inlet, and a caustic outlet; the scrubbing inlet being fluidly connected with the cooling outlet to receive the cooling outlet stream; the caustic outlet being suitable for conveying a caustic outlet stream comprising a metallic salt; and a return line being fluidly connected with the caustic outlet to receive the caustic outlet stream and convey the caustic outlet stream to the metallic salt inlet of the cooling tower.

85. The apparatus according to claim 84, characterized in that it further comprises a separation vessel comprising a separation inlet, a derived salt outlet and a separation outlet, the separation inlet being fluidly connected with the oxygenated compound outlet to receive the oxygenated compound outlet stream, the derived salt outlet being suitable for conveying a separation outlet stream comprising a derived salt, and the separation outlet being suitable for conveying a second oxygenated compound outlet stream comprising a substantial portion of the oxygenated compound.

86. The apparatus according to claim 85, / uu jo io 127 characterized in that the separation vessel further comprises a recycling line in fluid communication with the outlet of the diverted salt to receive the separation outlet stream and to deliver at least a portion of the separation outlet stream to the separation inlet of the separation vessel.

87. The apparatus according to claim 85, characterized in that the separation vessel further comprises a supplementary salt inlet suitable for introducing ethyl acetate into the separation vessel.

88. The apparatus according to claim 84, characterized in that it further comprises an amine washing tower comprising an amine inlet and an amine outlet, the amine inlet being in fluid communication with the cooling outlet to receive the cooling outlet stream, the amine washing tower being suitable for removing at least a portion of the carbon-based oxide from the cooling outlet stream, and the amine outlet being in fluid communication with the washing inlet of the caustic washing tower to deliver the cooling outlet stream to the washing inlet.

89. The apparatus according to claim 84, characterized in that the DHO outlet stream further comprises at least one of a sulfide, water, an unreacted alkane, or oxygen. / uuoo io 128 90. The apparatus according to claim 89, characterized in that it further comprises an oxygen eliminator comprising an eliminator inlet and an eliminator outlet, the eliminator inlet being fluidly connected with the DHO outlet to receive the DHO outlet stream, the oxygen eliminator being suitable for removing oxygen from the DHO outlet stream, and the eliminator outlet being fluidly connected with the cooling tower inlet to draw the DHO outlet stream to the cooling inlet.

91. The apparatus according to claim 84, characterized in that the cooling tower is suitable for a pH in a range of a pKa of the oxygenated compound to a pKa of the metallic salt.

92. The apparatus according to claim 91, characterized in that the oxygenated compound comprises acetic acid having a pKa of 4.7 and the metal salt comprises sodium bicarbonate having a pKa of 10.

3.

93. The apparatus according to claim 84, characterized in that the cooling tower further comprises a primary stage and a secondary stage, the primary stage comprising the cooling inlet, a first intermediate outlet and a second intermediate outlet, the first intermediate outlet being in fluid communication with an intermediate inlet of the secondary stage, the second intermediate outlet being suitable for removing an outlet stream of condensed oxygenated compound, and the second stage comprising the cooling outlet, the metal salt inlet and the oxygenated compound outlet.

94. The apparatus according to claim 84, characterized in that the caustic agent inlet is suitable for conveying at least one of sodium hydroxide, potassium hydroxide or ammonium hydroxide to the caustic washing tower.

95. The apparatus according to claim 84, characterized in that the metallic salt comprises at least one of the following: sodium bicarbonate, potassium carbonate, or ammonium bicarbonate.

96. The apparatus according to claim 84, characterized in that the carbon-based oxide comprises carbon monoxide, carbon dioxide, or a combination thereof.

97. The apparatus according to claim 84, characterized in that the oxygenated compound comprises at least one of the following: acetic acid, acrylic acid, maleic acid, or maleic anhydride.

98. The apparatus according to claim 84, characterized in that the derived salt comprises at least one of sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate or ammonium malonate.

99. The apparatus according to claim 84, characterized in that the lower alkane comprises ethane and the alkene comprises ethylene.

100. The apparatus according to claim 84, characterized in that the lower alkane comprises propane and the alkene comprises propylene.

101. The apparatus according to claim 84, characterized in that it further comprises a polymerization reactor suitable for preparing a derivative of the alkene.

102. The apparatus according to claim 100, characterized in that the olefin derivative comprises at least one of a polyethylene, a polypropylene, an ethylene oxide, a propylene oxide, a polyethylene oxide, a polypropylene oxide, a thermoplastic elastomer or a thermoplastic olefin.

