WO2016167708A1 - Techniques de nettoyage d'émissions de gaz de combustion dans un épurateur - Google Patents

Techniques de nettoyage d'émissions de gaz de combustion dans un épurateur Download PDF

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Publication number
WO2016167708A1
WO2016167708A1 PCT/SE2016/050308 SE2016050308W WO2016167708A1 WO 2016167708 A1 WO2016167708 A1 WO 2016167708A1 SE 2016050308 W SE2016050308 W SE 2016050308W WO 2016167708 A1 WO2016167708 A1 WO 2016167708A1
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Prior art keywords
scrubber
gas
liquid
cassettes
opening angle
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PCT/SE2016/050308
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English (en)
Inventor
Lars Waardahl
Ingvar HÄLLGREN
Kristina Waardahl
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Lkw Teknik Ab
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Application filed by Lkw Teknik Ab filed Critical Lkw Teknik Ab
Priority to SE1700273A priority Critical patent/SE541286C2/en
Publication of WO2016167708A1 publication Critical patent/WO2016167708A1/fr

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N3/00—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust
    • F01N3/02—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for cooling, or for removing solid constituents of, exhaust
    • F01N3/04—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for cooling, or for removing solid constituents of, exhaust using liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/02—Separating dispersed particles from gases, air or vapours by liquid as separating agent by passing the gas or air or vapour over or through a liquid bath
    • B01D47/021—Separating dispersed particles from gases, air or vapours by liquid as separating agent by passing the gas or air or vapour over or through a liquid bath by bubbling the gas through a liquid bath
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/16—Fractionating columns in which vapour bubbles through liquid
    • B01D3/163—Plates with valves
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/06—Spray cleaning
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2221/00—Applications of separation devices
    • B01D2221/08—Mobile separation devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D2247/04—Regenerating the washing fluid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D2247/08—Means for controlling the separation process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2247/00—Details relating to the separation of dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D2247/10—Means for removing the washing fluid dispersed in the gas or vapours
    • B01D2247/107—Means for removing the washing fluid dispersed in the gas or vapours using an unstructured demister, e.g. a wire mesh demister
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/608—Sulfates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/01—Engine exhaust gases
    • B01D2258/012—Diesel engines and lean burn gasoline engines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/12—Methods and means for introducing reactants
    • B01D2259/122—Gaseous reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/12—Methods and means for introducing reactants
    • B01D2259/124—Liquid reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact

