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WO2009091959A2 - Systèmes et procédés de traitement de l'urée pour réduire la charge de sorbant - Google Patents

Systèmes et procédés de traitement de l'urée pour réduire la charge de sorbant Download PDF

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Publication number
WO2009091959A2
WO2009091959A2 PCT/US2009/031224 US2009031224W WO2009091959A2 WO 2009091959 A2 WO2009091959 A2 WO 2009091959A2 US 2009031224 W US2009031224 W US 2009031224W WO 2009091959 A2 WO2009091959 A2 WO 2009091959A2
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Prior art keywords
reactor
ammonia
gaseous ammonia
stream
ammonium
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Ceased
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PCT/US2009/031224
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English (en)
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WO2009091959A3 (fr
WO2009091959A8 (fr
Inventor
Russell Thomas Joseph
David Mishelevich
Lina Gabrielaityte
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Xcorporeal Inc
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Xcorporeal Inc
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Publication of WO2009091959A2 publication Critical patent/WO2009091959A2/fr
Publication of WO2009091959A3 publication Critical patent/WO2009091959A3/fr
Anticipated expiration legal-status Critical
Publication of WO2009091959A8 publication Critical patent/WO2009091959A8/fr
Ceased legal-status Critical Current

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Classifications

    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61M—DEVICES FOR INTRODUCING MEDIA INTO, OR ONTO, THE BODY; DEVICES FOR TRANSDUCING BODY MEDIA OR FOR TAKING MEDIA FROM THE BODY; DEVICES FOR PRODUCING OR ENDING SLEEP OR STUPOR
    • A61M1/00—Suction or pumping devices for medical purposes; Devices for carrying-off, for treatment of, or for carrying-over, body-liquids; Drainage systems
    • A61M1/14—Dialysis systems; Artificial kidneys; Blood oxygenators ; Reciprocating systems for treatment of body fluids, e.g. single needle systems for hemofiltration or pheresis
    • A61M1/16—Dialysis systems; Artificial kidneys; Blood oxygenators ; Reciprocating systems for treatment of body fluids, e.g. single needle systems for hemofiltration or pheresis with membranes
    • A61M1/1694—Dialysis systems; Artificial kidneys; Blood oxygenators ; Reciprocating systems for treatment of body fluids, e.g. single needle systems for hemofiltration or pheresis with membranes with recirculating dialysing liquid
    • A61M1/1696—Dialysis systems; Artificial kidneys; Blood oxygenators ; Reciprocating systems for treatment of body fluids, e.g. single needle systems for hemofiltration or pheresis with membranes with recirculating dialysing liquid with dialysate regeneration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/0203—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of metals not provided for in B01J20/04
    • B01J20/0211—Compounds of Ti, Zr, Hf
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/0203—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of metals not provided for in B01J20/04
    • B01J20/0274—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of metals not provided for in B01J20/04 characterised by the type of anion
    • B01J20/0292—Phosphates of compounds other than those provided for in B01J20/048
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/06—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group B01J20/04
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
    • B01J20/28014—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their form
    • B01J20/28052—Several layers of identical or different sorbents stacked in a housing, e.g. in a column
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
    • B01J39/08—Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
    • B01J39/12—Compounds containing phosphorus
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2220/00—Aspects relating to sorbent materials
    • B01J2220/50—Aspects relating to the use of sorbent or filter aid materials
    • B01J2220/62—In a cartridge

