Source: https://patents.google.com/patent/US6537456B2/en
Timestamp: 2018-10-22 00:25:37
Document Index: 796731419

Matched Legal Cases: ['Application No. 02235899', 'Application No. 02235899', 'Application No. 61138486', 'Application No. 61138486', 'Application No. 6117235', 'Application No. 6117235']

US6537456B2 - Method and apparatus for high efficiency reverse osmosis operation - Google Patents
Method and apparatus for high efficiency reverse osmosis operation Download PDF
US6537456B2
US6537456B2 US09242249 US24224999A US6537456B2 US 6537456 B2 US6537456 B2 US 6537456B2 US 09242249 US09242249 US 09242249 US 24224999 A US24224999 A US 24224999A US 6537456 B2 US6537456 B2 US 6537456B2
US09242249
US20020125191A1 (en )
LSI=pHreject−pHs
where pHs=the pH at saturation of CaCO3 (reject)
Regeneration of the resin is accomplished by use of conveniently available and cost effective acid. It is well known by those in the art that regeneration of WAC ion-exchange resins may proceed quite efficiently, at near stoichiometric levels (generally, not more than about one hundred and twenty percent (120%) of ideal levels). Preferably, hydrochloric acid may be used, since in such cases highly soluble calcium chloride would be produced, and the regeneration process would not pose the potential danger of formation of insoluble sulfate precipitates, such as calcium sulfate, even with high strength acids. However, by use of a staged regeneration procedures, i.e., by using a low concentration acid followed by a higher concentration acid, it is possible to reliably utilize other acids, including sulfuric acid (H2SO4), while still avoiding undesirable precipitates on the resin. In this manner, hardness ions are solubilized to form soluble salts, which are eluted from the resin bed and are typically sewered. Use of sulfuric acid is particularly advantageous in semiconductor manufacturing operations, since such plants typically use large quantities of such acid, and waste or spent acid may be advantageously utilized for regeneration of a weak acid cation exchange bed.
Ca(HCO3)2+Ca(OH)2→2 CaCO3↓+2 H2O
Mg(HCO3)2+2Ca(OH)2→Mg(OH)2↓+2 CaCO3+2 H2O
Pilot RO Pilot RO Pilot RO
Raw Feed Reject Permeate Rejection Conventional RO
(ppm) (ppm) (ppm) (%) Rejection (%)
Sodium 29.9 460 0.955 99.73 95-98
Potassium 6.4 18.7 <0.003 99.98+ 90-95
Calcium 34 <0.1 <0.003 —
Magnesium 5.3 <0.1 <0.0001 —
Chloride 12.1 78.1 <0.004 99.99+ 97-98
Nitrate 0.74 9.42 0.003 99.96 90-95
Sulfate 46.1 278.4 <0.001 99.99+ 99.91
Boron 0.083 0.62 0.007 98.51 60-70
(Dissolved) Silica 67 480 0.46 99.87 95-99
TOC 0.64 1.1 <0.003 99.66+ 90-95
pH 8.0 10.8 10.3 — —
RO Permeate 193 955
Post Cation IX 0.431 <0.007
Constituent Conventional RO New Process
Boron Non-detectable Non-detectable
Silica 0.43 ppb 0.35 ppb
TOC 5.9 ppb <3.0 ppb
Rejection Rejection Passage Passage Passage Passage
(%) (%) (%) (%) Factor Reduction
Constituent Conventional HERO Conventional HERO Conv/HERO (%)
