Patent Application
20090260993
The invention relates to a method for obtaining sodium carbonate crystals. More particularly, it relates to a method for obtaining sodium carbonate crystals from a sodium hydroxide solution obtained by electrolysis.
Alkali metal carbonates and sodium carbonate in particular are very widespread industrial products with many applications. In the glass industry, sodium carbonate is an essential ingredient for easier processing of the glass. The detergent, textiles, pulp and paper industries are also examples of industries consuming a large quantity of sodium carbonate.
Due to this extremely high consumption, methods for producing sodium carbonate are of great economic and environmental importance.
Sodium carbonate can be obtained by purifying natural sodium carbonate extracted from trona deposits or by synthesis. Most synthetic sodium carbonate is currently produced by the “SOLVAY” process also called the ammonia process. In this process, ammonia is absorbed by a sodium chloride solution. The ammoniacal brine thus formed is contacted with carbon dioxide to produce bicarbonate, which is separated from the mother liquor and then calcined. The ammonia present in the mother liquor and the carbon dioxide liberated during calcination are recovered and recycled.
However, this process requires extremely high investments.
In patent BE861527 of the applicant, another method is described, in which an aqueous sodium chloride solution is electrolyzed in a cell with a membrane selectively permeable to the ions in order to produce chlorine and an aqueous sodium hydroxide solution which is carbonated and then evaporated to produce sodium carbonate crystals. In this method, the carbonation is carried out by mixing the sodium hydroxide with a bicarbonated solution in the electrolyzer. However, an efficient carbonation by liquid mixing has proved difficult to achieve.
It is the object of the invention to provide a simplified method, easy to implement and suitable for the economical production of crystals of sodium carbonate.
In consequence, the invention relates to a method for producing sodium carbonate, according to which an aqueous sodium chloride solution is electrolyzed in a cell with a membrane selectively permeable to ions in order to produce chlorine, hydrogen and an aqueous solution comprising sodium hydroxide, and the aqueous solution comprising sodium hydroxide is carbonated. According to the invention, the carbonation is carried out by directly contacting carbon dioxide with the aqueous solution comprising sodium hydroxide under conditions such as to cause the conversion of the aqueous solution into an aqueous slurry of anhydrous sodium carbonate crystals.
In the method according the invention, the cell with an ion permselective membrane is typically an electrolytic cell comprising at least one anode chamber and at least one cathode chamber separated by at least one membrane substantially impermeable to liquids (mainly aqueous solutions), but selectively permeable to ions. Membrane-type electrolytic cells are well known in the prior art and commonly used for producing aqueous sodium hydroxide solutions by the electrolysis of aqueous sodium chloride solutions.
In the method according to the invention, it is preferable for the membrane of the cell to be cation permselective. By definition, when such a membrane is contacted with an electrolyte between an anode and a cathode, it is crossed by cations of the electrolyte but is substantially impermeable to the transfer of anions.
In this preferred embodiment of the invention, the aqueous sodium chloride solution is introduced into the anode chamber of the cell and the aqueous sodium hydroxide solution is generated in the cathode chamber of the cell. Simultaneously, chlorine is produced in the anode chamber and hydrogen is produced in the cathode chamber.
According to a first aspect of the invention, the aqueous sodium hydroxide solution is drawn off outside the cell, before carbonation, and is carbonated in a reactor located outside the cell.
The carbonation of the aqueous sodium hydroxide solution is carried out by direct contact of the said solution with a gas containing carbon dioxide, in a gas-liquid contactor, under conditions regulated to crystallize anhydrous sodium carbonate. Data concerning the gas containing the carbon dioxide are given below.
The method according to the invention has the particular feature of a reaction in the presence of three distinct phases: a liquid phase, a gas phase and a crystalline solid phase in suspension in the liquid phase. Accordingly, the gas liquid contactor is advantageously a reactor adapted to the coexistence of these three phases.
In a particular embodiment of the invention, it is recommended to circulate the aqueous sodium hydroxide solution in countercurrent to the gas containing carbon dioxide, in a reactor comprising a tower consisting of the stack of at least two superimposed segments, separated by a partition perforated with at least two openings, the segments comprising at least one transverse wall for causing circulation of the solution in the said segment. Such a reactor facilitates and accelerates the reaction of the gas with the liquid and, in consequence, the crystallization of the sodium carbonate.
