WO2005019118A1 - Procedimiento, equipos y reactivos para la depuración de aguas residuales - Google Patents
Procedimiento, equipos y reactivos para la depuración de aguas residuales Download PDFInfo
- Publication number
- WO2005019118A1 WO2005019118A1 PCT/ES2003/000433 ES0300433W WO2005019118A1 WO 2005019118 A1 WO2005019118 A1 WO 2005019118A1 ES 0300433 W ES0300433 W ES 0300433W WO 2005019118 A1 WO2005019118 A1 WO 2005019118A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- effluent
- reactor
- tank
- temperature
- valve
- Prior art date
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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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
Definitions
- the present invention relates to a process, equipment and reagents for the purification of wastewater, whereby the oxidation reaction of organic pollutants in wastewater is optimized, by the Fenton reaction.
- the objective of the treatment is to reduce the Chemical Oxygen Demand (COD) of the effluents through chemical oxidation, increasing biodegradability. It characterizes in the procedure a complete automation in safety conditions.
- COD Chemical Oxygen Demand
- the Fenton reaction that occurs in the reactor is optimized at a certain temperature and pressure and with a catalyst specifically designed to increase the efficiency of the process, while minimizing fouling and precipitation.
- the present invention relates to a process, equipment and reagents for purification of wastewater based on the Fenton reaction.
- the Fenton reaction (hydrogen peroxide in the presence of iron salts), consists in the oxidation of the organic matter contained in effluents using hydroxyl radicals from the controlled decomposition of hydrogen peroxide as an oxidizing agent. Iron acts as an activator of hydrogen peroxide, generating hydroxyl radicals with an oxidation potential greater than permanganate.
- the Fenton reaction degrades organic matter into increasingly simple compounds until it reaches the final formation of C0 2 and H 2 0.
- H 2 0 2 The stoichiometric consumption of H 2 0 2 depends on the organic molecule to be oxidized that defines the chemical oxygen demand (COD).
- COD chemical oxygen demand
- TOC Total Organic Carbon
- Patent documents describe the purification of wastewater by treatment with Fenton reagent, such as the European patent with publication number EP0022525, which defines a process to reduce the chemical oxygen demand of effluents by treating them with hydrogen peroxide and in the presence of a transition metal.
- a wastewater treatment which decomposes the organic matter, adding iron salts and hydrogen peroxide, and heating at 50 ° C-70 ° C for more than 60 min. With stirring, it is subsequently treated with an anion exchange resin where the decomposed substances are adsorbed.
- Document DE4314521 describes a process for continuous (dis) operations to purify water from industrial waste contaminated with organic matter, by the addition of hydrogen peroxide and a homogeneous catalyst, preferably Fenton reagent. The reaction is carried out at 35 ° -40 ° C.
- the process, equipment and purification reagents of the present invention optimize the oxidation of organic pollutants in wastewater under advantageous conditions for the treatment of high flow rates.
- the present invention relates to a process, equipment and reagents for purification of wastewater.
- zone A of effluent preparation
- zone B of preparation of the reagents
- zone C of reaction
- zone D of neutralization and filtered out.
- zone A the effluent is collected and homogenized with stirring or recirculation, the pH is adjusted, and by means of two heat exchangers an increase in temperature is caused until the desired one is obtained in the reactor.
- the temperature of the untreated effluent is increased, at the same time as the effluent that leaves the reactor and goes to the neutralization tank decreases its temperature.
- zone B the reagents, 35% hydrogen peroxide and the catalyst specifically prepared to optimize the oxidation process, composed of metal salts, organic acid and an agent are prepared complexing will join the effluent that comes from zone A in the reactor feed line.
- the acidifying agent will be added to the homogenizing tank and the alkalizing agent to the neutralization tank to reach the desired pH.
- the reactor is located in zone C. Hydrogen peroxide and the catalyst in zone B and the effluent in zone A enter the reactor through the feed line.
