Development and applications of Baosteel sintering flue gas desulphurization technology

The research background and technical features of Baosteel sintering flue gas desulphurization （ FGD）--swirl- jet-absorbing wet limestone-gypsum sintering FGD technology, process and equipment are introduced in this paper. Main contents and achievements of the pilot experiment and the engineering practice of Baosteel FGD are analyzed and discussed systematically. Past engineering practice experiences indicate that Baosteel FGD has the following merits： wide applicability to sintering flue gas features, such as frequently changing temperatures, unstable SO2 concentration, intensively fluctuating flow rates ,etc. ,high pollutants removal efficiency ,low investment and energy consumption; stable and reliable operation ,utilizable byproduct （gypsum）, etc. It indicates that Baosteel sintering FGD is of extensive application value for the FGD of large and medium-scaled sintering machines.

Study on influencing factors of Baosteel’s swirl-jet sintering FGD technology

This paper introduced the research background and technical features of Baosteel＇ s sintering flue gas desulfurization （FGD）. It was also named swirl-jet-absorbing wet limestone-gypsum sintering FGD technology. By means of industrial online pilot plants, through continuous running and orthogonal tests, the effects of various influencing factors on SO2 removal efficiency of Baosteel sintering flue gas desulgurization （BSFGD） were studied carefully. The results indicate that the slurry pH value,temperature （T） and flow rate （Q） of inlet flue gas,liquid level （H） in the absorber and flue gas jet velocity （V） are the main influencing factors. Furthermore, when pH is between 5.0 and 5.5, H is between 4.2 m and 4.3 m, Q is 43 000 m3/h, T is below 65℃ and V is between 20 m/s and 28 m/s, the best desulfurization efficiency can be available.

A pilot-scale study of selective desulfurization via urea addition in iron ore sintering

The iron ore sintering process is the main source of SO_2 emissions in the iron and steel industry. In our previous research, we proposed a novel technology for reducing SO_2 emissions in the flue gas in the iron ore sintering process by adding urea at a given distance from the sintering grate bar. In this paper, a pilot-scale experiment was carried out in a commercial sintering plant. The results showed that, compared to the SO_2 concentration in flue gas without urea addition, the SO_2 concentration decreased substantially from 694.2 to 108.0 mg/m^3 when 0.10wt% urea was added. NH_3 decomposed by urea reacted with SO_2 to produce（NH_4）_2SO_4, decreasing the SO_2 concentration in the flue gas.

INTERACTION BETWEEN SO_2 FROM FLUE GAS AND SORBENT PARTICLES IN DRY FGD PROCESSES

Among the technologies to control SO2 emission from coal-fired boilers, the dry flue gas desulphurization (FGD) method, with appropriate modifications, has been identified as a candidate for realizing high SO2 removal efficiency to meet both technical and economic requirements, and for making the best quality byproduct gypsum as a useful additive for improving alkali soil. Among the possible modifications two major factors have been selected for study: (1) favorable chemical reaction kinetics at elevated temperatures and the sorbent characteristics; (2) enhanced diffusion of SO2 to the surface and within the pores of sorbent particles that are closely related to gas-solid two-phase flow patterns caused by flue gas and sorbent particles in the reactor. To achieve an ideal pore structure, a sorbent was prepared through hydration reaction by mixing lime and fly ash collected from bag house of power plants to form a slurry, which was first dewatered and then dried. The dry sorbent was found capable of rapid conversion of 70% of its calcium content at 700℃, reaching a desulphurization efficiency of over 90% at a Ca/S ratio of 1.3. Experiments confirmed that the diffusion effect of SO2 is an important factor and that gas-solid two-phase flow plays a key role to mixing and contact between SO2 and sorbent particles. For designing the FDG reactor, a new theoretical drag model was developed by combination of CFD with the Energy Minimization Multi-Scale (EMMS) theory for dense fluidi-zation systems. This new drag model was first verified by comparing calculated and measured drag values, and was then implemented in simulation of gas-solid two-phase flow in two circulating fluidized beds with different sizes and flow parameters. One riser has diameter and height of 0.15 m×3m and another one 0.2m×14.2m. Their superficial gas velocities are 4 and 5.2 m·s-1, respectively, and the circulating rate 53 and 489 kg·(m-2·s-1). FCC particles were used in both cases. The results show that not only the static pressure drop along the riser height, but also radial distributions of particle volume fraction have been very well predicted in comparison with experiments. The new drag model is expected to shed more light on the further improvement of SO2 diffusion to solid sorbent and optimization of reactor structure.