Definitions

  • the present invention generally relates to the field of dialysis, and more specifically to systems and methods of urea processing in spent dialysate to effectively reduce the amount of sorbent used in cleansing the dialysate or to eliminate the need for using sorbent entirely.
  • a dialysis system typically includes a system for circulating blood, a system for circulating dialysate fluid, and a semi -permeable membrane.
  • Urea and other blood components, but not blood cells, travel across the membrane from the blood side to the dialysate side as the blood and dialysate fluid both flow past the membrane.
  • dialysate fluid is recycled, urea and other blood waste compounds must be removed before the fluid is again passed by the membrane.
  • Dialysate regeneration systems comprising closed loop multi-pass sorbent-based hemodialyzers typically use a plurality of sorbents in the form of cartridges to cleanse spent dialysate.
  • One way to accomplish the removal of urea in the spent dialysate is to expose the urea to urease enzyme, which breaks the urea molecules down into ammonium ions and carbonate.
  • a sorbent type cartridge is provided in the dialysis system where urea is decomposed with the help of urease enzyme.
  • the ammonium ions or ammonium (NH4+) which are toxic and should not be exposed to the membrane, can be adsorbed, for example, by zirconium phosphate (ZrP).
  • zirconium phosphate acts as an ion exchanger and exchanges ammonium ions for sodium ions.
  • a ZrP layer is provided in the sorbent cartridge.
  • the ZrP layer can only adsorb a specific quantity of ammonia while the urease enzyme can produce ammonia as long as urea is present in the blood stream. Therefore it is possible for a patient with a high urea load to produce more ammonia than the ZrP layer can adsorb. When this happens, toxic ammonia enters the dialysate and can get into the patient, which can be very harmful to the patient. Ammonia exiting the sorbent cartridge, when the cartridge capacity to adsorb more ammonia is reached, is known as "Ammonia Breakthrough".
  • ammonium ions present in spent dialysate are converted into gaseous ammonia by raising the pH of the spent dialysate solution in a first reactor. Gaseous ammonia diffuses through a semi-permeable hydrophobic membrane at the outlet of the first reactor and into a second reactor via a gas channel. Ammonia is then captured and removed in the second reactor.
  • ammonia is disposed of in the second reactor by electro lyzing the ammonia gas in the presence of H 2 O and KOH to convert ammonia into nitrogen and hydrogen.
  • the hydrogen produced in this reaction is channeled to a hydrogen fuel cell.
  • ammonia is disposed off in the second reactor by first converting gaseous ammonia into an ammonium compound by mixing it with an acidic stream and then using industrial zeolite to capture the ammonium.
  • ammonia is removed by first converting gaseous ammonia into an ammonium compound by mixing with an acidic stream and then converting said ammonium compound into struvite mineral deposit by allowing it to react with magnesium salts and phosphorous.
  • the second reactor comprises a bio-reactor, and ammonia is removed by using a microorganism for oxidation of ammonia to nitrite.
  • the microorganism is nitrosomonas europea.
  • the second reactor comprises a three-sided horseshoe housing filled with an aqueous fluid devoid of ammonium ions. Ammonia is removed by first converting gaseous ammonia into an ammonium compound by mixing with an acidic stream and then extracting ammonium into the aqueous fluid by diffusion.
  • the present invention comprises a method of removing ammonia from a stream of used dialysate solution in a dialysis system, the method comprising a) passing the stream of used dialysate solution having a pH through a first reactor, b) raising the pH of the stream of used dialysate solution in said first reactor to a level sufficient to substantially convert ammonium ions in said stream to gaseous ammonia, c) releasing the gaseous ammonia from said stream by allowing it to diffuse through a semi-permeable hydrophobic membrane at the outlet of said first reactor, d) receiving the gaseous ammonia through a gas channel into a second reactor, and e) capturing and removing the gaseous ammonia in said second reactor.
  • the step of capturing and removing the gaseous ammonia in said second reactor further comprises converting the ammonia gas into nitrogen and hydrogen by electrolysis in the presence of H 2 O and KOH.
  • the hydrogen released in ammonia electrolysis is channeled to a hydrogen fuel cell.
