Steam stripping method of process condensate in CO conversion

A condensate and stripping technology, applied in the direction of heating water/sewage treatment, degassed water/sewage treatment, etc., can solve the problems affecting the long-term operation of the conversion device, ammonium salt crystals block the pipeline and condenser, etc., and achieve a solution The effect of ammonium salt crystallization blockage, improvement of recycling rate, and reduction of wastewater discharge

Active Publication Date: 2009-11-04
CHINA PETROCHEMICAL CORP +2
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Because the acid gas stripped by the traditional single-column process condensate stripping process contains carbon dioxide and ammonia at the same time, in the subsequent condensation process, carbon dioxide and ammonia are easy to generate ammonium salt crystals to block the pipeline and condenser, seriously affecting the conversion device Safe and stable long-term operation

Method used

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  • Steam stripping method of process condensate in CO conversion

Examples

Experimental program
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Effect test

Embodiment 1

[0021] The process condensate (temperature: 110°C; pressure (gauge pressure) 0.8MPa) from the gas-liquid separator in the conversion process first enters the carbon dioxide stripper 2 (operating temperature of the carbon dioxide stripper 2: 140°C; operating pressure (gauge pressure) ) 0.27MPa, packing height is 0.5 meter) upper part carries out flashing, and the secondary steam (temperature: 142 ℃; pressure (gauge pressure) 0.28MPa) from the ammonia stripper 3 upper part enters from the carbon dioxide stripper 2 bottom, Countercurrent contact stripping of carbon dioxide with the process condensate after flash evaporation, the acid gas (temperature: 138°C; pressure (gauge pressure) 0.27MPa) stripped from the top of the tower enters the carbon dioxide stripping tower condenser 4 to cool, and then passes through the carbon dioxide stripping tower Extractor separator 5, non-condensable acid gas (temperature of non-condensable acid gas: 50°C; pressure (gauge pressure) 0.20MPa) is se...

Embodiment 2

[0025] The process condensate (the temperature of the process condensate: 125°C; the pressure (gauge pressure) 1.0MPa) from the gas-liquid separator in the conversion process first enters the carbon dioxide stripper 2 (the operating temperature of the carbon dioxide stripper 2: 157°C; The operating pressure (gauge pressure) is 0.52MPa, and the packing height is 1.5 meters), and the upper part is flashed, and the secondary steam from the upper part of the ammonia stripper 3 (the temperature of the secondary steam: 160°C; the pressure (gauge pressure) 0.52MPa) Enter from the bottom of the carbon dioxide stripping tower 2, and carry out countercurrent contact with the flashed process condensate to strip carbon dioxide, and the acid gas (temperature of acid gas: 157°C; pressure (gauge pressure) 0.52MPa) stripped from the top of the tower is fed into carbon dioxide The stripper condenser 4 is cooled, and then through the carbon dioxide stripper separator 5, the non-condensable acid ...

Embodiment 3

[0029] The process condensate (the temperature of the process condensate: 115°C; the pressure (gauge pressure) 0.90MPa) from the gas-liquid separator in the conversion process first enters the carbon dioxide stripper 2 (the operating temperature of the carbon dioxide stripper 2: 144°C; The upper part of the operating pressure (gauge pressure) is 0.34MPa, and the packing height is 1.0m), and the upper part is flashed, and the secondary steam from the upper part of the ammonia stripper 3 (the temperature of the secondary steam: 148°C; pressure (gauge pressure) 0.35MPa) Enter from the bottom of the carbon dioxide stripping tower 2, and carry out countercurrent contact with the process condensate after flashing to strip carbon dioxide, and the acid gas (temperature of acid gas: 144°C; pressure (gauge pressure) 0.34MPa) stripped from the top of the tower is fed into carbon dioxide The stripper condenser 4 is cooled, and then through the carbon dioxide stripper separator 5, the non-c...

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Abstract

The invention relates to a steam stripping method of process condensate in CO conversion. The invention is characterized in that the process condensate firstly enters the upper part of a carbon dioxide steam stripping tower for flashing evaporation; secondary steam from the upper part of an ammonia-evaporated steam stripper tower enters the bottom part of the carbon dioxide steam stripping tower and steam strips carbon dioxide by countercurrent contacting with the process condensate after flashing evaporation; the process condensate after flash evaporation and the steam stripped carbon dioxide carry out countercurrent contact; the process condensate after flash evaporation and steam stripping enters the upper part of the ammonia-evaporated steam stripper tower from the bottom part of the carbon dioxide steam stripping tower and is steam-stripped by low-pressure steam entering from a kettle of the ammonia-evaporated steam stripper tower; gas phase is treated by secondary condensation to obtain non-acid-coagulated gas and condensate sewage; and steam stripping water is obtained from the bottom part of the ammonia-evaporated steam stripper tower. The invention carries out steam stripping on the upper and lower towers to carbon dioxide and ammonia in the process condensate respectively, thus avoiding the possibility of coexistence of carbon dioxide and ammonia in a condensing system, effectively solving the problem that the steam stripping system of the process condensate in the conversion procedure occurs ammonium salt crystallization blockage and prolonging the period of stable operation of a conversion device.

Description

technical field [0001] The present invention relates to a method for stripping process condensate in CO shift. Background technique [0002] The carbon monoxide in the feed gas of the ammonia synthesis plant is generally removed by shift reaction, which consumes only cheap water vapor, and can produce hydrogen equivalent to the reacted carbon monoxide, and at the same time convert carbon monoxide into carbon dioxide which is easy to remove. In order to control the shift reaction depth, bed temperature and suppress the occurrence of methanation side reactions, the general shift reaction needs to add excess water vapor, and the shift gas after reaction and the remaining water vapor will be cooled and condensed in the subsequent waste heat recovery system to obtain process condensation liquid. The condensed process condensate with dissolved ammonia and carbon dioxide is sent to the process condensate stripping tower for stripping, so as to improve the reuse rate of water in th...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C02F1/04C02F1/20
Inventor 郑明峰李继炳许仁春周忠立张骏驰梁忠东何英施程亮
Owner CHINA PETROCHEMICAL CORP
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