Patent Application
20150183649
Large-scale use of corrosive materials such as acids can be an essential part of many industrial procedures. Corrosion can lead to significant decreases in the useful lifespan of equipment in many technical areas. In some examples, the shortening of lifespan can be so severe that equipment repairs or replacement can form a major portion of long-term operational costs. One example of corrosive materials used in large-scale procedures is the use of aqueous acids to extract ammonia.
The Andrussow process generates hydrocyanic acid (HCN) from methane and ammonia in the presence of oxygen and a platinum catalyst. It is economical to operate the Andrussow HCN with recovery and recycle of unreacted ammonia, using an aqueous acid sorption loop to absorb ammonia from the reactor effluent stream. The acid can be a mineral acid such as phosphoric acid, which can extract ammonia gas by capturing it as an ammonium salt such as ammonium phosphate in an absorber. The ammonia can be liberated from the aqueous solution by heating in a stripper. Equipment that makes contact with the acid, including the absorber, stripper, and associated transfer piping, can experience high rates of corrosion. The elevated temperatures that occur in certain areas of the equipment, such as in the stripper and the associated reboiler, can exacerbate the corrosive effect.
Use of a corrosion-resistant material can reduce the rate of corrosion of the equipment. Examples of corrosion-resistant materials can include superalloys, such as nickel-copper alloys containing small amounts of iron and trace amounts of other elements such as Monel® 400, precipitation-strengthened nickel-iron-chromium alloys such as the such as Incoloy® brand alloys, for example Incoloy® 800 series, or austenitic nickel-chromium-based Inconel® brand alloys, or nickel-chromium-molybdenum alloys such as Hastelloy® brand alloys, for example, Hastelloy® G-30®, or zirconium such as Zr 702, or super duplex stainless steel, for example 2507 or 2205. However, the cost of equipment made with corrosion-resistant materials can significantly exceed the cost of equipment fabricated using more affordable and conventional materials such as austenitic stainless steels, such as 316L.
Certain corrosion accelerators can accumulate in the dilute phosphoric acid charged to the ammonia absorber in an ammonia extraction process. The present invention provides a method of decreasing corrosion during ammonia extraction. The method includes performing a process to extract ammonia using ammonia extraction equipment. The ammonia extraction equipment includes an ammonia absorber, an ammonia desorber, and an aqueous solution. The aqueous solution includes an acid or an ammonium salt thereof. The method also includes purging at least part of the aqueous solution. The purged part of the aqueous solution includes at least one corrosion-promoting ion. The method also includes adding a replacement aqueous solution to the aqueous solution. The replacement aqueous solution has a reduced concentration of the at least one corrosion-promoting ion as compared to the purged part of the aqueous solution.
Embodiments of the present invention can provide certain advantages over other methods of corrosion reduction. Embodiments of the present invention can provide an ammonia extraction process that can use equipment fabricated from an affordable material, such as an austenitic stainless steel, such as for example 316L, as a safe, reliable, and long-lasting material of construction. The purging and replacing steps of the present invention can be less costly and more efficient than the use of expensive and exotic corrosion-resistant materials. In addition, embodiment of the present invention can provide an ammonia extraction process that can use a corrosion-resistant material that experiences less corrosion than similar ammonia extraction processes that do not include the purging and replacing steps described herein. Embodiments of the present invention can advantageously help to avoid the clogging of ammonia recovery systems with formate salts, for example, ammonium formate, or other salts such as, for example, ammonium carbonate, ammonium phosphate, or ammonium oxalate.
The present invention provides a system for extracting ammonia. The system includes ammonia extraction equipment. The ammonia extraction equipment includes an ammonia absorber, an ammonia desorber, and an aqueous solution. The aqueous solution includes an acid or an ammonium salt thereof. The system includes a gaseous stream. The gaseous stream includes ammonia. In the ammonia absorber at least part of the ammonia in the gaseous stream is converted into an ammonium salt. In the ammonia desorber at least part of the ammonium salt is converted into ammonia. The aqueous solution is circulated between the absorber and the desorber. The system also includes a purge stream. The purge stream flows out of the circulated aqueous solution. The purge stream includes at least part of the aqueous solution. The purged part includes at least one corrosion-promoting ion. The corrosion-promoting ion can include formate, oxalate, fluoride, chloride, sulfate, and sulfide. The system also includes a replacement stream. The replacement stream flows into the circulated aqueous solution. The replacement stream has a reduced concentration of the at least one corrosion-promoting ion as compared to the purged part of the aqueous solution.
The present invention provides a method of decreasing corrosion during ammonia extraction. The method includes performing a process to recover unreacted ammonia from a gaseous reactor effluent stream. The gaseous reaction effluent stream is from an Andrussow process. The Andrussow process generates hydrogen cyanide. The ammonia extraction process is performed using ammonia recovery equipment. The ammonia recovery equipment includes an ammonia absorber. The ammonia recovery equipment also includes an ammonia desorber that includes an ammonia stripper tower and an ammonia stripper tower reboiler. The ammonia recovery equipment also includes an aqueous solution. The aqueous solution includes an acid or an ammonium salt thereof. In the ammonia absorber at least part of the ammonia in the gaseous stream is converted into an ammonium salt. In the ammonia desorber at least part of the ammonium salt is converted into ammonia. The aqueous solution is circulated between the absorber and the desorber. The method includes purging at least part of the aqueous solution. The purged part of the aqueous solution includes at least one corrosion-promoting ion. The corrosion-promoting ion can include formate, oxalate, fluoride, chloride, sulfate, and sulfide. The method also includes adding a replacement aqueous solution to the aqueous solution. The replacement aqueous solution has a reduced concentration of the at least one corrosion-promoting ion as compared to the purged part of the aqueous solution. The purging and replacing maintain a concentration of the formate ion below about 15 wt %.
In the drawings, which are not necessarily drawn to scale, like numerals describe substantially similar components throughout the several views. Like numerals having different letter suffixes represent different instances of substantially similar components. The drawings illustrate generally, by way of example, but not by way of limitation, various embodiments discussed in the present document.
Reference will now be made in detail to certain claims of the disclosed subject matter, examples of which are illustrated in the accompanying drawings. While the disclosed subject matter will be described in conjunction with the enumerated claims, it will be understood that they are not intended to limit the disclosed subject matter to those claims. On the contrary, the disclosed subject matter is intended to cover all alternatives, modifications, and equivalents, which can be included within the scope of the presently disclosed subject matter as defined by the claims.
References in the specification to “one embodiment,” “an embodiment,” “an example embodiment,” etc., indicate that the embodiment described can include a particular feature, structure, or characteristic, but every embodiment may not necessarily include the particular feature, structure, or characteristic. Moreover, such phrases are not necessarily referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with an embodiment, it is submitted that it is within the knowledge of one skilled in the art to affect such feature, structure, or characteristic in connection with other embodiments whether or not explicitly described.
Values expressed in a range format should be interpreted in a flexible manner to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a concentration range of “about 0.1% to about 5%” should be interpreted to include not only the explicitly recited concentration of about 0.1 wt % to about 5 wt %, but also the individual concentrations (e.g., 1%, 2%, 3%, and 4%) and the sub-ranges (e.g., 0.1% to 0.5%, 1.1% to 2.2%, 3.3% to 4.4%) within the indicated range.
In this document, the terms “a,” “an,” or “the” are used to include one or more than one unless the context clearly dictates otherwise. The term “or” is used to refer to a nonexclusive “or” unless otherwise indicated. In addition, it is to be understood that the phraseology or terminology employed herein, and not otherwise defined, is for the purpose of description only and not of limitation. Any use of section headings is intended to aid reading of the document and is not to be interpreted as limiting; information that is relevant to a section heading may occur within or outside of that particular section. Furthermore, all publications, patents, and patent documents referred to in this document are incorporated by reference herein in their entirety, as though individually incorporated by reference. In the event of inconsistent usages between this document and those documents so incorporated by reference, the usage in the incorporated reference should be considered supplementary to that of this document; for irreconcilable inconsistencies, the usage in this document controls.
In the methods of manufacturing described herein, the steps can be carried out in any order without departing from the principles of the invention, except when a temporal or operational sequence is explicitly recited.
Furthermore, specified steps can be carried out concurrently unless explicit claim language recites that they be carried out separately. For example, a claimed step of doing X and a claimed step of doing Y can be conducted simultaneously within a single operation, and the resulting process will fall within the literal scope of the claimed process.
The term “about” can allow for a degree of variability in a value or range, for example, within 10%, within 5%, or within 1% of a stated value or of a stated limit of a range. When a range or a list of sequential values is given, unless otherwise specified any value within the range or any value between the given sequential values is also disclosed.
As used herein, “substantially” refers to a majority of, or mostly, as in at least about 50%, 60%, 70%, 80%, 90%, 95%, 96%, 97%, 98%, 99%, 99.5%, 99.9%, 99.99%, or at least about 99.999%.
The term “scf” as used herein refers to standard cubic feet. “Scfh” refers to standard cubic feet per hour.
The term “air” as used herein refers to a mixture of gases with a composition approximately identical to the native composition of gases taken from the atmosphere, generally at ground level. In some examples, air is taken from the ambient surroundings. Air has a composition that includes approximately 78% nitrogen, 21% oxygen, 1% argon, and 0.04% carbon dioxide, as well as small amounts of other gases.
The term “room temperature” as used herein refers to ambient temperature, which can be, for example, between about 15° C. and about 28° C.
The term “gas” as used herein includes a vapor.
The term “absorb” or “absorption” as used herein refers to dissolution of a gas in a liquid or conversion of a gas to a soluble or insoluble salt in a liquid.
The term “desorb” or “desorption” as used herein refers to the conversion of gas that is dissolved in a liquid to gas that is no longer dissolved in the liquid, or to the conversion in a liquid of a soluble or insoluble salt of the compound to be desorbed into the desorbed compound. In one example, the soluble or insoluble salt is an ammonium salt, and the compound to be desorbed is ammonia.
The term “absorber” as used herein refers to one or more pieces of equipment that absorb or extract one or more compounds from a gas, vapor, or liquid, into a liquid. The absorbed or extracted compound or compounds can be dissolved in the absorbing liquid, or can be in the form of another compound in the absorbing liquid, such as a soluble or insoluble salt of the compound that is absorbed. In one example, the soluble or insoluble salt is an ammonium salt, and the compound to be absorbed is ammonia.