  • the step of capturing and removing the gaseous ammonia in said second reactor further comprises the steps of converting gaseous ammonia into an ammonium compound by mixing it with an acidic stream and exposing it to industrial zeolite.
  • the step of capturing and removing the gaseous ammonia in said second reactor further comprises the steps of converting gaseous ammonia into an ammonium compound by mixing with an acidic stream and converting said ammonium compound into struvite by reacting it with magnesium salts and phosphorous.
  • the second reactor is a bio-reactor and the step of capturing and removing the gaseous ammonia comprises using a microorganism, such as nitrosomonas europea, for oxidizing ammonia to nitrite.
  • the second reactor comprises a three-sided, e.g.
  • horseshoe, housing and the step of capturing and removing the gaseous ammonia further comprises the steps of converting gaseous ammonia into an ammonium compound by mixing it with an acidic stream, filling said horseshoe housing with an aqueous fluid devoid of ammonium ions, and extracting ammonium into said aqueous fluid by diffusion.
  • the release of gaseous ammonia from the dialysate stream is assisted by a vacuum or suction device in the gas channel.
  • the first reactor and said second reactor are disposable.
  • the present invention is directed to a system for removing ammonia from a stream of used dialysate solution during dialysis, the system comprising a) a first reactor through which the stream of used dialysate solution is passed and its pH raised such that ammonium ions in said stream are substantially converted to gaseous ammonia, wherein said gaseous ammonia is released from said stream by diffusion through a semi-permeable hydrophobic membrane at the outlet of said first reactor, and b) a second reactor for receiving the gaseous ammonia from the first reactor via a gas channel, wherein said second reactor captures and removes the gaseous ammonia.
  • the capturing and removing the gaseous ammonia in said second reactor comprises converting the ammonia gas into nitrogen and hydrogen by electrolysis in the presence of H 2 O and KOH.
  • the hydrogen released in ammonia electrolysis is channeled to a hydrogen fuel cell.
  • the capturing and removing the gaseous ammonia in said second reactor further comprises converting gaseous ammonia into an ammonium compound by mixing it with an acidic stream and using industrial zeolite to capture the ammonium.
  • the capturing and removing the gaseous ammonia in said second reactor further comprises converting gaseous ammonia into an ammonium compound by mixing with an acidic stream and converting said ammonium compound into struvite by reacting with magnesium salts and phosphorous.
  • the second reactor is a bio-reactor and capturing and removing the gaseous ammonia comprises using a microorganism for oxidizing ammonia to nitrite.
  • the second reactor comprises a three-sided horseshoe housing and capturing and removing the gaseous ammonia further comprises converting gaseous ammonia into an ammonium compound by mixing it with an acidic stream, filling said horseshoe housing with an aqueous fluid devoid of ammonium ions, and extracting ammonium into said aqueous fluid by diffusion.
  • the system further comprises a vacuum or suction device in the gas channel for assisting the release of gaseous ammonia from the dialysate stream.
  • Figure 1 is a block diagram illustrating an embodiment of the ammonia release and capture system of the present invention
  • Figure 2a is a block diagram illustrating an embodiment of the first ammonia- release reactor of the ammonia release and capture system of the present invention
  • Figure 2b is a graph illustrating the ammonia stripping rate as a function of pH
  • Figure 2c is a table illustrating the ammonia stripping rate as a function of pH
  • Figure 3 is a block diagram illustrating a first embodiment of the second ammonia-capture reactor of the ammonia release and capture system of the present invention
  • Figure 4 is a block diagram illustrating a second embodiment of the second ammonia-capture reactor of the ammonia release and capture system of the present invention
  • Figure 5 is a block diagram illustrating a third embodiment of the second ammonia-capture
  • Dialysate is regenerated for reuse in multi-pass dialysis systems by passing it through a regeneration section comprising a plurality of sorbent cartridges and suitable additives.
  • a typical sorbent cartridge system comprises a urease cartridge, a zirconium phosphate cartridge, a hydrous zirconium oxide cartridge and an activated carbon cartridge.
