WO2009149603A1 - 海船排烟脱硫方法及装置 - Google Patents

海船排烟脱硫方法及装置 Download PDF

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Publication number
WO2009149603A1
WO2009149603A1 PCT/CN2008/071307 CN2008071307W WO2009149603A1 WO 2009149603 A1 WO2009149603 A1 WO 2009149603A1 CN 2008071307 W CN2008071307 W CN 2008071307W WO 2009149603 A1 WO2009149603 A1 WO 2009149603A1
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WO
WIPO (PCT)
Prior art keywords
washing
seawater
water
scrubber
flue gas
Prior art date
Application number
PCT/CN2008/071307
Other languages
English (en)
French (fr)
Inventor
彭斯干
Original Assignee
Peng Sigan
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Peng Sigan filed Critical Peng Sigan
Priority to US12/304,752 priority Critical patent/US8038774B2/en
Priority to JP2011512811A priority patent/JP2011524800A/ja
Priority to EP08757718A priority patent/EP2295130A4/en
Priority to CN200880129626.5A priority patent/CN102112210B/zh
Priority to AU2008357630A priority patent/AU2008357630B2/en
Priority to PCT/CN2008/071307 priority patent/WO2009149603A1/zh
Priority to KR1020117000968A priority patent/KR101566936B1/ko
Priority to CA2765209A priority patent/CA2765209C/en
Publication of WO2009149603A1 publication Critical patent/WO2009149603A1/zh
Priority to HK11111361.5A priority patent/HK1156898A1/zh

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Classifications

    • 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
    • B01D53/14—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 by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1481—Removing sulfur dioxide or sulfur trioxide
    • 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
    • B01D53/14—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 by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • 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
    • B01D53/507—Sulfur oxides by treating the gases with other liquids
    • 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
    • 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
    • F01N13/00—Exhaust or silencing apparatus characterised by constructional features ; Exhaust or silencing apparatus, or parts thereof, having pertinent characteristics not provided for in, or of interest apart from, groups F01N1/00 - F01N5/00, F01N9/00, F01N11/00
    • F01N13/004—Exhaust or silencing apparatus characterised by constructional features ; Exhaust or silencing apparatus, or parts thereof, having pertinent characteristics not provided for in, or of interest apart from, groups F01N1/00 - F01N5/00, F01N9/00, F01N11/00 specially adapted for marine propulsion, i.e. for receiving simultaneously engine exhaust gases and engine cooling water
    • 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
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B01D2252/1035—Sea water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • 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
    • B01D2259/00—Type of treatment
    • B01D2259/45—Gas separation or purification devices adapted for specific applications
    • B01D2259/4566—Gas separation or purification devices adapted for specific applications for use in transportation means
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/12—Improving ICE efficiencies

Definitions

  • the present invention relates to a sea vessel smoke desulfurization method and device, which utilizes seawater to remove pollutants such as sulfur dioxide emitted from marine engine engines, and belongs to the fields of atmospheric environmental protection, development and utilization of marine resources, and prevention and control technologies for ship smoke pollution.
  • BACKGROUND OF THE INVENTION The problem of reducing sulfur dioxide emissions in sea-based ships has been continuously highlighted on a global scale, and relevant international legislation has been gradually tightened and improved.
  • As a shipping industry that maintains the lifeblood of a modern global economy ships with a large number of fuel-engined engines relying entirely on low-sulfur fuels to reduce sulfur oxides will lead to a significant increase in the economic costs of the shipping industry.
  • the flue gas desulfurization process is imperative.
  • the sea-based ship's flue gas desulfurization process device can be practical, and its economic problem is more than the emission reduction of land-based coal-fired industrial facilities. Prominent, that is, the total cost of manufacturing a ship's flue gas desulfurization unit must be significantly lower than the total cost saved by replacing the low-sulfur fuel.
  • the technical solution scrubber achieves the washing function by the hollow fiber membrane contactor, and the hollow fiber membrane is only tens of degrees Celsius in temperature resistance, and cannot be applied to the engine exhaust of the engine with the smoke temperature of up to 200 ⁇ 490 °C under the condition of the scheme. Processing occasions.
  • the scrubber uses a hollow fiber membrane contactor to achieve the washing function.
  • the pressure drop and resistance are large.
  • the booster fan is added, and the energy consumption and cost of the system operation are high.
  • the amount of water required 1), absorb SOx (during washing), 2), dilute the washing water to reach pH 6.5, 3), further dilute to achieve the pH value of the environmental seawater within 0.2 units, and the dissolved oxygen concentration is reduced by less than 1 %.
  • ... will require a much larger amount of water to wash and dilute. ... Therefore, detailed case studies are needed. For example, whether it is possible to aerate the washing water and add a neutralization facility. In order to reduce the amount of water required for dilution to eliminate acidic sulfur oxides, further research is needed to determine.
  • the blending process is defined as an acute mixed zone and a chronic mixed zone. region.
  • the pH limit of the boundary of the acute mixing zone is 6.5, which is required to be reached within 15 minutes; the pH of the boundary of the chronic mixing zone is limited to 0.2 units of the pH value of the ambient seawater.
