Device and method for drying chlorine gas through bubble cap drying tower

Abstract

The invention relates to a device and a method for drying chlorine by a bubble cap drying tower. The device comprises a bubble cap tower, an acid circulation system, a new acid feeding system and an acid circulation branch system, the bubble cap tower comprises a tower body, and a filler layer and a bubble cap layer which are sequentially arranged in the tower body from bottom to top, and a dry chlorine outlet is formed in the top of the tower body; firstly, a new acid feeding system is operated, and sulfuric acid is fed into a bubble cap layer; an acid circulation system is operated, so that sulfuric acid circulates in the filler layer; and finally, opening the acid circulation branch system, adjusting the accumulated sulfuric acid flow entering the bubble cap layer, controlling the flow of the sulfuric acid sent out by the new acid sending system to be less than half of the accumulated sulfuric acid flow, and after stable operation, introducing chlorine to be dried into the tower body, sequentially passing through the filler layer and the bubble cap layer, and discharging through a dry chlorine outlet, thereby completing the drying of the chlorine. The method effectively reduces the generation amount of waste sulfuric acid which is difficult to treat in chlor-alkali production, the minimum amount reaches 13.52 kg/ton, and the method is particularly suitable for the situation that the annual output is not higher than 100,000 tons.

Description

technical field [0001] The invention relates to the field of chlorine gas drying, in particular to a device and method for drying chlorine gas in a blister drying tower. Background technique [0002] At present, in the production process of drying chlorine gas in the bubble-cap tower in the industry, in order to ensure the drying effect of the bubble-cap layer of the bubble-cap tower, the flow of sulfuric acid into the bubble-cap layer of the bubble-cap tower with a processing capacity of 100,000 tons of chlorine per year should be controlled at 0.2~ 0.6m 3 / h, the sulfuric acid flow into the blister layer is lower than 0.2m 3 / h, it will reduce the layer height of the sulfuric acid foam in the blister layer, thereby causing the water content index in the chlorine to exceed the standard, causing corrosion of equipment and pipelines, and unqualified product quality affecting safe production. Therefore, in order to ensure that the water content index of chlorine gas reaches t...

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Problems solved by technology

[0002] At present, in the production process of drying chlorine gas in the bubble-cap tower in the industry, in order to ensure the drying effect of the bubble-cap layer of the bubble-cap tower, the flow of sulfuric acid into the bubble-cap layer of the bubble-cap tower with a processing capacity of 100,000 tons of chlorine per year should be controlled at 0.2~ 0.6m 3 / h, the sulfuric acid flow into the blister layer is lower than 0.2m 3 / h, it will reduce the layer height of the sulfuric acid foam in the blister layer, thereby causing the water content index in the chlorine to exceed the standard, causing corrosion of equipment and pipelines, and unqualified product quality affecting safe production. Therefore, in order to ensure that the water content index of chlorine gas reaches the standard (≤300PPm), it must Control the sulfuric acid flow into the blister layer at 0.2-0.6m 3 between / h

However, when the output of chlorine gas is lower than 70,000 tons / year, even if the sulfuric acid flow rate is controlled at 0.2m 3 The lowest flow rate per hour also causes the industry index of sulfuric acid consumption per ton of chlorine to be greater than 16kg, resulting in loss of economic benefits. At present, environmental protection fees are charged for the treatment of waste sulfuric acid containing chlorine radicals, so the relative increase in waste sulfuric acid has caused environmental protection. benefit loss

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