  • a typical sorbent cartridge system comprises a urease cartridge, a zirconium phosphate cartridge, a hydrous zirconium oxide cartridge and an activated carbon cartridge.
  • sorbents are similar to the sorbents employed by the commercially available REDYTM System.
  • the principle of the sorbent cartridge system is based on hydrolysis of urea to ammonium carbonate by the enzymatic reaction of urease.
  • the ammonia and ammonium ions are then removed by the zirconium phosphate (NaHZrP) in exchange for hydrogen ions and Na + ions.
  • the enzymatic conversion of urea in the urease cartridge causes one mole of urea to be decomposed into two moles of ammonia and one mole of carbon dioxide by way of the following reaction:
  • FIG. 1 shows a block diagram illustration of the present invention where spent dialysate, comprising uremic wastes including urea, is pumped through a plurality of sorbent cartridges for cleansing. As spent dialysate 105 passes through the urease cartridge 110, an enzymatic reaction resulting in hydrolysis of urea causes release of ammonia and ammonium ions apart from other by-products as discussed earlier.
  • the dialysate emanating from the urease cartridge 110 and comprising ammonia, substantially in the form of ammonium ions, is passed through an ammonia release and capture stage 115.
  • the ammonia release and capture stage 115 of the present invention in one embodiment, comprises a first ammonia-release reactor 112 where the ammonium ions in the dialysate are released as ammonia gas, which in turn is made to pass through an ammonia gas channel 113 to a second ammonia-capture reactor 114 where the ammonia gas is captured.
  • the dialysate 120 emanating from the ammonia release and capture stage 115 is substantially stripped of ammonia/ammonium ions.
  • the dialysate 120 with any residual ammonium ions flows onwards through subsequent sorbent cartridges 125 comprising layers of adsorbent materials such as ZrP and ZrO for further cleansing.
  • the first and second reactors, 112, 114, of the ammonia release and capture stage 115 are air-tight canisters that in one embodiment are disposable.
  • the first ammonia-release reactor 112 is a daily disposable canister while the second ammonia-capture reactor 114 is a weekly or monthly disposable canister or an even further long-term durable canister.
  • the first ammonia-release reactor 112 is a daily, weekly, monthly, or an even longer term disposable canister while the second ammonia-capture reactor 114 is a daily, weekly, monthly or an even longer-term disposable canister.
  • Figure 2a shows a block diagram illustrating an embodiment 200 of the first ammonia-release reactor 112 of the ammonia release and capture stage 115 of Figure 1. Turning to Figure 2a, the stream of dialysate 206 emanating from the urease cartridge 210 and comprising ammonium ions is processed in the first ammonia-release reactor 212 for the ammonium ion conversion.
  • the ammonium ion conversion comprises sufficiently increasing the pH of the dialysate stream 206 to convert ammonium in the stream to gaseous ammonia.
  • the dialysate stream 206 in the first reactor 212 is contacted with a weak and/or strong base 211, such as sodium hydroxide (NaOH) or potassium hydroxide (KOH) to raise the pH level above 9.5. That is, it is ensured that there is sufficient alkalinity available to supply the necessary equivalents to maintain a pH above 9.5 as the ammonia dissociates (NH4+ONH3 + H + ) and is stripped.
  • a pH sensor 250 is connected to the first reactor 212 to monitor and maintain its pH level.
  • the ammonia fraction is largely gaseous ammonia and is readily stripped from the dialysate stream 206.
  • the ammonia stripping rate is a function of the pH level as well as the temperature apart from other parameters such as the available surface area for the reaction in the reactor 212.
  • the temperature of the dialysate stream in the first reactor 212 is about 37 degrees C.
  • the reaction is further depicted in graph 230 and table 235, which are described in detail later in the specification, with reference to Figures 2b and 2c.
  • the first reactor 212 has a vent that is sealed with a microporous semi-permeable hydrophobic membrane 240 that allows gaseous ammonia to diffuse through but does not allow the aqueous dialysate stream 206 to pass.
  • Ammonia gas diffusing through the hydrophobic membrane 240 is collected via an ammonia channel 213 for further processing.
  • An ammonia sensor 214 is advantageously connected to the ammonia channel/collection device 213. In one embodiment the ammonia diffusing through the membrane 240 is collected without any vacuum or pressure.