Definitions

  • the principle of sulfur oxide purification is based on the basic chemical rule that an acid can be neutralized with an alkali, such as sodium hydroxide (NaOH).
  • an alkali such as sodium hydroxide (NaOH).
  • NaOH sodium hydroxide
  • the sulfur oxide which is released by burning fossil fuels containing sulfur, is neutralized when coming in contact with the washing liquid/ scrubber liquid, consisting of sodium hydroxide dissolved in water.
  • the sulfur is bonded as sodium sulfite (Na 2 SO 3 ) which after aeration is converted to sodium sulfate (Na 2 SO 4 ), a chemically very stable salt that can safely be discharged into the sea or in a land-based sewage.
  • a scrubber process depends on a variety of factors, primarily related to a creation of large areas where the gas and scrubbing liquid can react with each other.
  • the scrubbing liquid can be atomized into droplets in spray nozzles, and /or the scrubber can be filled with packings in order to increase the active contact surface.
  • Another method is to allow the exhaust gases to bubble through a number of so-called trays, flooded with process fluid, on its way up through the scrubber.
  • a prerequisite for the function of the scrubbers known to date, in use for purification of exhaust gases from diesel engines and other industrial processes, is that a majority of enclosed particulate matter is first separated from the gas to be purified. This is for example done by trapping the particles in an initial step, before the exhaust gas is led into the scrubber.
  • a marine scrubber In marine applications, where seawater is salty enough, it is not needed to add NaOH to the washing liquid, instead it is enough to wash the flue gas with large quantities of salt water.
  • the scrubber is then operated differently from a so-called closed loop fresh water scrubber, since the scrubbing liquid is continuously discarded into the sea, in a so-called open loop.
  • the requirement for discarding such a liquid is that it satisfies the condition that transparency (turbidity) is less than 25 NTU, otherwise the fluid must be cleaned from particulate matter, i.e. soot particles, before it is released l into the sea.
  • a marine scrubber is arranged so that it can run both closed loop freshwater and open loop saltwater, a so-called hybrid scrubber.
  • bottoms or trays can be used. These are very similar to the columns used in conventional absorption and distillation and which may for example be bell trays /or valve tray columns or sieve tray columns, where the contact surface between the gas and the liquid is made as large as possible. Tray columns usually have a wider operating range (L / G) than packing columns, while the valve trays have the widest.
  • a bell-bottom is a common tray in terms of both distillation and absorption.
  • the principle is to fill each tray with as many bell-like valves as possible. When the bells are closed, washing liquid is collected upon the tray, and when the gas pushes from below, the bells open up which gives the dynamics.
  • the problem with this technique is that the scrubber must be large if the necessary number of bells is to be fitted in, and also the problem with "dead areas" in the trays where the gas and liquid can't get in contact with each other. Bell trays are sensitive to particulate matter that slowly but surely will get the bell valves to jam.
  • Sieve trays are either course, with a small reaction area, or dense causing a high backpressure, if flow is increased, and also tend to be clogged by soot and other particulate matter.
  • soot particles in the exhaust gas is an overriding problem of constructing a fail-safe sulfur oxide scrubber for diesel engines and other processes.
  • flue gas is purified from
  • venturi step before the scrubber, Figure 1.
  • a venturi step involves a flow area restriction where liquid in the form of droplets meets the flue gas and the likelihood that the soot particles are captured by the drops is great.
  • Such a venturi step is primarily used for particulate matter/ soot separation in a first step and is complemented by a spray nozzles scrubber or a packing one in a second step, where the major sulfur oxide reduction takes place with alkali.
  • a venturi scrubber operates at a high gas velocity of 30-120 m /sec and a water pressure to the nozzles between 25 and 60 bars.
  • the contact time is short and a high pressure drop in the restriction causes a high energy consumption.
  • Liquid / gas mass flow ratio also becomes limited and rapid variations in the gas flow must be limited, even if the venturi flow area restriction can be regulated.
  • the venturi causes substantial additional costs in space and equipment in the form of pumps, pipes and control equipment, and furthermore an increased running cost for driving the liquid and gas flows.
  • the present invention can solve the above mentioned problems with exhaust gas from diesel engines, or similar demanding industrial processes, by having the features defined in the independent claims.
  • a scrubber may be permanently adjusted for a certain process with constant parameters, such as gas flow and pressure drop, and is therefore called a static scrubber.
  • Scrubbers capable of a varying gas flow without creating problems in the process are called dynamic.
  • Diesel engines are typically run with varying speed and load, and the flow of exhaust gases from such an engine will therefore vary over time. Diesel engines are also sensitive to variations in downstream back-pressure, which for example can be caused by long flue gas ducts or heat exchangers connected to an exhaust gas outlet which obstruct the exhaust flow and thereby creates a back pressure.
