CN112795004A - Production process and production system of fatty alcohol-polyoxyethylene ether sodium sulfate - Google Patents
Production process and production system of fatty alcohol-polyoxyethylene ether sodium sulfate Download PDFInfo
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Abstract
The invention belongs to the technical field of fine chemical engineering, and aims to provide a production process of fatty alcohol-polyoxyethylene ether sodium sulfate, wherein a sulfonating agent SO used in the production process3The gas is SO obtained by burning liquid sulfur and compressed and cooled process air2The mixed gas/air is oxidized into SO in a conversion tower under the action of a catalyst3The mixed gas at the outlet of the conversion tower can be directly used for sulfonating fatty alcohol-polyoxyethylene ether after cooling, atomizing and deacidifying in an atomizing tank and filtering by a demister to obtain the fatty alcohol-polyoxyethylene ether sodium sulfate meeting the requirements. Compared with the currently reported process, the process technology of the invention has the advantages of low dew point requirement on process air, simplified production equipment, shortened process flow and low process energy consumption, thereby having wide application prospect in actual production.
Description
Technical Field
The invention belongs to the technical field of fine chemical engineering, relates to a production process of sodium fatty alcohol-polyoxyethylene ether sulfate, and particularly relates to a method for obtaining SO with appropriate gas concentration by optimizing a sulfur burning method3The air mixed gas is used for the production process and the production system of the sulfonated fatty alcohol-polyoxyethylene ether.
Background
Sulfonation/sulfation reactions (collectively referred to as sulfonation reactions) have been widely studied both at home and abroad as the main chemical process employed in the industrial production of pigments, dyes, pesticides, organic intermediates, and other products. By using different sulfonating agents3) The group is introduced into the organic molecules to make the organic molecules have (-CS (O)2) OX) structure to give a variety of products including sulfonic acid (X ═ H), sulfate (X ═ M, M is a metal cation), sulfonyl halide (X is a halogen), etc., and to impart various surface activities to organic molecules such as emulsification, foaming, wetting, etc.; while utilizing (-CS (O)2) OX) group, which gives organic molecules better water solubility; selective sulfonation is used in the field of pharmaceutical production to separate isomers to obtain a series of intermediates. However, the most important industrial application of sulfonation is in the field of anionic surfactants, and the sulfonation products are produced mainly from alkylbenzene sulfonic acid, fatty alcohol polyoxyethylene ether sulfate, etc., the former is widely used for preparing detergents, and the latter is used in shampoosThe data show that over 200 million tons of sulfonated product are sold worldwide for home care products 2015 alone, which accounts for an extremely high proportion of total surfactant product. The sulfonating agent adopted by the sulfonation process in industrial production is various, and SO is common3Sulfuric acid, fuming sulfuric acid, sulfite and chlorosulfonic acid with different concentrations, different sulfonating agents have different properties and different occasions, and SO3The sulfonation is widely popularized and used due to advanced process and high sulfonated product quality.
SO3Is the most direct sulfonating agent theoretically used for sulfonating organic raw materials, and the use ratio of reactant raw materials is closer to the theoretical value. SO (SO)3Divided into liquid SO3And gas SO3Liquid SO3The sulfonation reaction is violent, the sulfonation reaction is only suitable for partial inactive aromatic compounds, the viscosity of the product at the reaction temperature is strictly required, and the liquid SO3The requirement on temperature is high in the storage process, and the liquid solidification caused by low temperature must be avoided; the violent reaction process results in SO in practical control process3The dosage is difficult to control accurately, the whole process is complex, and only a few domestic enterprises use the method. Gaseous SO3The method does not generate waste acid in the using process, does not corrode equipment and does not pollute the environment, and in order to control the reaction rate, gas or solution is usually used for diluting the catalyst for reuse, so that the reaction process is prevented from being fiercely and difficult to control. Due to SO3The sulfur-rich SO has a self-polymerization tendency, and can gradually change to a high-melting-point crystal form under the influence of temperature, SO on the premise of considering the use cost, the sulfur is combusted, converted and diluted by dry air to obtain the SO with a certain gas concentration3The sulfur burning method sulfonation generation process of the air mixed gas becomes the first choice of enterprises.