103. The apparatus according to claim 101, characterized in that the polyethylene comprises at least one of an ethylene homopolymer, an ethylene copolymer and an aolefin, a high-density polyethylene (HDPE), a medium-density polyethylene (MDPE), a low-density polyethylene (LDPE), a linear low-density polyethylene (LLDPE), or a very low-density polyethylene (VLDPE). 131 104. A system for the oxidative dehydrogenation (DHO) of a lower alkane, characterized in that it comprises: a DHO reactor configured to receive an inlet stream comprising oxygen and the lower alkane, the DHO reactor configured to produce an outlet stream of DHO comprising an alkene, an oxygenated compound and a carbon-based oxide;a cooling tower configured to receive the DHO outlet stream and a caustic outlet stream comprising a metallic salt, contacting the oxygenated compound with the metallic salt to convert a portion of the oxygenated compound into a derived salt, cooling the DHO outlet stream and substantially removing the unconverted oxygenated compound and the derived salt from the DHO outlet stream, the cooling tower being configured to produce a cooling outlet stream comprising at least a substantial portion of the alkene and at least a substantial portion of the carbon-based oxide, and an oxygenated compound outlet stream comprising at least a substantial portion of the unconverted oxygenated compound and at least a substantial portion of the derived salt;a caustic scrubbing tower configured to receive the cooling outlet stream and contact a substantial portion of the carbon-based oxide from the cooling outlet stream with a caustic agent to form a caustic outlet stream comprising a metallic salt; and a return line configured to direct the caustic outlet stream to the cooling tower and contact the caustic outlet stream with the DHO outlet stream to form the salt derived from the metallic salt and the oxygenated compound, wherein the oxygenated compound outlet stream comprises a substantial portion of the derived salt.

105. The system according to claim 104, characterized in that it further comprises a separation vessel configured to receive the oxygenated compound outlet stream and separate the oxygenated compound from the derived salt within the oxygenated compound outlet stream to produce a second oxygenated compound outlet stream comprising a substantial portion of the oxygenated compound from the oxygenated compound outlet stream and a separation outlet stream comprising a substantial portion of the derived salt from the first oxygenated compound stream.

106. The system according to claim 105, characterized in that the separation vessel further comprises a recycling line configured to recycle a portion of the salt derived from the outlet stream of the separation vessel to the separation vessel.

107. The system according to claim 105, characterized in that the separation vessel is configured to receive ethyl acetate.

108. The system according to claim 103, characterized in that it further comprises an amine washing tower configured to receive the cooling outlet stream, the amine washing tower being suitable for removing at least a portion of the carbon-based oxide from the cooling outlet stream and suitable for conveying the cooling outlet stream to the caustic washing tower.

109. The system according to claim 104, characterized in that the DHO outlet stream further comprises at least one of the following: a sulfide, water, an unreacted alkane, or oxygen.

110. The system according to claim 109, characterized in that it further comprises an oxygen eliminator configured to remove oxygen from the DHO outlet stream and suitable for supplying the DHO outlet stream to the cooling tower.

111. The system according to claim 104, characterized in that the cooling tower is configured to maintain a pH within a range of a pKa of the oxygenated compound to a pKa of the metallic salt. / uuoo io 134 112. The system according to claim 104, characterized in that the cooling tower is configured to maintain a pH in a range of 2 to 12.

113. The system according to claim 104, characterized in that the cooling tower includes a primary stage and a second stage, the primary stage being configured to remove a substantial portion of the oxygenated compound from the DHO outlet stream before directing the DHO outlet stream to the second stage, the second stage being configured to contact the DHO outlet stream with the caustic outlet stream to form a salt derived from the metallic salt and the oxygenated compound.

114. The system according to claim 104, characterized in that the caustic agent comprises at least one of sodium hydroxide, potassium hydroxide or ammonium hydroxide for the caustic scrubbing tower.

115. The system according to claim 104, characterized in that the metallic salt comprises at least one of the following: sodium bicarbonate, potassium carbonate, or ammonium bicarbonate.

116. The system according to claim 104, characterized in that the carbon-based oxide comprises at least one of either carbon monoxide or carbon dioxide.

117. The system according to claim 104, characterized in that the oxygenated compound comprises at least one of the following: acetic acid, acrylic acid, maleic acid or maleic anhydride.

118. The system according to claim 104, characterized in that the derived salt comprises at least one of sodium acetate, potassium acetate, ammonium acetate, sodium acrylate, potassium acrylate, ammonium acrylate, sodium malonate, potassium malonate or ammonium malonate.

119. The system according to claim 104, characterized in that the lower alkane comprises ethane and the alkene comprises ethylene.

120. The system according to claim 104, characterized in that the lower alkane comprises propane and the alkene comprises propylene.

121. The system according to claim 104, characterized in that it further comprises a polymerization reactor configured to produce an olefin derivative from the alkene.

122. The system according to claim 121, characterized in that the olefin derivative comprises at least one of a polyethylene, a polypropylene, an ethylene oxide, a propylene oxide, a polyethylene oxide, a polypropylene oxide, a thermoplastic elastomer, or a thermoplastic olefin.

123. The system according to claim 122, characterized in that the polyethylene comprises at least one of the following: 136 an ethylene homopolymer, an ethylene copolymer and an aolefin, a high-density polyethylene (HDPE), a medium-density polyethylene (MDPE), a low-density polyethylene (LDPE), a linear low-density polyethylene (LLDPE), and a very low-density polyethylene (VLDPE).