  • a scrubber with ideal back pressure characteristics for purification of exhaust gas should have a low and constant pressure drop,
  • Embodiments of a scrubber for cleaning exhaust gases from one or more diesel engines, or from a similar demanding industrial process.
  • Embodiments of the disclosed scrubber meet the requirements in terms of handling a variable gas flow and to keep the back pressure within an allowable range.
  • Embodiments of the described scrubber are also capable of purifying exhaust gases without a prior cleaning from particulate matter, which is a big advantage.
  • the cleaning efficiency of particulate matter for a KEBI-scrubber is normally about 75-80%. It is the smallest particles which passes the scrubber. If a "close to 100%" capture of particulate matter is in demand, then for example a wet electric precipitator (WESP) device can be installed, in the scrubber tower, above the top tray and preferably also over the inflow of the scrubbing liquid. This device collects the small particles below 2.5 micron, and is dependent on the extreme even gas flow distribution in the tower, created by the tray(s) with KEBI-cassettes. Indeed a nice symbiosis.
  • WESP wet electric precipitator
  • a scrubber of the invention with its tray design with a special kind of cassettes with hinged rocker valves, in the following called "KEBI- cassettes", can be adapted to meet the demands of a scrubber for purification of diesel exhaust gas or general industrial flue gases and moreover also of soot and particulate matter.
  • KEBI-scrubber A basic working principle of a "KEBI-scrubber” is described in Patent US 4,557,875 including this type of valve cassettes.
  • These cassettes have been used in the last 25 years, mainly in the pulp and paper industry for its generally good properties, since the requirement of dynamics in this context has been extremely limited. To consider this construction or parts thereof in a process with high demands on dynamics, and also pressure drop, is a novelty in the industry.
  • Similar demanding industrial processes refers to those that are dynamic in flow (amplitude) and at the same time sensitive to variations in back pressure and /or a demand on NOx purification over 8% and/ or demand on an extreme even gas flow distribution in the scrubber tower.
  • the epithet "demanding" may also include a requirement that the scrubber will have great effectiveness in relation to its size and /or have low energy and chemical
  • Figure 1 shows a flow diagram of a venturi scrubber, representing the prior art.
  • Figure 2 shows a variant of a rocker valve, a so-called hinged rocker valve with a counterweight and its opening angle a in a KEBI-cassette.
  • FIG. 3 shows a flowchart in accordance with a marine embodiment of the invention.
  • a scrubber with KEBI-cassettes has the following characteristics, from the use in the pulp and paper industry; 1) Very high separation of sulfur-oxides, in principle 100%.
  • the scrubber disclosed here differs from other scrubber designs on a number of points. Several of these points are listed below together with important advantages.
  • the heart of the disclosed scrubber is its tray design with its cassettes
  • the rocker valves may be manufactured in metal, plastic, plastic composite, rubber, or a combination of these or other equivalent materials.
  • the rocker valves may be of a hinged type or of a fixed leaf type, flexible bendable in itself. Minimum pressure drop and the best dynamic properties are obtained if the valves do not have any valve seats on their sides.
  • a scrubber with KEBI-cassettes is capable of keeping the pressure drop over the trays largely constant in a way that the process fluid recirculation flow is increased if the gas flow is reduced or else reduced if the gas flow is increased, fig.3. Increased recirculation flow actually leads to accumulation of more process fluid over the trays and vice versa, reduced recirculation flow leads to less process fluid collected over the trays.
  • valves immediately opens up fully after which the pressure drop is momentarily reduced.
  • the valves' maximum opening angle is normally mechanically limited to 8 ° -30 °, depending on the process and the choice of closed or open loop.
  • a scrubber with KEBI-cassettes is self-cleaned from deposit of particles and sodium sulfite crystals by the continuously valve movements.
  • the gas velocity up through the scrubber tower can be varied between 0.5 to 4.5 m /s, which is significantly more than any similar engineering. This denotes a considerably wider operating range and enables a freer choice of the cross section of the scrubber tower.
  • the gas flow is also always evenly distributed over the surface of a tray, which helps all the valves to move with the same frequency and amplitude.
  • the pressure drop for the scrubber process can be kept constant, independent of the gas flow, through regulating the amount of process liquid in place over the trays.
  • the KEBI-scrubber is designed mostly as rectangular or square, which is an advantage in tight spaces and to bring in as many cassettes as possible.
  • the extraction of particulate matter is significantly higher than in any known scrubber design, because the process fluid which accumulates over each tray is whipped to foam due to the rocker valves movements, which makes the probability of soot and particulate matter to get past a number of trays after each other, extremely small.
