Method of inhibiting corrosion in industrial hot water systems by monitoring and controlling oxidant/reductant feed through a nonlinear control algorithm
This invention provides a method of preventing corrosion in industrial water systems. The method includes maintaining a real-time oxidation-reduction potential at a set point, wherein the system is at operating temperature and pressure. A nonlinear equation is derived based upon theoretically derived or empirically collected data. The equation is then used to determine an inflow of active chemical species to the water system.
1. A method of preventing corrosion in an industrial water system by maintaining a real-time oxidation-reduction potential, (“ORP”) at an ORP set point, wherein the system is at operating temperature and pressure, the method comprising:
(a) determining the ORP set point;
(b) determining the real-time ORP, wherein the real-time ORP is determined at operating temperature and pressure of the industrial water system and is based on at least one additional factor other than hydrazine concentration in said system;
(e) determining concentrations of one or more active chemical species that influence the real-time ORP;
(d) determining a flow rate;
(e) creating a nonlinear control equation having as an input variable(s) one or more of the determined values from steps (a) to (d); and
(f) calculating an output of the nonlinear control equation thereby determining an inflow of the active chemical species to the industrial water system to maintain the ORP set point.
2. The method of claim 1 , wherein the industrial water system is a hot water system.
3. The method of claim 1 , wherein the ORP set point is a range.
4. The method of claim 1 , wherein the ORP set point is based on a theoretical calculation.
5. The method of claim 1 , including determining the real-time ORP without directly measuring the real-time ORP.
6. The method of claim 1 , wherein the real-time ORP is based on a theoretical calculation.
7. The method of claim 1 , including determining the real-time ORP at a point of control without directly measuring the real-time ORP at the point of control.
8. The method of claim 1 , including determining the real-time ORP by directly measuring the real-time ORP at any point in the industrial water system.
9. The method of claim 1 , including determining the real-time ORP at a point in the industrial water system other than a point of control and calculating the real-time ORP at the point of control based upon the real-time ORP at said other point.
10. The method of claim 1 , including determining the real-time ORP by measuring ORP at room temperature and calculating the real-time ORP.
11. The method of claim 1 , including measuring concentrations of the active chemical species at a point of control.
12. The method of claim 1 , including determining concentrations of the active chemical species based on theoretical calculations.
13. The method of claim 1 , including measuring concentrations of the active chemical species at a point other than a point of control and calculating the concentrations of said species at the point of control based upon said measurements at said other point.
14. The method of claim 1 , wherein at least one of the active chemical species is selected from the group consisting of: oxidants, reductants, and combinations thereof.
15. The method of claim 1 , wherein the flow rate includes feedwater flow and/or steam flow and/or boiler blowdown flow and/or a measurement or calculation for steam losses.
16. The method of claim 1 , wherein the flow rate includes feedwater flow from one or more sources and/or steam flow at one or more points.
17. The method of claim 1 , wherein determining the flow rate includes directly measuring the flow rate, using a flow rate indicator, and/or calculating the flow rate.
18. The method of claim 17 , wherein the input variable(s) includes the flow rate indicator and the output includes a signal operable to control the inflow of the active chemical species.
19. The method of claim 1 , wherein the inflow of at least one of the active chemical species includes using a chemical dose-pump.
20. The method of claim 1 , including iterating steps (b) to (d) a plurality of times prior to creating the nonlinear control equation.
21. The method of claim 20 , wherein each iteration involves a different concentration of the active chemical species and/or a different flow rate.
22. The method of claim 20 , including obtaining a first dataset with a first iteration and a second dataset with a second iteration, the first dataset including measured and/or theoretical data and the second dataset including measured and/or theoretical data.
23. The method of claim 22 , including a plurality of iterations each with a corresponding dataset.
24. The method of claim 1 , which is operable at a plurality of points in the industrial water system.
25. The method of claim 1 , which is operable through a data network.