Summary of the invention
In view of this, the present invention need to provide a kind of simple producer for preparing the method for thimerosal and realize the method.For at least one in solving the problems of the technologies described above, purpose of the present invention is to provide a kind of method for preparing thimerosal.
Another object of the present invention is to provide a kind of producer for preparing thimerosal.
One aspect of the present invention has been to provide a kind of method for preparing thimerosal, and the method comprises the following steps:
A, first by solution of chlorate, hydrochloric acid soln and catalyzer placing response device, the heating;
In B, extraction step A, the reaction chlorine that is able to is main mixed gas;
C, step B gained mixed gas is passed in water, aeration makes thimerosal.
Wherein, in described steps A, solution of chlorate comprises the strong metal solution of chlorate such as sodium chlorate solution, potassium chlorate solution, and described solution of chlorate mass concentration is 20%-40%, hydrochloric acid soln mass concentration 25%-36%; Described heating comprises heating in water bath, oil bath heating and direct heating, and type of heating adopts corrosion-resistant heating tube, and described heating tube is provided with temperature detection and temperature controlling system.
Wherein, in described steps A, catalyzer can be MnCl
2, FeCl
2, FeCl
3, MnSO
4, FeSO
4, Fe
2(SO
4)
2one or more, the amount of described catalyzer is the 1%-3% of added solution of chlorate amount, is the 3%-5% of added hydrochloric acid soln amount, described catalyzer does not reclaim; The described temperature that is heated to is 70-90 degree centigrade, and the reaction times is 10-60 minute.
The negative pressure that wherein in step B, in extraction step A, the reaction chlorine that is able to is main mixed gas formation is-90--5KPa.
Wherein the input material volume ratio of the solution of chlorate in steps A and hydrochloric acid soln is 1.5-0.5, according to the difference that generates amount of chlorine, reaction volume is also different, and it is 1.0-1.7L that general every generation 1kg chlorine needs the reactant solution total amount, and this reaction can generate 1kg/h chlorine continuously;
Wherein in step B and C, every generation 1-10kg/h chlorine passes in the water in water sprayer, and aeration absorbs the water yield 1-20m
3/ h, form concentration 200-1000mg/l thimerosal.
In order to realize the foregoing invention purpose, the present invention also provides the producer that completes above-mentioned thimerosal preparation method, and described producer comprises: the solution of chlorate storage tank, hydrochloric acid tank, the hydrochloric acid volume pump, the hydrochloric acid Traffic Monitor, controller, the solution of chlorate import, the hydrochloric acid import, the air inlet snubber, venting, air outlet, water sprayer, liquid level detector, reactor, heating jacket, the reactor sewage draining exit, temperature sensor, the heating jacket sewage draining exit, heating tube, the heating jacket liquid adding hole, oxymuriate volume pump and oxymuriate Traffic Monitor, is characterized in that, the outlet of described solution of chlorate storage tank, the outlet of hydrochloric acid tank is connected with the import of hydrochloric acid volume pump with the import of oxymuriate volume pump respectively, described oxymuriate metering pump outlet, hydrochloric acid metering pump outlet is connected with the import of hydrochloric acid Traffic Monitor with the import of oxymuriate Traffic Monitor respectively, with the solution of chlorate import, with hydrochloric acid, import is connected respectively in the outlet of the outlet of described oxymuriate Traffic Monitor and hydrochloric acid Traffic Monitor, described solution of chlorate outlet, hydrochloric acid outlet is connected with the import of reactor respectively, the outlet of described reactor is connected with an end of air inlet snubber, venting, reactor sewage draining exit and air outlet respectively, and the other end of described air outlet is connected with water sprayer.
Described reactor head is provided with venting, bottom is provided with sewage draining exit, air inlet snubber entrance is connected with atmosphere, the outlet of air inlet snubber is connected with the reactor bottom inlet mouth, the reactor outer setting has the immersion heating jacket, by heating jacket, the reactant in reactor is heated, heating tube, temperature sensor, liquid level detector, heating jacket are installed on described heating jacket and are provided with liquid adding hole, its bottom is provided with sewage draining exit.
Described director port is connected respectively the liquid level for automatically controlling reacting by heating thing, the temperature that shows reactant, detecting reactant and controls reactant injection rate and work output with hydrochloric acid volume pump, hydrochloric acid Traffic Monitor, liquid level detector, temperature sensor port.
Described reactor material is the titanium material, is provided with venting, reactor sewage draining exit on it, and aeration enters reactor by air by the air inlet snubber and carries out aeration, and described reactor outer setting heating jacket, heated reactor by heating jacket.
Described reactor is provided with controller, described controller is connected with oxymuriate volume pump, hydrochloric acid volume pump, oxymuriate Traffic Monitor, hydrochloric acid Traffic Monitor, heating tube, temperature sensor, liquid level detector by electric wire, realizes automatically controlling the amount of reactant, the temperature of reactant, liquid level and the injection rate of reactant and the work output of resultant of detecting reactant.
