CN211946872U

CN211946872U - Gas phase SO3Sulfonation production system

Info

Publication number: CN211946872U
Application number: CN201922418615.7U
Authority: CN
Inventors: 史立文; 钟凯; 徐坤华; 郭霞; 雷小英; 陶华东; 黄晴; 华文高
Original assignee: Zanyu Technology Group Co ltd; Jiaxing Zanyu Technology Development Co ltd
Current assignee: Zanyu Technology Group Co ltd; Jiaxing Zanyu Technology Development Co ltd
Priority date: 2019-12-27
Filing date: 2019-12-27
Publication date: 2020-11-17
Anticipated expiration: 2029-12-27

Abstract

The utility model belongs to the technical field of fine chemistry industry. Purpose(s) toIs to provide a gas phase SO₃A sulfonation production system; the sulfonation system basically has no waste gas emission, the environmental effect is good, and no dangerous solid wastes such as electrostatic acid and the like are generated. The technical scheme is as follows: gas phase SO₃A sulfonation production system, characterized by: the device comprises a Roots blower, a sulfur furnace and an SO which are communicated with each other in sequence by pipelines₂Conversion column, SO₃Cooler, SO₃A filter, a sulfonator, a gas-liquid separator and a subsequent treatment system; the gas suction end of the Roots blower is communicated with the gas-phase outlet of the gas-liquid separator, and the outlet end of the Roots blower is communicated with the gas-phase inlet of the sulfur burner; and the suction end of the Roots blower is also connected with an oxygen inlet.

Description

Gas phase SO3Sulfonation production system

Technical Field

The utility model belongs to the technical field of fine chemistry industry, concretely relates to gaseous SO for producing anion surfactant₃A sulfonation production system.

Background

In the field of industrial and domestic surfactants, the sulphonation process is the basic production process for obtaining sulphonated and sulphated products of the anionic surfactant type. The product is widely applied to preparation of civil products such as detergents, toothpaste, cosmetics and the like, and has wide application in the industrial fields of oil extraction, mineral separation, metal cutting processing, pesticides, textile, printing and dyeing, leather and the like.

Commonly used at presentThe sulfonation process generally adopts gas-phase SO₃The sulfonation process adopts SO with low gas concentration (generally 3-6 percent)₃Air mixed gas is contacted with the organic material for sulfonation. This technique SO₃High utilization rate, relative green environmental protection, but because of the need of a large amount of air as SO₃The diluent has large exhaust emission, and the exhaust emission per ton of active matter products is generally 1000-2000 m³Left and right. In addition, in order to ensure that the tail gas can reach the standard and be discharged, the tail gas generally needs to be subjected to electrostatic demisting combined alkali washing treatment, and the tail gas treatment process is complex; a certain amount of electrostatic acid is generated in the electrostatic demisting treatment, which belongs to dangerous solid waste and has high treatment difficulty; the caustic wash treatment also produces a relatively large amount of salt-containing wastewater, and the treatment is also complicated.

CN102513039 discloses a method for recycling sulfonated tail gas, which recycles tail gas after an electrostatic demister as SO₃The diluent of (1). However, the process still has an electrostatic demisting system, and electrostatic acid hazards still exist; the tail gas after passing through the electrostatic demister still contains trace organic acid fog drops, and the product quality can be influenced if the tail gas is not treated and recycled; in addition, the process is only applicable to SO₃The evaporation sulfonation process is not suitable for the common sulfonation process of a sulfur burning method at present.

SUMMERY OF THE UTILITY MODEL

The purpose of the present invention is to overcome the disadvantages of the prior art and to provide a gas phase SO₃A sulfonation production system; the sulfonation system basically has no waste gas emission, the environmental effect is good, and no dangerous solid wastes such as electrostatic acid and the like are generated.

The utility model provides a technical scheme is:

gas phase SO₃A sulfonation production system, characterized by: the device comprises a Roots blower, a sulfur furnace and an SO which are communicated with each other in sequence by pipelines₂Conversion column, SO₃Cooler, SO₃A filter, a sulfonator, a gas-liquid separator and a subsequent treatment system;

the gas suction end of the Roots blower is communicated with the gas-phase outlet of the gas-liquid separator, and the outlet end of the Roots blower is communicated with the gas-phase inlet of the sulfur burner; and the suction end of the Roots blower is also connected with an oxygen inlet.

And an oxygen content analyzer is arranged on a pipeline for communicating the outlet end of the Roots blower with the gas phase inlet of the sulfur burner.