In a preferred embodiment of the method according to the invention, the aqueous solution containing sodium hydroxide is essentially free of carbonate and/or bicarbonate ions when directly contacted with the carbon dioxide. In this embodiment of the invention, subjecting the said aqueous solution to a carbonation or a partial bicarbonation before contacting it directly with the carbon dioxide is therefore explicitly avoided.
In a recommended variant of the method according to the invention, the slurry collected from the carbonation or its mother liquor is subjected to evaporation. The evaporation has the function of causing additional crystallization. It is normally effected in an evaporator-crystallizer. This unit is not critical for the definition of the invention. A multistage evaporator or a mechanical vapour recompression evaporator is advantageously used.
In a first embodiment of this variant, the slurry is subjected to evaporation as such.
In a second embodiment of the variant, the slurry is first subjected to a mechanical separation of the crystals that it contains and the resulting mother liquor (aqueous sodium carbonate solution) is then subjected to evaporation.
The separation of the crystals from the slurry, before and/or after the evaporation can be carried out by any appropriate mechanical separating means, for example by settling, by centrifugation, by filtration or by a combination of these three separating means.
The mother liquor collected from the mechanical separation that follows the evaporation essentially consists of an aqueous sodium carbonate solution. It may advantageously be used to purify the aqueous sodium chloride solution, to be fed to the membrane type electrolytic cell. The crystals collected from the mechanical separation that follows the evaporation are then dried into anhydrous sodium carbonate crystals. To that end, use can be made of rotary dryers or of fluidized beds. The rotary dryers can be directly heated by combustion gases. It is however preferred to use indirect heating, for instance with steam circulating into an array of pipes.
In an advantageous embodiment of the invention, the electrolysis in the membrane-type cell is regulated so that the aqueous sodium hydroxide solution contains 25 to 40 (preferably 30 to 35%) by weight of sodium hydroxide.
The temperature inside the gas-liquid contactor, where the aqueous sodium hydroxide solution is carbonated, is preferably at a value above 100° C. Temperatures above 105 (preferably above 110)° C. and lower that 150 (preferably 140)° C. are advantageously used. Temperatures from 115 to 140° C. are specially preferred. It is recommended that such temperatures are reached sensibly everywhere in the contactor. It is essential that at least 90%, preferably 95%, more preferably 99%, most preferably 100% in weight of the sodium carbonate is in anhydrous form. The exothermic nature of the carbonation helps to get such high temperatures. In order to get full advantage of the exothermic nature of the reaction, it is recommended that the gas liquid contactor be thermally insulated.
It has to be noted that in the corresponding variant of execution of the invention, the operating conditions in the evaporator-crystallizer are however regulated in temperature and pressure so that the sodium carbonate which are produced essentially consist of crystals of sodium carbonate monohydrate. The anhydrous crystals produced in the gas-liquid contactor are then converted inside the crystallizer into monohydrate crystals.
The conversion according to the invention of the aqueous solution comprising sodium hydroxide into an aqueous slurry of sodium carbonate crystals which are anhydrous has the advantage of reducing the energy needed in the subsequent evaporation, compared to the situation where the aqueous slurry comprises monohydrate sodium carbonate crystals, despite the fact that such anhydrous crystals are advantageously subsequently converted in monohydrate crystals in an evaporator-crystalliser.
In a advantageous embodiment of the invention, at least part of the produced chlorine is utilized in a vinyl chloride monomer (VCM) production plant, at least part of the hydrochloric acid produced by the vinyl chloride monomer plant being reacted with limestone to produce at least part of the carbon dioxide used for the carbonation. In this embodiment it is advantageous to use a so called “simplified VCM”, which is a VCM production plant without oxychloration. Indeed, the hydrochloric acid produced in the pyrolysis is reacted with limestone and need not be absorbed in an oxychloration process. In other embodiments, at least part of the produced hydrogen is utilized in an hydrogen peroxide plant and/or part of the produced chlorine is utilized in a MDI (methylene diphenyl diisocyanate) and TDI (toluene diisocyanate) plant. In this last embodiment it is recommended that the hydrochloric acid produced in the MDI/TDI plant is valorized in a VCM plant based at least in part on a oxychloration process.