- the Fenton reaction in the reactor occurs at an absolute pressure of between 1 kg / cm 2 and 1.5 kg / cm 2 , and at a temperature between 110 ° C and 120 ° C.
- zone D Once the effluent is treated and cooled, it is taken to zone D, to a neutralization tank in which the pH is increased above seven, causing the precipitation of hydroxides.
- a pump sends the waters from the neutralizer tank to a subsequent filter or decanter separating the solid waste from the treated effluent.
- Figure 1 shows a diagram of the procedure
- the present invention relates to a process for purification of wastewater, where Figure 1 shows a diagram of the procedure, equipment and reagents necessary to carry out a treatment of wastewater, by a Fenton reaction under special conditions, maintaining Always the security conditions.
- the procedure is divided into four stages, A, of effluent preparation, B, of reagent preparation, C of reaction, and D of neutralization and filtering, which corresponds to four zones A, B, C, D, differentiated in the installation.
- the installation shows four different zones:
- Effluent preparation zone (A) This is the collection zone of the effluent in the homogenizer tank (1) where it is homogenized by means of an agitator (1.1), or by recirculation by means of a pump (1.4).
- the first pH adjustment is made in a range between 2-5 by adding acidifying agent from the acidifying agent storage tank (10.1), the pH control is carried out by a bypass (1.2) that joins two pH meters that are being continuously compared, so that the pH control is redundant.
- the volume of the homogenizer tank (1) must be greater than three times the volume of the main oxidation reactor (12), a reactor that will be cited below, in the event of an evacuation thereof, so the tank (1) counts homogenizer with a level indicator (1.3).
- the economizer (4) causes a first temperature increase, to 85 ° C in the waters to be treated due to heat exchange with the treated effluent from the main oxidation reactor (12), which is located at 115 ° C, this effluent in turn reduces the temperature, at 45 ° C before reaching the neutralization tank (6).
- a second steam or thermal oil exchanger (5) raises the temperature of the effluent until the desired temperature in the main oxidation reactor (12) is obtained, a temperature that should be in the range of 110 to 120 ° C, preferably 115 ° C.
- the building materials of the exchangers (4 and 5) are selected from 904 stainless steel, graphite, titanium-palladium, hastelloy and inconel.
- this zone (B) there is an area (8) of preparation of H 2 0 2 , which comprises a storage tank (8.1) of H 2 0 2 at 35%, a control valve (8.3) of the supply of H 2 0 2 , a dosing pump (8.2) of the H 2 0 2 that limits the flow of the H 2 0 2 to a maximum of 10% of the working flow of the treatment plant; the area of the alkalizing agent (9) comprising a storage tank of alkalizing agent (9.1) and a dosing pump of this alkalizing agent (9.2); the area of the acidifying agent (10) comprising a storage tank of acidifying agent (10.1) and a dosing pump of this acidifying agent (10.2); and the catalyst preparation area (11) which has a polyethylene tank (11.1) for the preparation of the catalyst solution, a tank (11.2) for the dosing of the catalyst solution and a metering pump (11.3) the dissolution of the catalyst composed mainly of metal salts.
- the catalyst composition will be specified later.
- a flow meter (11.4) is placed which allows, in the case of no catalyst solution entering the main oxidation reactor (12), to cause a previous stop and an alarm.
- the H 2 0 2 and catalyst (8.2, 11.3) drive pumps direct the dosages to the feed line (12.1) of the main oxidation reactor (12).
- the alkalizing agent pump (9.2) directs the dosage to the neutralization tank (6), and the acidifying pump (10.2) directs the dosage to the homogenizing tank (1).
- the main oxidation reactor (12) must ensure sufficient permanence of the reagents inside, and for this purpose it has a level control (12.3) that regulates the valve (12.9) located in the outlet line (12.10) .
- the residence time in the main oxidation reactor (12) is sixty minutes.