Introduce in detail below in conjunction with above-mentioned producer the process that the present invention prepares chlorine:
Solution of chlorate in described solution of chlorate storage tank enters in the oxymuriate volume pump from its outlet, secondly at first measure pump outlet by oxymuriate and enter into the oxymuriate Traffic Monitor, enter into reactor in outlet and the solution of chlorate outlet by the oxymuriate Traffic Monitor successively; Secondly hydrochloric acid in described hydrochloric acid tank enters into the hydrochloric acid volume pump from its outlet, at first by hydrochloric acid, measures pump outlet and enters into the hydrochloric acid Traffic Monitor, enters into reactor at outlet and the hydrochloric acid outlet by the hydrochloric acid Traffic Monitor successively; By catalyzer MnCl
2, FeCl
2, FeCl
3, MnSO
4, FeSO
4, Fe
2(SO
4)
2one or more together with above-mentioned reactant in the placing response device, described reactor is heated to 70-95 degree centigrade by heating jacket to reactant, 10-60 minute is carried out in reaction, resultant be take chlorine as main, and, with a small amount of dioxide peroxide, the gas of generation is extracted by water sprayer through air outlet, aeration, form thimerosal, be transported to water body by pipeline and carry out disinfection; In addition, reactor, under the water sprayer decimate action, forms the negative pressure of-90-5KPa, enters reactor bottom by the air inlet snubber and carries out aeration, is conducive to reaction and carries out and gas overflowing.
By experiment, the invention has the beneficial effects as follows: energy consumption is little, and cost is low, and performance safety is reliable, and output is high, and transformation efficiency is high, and technique is simple, is convenient to automatization and controls, installation, easy to operate.
Embodiment
For the problem of above-mentioned existence, below in conjunction with drawings and the specific embodiments, the present invention is described in detail.
Embodiment 1
Described solution of chlorate is the sodium chlorate solution, get the sodium chlorate solution that 500ml concentration is 20%, quantitatively be transported to reactor 13 by oxymuriate volume pump 20, the hydrochloric acid that is 25% by 750ml concentration again, quantitatively be transported to reactor 13 by hydrochloric acid volume pump 3, by add the sodium chlorate solution to measure 1% and add 3% of hydrochloric acid soln amount and add catalyzer MnCl
2,feCl
2, FeCl
3,enter into reactor 13 together with above-mentioned reactant, described reactor 13 is heated to 70 degrees centigrade by heating jacket 14, and the reaction times is 60min, reaction pressure-90KPa, being able to chlorine is main mixed gas, described mixed gas is extracted by water sprayer 11 through air outlet 10, with the interior water of water sprayer 11, mixes, and forms thimerosal, thimerosal to water sprayer 11 exits is detected, chlorine output detected and reach 1 kg/h, chlorine ratio 60%, transformation efficiency 90%.
Embodiment 2
Described solution of chlorate adopts the sodium chlorate solution, getting 800ml concentration is 25% sodium chlorate solution, quantitatively be transported to reactor 13 by oxymuriate volume pump 20, getting 400ml concentration is 31% hydrochloric acid soln, quantitatively be transported to reactor 13 by hydrochloric acid volume pump 3, by add the sodium chlorate solution to measure 3% and add 5% of hydrochloric acid soln amount and add catalyzer MnSO
4, FeSO
4, Fe
2(SO
4)
2enter into reactor 13 together with above-mentioned reactant, 50 degrees centigrade of temperature of reaction, reaction times 40min, reaction pressure-50KPa, being able to chlorine is main mixed gas, described mixed gas is extracted by water sprayer 11 through air outlet 10, with the interior water of water sprayer 11, mixes, and forms thimerosal, water sprayer 11 exit thimerosals are detected, chlorine output detected and reach 5 kg/h, chlorine ratio 65%, transformation efficiency 93%.
Embodiment 3
Described solution of chlorate adopts the sodium chlorate solution, get the sodium chlorate solution that 1200ml concentration is 33%, quantitatively be transported to reactor 13 by oxymuriate volume pump 20, getting 1200ml concentration is 31% hydrochloric acid again, quantitatively be transported to reactor 13 by oxymuriate volume pump 20, by add the sodium chlorate solution to measure 2.5% and add 4% of hydrochloric acid soln amount and add catalyst Fe Cl
3enter into reactor 13 together with above-mentioned reactant, 45 degrees centigrade of temperature of reaction, reaction times 30min, reaction pressure-10KPa, being able to chlorine is main mixed gas, described mixed gas is extracted by water sprayer 11 through air outlet 10, with the interior water of water sprayer 11, mixes, and forms thimerosal, thimerosal to water sprayer 11 exits is detected, chlorine output detected and reach 10 kg/h, chlorine ratio 80%, transformation efficiency 97%.
Embodiment 4
Described solution of chlorate adopts the sodium chlorate solution, get the sodium chlorate solution that 650ml concentration is 40%, quantitatively be transported to reactor 13 by oxymuriate volume pump 20,780ml concentration is 36% hydrochloric acid soln, quantitatively be transported to reactor 13 by oxymuriate volume pump 20, by add the sodium chlorate solution to measure 1.8% and add 2.5% of hydrochloric acid soln amount and add catalyst Fe
2(SO
4)
2enter into reactor 13 together with above-mentioned reactant, temperature of reaction 90 degree, reaction times 25min, reaction pressure-5KPa, being able to chlorine is main mixed gas, described mixed gas is extracted out by water sprayer 11 through air outlet 10, with the interior water of water sprayer 11, mixes, and forms thimerosal, thimerosal to water sprayer 11 exits is detected, chlorine output detected and reach 20 kg/h, chlorine ratio 72%, transformation efficiency 95%.
The foregoing is only preferred embodiment of the present invention, in order to limit the present invention, within the spirit and principles in the present invention not all, any modification of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.