The term “desorber” as used herein refers to one or more pieces of equipment that desorb one or more compounds from a liquid, such as that desorb one or more gases from a liquid. The one or more compounds can be dissolved in the liquid, or can be absorbed in the liquid in the form of a soluble or insoluble salt of the compound to be desorbed. In one example, the soluble or insoluble salt is an ammonium salt, and the compound to be desorbed is ammonia. Heat can be used to desorb the one or more compounds from the liquid. Pressure differences or added compounds can be used to desorb the one or more compounds from the liquid. Any suitable method or combination of methods can be used to desorb the one or more compounds from the liquid.
The term “reboiler” as used herein refers to a heat transfer unit used for heating a liquid. A reboiler can be present near the bottom of a tower, and supplies heat to the contents of the tower, such that the tower can be used for separation purposes, such as stripping (e.g. desorption) or distillation.
The term “transfer piping” as used herein refers to materials and equipment, such as pipes, pumps, and other equipment, which contact an aqueous liquid or vapor as it is transferred from one piece of equipment to another, such as between a reboiler and a stripper tower, between a stripper tower and an absorber tower, or between a stripper tower and a condenser.
The term “corrosion” as used herein refers to the disintegration of a material due to chemical reactions with its surroundings.
The term “sparge” as used herein refers to the injection of a gas into a liquid, such that the gas contacts the liquid.
The term “mil” as used herein refers to a thousandth of an inch, such that 1 mil=0.001 inch.
The present invention provides a method of decreasing corrosion during ammonia extraction. The present invention also provides a system that can perform the method. The present invention solves the technical problem of excessive corrosion during ammonia extraction by purging and replacing a portion of the aqueous solution used to extract the ammonia.
The ammonia extraction equipment can include any suitable ammonia extraction equipment. The ammonia extraction equipment can include an ammonia absorber, an ammonia desorber, and an aqueous solution. For example, the ammonia extraction equipment can include at least one of an ammonia sorption tower, ammonia sorption tower top, ammonia sorption tower bottom, ammonia stripper tower, ammonia stripper tower top, ammonia stripper tower bottom, stripper tower reboiler, ammonia condenser, distillation column, ammonia enricher, heat exchanger, and transfer piping for each piece of equipment present. The transfer piping can include, for example, pipes or equipment. The transfer piping can include any materials that contact the aqueous solution as it flows between various pieces of equipment. The ammonia extraction equipment can be industrially sized.
The ammonia extraction equipment extracts ammonia from a feed stream. The feed stream can be in any suitable form, such as a gas, vapor, liquid, or combination thereof. The feed stream can include water, or the feed stream can be substantially free of water. An ammonia feed stream with a particular composition can be in different forms depending on the temperature and pressure of the feed stream. For example, a high pressure or chilled feed stream can include materials in a liquid state, whereas the feed stream with a substantially identical composition under lower pressure or higher temperature can include materials in a gaseous state. The extraction equipment can extract any suitable number of components from the feed stream. The ammonia feed stream can have any suitable composition, and can contain any suitable amount of ammonia and other gases. For example, the ammonia feed stream can be about 1 wt %, 2, 5, 10, 20, 30, 40, 50, 60, 70, 80, 90, 95, 98, or about 99 wt % ammonia. The ammonia feed stream can include ammonia and hydrogen cyanide. For example, the ammonia feed stream can be about 1 wt %, 2, 5, 10, 20, 30, 40, 50, 60, 70, 80, 90, 95, 98, or about 99 wt % hydrogen cyanide.
The ammonia feed stream that is extracted by the ammonia extraction equipment can originate from any suitable source. For example, the ammonia feed stream can originate from a hydrogen cyanide production process, a fertilizer production process, a wastewater purification process, an ammonia production process, a pollution prevention process, a fossil fuel combustion process, a coke manufacture process, a livestock management process, or a refrigeration process. The ammonia feed stream can include unreacted ammonia from a hydrogen cyanide generation process. The ammonia extraction equipment can recover ammonia from an Andrussow process for generating hydrogen cyanide, wherein methane and ammonia are allowed to react with oxygen in the presence of a platinum group catalyst to give hydrogen cyanide and water.
The ammonia extraction equipment uses the aqueous solution to extract the ammonia. During the extraction, the aqueous solution contacts at least part of the inside of the equipment, and is circulated therein between an ammonia absorber and an ammonia desorber via transfer piping disposed therebetween. The ammonia is absorbed into the aqueous solution either as a dissolved gas or as an ammonium salt, and is then liberated from the aqueous solution in the desorber. The liberated ammonia can be condensed. The ammonia can be not condensed, or can be only partially condensed. The recovered ammonia can be reused in the chemical reaction or process from which it was recovered, such as in an Andrussow process for generation of HCN, it can be used in other reactions, or it can be sold as a valuable byproduct. Portions of the aqueous solution can be removed during the extraction. The removed solution can be treated and returned to the extraction equipment, or can be treated or separated to recover the one or more ammonium salts therein which can be optionally purified and can be sold as a valuable byproduct, such that an ammonium salt is recovered.
The ammonia absorber can be any suitable ammonia absorber. The ammonia absorber absorbs ammonia from the ammonia feed stream into the aqueous solution. The ammonia absorber can absorb any suitable amount of ammonia from the ammonia feed stream, e.g., about 1 wt %, 2, 5, 10, 20, 30, 40, 50, 60, 70, 80, 90, 95, 98, 99, 99.5, 99.9, 99.99, or about 100 wt % of the ammonia in the ammonia feed stream can be absorbed into the aqueous solution in the ammonia absorber. The ammonia feed stream that has undergone absorption in the ammonia absorber can continue to other equipment for further processing. The further processing can include recycling at least part of the unabsorbed ammonia back to the absorber. The further processing can include the extraction of other compounds, or can include suitable treatments for release into the atmosphere.
The ammonia is absorbed in the form of a dissolved gas, or in the form of an ammonium salt, e.g. ammonium phosphate ((NH4)3PO4), diammonium phosphate ((NH4)2HPO4), or monoammonium phosphate ((NH4)(H2PO4)). The salt is formed from ions present in the aqueous solution which may or may not be present in the form of a salt. The ammonia absorber contacts the ammonia feed stream with the aqueous solution to extract the ammonia into the aqueous solution. The contacting can occur in any suitable fashion. For example, the contacting can be counter-current contacting, wherein the ammonia feed stream and the aqueous solution move in opposite directions through the absorber, which can help to maximize contact therebetween. In some examples, the ammonia feed stream can enter the absorber near the bottom section, while the aqueous solution enters near the top section. The aqueous solution can be liquid, vapor, or a combination thereof. The ammonia feed stream can move toward the top of the absorber through the aqueous. The aqueous solution can move from the top section of the absorber to the bottom section of the absorber. The absorber can include functional architecture or packing material therein that increases contacting between the aqueous solution and the ammonia feed stream, which can help to maximize the amount of ammonia absorbed from the feed stream during its residence in the absorber. The absorber can be an absorption tower.
An ammonia absorber can be of any suitable design and generally operates countercurrently. Acid-risk sorbent liquid can enter the absorber tower near the top and flows downwardly. The absorber tower may contain internals to facilitate liquid-liquid contact. Examples of suitable internals are taught in Kirk-Othmer Encyclopaedia of Chemical Technology, 3rd Edition, vol. 1, pp. 53-96 (John Wiley & Sons, 1978), and include trays, plates, rings and saddles, merely to name a few. An ammonia-containing gas can enter the tower near the bottom and flow upwardly, contacting the sorbent liquid countercurrently if the liquid is introduced near the top of the column. Gas and liquid flows to the absorber column are regulated to provide for efficient contacting, while flooding the column (due to excessively high liquid charge), entraining liquid in the ammonia-enriched gas (due to excessive flow of gas) or low absorption performance caused by an inadequate flow of gas to the absorption column. The choices of column length, diameter, and type of internal(s) can be determined by one of ordinary skill in the art given the throughput and purity requirements for the ammonia recycle stream. Incentive for recycling ammonia can include the cost of disposing of the used ammonia stream or to minimize the possibility of venting the ammonia to atmosphere. The ammonia can be recycled to an Andrussow process.
The resulting HCN-containing effluent stream from the ammonia absorber can contain, for example, between about 0 wt % and about 3 wt % ammonia, or between about 3 wt % and about 5 wt % ammonia, or between about 5 wt % and about 20 wt % ammonia.
The aqueous solution that contains the absorbed ammonia then passes via transfer piping to the desorber. The aqueous solution, or portions of the aqueous solution, can undergo any suitable treatment prior to entering the desorber. In some examples, portions of the aqueous solution can be removed between the absorber and the desorber. The removed portions can be suitably treated and returned to the aqueous solution at a suitable location, or can be permanently removed. The removed portions can be filtered.
Any suitable configuration of columns to form an ammonia absorption system can be use, including, for example, one column or multiple column arrangements. Although a single column can provide the necessary contact time between the aqueous solution and the feed stream to effectively remove a desired amount of ammonia, it can sometimes be more convenient to use several columns in place of one. For example, tall or large columns can be expensive to build, house, and maintain. Any description herein of an ammonia absorber can include any suitable number of columns that together form the ammonia absorber. The ammonia absorber can include an absorber unit and a stripper unit, for example in embodiments that separate ammonia from an Andrussow process reaction effluent, an HCN stripper unit. In such an embodiment, the absorber unit extracts ammonia from a feed stream using the aqueous solution. The aqueous solution that enters the absorber unit can be an aqueous solution recycle stream from the desorber. The absorber allows the feed stream and the aqueous solution to separate, at least to some extent. The top stream of the absorber unit, which can contain HCN separated from the majority of the ammonia, then can pass to an HCN recovery system. The aqueous solution, which can contain residual feed stream materials including HCN can then enter the stripper unit, which heats the aqueous solution. The stripper unit allows the aqueous solution and other materials to separate, for example residual feed stream materials including residual HCN can be more fully separated from the aqueous solution in the stripper unit. Ammonia absorption can also occur in the stripper unit. The top stream of the stripper unit, which can include residual HCN or other materials, can return to the absorber unit, for example entering with the feed stream. The bottom stream of the stripper unit can then pass to the ammonia desorber.