  • the literature study calculates that the engine is a 12 MW ship exhaust and desulfurization system. To meet the environmental requirements of flue gas and seawater discharge, the number of hours required on the ship is required. Thousands of tons of seawater, after the seawater is discharged from the ship, it needs to continue to be diluted and further mixed with not less than 40,000 times of environmental seawater.
  • the research described in this document has not yet proposed a technical solution for a practical process and apparatus.
  • the scrubber (US7056367) adopts the "exhaust gas into the pool washing liquid", that is, the bubbling washing method, and the cooling and washing absorption of the high-temperature flue gas is simultaneously The same pool of water bears, the mass transfer efficiency is very low, and the cooling and absorption are contradictory. To increase the absorption rate, only increasing the amount of washing water and increasing the pressure loss will result in a significant increase in energy consumption and operating costs. Obviously, the seawater washing process system and apparatus using the scrubber have the disadvantages of cooling the high temperature flue gas and low temperature absorbing sulfur dioxide, and the contradiction between the washing effect and the cost reduction.
  • the first object of the present invention is to overcome the shortcomings of the existing sea-ship smoke desulfurization method, and to provide a high desulfurization efficiency, a small amount of seawater used for washing and dilution, low energy consumption and low cost, and is suitable for use in different Sea area, control area sailing mobile sea boat smoke desulfurization method.
  • Another object of the present invention is to overcome the shortcomings of the existing sea-ship smoke desulfurization device, and provide a high desulfurization efficiency, a small amount of washing and diluting seawater, low equipment manufacturing and operation cost, small volume, long service life, and suitable for A sea-ship smoke desulfurization device with a small space and a large navigation range.
  • the technical proposal of the sea vessel flue gas desulfurization method of the invention comprises the following steps:
  • washing cooling the high temperature flue gas containing S0 2 discharged from the engine of the ship, and then discharging the purified flue gas; the washing is washing with seawater in the scrubber;
  • Acid removal treatment Incorporate alkaline seawater into the acidic seawater entering the water-saving acid remover to make it into mixed seawater, and inject air into the mixed seawater;
  • Drainage Discharge the dehydrated seawater into the sea.
  • the sea vessel flue gas desulfurization method in which the washing step is washed with seawater in a scrubber, is carried out in a scrubber having a packed washing layer.
  • the sea vessel flue gas desulfurization method, the alkaline seawater mixed into the water-saving acid remover in the acid removal step, the flow rate is regulated by a regulator, and the regulator is adjusted by the opening degree
  • the valve or / and the output of the adjustable pump can be adjusted; the air blown into the mixed seawater in the water-saving acid remover, the flow rate of which is regulated by the regulator, the regulator is adjusted, the valve can be adjusted by the opening degree, The baffle or / and the output of the fan can be adjusted.
  • the regulator adjustment is controlled by an artificial or/and desulfurization controller according to the environmental requirements of the flue gas and seawater discharge in the sea area where the ship is located.
  • there is a step of separating impurities between the washing step and the acid removing treatment step wherein the separator is used to separate the impurities and the separated impurities are discharged through the sewage pipe.
  • the marine ship flue gas desulfurization device used in the sea vessel flue gas desulfurization method of the present invention has the technical proposal that: it comprises a scrubber, a water-saving acid remover; the scrubber, the upper part of which is a washing layer, and washing
  • the sea water pump is connected through the pipeline; the lower part is the cooling layer; one end of the scrubber is connected with the exhaust pipe of the engine of the ship through the washing intake pipe, and the other end is connected with the washing exhaust pipe; the lower part of the scrubber is connected with the water-saving acid remover;
  • the degreaser is connected to the mixed sea water pump, the fan and the acid-treated total drain pipe.
  • the marine vessel flue gas desulfurization device has a water-saving acid remover incorporated into an alkaline seawater channel, and the channel is provided with an alkaline seawater flow regulator, which is selected from a valve or/and a force that can be adjusted at an opening degree.
  • the water-saving acid remover has an air injection passage, and the passage is provided with an air flow regulator, which is selected from a valve, a baffle or/and a fan whose output can be adjusted.
  • the scrubber has a washing seawater injection passage, and the passage is provided with a washing seawater flow regulator, which is selected from a valve capable of adjusting the opening degree or a pump capable of adjusting the output.
  • the sea vessel flue gas desulfurization device has a control rod disposed on a valve and a baffle, and a motor governor is disposed on the pump and the fan; the control rod, the motor governor and the desulfurization controller are connection.
  • the scrubber comprises a casing, a cooling layer, a packing washing layer, and a sump; wherein the cooling layer is below the packing washing layer.
  • the marine vessel flue gas desulfurization device includes a desulfurization controller including a commander, a sensor, a central processing unit, an actuator, and a global sea area locator.
  • the technical principle and comprehensive technical effects of the sea vessel flue gas desulfurization method and the sea vessel flue gas desulfurization device of the present invention are as follows:
  • the strong dissolved and absorbed capacity of seawater requires a strong mass transfer capability to transport pollutants from the exhaust gas to the seawater liquid.
  • the smoke temperature of a marine diesel engine may be as high as 490 ° C. Whether it is to absorb the sulfur dioxide in the washing or to protect the process equipment, the high temperature flue gas must be cooled before entering the washing.