A pressure regulating system is arranged on a pipeline for communicating the gas-phase outlet of the gas-liquid separator with the suction end of the Roots blower; the pressure regulating system is mainly used for regulating SO at the inlet of the sulfonator₃The gas phase pressure of the gas, including when the inlet gas phase pressure is lower, appropriately supplementing dry air (or nitrogen); when the gas phase pressure at the inlet is higher, gas is properly pumped out;

the liquid phase outlet of the gas-liquid separator is communicated with a subsequent treatment system; the subsequent treatment system can be one of a fatty alcohol-polyoxyethylene ether vacuum neutralization system, an alkylbenzene aging hydrolysis system, an alpha olefin neutralization hydrolysis system, a fatty acid methyl ester aging system, a re-esterification bleaching system and a neutralization drying system according to different organic materials entering the sulfonator.

The utility model has the advantages that:

1) the utility model discloses with the tail gas behind the sulfonation gas-liquid separator, after the ration supplyed oxygen, regard as process gas again and use, make the sulfonation system basically not have exhaust emission, environmental effect is good.

2) The sulfonated tail gas is recycled, and basically no waste gas is discharged, so that an electrostatic demister, an alkali absorption tower and other related tail gas treatment devices required by the original system are not required, and the equipment investment and the operation cost are greatly reduced; meanwhile, dangerous solid wastes such as electrostatic acid and the like are not generated.

3) The sulfonated tail gas enters a sulfur burning furnace, and the organic acid mist in the original tail gas is completely burned by utilizing high temperature, so that the direct recycling of the tail gas, the influence of the organic acid mist carried in the tail gas and the like on the product quality are avoided;

4) due to the limitation of the catalytic efficiency of the conversion tower, the original SO₂The gas is converted into SO after passing through a conversion tower₃About 98% conversion, unconverted SO₂Finally, the tail gas is absorbed by an alkali absorption tower, so that a large amount of waste is caused; utilize the utility model discloses technology sulfonation tail gas realizes cyclic utilization, unconverted SO₂Returning to the conversion tower again for conversion, theoretically realizing the conversion from sulfur to SO₃The sulfur consumption of the sulfonated product is reduced.

5) By reducing the head gas phase pressure of the sulfonator, the organic material is made to be in higher SO₃The process can be stably carried out under the condition of gas concentration (5-7% of volume gas concentration under the standard condition), and a high-quality product is obtained. In the normal sulfonation process, the sulfonation is especially carried out on fatty alcohol-polyoxyethylene ether and alpha olefin, and SO₃The gas volume concentration should be maintained at 2.5-3.5%, and too high a gas volume concentration may cause severe over-sulfonation and seriously affect the product quality. However, in order to realize the complete recycling of the tail gas, the concentration of 2.5-3.5% of the gas is controlled according to the combustion heat of the sulfur, SO that the temperature of the sulfur furnace can only reach about 300 ℃, and the SO can not be met₂Conversion requirements and incomplete combustion. In addition, the gas phase pressure of the sulfonator is reduced, and the product quality is also improved.

6) The production system adopts the existing mature equipment, so the production system has the characteristics of investment saving, convenient maintenance and long service life.

Drawings

Fig. 1 is a schematic structural diagram of the production system of the present invention.

In the figure: 1 is an oxygen inlet, 2 is a liquid sulfur inlet, 3 is an organic material inlet, 4 is a Roots blower, 5 is a sulfur furnace, 6 is a conversion tower, 7 is a cooler, and 8 is SO₃A filter, 9 a sulfonator, 10 a gas-liquid separator, 11 a pressure regulating system and 12 a subsequent treatment system.

Detailed Description

The following further description is made with reference to the embodiments shown in the drawings.

Example 1:

after being sulfonated, the tail gas after gas-liquid separation is mixed with oxygen input into a system and then enters a sulfur furnace through a Roots blower; adjusting the oxygen amount, and controlling the oxygen concentration of the mixed gas entering the sulfur furnace to be 22%.

Simultaneously, liquid sulfur enters a sulfur burning furnace according to the flow of 400kg/h, is in contact combustion in the sulfur burning furnace, adjusts the frequency of a Roots blower, controls the temperature of the sulfur burning to be 650 DEG C. SO produced by combustion₂Gas is converted by a conversion tower, cooled by a cooler and SO according to the conventional process₃Filtering with a filter to obtain SO with the temperature of 60 DEG C₃Gas enters a falling film type sulfonation reactor; simultaneously, the dodecylbenzene enters the sulfonator at the flow rate of 2700kg/h and is mixed with SO₃The gas contacts to carry out sulfonation reaction.

