Patent Application
20070237708
The present invention relates to a process and a production unit for the production of chlorine dioxide from alkali metal chlorate, acid and a reducing agent.
Chlorine dioxide is used in various applications such as pulp bleaching, fat bleaching, water purification and removal of organic materials from industrial wastes. Since chlorine dioxide is not storage stable, it is generally produced on-site.
In large scale processes chlorine dioxide is usually produced by reacting alkali metal chlorate with a reducing agent in an aqueous reaction medium. Chlorine dioxide may be withdrawn from the reaction medium as a gas, like in the processes described in e.g. U.S. Pat. Nos. 5,091,166, 5,091,167 and EP patent 612686. Normally the chlorine dioxide gas is then absorbed into water to form an aqueous solution thereof. These large-scale processes are highly efficient but require extensive process equipment and instrumentation.
For the production of chlorine dioxide from alkali metal chlorate in small-scale units, such as for water purification applications or small bleaching plants, the chlorine dioxide is usually not separated from the reaction medium. Instead, a product stream comprising chlorine dioxide, salt, excess acid and optionally un-reacted chlorate is withdrawn from the reactor and used directly, usually after dilution with water in an eductor. Such processes have in recent years become commercial and are described in e.g. U.S. Pat. Nos. 2,833,624, 4,534,952, 5,895,638, 6,387,344, 6,790,427 and 7,070,710, and in US patent applications Publ. No. 2004/0175322, Publ. No. 2003/0031621, Publ. No 2005/0186131 and Publ. No. 2006/0133983. The required process equipment and instrumentation are considerably less extensive than in the large-scale processes described above. However, for some applications where small-scale units would be suitable, it may be desirable to obtain the chlorine dioxide as a gas phase, or as an aqueous solution of high concentration and/or without the excess acid and salt by-product.
It is an object of the invention to provide a simple process for the production of chlorine dioxide of high concentration and/or being substantially free from excess acid and salt by-product.
It another object of the invention to provide a production unit for performing the process.
It has been found possible to meet these objects in a process where a product stream from a reactor is diluted in an eductor fed with a gaseous motive stream. Thus, one aspect of the invention concerns a process for the production of chlorine dioxide, said process comprising the steps of continuously: feeding to a reactor an acid, alkali metal chlorate and a reducing agent; reacting the alkali metal chlorate with the acid and the reducing agent to form a product stream comprising chlorine dioxide, water and alkali metal salt of the acid; and, bringing the product stream from the reactor to an eductor and mixing it with a gaseous motive stream fed to the eductor and thereby forming a diluted product stream. This diluted product stream can be used as such, e.g. as a bleaching agent, for water purification or any other suitable application for chlorine dioxide, but can also be treated in one or more unit operations.
An embodiment of the invention further comprises the steps of bringing the diluted product stream to a gas-liquid separator; separating gas from liquid in the diluted product stream to form a gas stream comprising chlorine dioxide; and, withdrawing the gas stream comprising chlorine dioxide from the gas-liquid separator. This gas stream can be used as such in any suitable application for chlorine dioxide in gas phase such as bleaching or water purification, or be treated in one or more unit operations, such as absorption into water. In the latter case, the process preferably further comprises the steps of bringing the gas stream comprising chlorine dioxide from the gas-liquid separator to an absorber; contacting said gas stream with a flow of water to form an aqueous solution containing chlorine dioxide; and, withdrawing the aqueous solution containing chlorine dioxide from the absorber. This aqueous solution may then be used for any suitable application such as bleaching or water purification.
Another embodiment of the invention comprises the steps of bringing the diluted product stream from the eductor to an absorber; contacting the diluted product stream with a flow of water to form an aqueous solution containing chlorine dioxide; and, withdrawing the aqueous solution containing chlorine dioxide from the absorber. Thus, the diluted product stream is brought to the absorber without any previous gas-liquid separation. The aqueous solution obtained may be used for any suitable application such as bleaching or water purification.