  • Sulfur oxide capture will also be extra efficient, inter alia, thanks to the rocker valves and their counter weights creating a large wet reaction surface, and their movements leading to the gas being dispersed in the process liquid and the process liquid being dispersed in the gas.
  • the low pressure drop is a great advantage in connection with the purification of exhaust gas from diesel engines, as these engines are sensitive to high back pressure. Pilot runs on different flue gases in marine and industrial processes have shown that the optimal pressure drop across each tray lies between 300 and 500 Pa.
  • the chemical process in a KEBI-scrubber works like in any other scrubber type, with the difference that the installation and operation is more easy and efficient thanks to the above-related differences and advantages.
  • part 1
  • the exhaust gas to be purified is passed directly into the lower half of the scrubber tower. It can advantageously be cooled down in a gas/ water heat exchanger, as the scrubbing process is most effective at lower temperatures. Accordingly there is no need for a venturi step, including a control system and a pumping system, in order to prevent particulate matter from entering the scrubber process.
  • the above-mentioned trays with their cassettes and the rocker valves are installed in at least one level.
  • An extra, empty level can be set up to be kept in reserve in case the purification requirements would be increased in the future.
  • the KEBI-scrubber is arranged for closed loop operation, fresh water is mixed with sodium hydroxide NaOH in a recirculation tank and this mixture is then pumped up to the top part of the tower to the top tray, where the liquid is distributed evenly over the cassettes after which it leaks down to the next tray etc., until the liquid ends up in the recirculation tank again.
  • the pressure drop over the scrubber is at least held relatively constant, by controlling the recirculating flow. If necessary, the recirculating flow is also cooled.
  • sodium sulfite Na2SO3 is created in the scrubbing liquid, and as the level increases a portion of the scrubbing liquid is bled out to a treatment plant, where the dust is separated out into a sludge tank, and is thereafter oxygenated into sodium sulfate Na 2 S0 4 before it can be poured into a drain or into the sea. New alkaline NaOH and fresh water replaces the bled out amount.
  • the above-described recirculation loop is replaced by a direct supply of seawater on at least two tray levels in the upper part of the scrubber tower.
  • sea water has passed the scrubber, it is led directly back to the sea, through a treatment plant.
  • a "demister” / mist eliminator is passed, where residual liquid droplets are separated out. Downstream of the demister, usually a variable speed sucking fan is installed, which further helps to keep a diesel engine back pressure at a low stable level.
  • part 2
  • the exhaust gas to be cleaned from particulate matter, sulfur- and nitrogen-oxides is first cooled in a heat exchanger 1 and is then sucked into a scrubber tower 2 through an inlet 3 located in the lower half.
  • the exhaust gas first passes through a first tray 4 consisting of so-called hinged rocker valve cassettes, over which there is a level of process liquid and foam, which the exhaust gas has to pass, after which it then rises up to a following identical tray and so on until it finally passes a top tray 5 and leaves the scrubber tower 2 through a mist eliminator 6 and further through an outlet 7, connected to a downstream suction fan.
  • the process liquid leaking downwards in the scrubber tower 2 is collected in a lower reservoir 8 which leads to a recirculation tank 9 in which new washing liquid is prepared by mixing sodium hydroxide and freshwater. This occurs at the same rate as old washing liquid is bled out to a purification device 10a, where the slurry of particulate matter is separated out into a holding tank 10b, which, for example, later can be emptied in a harbor, provided the effluent consisting of sodium sulfite was first oxygenized and transformed into sodium sulfate before being discharged into the sea or into a drain.
  • the content in the recirculation tank 9 will consist of sodium sulfite and soot particles dissolved in the process water.
  • the concentration of particles and sodium sulfite increase constantly, until new washing liquid is mixed in and the old is bled out.
  • a typical upper limit is in the range 45-50 grams of sodium sulfite / liter of washing liquid.
  • a pump 11 pushes the washing liquid through a cooler 12 in an upper part 13 of the scrubber tower 2.
  • the pressure drop over the trays 4 to 5 is recorded by a differential pressure gauge 14 which controls the recirculation flow by means of a control valve 15 and thus regulates the amount of washing liquid which is situated above each tray 4 to 5. With this regulation, the pressure drop is kept largely constant, regardless of the level of exhaust gas flow and thus
  • control valve 15 can be manually operated to a predetermined pressure drop across the trays and the scrubber is then only semi-dynamic. A faster and more accurate control of the pressure drop over the trays may be obtained if the pressure drop is measured over each individual tray and the washing liquid is regulated to each tray individually.
  • the two heat exchangers 1 and 12 are supplied with cooling water from a pump 16.
  • a KEBI-scrubber can also be run in a so-called open salt water mode, in contrast to the above described environmentally friendly closed freshwater mode.
