Patent Application
20050186131
The present invention relates to a process for producing 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 must be produced on-site.
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 Chlorine dioxide may be withdrawn from the reaction medium as a gas, as in the processes described by U.S. Pat. Nos. 5,091,166, 5,091,167 and EP patent 612686. The chlorine dioxide gas can then be absorbed in water to form an aqueous solution thereof. These are preferably large-scale processes which require extensive process equipment and instrumentation.
For production of chlorine dioxide in small-scale units, such as for water purification applications or small bleaching plants, it is favourable not to separate chlorine dioxide from the reaction medium but to recover a chlorine dioxide containing solution directly from the reactor, optionally after dilution with water. Such processes are described in U.S. Pat. Nos. 2,833,624, 4,534,952, 5,895,638, 6,790,427, in WO 00/76916, and in US patent applications Publ. No. 2004/0175322 and Publ. No. 2003/0031621, and have in recent years become commercial. The required process equipment and instrumentation is considerably less extensive than in the large-scale processes described above. However, there is still a need for further improvements.
In the small-scale processes it has been difficult to obtain solutions with such a high concentration of chlorine dioxide as desired for many applications, like recycle paper bleaching, bagasse bleaching, or small-scale pulp bleaching.
Another problem with the existing small-scale processes for chlorine dioxide production is that the chlorine dioxide concentration of the product may fluctuate depending on the chlorine dioxide production rate.
It is an object of the invention to provide a process for the production of chlorine dioxide enabling direct production of chlorine dioxide in an aqueous solution with a high chlorine dioxide concentration.
It is another object of the invention to provide a process for the production of chlorine dioxide enabling direct production of chlorine dioxide in an aqueous solution with a chlorine dioxide concentration that can be kept constant independently of the chlorine dioxide production rate.
It is still another object of the invention to provide an apparatus for performing the process.
It is a further object of the invention to provide a novel chlorine dioxide solution of high concentration.
It has surprisingly been found possible to meet these objects by providing a process for continuously producing chlorine dioxide comprising the steps of continuously:
feeding to a reactor an acid, a reducing agent and alkali metal chlorate; reacting the alkali metal chlorate with the acid and the reducing agent to form a product stream containing chlorine dioxide and the alkali metal salt of the acid; and, bringing said product stream from the reactor to an absorption tower, where it is contacted with a flow of water to form an aqueous solution containing chlorine dioxide.
It has been found that by bringing the product stream to an absorption tower it is possible to obtain an aqueous solution with a high concentration of chlorine dioxide, preferably above about 3 g/liter, most preferably above about 4 g/liter, without first separating the chlorine dioxide gas from the reaction medium and then absorbing it into water. Any soluble species such as alkali metal salt of the acid and unreacted feed chemicals are also absorbed in the absorption tower. The flow rate of the water to the absorption tower, 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 absorption tower can have a chlorine dioxide concentration of 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, from about 0.1 to about 1, preferably from about 0.2 to about 0.8.
By the term absorption tower 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. Gas and liquid preferably flow counter-currently. Inside the absorption tower 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 that can be used are sieve plates and bubble cap plates.
Preferably a device creating a subatmospheric pressure is connected to the absorption tower bringing the product stream, including any liquid, foam and gas therein, to flow into the absorption tower. The non-absorbed gas is withdrawn from the absorption tower by said device. Any commonly used devices such as fans, eductors etc. can be used, preferably an eductor. In the latter case the eductor is fed with motive water, which may be provided from a separate storage tank and a pump that only serves the eductor. The storage tank is preferably ventilated so that non-absorbed process gas can be removed.
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. Several reducing agents can be used e.g. hydrogen peroxide, methanol, chloride ions etc., of which hydrogen peroxide is most preferred. In the latter case where hydrogen peroxide is used, 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. 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 mole %, preferably below about 0.1 mole %, more preferably less than about 0.05 mole %, most preferably less than about 0.02 mole % Cl− of the ClO3−.