Using a gaseous motive stream instead of a liquid for the eductor enables production of chlorine dioxide of high concentration and/or substantially free from excess salts and acid with comparatively low duty on following unit operations such as gas-liquid separation and/or absorption. Moreover, the need for adding inert gas at a later stage to further dilute the chlorine dioxide to minimize the risk for decomposition is reduced and in some cases eliminated.
The reactor can be operated as described in the earlier mentioned U.S. Pat. Nos. 2,833,624, 4,534,952, 5,895,638, 6,387,344, 6,790,427 and 7,070,710, and US patent application Publ. No. 2004/0175322, Publ. No. 2003/0031621 and Publ No. US2005/0186131, which hereby are incorporated as references.
Any reducing agent commonly used in chlorine dioxide production such as sulphur dioxide, chloride, methanol and hydrogen peroxide can be used, of which hydrogen peroxide is particularly preferred.
The alkali metal chlorate is suitably fed to the reactor as an aqueous solution. The alkali metal may, for example, be sodium, potassium or mixtures thereof, of which sodium is most preferred. The acid is preferably a mineral acid such as sulfuric acid, hydrochloric acid, nitric acid, perchloric acid or mixtures thereof, of which sulfuric acid is most preferred. If the reducing agent is hydrogen peroxide, the molar ratio H2O2 to ClO3− fed to the reactor is suitably from about 0.2:1 to about 2:1, preferably from about 0.5:1 to about 1.5:1, most preferably from about 0.5:1 to about 1:1. Usually it is preferred that the molar ratio of reducing agent to chlorate is at least stoichiometric. Alkali metal chlorate always contains some chloride as an impurity, but it is fully possible also to feed more chloride to the reactor, such as metal chloride or hydrochloric acid. However, in order to minimize the formation of chlorine it is preferred to keep the amount of chloride ions fed to the reactor low, suitably below about 1 mol %, preferably below about 0.1 mol %, more preferably less than about 0.05 mol %, most preferably less than about 0.02 mol % Cl− of the ClO3− (including chloride present in the chlorate as an impurity from the production thereof).
In the case sulfuric acid is used as a feed to the reactor, it preferably has a concentration from about 60 to about 98 wt %, most preferably from about 70 to about 85 wt % and preferably a temperature from about 0 to about 80° C., most preferably from about 20 to about 60° C. Preferably from about 2 to about 7 kg H2SO4, most preferably from about 3 to about 5 kg H2SO4 is fed per kg ClO2 produced. In order to use sulphuric acid of high concentration, a dilution and cooling scheme as described in US patent application Publ. No. 2004/0175322 is preferably applied.
In a particularly preferred embodiment alkali metal chlorate and hydrogen peroxide is fed to the reactor in the form of a premixed aqueous solution, for example a composition as described in U.S. Pat. No. 7,070,710. Such a composition may be an aqueous solution comprising from about 1 to about 6.5 moles/litre, preferably from about 3 to about 6 moles/litre of alkali metal chlorate, from about 1 to about 7 moles/litre, preferably from about 3 to about 5 moles/litre of hydrogen peroxide and at least one of a protective colloid, a radical scavenger or a phosphonic acid based complexing agent, wherein the pH of the aqueous solution suitably is from about 0.5 to about 4, preferably from about 1 to about 3.5, most preferably from about 1.5 to about 3. Preferably, at least one phosphonic acid based complexing agent is present, preferably in an amount from about 0.1 to about 5 mmoles/litre, most preferably from about 0.5 to about 3 mmoles/litre. If a protective colloid is present, its concentration is preferably from about 0.001 to about 0.5 moles/litre, most preferably from about 0.02 to about 0.05 moles/litre. If a radical scavenger is present, its concentration is preferably from about 0.01 to about 1 moles/litre, most preferably from about 0.02 to about 0.2 moles/litre. Particularly preferred compositions comprise at least one phosphonic acid based complexing agent selected from the group consisting of 1-hydroxyethylidene-1,1-diphosphonic acid, 1-aminoethane-1,1-diphosphonic acid, aminotri (methylenephosphonic acid), ethylene diamine tetra (methylenephosphonic acid), hexamethylene diamine tetra (methylenephosphonic acid), diethylenetriamine penta (methylenephosphonic acid), diethylenetriamine hexa (methylenephosphonic acid), 1-aminoalkane-1,1-diphosphonic acids (such as morpholinomethane diphosphonic acid, N,N-dimethyl aminodimethyl diphosphonic acid, aminomethyl diphosphonic acid), reaction products and salts thereof, preferably sodium salts. Useful protective colloids include tin compounds, such as alkali metal stannate, particularly sodium stannate (Na2(Sn(OH)6). Useful radical scavengers include pyridine carboxylic acids, such as 2,6-pyridine dicarboxylic acid. Suitably the amount of chloride ions is below about 300 mmoles/litre, preferably below about 50 mmoles/litre, more preferably below about 5 mmoles/litre, most preferably below about 0.5 mmoles/litre.