- the main oxidation reactor (12) has a pressure control (12.6) that releases the gases and vapors generated towards a bubbler.
- the main oxidation reactor (12) has a line (12.4) of water or nitrogen vapor that, according to an established sequence, purges the main oxidation reactor (12) to avoid the formation of explosive mixtures and prevents risks of inflammation.
- the nitrogen or steam inlet is controlled with a valve (12.8) inertization.
- the main oxidation reactor (12) has an automatic drain valve (12.7) which in case of emergency opens the main oxidation reactor (12) in the homogenizer tank (1).
- the main oxidation reactor (12) has a valve (12.9) for controlling the level of the main oxidation reactor (12).
- the construction material of the main oxidation reactor (12) can be 904 stainless steel or enamelled carbon steel inside, or Teflon coated carbon steel inside.
- Water lines at temperatures above 60 ° C are tefloned inside or are made of 904 stainless steel or are made of titanium-palladium.
- the main oxidation reactor (12) has an agitator (12.2) that starts automatically when the level inside is greater than 30%. If the agitator (12.2) of the main oxidation reactor (12) is stopped, the process cannot work.
- the effluent leaves the main oxidation reactor (12) through an outlet line (12.10) that directs the effluent to the economizer (4).
- the level of the main oxidation reactor (12) is controlled through a PID interlock that regulates a valve (12.9) for this purpose. Zone D neutralization and filtering.
- the effluent once treated and cooled is taken to the neutralization tank (6) with stirrer
- the neutralization tank (6) has a pH controller (6.2) and a level controller (6.3).
- a pump (6.4) sends the water from the neutralization tank (6) to a spark plug filter (7). After the spark plug filter (7) there is an outlet line
- the separation of the effluent and the solid residue can also be carried out in a lamellar or static decanter or by bag filtration.
- the effluent treatment limit characteristics are: Indifferent pH Flow rate, m 3 / h 100 1 / h up to 100 m 3 / h Sodium Sulfate, g / 1 maximum 40gr / l Sodium chloride, g / 1 maximum 200gr / l TOC, g / 1 maximum 15gr / l COD, g / 1 maximum 40gr / l H 2 or 2 maximum 40gr / l Solids in suspension maximum 500gr / l For effluents whose concentration in matter or- In the case of a dose exceeding the value of 40gr / l in COD, a dilution will be provided in the homogenization tank.
- the first step of the procedure is the start-up of the system, in which the different transients must be taken into account until the system conditions are reached in all the equipment.
- the alarms that prevent the start-up are the levels of the different tanks and tanks, and the pH values of the different points of the procedure: High level homogenization tank 60% Level under homogenization tank 20% High level neutralizer tank 50% Low level neutralizing tank 10% • high pH setting homogenization 5'0 pH low setting homogenization 2'0 high pH neutralizing tank 9'0 pH under neutralizing tank 7'0 Parameters of interest for process control debugging time:
- the parameters of emergency stop, total stoppage of the installation are: high temperature of the main oxidation reactor, (temperature greater than 125 ° C), high pressure of the main oxidation reactor, (pressure greater than 1.5 Kg / cm 2 ) and exceed a maximum pre-stop time, 600 sec. , • Automatic sequence parameters that are activated at start-up: PID (Proportional Integral-Derivative) homogenizing pH control, 3 '0, (regulates the acid dosage), PID temperature inside the reactor 115 ° C , regulates heating through exchanger 5, PID reactor level (100%), regulates valve opening 12.9, PID reactor pressure 1.0 bar, regulates valve opening 12.5,
- PID Proportional Integral-Derivative
- the program closes the inertization valve (12.8). From this temperature the vapors generated in the effluent inert the reactors. If the temperature drops below 110 ° C, the inertization is restarted again. If the temperature drops below 100 ° C, the pre-shutdown alarm is activated due to the temperature below the main reactor (12). Permanent phase:
- the effluent increases the temperature in the heat exchangers (4 and 5) until it reaches a range between 110 or C-120 ° C, preferably 115 ° C, and before entering the main oxidation reactor (12) it is mixed with the hydrogen peroxide and catalyst in the feed line (12.1) of the main oxidation reactor (12).