  • the seawater pump 16 feeds the sea water to a maximum of two levels 17 and 18 in the scrubbing tower 2 wherein the recirculation loop is disabled, after which the scrubbing liquid directly goes to the particle separation treatment plant 10a, 10b for removing of sludge, before being deposited in the sea.
  • the higher sodium content in the recirculation loop brings the added bonus that the nitrogen oxides reduction in the scrubbing tower 2 increases from the previous maximum of 8% to over 25%.
  • Higher NOx reduction is not possible to reach because the scrubbing process only works mainly on nitrogen dioxide (N0 2 ) and not on the nitrogen oxide (NO).
  • a gas mixture of chlorine dioxide should be injected into the flue gas duct upstream of the scrubber so that the residence time in the duct is at least 0.5 second before the mixture reaches the scrubber.
  • a location upstream of an elbow duct is chosen in order to use the turbulence after the bend for the gas to be mixed with the flue gases.
  • the chlorine dioxide gas that not yet had time to react with NO
  • the scrubber's first tray 4 where a uniform flow distribution is obtained, due to the pressure resistance the first tray creates and then moves up in the scrubber tower and is found in the about 200 mm high foam layer over each tray, leading to a 100% conversion of NO to NO2, which is then converted to nitrate by the sulfite solution in the scrubber.
  • the temperature in the scrubber is kept below 85 °C, where the SOx purification is relatively effective, while the chlorine dioxide gas does not dissolve in the scrubbing liquid at this temperature level.
  • a scrubber with KEBI-cassettes allows a very effective and close to 100% simultaneous cleaning of both NOx and SOx thanks to its large wet reaction area (rocker valves with counter weights) in combination with the foam layer over each tray and not least the ability to create an even gas flow over the cross-sectional area and to handle a high particulate matter content and a high sulfite content without showing clogging problems.
  • These properties which are unique in the industry, means that a KEBI-scrubber can be made smaller than other scrubber types, which is a characteristic that is appreciated in industrial contexts. Furthermore, the possibility of operating at a higher sulfite level saves chemicals.
  • a scrubber with KEBI-cassettes does not have this problem, because its construction with trays filled with cassettes with rocker valves over which a foam phase are present, effectively solves the excess ammonia, since the ammonia is readily soluble in water.
  • a scrubber with KEBI-cassettes is particularly adapted to use for NOx purification by means of ammonia, the method has a major drawback in that the reaction requires a
  • the bubble and foam process that is present over the KEBI-cassettes, is an excellent oxy generator if air is supplied e.g. beneath one or more trays. In this manner the conversion of sodium sulfite to sodium sulfate is speeded up. The oxygenation may not be pushed so far that it the impacts the sulfur oxide purification.
  • the flow of scrubbing liquid is regulated so that the back pressure is kept at least relatively constant, and within predetermined limit values. This will for example ensure that a diesel engine run as effective as possibly.
  • concentration in the range of 50-200 g / 1 is used, which is considerably higher than normal practice. This provides, as mentioned earlier, an enhanced purification of nitrogen oxides, from a normal 8% up to 25-30%.
  • the rocker valves in the cassette or cassettes in the top-tray 5 are set so that they have a maximum opening angle greater than the maximum opening angle of the rocker valves in the cassette or cassettes in the other trays.
  • This enables the level of liquid and foam to be lower over this tray, than over the other trays, which can be advantageous for example when you do not want to risk that the level of foam reaches the demister or the exit of the scrubber.
  • the maximum opening angle of the rocker valves in the top tray cassettes is adjusted to be about 40% -60% greater than the opening angle of the rocker valves in the cassettes of the other trays.
  • the rocker valve's maximum opening angle is variable and remotely controllable. This can apply to all rocker valves, or for some, such as the ones in the top-tray.
  • the rocker valves' maximum opening angle can also be controlled separately, e.g. for different trays.
  • the maximum rocker valve opening angle can be adjusted in the range of 8-30°, depending on the pre-selected and temperature-dependent gas velocity through the cassettes, where the gas velocity is in the range 0.5-4.5 m/s. In some embodiments the rocker valve's maximum opening angle is adapted to about 30° at a mass flow ratio of about 10 (liquid) to 1 (gas).
  • a control valve 15 is controlled so that the liquid to gas mass flow ratio is about 1 to 1 in the scrubber, when the diesel engine or a similar demanding industrial process runs at its highest nominal output power rating.
  • control valve 15 is controlled so that the mass flow ratio in the scrubber, in a closed loop case, is about 6 (liquid) tol(gas) at the diesel engine's or a similar demanding industrial process' lowest nominal output power rating.
  • air is supplied under at least one tray in order to let the sodium sulfite in the scrubbing liquid to be oxygenated to sulfate directly in the purification process.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)
  • Exhaust Gas After Treatment (AREA)