CO_(2)emission evaluation and cost analysis of oxygen blast furnace process with sintering flue gas injection

In order to achieve ultra-low emissions of SO_(2)and NO_(x),the oxygen blast furnace with sintering flue gas injection is presented as a promising novel process.The CO_(2)emission was examined,and a cost analysis of the process was conducted.The results show that in the cases when the top gas is not circulated(Cases 1–3),and the volume of injected sintering flue gas per ton of hot metal is below about 1250 m^(3),the total CO_(2)emissions decrease first and then increase as the oxygen content of the blast increases.When the volume of injected sintering flue gas per ton of hot metal exceeds approximately 1250 m^(3),the total CO_(2)emissions gradually decrease.When the recirculating top gas and the vacuum pressure swing adsorption are considered,the benefits of recovered gas can make the ironmaking cost close to or even lower than that of the ordinary blast furnace.Furthermore,the implementation of this approach leads to a substantial reduction in total CO_(2)emissions,with reductions of 69.13%(Case 4),70.60%(Case 5),and 71.07%(Case 6),respectively.By integrating previous research and current findings,the reasonable oxygen blast furnace with sintering flue gas injection can not only realize desulfurization and denitrification,but also achieve the goal of reducing CO_(2)emissions and ironmaking cost.

Reaction intermediates and products characterisation of NH_(3) in desulphurisation with activated coke

The sulphate is an important factor restricting the efficient and stable operation of the activated coke (AC) flue gas purification system. The simulation experiments and in situ infrared tests of AC taken from desorption tower of the AC flue gas purification system were carried out to first calibrate the thermal desorption characteristics of adsorbed NH_(3) and sulphate and explore the reaction behaviour of NH_(3) with SO_(2) and H_(2)SO_(4). On this basis, some advice for optimising the sulphate generation was put forward to improve the purification efficiency of the AC system. The results show that the temperatures of the desorption of adsorbed NH_(3), the decomposition of (NH_(4))_(2)SO_(4) and NH_(4)HSO_(4) are 224, 276 and 319 ℃, respectively, which lays the foundation for the quantitative analysis of sulphate on AC. Regardless of the NH_(3) amount, only a small portion of H_(2)SO_(4) is converted to sulphate, as the H_(2)SO_(4) deposited in AC pores or agglomerated together could not come into contact with NH_(3). The final reaction product of NH_(3) and SO_(2) is mainly (NH_(4))_(2)SO_(4) which is continuously generated because the newly generated H_(2)SO_(4) is continually exposed to NH_(3), if NH_(3) is enough. The reaction of NH_(3) with H_(2)SO_(4) takes precedence over with NH_(4)HSO_(4). In the initial stages in which H_(2)SO_(4) is exposed to NH_(3), the product is essentially all NH_(4)HSO_(4) as intermediate. Then, it is further converted to (NH_(4))_(2)SO_(4) whose amount reaches equilibrium when the accessible H_(2)SO_(4) is exhausted. All the NH_(3) adsorbed on AC entering the desulphurisation tower generates NH_(4)HSO_(4), but the amount is limited. The remaining SO_(2) entering the denitrification tower mainly generates (NH_(4))_(2)SO_(4);thus, limiting the remaining SO_(2) amount is necessary to guarantee denitrification efficiency. When the NH_(3) injection is changed to the desulphurisation tower, the initial NH_(3) injection rate can be increased to complete the conversion of accessible H_(2)SO_(4) as soon as possible in order to obtain higher denitrification efficiency.