In the production apparatus of sulfonation process, including Ballestra, Chemiten, Messanicoh, Moderne and Lion, in SO3The difference of the air generation process is very little, and the general flow is as follows: cooling and drying the compressed air to obtain dry air with dew point below-60 deg.C, introducing into sulfur furnace, contacting with liquid sulfur, igniting and burning to obtain SO carrying large amount of heat2Mixed gas (es)A body; then the mixed gas is cooled to 450 ℃ and enters a conversion tower, and is continuously oxidized into SO under the action of a catalyst3，SO3The air is cooled to 45-55 ℃ by a multi-stage cooler, and enters a sulfonator to participate in reaction after a little acid mist is filtered by a demister. Dried SO3Air is extremely important for obtaining high-quality and high-yield sulfonated products, the moisture in the air can cause the generation of sulfuric acid and fuming sulfuric acid which can cause corrosion to equipment, and the color and luster of the products can be deepened and side reaction can be caused after the products enter a sulfonator, unexpected by-products are generated, the product quality is influenced, and therefore, the process air must be ensured to be dried until the dew point reaches-60 to-70 ℃. The drying of process air needs to be carried out in a drying tower filled with regenerative filler (silica gel and activated alumina), the drying tower is divided into an upper layer and a lower layer which are used alternately, and the filler needs to be dried, dehydrated and cooled for reuse after absorbing moisture, so that the two layers of drying layers are used one by one, and the regeneration of one layer is prepared, which leads to the complexity of the whole process, and the dew point fluctuation of the drying air can generate great influence on the quality of subsequent products, thus being not beneficial to continuous production.
Due to sulfur combustion method SO3The air mixed gas generation process has strict requirements on the dew point of dry air, long process flow, complex operation and more influence factors on the product quality, mainly the moisture in the process air has great influence on the quality of sulfonated products, and the SO is directly carried out by utilizing cooling air at present3The sulfonation process by air generation has not been reported.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a production process of sodium fatty alcohol polyoxyethylene ether sulfate; the process does not need drying process air with a low dew point, can be used for sulfonating fatty alcohol-polyoxyethylene ether by cooling air and liquid sulfur combustion, conversion of a conversion tower, cooling and atomized spraying, secondary cooling and demister filtration, and the quality of the obtained product is the same as that of the product produced under the existing process conditions; the process has simple control conditions, and can be conveniently realized by modifying the existing production device.
The invention also provides a production system used by the production process.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a production process of fatty alcohol-polyoxyethylene ether sodium sulfate, which comprises the following steps:
1) the method comprises the following steps that (1) outside air is subjected to impurity removal through an air filter, enters a Roots blower to be heated and pressurized, is conveyed to an air low-temperature condenser, is subjected to cooling treatment through two cooling media, most of water vapor in the air is removed, and the obtained cooling air enters a sulfur furnace through a gas phase inlet of the sulfur furnace; simultaneously, liquid sulfur enters the sulfur burning furnace from a liquid phase inlet of the sulfur burning furnace through a liquid sulfur conveying pump, is in countercurrent contact with cooling air, is ignited and burned to generate SO2A gas;
2) diluted SO2The gas enters a conversion tower and is catalyzed to obtain SO3Mixing the gas with cooling air for dilution, and diluting to obtain diluted SO3The air mixed gas enters an atomization tank after being cooled by a primary air cooler, and fuming sulfuric acid or liquid SO is sprayed in through atomization3Removal of SO3Sulfuric acid droplets precipitated from the air-mixed gas;
3) SO after sulfuric acid liquid drop removal3The air is further cooled by a secondary air cooler, a small amount of acid mist is removed by a demister, and then the air enters a sulfonator to be subjected to sulfonation reaction with fatty alcohol-polyoxyethylene ether;
4) and (3) removing gas from the reacted sulfate through a cyclone separator, conveying the process water and the liquid caustic soda to a neutralization mixer through a neutralization mixing pump, and obtaining the product fatty alcohol-polyoxyethylene ether sodium sulfate after neutralization.