The ammonia desorber can be any suitable desorber. The ammonia desorber desorbs ammonia from the aqueous solution. The ammonia desorber can desorb any suitable amount of ammonia from the aqueous solution, e.g. about 1 wt %, 2, 5, 10, 20, 30, 40, 50, 60, 70, 80, 90, 95, 98, 99, 99.5, 99.9, 99.99, or about 100 wt % of the ammonia in the aqueous solution can be desorbed from the aqueous solution in the ammonia desorber. The desorbed ammonia can be removed from the desorber to be further processed, for example to be condensed or pressurized into a liquid form, or to be used directly without liquification. A condenser can be used to remove water from the ammonia gas, which can render it more suitable for its intended use. A series of condensers can be included, such as a condenser designed to remove water or other materials from the gas stream exiting the desorbed, and another cooler or lower pressure condenser designed to liquefy ammonia. The desorbed ammonia can be recycled to provide at least a portion of the ammonia feed for an Andrussow HCN process.
Any suitable configuration of columns to form an ammonia desorption system is encompassed by the present invention, including, for example, one column or multiple column arrangements. Although a single column can provide the necessary heating and separation of the aqueous solution and the ammonia, it can sometimes be more convenient to use several columns in place of one. Any description herein of an ammonia desorber can encompass any suitable number of columns that together form the ammonia desorber. The ammonia desorber can include an ammonia stripper unit and an ammonia enricher unit. In such an embodiment, the ammonia desorber heats the aqueous solution to remove the ammonia therefrom. The ammonia desorber allows the ammonia to separate from the aqueous solution, to some extent. The bottom stream of the stripper unit includes aqueous solution that can be returned to the absorber. The top stream includes ammonia and aqueous solution that can be sent to the enricher unit. The enricher further heats the aqueous solution, to further remove ammonia from the aqueous solution, and to allow aqueous solution to separate from the ammonia. The bottom stream of the enricher can pass back to the stripper unit of the desorber. The top stream of the enricher contains predominantly ammonia and water vapor. The water vapor can be condensed out of the ammonia, and the ammonia can be used in any suitable fashion, such as by being recycled to be used as a starting material for an Andrussow HCN process.
The ammonia absorbed in the aqueous solution in the form of a dissolved gas or an ammonium salt is desorbed from the aqueous solution to give ammonia and the corresponding ions, which may or may not be present in the form of a salt. The ammonia desorber heats, applies vacuum pressure, or otherwise treats the aqueous solution to cause the ammonium salt to release to ammonia. The treatment can occur in any suitable fashion. The desorber can be a tower, or a stripping tower. A tower can allow for better temperature control of the aqueous solution, for example as cooler aqueous solution enters the tower it can contact a smaller proportion of the liquid therein prior to becoming heated which can allow the majority of heated liquid in the tower to remain heated. Heating can occur via gas injection at the bottom of the tower, for example using any suitable gas such as air or steam, and a tower can facilitate contacting and heat transfer between the gas and the aqueous solution therein.
A reboiler can provide heat to the aqueous solution in the desorber. In some examples, the ammonia desorber includes a stripper tower and a stripper tower reboiler. A reboiler can be connected to a stripping tower via transfer piping at any suitable section of the tower, for example near the bottom section of the tower. The reboiler can be any suitable reboiler. The aqueous solution can be fed to the tower at any suitable section of the tower, for example near the top section of the tower. One or more pumps can be included in the transfer piping that is disposed between the stripper and the reboiler, which can circulate aqueous solution between the stripper tower and the reboiler. The rate of circulation of the liquid between the stripper and the reboiler, or the amount of heat transferred to the liquid by the reboiler, can be suitably adjusted such that an economical balance between energy use and ammonia recovery can be made. Ammonia gas and water can move to the top of the tower where it can be removed, for example via transfer piping. The aqueous solution can be removed from the desorber in any suitable location. For example, the aqueous solution can be removed from the stripper in the bottom section of the stripper, or from transfer piping between the reboiler and the stripper, or in the top section of the stripper.
The strippers herein can be of any suitable design. Generally, a stripper is similar to a distillation column, and has a reboiler unit near the bottom that heats the contents. The more volatile contents leave the top of the column, and the less volatile contents leave the bottom of the tower. The stripper tower can contain internals to facilitate chemical reactions and multiple equilibriums between gas and liquid phase. Examples of suitable internals are taught in Kirk-Othmer Encyclopaedia of Chemical Technology, 3rd Edition, vol. 1, pp. 53-96 (John Wiley & Sons, 1978), and include trays, plates, rings and saddles, merely to name a few. The choices of column length, diameter, and type of internals) can be determined by one of ordinary skill in the art given the throughput and purity requirements for the ammonia recycle stream.
The aqueous solution that has been desorbed can return via transfer piping to the absorber. The aqueous solution, or portions of the aqueous solution, can undergo any suitable treatment prior to entering the absorber. In some examples, portions of the aqueous solution can be removed between the desorber and the absorber. The removed portions can be suitably treated and returned to the aqueous solution at a suitable location, or can be permanently removed.
The pressure that occurs in any of the absorber or desorber or any component thereof can be any suitable pressure. For example, a suitable pressure can be equal to or less than 1 psig, 2 psig, 5 psig, 7 psig, 9 psig, 11 psig, 13 psig, 15 psig, 17 psig, 19 psig, 21 psig, 23 psig, 25 psig, 27 psig, 29 psig, 31 psig, 33 psig, 35 psig, 37 psig, 39 psig, 41 psig, 43 psig, 45 psig, 47 psig, 49 psig, 51 psig, 53 psig, 55 psig, 57 psig, or 59 psig or more. The temperature that occurs in any of the absorber or desorber or any component thereof can be any suitable temperature. For example, a suitable temperature can be equal to or less than 50° C., 60° C., 70° C., 80° C., 90° C., 100° C., 110° C., 120° C., 130° C., 140° C., 150° C., 160° C., 170° C., 180° C., 190° C., 200° C., 210° C., 220° C., 230° C., 240° C., or 250° C. or more. The pH that occurs in any of the absorber or desorber or any component thereof can be any suitable pH, for example, the pH can be equal to or below 1, 2, 3, 4, 5, 6, 7, or about 8.
An oxygen-containing gas can be sparged into the aqueous solution in the ammonia absorber, the ammonia desorber, the desorber reboiler, or in any suitable location therebetween. Other embodiments include no sparging. Sparging combined with purging and replacing can have a synergistic effect (e.g. greater than additive) on corrosion reduction, or sparging combined with purging and replacing can have an additive effect on corrosion reduction. In sparging, a gas can be injected into a liquid, for example such that bubbles of the gas are formed in the liquid; alternatively, a gas can be injected directly into a gas or vapor phase wherein the solution into which sparging is occurring is raining down from above. The gas can be sparged into a small amount of liquid, such that bubbles do not form but rather the sparged gas immediately enters a gas or vapor phase. In embodiments including the sparging of gas into a stripper tower, the contacting between the gas and the aqueous solution is advantageously facilitated by a tower design. The desorber can include functional architecture or media therein that increases contacting between the aqueous solution and any gas that may be present therein, or that can increase the mixing of the aqueous solution therein, which can help to maximize the amount of ammonia desorbed from the feed stream during its residence in the desorber.
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The ammonia extraction equipment includes an aqueous solution. The aqueous solution circulates between the absorber and the desorber, and is used to absorb the ammonia from the ammonia feed stream. The aqueous solution absorbs ammonia as dissolved gas, or as an ammonium salt. The aqueous solution contacts at least part of the interior of the ammonia extraction equipment, including the absorber, the desorber, and associated transfer piping. The portions of the equipment that contact the aqueous solution can experience corrosion, at least some of which is reduced by use of the present invention as compared to the corresponding corrosion experienced without performing the purging and replacing as described herein.
The aqueous solution absorbs ammonia as dissolved gas, or as an ammonium salt. The ammonium salt includes an ammonium ion and a counterion. The counterion can be provided from an acid in the aqueous solution. Alternatively, the counterion can be provided by a salt already present in the solution.
For example, the aqueous solution can include a mineral acid such as hydrochloric acid or sulfuric acid. For example, if the acid is hydrochloric acid, the ammonia can react with the hydrochloric acid upon contacting the ammonia feed stream with the aqueous solution to form ammonium chloride. In the desorber, the ammonium chloride can be converted to ammonia and hydrogen chloride.
In another example, the aqueous solution can include phosphoric acid (H3PO3), monoammonium phosphate ((NH4)(H2PO4)) (e.g. “ammonium dihydrogen phosphate”), diammonium phosphate ((NH4)2(HPO4)) (e.g. “ammonium hydrogen phosphate”), ammonium phosphate ((NH4)3PO4) (e.g. “triammonium phosphate”), or any combination thereof. In the absorber, the aqueous solution can include at least one of phosphoric acid, monoammonium phosphate, and diammonium phosphate, or any combination thereof, and optionally also contains ammonium phosphate. In the desorber, the aqueous solution can include at least one of ammonium phosphate, diammonium phosphate, and monoammonium phosphate, or any combination thereof, and optionally also contains phosphoric acid. The ammonia can react with the aqueous solution upon contact with the ammonia feed stream to form ammonium salts with counterions such as (H2PO4)−1, (HPO4)−2, or (PO3)−3. For example, a molecule of phosphoric acid (H3PO3) can react with a molecule of ammonia to form a molecule of monoammonium phosphate ((NH4)(H2PO4)). In another example, a molecule of monoammonium phosphate ((NH4)2(HPO4)) can react with a molecule of ammonia to form a molecule of diammonium phosphate ((NH4)2(HPO4)). In another example, a molecule of diammonium phosphate ((NH4)2(HPO4)) can react with a molecule of ammonia to form a molecule of triammonium phosphate ((NH4)3PO4). Alternatively, multiple molecules of ammonia can combine with a single molecule of phosphate salt or phosphoric acid to generate a single salt molecule. For example, two molecules of ammonia can react with a molecule of phosphoric acid to form a molecule of diammonium phosphate ((NH4)2(HPO4)). In another example, two molecules of ammonia can react with a molecule of monoammonium phosphate ((NH4)(H2PO4)) to form a molecule of ammonium phosphate ((NH4)3PO4). In another example, three molecules of ammonia can react with a molecule of phosphoric acid (H3PO3) to form a molecule of ammonium phosphate ((NH4)3PO4). In the desorber, the phosphate salts can be converted to ammonia and the corresponding phosphorus compounds. For example, a molecule of ammonium phosphate ((NH4)3PO4) can give a molecule of ammonia and a molecule of diammonium phosphate ((NH4)2(HPO4)). In another example, a molecule of diammonium phosphate ((NH4)2(HPO4)) can give a molecule of ammonia and a molecule of monoammonium phosphate ((NH4)(H2PO4)). In another example, a molecule of monoammonium phosphate ((NH4)(H2PO4)) can give a molecule of ammonia and a molecule of phosphoric acid (H3PO3). Alternatively, a single molecule of ammonium salt can form a single molecule of phosphate salt or phosphoric acid and multiple molecules of ammonia. For example, a molecule of diammonium phosphate ((NH4)2(HPO4)) can form a molecule of phosphoric acid (H3PO3) and two molecules of ammonia. In another example, a molecule of ammonium phosphate ((NH4)3PO4) can form a molecule of monoammonium phosphate ((NH4)(H2PO4)) and two molecules of ammonia. In another example, a molecule of ammonium phosphate ((NH4)3PO4) can form a molecule of phosphoric acid (H3PO3) and three molecules of ammonia. One of skill in the art will readily understand that certain ions can interconvert, e.g. a proton can move between an (HPO4)−2 and (H2PO4)−1 to form (H2PO4)−1 and (HPO4)−2.