  • the washing process of the method of the present invention uses a countercurrent packing washing, and an efficient method and apparatus for cooling and washing, wherein the washing liquid is seawater, the washing functional zone is composed of a packing layer, and the washing liquid sea water is uniformly distributed by the water distributor.
  • the top-down rinsing agent is distributed, and the high-temperature gas for exhausting smoke is first cooled, and then passes through the packing layer from bottom to top.
  • the washing water passes through the packing layer from top to bottom. Due to the large surface area formed by the filler, it is between gas and liquid. Providing a huge contact area, which has a strong mass transfer capacity and washing absorption efficiency, can achieve the purpose of efficient emission reduction.
  • the filling technology scheme can significantly reduce the resistance to passing gas, and ensure the technical and economic performance of achieving efficient absorption washing while reducing the operating cost of the process device.
  • the present invention reduces the amount of dilution water required by adding a water-saving acid remover.
  • Sulfur dioxide is dissolved in the washed seawater to form an acidic substance such as sulfite, and is mixed with fresh alkaline seawater to form an acidic substance such as carbonic acid. Therefore, the pH of the simple dilution method rises slowly, and the amount of dilution water required is large.
  • the invention adopts the flow regulation of the mixed seawater for washing the seawater and the water-saving acid remover, and adjusts the air volume of the air spurted by the water-saving acid remover, and includes The controller of the central processor controls the above adjustments to adapt the flue gas desulfurization method and device to the needs of the voyage of the marine vessel.
  • the sea vessel smoke desulfurization method and the sea boat smoke desulfurization device performance index comply with environmental protection regulations, and the technical effects thereof are remarkable:
  • the high efficiency of abatement can achieve the technical effect of reducing sulfur oxide by 99%, reducing nitrogen oxide by 20% and reducing particulate matter by 80%. This is particularly important for the international maritime industry to achieve its environmental goals: IMO has defined SECA (sulfur oxide emission control zone) in 2005.
  • SECA sulfur oxide emission control zone
  • the fuel used in ships must not exceed 1.5%, or install flue gas desulfurization equipment to discharge
  • the flue gas is equivalent to the sulfur emission when the sulfur content of the fuel does not exceed 1.5%, that is, the "sulphur content of the desulfurization equivalent fuel” does not exceed 1.5; and the international organization is committed to promoting the goal of reducing the sulfur content of the fuel to 0.1%.
  • the average sulfur content of heavy oil in the world is close to 3%.
  • the required washing efficiency is 50%, and to achieve the desulfurization equivalent fuel sulfur content of 0.1%, the required washing efficiency is 96.7 %.
  • the ship is environmentally friendly.
  • the wash water discharged by the EPA and IMO regulations must have a pH of 6.5 in the boundary of the acute mixing zone within 15 minutes. Since the drainage pH of the method and device of the present invention reaches 6.5 from the ship to the sea area, the acute mixing zone is not needed, and the first step eliminates the adverse effect on the marine environment for 15 minutes.
  • the dilution ratio in the chronic mixing zone can be From 1:40000 to 1:2000, that is, only one-twentieth of the existing technology seawater mixing is required, the scope of the chronic mixing zone is greatly reduced, and the friendliness of ship drainage and environment is greatly improved.
  • 1 is a schematic view of a method and apparatus for de-sulfurization of a sea-going vessel of the present invention.
  • This embodiment has a desulfurization controller.
  • 2 is a schematic view showing still another embodiment of the method and apparatus for exhausting flue gas desulfurization of the marine vessel of the present invention.
  • the scrubber 3 has a bypass exhaust pipe, that is, a smoke exhaust pipe in which the ship engine 1 and the washing exhaust pipe 4 are directly connected, which facilitates switching of the scrubber 3.
  • Figure 3 is a schematic view showing the structure of an embodiment of the scrubber 3 in the sea-ship exhaust gas desulfurization apparatus of the present invention:
  • the high-temperature flue gas 3.2 introduced from the lower portion of the scrubber 3 by the intake pipe 3.1 is suitable for the implementation of the flue gas vertically entering the scrubber occasion.
  • FIG. 4 is a schematic structural view of still another embodiment of the scrubber 3 in the marine vessel flue gas desulfurization apparatus of the present invention:
  • the high temperature flue gas 3.2 introduced from the lower side wall of the scrubber 3 by the intake pipe 3.1 is suitable for the flue gas laterally entering the scrubber Then the smoke is applied upwards.
  • FIG. 5 is a block diagram showing the flow of the desulfurization controller of the marine vessel flue gas desulfurization device of the present invention.
  • FIG. 6 is a schematic diagram of a prior art "EcoSilencer sea water scrubbing system", the scrubber adopts the technical solution of US Pat. No. 7,065,367, including: a coaxially embedded intake duct, a heat pipe, and a discharge pipe, a reverse-passing exhaust gas, a water tank for loading the washing liquid; a heat pipe end and an outlet pipe are connected to each other and immersed in the washing liquid of the water tank, the heat pipe has a star-shaped cross section, and the heat transfer area is increased to make more The heat is then reheated and the target is to raise the exhaust temperature by at least 30 V above the dew point.