As a preferable scheme of the invention, the temperature of the cooling gas at the outlet of the air low-temperature condenser in the step 1) is 4-8 ℃.
As a preferable scheme of the invention, the molar ratio of the flow of the liquid sulfur to the flow of the fatty alcohol-polyoxyethylene ether entering the sulfonator is 1.02-1.12: 1.
As a preferable scheme of the invention, SO at the outlet of the sulfur burning furnace in the step 1)2The gas temperature was 450-700 ℃.
As a preferred embodiment of the present invention, the outlet SO of the conversion tower in the step 2) is3The temperature of the air mixed gas is 440-470 ℃.
As a preferable embodiment of the present invention, SO in the step 2)3The air mixed gas is cooled to 270 ℃ after passing through a primary air cooler, and atomized and sprayed into fuming sulfuric acid or liquid SO3The flow rate of the gas is 0.1-0.5 per mill of the gas flow rate at the inlet, and the grain diameter of the sprayed liquid drop is controlled to be 20-80 mu m.
As a preferable embodiment of the present invention, SO in the step 3)3The temperature of the air mixture gas is cooled to 45-60 ℃ after passing through a secondary air cooler, and the SO is at the moment3The gas volume concentration is 3-6%.
In a preferable embodiment of the invention, the process water flow rate in the step 4) is 15-20% of the acid ester flow rate, and the 32% liquid caustic soda flow rate is 35-40% of the acid ester flow rate.
The invention also provides a production system of the fatty alcohol-polyoxyethylene ether sodium sulfate, all devices are sequentially connected through pipelines and comprise an air filter, a Roots blower, an air low-temperature condenser, a sulfur furnace, a conversion tower, a primary air cooler, an atomization tank, a secondary air cooler, a demister, a sulfonator, a gas-liquid separator, a neutralization mixing pump and a neutralization mixer.
The sulfur burning furnace is provided with a liquid sulfur inlet; the primary air cooler is provided with a nicotinic acid discharge port; the atomization tank is provided with a nicotinic acid outlet; the secondary air cooler is provided with a nicotinic acid discharge port; the demister is provided with a nicotinic acid discharge port; the sulfonator is provided with a fatty alcohol-polyoxyethylene ether inlet; the gas-liquid separator is provided with an acid gas outlet; the neutralizer mixer has a gas discharge outlet.
As a preferred scheme of the invention, two cooling medium flowing pipelines, a circulating cooling water pipeline and a freezing glycol aqueous solution pipeline are arranged in the air low-temperature condenser, and compressed air is subjected to heat exchange by the two cooling media in the condenser in sequence; the atomization tank is provided with an atomized nicotinic acid injection port, has larger volume to ensure enough gas retention time, and receivesSO from primary air cooler3The top of the mixed gas is communicated with a secondary air cooler.
Compared with the prior art, the process technology related by the invention has the following advantages:
1) according to the process, the cooling air with the temperature of 4-8 ℃ is obtained through the air low-temperature condenser, and then the silica gel drying tower is not needed for further drying and dewatering, so that the dew point requirement on the used process air is low. This is because the sulfur-burning process gas SO provided in the present invention3In the air generation process, cooling air and liquid sulfur are directly used for combustion and conversion to obtain SO3After the air mixed gas is cooled, the mixed gas is cooled through a primary air cooler, the temperature is controlled to be above the boiling point of sulfuric acid, the relative humidity of the gas is greatly changed due to cooling, residual moisture can be gradually separated out, and SO and the residual moisture are gradually separated out3Acting to form droplets of sulfuric acid, i.e. oleum; and fuming sulfuric acid or liquid SO is sprayed into the atomization tank through atomization3The size of the droplet is changed by controlling the spraying flow, so that the separated sulfuric acid droplets are polymerized with each other, the particle size is rapidly enlarged, the sulfuric acid droplets are gradually separated from gas under the action of gravity settling and fall in an atomization tank, and light component gas is continuously discharged from the top of the tank, so that the influence of residual moisture in process air on sulfonated products is avoided;
2) the gas generation process flow does not need a silica gel tower drying link, the cost and energy consumption of used equipment are greatly reduced, and the starting time and the stopping time can be shortened;
3) the process flow related by the invention is short, the control is simple, and the obtained SO3The quality of the fatty alcohol-polyoxyethylene ether sulfuric acid product obtained by using the air mixed gas for sulfonating the fatty alcohol-polyoxyethylene ether is the same as that of the original process, and the product meets the product qualification standard.