The aqueous solution can include sulfuric acid (H2SO4), ammonium bisulfate (NH4(HSO4)), ammonium sulfate ((NH4)2SO4), or any combination thereof. In the absorber, the aqueous solution can include at least one of sulfuric acid and ammonium bisulfate, and optionally can include ammonium sulfate. In the desorber, the aqueous solution can include at least one of ammonium bisulfate and ammonium sulfate, and optionally can include sulfuric acid. In the absorber, the ammonia can combine with the acid or a sulfate salt to form a sulfate salt. For example, a molecule of sulfuric acid can combine with a molecule of ammonia to form a molecule of ammonium bisulfate. In another example, a molecule of ammonium bisulfate can combine with a molecule of ammonia to form a molecule of ammonium sulfate. In another example, a molecule of sulfuric acid can combine with two molecules of ammonia to form a molecule of ammonium sulfate. In the desorber, the sulfate salt can form ammonia and a sulfate salt or the acid. For example, a molecule of ammonium sulfate can form a molecule of ammonia and a molecule of ammonium bisulfate. In another example, a molecule of ammonium bisulfate can form a molecule of ammonia and a molecule of sulfuric acid. In another example, a molecule of ammonium sulfate can form two molecules of ammonia and a molecule of sulfuric acid.
The aqueous solution can include nitric acid or acetic acid. The ammonia can react with the acid in the absorber to generate ammonium nitrate or ammonium acetate. In the desorber, the ammonium nitrate or ammonium acetate can be converted to ammonia and the acid.
The method includes purging at least part of the aqueous solution. The purged solution is purged from the circulating aqueous solution. The purged part of the aqueous solution comprises at least one corrosion-promoting ion. By purging part of the circulating aqueous solution that includes the at least one corrosion-promoting ion, and adding a replacement aqueous solution to the circulating aqueous solution, wherein the replacement aqueous solution is substantially free of the at least one corrosion-promoting ion, the method removes at least some of the at least one corrosion-promoting ion from the circulating aqueous solution. By removing at least some of the at least one corrosion-promoting ion from the circulating aqueous solution, the present method can maintain or decrease the concentration of the at least one corrosion-promoting ion in the circulating aqueous solution, allowing reduction of corrosion of the ammonia extraction equipment, such as the absorber or the desorber for example. By removing at least some of the at least one corrosion-promoting ion from the circulating aqueous solution, the concentration of the at least one corrosion-promoting ion in the circulating aqueous solution can be prevented from rising as quickly.
The purging can be performed at any suitable location in the ammonia extraction apparatus. For example, the purging can be performed in an ammonia absorption tower, ammonia absorption tower top, ammonia sorption tower bottom, ammonia stripper tower, ammonia stripper tower top, ammonia stripper tower bottom, stripper tower reboiler, ammonia condenser, distillation column, ammonia enricher, heat exchanger, transfer piping for each piece of equipment present, or a combination thereof.
The purging can be conducted at any suitable rate. In some examples, the purging can be conducted continuously. In other examples, the purging can be conducted in a batch-wise fashion. In some examples, the rate of purging can be varied. The rate of purging can be varied to control the rate of corrosion of various parts of the apparatus. The rate of purging can be varied to control the concentration of one or more corrosion-promoting ions in the circulating aqueous solution. In some examples, the rate of purging can be varied to keep the concentration of one or more corrosion-promoting ions below a particular maximum concentration. The maximum concentration can be set such that corrosion of the ammonia extraction equipment, for example the absorber or the desorber, is reduced. The purging can be controlled in conjunction with the rate of replacement of the aqueous solution.
A salt can be recovered from the purged aqueous solution. In some examples, the salt can be a valuable byproduct. The salt can be a salt of an acid, such as an ammonium salt, such as an ammonium phosphate salt. Ammonium phosphate salts can be sold as fertilizer or fertilizer ingredients.
The purging can be performed at any suitable rate, for example at an average rate of 50 lb/h, 100 lb/h, 150 lb/h, 200 lb/h, 250 lb/h, 300 lb/h, 350 lb/h, 400 lb/h, 450 lb/h, 500 lb/h, 550 lb/h, 600 lb/h, 700 lb/h, 900 lb/h, 1500 lb/h, 2000 lb/h, 3000 lb/h, or more. The purging can be scaled to the flow rate of the aqueous liquid passing from the desorber to the absorber. The purging can be scaled in any suitable ratio. For example, about 1 lb of liquid can be purged for every 100, 250, 500, 750, 800, 900, 1000, 1100, 1200, 1300, 1500, 1750, 2000, 2500, 3000, 4000, or for every about 5000 lb of liquid that pass from the desorber to the absorber.
The at least one corrosion-promoting ion can be any suitable corrosion-promoting ion. In some examples, the presence of a corrosion-promoting ion can cause or allow corrosion to occur at a greater rate on certain materials, such as austenitic steels, such as in acidic solutions, than if the corrosion-promoting ion was present below that concentration.
The corrosion-promoting ion can promote corrosion via any suitable mechanism. Embodiments of the present invention are not restricted to a specific mechanism of action of the corrosion-promoting ion.
In some examples, the corrosion-promoting ion can be formate, oxalate, fluoride, chloride, sulfate, and sulfide. The corrosion-promoting ion can exist as a completely solvated ion, as an ion coordinated via an ionic bond to a counterion, or any state in between. The corrosion-promoting ion can be coordinated to any suitable counterion, or solvated by any suitable solvent.
The method includes adding a replacement aqueous solution to the circulating aqueous solution. The replacement aqueous solution is substantially free of the at least one corrosion-promoting ion. By purging a portion of the circulating aqueous solution that includes at least one corrosion-promoting ion, and adding replacement solution into the circulating aqueous solution that is substantially free of the at least one corrosion-promoting ion, the at least one corrosion-promoting ion can be removed from the circulating aqueous solution.
The replacement aqueous solution can be added into the circulating aqueous solution in any suitable location. For example, the replacement aqueous solution can be added into the circulating aqueous solution in an ammonia absorption tower, ammonia absorption tower top, ammonia sorption tower bottom, ammonia stripper tower, ammonia stripper tower top, ammonia stripper tower bottom, stripper tower reboiler, ammonia condenser, distillation column, ammonia enricher, heat exchanger, and transfer piping for each piece of equipment present, or any combination thereof.
The replacing can be conducted at any suitable rate. In some examples, the replacing can be conducted continuously. In other examples, the replacing can be conducted in a batch-wise fashion. In some examples, the rate of replacing can be varied. The rate of replacing can be varied to control the rate of corrosion of various parts of the apparatus. The rate of replacing can be varied to control the concentration of one or more corrosion-promoting ions in the circulating aqueous solution. In some examples, the rate of replacing can be varied to keep the concentration of one or more corrosion-promoting ions below a particular maximum concentration. The maximum concentration can be set such that corrosion of the ammonia extraction equipment, for example the absorber or the desorber, is reduced. The replacing can be controlled in conjunction with the rate of purging of the aqueous solution.
The replacing can occur directly in the ammonia recovery system, or the replacing can occur directly in another part of a chemical plant, such as an HCN recovery train, and can then be sent (e.g. from a packed cooler) to the ammonia recovery system. The replacement can occur at any suitable rate, and at any suitable location. The rate of replacement into an HCN recovery system can be the same as the rate at which replacement liquid moves from the HCN recovery system into the ammonia recovery system. Liquid can transfer to the ammonia recovery system from an HCN recovery system at a different rate than the replacement solution is added to the HCN recovery system, for example the replacement solution can be added to the HCN recovery system at about 0.01, 0.1, 0.2, 0.4, 0.6, 0.8, 1.2, 1.4, 1.8, 2.0, 2.5, 3.0, 3.5, 4.0, 5.0, 7.0, 10.0, 15.0, 20.0, 50, or about 1000 times the rate the liquid is transferred from the HCN recovery system to the ammonia recovery system. The replacement solution can be any suitable replacement solution. The replacement solution can be any suitable aqueous phosphoric acid solution, suitable to replace the phosphoric acid and other phosphorus ions that are purged, for example equal to or less than 10 wt % aqueous phosphoric acid, 20 wt %, 30 wt %, 40 wt %, 50 wt %, 60 wt %, 70 wt %, 80 wt %, or 85 wt % aqueous phosphoric acid.