The temperature in the reactor is suitably maintained below the boiling point of the reactants and the liquid part of the product stream at the prevailing pressure, preferably from about 20 to about 80° C., most preferably from about 30 to about 60° C. The pressure maintained within the reactor is suitably slightly subatmospheric, preferably from about 30 to about 100 kPa absolute, most preferably from about 65 to about 95 kPa absolute.
The reactor may comprise one or several vessels, for example arranged vertically, horizontally or inclined. The reactants may be fed directly to the reactor or via a separate mixing device. Suitably the reactor is a preferably substantially tubular through-flow vessel or pipe, most preferably comprising means for mixing the reactants in a substantially uniform manner. Such means for mixing are described in e.g. U.S. Pat. No. 6,790,427 and US patent application Publ. No. 2004/0175322.
The feed chemicals, including acid, alkali metal chlorate and reducing agent, are preferably fed close to one end of the reactor and the product stream is preferably withdrawn at the other end of the reactor.
The length (in the main flow direction) of the reactor used is preferably from about 150 to about 1500 mm, most preferably from about 300 to about 900 mm. It has been found favourable to use a substantially tubular reactor with an inner diameter from about 25 to about 300 mm, preferably from about 50 to about 150 mm. It is particularly favourable to use a substantially tubular reactor having a preferred ratio of the length to the inner diameter from about 12:1 to about 1:1, most preferably from about 8:1 to about 4:1. A suitable average residence time in the reactor is in most cases from about 1 to about 60 seconds, preferably from about 3 to about 20 seconds.
The reaction between alkali metal chlorate, acid and reducing agent results in the formation of a product stream comprising chlorine dioxide, alkali metal salt of the acid, water and, in most cases some remaining unreacted feed chemicals. If hydrogen peroxide is used as reducing agent, the product stream also comprises oxygen. If sulfuric acid is used as acid, the product stream comprises alkali metal sulfate. In most cases the product stream comprises both liquid and gas and may at least partly be in the form of foam. Chlorine dioxide and oxygen may be present both as dissolved in the liquid and as gas bubbles, while the alkali metal salt of the acid usually is dissolved in the liquid.
It has been found possible to achieve a conversion degree of alkali metal chlorate to chlorine dioxide from about 75% to 100%, preferably from about 80 to 100%, most preferably from about 95 to 100%.
The product stream withdrawn from the reactor, including any liquid and gas therein, is brought to the eductor, preferably by a suction force created by the eductor. The product stream is then mixed in the eductor with the gaseous motive stream fed thereto to form a diluted product stream, usually also comprising both liquid and gas. Any kind of eductor that can be operated with a gaseous motive stream may be used, and such eductors are also commercially available. The gaseous motive stream, also referred to as motive gas, is preferably a gas or mixture of gases that is inert in respect of chlorine dioxide. Examples of such gases include nitrogen, oxygen and noble gases. For practical and economical reasons air is preferred.