Drawings
FIG. 1 is a schematic diagram of a production system according to the present invention.
In the figure, 1 is an air filter, 2 is a roots blower, 3 is an air low-temperature condenser, 4 is a sulfur furnace liquid sulfur inlet, 5 is a sulfur furnace, 6 is a conversion tower, 7 is a primary air cooler, 8 is an atomization tank, 9 is a secondary air cooler, 10 is a demister, 11 is a sulfonator, 12 is a cooling water pipeline in the air low-temperature condenser, 13 is a frozen ethylene glycol aqueous solution pipeline in the air low-temperature condenser, 14 is a primary air cooler nicotinic acid discharge port, 15 is an atomization tank nicotinic acid discharge port, 16 is a secondary air cooler nicotinic acid discharge port, 17 is a demister nicotinic acid discharge port, 18 is an atomization tank atomization fuming sulfuric acid spray inlet, 19 is a sulfonator fatty alcohol polyoxyethylene ether inlet, 20 is a gas-liquid separator, 21 is a neutralization mixing pump, 22 is a neutralization mixer, and 23 is a gas-liquid separator acid gas discharge port; 24 is a gas outlet of the neutralization mixer; and 25 is a product outlet.
Detailed Description
The present invention will be described in detail with reference to the following examples, which are carried out on the premise of the technical solution of the present invention, and give detailed embodiments and specific procedures, but the scope of the present invention is not limited to the following examples.
Referring to fig. 1, the invention provides a production system of sodium fatty alcohol polyoxyethylene ether sulfate, all devices are connected in sequence by pipelines, and the system comprises an air filter 1, a roots blower 2, an air low-temperature condenser 3, a sulfur burner 5, a conversion tower 6, a primary air cooler 7, an atomization tank 8, a secondary air cooler 9, a demister 10, a sulfonator 11, a gas-liquid separator 20, a neutralization mixing pump 21 and a neutralization mixer 22.
The sulfur burning furnace 5 is provided with a liquid sulfur inlet 4; the primary air cooler 7 is provided with a nicotinic acid discharge port 14; the atomization tank 8 is provided with a nicotinic acid discharge port 15; the secondary air cooler 9 is provided with a nicotinic acid discharge port 16; the demister 10 is provided with a nicotinic acid discharge port 17; the sulfonator 11 is provided with a fatty alcohol-polyoxyethylene ether inlet 19; the gas-liquid separator 20 has an acid gas discharge port 23; the neutralizer mixer 22 has a gas outlet 24.
Two cooling medium flowing pipelines, namely a circulating cooling water pipeline 12 and a freezing glycol aqueous solution pipeline 13, exist in the air low-temperature condenser 3, and compressed air sequentially passes through the two cooling media to exchange heat in the air low-temperature condenser 3;
the atomization tank 8 is provided with an atomized nicotinic acid injection port 18, the atomization tank 8 has larger volume to ensure enough gas retention time, and the atomization tank 8 receives SO from the primary air cooler 73The top of the air/air mixture is communicated with a secondary air cooler 9.