  • Figure 1 Figure 2: 1-ship engine, 2-wash intake manifold, 3-washer; Figure 3, Figure 4: 3.1-shell, 3.2-cooling layer, 3.3-filler wash layer, 3.4-flue Import, 3.5--discharge clean flue gas, 3.6-washing seawater inlet pipe, 3.7-collection tank; Figure 1, Figure 2: 4-washing exhaust pipe, 5-washing seawater pump, 6-washing speed regulating motor, 7-separator, 8-separator drain pipe, 9-blended sea water pump, 10-water acid remover, 11-fan, 12-exhaust pipe, 13-total water inlet pipe, 14-total drain pipe, 15 - Desulfurization controller; Figure 5: 15.1 - Commander, 15.2 - Sensor, 15.3 - Central Processing Unit, 15.4-Actuator, 15.5 - Global Sea Area Locator.
  • Figure 6 16.1 Washing and reheating the exhaust gas, 16.2 Washing gas reheating zone, 16.3 Mixing the exhaust gas and seawater in the scrubber, 16.4 seawater entering, 16.5 seawater discharging to the separator and heat exchanger, 16.6 exhaust gas, 16.7 separation and filtration Installation, 16.8 discharge of clean water, 16.9 discharge of sludge. detailed description
  • sea vessel smoke desulfurization method and the sea vessel smoke desulfurization device of the present invention are further described as follows with reference to the accompanying drawings and embodiments:
  • Example 1 As shown in Fig. 1, there is a desulfurization controller.
  • the steps of the sea vessel flue gas desulfurization method of the present embodiment are as follows: a. washing: the high temperature flue gas containing 30 2 discharged from the engine of the ship is cooled and then washed, and then the flue gas after washing and purging is discharged; the washing is in Washing with seawater in the scrubber; b, transferring out acidic seawater: transferring the acidic seawater formed by S0 2 from the scrubber to the water-saving acid remover in the washing process; c.
  • removing acid treatment removing water into the water
  • the acidic seawater of the acidifier is mixed with alkaline seawater to make it into mixed seawater, and the mixed seawater is blown into the air;
  • Drainage discharges the acid-treated seawater into the sea area;
  • the scrubber is washed with sea water and is washed in a scrubber having a packed wash layer;
  • the acid removal process in the acid removal process of the present invention The alkaline seawater is mixed, and the flow rate is regulated by a regulator.
  • the regulator is adjusted by a pump that can be adjusted by the output force, or can be adjusted by a valve whose opening degree can be adjusted, or can be adjusted by opening degree.
  • the adjusted valve and the pump whose output can be adjusted are adjusted; the air that is blown into the mixed seawater in the water-saving acid remover is regulated by the regulator, and the regulator is adjusted by the fan that can be adjusted by the output force, It can be selected as valve adjustment with adjustable opening, or baffle adjustment, and can also be selected as valve and fan adjustment, or baffle and fan adjustment; the washing water used in the washing step, the flow rate is regulated by the regulator; The regulator is adjusted by the pump that can be adjusted by the output force. It can also be adjusted by the valve that can be adjusted by the opening degree.
  • Adjustable valve and pump adjustment with adjustable output is that the desulfurization controller controls the adjustment according to the environmental requirements of the flue gas and seawater discharge in the sea area where the ship is located; manual manual control adjustment is another embodiment; There is a step of separating impurities between the washing step and the acid removing step, in which the separator is used to separate the impurities and the separated impurities are discharged through the drain pipe.
  • the ship used in this embodiment is equipped with a 12 MW diesel engine with a discharge temperature of 200 490 V and a flue gas emission of about 67,095 Nm 3 /h.
  • the desulfurization method of the present invention is implemented to reduce emissions under the condition of 3% sulfur content of the fuel.
  • the sulfur dioxide to desulfurization equivalent fuel has a sulfur content of 0.1% and a drainage pH of 6.5.
  • the seawater consumption in different sea areas is: The amount of seawater washed in the Baltic Sea is 300m 3 /h The amount of seawater mixed is 1100m 3 /h
  • the amount of seawater washed in the North Sea is 280m 3 /h.
  • the amount of seawater mixed is 950m 3 /h.
  • Embodiment 2 As shown in FIG. 2, this embodiment differs from Embodiment 1 in that the scrubber 3 has a parallel bypass exhaust pipe, that is, a smoke exhaust pipe in which the ship engine 1 and the washing exhaust pipe 4 are directly connected, which is convenient. Switch the scrubber 3.
  • the desulfurization control is manually controlled manually.
  • the ship used in this embodiment has a large tonnage and is equipped with a 60 MW diesel engine.
  • the exhaust smoke temperature is 200 430 ° C, and the exhaust gas volume is about 310,100 Nm 3 /h.
  • the desulfurization method of the present invention is implemented, and the fuel sulfur content is 3%. Under the conditions, the sulfur content of sulfur dioxide to desulfurization equivalent fuel meets the CSCA control standard (2005) 1.5%, the drainage pH 6.5, the seawater consumption in different sea areas is:
  • the amount of seawater washed in the Baltic Sea is 980m 3 /h.
