WO2009020517A1 - Ammonia removal apparatus and method - Google Patents

Ammonia removal apparatus and method Download PDF

Info

Publication number
WO2009020517A1
WO2009020517A1 PCT/US2008/008812 US2008008812W WO2009020517A1 WO 2009020517 A1 WO2009020517 A1 WO 2009020517A1 US 2008008812 W US2008008812 W US 2008008812W WO 2009020517 A1 WO2009020517 A1 WO 2009020517A1
Authority
WO
WIPO (PCT)
Prior art keywords
ions
substantial portion
permeate
wastewaters
ammonium
Prior art date
Application number
PCT/US2008/008812
Other languages
French (fr)
Inventor
Frank S. Craft, Sr.
Original Assignee
Basin Water, Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Basin Water, Inc. filed Critical Basin Water, Inc.
Publication of WO2009020517A1 publication Critical patent/WO2009020517A1/en
Priority to US15/215,994 priority Critical patent/US10176324B2/en

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/06—Specific process operations in the permeate stream
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities

Definitions

  • the present invention relates, to an apparatus and method for removing ammonia from wastewaters, and in particular, to removing ammonia from wastewaters associated with mining and other industrial activities.
  • Ammonia may be removed from mining and other industrial wastewaters using stripping tower.
  • the pH of the wastewater stream is raised to convert to convert NH 3 in the wastewater to NH 4 OH.
  • the water is typically neutralized by acid addition.
  • Conventional ammonia stripping also often requires that the water temperature be elevated in order to reduce the effluent ammonia to the required specification.
  • the present invention is an apparatus and method for removing ammonia from mining and other industrial wastewaters comprising (1 ) a membrane separation system with molecular weight cutoff above around 200 (nanofiltration) to reject most of divalent ions but pass most of the ammonium and other monovalent ions with the permeate (filtrate), (2) a water softening system (cation exchange resin in sodium form regenerated with salt brine), (3) one or more strong acid cation NH 3 removal column(s), (4) an alkaline (5-10% NaOH or other alkaline solution) storage tank for regeneration of the NH 3 removal column(s), and (5) a stripping tower for ammonia (NH 4 OH) removal.
  • a membrane separation system with molecular weight cutoff above around 200 (nanofiltration) to reject most of divalent ions but pass most of the ammonium and other monovalent ions with the permeate (filtrate)
  • a water softening system cation exchange resin in sodium form regenerated with salt brine
  • the membrane system rejects divalent ions well, such as hardness, but does not reject NH 3 well.
  • the softener adsorbs most of the divalent ions that the membrane passes, but the NH 3 passes through the softener.
  • the NH 3 loads well on the NH 3 removal column because the divalent ions have been mostly eliminated and will not impede NH 3 loading.
  • sodium which would be exchanged for divalent ions during water softening
  • Sodium also impedes NH 3 loading on the cation resin in the NH 3 columns. If hardness (Ca + Mg) plus sodium is reasonably low (less than approximately 500), the membrane system is not necessary.
  • the present invention reuses the alkaline regenerant solution after the ammonia has been stripped from it with only about 5% loss of regenerant per regeneration cycle.
  • the alkaline regenerant solution of the present invention is maintained at a pH near 14 for the most expedient conversion of NH 3 to NH 4 OH at relatively low temperature.
  • Fig. l is a block diagram of an embodiment of the present invention.
  • the present invention is an apparatus and method for removing ammonia from mining and other industrial wastewaters.
  • the wastewater 11 is pumped by pump 12 to membrane separation system 10.
  • Membrane separation system 10 is preferably a nanofiltration system with molecular weight cutoff above around 200.
  • Most of the divalent ions in the wastewater 11 are rejected in reject line 13 but most of the ammonium and other monovalent ions are passed in permeate line 14.
  • the permeate 14 is fed to water softening system 20.
  • Water softening system 20 is preferably a cation exchange resin in sodium form.
  • the resin is regenerated with salt brine 15.
  • the effluent 21 from water softening system 20 is passed to a strong acid cation NH 3 removal column 30.
  • the NH 3 removal column 30 may actually comprise one or more columns.
  • the removal column 30 is regenerated with an alkaline solution stored in one or more storage tanks 40, 50.
  • the alkaline solution is preferably 5-10% NaOH or other alkaline solution.
  • the alkaline solution is maintained at a pH near 14 for the most expedient conversion of NH 3 to NH 4 OH at relatively low temperature.
  • the alkaline solution is stripped of ammonium hydroxide in stripping tower 61 using air blown by blower 60.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Nanotechnology (AREA)
  • Physical Water Treatments (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

An apparatus and method for removing ammonia from mining and other industrial wastewaters having a nanofiltration membrane separation system (10) to reject most divalent ions but pass most ammonium and other monovalent ions with the permeate (14) to a water softening system (20) with the effluent (21 ) to one or more strong acid cation NH3 removal column(s) (30). Alkaline storage tank(s) (40, 50) provide for the regeneration of the NH3 removal column(s) (30). A stripping tower (61 ) is provided for ammonia (NH4OH) removal.