SO maintenance at gas phase inlet of sulfonator by pressure regulation system₃The pressure of the gas was 20 kPa. The pressure regulating system is mainly used for supplementing nitrogen to maintain pressure when the system pressure is low (mainly in the early stage of driving and the positive pressure part of the system, namely the outlet of the Roots blower to the gas phase inlet end of the sulfonator, and trace gas leakage exists); when the pressure of the system is higher (mainly expressed as that the negative pressure part of the system, namely the outlet of the sulfonator to the inlet of the Roots blower, has air micro-suction), a small vacuum pump is used for sucking air to maintain the pressure.

Separating the sulfonated product by a gas-liquid separator, and recycling the gas phase (mixing with oxygen, and conveying the mixture into a sulfur furnace by a Roots blower); the liquid phase is sulfonate, and the dodecylbenzene sulfonic acid is produced through an aging and hydrolysis system. The quality of the obtained product is as follows:

specific emission reduction contrast

Example 2:

mixing the tail gas after gas-liquid separation after sulfonation with oxygen input into a system, and feeding the mixture into a sulfur furnace through a Roots blower; adjusting the oxygen amount, and controlling the oxygen concentration of the mixed gas entering the sulfur furnace to be 22%.

Simultaneously, liquid sulfur enters a sulfur burning furnace according to the flow of 300kg/h and is combusted in the sulfur burning furnace in a contact way; the frequency of the Roots blower is adjusted, and the temperature of the combustion sulfur is controlled to be 650 ℃. SO produced by combustion₂Gas, pressConventional process, conversion in conversion tower, cooling in cooler, and SO₃Filtering with a filter to obtain SO with the temperature of 55 DEG C₃Gas enters a falling film type sulfonation reactor; simultaneously, the fatty alcohol-polyoxyethylene ether enters a sulfonator at the flow rate of 2500kg/h and reacts with SO₃The gas contacts to carry out sulfonation reaction.

SO maintenance at gas phase inlet of sulfonator by pressure regulation system₃The pressure of the gas was-10 kPa. The pressure regulating system is mainly used for supplementing nitrogen to maintain the pressure when the system pressure is lower; when the system pressure is higher, a small vacuum pump is used to suck air to maintain the pressure.

The sulfonated product is separated by a gas-liquid separator, and the gas phase is recycled (mixed with oxygen and then conveyed into a sulfur furnace by a Roots blower). The liquid phase is sulfate, and the fatty alcohol-polyoxyethylene ether sodium sulfate is obtained through production by a vacuum neutralization system. The quality of the obtained product is as follows:

specific emission reduction contrast

Example 3:

Meanwhile, liquid sulfur enters a sulfur burning furnace according to the flow of 280kg/h, is in contact combustion in the sulfur burning furnace, the frequency of a Roots blower is adjusted, and the temperature of the sulfur burning is controlled to be 600 ℃. SO produced by combustion₂Gas is converted by a conversion tower, cooled by a cooler and SO according to the conventional process₃Filtering with a filter to obtain SO with the temperature of 55 DEG C₃Gas enters a falling film type sulfonation reactor; simultaneously, alpha olefin enters a sulfonator at the flow rate of 1700kg/h and is mixed with SO₃By contact of gasesAnd (4) carrying out sulfonation reaction.

And (4) separating the sulfonated product by a gas-liquid separator, and recycling the gas phase. The liquid phase is sulfonate, and sodium alpha olefin sulfonate is produced through a neutralization hydrolysis system. The quality of the obtained product is as follows:

specific emission reduction contrast

Claims

1. Gas phase SO₃A sulfonation production system, characterized by: the device comprises a Roots blower, a sulfur furnace and an SO which are communicated with each other in sequence by pipelines₂Conversion column, SO₃Cooler, SO₃A filter, a sulfonator, a gas-liquid separator and a subsequent treatment system;

2. Gas-phase SO according to claim 1₃A sulfonation production system, characterized by: an oxygen content analyzer is arranged on a pipeline for communicating the outlet end of the Roots blower with the gas phase inlet of the sulfur burner;

and a pressure regulating system is arranged on a pipeline for communicating the gas-phase outlet of the gas-liquid separator with the suction end of the Roots blower.

3. The gas phase of claim 2SO₃A sulfonation production system, characterized by: the liquid phase outlet of the gas-liquid separator is communicated with a subsequent treatment system; the subsequent treatment system is one of a fatty alcohol-polyoxyethylene ether vacuum neutralization system, an alkylbenzene aging hydrolysis system, an alpha olefin neutralization hydrolysis system, a fatty acid methyl ester aging system, a re-esterification bleaching system or a neutralization drying system.