CaSO₃+H₂O+SO₂ → Ca(HSO₃)₂
Mention their States
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h20 is liquid state
raghavsarmukad:
I too know that!!
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A flue gas desulfurization process comprising; a cooling step of cooling and dedusting a sulfur oxides (SOx)-containing flue gas;
an absorption step of contacting the flue gas cooled in the cooling step with a limestone slurry to absorb and remove SOx in the gas;
a pH-adjusting step of adjusting the pH of the resulting slurry containing calcium sulfite and calcium hydrogen sulfite formed in the absorption step;
an oxidation step of oxidizing the resulting slurry obtained in the pH-adjusting step, by contacting it with an oxygen-containing gas to form gypsum;
a concentration step of concentrating the resulting gypsum-containing slurry obtained in the oxidation step to obtain a concentrated gypsum slurry;
a step of adjusting the concentration of the resulting concentrated gypsum slurry;
a step of centrifugally separating gypsum from the concentrated gypsum slurry; and
a step of treating the effluent discharged from the flue gas-cooling step, which includes mixing
the effluent discharged from said cooling step with a portion of said concentrated gypsum slurry, adding a limestone slurry to adjust the pH of the mixture, and then subjecting the mixture to solid-liquid separation to obtain gypsum separately from said concentrated gypsum slurry.
A flue gas desulfurization process as claimed in Claim 1, wherein the pH in the pH-adjusting step is in the range of 4 to 5; the amount of air blown in the oxidation step is in the range of 1.5 to 3 times its theoretical amount; and fine particles of gypsum having passed through a centrifugal separator (53) in the centrifugal separation step are returned to the absorption step and the gypsum concentration in the slurry of said absorption step is 5% by weight or higher.
A flue gas desulfurization process as claimed in Claim 1 or 2 wherein a portion of the flue gas exhausted from the cooling step or a gas obtained by adding air to the said portion is contacted with the slurry withdrawn from said absorption step to obtain gypsum directly.
A flue gas desulfurization process as claimed in Claim 3 wherein an ejector, a reactor provided with a bubble-generating rotor or a reactor further provided with a mechanism for concentrating gypsum in addition to the above rotor is used as a means for said gas-liquid contact.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein the cooling step and the absorption step are carried out in a single tower.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein said step of adjusting the concentration of the concentrated gypsum slurry is carried out by detecting the gypsum concentration by means of a concentration detector (101) and based on the detection signal, controlling the amount of the concentrated slurry and that of the diluted water from said gypsum concentration step.
A flue gas desulfurization process as claimed in claim 6, wherein the concentration of the concentrated gypsum slurry is controlled in the range of 15 to 25% by weight.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein the centrifugal separator (53) used in said centrifugal separation step is provided with an effluent hopper (135) as a receiving dish and an effluent duct (133), said effluent hopper (135) having its opening in said effluent duct (133) and being connected thereto by the medium of bellows (145A,145B) so that a reciprocating motion of the effluent hopper (135) in the lateral direction is effected.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein an oxidation tower (29) is used for said oxidation step, which tower (29) is provided with an atomizer (69) having a conical rotor (67) at its lower part.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein an oxidation tower (29) is used for said oxidation step, and an urgent blow tank (37) provided with fluid-ejecting nozzles directed towards its bottom part in the vertical direction is connected to said oxidation tower (29).
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein said oxidation step is provided with a step of feeding water for controlling the temperature elevation of slurry due to the oxidation reaction of calcium sulfite.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein the water content of the slurry in said oxidation step is adjusted within a range of 92 to 94% by weight
an absorption step of contacting the flue gas cooled in the cooling step with a limestone slurry to absorb and remove SOx in the gas;
a pH-adjusting step of adjusting the pH of the resulting slurry containing calcium sulfite and calcium hydrogen sulfite formed in the absorption step;
an oxidation step of oxidizing the resulting slurry obtained in the pH-adjusting step, by contacting it with an oxygen-containing gas to form gypsum;
a concentration step of concentrating the resulting gypsum-containing slurry obtained in the oxidation step to obtain a concentrated gypsum slurry;
a step of adjusting the concentration of the resulting concentrated gypsum slurry;
a step of centrifugally separating gypsum from the concentrated gypsum slurry; and
a step of treating the effluent discharged from the flue gas-cooling step, which includes mixing
the effluent discharged from said cooling step with a portion of said concentrated gypsum slurry, adding a limestone slurry to adjust the pH of the mixture, and then subjecting the mixture to solid-liquid separation to obtain gypsum separately from said concentrated gypsum slurry.
A flue gas desulfurization process as claimed in Claim 1, wherein the pH in the pH-adjusting step is in the range of 4 to 5; the amount of air blown in the oxidation step is in the range of 1.5 to 3 times its theoretical amount; and fine particles of gypsum having passed through a centrifugal separator (53) in the centrifugal separation step are returned to the absorption step and the gypsum concentration in the slurry of said absorption step is 5% by weight or higher.
A flue gas desulfurization process as claimed in Claim 1 or 2 wherein a portion of the flue gas exhausted from the cooling step or a gas obtained by adding air to the said portion is contacted with the slurry withdrawn from said absorption step to obtain gypsum directly.
A flue gas desulfurization process as claimed in Claim 3 wherein an ejector, a reactor provided with a bubble-generating rotor or a reactor further provided with a mechanism for concentrating gypsum in addition to the above rotor is used as a means for said gas-liquid contact.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein the cooling step and the absorption step are carried out in a single tower.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein said step of adjusting the concentration of the concentrated gypsum slurry is carried out by detecting the gypsum concentration by means of a concentration detector (101) and based on the detection signal, controlling the amount of the concentrated slurry and that of the diluted water from said gypsum concentration step.
A flue gas desulfurization process as claimed in claim 6, wherein the concentration of the concentrated gypsum slurry is controlled in the range of 15 to 25% by weight.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein the centrifugal separator (53) used in said centrifugal separation step is provided with an effluent hopper (135) as a receiving dish and an effluent duct (133), said effluent hopper (135) having its opening in said effluent duct (133) and being connected thereto by the medium of bellows (145A,145B) so that a reciprocating motion of the effluent hopper (135) in the lateral direction is effected.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein an oxidation tower (29) is used for said oxidation step, which tower (29) is provided with an atomizer (69) having a conical rotor (67) at its lower part.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein an oxidation tower (29) is used for said oxidation step, and an urgent blow tank (37) provided with fluid-ejecting nozzles directed towards its bottom part in the vertical direction is connected to said oxidation tower (29).
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein said oxidation step is provided with a step of feeding water for controlling the temperature elevation of slurry due to the oxidation reaction of calcium sulfite.
A flue gas desulfurization process as claimed in any one of the preceding claims, wherein the water content of the slurry in said oxidation step is adjusted within a range of 92 to 94% by weight
I just asked their states :p
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