Sodium 98 99.73 2 0.27 7.4 87
Potassium 90 99.98 10 0.02 500.0 99
Chloride 98 99.99 2 0.01 200.0 99
Silica 99 99.87 1 0.13 7.7 87
Boron 70 98.51 30 1.49 20.1 95
TOC 95 99.66 5 0.34 14.7 93
Raw Water RO Reject RO Product
Na + K 125 1.350 <1
Ca 7 0 0
Mg 13 0 0
HCO3 85 50 <1
CO3 0 50 <1
NO3 1 10 <1
SO4 30.8 308 <1
Cl 28.2 282 <1
SiO2 50 500 <1
pH 7.1 10.8 10.2
1. Analysis of RO feed is not shown in the table, nor is the hydroxide content of RO reject and RO Product.
2. The chemistry is based on 90 percent RO recovery, while maximum recovery feasible is approximately 96 percent.
3. Except for pH, all constituents are reported as mg/l as CaCO3
Water/Waste Water Savings 244,000 (US $/Yr)
Antisealant Elimination 30,000 (US $/Yr)
Power Savings 17,000 (US $/Yr)
Additional Chemical Costs (40,000) (US $/Yr)
Additional Miscellaneous Costs (20,000) (US $/Yr)
Net Annual Savings 231,000 (US $/Yr)
Conversion (Capital) Cost 200,000 (One Time)
Simple Pay-Back Period 10.4 (Months)
Conventional HERO
Equipment Capital Cost (US $MM) 12 7.8
Operating Cost (US $/1,000 US Gallon) 5.75 <4.00
See Section 5.0 for basis.
regenerations. Absence of carbon dioxide, as well as bicarbonate in the RO permeate (due to a high pH, typically at least 10) , will also increase on-line time before silica/boron leakage exceeds normal threshold values. Reduction of strongly ionized species concentration in the RO permeate is of relatively less significance, since most post-RO ion exchange is ultimately silica or boron limited.
1. A process for treatment of a feedwater stream in membrane separation equipment, said membrane separation equipment comprising at least one unit having a membrane separator, to produce a low solute containing product stream and a high solute containing reject stream, said process comprising:
(iii) at least one molecular species which is sparingly ionized when in neutral or near neutral pH aqueous solution said at least one molecular species comprising one or more of
(1) at least some TOC, or
(2) at least some silica, or
(3) at least some boron;
(b) concentrating said feedwater stream in a first unit of said membrane separation equipment after reducing the tendency of said feedwater to form scale when said feedwater is concentrated to a preselected concentration factor at a selected pH, by effecting, in any order, two or more of the following:
(iii)removing dissolved gas from said feedwater stream, whether initially present or created during said hardness or said alkalinity removal step;
(d) passing the product from step (c) above through said membrane separation equipment, said membrane separation equipment substantially resisting passage of dissolved species therethrough, to concentrate said feedwater to said preselected concentration factor, to produce
(i) a high solute containing reject stream,
(iii) wherein TOC in said product stream is less than five percent (5%) of said at least some TOC in said feedwater.
2. The process as set forth in claim 1, wherein the steps of (a) removing hardness, and (b) removing substantially all alkalinity, associated with hardness, are accomplished in a single unit operation.
(iii) at least one molecular species which is sparingly ionized when in neutral or near neutral pH aqueous solution, said at least one molecular species comprising one or more of
(b) concentrating said feedwater stream in a first unit of said membrane separation equipment after effectively eliminating the tendency of said feedwater to form scale when said feedwater is concentrated to a preselected concentration factor at a selected pH, by effecting, in any order, two or more of the following:
(ii)removing substantially all non-hydroxide alkalinity from said feedwater stream;
(iii) removing dissolved gases, whether initiallly present or created during said hardness or said alkalinity removal step;
(c) raising the pH of the product from step (a) to a selected pH of at least about 8.5 by adding a selected base thereto, to urge said at least one molecular species which is sparingly ionized when in neutral or near neutral pH aqueous solution toward increased ionization;
(d) passing the product from step (c) above through said membrane separation equipment to produce a reject stream and a product stream, said membrane separation equipment substantially resisting passage of dissolved species therethrough, to concentrate said feedwater to said preselected concentration factor, to produce
(ii) a low solute containing permeate product stream, and
8. The process according to claim 1 or claim 7, wherein said membrane separation equipment comprises a reverse osmosis equipment.
US09242249 1996-08-12 1997-08-12 Method and apparatus for high efficiency reverse osmosis operation Expired - Lifetime US6537456B2 (en)
US7718996 true 1996-08-12 1996-08-12
US3668297 true 1997-03-01 1997-03-01
PCT/US1997/014239 WO1998006483A1 (en) 1996-08-12 1997-08-12 Method and apparatus for high efficiency reverse osmosis operation
US09242249 US6537456B2 (en) 1996-08-12 1997-08-12 Method and apparatus for high efficiency reverse osmosis operation
US20020125191A1 true US20020125191A1 (en) 2002-09-12
US6537456B2 true US6537456B2 (en) 2003-03-25
ID=27365077
US09242249 Expired - Lifetime US6537456B2 (en) 1996-08-12 1997-08-12 Method and apparatus for high efficiency reverse osmosis operation
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