  • the amount of seawater mixed is 3600m 3 /h.
  • the amount of seawater washed in the Pacific Ocean is 880m 3 /h.
  • the amount of seawater mixed is 2600m 3 /h.
  • FIG. 1 and FIG. 3 there is a sea vessel flue gas desulfurization device used in the method of the present invention.
  • the intake pipe 3.1 of the scrubber 3 is introduced from the lower portion of the scrubber 3 with high temperature flue gas 3.2, which is suitable for vertical gas flow. Go up into the implementation of the scrubber.
  • a sea vessel flue gas desulfurization device which has a scrubber 3, a water-saving acid remover 10; the scrubber 3, the upper part of which is a washing layer 3.3, communicates with the washing sea water pump 5 through a pipeline; the lower part is a cooling layer 3.2; one end of the scrubber 3 is connected to the exhaust pipe of the engine 1 of the ship through the washing intake pipe 2, and the other end is connected with the washing exhaust pipe 4; the lower part of the scrubber 3 is connected with the water-saving acid remover 10; the water-saving acid remover 10 is connected with the mixed sea water pump 9, the fan 11 and the acid-treated total drainage pipe 14; the water-saving acid remover 10 is mixed with an alkaline seawater channel, and the channel is provided with an alkaline seawater flow regulation
  • the utility model is a pump capable of adjusting the output, a valve capable of adjusting the opening degree, a valve and a pump capable of adjusting the output at the same time; the water-saving acid remover 10 has an air injection passage, and the passage
  • the scrubber 3 has a washing seawater injection
  • the passage is provided with a washing seawater flow regulator, which is a pump capable of regulating the output, or a valve whose opening degree can be adjusted, or a valve and a pump capable of adjusting the output at the same time;
  • the above-mentioned valve and baffle are resistant a control lever is disposed, the pump and the fan are provided with a motor governor;
  • the control rod and the motor governor are connected with the desulfurization controller 15;
  • the scrubber 3 comprises a housing 3.1, a cooling layer 3.2, a packing washing layer 3.3, a sump 3.7; wherein, the cooling layer 3.2 is below the packing washing layer 3.3; a separator 7 for separating impurities is installed between the scrubber 3 and the water-saving acid remover 10;
  • FIG. 2 and FIG. 4 it is another sea vessel smoke desulfurization device used in the method of the present invention, and the above implementation The difference is that the high-temperature flue gas enters the scrubber 3 from the lateral flue gas inlet 3.4 horizontal direction, and is suitable for the occasion where the flue gas flows into the scrubber laterally, and then the flue gas flows upward.
  • the desulfurization control adjustment is manual operation.

Description

海船排烟脱硫方法及装置
技术领域 本发明涉及一种海船排烟脱硫方法及装置，是利用海水来脱除海运船舶发动机排放 的二氧化硫等污染物， 属于大气环境保护、 海洋资源开发利用和船舶烟气污染防治技术 领域。 背景技术 海基船舶二氧化硫减排问题在全球范围内被不断突出，相关国际立法逐步严格和完 善。 作为维系现代全球化经济命脉的航运业， 拥有大量安装燃油发动机的船舶， 完全依 靠低硫燃料来实现减排硫氧化物将导致航运业经济成本的大幅提升， 因此， 为船舶提供 经济实用的排烟脱硫工艺势在必行。
在烟温高达 200~490°C并处于不同海区间航行移动的状态下， 海基船舶的排烟脱硫 工艺装置能否实用， 其经济性问题比陆基燃煤工业设施的减排显得更为突出， 即船舶排 烟脱硫装置制造运行的总成本， 必须显著低于替代低硫燃料所节省的总成本。
因此， 在 2005年 IMO (国际海事组织） 提出船舶二氧化硫减排规则后， 很快就出 现了看重具有潜在经济性优势的海水法排烟脱硫技术的趋势。 2007年， 四所国际著名大 学联合研究的结论清晰表达出： 利用海洋资源即海水实现船舶二氧化硫减排， 是人们长 期以来迫切希望实现而未能实现的期待。
美国麻省理工学院（Massachusetts Institute of Technology )、日本东京大学（Univeristy of Tokyo) 、 瑞典查尔墨科技大学 （Chalmers University of Technology) 、 瑞士联邦苏黎 世工业学院（Swiss Federal Institute of Technology Zurich)四所大学联合基金会的一份名 为 "海水洗涤-减少从船舶废气排放的 SOx"的研究报告 （ISBN: 978-91-976534-1-1 ) 指 出： "海水洗涤， 对于减少从船舶排放的硫氧化物， 是一种很有前途的技术。 ……还需 要进行详细的案例研究。 ……需要进一步的研究才能确定" 。
目前， 以海水洗涤减少船舶排烟污染的现有技术有： 1、 2008年 1月 16日公开的中国专利申请号为 200710012371.1 , 名称为 "一种对船 舶尾气进行海水洗涤处理的装置和方法"， 在作为洗涤器的中空纤维膜接触器内， 对经 过除尘预处理的船舶尾气进行海水洗涤处理， 由 S02浓度监测仪、水质监测仪和 PLC可 编程控制器组成的控制系统， 实现对处理后的船舶尾气中的 S02浓度、 废水水质的实时 检测和存储以及对排水的控制。 该技术存在下述问题：
1 ) 该技术方案洗涤器以中空纤维膜接触器实现洗涤功能， 而中空纤维膜耐温仅为 数十摄氏度， 在该方案条件下不能应用于烟温高达 200~490°C的船舶发动机排烟处理场 合.