The replacing can be performed at an average rate of 10 lb/h, 20 lb/h, 50 lb/h, 75 lb/h, 100 lb/h, 125 lb/h, 150 lb/h, 175 lb/h, 200 lb/h, 250 lb/h, 300 lb/h, 350 lb/h, 400 lb/h, 450 lb/h, 500 lb/h, or about 1000 lb/h or more. The rate of replacement can be about the same as the rate of purging. The rate of replacement can be different than the rate of purging. The rate of replacement can be scaled to the amount of aqueous solution that passes from the desorber to the absorber. The rate of replacement can be scaled to the amount of aqueous solution passing from the desorber to the absorber in any suitable way. For example, the rate of replacement can be about 1 lb for every about 1000 lb of aqueous solution passing from the desorber to the absorber, or for every about 1500 lb, 2000 lb, 2500 lb, 3000 lb, 3500 lb, 4000 lb, 4500 lb, 5000 lb, 5500 lb, 6000 lb, 6500 lb, 7000 lb, 7500 lb, 8000 lb, 8500 lb, 9000 lb, 9500 lb, 10,000 lb, 15,000 lb or more lb of aqueous solution passing from the desorber to the absorber.
The replacement aqueous solution can include any suitable aqueous solution that is substantially free of the at least one corrosion-promoting ion. In some examples, the replacement solution includes water mixed with acid or the ammonium salt thereof. In some examples, the replacement solution can be prepared on site, whereas in other examples, the replacement solution can be commercially provided. The replacement solution can be formed by substantially removing the at least one corrosion-promoting ion from at least part of the purged aqueous solution.
The purging and replacing is sufficient to reduce corrosion of the ammonia absorber or the ammonia desorber. The reduction is as compared to the process as performed without the purging and replacing, wherein with reduced corrosion the amount of corrosion per time is less. The reduction of corrosion can occur in the piece of equipment wherein purging and replacing is performed, in a piece of equipment connected to the piece of equipment wherein purging and replacing is performed, in transfer piping connecting the piece of equipment wherein purging and replacing is performed to other equipment, or in any combination thereof. In one example, the piece of equipment in which purging and replacing is performed has the greatest reduction in corrosion, as compared to a peripheral piece of equipment that also experiences a reduction in corrosion.
Corrosion is the disintegration of a material due to chemical reactions with its surroundings. Corrosion can be measured in any suitable fashion. For example, corrosion can be measured as the amount of material that is lost per period of time. The amount of material can be defined as a volume of material, or as a thickness of material. Such quantities are not necessarily equivalent, since pitting can sometimes occur, and since the thickness of material corroded may not be consistent throughout a piece of equipment. Although a volumetric measurement of material lost can be a very accurate measurement of corrosion rate, generally it is more practical and substantially as useful to measure a change in thickness per time. In some examples, a thickness change per time can be averaged over the entire corrosion-prone surface area of a piece of equipment, can be averaged over a particular section of the surface area of a piece of equipment, or can be the measure of the change of thickness of a specific part of the piece of equipment.
Corrosion can occur on surfaces of the ammonia extraction equipment that contacts the aqueous solution, or that contacts solution that condenses. The rate of corrosion can be especially severe in areas of the ammonia extraction equipment that contact heated aqueous solution. Equipment that contacts heated aqueous solution can include the desorber, such as a stripping tower, the reboiler, and the transfer piping disposed therebetween. The materials used in any of the ammonia recovery equipment can be any one or any combination of any suitable corrosion-prone or corrosion-resistant material.
The term “corrosion-prone” is used herein to designate material that is corrosion-prone as compared to specialized and generally more expensive corrosion-resistant materials, rather than as compared to materials that are generally corrosion-prone as compared to all metals such as iron or non-stainless steel (e.g. steel not having sufficient chromium to allow formation of a protective chromium-oxide barrier against corrosion). Examples of corrosion-resistant materials can superalloys, such as nickel-copper alloys containing small amounts of iron and trace amounts of other elements such as Monel® 400, precipitation-strengthened nickel-iron-chromium alloys such as Incoloy® brand alloys, for example Incoloy® 800 series, or austenitic nickel-chromium-based Inconel® brand alloys, or nickel-chromium-molybdenum alloys such as Hastelloy® brand alloys, for example, Hastelloy® G-30®. Examples of corrosion-resistant materials include any suitable corrosion-resistant material, such as super austenitic stainless steels (e.g. AL6XN, 254SMO, 904L), duplex stainless steels (e.g. 2205), super duplex stainless steels (e.g. 2507), nickel-based alloys (e.g. alloy C276, C22, C2000, 600, 625, 800, 825), titanium alloys (e.g. grade 1, 2, 3), zirconium alloys (e.g. 702), Hasteloy 276, duplex 2205, super duplex 2507, Ebrite 26-1, Ebrite 16-1, Hasteloy 276, Duplex 2205, 316 SS, 316L and 304SS, zirconium, zirconium clad 316, ferralium 255, or any combination thereof.
Corrosion-prone parts of the ammonia extraction equipment that contacts the aqueous solution can become corroded. Corrosion-prone areas include metals contacting the aqueous solution. Corrosion-prone metals can include any suitable corrosion-prone metal. For example, corrosion-prone metals can include steel, such as stainless steel. Stainless steel can include, for example, austenitic steel, ferritic steel, martensitic steel, and combinations thereof in any suitable proportion. Stainless steels can include any suitable series of stainless steel, such as for example 440A, 440B, 440C, 440F, 430, 316, 409, 410, 301, 301LN, 304L, 304LN, 304, 304H, 305, 312, 321, 321H, 316L, 316, 316LN, 316Ti, 316LN, 317L, 2304, 2205, 904L, 1925hMo/6MO, 254SMO. Austenitic steels can include 300 series steels, for example having a maximum of about 0.15% carbon, a minimum of about 16% chromium, and sufficient nickel or manganese to retain an austenitic structure at substantially all temperatures from the cryogenic region to the melting point of the alloy. Austenitic steel can include, for example, 316L steel. The majority or entirety of a piece of equipment such as for example the absorber, desorber, and transfer piping, can be made from corrosion-prone material.
Corrosion-resistant materials can also experience corrosion, but generally the corrosion occurs at a lower rate on these materials as compared to corrosion-prone materials. The ammonia extraction equipment of the present invention can include corrosion-resistant materials on all or part of the surfaces that become corroded due to contacting the aqueous solution or vapor. The pieces of equipment that can experience the most corrosive conditions, such as the desorber, can include corrosion-resistant materials in all or some of the locations that contact the aqueous solution or vapor. The pieces of equipment that can experience less corrosive conditions, such as the absorber, can include corrosion-resistant material in all or some of the locations that contact the aqueous solution or vapor. Locations of equipment that do not contact the aqueous solution or vapor can also include corrosion-resistant materials, including areas that may be exposed to corrosive vapors, and including areas of the equipment that would be difficult to fabricate from materials that differ from the material that the rest of the particular section of the equipment is made from. Any piece of equipment can be made from a combination of corrosion-resistant and corrosion-prone materials.
In some examples, the corrosion rate with purging and replacing can be about 1%, or about 2%, 3%, 4%, 5%, 6%, 7%, 8%, 9%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or about 95% of the rate of corrosion without purging and replacing. In some embodiments, with purging and replacing, corrosion in the majority of areas of the ammonia absorber, desorber, reboiler, and associated transfer piping, can be about 0.1 mils/year, or about 0.5 mils/year, 1 mils/year, 2 mils/year, 3 mils/year, 4 mils/year, 5 mils/year, 10 mils/year, 15 mils/year, 20 mils/year, 25 mils/year, 30 mils/year, 35 mils/year, 40 mils/year, 45 mils/year, 50 mils/year, 55 mils/year, 60 mils/year, 65 mils/year, 70 mils/year, 75 mils/year, 80 mils/year, 85 mils/year, 90 mils/year, 95 mils/year, 100 mils/year, 105 mils/year, 110 mils/year, 115 mils/year, 120 mils/year, 125 mils/year, 130 mils/year, 135 mils/year, 140 mils/year, 145 mils/year, or about 150 mils/year. In some embodiments, the purging and replacing can allow the corrosion rate of metals that include chromium to be lowered sufficiently such that concentration of chromium in the aqueous solution can be 1000 ppm after 90 days of operation of the recovery system, or about 900 ppm, 800 ppm, 700 ppm, 600 ppm, 500 ppm, 400 ppm, 300 ppm, 200 ppm, 100 ppm 50 ppm, 25 ppm, 10 ppm, 5 ppm, or about 1 ppm after 90 days.
Corrosion, or the degree or rate or corrosion, can be detected in any suitable manner. In one example, a visual inspection of the corrosion-prone surface can detect corrosion or the rate of corrosion. In another example, a mechanical measuring device can be used, such as a ruler or a caliper. For nondestructive testing of a general decrease in vessel wall thickness, an ultrasonic thickness gauge can be used. Examples of such gauges include the Magnaflux MT-21B thickness gauge, available from Magnaflux, 3624 W. Lake Ave., Glenview, Ill. 60026, the DeFelsko Positector UTG Standard available from DeFelsko Corporation, 802 Proctor Avenue, Ogdensburg, N.Y. 13669, and the General Tools UTEGEMTT2 ultrasonic thickness gauge, available from General Tools, 80 White Street, Suite #1, New York, N.Y. 10013. Any suitable nondestructive method of testing can be used, including, for example, ultrasound (from inside or outside), using a mold of an original wall to compare, caliper of depth gauge to measure pitting, comparison to a nearby wall (e.g. weld), x-ray, and the like.
In another example, a corrosion rate can be detected using instantaneous corrosion measurement. The instantaneous corrosion rate can be measured using techniques such as those described in Instantaneous Corrosion Rate Measurement with Small-Amplitude Potential Intermodulation Techniques Corrosion 52, 204 (1996); doi:10.5006/1.3292115, R. W. Bosch and W. F. Bogaerts, Katholieke Universiteit Leuven, Department of Metallurgy and Materials Engineering, de Croylaan 2, 3001, Heverlee, Belgium, or in U.S. Pat. No. 7,719,292 to Eden (Honeywell), “Method and apparatus for electrochemical corrosion monitoring.” In one example instantaneous corrosion measurement can be performed using a corrosion probe, such as any suitable corrosion probe. In one example, a corrosion probe can include suitable metals with an insulator therebetween, the metals being connected to an instrument which can detect corrosion. In another example, concentration of compounds produced from corrosive reactions can be measured.
A predetermined maximum concentration of one or more corrosion-promoting ions can be selected. The predetermined maximum concentration can be the same for multiple corrosion-promoting ions, or it can be different between multiple corrosion-promoting ions. The predetermined maximum concentration is any suitable predetermined maximum concentration for one or more corrosion-promoting ions such that when the concentration of the particular corrosion-promoting ion in the circulated aqueous solution is maintained at or below that concentration, the rate of corrosion of the ammonia extraction equipment, such as the absorber or the desorber, is reduced.