  • a venturi is used, at the ammonia channel 213, such that ammonia gas is withdrawn from the first reactor 212 under vacuum into the suction side of the venturi for onward communication and further processing.
  • the venturi associated with the first reactor 212 provides a nearly full vacuum on the first reactor 212 thus allowing for rapid and nearly complete separation of ammonia gas from the dialysate stream 206.
  • an impeller (not shown) is used in the ammonia channel 213 to suction out ammonia gas from the first reactor 212 through the hydrophobic membrane 240.
  • the aqueous dialysate stream 207 comprising residual ammonia flows through an opening into an auxiliary air-tight canister 245.
  • An acid 244, such as hydrochloric acid (HCl) is injected into the auxiliary canister 245 lowering the pH level of the dialysate stream 207 to about 7. At such lowered pH levels the residual ammonia is converted to ammonium ions that remain in aqueous state dissolved in the dialyate stream 207.
  • First and second pH sensors, 246, 247 are advantageously connected to monitor the pH level of the dialysate stream 207 in the canister 245 and the stream 208 flowing out therefrom.
  • the dialysate 208 with residual ammonium ions flows onwards through subsequent sorbent cartridges 225 such as ZrP, ZrO for further cleansing.
  • graph 230 depicts that beyond a pH level of 8.5 the equilibrium rapidly shifts in the direction of gaseous ammonia (NH 3 ).
  • the graph 230 corresponds to the readings in table 235 shown in Figure 2c.
  • table 235 provides ammonium and ammonia levels at pH levels of 9, 10 and 11 at a dialysate stream temperature of 37 degrees C. It is apparent from table 235 and graph 230, that at pH of 10 and temperature of 37 degrees C the level of ammonia gas is 92.96%. It should be appreciated that the system can regenerate dialysate without requiring the use of a final sorbent stage.
  • the system of the present invention does not employ a residual sorbent stage, thereby eliminating sorbent 125 ( Figure 1) and 225 ( Figure 2).
  • sorbent 125 Figure 1
  • 225 Figure 2
  • all of the embodiments disclosed herein further include a system wherein the use of sorbents, or inclusion of a sorbent-based regeneration phase, is eliminated.
  • each of the disclosed embodiments further include a version wherein the conversion of ammonium to ammonia is facilitated by increasing temperature of the dialysate fluid above 37 degrees Celsius (e.g.,at 42 degrees Celsius there is 94.7% ammonia conversion; at 37 degrees Celsius there is 92.96% ammonia conversion), and then cooling the dialysate down again to 37 degrees Celsius prior to the dialysate fluid passing through the dialyzer.
  • Figure 3 shows a block diagram illustrating a first embodiment 300 of the second ammonia-capture reactor 114 of the ammonia release and capture stage 115 of Figure 1.
  • the ammonia gas is received in a first compartment 302 of the reactor 314 through an inlet that is sealed with a hydrophobic membrane 340.
  • the hydrophobic membrane 340 allows gases to diffuse through but prevents aqueous fluids from passing.
  • Ammonia gas is converted by mixing the gas with an acidic stream 315, such as sulfuric acid, that is injected into the compartment 302.
  • the pH of the contents of the first compartment 302 is maintained in the range from 6 to 7.
  • the ammonia gas reacts with the acid 315 to form an ammonium compound.
  • the acidic stream 315 becomes saturated with NH 4 , a solution of the ammonium compound is obtained.
  • an ammonium sulfate solution is obtained by the reaction of ammonia gas with the acid.
  • the obtained solution is pumped using a peristaltic pump, through a tube, 320, into a second compartment 304, which comprises a pack or column of an industrial zeolite compound.
  • FIG. 4 shows a block diagram illustrating a second embodiment 400 of the second ammonia-capture reactor 114 of the ammonia release and capture stage 115 of Figure 1.
  • the ammonia gas is received in a first compartment 402 of the reactor 414 through an inlet that is sealed with a hydrophobic membrane 440 (that allows gases to diffuse through but prevents aqueous fluids from passing) for conversion to NH 4 .
  • Ammonia gas is converted by mixing the gas with an acidic stream 415, such as sulfuric acid, that is injected into the compartment 402 through an inlet.
  • an acidic stream 415 such as sulfuric acid
  • the ammonia gas reacts with the acid 415 to form an ammonium compound.
  • the ammonium compound solution (such as ammonium sulfate solution in case the acidic stream is that of sulfuric acid) is pumped by a peristaltic pump, through a tube 420, into a compartment 404, where it is converted to an insoluble mineral deposit such as struvite.