In the method according to the invention, the gas containing carbon dioxide may be a rich gas or a lean gas. Rich gas containing at least 50%, if possible 60%, preferably 70%, more preferably 80%, most preferably 90% carbon dioxide is recommended. In an advantageous embodiment of the invention, the rich gas is obtained by attacking limestone with an aqueous hydrochloride acid solution, which is obtained by absorbing, in water, hydrogen chloride that is obtained by reacting chlorine and hydrogen produced in the membrane-type cell. In this embodiment, it is particularly advantageous to retrieve the energy produced by the exothermicity of the reaction of hydrogen with chloride and use it to dry the monohydrate sodium carbonate produced f.i. in the evaporator crystalliser (3).
In another embodiment of the invention, using lean gas, this comprises a flue gas issuing from a thermal installation for instance a cogeneration of heat and power.
The cogeneration installation advantageously at least partly supplies a proximate chlorine derivative production unit which generates carbon dioxide used by the sodium carbonate production unit with electricity and/or steam. It also advantageously supplies the electrolyzer with electricity and the evaporator with steam.
In the method according to the invention, a dilute brine of sodium chloride is collected from the membrane-type cell. This brine may be discharged or used in another production unit.
In a preferred embodiment of the invention, the dilute brine collected from the membrane-type cell is recycled in the anode chamber of the cell, after having been purified and concentrated with sodium chloride. Purification commonly and conventionally comprises, in a known way, a dechlorination, a dechloratation and a desulphation. To concentrate the dilute brine, solid sodium chloride, for example rock salt, can be added to it. It is preferable to circulate it through a rock salt deposit.
The concentrated brine must be stripped, particularly of calcium ions, magnesium ions and sulphate ions. To strip the concentrated brine of calcium ions, it can advantageously be treated with a fraction of the mother liquor from the sodium carbonate crystallization. To strip it of magnesium ions, it can be treated with a fraction of the aqueous sodium hydroxide solution produced in the electrolytic cell.
The method according to the invention is suitable for easily and economically producing high purity sodium carbonate, particularly from optimum-grade concentrated caustic soda, without requiring a costly industrial investment.
Particular features and details of the invention will appear from the non limiting description below of the drawings appended hereto.
In these figures, similar reference numerals denote the same elements.
The installation shown schematically in
The electrolytic cell 1 is of the type with cation permselective membranes. It comprises anode chambers and cathode chambers which are separated from the anode chambers by cation permselective membranes. The cell may be of the single-pole or two-pole type.
Cells with cation permselective membranes are well known in electrolytic technique and widely used for the industrial production of aqueous sodium hydroxide solutions from brines or aqueous sodium chloride solutions.
According to the invention, an aqueous solution 5 substantially saturated with sodium chloride is introduced into the anode chambers of the electrolytic cell 1, and water 6 is introduced into the cathode chambers of the cell. During electrolysis, chlorine 7 is generated in the anode chambers of the cell and extracted therefrom. Simultaneously, hydrogen 8 and an aqueous sodium hydroxide solution 9 are produced in the cathode chambers and extracted therefrom.
The chlorine 7 and the hydrogen 8 are sent to a reaction chamber 10 that is also supplied with a defined flow rate of water 11. An aqueous hydrochloric acid solution 12 is extracted from the chamber 10 and sent to a reactor 13, supplied with limestone 14. In the reactor 13, the limestone is attacked and decomposed by the hydrochloric acid to produce a gas 15 containing carbon dioxide and a waste aqueous solution of calcium chloride 39.
The aqueous sodium hydroxide solution 9 and the gas containing the carbon dioxide 15 are sent to the carbonation tower 2, where they are circulated in countercurrent and in contact with each other. In an advantageous embodiment, to intensify the contact of the gas with the aqueous solution and, consequently, the yield of the reaction between the gas and the solution, the column consists of the stack of several segments, separated by substantially horizontal or slightly inclined partitions. Each partition is perforated with an opening near its periphery, for the downflow of the solution, and with one or a plurality of openings in its central zone, for the upflow of the gas. The segments are further compartmentalized by vertical partitions forming baffles for the circulation of the solution.
A temperature of about 130° C. is maintained in the carbonation tower 2 in order to crystallize anhydrous sodium carbonate.
An aqueous slurry of anhydrous sodium carbonate crystals 16 is collected in the carbonation tower 2, and immediately sent to the evaporator-crystallizer 3. In this unit, the slurry is subjected to controlled evaporation to crystallize sodium carbonate. Evaporation is normally effected at a near atmospheric pressure, and at a temperature corresponding to the crystallization of the sodium carbonate in monohydrate form. The slurry 17 collected from the evaporator-crystallizer 3 is advantageously sent to the centrifuge chamber 4 where the crystals of sodium carbonate monohydrate 18 and a mother liquor 19 are separated. In the centrifuge chamber 4, the crystals of sodium carbonate monohydrate can also be subjected to washing with a controlled stream of water, if necessary.