The predetermined maximum concentration of one or more corrosion-promoting ions can be determined by measuring the rate of corrosion, for example visually or instantaneously, and determining whether the rate of corrosion is as low as desired. By varying the concentration of various corrosion-promoting ions and measuring the corrosion rate, the predetermined maximum concentration of one or more corrosion-promoting ions can be optimized. However, less than optimal predetermined maximum concentrations can be used, wherein maintaining of the one or more corrosion-promoting ions at or below the respective maximum concentrations is still effective to reduce the rate of corrosion, for example of the absorber or the desorber.
The concentration of a corrosion-promoting ion can be measured in any suitable way. Any suitable analytical method can be used. For example, gas chromatography can be used, or LCMS, or HPLC, or NMR. Qualitative tests can be used.
The purging and replacing steps maintain a concentration of the at least one corrosion-promoting ion in the aqueous solution at or below a predetermined concentration. In some examples, the purging and replacing are sufficient to reduce corrosion of at least one of the ammonia absorber and the ammonia desorber, wherein the maintaining of the concentration of the at least one corrosion-promoting ion in the aqueous solution below the predetermined concentration is sufficient to allow the reduced corrosion to occur. The purging and replacing are sufficient to reduce corrosion of at least one of the ammonia absorber and the ammonia desorber, wherein maintaining of the concentration of the at least one corrosion-promoting ion is sufficient to allow formation of a corrosion-reducing layer on the ammonia extraction equipment having reduced corrosion.
All ppm given herein are ppmw unless otherwise noted.
The predetermined maximum concentration of formate can be less than about 0.1 wt %, 0.5 wt %, 1 wt %, 2 wt %, 3 wt %, 4 wt %, 5 wt %, 6 wt %, 7 wt %, 8 wt %, 9 wt %, 10 wt %, 11 wt %, 12 wt %, 13 wt %, 14 wt %, 15 wt %, 20 wt %, 25 wt %, 30 wt %, or about 40 wt % or more.
The predetermined maximum concentration of oxalate can be less than about 1 ppm, 10 ppm, 25 ppm, 50 pppm, 100 ppm, 250 ppm, 500 ppm, 750 ppm, 1000 ppm, 1500 ppm, 2000 ppm, 2500 ppm, 5000 ppm, 1 wt %, 2 wt %, 3 wt %, 4 wt %, 5 wt %, 6 wt %, 7 wt %, 8 wt %, 9 wt %, 10 wt %, 20 wt %, or about 30 wt % or more.
The predetermined maximum concentration of fluoride can be less than about 1 ppm, 2 ppm, 3 ppm, 4 ppm, 5 ppm, 10 ppm, 25 ppm, 50 pppm, or about 100 ppm or more.
The predetermined maximum concentration of chloride can be less than about 1 ppm, 10 ppm, 25 ppm, 50 pppm, 100 ppm, 250 ppm, 500 ppm, 750 ppm, 1000 ppm, 1500 ppm, 2000 ppm, 2500 ppm, 5000 ppm, 1 wt %, 2 wt %, 3 wt %, 4 wt %, 5 wt %, 6 wt %, 7 wt %, 8 wt %, 9 wt %, 10 wt %, 20 wt %, or about 30 wt % or more.
The predetermined maximum concentration of sulfide can be about 1 ppm, 10 ppm, 25 ppm, 50 pppm, 100 ppm, 250 ppm, 500 ppm, 750 ppm, 1000 ppm, 1500 ppm, 2000 ppm, 2500 ppm, 5000 ppm, 1 wt %, 2 wt %, 3 wt %, 4 wt %, 5 wt %, 6 wt %, 7 wt %, 8 wt %, 9 wt %, 10 wt %, 20 wt %, or about 30 wt % or more.
The predetermined maximum concentration of sulfate can be less than about 1 ppm, 5 ppm, 10 ppm, 25 ppm, 50 pppm, 75 ppm, 100 ppm, 125 ppm, 200 ppm, 250 ppm, 500 ppm, 750 ppm, 1000 ppm, 1500 ppm, 2000 ppm, 2500 ppm, 5000 ppm, 1 wt %, 2 wt %, 3 wt %, 4 wt %, 5 wt %, 6 wt %, 7 wt %, 8 wt %, 9 wt %, 10 wt %, 20 wt %, or about 30 wt % or more.
The predetermined maximum concentration of chrome, the presence of which can indicate corrosion of certain equipment, can be less than about 1 ppm, 2 ppm, 3 ppm, 4 ppm, 5 ppm, 7 ppm, 10 ppm, 15 ppm, 20 ppm, 25 ppm, 30 ppm, 35 ppm, 40 ppm, 45 ppm, 50 ppm, 75 ppm, or about 100 ppm or more.
The predetermined maximum concentration of zirconium, the presence of which can indicate corrosion of certain equipment, can be less than about 1 ppm, 2 ppm, 3 ppm, 4 ppm, 5 ppm, 7 ppm, 10 ppm, 15 ppm, 20 ppm, 25 ppm, 30 ppm, 35 ppm, 40 ppm, 45 ppm, 50 ppm, 75 ppm, or about 100 ppm or more.
The present invention can include a control system. A control system can allow adjustment of various factors related to the purging and replacing, such as the rate of purging or replacing. Control systems are known in the art, and one of ordinary skill will readily appreciate that the method and system described herein are amenable to the use of any suitable control system such that corrosion-reduction occurs.
A control system can be manually operated, such that an operator makes a decision based on particular data or operating procedures and tells the controller that particular factor is to be set in a particular way. A manually set factor can be permanently set as such or can be set as such until another event occurs, for example until a set duration of time passes or another event triggers an end to the change or a new change. A manual controller could be used to maintain the concentration of one or more corrosion-promoting ions in the aqueous solution at or below a maximum concentration, or could be used to maintain the flow rate of the purge or replacement stream above a suitable minimum or below a suitable maximum. For example, a visual inspection of corrosion or an instantaneous measurement of corrosion can cause an operator to adjust the predetermined maximum concentration of various corrosion-promoting ions or the flow rate of the purging or replacing such that the rate of corrosion-reduction is maintained or increased.
A control system can be automatic, such that information or data is fed to the control system and the control system maintains or modifies particular factors related to the purging or replacing in response to the data. For example, information about the concentration of one or more corrosion-promoting ions can be fed to the controller, and the controller can adjust, for example, the flow rate of the purge or replacement streams such that the concentration of one or more corrosion-promoting ions in the aqueous solution is maintained at or below a suitable maximum concentration. In another example, the corrosion can be instantaneously measured and the measurements thereof can be fed to the controller, and in response the controller can adjust various aspects of the predetermined maximum concentration or the flow rate of the purge or replacement stream to maintain or increase the degree of corrosion-reduction. Any suitable information can be fed to the controller, and in response the controller can modify any suitable aspect of the purging, replacing, or any other aspects of the operation of the ammonia extraction equipment in response to help achieve a maximized or sustained corrosion-reducing effect.
The present invention can be better understood by reference to the following examples which are offered by way of illustration. The present invention is not limited to the examples given herein.
Absorber.
Gaseous reaction effluent from the reaction of methane with ammonia gas in the presence of oxygen and platinum catalyst, which includes primarily hydrogen cyanide and ammonia, is sent to an absorber tower. Approximately 99 wt % of the charged ammonia is removed. The reaction effluent enters the bottom section of the absorber tower, while an aqueous solution including phosphoric acid and/or ammonium phosphate salts such as monoammonium phosphate and diammonium phosphate enter the top section of the absorber tower. The absorber/desorber system is industrially sized, having a total volume of liquid of approximately 500,000 lbs, and produces scrubbed HCN having less than 1 wt % ammonia. The scrubbed gaseous reaction effluent exited the top of the absorber tower. The ammonium-salt solution exits the bottom of the absorber tower.
Desorber.
The ammonia-salt solution enters the top section of the ammonia stripper tower. The stripper tower removes ammonia from the solution by heating, causing the ammonium salt to release ammonia. The stripper tower includes a reboiler unit near the bottom of the stripper tower, which transfers heat into liquid in the stripper tower via a reboiler loop. Gas evolves from the liquid in the stripper tower exits the top section of the stripper tower. Liquid exits the bottom section of the stripper tower, to be at least partially recycled back to the absorber tower.
The absorber, desorber, and the reboiler are made primarily of austenitic stainless steels (304 and 316).
The general procedure is followed, with no purging of the aqueous solution. Clogging of pipes and valves due to formation of materials such as ammonium formate or other salts such as, for example, ammonium carbonate, ammonium phosphate, or ammonium oxalate occurred, requiring cleanings every few months. The rate of corrosion of the austenitic stainless steels in the majority of areas of the ammonia absorber, desorber, reboiler, and associated transfer piping, is approximately 0-150 mils/year, with an average of about 20-40 mils/year, with deep corrosion such as pitting occurring over localized areas, especially concentrated in the reboiler and the desorber.
The general procedure is followed, with sparging of gas. The gas used is compressed ambient air having sufficient nitrogen added to bring the oxygen concentration to about 9 mol %. The gas is sparged into the aqueous solution in the stripper reboiler. A flow rate of about 3000 scfh of the gas is used, the gas having about 9.5-10 mole % oxygen. The rate of corrosion of austenitic stainless steels in the majority of areas of the ammonia absorber, desorber, reboiler, and associated transfer piping, is approximately 0-50 mils/year, with an average of about 5-20 mils/year, with fewer localized areas of deep corrosion such as pitting than Comparative Example 1, including particularly in the reboiler and the desorber.
The general procedure is followed, with sparging of gas and purging. The gas used is compressed ambient air having sufficient nitrogen added to bring the oxygen concentration to about 9 mol %. The gas is sparged into the aqueous solution in the stripper reboiler. A flow rate of about 3000 scfh of the gas is used, the gas having about 9.5-10 mole % oxygen. The purging of the circulated aqueous solution occurs from a tank between the stripper and the absorber with an average flow rate of about 1250 lbs/h. A replacement solution of aqueous phosphoric acid is added in the ammonia recovery system. The replacement rate is sufficient such that the average concentration of formate ions are between about 5-10 wt %, sulfate ions are between about 0-100 ppm, oxalate is about 1100 ppm, and fluoride is below about 1 ppm. Corrosion products of the equipment are measured, including chrome which is about 17 ppmw, and zirconium which is between about 4-12 ppmw.