  • acid 411 such as sulfuric acid
  • Mg ++ ions 412 in the form of magnesium salts such as MgCl 2 , MgO
  • phosphorus 413 are injected into the compartment 404 for mixing with the pumped solution.
  • Ammonium and magnesium combine with phosphorous in a 1 :1 :1 molar ratio to form an insoluble mineral struvite as follows: NH 4 + + Mg 2+ + PO 4 3" + 6H 2 O -> NH 4 MgPO 4 .6H 2 O (struvite)
  • the struvite gets deposited on substrates 420 in the compartment 404 in the form of large crystals and may be removed periodically. As the solution percolates through the compartment 404 the ammonium ions are captured and precipitated out in the form of struvite, while the resultant solution, substantially stripped of ammonium ions and comprising any residual ammonium, is circulated back to the first compartment through tube 405.
  • FIG. 5 shows a block diagram illustrating a third embodiment 500 of the second ammonia-capture reactor 114 of the ammonia release and capture stage 115 of Figure 1.
  • the ammonia gas diffusing out from the first ammonia-release reactor or suctioned by a venturi, as described with reference to Figure 2a, is passed through the second ammonia-capture reactor 514 for ammonia removal/capture via ammonia channel 510.
  • the ammonia gas is received in the reactor 514 through an inlet that is sealed with a hydrophobic membrane 540 (that allows gases to diffuse through but prevents aqueous fluids from passing).
  • the reactor 514 is a bio-reactor comprising suitable micro- organisms that feed on ammonia to organically capture and convert ammonia.
  • the micro-organism is nitrosomonas europeae.
  • nitrosomonas europea is a Gram-negative obligate chemolithoautotroph that can derive all its energy and reductant for growth from the oxidation of ammonia to nitrite.
  • This microbe prefers an optimum pH of 6.0 to 9.0, fairly neutral conditions, has an aerobic metabolism and prefers a temperature range of 20 to 30 degrees Celsius.
  • Figure 6 shows a block diagram illustrating a fourth embodiment 600 of the second ammonia-capture reactor 114 of the ammonia release and capture stage 115 of Figure 1.
  • the ammonia gas is received in the reactor 614 through an inlet, at a first side 601 that is sealed with a hydrophobic membrane, that allows gases to diffuse through but prevents aqueous fluids to pass, for conversion to NH 4 .
  • Ammonia gas is converted by mixing the gas with an acidic stream, such as sulfuric acid, that is injected into the reactor 614.
  • the pH of the contents of the reactor 614 is maintained in the range from 6 to 7. At such reduced pH levels, the ammonia gas reacts with the acid to form an ammonium compound.
  • the other three sides, 602, 603 and 604, of the reactor 614 are partially or completely made of a semi- permeable membrane that allows solutes and other compounds in aqueous solutions to diffuse through due to osmotic pressure differentials.
  • a module 620 conformed as a horseshoe, or U-shaped, housing is capable of being removably slipped onto the reactor 614 such that the horseshoe housing covers the three sides, 602, 603 and 604, of the reactor 614 comprising the semi-permeable membranes.
  • the housing in one embodiment, comprises an inlet from where an aqueous fluid, such as water, devoid of ammonium ions is introduced in the horseshoe housing to completely fill it.
  • FIG. 7 shows a block diagram illustrating a fifth embodiment 700 of the second ammonia-capture reactor 114 of the ammonia release and capture stage 115 of Figure 1.
  • Ammonia gas diffusing out from the first ammonia-release reactor or suctioned by a venturi, as described with reference to Figure 2a, is passed through the second ammonia- capture reactor 714, via ammonia channel 710, for electrolysis.
  • the ammonia gas is received in the reactor 714 through an inlet 710, which is sealed with a hydrophobic membrane 740 (that allows gases to diffuse through but prevents aqueous fluids from passing).
  • the reactor 714 comprises an anode 716 and cathode 717 at two opposing sides. First and second exhausts 711, 712 are provided on a second side of reactor 714 such that they are proximal to the anode 716 and cathode 717 respectively.
  • the reactor 714 comprises an aqueous base, such as potassium hydroxide (KOH), as an electrolyte such that electrolysis of ammonia occurs in the presence OfH 2 O and KOH as follows:
  • the resulting N 2 at the anode is vented out through first exhaust 711 while the H 2 is let out via second exhaust 712.
  • the second exhaust 712 venting H 2 is optionally connected to a Hydrogen Fuel Cell 720 that uses the vented hydrogen as fuel.