2) 同时， 洗涤器以中空纤维膜接触器实现洗涤功能， 压降和阻力很大， 增设增压 风机， 系统运行的能耗和成本很高。
2、 美国 2007年文献。 题为 "海水洗涤一减少从船舶废气排放的 SOx"的研究报告 (ISBN: 978-91-976534-1-1 ) ： "海水洗涤， 对于减少从船舶排放的硫氧化物， 是一种 很有前途的技术。 该文以 12兆瓦发动机， 燃烧 3 %的含硫量燃料作为计算基础， 进行 船用海水洗涤的海洋化学分析， 得到了不同脱硫效率， 不同水温时， 6个不同类型的水 域所需要的水量： 1 ) 、 吸收 SOx (洗涤过程中） ， 2) 、 稀释洗涤水以达到 pH值 6.5 ， 3) 、 进一步稀释以达到环境海水的 pH值 0.2单位以内， 溶解氧浓度减少不超过 1 %。 为保持一定的洗涤效率， ……将需要大得多的水量来洗涤及稀释。 ……因此， 还需要进 行详细的案例研究。例如， 是否可以通过对洗涤水曝气和加入中和设施以消除酸性硫氧 化物的方式， 来减少稀释所需要的水量， 都还需要进一步的研究才能确定" 。
该文献是目前研究以海水洗涤方式减排海洋船舶二氧化硫的代表性文献，该研究尚 处于工艺原理探索阶段，所面临的吸收效率低和稀释水量大的问题还有待进一步研究解 决。 为防止由于排水对环境的损害， 美国国家环保局 （EPA) 和国际海事组织 （IMO) 已经通过法规， 规范洗涤排放水与环境海水的混合： 混和过程界定为急性混合区和慢性 混合区两个区域。 急性混合区边界 pH值限值为 6.5， 要求在 15分钟内达到； 慢性混合 区边界 pH值限定为环境海水 pH值的 0.2单位以内。 该文献研究计算的发动机为 12兆 瓦的船舶排烟脱硫系统， 要满足烟气和海水排放的环保要求， 船舶上需要提供每小时数 千吨海水， 海水排出船舶后还需继续稀释， 与不少于 40000倍的环境海水进一步混合。 该文献所述的研究目前尚未提出实用工艺和装置的技术方案。
3、 加拿大文献， 2006年 2月， 艾克赛勒废气清洁介绍 （EcoSilencer Exhaust Gas Cleaning Presentation)。文献对 EcoSilencer方式的海水洗涤工艺系统和装置进行介绍（附 图 5 ) ， 该工艺装置截至 2006年经过 6年多试验， 其核心部件洗涤器采用美国专利号 US7056367 , 名称为 "利用混合叶片洗涤气体的方法和装置" （附图 4) 的发明专利技 术方案。
由于船舶发动机排放的高温烟气必须冷却才能吸收其中的二氧化硫， 该洗涤器 (US7056367 ) 采用 "排气通入水池洗涤液中" 即鼓泡洗涤方式， 对高温烟气的冷却和 洗涤吸收同时由同一池水体承担， 传质效率很低， 而且降温和吸收相互矛盾。 要提高吸 收率， 唯有加大洗涤水量和加大压力损失， 将导致能耗和运行成本大幅增加。 显然， 采 用该洗涤器的海水洗涤工艺系统和装置， 目前存在冷却高温烟气和低温吸收二氧化硫相 互矛盾， 以及洗涤效果和降低成本相互矛盾等不足。
综上， 现有研究和试验技术进入实用领域面临的共同问题主要是：
1 ) 、 在目前可以接受的成本条件下， 尚难以满足烟气排放和海水排放的环境要求; 按目前限制的排水条件要求， 耗用的洗涤水量和稀释水量大， 能耗和成本高； 今后如进 一步提高排水条件要求， 其成本还将进一步上升。
2) 、 不适应船舶航行移动， 各不同海区、 不同控制区的各项环境条件和控制条件 不同， 海运船舶在不同的海区和控制区之间航行， 所处的环境条件在不断变化， 如： 海 水水质、 不同批次燃油含硫量、 不同环境的排放限制条件等等， 工艺参数固定不变的排 烟脱硫系统将不能实际应用于海运船舶。
显然， 以上问题如不解决， 人们期待的利用海洋资源消除船舶大气污染的愿望就无 法实现。 发明内容 随着船舶减排二氧化硫的国际立法日趋严格和完善，要实现利用海洋资源消除船舶 大气污染的愿望， 就需要提出利用海水减排二氧化硫的实用海船排烟脱硫方法和装置。 本发明的第一个目的在于， 克服现有海船排烟脱硫方法存在的缺点， 提供一种脱硫 效率高、 用于洗涤和稀释的海水用量少、 能耗和成本低， 适用于在不同海区、 控制区间 航行移动的海船排烟脱硫方法。