The chromium concentration is maintained at a steady state concentration of 17 ppm. The amount of chromium lost to the purging can be expressed as 17 ppm*(1250 lb/h)*(24 h)*(90 d)=about 45.9 lbs of chromium purged over 90 days. Adding the amount of chromium in solution, 17 ppm*500,000 lbs=8.5 lbs chromium, the total amount of chromium generated over 90 days is 8.5 lbs+45.9 lbs=about 54.4 lbs, indicating that the corrosion rate is approximately 44% of the rate of corrosion with air sparging but without the purging and replacing (e.g. see Comparative Example 2), and approximately 18% of the rate of corrosion without the purging and replacing and also without the sparging.
The general procedure is followed, with sparging of gas and purging. The gas used is compressed ambient air having sufficient nitrogen added to bring the oxygen concentration to about 9 mol %. The gas is sparged into the aqueous solution in the stripper reboiler. A flow rate of about 3000 scfh of the gas is used, the gas having about 9.5-10 mole % oxygen. The purging of the circulated aqueous solution occurred from a tank between the stripper and the absorber with an average flow rate of about 1250 lbs/h. A replacement solution of aqueous phosphoric acid is added in the ammonia recovery system. The replacement rate is sufficient such that the average concentration of formate ions were between about 5-10 wt %, sulfate ions are between about 50-100 ppm, oxalate is about 1100 ppm, and fluoride are below about 1 ppm. Corrosion products of the equipment are measured, including chrome which is about 17 ppmw, and zirconium which is between about 4-12 ppmw.
After 90 days, the chromium concentration is 17 ppm. Assuming the increase in concentration of the chromium over the 90 days is linear and that it started at about zero, the amount of chromium lost to the purging can be expressed as
which is approximately 23.2 lbs total of chromium purged over 90 days. Adding the amount of chromium in solution, 17 ppm*500,000 lbs=8.5 lbs chromium, the total amount of chromium generated over 90 days is 8.5 lbs+23.2 lbs=about 31.7 lbs, indicating that the corrosion rate is approximately 25% of the rate of corrosion with air sparging but without the purging and replacing (e.g. see Comparative Example 2), and approximately 11% of the rate of corrosion without the purging and replacing and also without the sparging.
The general procedure is followed, with purging and no sparging of air. The purging of the circulated aqueous solution occurs from a tank between the stripper and the absorber with an average flow rate of about 1250 lbs/h. A replacement solution of aqueous phosphoric acid is added to the ammonia recovery system, with replacement solution entering the absorber/desorber loop at a rate of about 1250 lbs/h.
The chromium concentration is maintained at a steady state concentration of about 41 ppm. The amount of chromium lost to the purging can be expressed as 41 ppm*(1250 lb/h) (24 h)*(90 d)=about 110.7 lbs of chromium purged over 90 days. Adding the amount of chromium in solution, 41 ppm*500,000 lbs=about 20.5 lbs, the total amount of chromium generated over 90 days is 110.7 lbs+20.5 lbs=about 131.2 lbs, which indicates approximately 44% of the rate of corrosion without the purging and replacing (e.g. see Comparative Example 1).
The general procedure is followed, with purging and no sparging of air. The purging of the circulated aqueous solution occurs from a tank between the stripper and the absorber with an average flow rate of about 1250 lbs/h. A replacement solution of aqueous phosphoric acid is added to the ammonia recovery system, with replacement solution entering the absorber/desorber loop at a rate of about 1250 lbs/h.
After 90 days, the chromium concentration is about 41 ppm. Assuming the increase in concentration of the chromium over the 90 days is linear and that it started at about zero, the amount of chromium lost to the purging can be expressed as
which is approximately 55.7 lbs total of chromium purged over 90 days. Adding the amount of chromium in solution, 41 ppm*500,000 lbs=about 20.5 lbs, the total amount of chromium generated over 90 days is 55.9 lbs+20.5 lbs=about 76.4 lbs, which indicates approximately 25% of the rate of corrosion without the purging and replacing (e.g. see Comparative Example 1).
The general procedure is followed, with purging of the circulated aqueous solution from a tank between the stripper and the absorber. Replacement solution of aqueous phosphoric acid is added in the ammonia recovery system. The purge and replacement rate are sufficient such that the concentrations of materials were as found in Example 1. The stripper tower, stripper tower reboiler, absorber, and associated transfer piping experience decreased corrosion and greater lifetime as compared to Comparative Examples 1 and 2, similar to the improvement experienced in Examples 1 and 2.
The general procedure is followed. In this example, a feedback loop is used that controls the purging and replacement rate based upon the instantaneous corrosion rate measurement. The stripper tower, stripper tower reboiler, absorber, and associated transfer piping experience decreased corrosion and greater lifetime as compared to Comparative Examples 1 and 2, similar to the improvement experienced in Examples 1 and 2.
The general procedure is followed, with purging and replacing as conducted in Examples 2-3. In this example ammonia is extracted from a fertilizer production process, a wastewater purification process, an ammonia production process, a pollution prevention process, a fossil fuel combustion process, a coke manufacture process, a livestock management process, or a refrigeration process. The stripper tower, stripper tower reboiler, absorber, and associated transfer piping experience decreased corrosion and greater lifetime as compared to Comparative Examples 1 and 2, similar to the improvement experienced in Examples 1 and 2.
The general procedure is followed, with purging and replacing as conducted in Examples 2-3. In this Example, the desorber, reboiler, and transfer piping are constructed of super austenitic stainless steels (e.g. AL6XN, 254SMO, 904L), duplex stainless steels (e.g. 2205), super duplex stainless steels (e.g. 2507), nickel-based alloys (e.g. alloy C276, C22, C2000, 600, 625, 800, 825), titanium alloys (e.g. grade 1, 2, 3), zirconium alloys (e.g. 702), Hasteloy 276, duplex 2205, super duplex 2507, Ebrite 26-1, Ebrite 16-1, Hasteloy 276, Duplex 2205, 316 SS, 316L and 304SS, zirconium, zirconium clad 316, ferralium 255, or any combination thereof. The stripper tower, stripper tower reboiler, absorber, and associated transfer piping experience decreased corrosion and greater lifetime as compared to an experiment run in accordance with the conditions of Comparative Examples 1 or 2 but constructed of the same material used in this Example as used for the equipment that has the purging and replacing, similar to the improvement experienced in Examples 1 or 2.
The terms and expressions which have been employed are used as terms of description and not of limitation, and there is no intention that in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the invention claimed. Thus, it should be understood that although the present invention has been specifically disclosed by preferred embodiments and optional features, modification and variation of the concepts herein disclosed may be resorted to by those skilled in the art, and that such modifications and variations are considered to be within the scope of this invention as defined by the appended claims.
The present invention provides for the following exemplary embodiments, the numbering of which is not to be construed as designating levels of importance:
Embodiment 1 provides a method of decreasing corrosion during ammonia extraction, including: performing a process to extract ammonia using ammonia extraction equipment including an ammonia absorber, ammonia desorber, and an aqueous solution including an acid or an ammonium salt thereof; purging at least part of the aqueous solution, wherein the purged part of the aqueous solution includes at least one corrosion-promoting ion; and adding a replacement aqueous solution to the aqueous solution, wherein the replacement aqueous solution has a reduced concentration of the at least one corrosion-promoting ion as compared to the purged part of the aqueous solution.
Embodiment 2 provides the method of Embodiment 1, wherein the replacement aqueous solution is substantially free of the at least one corrosion-promoting ion.
Embodiment 3 provides the method of any one of Embodiments 1-2, wherein the purging and replacing are sufficient to reduce corrosion of at least one of the ammonia desorber and the reboiler for the ammonia desorber.
Embodiment 4 provides the method of any one of Embodiments 1-3, wherein the at least one corrosion-promoting ion is selected from formate, oxalate, fluoride, chloride, sulfate, and sulfide.
Embodiment 5 provides the method of any one of Embodiments 1-4, wherein the aqueous solution is circulated between the absorber and the desorber.
Embodiment 6 provides the method of any one of Embodiments 1-5, wherein in the desorber, an ammonium salt in the solution is converted into a product mixture that includes ammonia.
Embodiment 7 provides the method of any one of Embodiments 1-6, wherein in the absorber, the ammonia is extracted from an ammonia-containing gas stream into the aqueous solution as an ammonium salt.
Embodiment 8 provides the method of any one of Embodiments 1-7, wherein the purging and replacing steps are sufficient to maintain a concentration of the at least one corrosion-promoting ion in the aqueous solution at or below a predetermined concentration.
Embodiment 9 provides the method of Embodiment 8, wherein the purging and replacing are sufficient to reduce corrosion of at least one of the ammonia desorber and the reboiler for the ammonia desorber, wherein the maintaining of the concentration of the at least one corrosion-promoting ion in the aqueous solution below the predetermined concentration is sufficient to allow the reduced corrosion to occur.
Embodiment 10 provides the method of any one of Embodiments 8-9, wherein the purging and replacing are sufficient to reduce corrosion of at least one of the ammonia desorber and the reboiler for the ammonia desorber, wherein maintaining of the concentration of the at least one corrosion-promoting ion is sufficient to allow formation of a corrosion-reducing layer on the ammonia extraction equipment having reduced corrosion.
Embodiment 11 provides the method of any one of Embodiments 1-10, wherein the at least one corrosion-promoting ion is formate.
Embodiment 12 provides the method of any one of Embodiments 4-11, wherein the purging and replacing steps are sufficient to maintain a concentration of formate ion in the aqueous solution at or below about 15 wt %.
Embodiment 13 provides the method of any one of Embodiments 1-12, wherein the at least one corrosion-promoting ion is oxalate.
Embodiment 14 provides the method of Embodiment 13, wherein the purging and replacing steps are sufficient to maintain a concentration of the oxalate ion in the aqueous solution at or below about 0.4 wt %.
Embodiment 15 provides the method of any one of Embodiments 1-14, wherein the at least one corrosion-promoting ion is sulfate.