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Abstract

La présente invention concerne de nouveaux procédés d'extraction et d'élimination d'ammoniac d'un dialysat utilisé dans un système de dialyse. Les ions d'ammonium présents dans le dialysat utilisé sont convertis en ammoniac gazeux par augmentation du pH de la solution du dialysat utilisé dans un premier réacteur. L'ammoniac gazeux est diffusé à travers une membrane hydrophobe semi-perméable dans un second réacteur via un canal gazeux. Le second réacteur convertit l'ammoniac gazeux en composé d'ammonium facile à éliminer.
PCT/US2009/031224 2008-01-18 2009-01-16 Systèmes et procédés de traitement de l'urée pour réduire la charge de sorbant Ceased WO2009091959A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US2198708P 2008-01-18 2008-01-18
US61/021,987 2008-01-18

Publications (3)

Publication Number Publication Date
WO2009091959A2 true WO2009091959A2 (fr) 2009-07-23
WO2009091959A3 WO2009091959A3 (fr) 2009-09-03
WO2009091959A8 WO2009091959A8 (fr) 2010-11-11

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL2003429C2 (en) * 2009-09-02 2011-03-03 Dhv B V Method for the production of electrical energy from ammonium.
WO2011140389A3 (fr) * 2010-05-05 2012-05-10 C-Tech Biomedical, Inc. Électrolyseur à membrane et système d'hémodialyse l'utilisant
EP2747808A4 (fr) * 2011-08-22 2015-04-22 Medtronic Inc Cartouche de sorbant à double flux
CN105967455A (zh) * 2016-06-30 2016-09-28 华东交通大学 一种垃圾渗滤液自供电脱硝的装置及其方法
WO2021234434A1 (fr) * 2020-05-19 2021-11-25 Ecole Polytechnique Federale De Lausanne (Epfl) Procédé et système de production d'une solution riche en espèces carbonatées et exempte d'espèces azotées.

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US20050218074A1 (en) * 2004-04-06 2005-10-06 Pollock David C Method and apparatus providing improved throughput and operating life of submerged membranes
US6878284B2 (en) * 2001-05-21 2005-04-12 Mitsubishi Denki Kabushiki Kaisha Method and apparatus of treating water containing a nitrogen compound
US20030113931A1 (en) * 2001-12-14 2003-06-19 Li Pan Ammonia and ammonium sensors
CA2542313C (fr) * 2003-10-10 2012-12-04 Ohio University Electrocatalyseurs d'oxydation de l'ammoniac dans des milieux alcalins
CN101553435B (zh) * 2006-03-08 2016-05-11 西门子能源公司 废水处理系统和方法

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL2003429C2 (en) * 2009-09-02 2011-03-03 Dhv B V Method for the production of electrical energy from ammonium.
WO2011028104A1 (fr) * 2009-09-02 2011-03-10 Dhv B.V. Procédé de production d'énergie électrique à partir d'ammonium
US8802323B2 (en) 2009-09-02 2014-08-12 Haskoningdhv Nederland B.V. Method for the production of electrical energy from ammonium
WO2011140389A3 (fr) * 2010-05-05 2012-05-10 C-Tech Biomedical, Inc. Électrolyseur à membrane et système d'hémodialyse l'utilisant
EP2747808A4 (fr) * 2011-08-22 2015-04-22 Medtronic Inc Cartouche de sorbant à double flux
CN105967455A (zh) * 2016-06-30 2016-09-28 华东交通大学 一种垃圾渗滤液自供电脱硝的装置及其方法
WO2021234434A1 (fr) * 2020-05-19 2021-11-25 Ecole Polytechnique Federale De Lausanne (Epfl) Procédé et système de production d'une solution riche en espèces carbonatées et exempte d'espèces azotées.
US20230203374A1 (en) * 2020-05-19 2023-06-29 Ecole Polytechnique Federale De Lausanne (Epfl) Method and system for producing a carbonate-containing species-rich, nitrogen-containing species-free solution

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