HIGH RECOVERY SULFATE REMOVAL PROCESS
A high recovery sulfate removal process comprises treating a feed water stream conditioned with antiscalant from a source with a reverse osmosis membrane system to produce a purified water permeate stream and a reject stream containing the retained or rejected ions and organic matter. The reject stream is further treated to remove dissolved and suspended species. The reject stream flows to a desaturation/clarification process. A preferred process includes a constant stirred tank reactor (CSTR) where co-precipitation agent is added followed by a clarifier. Water recycled from the clarifier overflow is blended with feed water stream. The removed solids are collected as sludge or a slurry and disposed of in a manner consistent with applicable regulations.
1 . A high recovery process for sulfate removal from a water source comprising the steps of;
providing a pretreated sulfate containing water input containing soluble and slightly soluble inorganic compounds and organic matter;
blending said input water in a blending volume with clarified recycle water from a co-precipitated reverse osmosis reject stream to produce a blended input water,
conditioning said blended water with antiscalant;
introducing said conditioned blended water into the high pressure side of a RO membrane system;
pressurizing said conditioned blended feed stream on said high pressure side of said RO membrane system to produce purified water permeate on the low pressure side of said RO membrane system substantially free of inorganic compounds;
removing a reject stream containing concentrated inorganic compounds from the high pressure side of the RO system;
subjecting the reject stream to a co-precipitating process capable of removing a sufficient portion of the inorganic compounds so as to produce a clarified recycle water stream suitable for blending with the pretreated water input and a concentrated solids—water slurry;
removing said slurry to drain or by other suitable waste disposal means; and
recycling said clarified water stream to said blending volume.
2 . The process of claim 1 wherein the input water is blended with the clarified recycle water in a ratio of from about 7 to 3 to a ratio of about 9 to 1.
3 . The process of claim 1 wherein the co-precipitation process comprises flowing the reject stream into a CSTR, adding at least one co-precipitating agent, and after a suitable reaction time in the CSTR, flowing the reacted reject stream to a settling tank where the precipitated ion compounds are separated, collected and removed and clarified water is recycled to the blending volume.
4 . The process of claim 3 wherein the at least one co-precipitating agent is chosen from the group consisting of ferric chloride, ferrous chloride, and ferric sulfate.
5 . The process of claim 3 wherein the at least one co-precipitating agent is ferric chloride.
6 . The process of claim 5 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 400 mg/liter.
7 . The process of claim 5 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 100 mg/liter.
8 . The process of claim 5 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 25 mg/liter.
9 . The process of claim 3 wherein gypsum seed particles are used as co-precipitating agent.
10 . The process of claim 9 wherein gypsum seed particles are added at a rate of about approximately 5 grams to about approximately 50 grams per liter of liquid in the CSTR.
11 . The process of claim 9 wherein gypsum seed particles are obtained from the slurry of the settling tank.
12 . The process of claim 9 wherein gypsum seed particles are reused from about approximately 3 to approximately 6 times.
13 . The process of claim 3 wherein gypsum seed particles and ferric chloride are used as co-precipitating agents.
14 . The process of claim 13 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 400 mg/liter.
15 . The process of claim 13 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 100 mg/liter.
16 . The process of claim 13 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 25 mg/liter.
17 . The process of claim 13 wherein gypsum seed particles are added at a rate of about approximately 5 grams to about approximately 50 grams per liter of liquid in the CSTR.
18 . The process of claim 13 wherein gypsum seed particles are obtained from the slurry of the settling tank.
19 . The process of claim 13 wherein gypsum seed particles are recycled from about approximately 3 to approximately 5 times.
20 . The process of claim 1 wherein molybdenum in the reject stream is reduced to about 0.001 mg/l in the recycle water stream.
21 . A high recovery process for sulfate and TOC removal from a water source comprising the steps of:
providing a pretreated sulfate containing water input containing soluble and slightly soluble inorganic compounds and TOC;
blending said input water in a blending volume with clarified recycle water from a co-precipitated reverse osmosis reject stream to produce a blended input water;
conditioning said blended water with antiscalant;
introducing said conditioned blended water into the high pressure side of a RO membrane system;
pressurizing said conditioned blended feed stream on said high pressure side of said RO membrane system to produce purified water permeate on the low pressure side of said RO membrane system substantially free of inorganic compounds and TOC;
removing a reject stream containing concentrated inorganic compounds and concentrated TOC from the high pressure side of the RO system;
subjecting the reject stream to a co-precipitating process capable of removing a sufficient portion of the inorganic compounds and TOC so as to produce a clarified recycle water stream suitable for blending with the pretreated water input and a concentrated solids—water slurry;
removing the slurry to drain or by other suitable waste disposal means; and
flowing said clarified recycle stream to said blending volume.
22 . The process in claim 21 wherein the input water is blended with the clarified recycle water in a ratio of from about 7 to 3 to a ratio of about 9 to 1.
23 . The process of claim 21 wherein the co-precipitation process comprises flowing the reject stream into a CSTR, adding at least one co-precipitating agent, and after a suitable reaction time in the CSTR, flowing the reacted reject stream to a settling tank where the precipitated ion compounds are separated, collected and removed and clarified water is recycled to the blending volume.
24 . The process of claim 23 wherein the at least one co-precipitating agent is chosen from the group consisting of ferric chloride, ferrous chloride, and ferric sulfate.
25 . The process of claim 23 wherein the at least one co-precipitating agent is ferric chloride.
26 . The process of claim 25 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 400 mg/liter.
27 . The process of claim 25 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 100 mg/liter.
28 . The process of claim 25 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 25 mg/liter.
29 . The process of claim 23 wherein gypsum seed particles are used as co-precipitating agent.
30 . The process of claim 29 wherein gypsum seed particles are added at a rate of about approximately 5 grams to about approximately 50 grams per liter of liquid in the CSTR.
31 . The process of claim 29 wherein gypsum seed particles are obtained from the slurry of the settling tank.
32 . The process of claim 29 wherein gypsum seed particles are reused from about approximately 3 to approximately 6 times.
33 . The process of claim 23 wherein gypsum seed particles and ferric chloride are used as co-precipitating agents.
34 . The process of claim 33 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 400 mg/liter.
35 . The process of claim 33 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 100 mg/liter.
36 . The process of claim 33 wherein ferric chloride is added to the CSTR to attain a concentration of from about 10 mg/L to about 25 mg/liter.
37 . The process of claim 33 wherein gypsum seed particles are added at a rate of about approximately 5 grams to about approximately 50 grams per liter of liquid in the CSTR.
38 . The process of claim 33 wherein gypsum seed particles are obtained from the slurry of the settling tank.
39 . The process of claim 33 wherein gypsum seed particles are recycled from about approximately 3 to approximately 6 times.
40 . The process of claim 23 wherein the clarified recycle water contains about approximately 40% to about approximately 60% of TOC of the reject stream entering the CSTR.
41 . The process of claim 21 wherein molybdenum in the reject stream is reduced to about 0.001 mg/l in the recycle water stream.
42 . The process of claim 1 wherein the RO membrane system comprises a reverse osmosis membrane module comprising one of seawater membranes, brackish water membranes or nanofiltration membranes.
43 . The process of claim 21 wherein the RO membrane system comprises a reverse osmosis membrane module comprising one of seawater membranes, brackish water membranes or nanofiltration membranes.