Example 1
This example provides a process for producing sodium fatty alcohol-polyoxyethylene ether sulfate with a flow of 4580m3After impurities of outside air are removed through a filter, a Roots blower is compressed, the pressure at the outlet of the Roots blower is increased to about 56KPa, and then the air enters a low-temperature air condenser; the hot air in the low-temperature air condenser is sequentially cooled by two cooling media, namely cooling water and a glycol solution at 0 +/-4 ℃, and the hot air is cooled by the two cooling media to obtain cooling air at the temperature of 8 ℃; the cooling air directly enters the sulfur burning furnace, and is combusted with the liquid sulfur with the flow rate of 240kg/h conveyed by the liquid sulfur conveying pump in the sulfur burning furnace to form SO2Air mixed gas, the temperature of the outlet of the sulfur burning furnace is 600 ℃; SO (SO)2The air mixture is cooled to about 450 ℃ by an air cooler at the upper part of the conversion tower and then is loaded with V in the conversion tower2O5Of SO, the catalyst bed of2Catalyzing and converting into SO3Finally, SO with the temperature of 480 ℃ is obtained at the outlet of the conversion tower3Air mixed gas; SO (SO)3The air mixed gas enters a first-stage air cooler to be cooled to 270 ℃, then enters an atomization tank, and 60% fuming sulfuric acid (liquid SO for the other production line) is atomized and sprayed into the upper part of the atomization tank by a spray head3Control) is carried out, the particle size of atomized oleum is controlled to be about 60 mu m by adjusting the flow rate of the sprayed oleum to be 200L/h, and the SO is added at the moment3Fuming sulfuric acid begins to be separated from the air mixed gas, the fuming sulfuric acid is combined with the fuming sulfuric acid sprayed in an atomizing mode, the particle size is increased, the fuming sulfuric acid is settled to the bottom of the tank under the action of gravity, and SO is generated3Air flows out from the top of the atomization tank; SO passing through the atomization tank3The mixed gas enters a secondary air cooler to be cooled to 55 ℃, and the SO is generated at the moment3The volume concentration of the gas is 5.5 percent, and meanwhile, the flow rate of the fatty alcohol-polyoxyethylene ether is adjusted to 1745kg/h, and the gas is mixed with SO3The air mixture enters togetherAnd (4) feeding the mixture into a sulfonator for reaction. By combustion of sulfur process gases SO3The mixed gas obtained by the air generation process enters a distributor from the top of a sulfonator, reacts with fatty alcohol-polyoxyethylene ether conveyed by an organic material pump in the sulfonator, the reaction heat is removed in time by using circulating water with large reaction heat release, the temperature of circulating cooling water of the sulfonator is controlled to be about 32 ℃, and at the moment, sulfate is obtained at the bottom of the sulfonator; separating acid gas and acid ester by using a sulfuric acid ester through a gas-liquid separator and a cyclone separator, leading the gas to a tail gas absorption section, conveying 32% liquid alkali (920kg/h) and process water (450kg/h) to a neutralization mixer through a neutralization mixing pump by using liquid acid ester, and neutralizing to obtain the product of the sodium fatty alcohol polyoxyethylene ether sulfate.
Comparative example: the only difference was that no nebulized sample was passed through the nebulizing canister, as in example 1.
The product testing data obtained are shown in table 1:
TABLE 1 test data
Example 2
The embodiment provides a production process of fatty alcohol-polyoxyethylene ether sodium sulfate, wherein the flow rate is 4200m3After impurities of outside air are removed through a filter, a Roots blower is compressed, the pressure at the outlet of the blower is increased to about 55KPa, and then the air enters a low-temperature air condenser; the hot air in the low-temperature air condenser is sequentially cooled by two cooling media, namely cooling water and a glycol solution at 0 +/-4 ℃, and the hot air is cooled by the two cooling media to obtain cooling air at the temperature of 8 ℃; the cooling air directly enters the sulfur burning furnace, and is combusted with the liquid sulfur with the flow rate of 240kg/h conveyed by the liquid sulfur conveying pump in the sulfur burning furnace to form SO2Air mixed gas, the outlet temperature of the sulfur burner is 610 ℃; SO (SO)2The air mixture is cooled to about 450 ℃ by an air cooler at the upper part of the conversion tower and then is loaded with V in the conversion tower2O5Of SO, the catalyst bed of2Conversion to SO3At the mostFinally obtaining SO with the temperature of 480 ℃ at the outlet of the conversion tower3Air mixed gas; SO (SO)3The air mixed gas enters a first-stage air cooler to be cooled to 270 ℃, then enters an atomization tank, and 60% fuming sulfuric acid (liquid SO for the other production line) is atomized and sprayed into the upper part of the atomization tank by a spray head3Control is carried out), the particle size of atomized oleum is controlled