CN211734228U

CN211734228U - Gas phase SO3Sulfonated tail gas recycling production system

Info

Publication number: CN211734228U
Application number: CN201922417929.5U
Authority: CN
Inventors: 方银军; 葛赞; 史立文; 方灵丹; 胡剑品; 邹欢金
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: 2020-10-23
Anticipated expiration: 2029-12-27

Abstract

The utility model belongs to the technical field of fine chemistry industry. Aims to provide a gas phase SO₃The sulfonated tail gas is recycled to the production system; the production system has the characteristics of investment saving and convenient maintenance. The technical scheme is as follows: gas phase SO₃Recycling of sulfonated tail gasThe production system is characterized in that the device comprises a Roots blower, a sulfur furnace and an SO which are communicated in sequence by pipelines₂Conversion column, SO₃Cooler, SO₃The device comprises a filter, a sulfonator, a gas-liquid separator and an electrostatic demister, wherein a liquid phase outlet of the gas-liquid separator is communicated with a subsequent treatment system; the gas suction end of the Roots blower is communicated with a gas phase outlet of the electrostatic demister through a pipeline, and the outlet end of the Roots blower is communicated with a gas phase inlet of the sulfur burner through a pipeline; and an oxygen inlet is also arranged on the pipeline of the suction end of the Roots blower.

Description

Gas phase SO3Sulfonated tail gas recycling production system

Technical Field

The utility model belongs to the technical field of fine chemistry industry, concretely relates to gaseous SO for producing anion surfactant₃Sulfonated tail gas recycling 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 sulfonation process commonly used at present generally adopts gas-phase SO₃Sulfonation, i.e. converting sulfur and dry air into SO with low gas concentration (generally 3-6%) by combustion₃Mixing air with the gas, and sulfonating by contacting with organic material. This technique SO₃High utilization rate, relative green environmental protection, but because of the need of a large amount of air as SO₃The exhaust emission of the diluent is large, and the exhaust emission of one ton of products (measured by active matters) is about 1500-2000 m3 generally. At the same time due to SO₂To SO₃The conversion of (A) is generally only 98.5%, SO that the final tail gas contains a certain amount of SO₂Only using alkali absorption tower for treatment and consumptionAnd a large amount of saline-alkali containing washing water is generated at the same time of alkali, and the treatment is complicated.

CN102513039 discloses a method for recycling sulfonated tail gas, which recycles tail gas after an electrostatic demister as SO₃The diluent of (1). However, in the process, 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 liquid 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 SO₃The sulfonated tail gas is recycled to the production system; the production system has the characteristics of investment saving and convenient maintenance.

The utility model provides a technical scheme is:

gas phase SO₃The sulfonated tail gas recycling production system is characterized in that the device comprises a Roots blower, a sulfur furnace and an SO which are communicated with each other in sequence by pipelines₂Conversion column, SO₃Cooler, SO₃The device comprises a filter, a sulfonator, a gas-liquid separator and an electrostatic demister, wherein a liquid phase outlet of the gas-liquid separator is communicated with a subsequent treatment system;

the gas suction end of the Roots blower is communicated with a gas phase outlet of the electrostatic demister through a pipeline, and the outlet end of the Roots blower is communicated with a gas phase inlet of the sulfur burner through a pipeline; and an oxygen inlet is also arranged on the pipeline of the suction end of the Roots blower.

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 adjusting system is arranged on a pipeline communicated with the gas phase outlet of the electrostatic demister and 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 is regulated in the following way: when the inlet gas phase pressure is lower, appropriately supplementing dry air (or nitrogen); when the gas phase pressure at the inlet is higher, the gas is properly pumped out.

The liquid phase outlet of the gas-liquid separator is connected with a subsequent treatment system through a pipeline; the post-treatment system can be a fatty alcohol-polyoxyethylene ether vacuum neutralization system or an alpha olefin neutralization hydrolysis 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 gas-liquid separator, the electrostatic defogging of sulfonation, 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 alkali absorption tower and other related tail gas treatment devices and a dry air system required by the original system are not required, and the equipment investment and the operation cost are greatly reduced.

3) By reducing the head gas phase pressure of the sulfonator, the organic material is made to be in higher SO₃The method 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 of fatty alcohol-polyoxyethylene ether and alpha olefin, and SO₃The gas volume concentration should be maintained at 2.5-3.5%, and too high gas volume concentration can cause serious 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.

4) The gas phase pressure at the head of the sulfonator is reduced, the gas flow state in the pipe bundle of the sulfonator can be changed, the entrainment amount of organic acid mist in the sulfonated tail gas is reduced, and finally the generation of electrostatic acid is reduced. By using the process, the electrostatic acid can be reduced by about 20 percent. Meanwhile, in the process of sulfonating fatty alcohol polyoxyethylene ether, the dioxane in the acid ester can be reduced to be within 20ppm from about 50ppm originally.