- the effluent next to the catalyst and the hydrogen peroxide enters the main oxidation reactor (12), the oxidation reaction being carried out continuously and with the aid of a stirrer (12.2).
- the oxidation reaction of organic matter with the hydrogen peroxide occurs in the presence of metal catalysts. If not enter effluent in the reactor Prin- pal oxidation 'causes a previous stop and an alarm, the no effluent inlet is measured through a flowmeter (13) located immediately before the economizer (4). If the flow of the effluent falls below a setpoint, determined by half the volume of the main oxidation reactor, the plant goes to the state of pre-preparation or shutdown.
- the effluent discharge pumps (2, 3) have a nominal flow rate equal to twice the volume of the main oxidation reactor (12), thus preventing the reaction time from being excessively reduced.
- There is a safety system inside the main oxidation reactor (12) whereby a pressure greater than 3 '5 kg / cm 2 , involves the opening of a safety valve (12.5) or rupture disc, installed for such end.
- the temperature conditions in the main oxidation reactor (12) are in the range of 110 ° C to 120 ° C and the pressure conditions in the range of 1 kg / cm 2 and 1.5 kg / cm 2 .
- the catalyst formulation consists of the following compounds: iron II, in concentration between 2% and 30% in the form of ferrous sulfate or ferrous chloride, copper II, in concentration between 1% and 10%, in the form of copper sulfate, acid organic, selected from tartaric acid, oxalic acid or citric acid, in concentration from 1% to 10%, iron complexing agent, such as EDTA or / and HDPE in concentration from 1% to 5%, phosphoric, hydrochloric or sulfuric acid, for adjust the pH to a range between 1 and 2.
- Said catalyst is dosed in a concentration of 0.01% to 1% over the total flow to be treated.
- the reaction temperature is maintained in the main oxidation reactor (12) by a control duplicated by PT-100 probes.
- the effluent is treated in the main oxidation reactor (12) and cooled in the economizer (4) to 45 ° C, it is taken to the neutralization tank (6).
- the pH is increased above 7 by the addition of NaOH or other alkalizing agent causing the precipitation of metal hydroxides.
- the neutralization tank (6) there is a pH controller (6.2), which controls that the pH range is between 7 and 9 and a level controller (6.3).
- pumps (6.4) send the water to the filter (7) or subsequent decanter.
- the control system executes the following actions: it closes the valve (8.3) of the H 2 0 2 passage and the dosing pump (8.2) of H 2 0 2 , for the catalyst dosing pump (11.3), cancels the interlocks leading to emergency preparation, deactivates the heating interlock, opens the valve (12.8) for automatic inerting of nitrogen or steam purge.
- a timer effluent recirculation start time
- the control system diverts the effluent to the homogenization tank (1).
- the reactor drain valve (12.7) is opened 100%, the effluent pump (2 and 3) is stopped, the agitator is stopped (12.2) of the reactor, the reactor level controller (12.3) that leaves the valve (12.7) in manual-open position is deactivated, the reactor pressure controller (12.6) leaving the safety valve (12.5) is deactivated In manual-open position, the drain valves (12.5 12.7, 12.9) of the reactor are in the safe (open) position, the inerting valve (12.8) is automatically closed.
- This stage is to safely stop the installation in the event of an irregular operating situation that could cause a greater risk.
- a low effluent / H 2 0 2 ratio would force an excessive supply of hydrogen peroxide with the risk of explosive mixtures. If this is the case, it should act by diluting the effluents to a greater degree.