Description

Description Ammonia Removal Apparatus And Method
Technical Field
The present invention relates, to an apparatus and method for removing ammonia from wastewaters, and in particular, to removing ammonia from wastewaters associated with mining and other industrial activities.
Background Art
Ammonia may be removed from mining and other industrial wastewaters using stripping tower. The pH of the wastewater stream is raised to convert to convert NH3 in the wastewater to NH4OH. After stripping, the water is typically neutralized by acid addition. Conventional ammonia stripping also often requires that the water temperature be elevated in order to reduce the effluent ammonia to the required specification.
Disclosure of Invention
The present invention is an apparatus and method for removing ammonia from mining and other industrial wastewaters comprising (1 ) a membrane separation system with molecular weight cutoff above around 200 (nanofiltration) to reject most of divalent ions but pass most of the ammonium and other monovalent ions with the permeate (filtrate), (2) a water softening system (cation exchange resin in sodium form regenerated with salt brine), (3) one or more strong acid cation NH3 removal column(s), (4) an alkaline (5-10% NaOH or other alkaline solution) storage tank for regeneration of the NH3 removal column(s), and (5) a stripping tower for ammonia (NH4OH) removal.
The membrane system rejects divalent ions well, such as hardness, but does not reject NH3 well. The softener adsorbs most of the divalent ions that the membrane passes, but the NH3 passes through the softener. The NH3 loads well on the NH3 removal column because the divalent ions have been mostly eliminated and will not impede NH3 loading. Also, because of the use of nanofiltration for the bulk of the divalent ion removal, sodium (which would be exchanged for divalent ions during water softening) is minimized. Sodium also impedes NH3 loading on the cation resin in the NH3 columns. If hardness (Ca + Mg) plus sodium is reasonably low (less than approximately 500), the membrane system is not necessary.
Conventional ammonia strippers treat the water stream, requiring a large stripping tower. The present invention system only strips the alkaline regenerant solution from the NH3 removal media, which is roughly 1% of the volume of the treated water, requiring a much smaller stripper, which operates only about 5% of the time that the water is being treated.
It is necessary to raise the pH of the stream to approximately 11.5 to convert NH3 to NH4OH with conventional ammonia strippers. After stripping, the water is typically neutralized by acid addition. Therefore, chemical feed systems and pH controls are necessary as well as the chemical costs associated with the continuous pH adjustments. The present invention reuses the alkaline regenerant solution after the ammonia has been stripped from it with only about 5% loss of regenerant per regeneration cycle.
Conventional ammonia stripping often requires that the water temperature be elevated, with inherent energy cost, in order to reduce the effluent ammonia to the required specification. The alkaline regenerant solution of the present invention is maintained at a pH near 14 for the most expedient conversion of NH3 to NH4OH at relatively low temperature.
Calcium and other divalent ions which contribute to scaling and impede ammonia stripping are diverted around the NH3 removal column so that the scaling potential of the stripping tower is greatly minimized or eliminated and stripping efficiency is enhanced.
These and other features, objects and advantages of the present invention will become better understood from a consideration of the following detailed description of the preferred embodiments and appended claims in conjunction with the drawings as described following:
Brief Description Of Drawings
Fig. l is a block diagram of an embodiment of the present invention.
Best Mode for Carrying Out the Invention With reference to Fig. 1 , the preferred embodiment of the present invention may be described as follows.
The present invention is an apparatus and method for removing ammonia from mining and other industrial wastewaters. The wastewater 11 is pumped by pump 12 to membrane separation system 10. Membrane separation system 10 is preferably a nanofiltration system with molecular weight cutoff above around 200. Most of the divalent ions in the wastewater 11 are rejected in reject line 13 but most of the ammonium and other monovalent ions are passed in permeate line 14. The permeate 14 is fed to water softening system 20. Water softening system 20 is preferably a cation exchange resin in sodium form. The resin is regenerated with salt brine 15. The effluent 21 from water softening system 20 is passed to a strong acid cation NH3 removal column 30. If hardness (Ca + Mg) plus sodium in the wastewater is reasonably low (less than approximately 500), the membrane system 10 is not necessary. The NH3 removal column 30 may actually comprise one or more columns. The removal column 30 is regenerated with an alkaline solution stored in one or more storage tanks 40, 50. The alkaline solution is preferably 5-10% NaOH or other alkaline solution. The alkaline solution is maintained at a pH near 14 for the most expedient conversion of NH3 to NH4OH at relatively low temperature. The alkaline solution is stripped of ammonium hydroxide in stripping tower 61 using air blown by blower 60.
The present invention has been described with reference to certain preferred and alternative embodiments that are intended to be exemplary only and not limiting to the full scope of the present invention as set forth in the appended claims.