4) 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;

5) due to limitations in catalytic efficiency of the converterPreparation of 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.

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 view of the structure of a production system according to 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 SO₃The device comprises a filter, a sulfonator, a gas-liquid separator, a static demister, a pressure regulating system and a subsequent treatment system, wherein the filter is 9, the gas-liquid separator is 10, the static demister is 11, and the subsequent treatment system is 13.

Detailed Description

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

Gas phase SO shown in FIG. 1₃The sulfonated tail gas recycling production system comprises a Roots blower 4, a sulfur furnace 5 and SO which are communicated with each other in sequence by pipelines₂Conversion tower 6, SO₃Cooler 7, SO₃The filter 8, the sulfonator 9, the gas-liquid separator 10 and the electrostatic demister 11, wherein a liquid phase outlet of the gas-liquid separator is communicated with a subsequent treatment system 13;

A pressure adjusting system 12 is arranged on a pipeline communicated with the gas phase outlet of the electrostatic demister and the suction end of the Roots blower; what is needed isThe pressure regulating system is mainly used for regulating SO at the inlet of the sulfonator₃The gas phase pressure of the gas is regulated in the following way: when the inlet gas phase pressure is lower, appropriately supplementing dry air (or nitrogen); when the gas phase pressure at the inlet is higher, the gas is properly pumped out.

Example 1:

the tail gas after being sulfonated and subjected to electrostatic demisting is mixed with oxygen with a certain flow in front of a Roots blower, and then enters a sulfur furnace through the Roots blower, and the oxygen amount is adjusted to control the oxygen concentration of the mixed gas entering the sulfur furnace to be 22%.

Meanwhile, liquid sulfur enters a sulfur burning furnace according to the flow of 300kg/h, is in contact combustion in the sulfur burning furnace, the frequency of a Roots blower is adjusted, and the sulfur burning temperature is controlled to be 650 ℃. 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, 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-20 kPa. The pressure regulating system mainly uses a small vacuum pump to suck air to maintain the pressure.

And (4) separating the sulfonated product by a gas-liquid separator, and recycling the gas phase after electrostatic demisting. The liquid phase is fatty alcohol polyoxyethylene ether sodium sulfate produced by a vacuum neutralization system of sulfate. The quality of the obtained product is as follows:

specific emission reduction contrast

Example 2:

the tail gas after being sulfonated and subjected to electrostatic demisting is mixed with oxygen with a certain flow in front of a Roots blower, and then enters a sulfur furnace through the Roots blower, and the oxygen amount is adjusted to control the oxygen concentration of the mixed gas entering the sulfur furnace to be 24%.

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 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 mainly maintains the pressure by supplementing nitrogen when the system pressure is lower (less occurs); when the system pressure is higher (mainly in the early stage of driving and the negative pressure part of the system, a small amount of air is sucked), a small vacuum pump is used for sucking air to maintain the pressure.

And (4) separating the sulfonated product by a gas-liquid separator, and recycling the gas phase after electrostatic demisting. The liquid phase is sulfonate, and alpha olefin sodium sulfonate is produced through a neutralization hydrolysis 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 300kg/h, is in contact combustion in the sulfur burning furnace, the frequency of a Roots blower is adjusted, and the sulfur burning temperature is controlled to be 500 ℃. 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, 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 0 kPa. The pressure regulating system mainly uses a small vacuum pump to suck air to maintain the pressure.

specific emission reduction contrast

Claims

1. Gas phase SO₃The sulfonated tail gas recycling production system is characterized in that: the device comprises a Roots blower (4), a sulfur furnace (5) and an SO which are communicated with each other in sequence by pipelines₂Conversion tower (6), SO₃Cooler (7), SO₃The device comprises a filter (8), a sulfonator (9), a gas-liquid separator (10) and an electrostatic demister (11), wherein a liquid phase outlet of the gas-liquid separator is communicated with a subsequent treatment system (13);

the gas suction end of the Roots blower is communicated with a gas phase outlet of the electrostatic demister through a pipeline, and the outlet end of the Roots blower is communicated with a gas phase inlet of the sulfur burner through a pipeline; and an oxygen inlet (1) is also arranged on the pipeline of the suction end of the Roots blower.

2. Gas-phase SO according to claim 1₃The sulfonated tail gas recycling production system is characterized in that: 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 (12) is arranged on a pipeline communicated with the gas phase outlet of the electrostatic demister and the suction end of the Roots blower.

3. Gas-phase SO according to claim 2₃The sulfonated tail gas recycling production system is characterized in that: the liquid phase outlet of the gas-liquid separator is connected with a subsequent treatment system through a pipeline; the post-treatment system is a fatty alcohol-polyoxyethylene ether vacuum neutralization system or an alpha olefin neutralization hydrolysis system.