本发明的另一个目的在于， 克服现有海船排烟脱硫装置存在的缺点， 提供一种脱硫 效率高、 洗涤和稀释海水用量小、 设备制造和运行成本低、 体积小， 寿命长， 适用于可 用空间小、 航行范围大的海船排烟脱硫装置。
本发明的海船排烟脱硫方法的技术方案， 包括下述步骤：
a、 洗涤： 将船舶发动机排出的含有 S02的高温烟气冷却后进行洗涤， 然后将洗涤 净化后的烟气排放； 所述的洗涤是在洗涤器中用海水洗涤；
b、 转出酸性海水： 将洗涤过程吸收了 S02形成的酸性海水从洗涤器内转出到省水 除酸器中；
c、 除酸处理： 向进入省水除酸器的酸性海水中掺入碱性海水， 使成为混合海水， 并对混合海水鼓入空气；
d、 排水： 将经过除酸处理的适排海水排放至海域。
在上述海船排烟脱硫方法技术方案基础上，具有附加技术特征的更进一步技术方案 是：
所述的海船排烟脱硫方法， 其洗涤步骤中的在洗涤器中用海水洗涤， 是在具有填料 洗涤层的洗涤器中进行洗涤。
所述的海船排烟脱硫方法， 其除酸处理步骤中向省水除酸器中掺入的碱性海水， 其 流量由调节器调节，所述的调节器调节，是通过开度能够调节的阀门或 /和出力能够调节 的泵调节； 对省水除酸器中的混合海水鼓入的空气， 其流量由调节器调节， 所述的调节 器调节， 是通过开度能够调节的阀门、 挡板或 /和出力能够调节的风机调节。
所述的海船排烟脱硫方法， 其洗涤步骤中所用的洗涤海水， 其流量由调节器调节； 所述的调节器调节， 是通过开度能够调节的阀门或 /和出力能够调节的泵调节。
所述的海船排烟脱硫方法，其调节器调节是由人工或 /和脱硫控制器根据船舶所在海 区的烟气和海水排放的环境要求控制调节。 所述的海船排烟脱硫方法， 其洗涤步骤与除酸处理步骤之间有一个分离杂质步骤， 是用分离器分离杂质并将所分离出的杂质经排污管排出。
用于本发明的上述海船排烟脱硫方法的海船排烟脱硫装置， 其技术方案是： 它包括 洗涤器， 省水除酸器； 所述的洗涤器， 其上部为洗涤层， 与洗涤海水泵通过管道连通； 下部为冷却层； 洗涤器的一端与船舶发动机的排烟管通过洗涤进气管连通， 另一端连接 有洗涤排气管； 洗涤器下部与省水除酸器连通； 省水除酸器与掺混海水泵、 风机以及经 除酸处理后的适排海水总排水管连接。
在上述海船排烟脱硫装置技术方案基础上，具有附加技术特征的更进一步技术方案 是：
所述的海船排烟脱硫装置， 其省水除酸器有掺入碱性海水通道， 该通道设置有碱性 海水流量调节器，选自于开度能够调节的阀门或 /和出力能够调节的泵；省水除酸器有空 气注入通道， 该通道设置有空气流量调节器， 选自于开度能够调节的阀门、挡板或 /和出 力能够调节的风机。
所述的海船排烟脱硫装置， 其洗涤器有洗涤海水注入通道， 该通道设置有洗涤海水 流量调节器， 选自于开度能够调节的阀门或 /和出力能够调节的泵。
所述的海船排烟脱硫装置， 其阀门、 挡板上设置有控制杆， 所述的泵和风机上设置 有电机调速器； 所述的控制杆、 电机调速器与脱硫控制器相连接。
所述的海船排烟脱硫装置， 其洗涤器包括壳体， 冷却层， 填料洗涤层， 集液池； 其 中， 冷却层在填料洗涤层的下方。
所述的海船排烟脱硫装置， 其洗涤器与省水除酸器之间安装一分离杂质的分离器。 所述的海船排烟脱硫装置， 其脱硫控制器包括有指令器、 传感器、 中央处理器、 执 行器和全球海区定位器。
本发明海船排烟脱硫方法、 海船排烟脱硫装置的技术原理和综合技术效果是： 技术原理： 海船排烟脱硫方法和装置的主要功能和需要解决的问题是洗涤吸收、 排 水处理和航行移动三个方面。
1 ) 、 洗涤吸收， 为脱除海船燃油发动机排烟气体中的二氧化硫等污染物， 以海水 洗涤净化烟气； 海水因其物理化学性质对二氧化硫有很强的溶解吸收能力， 同时还可以 良好洗涤吸收氮氧化物和颗粒物， 但由于海船的可用空间狭小， 作为船舶的实用工艺方 法和实用工业装置， 排烟脱硫装置的尺寸相应短小， 处理时间必然很短， 上述吸收和洗 涤必须在很短时间内完成。 也就是说工艺装置不仅要有很高的总吸收率， 而且必须要具 备很高的吸收速率， 吸收和洗涤的效率必须很高。 因此， 海水强大的溶解吸收能力， 需 要有从排烟气体向海水液体输送污染物质的强大传质能力相匹配。 