Abstract

La présente invention concerne un épurateur avec un ou plusieurs niveau(x) de plateau, équipé(s) de cassettes de soupape à bascule, qui nettoie les gaz d'échappement d'un moteur diesel marin en éliminant des oxydes de soufre et des oxydes d'azote, étant donné que la contrepression est faible et qui grâce à l'invention peut être maintenue constante et à l'intérieur de limites permises, et ce sur l'ensemble du registre de la vitesse de rotation du moteur et de la puissance nominale, car ces moteurs sont particulièrement sensibles à des niveaux élevés de contre-pression. L'invention peut également être appliquée dans des procédés industriels exigeants analogues tels que ceux qui sont sensibles aux variations de contre-pression ou ayant des exigences pour une épuration à 100 % de SOx et/ou d'épuration supérieure à 8% de NOx. Lors d'essais, effectués avec du carburant diesel à teneur accrue en soufre, une épuration efficace à 100 % d'oxyde de soufre a été confirmée ainsi qu'une épuration de NOx simultanée jusqu'à 25 % et il a également été vérifié que le gaz d'échappement peut être introduit directement dans l'épurateur, sans problèmes de colmatage dus à la suie dans l'échappement. D'autres avantages sont obtenus en ce qu'un épurateur selon l'invention fonctionne à haute teneur en sulfite, jusqu'à au moins 200 g/L, moins de produits chimiques et d'eau douce étant épuisés, tandis que l'espace pour réservoirs de stockage est réduit. Les applications sont principalement dans le secteur maritime.
PCT/SE2016/050308 2015-04-14 2016-04-12 Techniques de nettoyage d'émissions de gaz de combustion dans un épurateur WO2016167708A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
SE1700273A SE541286C2 (en) 2015-04-14 2016-04-12 A scrubber designed to purify exhaust gas, the use of it and a method

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SE1500177A SE538815C2 (sv) 2015-04-14 2015-04-14 Sätt att rena dieselmotorers avgaser från sot, svavel- och kväveoxider
SE1500177-9 2015-04-14

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CN106422734A (zh) * 2016-12-02 2017-02-22 江苏瑞洁环境工程科技有限责任公司 一种鼓泡式烟气脱硫装置
WO2019008142A1 (fr) * 2017-07-06 2019-01-10 Bilfinger Engineering & Technologies Gmbh Dispositif et procédé de purification de gaz de fumées et de filtrage de l'eau de lavage
CN111167245A (zh) * 2020-01-03 2020-05-19 北京路新沥青混凝土有限公司 一种沥青烟净化处理方法
US11124714B2 (en) 2020-02-19 2021-09-21 Marathon Petroleum Company Lp Low sulfur fuel oil blends for stability enhancement and associated methods
CN114599864A (zh) * 2019-09-10 2022-06-07 阿法拉伐股份有限公司 清洁排气的排气清洁系统和方法以及排气清洁系统的使用
WO2022234250A1 (fr) * 2021-05-05 2022-11-10 LGE IP Management Company Limited Procédé de traitement d'un flux de gaz de purge pour éliminer l'ammoniac
US11802257B2 (en) 2022-01-31 2023-10-31 Marathon Petroleum Company Lp Systems and methods for reducing rendered fats pour point
US11860069B2 (en) 2021-02-25 2024-01-02 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US11891581B2 (en) 2017-09-29 2024-02-06 Marathon Petroleum Company Lp Tower bottoms coke catching device
US11898109B2 (en) 2021-02-25 2024-02-13 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of hydrotreating and fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US11905468B2 (en) 2021-02-25 2024-02-20 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of fluid catalytic cracking (FCC) processes using spectroscopic analyzers
EP4344766A1 (fr) * 2022-09-28 2024-04-03 Valmet Technologies Oy Procédé pour minimiser la consommation d'un agent réducteur lors de l'élimination de nox
US11970664B2 (en) 2021-10-10 2024-04-30 Marathon Petroleum Company Lp Methods and systems for enhancing processing of hydrocarbons in a fluid catalytic cracking unit using a renewable additive
US11975316B2 (en) 2019-05-09 2024-05-07 Marathon Petroleum Company Lp Methods and reforming systems for re-dispersing platinum on reforming catalyst
US12000720B2 (en) 2019-09-06 2024-06-04 Marathon Petroleum Company Lp Product inventory monitoring