Claims

Claims
1. An apparatus for removing ammonia from wastewaters containing divalent ions and monovalent ions including ammonium ions, comprising: a nanofiltration membrane separation system for passing in a permeate a substantial portion of the monovalent ions including ammonium ions in the wastewaters while rejecting a substantial portion of the divalent ions in the wastewaters; a water softening system for receiving the permeate from the membrane separation system and absorbing a substantial portion of divalent ions remaining in the permeate; a strong acid cation ion exchange column for receiving the permeate from the water softening system and for removing a substantial portion of the ammonium ions in the permeate; a storage tank containing an alkaline solution for regeneration of the strong acid cation ion exchange column removal column and producing an ammonium hydroxide brine; and a stripping tower for stripping ammonium hydroxide from the brine.
2. An apparatus for removing ammonia from wastewaters containing divalent ions and monovalent ions including ammonium ions, comprising: a water softening system for passing a substantial portion of the monovalent ions including ammonium ions in the wastewater while absorbing a substantial portion of divalent ions in the wastewaters; a strong acid cation ion exchange column for receiving the effluent from the water softening system and for removing a substantial portion of the ammonium ions in the effluent; a storage tank containing an alkaline solution for regeneration of the strong acid cation ion exchange column removal column and producing an ammonium hydroxide brine; and a stripping tower for stripping ammonium hydroxide from the brine.
PCT/US2008/008812 2007-08-03 2008-07-18 Ammonia removal apparatus and method WO2009020517A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US15/215,994 US10176324B2 (en) 2007-12-21 2016-07-21 System, method and computer program product for protecting software via continuous anti-tampering and obfuscation transforms

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US96334607P 2007-08-03 2007-08-03
US60/963,346 2007-08-03

Publications (1)

Publication Number Publication Date
WO2009020517A1 true WO2009020517A1 (en) 2009-02-12

Family

ID=40341568

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2008/008812 WO2009020517A1 (en) 2007-08-03 2008-07-18 Ammonia removal apparatus and method

Country Status (1)

Country Link
WO (1) WO2009020517A1 (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2447218A1 (en) * 2010-10-29 2012-05-02 Siemens Aktiengesellschaft Method for processing mine waters

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3970467A (en) * 1973-05-09 1976-07-20 Anheuser-Busch, Incorporated Method for making corrugating adhesives with flexographic press waste water
US7132052B2 (en) * 2003-12-11 2006-11-07 General Electric Company System for the purification and reuse of spent brine in a water softener
US20070039893A1 (en) * 2005-08-11 2007-02-22 Kemp Philip M Ammonium/ammonia removal from a stream

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3970467A (en) * 1973-05-09 1976-07-20 Anheuser-Busch, Incorporated Method for making corrugating adhesives with flexographic press waste water
US7132052B2 (en) * 2003-12-11 2006-11-07 General Electric Company System for the purification and reuse of spent brine in a water softener
US20070039893A1 (en) * 2005-08-11 2007-02-22 Kemp Philip M Ammonium/ammonia removal from a stream

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2447218A1 (en) * 2010-10-29 2012-05-02 Siemens Aktiengesellschaft Method for processing mine waters
WO2012055776A1 (en) * 2010-10-29 2012-05-03 Siemens Aktiengesellschaft Method for reprocessing mine waters

Similar Documents

Publication Publication Date Title
KR101563169B1 (en) Pure water production apparatus and pure water production method
KR102047155B1 (en) Method and device for treating boron-containing water
CN105084587A (en) Treatment method and equipment of high-salt waste water
CN110603339B (en) Method for softening lithium salt water by using nanofiltration
US20130126353A1 (en) Electrodialysis with ion exchange and bi-polar electrodialysis
CA2659451A1 (en) Desalination methods and systems that include carbonate compound precipitation
EA011830B1 (en) Method (embodiments) for liquid treatment by reverse osmosis under acidic conditions
CN101939262A (en) Process and apparatus for producing ultrapure water, and method and apparatus for cleaning electronic component members
CN113105025B (en) Combined treatment method for regenerating high-concentrated-salt wastewater by sodium ion exchanger
CN202744400U (en) System for recycling electroplating wastewater and heavy metal ions
JP4599803B2 (en) Demineralized water production equipment
US6080315A (en) Process for the partial desalination of water
CN202808519U (en) Purified water reverse osmosis system
CN102897947A (en) Reverse osmosis (RO) desalting treatment method and treatment system with ultrahigh water recovery rate for waste water containing high sulfate radicals
CN211226645U (en) Coupling flue gas purification handles contains salt effluent disposal system
CN103508596B (en) Treatment system and recycling method of ammonium adipate cleansing wastewater
JP2000070933A (en) Production of pure water
WO2009020517A1 (en) Ammonia removal apparatus and method
JP3417052B2 (en) Ultrapure water production method
WO2010019116A1 (en) Ammonia removal apparatus and method
JP2001191080A (en) Electric deionizing device and electric deionizing treatment method using the same
JP5951605B2 (en) Method and system for treating water
US11890577B2 (en) Reverse osmosis or nanofiltration process for cleaning water
JP2019118891A (en) Pure water producing apparatus and pure water producing method
CA2893345C (en) Hybrid electrochemical softening desalination system and method

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 08794583

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 08794583

Country of ref document: EP

Kind code of ref document: A1