In the embodiments in which the diluted product stream from the eductor is brought to a gas-liquid separator, at least part of the gas dissolved in the liquid therein is separated therefrom. To facilitate the separation inert gas may be added to the diluted product stream, either within the gas-liquid separator or prior to entering the separator. Depending on how much gas that has been mixed into the product stream in the eductor, inert gas added in connection with gas-liquid separation may also serve the purpose of further diluting the chlorine dioxide and thereby minimising the risk for decomposition. In some cases inert gas may be introduced into to the gas stream leaving the gas-liquid separator. Any inert gas suitable as motive gas for the eductor can be used also for the gas-liquid separator. The gas stream withdrawn preferably comprises from about 1 to about 15 wt %, most preferably from about 3 to about 12 wt % of chlorine dioxide. Low concentrations are desirable for some applications like treatment of flue gas, while high concentrations are preferable in embodiments where the gas stream are brought to an absorber to produce an aqueous solution containing chlorine dioxide.
In order to facilitate the gas-liquid separation the temperature in the separator is preferably maintained from about 30 to about 90° C., most preferably from about 40 to about 80° C., particularly from about 50 to about 75° C.
In some cases it may be favourable to separate only part of the chlorine dioxide and thus withdraw in the gas stream, for example, from about 20 to about 80% or from about 30 to about 70% of the chlorine dioxide from the diluted product stream. In order to utilise the chlorine dioxide remaining in the liquid phase, this may at least partly be recovered as a liquid product and used for bleaching or water treatment where the remaining acid, salt and other possible by-products do not make any significant harm.
The term gas-liquid separator as used herein, refers to any kind of equipment suitable for separating gas and liquid. Examples of gas-liquid separators are stripper columns, cyclone separators, vented tanks, etc.
Examples of stripper columns include plate columns, packed bed columns and wetted-wall (falling film) columns. In an embodiment the stripper column is a packed bed column that may comprise any kind of standard packing, examples of which include Raschig rings, Berl saddles, Intalox saddles etc. A stripper column is preferably operated by entering the diluted product stream into the upper part of the column and blowing inert gas into the lower part thereof. The liquid phase is then preferably collected at the bottom of the column and withdrawn while the gas stream comprising chlorine dioxide can be withdrawn at any position above the liquid level.
Examples of cyclone separators include those comprising a substantially cylindrical or at least partially conical vessel where the diluted product stream from the eductor is introduced substantially tangentially into the vessel, preferably into the upper part thereof. The liquid phase is preferably leaving the vessel at the bottom while the gas stream comprising chlorine dioxide preferably is leaving at the upper part of the vessel. To further facilitate the gas-liquid separation the cyclone separator is preferably operated at subatmospheric pressure. In case inert gas is added, it is preferably introduced directly into the cyclone separator or to the diluted product stream prior to entering the cyclone separator or to the gas stream leaving the gas-liquid separator.
In case a tank is used as a gas-liquid separator it is preferably supplied with a blower for inert gas close to the bottom.
The gas stream comprising chlorine dioxide may be withdrawn from the gas-liquid separator by any suitable means e.g. a device creating a subatmospheric pressure, such as a fan. The device may, for example, be placed directly after the gas-liquid separator or after an optional absorber.