- An "Emergency Stop" is not only caused because an anomaly that implies a Preparedness has not been solved in a certain time, 600 sec. , but also because the temperature of the main oxidation reactor (12) is greater than a set value, 125 ° C, this high temperature in reactors can accelerate the reaction and become uncontrollable with the risks involved, because the reactor pressure ( 12) main oxidation is greater than a set value, 1.5 Kg / cm 2 , excessive pressure may indicate an abrupt decomposition that is not able to dislodge the system provided for that purpose, or because a button is manually operated provided for this purpose, or the Emergency Stop is activated through a control system.
Abstract
Description
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Priority Applications (11)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DK03816982.7T DK1647529T3 (da) | 2003-08-22 | 2003-08-22 | Fremgangsmåde til oprensing af spildevand |
MXPA06002078A MXPA06002078A (es) | 2003-08-22 | 2003-08-22 | Procedimiento, equipos y reactivos para la depuracion de aguas residuales. |
JP2005508158A JP2007514515A (ja) | 2003-08-22 | 2003-08-22 | 排水精製方法、装置及び薬剤 |
CNB038269457A CN100379688C (zh) | 2003-08-22 | 2003-08-22 | 用于废水净化的方法、装置和试剂 |
EP03816982.7A EP1647529B1 (en) | 2003-08-22 | 2003-08-22 | Method for purifying wastewaters |
ES03816982.7T ES2554460T3 (es) | 2003-08-22 | 2003-08-22 | Método para purificar aguas residuales |
AU2003260523A AU2003260523A1 (en) | 2003-08-22 | 2003-08-22 | Method, devices and reagents which are used for wastewater treatment |
CA2536302A CA2536302C (en) | 2003-08-22 | 2003-08-22 | Method, devices and reagents for wastewater treatment |
US10/568,994 US7666315B2 (en) | 2003-08-22 | 2003-08-22 | Methods, devices and reagents for wastewater treatment |
PCT/ES2003/000433 WO2005019118A1 (es) | 2003-08-22 | 2003-08-22 | Procedimiento, equipos y reactivos para la depuración de aguas residuales |
IL169935A IL169935A0 (en) | 2003-08-22 | 2005-07-27 | Method, devices and reagents which are used for wastewater treatment |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/ES2003/000433 WO2005019118A1 (es) | 2003-08-22 | 2003-08-22 | Procedimiento, equipos y reactivos para la depuración de aguas residuales |
Publications (1)
Publication Number | Publication Date |
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WO2005019118A1 true WO2005019118A1 (es) | 2005-03-03 |
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/ES2003/000433 WO2005019118A1 (es) | 2003-08-22 | 2003-08-22 | Procedimiento, equipos y reactivos para la depuración de aguas residuales |
Country Status (11)
Country | Link |
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US (1) | US7666315B2 (es) |
EP (1) | EP1647529B1 (es) |
JP (1) | JP2007514515A (es) |
CN (1) | CN100379688C (es) |
AU (1) | AU2003260523A1 (es) |
CA (1) | CA2536302C (es) |
DK (1) | DK1647529T3 (es) |
ES (1) | ES2554460T3 (es) |
IL (1) | IL169935A0 (es) |
MX (1) | MXPA06002078A (es) |
WO (1) | WO2005019118A1 (es) |
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CN1819974A (zh) | 2006-08-16 |
IL169935A0 (en) | 2009-02-11 |
MXPA06002078A (es) | 2006-08-31 |
EP1647529A1 (en) | 2006-04-19 |
AU2003260523A1 (en) | 2005-03-10 |
US7666315B2 (en) | 2010-02-23 |
CA2536302A1 (en) | 2005-03-03 |
EP1647529B1 (en) | 2015-09-30 |
US20080035583A1 (en) | 2008-02-14 |
CN100379688C (zh) | 2008-04-09 |
DK1647529T3 (da) | 2015-12-21 |
CA2536302C (en) | 2011-08-09 |
ES2554460T3 (es) | 2015-12-21 |
JP2007514515A (ja) | 2007-06-07 |
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