to be about 65 mu m by adjusting the flow rate of the sprayed oleum to be 210L/h, and the SO is at the moment3Fuming sulfuric acid begins to be separated from the air mixed gas, the fuming sulfuric acid is combined with the fuming sulfuric acid sprayed in an atomizing mode, the particle size is increased, the fuming sulfuric acid is settled to the bottom of the tank under the action of gravity, and SO is generated3Air flows out from the top of the atomization tank; SO passing through the atomization tank3The mixed gas enters a secondary air cooler to be cooled to 55 ℃, and the SO is generated at the moment3The volume concentration of the gas is 6 percent, and the flow rate of the fatty alcohol-polyoxyethylene ether is adjusted to be 2050kg/h and SO3The air mixed gas enters the sulfonator together for reaction. By combustion of sulfur process gases SO3The mixed gas obtained by the air generation process enters a distributor from the top of a sulfonator, reacts with fatty alcohol-polyoxyethylene ether conveyed by an organic material pump in the sulfonator, the reaction heat is removed in time by using circulating water with large reaction heat release, the temperature of circulating cooling water of the sulfonator is controlled to be about 32 ℃, and at the moment, sulfate is obtained at the bottom of the sulfonator; separating acid gas and acid ester by using a gas-liquid separator and a cyclone separator for sulfuric ester, leading the gas to a tail gas absorption section, conveying 32% liquid alkali (990kg/h) and process water (460kg/h) to a neutralization mixer by using a neutralization mixing pump for liquid acid ester, and neutralizing to obtain the product sodium fatty alcohol polyoxyethylene ether sulfate.
The product testing data obtained are shown in table 2:
TABLE 2 test data
Example 3
The embodiment provides a production process of fatty alcohol-polyoxyethylene ether sodium sulfate, wherein the flow rate is 5775m3The/h external air is filtered to remove impurities and then enters the Roots blowerCompressing, increasing the pressure at the outlet of the fan to about 56KPa, and then introducing the gas into a low-temperature air condenser; the hot air in the low-temperature air condenser is sequentially cooled by two cooling media, namely cooling water and a glycol solution at 0 +/-4 ℃, and the hot air is cooled by the two cooling media to obtain cooling air at the temperature of 8 ℃; the cooling air directly enters the sulfur burning furnace and is combusted with the liquid sulfur with the flow rate of 330kg/h conveyed by the liquid sulfur conveying pump in the sulfur burning furnace to form SO2Air mixed gas, the temperature of the outlet of the sulfur burning furnace is 600 ℃; SO (SO)2The air mixture is cooled to about 450 ℃ by an air cooler at the upper part of the conversion tower and then is loaded with V in the conversion tower2O5Of SO, the catalyst bed of2Conversion to SO3Finally, SO with the temperature of 480 ℃ is obtained at the outlet of the conversion tower3Air mixed gas; SO (SO)3The air mixed gas enters a first-stage air cooler to be cooled to 270 ℃, then enters an atomization tank, and 60% fuming sulfuric acid (liquid SO for the other production line) is atomized and sprayed into the upper part of the atomization tank by a spray head3) The particle size of atomized oleum is controlled to be about 750 mu m by adjusting the flow rate of the injected oleum to be 320L/h, and the SO is added at the moment3Fuming sulfuric acid begins to be separated from the air mixed gas, the fuming sulfuric acid is combined with the fuming sulfuric acid sprayed in an atomizing mode, the particle size is increased, the fuming sulfuric acid is settled to the bottom of the tank under the action of gravity, and SO is generated3Air flows out from the top of the atomization tank; SO passing through the atomization tank3The mixed gas enters a secondary air cooler to be cooled to 55 ℃, and the SO is generated at the moment3The volume concentration of the gas is 6 percent, the flow of the fatty alcohol-polyoxyethylene ether is adjusted to be 2510kg/h, and the gas and SO are mixed3The air mixed gas enters the sulfonator together for reaction. By combustion of sulfur process gases SO3The mixed gas obtained by the air generation process enters a distributor from the top of a sulfonator, reacts with fatty alcohol-polyoxyethylene ether conveyed by an organic material pump in the sulfonator, the reaction heat is removed in time by using circulating water with large reaction heat release, the temperature of circulating cooling water of the sulfonator is controlled to be about 32 ℃, and at the moment, sulfate is obtained at the bottom of the sulfonator; separating acid gas and acid ester with sulfuric acid ester by gas-liquid separator and cyclone separator, introducing the gas to tail gas absorption section, and neutralizing and mixing the liquid acid ester32 percent liquid caustic soda (1275kg/h) and process water (650kg/h) are conveyed to a neutralization mixer by a pump, and the product of the sodium fatty alcohol-polyoxyethylene ether sulfate is obtained after neutralization.