The mother liquor 19 from the crystallization of the monohydrate is split into two fractions 20 and 21. The fraction 20 is recycled in the evaporator-crystallizer 3. The destination of the fraction 21 will be explained below.
In the evaporator-crystallizer 3, steam 23 is also produced, condensed and sent to a rock salt deposit 22, where a saturated brine of sodium chloride 24 is collected. This is sent to a reactor 25, where the calcium and magnesium ions are stripped off with the fraction 21 of the mother liquor and with the fraction 40 of the aqueous sodium hydroxide solution produced in the electrolytic cell 1. The brine collected from the reactor 25 is then filtered (26) and purified (27), and then sent to the anode chambers of the electrolytic cell 1. Sludges 38 containing calcium carbonate are also collected from the reactor 25, and sent to the reactor 13.
The dilute brine 29 collected from the anode chambers of the electrolytic cell 1 is sent to a succession of reaction chambers 30, 31, 32, where it is successively subjected to dechloratation, dechlorination and desulphatation treatments. The dilute and purified brine 33 is then treated in a mechanical vapour recompression installation 34 to saturate it with sodium chloride. A substantially saturated brine 35 is collected from the apparatus 34, on the one hand, and sent to the anode chambers of the electrolytic cell 1, and, on the other, steam 36, which is condensed and sent to the rock salt deposit 22, with make-up water 37.
The method implemented in the installation in
The example below serves to illustrate the invention. It refers to
1.134.6 t/h of a substantially saturated brine (5), containing, per kg, 253 g of sodium chloride, 7.0 g of sodium sulphate and 740 g of water, are introduced into the anode chamber of the membrane-type cell (1). The following are obtained from the cell (1):
A fraction (40) of the sodium hydroxide solution (9), equal to 4.3 t/h, is sent to the purification reactor (25). The remainder of the aqueous sodium hydroxide solution is sent to the carbonation tower (2), maintained at a temperature of about 130° C. Thus 281.6 t/h of solution are sent to the carbonation tower (2), containing, per kg, 320 g of sodium hydroxide and 680 g of water.
49.6 t/h of carbon dioxide (15) are introduced into the carbonation tower (2), from which 48.7 t/h of water and 282.4 t/h of an aqueous slurry (16) containing 421 g of anhydrous sodium carbonate per kg, are withdrawn.
The slurry (16) is introduced into the evaporator-crystallizer (3) in a mixture with 262 t/h of mother liquor (20), containing, per kg, 281.9 g of dissolved sodium carbonate and 669 g of water. 162 t/h of water (23) and 382.3 t/h of slurry (17) containing 505 g of sodium carbonate per kg, are extracted from the evaporator-crystallizer (3). In the centrifuge chamber (4), the slurry (17) is introduced with 28.5 t/h of water (28) serving to wash the crystals of sodium carbonate. 142.6 t of crystals of sodium carbonate and 268 t/h of dilute mother liquor (19) are collected from the centrifuge chamber (4). After separation of the 262 t/h (20) recycled in the evaporator-crystallizer (3), the remainder of the dilute mother liquor (21) (6.2 t/h) is sent to the purification reactor (25).
The dilute brine (29) (830.1 t/h) extracted from the electrolytic cell (1) is treated in the purification installation (30, 31, 32), from which 772.7 t/h of dilute and purified brine (33) are extracted. This is sent to the mechanical vapour recompression installation (34), from which 577.6 t/h of saturated brine (35) and 195.1 t/h of water are collected and sent to the salt deposit (22). The saturated brine (35) contains 250 g of sodium chloride per kg. It is sent to the anode chamber of cell (1) with 557.0 t/h of saturated brine issuing from the brine purification reactors (25, 26, 27).
To produce the carbon dioxide used in the carbonation tower (2), the abovementioned hydrogen chloride (83.5 t/h) is dispersed in 185.8 t/h of water and the hydrochloric acid (12) thus produced is introduced into the reactor (13) with 111.6 t/h of limestone (14) and 19.1 t/h of sludge (38), issuing from the purification of the brine.
| Number | Date | Country | Kind |
|---|---|---|---|
| 06120691.8 | Sep 2006 | EP | regional |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP2007/059558 | 9/12/2007 | WO | 00 | 3/9/2009 |