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US3807711A (en) * 1970-02-27 1974-04-30 Seitetsu Kagaku Co Ltd Tray for fluid contactor apparatus
US4557875A (en) * 1981-03-16 1985-12-10 Orszagos Koolaj Es Gazipari Troszt Phase-contacting plate for a phase-contacting column
EP2708274A1 (fr) * 2011-05-11 2014-03-19 Kawasaki Jukogyo Kabushiki Kaisha Dispositif de purification de gaz d'échappement par voie humide

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106422734A (zh) * 2016-12-02 2017-02-22 江苏瑞洁环境工程科技有限责任公司 一种鼓泡式烟气脱硫装置
WO2019008142A1 (fr) * 2017-07-06 2019-01-10 Bilfinger Engineering & Technologies Gmbh Dispositif et procédé de purification de gaz de fumées et de filtrage de l'eau de lavage
US11891581B2 (en) 2017-09-29 2024-02-06 Marathon Petroleum Company Lp Tower bottoms coke catching device
US11975316B2 (en) 2019-05-09 2024-05-07 Marathon Petroleum Company Lp Methods and reforming systems for re-dispersing platinum on reforming catalyst
US12000720B2 (en) 2019-09-06 2024-06-04 Marathon Petroleum Company Lp Product inventory monitoring
US20220325646A1 (en) * 2019-09-10 2022-10-13 Alfa Laval Corporate Ab Exhaust gas cleaning system and method for cleaning exhaust gas and use of exhaust gas cleaning system
CN114599864A (zh) * 2019-09-10 2022-06-07 阿法拉伐股份有限公司 清洁排气的排气清洁系统和方法以及排气清洁系统的使用
CN111167245A (zh) * 2020-01-03 2020-05-19 北京路新沥青混凝土有限公司 一种沥青烟净化处理方法
US11124714B2 (en) 2020-02-19 2021-09-21 Marathon Petroleum Company Lp Low sulfur fuel oil blends for stability enhancement and associated methods
US11384301B2 (en) 2020-02-19 2022-07-12 Marathon Petroleum Company Lp Low sulfur fuel oil blends for stability enhancement and associated methods
US11667858B2 (en) 2020-02-19 2023-06-06 Marathon Petroleum Company Lp Low sulfur fuel oil blends for stability enhancement and associated methods
US11352578B2 (en) 2020-02-19 2022-06-07 Marathon Petroleum Company Lp Low sulfur fuel oil blends for stabtility enhancement and associated methods
US11352577B2 (en) 2020-02-19 2022-06-07 Marathon Petroleum Company Lp Low sulfur fuel oil blends for paraffinic resid stability and associated methods
US11920096B2 (en) 2020-02-19 2024-03-05 Marathon Petroleum Company Lp Low sulfur fuel oil blends for paraffinic resid stability and associated methods
US11905479B2 (en) 2020-02-19 2024-02-20 Marathon Petroleum Company Lp Low sulfur fuel oil blends for stability enhancement and associated methods
US11860069B2 (en) 2021-02-25 2024-01-02 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US11906423B2 (en) 2021-02-25 2024-02-20 Marathon Petroleum Company Lp Methods, assemblies, and controllers for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US11898109B2 (en) 2021-02-25 2024-02-13 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of hydrotreating and fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US11905468B2 (en) 2021-02-25 2024-02-20 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US11921035B2 (en) 2021-02-25 2024-03-05 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US11885739B2 (en) 2021-02-25 2024-01-30 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
WO2022234250A1 (fr) * 2021-05-05 2022-11-10 LGE IP Management Company Limited Procédé de traitement d'un flux de gaz de purge pour éliminer l'ammoniac
US11970664B2 (en) 2021-10-10 2024-04-30 Marathon Petroleum Company Lp Methods and systems for enhancing processing of hydrocarbons in a fluid catalytic cracking unit using a renewable additive
US11802257B2 (en) 2022-01-31 2023-10-31 Marathon Petroleum Company Lp Systems and methods for reducing rendered fats pour point
EP4344766A1 (fr) * 2022-09-28 2024-04-03 Valmet Technologies Oy Procédé pour minimiser la consommation d'un agent réducteur lors de l'élimination de nox

Also Published As

Publication number Publication date
SE1700273A1 (sv) 2017-11-09
SE1500177A1 (sv) 2016-10-15
SE538815C2 (sv) 2016-12-13
SE541286C2 (en) 2019-06-11

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