Upgrading And Transformation Of Recovery And Purification System Of The Coal Coking Company Of Tianan

Gas cleaning and recovery system is an important part of coke-making process, the pollutant emissions and cost control must bring forward higher requires to the Coking enterprise with the economic and social development. While due to the difference of technology and equipment, management and operation level, the efficiency of management and operation are greatly different in the gas purification and recovery system. Therefore, the problems are systematic through internships practice, process units and individual equipment testing, comparison and analysis of the theoretical work in whole process of gas purification and recovery system for Coal Coking Company of Tian an, Xuzhou in this paper. The problems of production disturbance, gas containing H2 S and NH3-N over proof would be fundamental solution through separating the impact of operations run key and parameters and gradual implementation of technological innovation and improve.That focuses on the primary gas cooling process, improvement and transformation processes of PDS desulfurization and wastewater ammonia evaporation in this paper. The results showed that:(1) The key influence of whole purification system is the operation of primary gas cooling. The gas temperature of after initial cold was higher than the design value of about 4 ?, the actual temperature was sometimes higher than 10? in summer through field test and analysis, which would bring about being not normal to the subsequent process operation and being poor results for degreasing, naphthalene. The problem was serious clogging the cooling tower, an insufficient amount of cold water in summer and so on. To do this, first a primary cooler, maintenance and reconstruction of the cold frame, reducing the drain pipe string; secondly need to add cold water 574.1m3/h or the ability to transform and upgrade the refrigerator; the third to improve water quality and water cooling towers except dirt and so on.(2) For the desulfurization system, due to the pre-cooling tower gas inlet and coolant temperature was high leading to the temperature of the gas into the desulfurization tower above the design value of 3 ~ 5 ?, ammonia and lye temperature steam from the high post, resulting in the desulfurization process Deputy salt increased production and constantly adjust desulfurization catalyst PDS content, improve the desulfurization efficiency of the operation was not desirable. The reasonable solution was to stabilize and control the amount of catalyst performance, keeping the reaction temperature by gas desulfurization before the procedure.(3) There was unstable operation and NH3-N content was too high in waste water mainly due to fluctuation of water inflow, the remaining ammonia containing more oil, bottoms indirect steam heat resistance being more, eventually leading to lower tray efficiency in Ammonia evaporation system. Soda was used to increase the value pH from the value of design8~9 to9~10.5, NH3-N content could be made on the surface of the standards, while alkaline overweight is bad for microbial life in biochemical. To this end, the first increase in the surplus ammonia tank ceramic filters to reduce the oil content of water; Second, before the high ammonia evaporation tower increase the buffer tank, stable Ammonia Stripper capacity; third, a comprehensive clean ammonia evaporation tower blockage, or summer use steam instead of direct indirect steam heating and flow control to 0.265 Kg / kg water; fourth, after replacing the ammonia steam towers vapor condensing points, a cryogenic cooler condensate while increasing the amount of water to ensure that the temperature of the liquid ammonia into the desulfurization tower 40 ?.The remaining measures have been effective in addition to the cooling water system being not completed after nearly a year of transformation and practice. The operation showed that the H2 S and NH3-N content had been normal standards after gas purification, the operation was stable.