TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Method: The fertilizer product produced by: the steps (a)-(d) as above per se, and providing gas exiting the third catalytic bed with at least 90% reduction in sulfur oxides, nitrogen oxides and carbon oxide as compared to the stack gases delivered to the catalytic flow-through bed through the stack; and the step (e1) as above per se. In the methods (M1) and (M2): the beds providing each of the first, second and third catalytic beds are positioned between screens having 150-350 mesh; each of the first, second and third catalytic beds are provided on a rotating disk; the stack gases exiting from third catalytic bed through the stack have at least 95% reduction in sulfur oxides, nitrogen oxides and carbon oxide as compared to the stack gases delivered to the first catalytic flow-through bed; the stack gases exiting from third catalytic bed through the stack have at least 95% reduction in aluminum compounds, sulfur oxides, nitrogen oxides and carbon oxide as compared to the stack gases delivered through the stack to the fourth catalytic flow-through bed; the stack gases exiting a stack from the third catalytic bed through the stack are at least 99% reduction in sulfur oxides, nitrogen oxides and carbon oxide as compared to the stack gases delivered through the stack to the first catalytic flow-through bed; and the gases exiting the stack from the third catalytic bed are at least 99% reduction in aluminum compounds, sulfur oxides, nitrogen oxides and carbon oxide as compared to the stack gases delivered through the stack to the fourth catalytic flow-through bed. The methods (M1) and (M2) further comprise providing a fourth catalytic flow-through bed of calcium zeolite comprising zeolite particles of 44-64 mu m in size positioned in the stack before the first catalytic bed with an electrical charge beneath the fourth catalytic flow-through bed to collect aluminum compounds from the stack gases before passing through the first catalytic bed. In the step (e1), the first, second and third catalytic beds are purged with liquid nitrogen to remove solids and liquids collected from the stack gases by the beds. In the method (M2) and production method of fertilizer product, the first, second and third catalytic beds are provided on the rotating disk, so that the stack gases in the step (d1) can be continuously passed through the first, second and third catalytic beds to provide collection of solids and liquids from the stack gases while other portions of the same beds or like beds are purged with nitrogen to remove solids and liquids collected from the stack gas by the beds. In the method (M2), the fourth catalytic flow-through bed is on the rotating disk, so that the stack gases are continuously move through the fourth bed while other portions of the same beds or a like bed are purged with nitrogen i.e. liquid nitrogen to remove solids and liquids collected from the stack gas by the fourth bed. In the methods (M1), (M2) and (M3), at least two series of sequential through the first, second and third catalytic beds are provided in a parallel, so stack gas can be cleaned by the method through one series of beds while other series of the beds can be cleaned. The method (M3) further comprises providing an another catalytic flow-through bed of calcium zeolite comprising zeolite particles of 44-64 mu m in size positioned in the stack before the first stated catalytic bed with an electrical charge beneath the another catalytic flow-through bed to collect aluminum compounds from the stack gases before passing through the first stated catalytic bed. In the method (M3): the catalytic flow-through bed is intermittently purged with liquid nitrogen to remove solids and liquids collected from the stack gases by the beds; the catalytic flow-through bed is provided on the rotating disk, so that the stack gases in the step (b2) can be continuously passed through the catalytic bed to provide collection of solids and liquids from the stack gases while other portions of the same beds or like beds are purged with nitrogen to remove solids and liquids collected from the stack gas by the bed; the catalytic flow-through bed is purged with liquid nitrogen to remove solids and liquids collected by the beds from the stack gas; the another catalytic flow-through bed is on the rotating disk, so the stack gases are continuously moved through that bed while other portions of the same bed or a like bed are purged with nitrogen i.e. liquid nitrogen to remove solids and liquids collected from the stack gas by the bed; the stack gases exiting from catalytic flow-through bed through the stack have at least 95% reduction in sulfur oxides compared to the stack gases delivered to the first catalytic flow-through bed; the stack gases exiting from the catalytic flow-through beds through the stack have at least 95% reduction in aluminum compounds and sulfur oxides compared to the stack gases delivered through the stack to the other catalytic flow-through beds; the stack gases exiting from catalytic flow-through bed through the stack have at least 99% reduction in sulfur oxides compared to the stack gases delivered through the stack to the first catalytic flow-through bed; and the stack gases exiting from the catalytic flow-through beds through the stack have at least 99% reduction in aluminum compounds and sulfur oxides compared to the stack gases delivered through the stack to the catalytic flow-through beds.    TECHNOLOGY FOCUS - INSTRUMENTATION AND TESTING - Preferred Components: In the apparatuses (A1) and (A2): each of the first, second and third catalytic beds are assembled between screens having 150-350 mesh, and are assembled on the rotating disk, so that stack gases can be continuously passed through the first, second and third catalytic beds to provide collection of solids and liquids from the stack gases while other portions of the same beds or like beds are purged with nitrogen to remove solids and liquids collected from the stack gas by the beds; two series of sequential through the first, second and third catalytic beds are assembled in parallel, so that stack gas can be cleaned through one series of beds while the other series of the beds can be cleaned; and the first, second and third catalytic beds are adapted to collect solids in the catalytic beds, so that stack gases exiting the third catalytic bed have at least at least 95%, preferably at least 99% reduction in sulfur oxides, nitrogen oxides and carbon oxides as compared to the stack gases delivered to the first catalytic flow-through bed or the fourth catalytic flow-through bed through the stack. In the apparatus (A1), the first, second, third and fourth catalytic beds are adapted to collect solids in the catalytic beds, so that stack gases exiting the third catalytic have at least at least 95% reduction in aluminum oxides, sulfur oxides, nitrogen oxides and carbon oxides as compared to the stack gases delivered to the series of catalytic flow-through bed through the stack. The apparatuses (A1) and (A2) additionally comprise the fourth catalytic flow-through bed of calcium zeolite. In the apparatus (A2): an input of purge nitrogen is liquid nitrogen; and the fourth catalytic flow-through bed is on the rotating disk, so that the stack gases can be continuously passed through the fourth catalytic bed to provide collection of aluminum oxides from the stack gases, while other portions of the same beds or like beds are purged with nitrogen to remove aluminum oxides collected from the stack gas by the fourth catalytic flow-through bed. In the apparatuses (A3) and (A4): the catalytic flow-through bed is assembled on the rotating disk, so that the stack gases can be continuously passed through a catalytic flow-through bed to provide collection of sulfur oxide compounds from the stack gases while other portions of the same beds or like beds are purged with nitrogen to remove sulfur compounds collected from the stack gas by the bed; the catalytic flow-through bed is positioned between screens having 150-350 mesh; the first stated catalytic bed collects solids, so that stack gases exiting the catalytic bed provides at least 95% reduction in sulfur oxides compared to the stack gases delivered to the catalytic flow-through bed through the stack; and the catalytic flow bed provides at least at least 99% reduction in sulfur oxides compared to the stack gases delivered to the catalytic flow-through bed through the stack as compared to the stack gases delivered to the catalytic flow-through bed through the stack. In the apparatus (A3): at least two catalytic beds are assembled in parallel, so that stack gas can be cleaned through one of catalytic beds, while at least one other of the beds can be cleaned. The apparatuses (A3) and (A4) further comprises the another catalytic flow-through bed of calcium zeolite. The fertilizer product comprises the fourth catalytic flow-through bed of calcium zeolite. EXAMPLE - No suitable example given.