In the case that 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., as it then may be possible to operate the process substantially adiabatically. 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 U.S. 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 WO 00/76916, which hereby is incorporated by reference. Such a composition may be an aqueous solution comprising from about 1 to about 6.5 moles/liter, preferably from about 3 to about 6 moles/liter of alkali metal chlorate, from about 1 to about 7 moles/liter, preferably from about 3 to about 5 moles/liter 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/liter, most preferably from about 0.5 to about 3 mmoles/liter. If a protective colloid is present, its concentration is preferably from about 0.001 to about 0.5 moles/liter, most preferably from about 0.02 to about 0.05 moles/liter. If a radical scavenger is present, its concentration is preferably from about 0.01 to about 1 moles/liter, most preferably from about 0.02 to about 0.2 moles/liter. 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/liter, preferably below about 50 mmoles/liter, more preferably below about 5 mmoles/liter, most preferably below about 0.5 mmoles/liter.
The reduction of alkali metal chlorate to chlorine dioxide results in the formation of a product stream in the reactor, normally comprising both liquid and foam, and containing chlorine dioxide, alkali metal salt of the acid and, in most cases, some remaining unreacted feed chemicals. If hydrogen peroxide is used as reducing agent the product stream also contains oxygen. Chlorine dioxide and oxygen may be present both as dissolved in the liquid and as gas bubbles. If sulphuric acid is used the alkali metal salt is a sulphate salt. 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 temperature in the reactor is suitably maintained below the boiling point of the reactants and 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 U.S. patent application Publ. No. 2004/0175322.
The feeds, 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 process of the invention is particularly suitable for production of chlorine dioxide in small-scale, for example from about 0.5 to about 200 kg/hr, preferably from about 10 to about 150 kg/hr. A typical small-scale production unit 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. If more than one reactor is used then it is optional if every reactor is connected to a separate absorption tower and a separate device creating a subatmospheric pressure or if all reactors are connected to one single absorption tower and one device creating a subatmospheric pressure.
The invention further relates to a novel aqueous solution containing chlorine dioxide that can be produced by the process as described above. The chlorine dioxide concentration in the novel aqueous solution is from about 4 to about 12 g/liter, preferably from about 4 to about 8 g/liter, most preferably from about 4 g/liter to about 6 g/liter. The pH of the novel aqueous chlorine dioxide solution is from about 0.1 to about 1, preferably from about 0.2 to about 0.8. The sulphate concentration in the aqueous solution is from about 1.1 moles/mole ClO2 to about 3.8 moles/mole ClO2, preferably from about 1.1 moles/mole ClO2 to about 3.2 moles/mole ClO2. The residual chlorate concentration in the aqueous solution 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 invention further relates to an apparatus for producing chlorine dioxide according to the above described process. The apparatus comprises a reactor provided with one or more feed lines for alkali metal chlorate, hydrogen peroxide and acid, the reactor being connected to an absorption tower. The apparatus further comprises a device for creating a subatmospheric pressure in the reactor and the absorption tower. Such a device is preferably an eductor fed with motive water.
The process of the invention makes it possible to produce an aqueous solution with a high chlorine dioxide concentration, i.e. above about 3 g/liter, preferably above about 4 g/liter, with equipment that is simple and easy to operate.
Preferred embodiments of the apparatus are apparent from the above description of the process and the following description referring to the drawings. The invention is, however, not limited to the embodiments shown in the drawings and encompasses many other variants within the scope of the claims.
The FIGURE shows a schematic process diagram for an embodiment of the present invention.
Referring to the FIGURE, a preferably substantially tubular through-flow reactor 1 is supplied with sulphuric acid through a feed line 2 and a pre-mixed aqueous solution of sodium chlorate and hydrogen peroxide through a feed line 3. In the reactor 1 the feed streams are mixed and reacted to form a product stream of liquid, foam and gas comprising chlorine dioxide, oxygen, sodium sulphate and some remaining sulphuric acid and sodium chlorate. The product stream is brought to the lower end of an absorption tower 4 which is fed with water at the top 6. The chlorine dioxide is absorbed in the water to form a product solution that is withdrawn from the absorption tower at the bottom 5.
To create a subatmospheric pressure in the reactor 1 and the absorption tower 4 an eductor 7 is connected to the absorption tower. The eductor 7 is fed with motive water that is recirculated through a storage tank 8 and then pumped through the eductor by a pump 9.
The motive water storage tank is ventilated so that any product gas not absorbed in the absorption tower, such as oxygen, can be removed.
| Number | Date | Country | |
|---|---|---|---|
| 60546199 | Feb 2004 | US |
