In view of the characteristics of logistic transportation in JSW DCPL coking project in India,modular design philosophy is applied in the design for primary cooler.According to Indian logistic requirement,the primary cooler shall be cut into modules and selected so as to cater to the need of the project.The application of the modular design for primary cooler is demonstrated by cases in terms of design,manufacturing and installation,etc..

With JH coal as raw material，deashed coal was produced by using the method of two steps of hydrochloric acid-hydrofluoric acid.The effect of reaction conditions on the properties of deashing coal was investigated by single factor method.Through industrial analysis，element analysis，infrared spectrum analysis and gieseler fluidity，the changes of physicochemical properties of JH coal before and after acid cleaning and deashing are analyzed.The results show that the demineralization can reduce the ash content in coal down to 0.51%; the deashing has little effect on the aliphatic hydrocarbon compounds in coal，but has great influence on the aromatic hydrocarbon compounds and the oxygen-containing functional groups; It is also found that under N2 shielded，the deashing has an influence on the fluidity rather than the caking property of coal.

In this paper,the influence of different cokemaking processes on coke quality between top-charge battery and stamp-charge battery is studied.Based on actual production,the coke qualities by the two processes with different coal blending compositions are analyzed.The result shows that the stamp-charge cokemaking can obviously improve the abrasion resistance (M10) and coke strength after reaction (CSR),but has little improvement of coke reactivity index (CRI).The crushing strength of coke (M40) could be possibly improved or degraded,it depends on the proportion of premium coking coal and fat coal.

In view of the problems occurred in charging device of CDQ system for 7.63 m coke oven in Masteel,such as charging emission,poor dust collection and interrupted coke discharging,optimization is put forward,i.e.the charging hopper is added with dust-proof cover;dust main design is optimized;Fit dimensions of the lower hopper and distributor are properly adjusted;besides,the steel structure foundation,framework and electrical cylinder of the existing charging device are reused so that the said problems can be solved.

According to the thermal characteristics of 7.63 m battery and based on the statistical analysis of thermal data and the method of adjusting oven temperature by pausing heating time,a number of oven temperature regulation models are established to solve the problem of accurate control of coke oven temperature under the conditions of environmental temperature,change of coal moisture and fluctuation of production.The oven temperature model improves the maturity of coke cake and effectively reduces the energy consumption for cokemaking.

When coke oven becomes aged,the oven sole bricks would appear damages,which could cause higher pushing current even pushing trouble.The damaged oven sole bricks are replaced by zero expansion silica brick.Its hot repair process is introduced.As a result,the pushing resistance can be dramatically reduced so that the service life of coke oven can be extended.

Analysis is made to the factors affecting the operation of COG ammonia scrubbing by H3PO4 for 7 m top-charge battery.Measures are taken by optimizing the demisting process of ammonia absorber,improving de-oiling efficiency from rich oil,restructuring heat exchanger and improving lean liquor de-sludging,etc..After the optimization,stable operation of the ammonia scrubbing system by H3PO4 can be extended from 3 months to 12 months,and the H3PO4 consumption rate can be reduced from 2.3 kg/t to 1.7 kg/t,which plays a decisive role in COG purification and stable delivery.

This paper introduced the gas purification process in the plant.It analyzed the problems encountered in naphthalene scrubbing in the primary cooler,and proposed several measures,which have achieved a good result so that the net naphthalene content in the COG can meet the requirements for the gas in industrial and domestic use.

Catalyst feed system upgrading in COG desulfurization process is introduced.The upgraded system realizes fully-mixed catalyst solution and stable feeding for a higher desulfurization efficiency,20% lower catalyst cost,less labor intensity of operator and better ambient environment.

This paper introduces that the WSA system of TISCO Coking Plant has been operating with environmental benefits for years.It discusses the WSA principle and process flow and puts forward solutions to the problems such as incomplete combustion,low temperature at outlet of boiler,malfunctions of three-stage heat exchanger,etc..

Through development of a new safety control system for gas exhauster，the exhauster can be switched in time to industrial frequency operation when the exhauster is shut down due to the inverter failure during the frequency conversion operation，so as to avoid a large amount of gas bleeding and ensure stable pressure of the gas pipe network and production.

After long-time operation of final cooler, the built-in light porcelain packings would be adhered with tar and coal dust,it could lead to blockage and higher resistance in the packings, which may affect gas delivery.Online cleaning can solve the problem of high resistance in the final cooler.

In the crude benzene distillation process，there is a phenomenon of wash oil leakage in the separation cylinder.After dismantling the benzol stripper，large amount of oil residue on the tray is found at the inlet of the benzol stripper.The feed inlet is lowered by one layer of tray.The lean oil is observed to see if any change on its quality.As a result，the benzene containing in the lean oil has slightly increased，but due to the reduction of gas volume，the yield of light benzene has not decreased.

In coking project phase 1 for Baosteel,a process of Spray Dryer Absorber (SDA)+bag filter system+Selective Catalytic Reduction (SCR) is adopted for coke oven flue gas DeSOx and DeNOx,which was put into operation in October 2016; for phase 3 & 4,a process of active carbon Soda DeSOx (SDS)+medium & low temperature SCR,which were put into operation in November 2019.Operation of the two processes are compared in terms of operability,DeSOx and DeNOx efficiency,by-products treatment and operating cost.