In case the diluted product stream from the eductor is brought to an absorber, soluble species such as alkali metal salt of the acid and unreacted feed chemicals are also absorbed into the water, while gaseous components with limited solubility, like oxygen, are withdrawn in a gas phase. The flow rate of the water to the absorber, either chilled or not, is preferably adjustable so that the chlorine dioxide concentration can be kept constant independently of the production rate. The aqueous solution obtained in the absorber can have a chlorine dioxide concentration within a wide range, for example from about 0.1 g/liter to about 12 g/liter, preferably from about 3 g/liter to about 10 g/liter, most preferably from about 4 g/liter to about 8 g/liter. The concentration of unreacted chlorate in the aqueous solution, which is dependent on the conversion degree, is suitably below about 0.33 moles/mole ClO2, preferably below about 0.11 moles/mole ClO2, most preferably below about 0.053 moles/mole ClO2. The alkali metal salt concentration is dependent on the chlorine dioxide concentration and is suitably from about 0.74 mmoles/liter to about 59 mmoles/liter. The pH of the aqueous solution can vary within a wide range, partly dependent of the chlorine dioxide concentration, for example from about 0.1 to about 1, preferably from about 0.2 to about 0.8.
If a gas stream comprising chlorine dioxide from a gas-liquid separator is brought to an absorber, this is also operated as described above with the exception that non-gaseous components are not included. Thus, it is then possible to obtain an aqueous solution of chlorine dioxide substantially free from unreacted acid fed to the reactor or salts thereof, as well as of unreacted chlorate. The chlorine dioxide concentration of such a solution may be as stated above, while the pH in most cases is from about 2 to about 4.
By the term absorber as used herein is meant any column or tower or the like where gas is contacted with a liquid flow to absorb soluble compounds therein, preferably in a continuous counter-current flow. Inside the absorber are preferably placed devices such as plates or packing elements to provide interfacial surfaces where the mass transfer between the gas and the liquid can take place. Examples of useful packing elements include Raschig rings, Berl saddles, Intalox saddles etc. Examples of plates include sieve plates and bubble cap plates.
The process of the invention is particularly suitable for the production of chlorine dioxide in small-scale, for example from about 0.5 to about 250 kg ClO2/hr, preferably from about 10 to about 150 kg ClO2/hr.
A typical small-scale production unit of the invention normally includes only one reactor, although it is possible to arrange several, for example up to about 15 or more reactors in parallel, for example as a bundle of tubes.
The invention further concerns a production unit for the production of chlorine dioxide, said unit comprising a reactor provided with one or more feed inlets for acid, reducing agent and alkali metal chlorate and an outlet for a product stream; an eductor connected to the reactor provided with an inlet for a gaseous motive stream, means for mixing a product stream comprising chlorine dioxide from the reactor with the gaseous motive stream to obtain a diluted product stream, and an outlet for said diluted product stream.
In an embodiment the production unit further comprises a gas-liquid separator connected to the outlet of the eductor, means for withdrawing a gas stream comprising chlorine dioxide from the gas-liquid separator, and optionally an absorber and means for bringing the gas stream comprising chlorine dioxide to the absorber.
In an another embodiment the production unit comprises an absorber and means for bringing the diluted product stream from the eductor to the absorber.
The production unit of the invention is particularly suitable for use in the process of the invention and regarding further optional and preferred features the above description of the process is referred to.
Embodiments of the invention will now be described with reference to the enclosed drawing. The scope of the invention is, however, not limited to these embodiments but only to the scope of the appended claims.
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The process equipment, including the reactor 1, the eductor 3 and the optional gas-liquid separator 6 and absorber 10, are suitably made from materials resistant to the chemicals they are in contact with, such as one or more of hydrogen peroxide, sodium chlorate, sulfuric acid and chlorine dioxide. Such materials include, for example, glass, tantalum, titanium, fiberglass reinforced plastic, fluoro plastics like PVDF (polyvinylidene fluoride) CPVC (chlorinated polyvinyl chloride), PTFE (polytetrafluoro ethylene), PFA (perfluoro alkoxy polymer), ECTFE (ethylene chlorotrifluoro ethylene) or FEP (fluorinated ethylene propylene), or the use of these materials as a liner material to a structural material like steel or stainless steel. Suitable fluoro plastics are sold under the trademarks Kynar®, Teflon® or Halar®.
| Number | Date | Country | |
|---|---|---|---|
| 60790523 | Apr 2006 | US |