The product test data obtained are shown in table 3:
TABLE 3 test data
As can be seen from tables 1, 2 and 3, SO obtained by using the production process of sodium fatty alcohol-polyoxyethylene ether sulfate provided by the invention3The quality of the fatty alcohol-polyoxyethylene ether sulfuric acid product obtained by sulfonating fatty alcohol-polyoxyethylene ether by using the air mixed gas is the same as that of the original process, but a silica gel tower drying link is not needed in the gas generation process flow related by the invention, the cost of the used equipment and the energy consumption are greatly reduced, the starting and stopping time can be shortened, the cost and the energy consumption are saved, and the method is suitable for industrial production.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that various changes in the embodiments and/or modifications of the invention can be made, and equivalents and modifications of some features of the invention can be made without departing from the spirit and scope of the invention.
Claims (10)
1. The production process of the sodium fatty alcohol polyoxyethylene ether sulfate is characterized by comprising the following steps:
1) removing impurities from outside air, heating and pressurizing, and cooling by two cooling media to obtain cooled air which enters a sulfur furnace; simultaneously, liquid sulfur enters a sulfur burning furnace to be in countercurrent contact with cooling air, and is ignited and burned to generate SO2A gas;
2) SO diluted in the step 1)2The gas enters a conversion tower and is subjected to catalytic conversion to obtain SO3Diluting the gas with cooling air, and diluting with diluted SO3Air mixerAfter the resultant gas is subjected to primary cooling, fuming sulfuric acid or liquid SO is sprayed in through atomization3Removal of SO3Sulfuric acid droplets precipitated from the air-mixed gas;
3) SO obtained after sulfuric acid liquid drops are removed in the step 2)3Filtering acid mist of the air mixed gas by a secondary cooler and a demister, and then carrying out sulfonation reaction with fatty alcohol-polyoxyethylene ether to obtain reactant sulfate;
4) and (3) after removing acid gas from the reactant sulfate reacted in the step 3), carrying out neutralization reaction with process water and liquid alkali, and obtaining the product sodium fatty alcohol-polyoxyethylene ether sulfate after the neutralization is finished.
2. The production process of sodium fatty alcohol polyoxyethylene ether sulfate according to claim 1, wherein the temperature of the cooling air subjected to the temperature reduction treatment in the step 1) is 4-8 ℃.
3. The production process of sodium fatty alcohol-polyoxyethylene ether sulfate according to claim 1, wherein the molar ratio of the liquid sulfur to the flow of the fatty alcohol-polyoxyethylene ether is 1.02-1.12: 1.
4. The production process of sodium fatty alcohol-polyoxyethylene ether sulfate according to claim 1, wherein SO obtained after combustion in step 1) is used as the SO2The temperature of the gas is 450-700 ℃.
5. The production process of sodium fatty alcohol-polyoxyethylene ether sulfate according to claim 1, wherein the diluted SO in the step 2) is3The temperature of the/air mixed gas is 440-470 ℃.
6. The production process of sodium fatty alcohol-polyoxyethylene ether sulfate according to claim 1, wherein SO in the step 2) is used as SO3The temperature of the air mixed gas after primary cooling is 270 ℃; atomized into fuming sulfuric acid or liquid SO3The flow rate of the gas is 0.1-0.5 per mill of the gas flow rate of the inlet, and the gas is sprayedThe particle diameter of the shot liquid drop is controlled to be 20-80 mu m.
