Process control of continuous sodium-limestone flue gas desulfurization system

• US 4,431,618 A
• Filed: 10/12/1982
• Issued: 02/14/1984
• Est. Priority Date: 10/12/1982
• Status: Expired due to Term

• Current Assignee: Ontario Hydro A Corporation Continued Under The Power Corporation Act RSO 1980 Chapt 384
• Original Assignee: FMC Corporation
• Inventors: Boward, Willard L. Jr., Wang, Kuei H.
• Primary Examiner(s): HELLER, GREGORY
• Application Number:
  US06/433,578
• Time in Patent Office: 490 Days
• Field of Search: 423/242 A, 423/242 R, 423/243, 423/244 A, 423/244 R, 422/62, 436/55, 436/163
• US Class Current: 423/243.09
• CPC Class Codes: B01D 53/501 by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
• CPC Class Codes: Y10T 436/12 Condition responsive control

Abstract

A method of controlling the continuous operation of the absorption and regeneration processes of a sodium-limestone double alkali flue gas desulfurization system, in which measurements of absorber effluent solution pH or flow diverted for regeneration are used as the primary control parameter governing the limestone addition rate.

Claims

1. In a sodium-limestone double alkali process for the continuous desulfurization of flue gas, having the steps of absorbing sulfur dioxide from a SO₂ -containing gas stream in an absorber with an aqueous solution of sodium sulfite and sodium bisulfite, diverting at least a portion of the absorber effluent solution for regeneration with limestone, introducing limestone into the diverted absorber effluent solution to convert bisulfite to sulfite, separating byproduct solids from the limestone-treated solution, and returning regenerated solution to the absorber, the improvement for controlling the continuous, integrated operation of the absorption and regeneration which comprises

(a) diverting absorber effluent solution for limestone regeneration, such absorber effluent solution having a pH in the range of from 5.5-6.7;

(b) introducing into the diverted absorber effluent solution less than a stoichiometric amount of ground limestone, based on the theoretical calcium carbonate required to completely neutralize the bisulfite content of such absorber solution to sulfite, to maintain the pH of the regenerated solution at a higher pH value within the range of 6.2-7.0 and to convert from 20-70% of the solution bisulfite content to sulfite;

(c) controlling the limestone addition primarily via either

(i) feed forward pH measurements of the diverted absorber effluent solution, the flow of diverted absorber solution being maintained at a relatively constant rate, or

(ii) feed forward flow measurements of the diverted absorber effluent solution, the flow of diverted absorber effluent solution being adjusted automatically to provide a relatively constant absorber effluent solution, pH, with feedback pH measurements of the limestone-treated solution being used to provide trimming control of the limestone addition; and

(d) compensating for process losses of sodium values by adding soda ash or sodium hydroxide at a rate sufficient to maintain the system solution active sodium content at a value within the range of 0.2-2 M, measured as the sum of the bisulfite molar concentration plus twice the sulfite molar concentration of the absorber effluent solution.

4. The process of claim 1, 2 or 3 wherein the absorber effluent solution pH is within the range of 6.0-6.3.

5. The process of claim 1, 2 or 3 wherein the regenerated solution pH is within the range of 6.4-6.8.

6. The process of claim 1, 2 or 3 wherein from 20-60% of the solution bisulfite content is converted to sulfite during regeneration.

7. The process of claim 1, 2 or 3 wherein the active sodium content is maintained at a value within the range of from 0.5-1.5 M.

8. The process of claim 1, 2 or 3 wherein evaporative losses of water during the absorption process are compensated for by the addition of make-up water during the regeneration.

2. In a sodium-limestone double alkali process for the continuous desulfurization of flue gas, having the steps of absorbing sulfur dioxide from a SO₂ -containing gas stream in an absorber with an aqueous solution of sodium sulfite and sodium bisulfite, diverting at least a portion of the absorber effluent solution for regeneration with limestone, introducing limestone into the diverted absorber effluent solution to convert bisulfite to sulfite, separating byproduct solids from the limestone-treated solution, and returning regenerated solution to the absorber, the improvement for controlling the continuous, integrated operation of the absorption and regeneration which comprises

(a) diverting a relatively constant flow of absorber effluent solution for limestone regeneration, such flow selected to provide an absorber effluent solution pH in the range of from 5.5-6.7 for design gas stream flow and SO₂ -level conditions;

(b) introducing into the diverted absorber effluent solution less than a stoichiometric amount of ground limestone, based on the theoretical calcium carbonate required to completely neutralize the bisulfite content of such absorber solution to sulfite, to maintain the pH of the regenerated solution at a higher pH value within the range of 6.2-7.0 and to convert from 20-70% of the solution bisulfite content to sulfite, such limestone addition being controlled via feed forward pH measurements of the absorber effluent solution and trimmed via feedback pH measurements of the limestone-treated solution; and

(c) compensating for process losses of sodium values by adding soda ash or sodium hydroxide at a rate sufficient to maintain the system solution active sodium content at a value within the range of 0.2-2 M, measured as the sum of the bisulfite molar concentration plus twice the sulfite molar concentration of the absorber effluent solution.

3. In a sodium-limestone double alkali process for the continuous desulfurization of flue gas, having the steps of absorbing sulfur dioxide from a SO₂ -containing gas stream in an absorber with an aqueous solution of sodium sulfite and sodium bisulfite, diverting at least a portion of the absorber effluent solution for regeneration with limestone, introducing limestone into the diverted absorber effluent solution to convert bisulfite to sulfite, separating byproduct solids from the limestone-treated solution, and returning regenerated solution to the absorber, the improvement for controlling the continuous, integrated operation of the absorption and regeneration which comprises

(a) diverting absorber effluent solution for limestone regeneration in an amount such that the absorber effluent solution pH is maintained at a relatively constant value in the range of from 5.5-6.7, the flow rate of diverted absorber effluent solution being adjusted automatically via pH measurements of such effluent solution;

(b) introducing into the diverted absorber effluent solution less than a stoichiometric amount of ground limestone, based on the theoretical calcium carbonate required to completely neutralize the bisulfite content of such absorber solution to sulfite, to maintain the pH of the regenerated solution at a higher pH value within the range of 6.2-7.0 and to convert from 20-70% of the solution bisulfite content to sulfite, such limestone addition being controlled via feed forward flow measurements of the diverted absorber effluent solution and trimmed via feedback pH measurements of the limestone-treated solution; and

(c) compensating for process losses of sodium values by adding soda ash or sodium hydroxide at a rate sufficient to maintain the system solution active sodium content at a value within the range of 0.2-2 M, measured as the sum of the bisulfite molar concentration plus twice the sulfite molar concentration of the absorber effluent solution.