Embodiment 16 provides the method of Embodiment 15, wherein the purging and replacing steps are sufficient to maintain a concentration of the sulfate ion in the aqueous solution at or below about 200 ppm.
Embodiment 17 provides the method of any one of Embodiments 1-16, wherein the replacement aqueous solution includes the acid or the ammonium salt thereof.
Embodiment 18 provides the method of any one of Embodiments 1-17, further including forming the replacement aqueous solution by mixing water and the acid or the ammonium salt thereof.
Embodiment 19 provides the method of any one of Embodiments 1-18, further including producing solid ammonium salt from the purged aqueous solution as valuable material, wherein the solid ammonium salt is the ammonium salt of the acid.
Embodiment 20 provides the method of any one of Embodiments 1-19, further including forming the replacement aqueous solution by substantially removing the at least one corrosion-promoting ion from at least part of the purged aqueous solution.
Embodiment 21 provides the method of any one of Embodiments 1-20, wherein the purging occurs in at least one selected from an ammonia absorption tower, ammonia absorption tower top, ammonia sorption tower bottom, ammonia stripper tower, ammonia stripper tower top, ammonia stripper tower bottom, stripper tower reboiler, ammonia condenser, distillation column, heat exchanger, and transfer piping.
Embodiment 22 provides the method of any one of Embodiments 1-21, wherein the replacing occurs in at least one selected from an ammonia absorption tower, ammonia absorption tower top, ammonia sorption tower bottom, ammonia stripper tower, ammonia stripper tower top, ammonia stripper tower bottom, stripper tower reboiler, ammonia condenser, distillation column, heat exchanger, and transfer piping.
Embodiment 23 provides the method of any one of Embodiments 1-22, wherein the purging is performed at an average rate of about 1 lb of purged liquid for every about 100 lb to about 5,000 lb of aqueous solution that passes from the desorber to the absorber.
Embodiment 24 provides the method of any one of Embodiments 1-23, wherein the purging is performed at an average rate of about 1 lb of purged liquid for every about 500 lb to about 2000 lb of aqueous solution that passes from the desorber to the absorber.
Embodiment 25 provides the method of any one of Embodiments 1-24, wherein the replacing is performed at an average rate of about 1 lb of replacement liquid for every about 1,500 to about 15,000 lb of aqueous solution that passes from the desorber to the absorber.
Embodiment 26 provides the method of any one of Embodiments 1-25, wherein the replacing is performed at an average rate of about 1 lb of replacement liquid for every about 3000 to about 6000 lb of aqueous solution that passes from the desorber to the absorber.
Embodiment 27 provides the method of any one of Embodiments 1-26, wherein the ammonia desorber includes a stripper tower and a stripper tower reboiler.
Embodiment 28 provides the method of any one of Embodiments 3-27, wherein the corrosion of the ammonia desorber is reduced.
Embodiment 29 provides the method of any one of Embodiments 3-28, wherein corrosion of transfer piping between the ammonia absorber and the ammonia desorber is reduced.
Embodiment 30 provides the method of any one of Embodiments 1-29, wherein the acid is phosphoric acid, sulfuric acid, hydrochloric acid, nitric acid, or acetic acid.
Embodiment 31 provides the method of any one of Embodiments 1-30, wherein the ammonium salt is monoammonium phosphate or diammonium phosphate.
Embodiment 32 provides the method of any one of Embodiments 3-31, wherein reducing the corrosion includes a reduction in rate or severity of corrosion as compared to corrosion of corresponding equipment in an ammonia extraction process that does not include the purging and the replacing.
Embodiment 33 provides the method of any one of Embodiments 1-32, wherein the ammonia extraction equipment includes at least one of an ammonia absorption tower, ammonia absorption tower top, ammonia sorption tower bottom, ammonia stripper tower, ammonia stripper tower top, ammonia stripper tower bottom, stripper tower reboiler, ammonia condenser, distillation column, heat exchanger, and transfer piping.
Embodiment 34 provides the method of any one of Embodiments 1-33, wherein the ammonia is extracted from a gaseous or vaporous stream.
Embodiment 35 provides the method of any one of Embodiments 1-34, wherein the ammonia is extracted from a hydrogen cyanide generation process, a fertilizer production process, a wastewater purification process, an ammonia production process, a pollution prevention process, a fossil fuel combustion process, a coke manufacture process, a livestock management process, or a refrigeration process.
Embodiment 36 provides the method of any one of Embodiments 1-35, wherein the ammonia extraction process recovers unreacted ammonia from a hydrogen cyanide generation process.
Embodiment 37 provides the method of any one of Embodiments 1-36, wherein the ammonia is recovered from an Andrussow process for generating hydrogen cyanide.
Embodiment 38 provides the method of any one of Embodiments 3-37, wherein the at least one of the ammonia desorber and the reboiler for the ammonia desorber having reduced corrosion includes stainless steel.
Embodiment 39 provides the method of any one of Embodiments 3-38, wherein the at least one of the ammonia desorber and the reboiler for the ammonia desorber having reduced corrosion includes austenitic steel, ferritic steel, martensitic steel, a stainless steel series including 440A, 440B, 440C, 440F, 430, 316, 409, 410, 301, 301LN, 304L, 304LN, 304, 304H, 305, 312, 321, 321H, 316L, 316, 316LN, 316Ti, 316LN, 317L, 2304, 2205, 904L, 1925hMo/6MO, 254SMO series steel, or a combination thereof.
Embodiment 40 provides the method of any one of Embodiments 3-39, wherein the at least one of the ammonia desorber and the reboiler for the ammonia desorber having reduced corrosion includes superalloy, nickel-copper alloy, Monel 400, precipitation-strengthened nickel-iron-chromium alloy, Incoloy brand alloy, Incoloy 800 series, austenitic nickel-chromium-based Inconel brand alloy, nickel-chromium-molybdenum alloy, Hastelloy brand alloy, Hastelloy G-30, super austenitic stainless steel, AL6XN, 254SMO, 904L, duplex stainless steel, 2205, super duplex stainless steel, 2507, nickel-based alloy, C276, C22, C2000, 600, 625, 800, 825, titanium alloy, zirconium alloy, Zr 702, Hastelloy 276, duplex 2205, super duplex 2507, Ebrite 26-1, Ebrite 16-1, Hastelloy 276, Duplex 2205, 316 SS, 316L and 304SS, zirconium, zirconium clad 316, ferralium 255, or a combination thereof.
Embodiment 41 provides the method of any one of Embodiments 3-40, wherein the at least one of the ammonia desorber and the reboiler for the ammonia desorber having reduced corrosion includes 316L austenitic steel.
Embodiment 42 provides the method of any one of Embodiments 1-41, further including using a controller to control the purging or replacing such that the concentration of the at least one corrosion-promoting ion in the aqueous solution is maintained below a predetermined maximum concentration.
Embodiment 43 provides the method of Embodiment 42, wherein the purging and replacing are sufficient to reduce corrosion of at least one of the ammonia desorber and the reboiler for the ammonia desorber, further including using the amount of corrosion that has occurred to the at least one of the ammonia desorber and the reboiler for the ammonia desorber having reduced corrosion to determine the predetermined maximum concentration.
Embodiment 44 provides the method of Embodiment 43, wherein the amount of corrosion that has occurred is determined visually, or by instantaneous corrosion rate measurement.
Embodiment 45 provides a system for extracting ammonia with decreased corrosion, including: ammonia extraction equipment including an ammonia absorber, an ammonia desorber, and an aqueous solution including an acid or an ammonium salt thereof; a gaseous stream including ammonia, wherein in the ammonia absorber at least part of the ammonia in the gaseous stream is converted into an ammonium salt, in the ammonia desorber at least part of the ammonium salt is converted into ammonia, and the aqueous solution is circulated between the absorber and the desorber; a purge stream from the circulated aqueous solution including at least part of the aqueous solution including at least one corrosion-promoting ion selected from formate, oxalate, fluoride, chloride, sulfate, and sulfide; and a replacement stream to the circulated aqueous solution that has a reduced concentration of the at least one corrosion-promoting ion as compared to the purged part of the aqueous solution.
Embodiment 46 provides the system of Embodiment 45, wherein the purging and replacing are sufficient to reduce corrosion of at least one of the ammonia desorber and a reboiler for the ammonia desorber.
Embodiment 47 provides the system of any one of Embodiments 45-46, further including a controller, wherein the controller controls the purging or replacing such that the concentration of the at least one corrosion-promoting ion in the aqueous solution is maintained below a predetermined maximum concentration.
Embodiment 48 provides the system of Embodiment 47, further including a corrosion sensor, wherein the corrosion sensor measures the rate of corrosion, wherein the rate of corrosion is used to determine the predetermined maximum concentration.
Embodiment 49 provides a method of decreasing corrosion during ammonia extraction, including: performing a process to recover unreacted ammonia from a gaseous reactor effluent stream from an Andrussow process to generate hydrogen cyanide, wherein the process is performed using ammonia recovery equipment including an ammonia absorber, an ammonia desorber including an ammonia stripper tower and an ammonia stripper tower reboiler, and an aqueous solution including an acid or an ammonium salt thereof, wherein in the ammonia absorber at least part of the ammonia in the gaseous stream is converted into an ammonium salt, in the ammonia desorber at least part of the ammonium salt is converted into ammonia, and the aqueous solution is circulated between the absorber and the desorber; purging at least part of the aqueous solution, wherein the purged part of the aqueous solution includes at least one corrosion-promoting ion selected from formate, oxalate, fluoride, chloride, sulfate, and sulfide; and adding a replacement aqueous solution to the aqueous solution, wherein the replacement aqueous solution has a reduced concentration of the at least one corrosion-promoting ion as compared to the purged part of the aqueous solution; wherein the purging and replacing are sufficient to maintain a concentration of the at least the formate ion in the aqueous solution at or below about 15 wt %.
Embodiment 50 provides the apparatus or method of any one or any combination of Embodiments 1-49 optionally configured such that all elements or, options recited are available to use or select from.
This application claims benefit of priority from U.S. Provisional Application No. 61/673,508 filed Jul. 19, 2012. This application hereby incorporates by reference this application in its entirety.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/US2013/047355 | 6/24/2013 | WO | 00 |
| Number | Date | Country | |
|---|---|---|---|
| 61673508 | Jul 2012 | US |