7. The production process of sodium fatty alcohol-polyoxyethylene ether sulfate according to claim 1, wherein SO in the step 3) is used as SO3The temperature of the air mixed gas after secondary cooling is 45-60 ℃, and the SO after secondary cooling3In air mixture, SO3The gas volume concentration is 3-6%.
8. The production process of sodium fatty alcohol-polyoxyethylene ether sulfate according to claim 1, wherein the process water flow in the step 4) is 15-20% of the sulfate ester flow, and the liquid caustic soda flow is 35-40% of the sulfate ester flow.
9. The production system of sodium fatty alcohol polyoxyethylene ether sulfate according to claim 1, wherein the production system comprises an air filter, a Roots blower, an air low-temperature condenser, a sulfur burner, a conversion tower, a primary air cooler, an atomization tank, a secondary air cooler, a demister, a sulfonator, a gas-liquid separator, a neutralization mixing pump and a neutralization mixer which are sequentially connected through pipelines; wherein the sulfur burning furnace is provided with a liquid sulfur inlet; the primary air cooler is provided with a nicotinic acid discharge port; the atomization tank is provided with a nicotinic acid outlet; the secondary air cooler is provided with a nicotinic acid discharge port; the demister is provided with a nicotinic acid discharge port; the sulfonator is provided with a fatty alcohol-polyoxyethylene ether inlet; the gas-liquid separator is provided with an acid gas outlet; the neutralizer mixer has a gas discharge outlet.
10. The system for producing sodium fatty alcohol polyoxyethylene ether sulfate according to claim 9, wherein two cooling medium flow pipelines, a circulating cooling water pipeline and a freezing glycol aqueous solution pipeline, are arranged in the air low-temperature condenser; the atomization tank is provided with an atomized nicotinic acid injection port and receives SO from the primary air cooler3Air mixture, top and secondary air coolerAre communicated with each other.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112680208A (en) * | 2021-01-06 | 2021-04-20 | 中国日用化学研究院有限公司 | Preparation process of oleyl alcohol polyoxyethylene ether sulfonate/sulfate |
| CN116903497A (en) * | 2023-09-11 | 2023-10-20 | 南京为先科技有限责任公司 | Method for preparing sulfonate surfactant by sulfur trioxide film sulfonation |
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| GB808394A (en) * | 1955-10-28 | 1959-02-04 | Continental Oil Co | Improvements in or relating to process for sulfonation of hydrocarbons |
| CN106563386A (en) * | 2015-10-11 | 2017-04-19 | 宁夏际华环境安全科技有限公司 | Production process for fatty alcohol-polyoxyethylene ether |
| CN111100284A (en) * | 2019-12-27 | 2020-05-05 | 赞宇科技集团股份有限公司 | Production process and device of high-quality fatty alcohol-polyoxyethylene ether sulfate |
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| GB808394A (en) * | 1955-10-28 | 1959-02-04 | Continental Oil Co | Improvements in or relating to process for sulfonation of hydrocarbons |
| CN106563386A (en) * | 2015-10-11 | 2017-04-19 | 宁夏际华环境安全科技有限公司 | Production process for fatty alcohol-polyoxyethylene ether |
| CN111100284A (en) * | 2019-12-27 | 2020-05-05 | 赞宇科技集团股份有限公司 | Production process and device of high-quality fatty alcohol-polyoxyethylene ether sulfate |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112680208A (en) * | 2021-01-06 | 2021-04-20 | 中国日用化学研究院有限公司 | Preparation process of oleyl alcohol polyoxyethylene ether sulfonate/sulfate |
| CN116903497A (en) * | 2023-09-11 | 2023-10-20 | 南京为先科技有限责任公司 | Method for preparing sulfonate surfactant by sulfur trioxide film sulfonation |
| CN116903497B (en) * | 2023-09-11 | 2024-03-29 | 南京为先科技有限责任公司 | Method for preparing sulfonate surfactant by sulfur trioxide film sulfonation |
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