另一方面， 船舶柴油 机排放烟温有可能高达 490°C， 不论是为吸收洗涤其中的二氧化硫， 还是为保护工艺装 置， 高温烟气都必须在进入洗涤之前加以冷却。 为此， 本发明方法的洗涤工序， 采用逆 流式填料洗涤， 和冷却、 洗涤分段进行的高效方法和装置， 其洗涤液采用海水， 洗涤功 能区由填料层组成， 洗涤液海水由水分配器均匀分布自上而下淋洗填料， 排烟的高温气 体先经过冷却， 再自下而上经过填料层， 洗涤海水则自上而下经过填料层， 由于填料形 成的巨大表面积， 为气体和液体间提供了巨大的接触面积， 从而具有强大的传质能力和 洗涤吸收效率， 可以实现高效减排的发明目的。 同时， 采用填料技术方案可以显著减小 对通过气体的阻力，保证实现高效吸收洗涤的同时降低工艺装置运行成本的技术经济性 能。
2) 、 排水处理。 洗涤并溶入了二氧化硫的海水呈酸性， 需要进行处理以提升其 pH 后才能排放到自然海域。 为克服现有技术单纯稀释方式耗用稀释水量大， 对应能耗和成 本高的缺点， 本发明采用加入省水除酸器的方法减少所需的稀释水量。 二氧化硫溶入洗 涤海水中生成亚硫酸根等酸性物质，掺入新鲜的碱性海水后生成碳酸等酸性物质，因此， 单纯稀释方式的 pH值上升缓慢， 所需的稀释水量大。 本发明在加入的省水除酸器中， 一边掺入新鲜的碱性海水， 一边鼓入空气， 使碳酸很快挥发， 洗涤海水的 pH上升迅速， 所需的稀释水量大为减少。
3) 、 移动调整。 海运船舶经常航行移动于不同海域， 其面临不同海域的海水水质、 不同批次燃油含硫量、 不同环境的排放限制条件等等都在不断变化。 因此， 工艺参数指 标固定不变的脱硫工艺系统将无法实用于海运船舶。本发明采用对洗涤海水、 省水除酸 器的混合海水进行流量调节， 对省水除酸器鼓入的空气进行风量调节， 以及用包括有中 央处理器的控制器对以上调节加以控制的方式，使排烟脱硫方法和装置适应海运船舶不 断航行移动的需要。
本发明海船排烟脱硫方法、海船排烟脱硫装置性能指标符合环保法规， 其技术效果 显著：
其一， 减排效率高， 可以实现减少硫氧化物 99%， 减少氮氧化物 20%和减少颗粒 物 80%的技术效果。 这对于国际海运业实现其环境目标具有特别重要的意义： IMO于 2005年已限定 SECA (硫氧化物排放控制区） 船舶使用的燃油含硫量不得超过 1.5%， 或安装烟气脱硫设备使排放烟气等效于燃油含硫量不超过 1.5 %时的硫排放量， 即 "脱 硫等效燃油含硫量"不超过 1.5 ；还有国际组织致力推动实现将燃油硫含量减少到 0.1 %的目标。 目前全球重油的平均硫含量接近 3 %， 要实现脱硫等效燃油含硫量 1.5 % , 需要的洗涤效率为 50 % ，而要实现脱硫等效燃油含硫量 0.1 %， 所 需 要 的 洗 涤 效 率为 96.7 % 。
其二， 有实施例表明： 适于在不同海域间的航行移动时， 海水水质、 燃油含硫量、 环境的排放限制条件等因素不断变化的场合下， 都能确保其优良的减排效果和环保性 能。
其三， 船舶排水环境友好。 如前所述， 为防止和减少船舶排水对海洋环境的损害， EPA和 IMO规范船舶排放的洗涤水必须在 15分钟内使急性混合区边界 pH值达到 6.5。 由于本发明方法和装置的排水 pH值达到 6.5才从船舶排放到海域， 所以无需急性混合 区， 第一步就消除了对海洋环境 15分钟的不良影响， 其次， 在慢性混合区内稀释倍率 可以从 1:40000下降到 1:2000， 也就是仅需现有技术二十分之一的环境海水混合， 慢性 混合区的范围大为縮小， 船舶排水和环境间的友好性得到大幅度提升。
其四， 大幅度降低制造和运行成本， 包括减少运行能耗和海水量， 从而确保实现总 成本显著低于替代低硫燃料所节省的总成本的优良技术经济指标。 附图说明
图 1、 是本发明海船排烟脱硫方法及装置的示意图。 本实施例具有脱硫控制器。 图 2、 是本发明海船排烟脱硫方法及装置的又一实施例示意图。 本实施例没有脱硫 控制器，洗涤器 3有旁路排烟管，即船舶发动机 1与洗涤排气管 4有直接联通的排烟管， 便于切换洗涤器 3。
图 3、 是本发明海船排烟脱硫装置中的洗涤器 3的一个实施例结构示意图： 进气管 3.1从洗涤器 3下部导入的高温烟气 3.2， 适用于烟气垂直向上进入洗涤器的实施场合。
图 4、 是本发明海船排烟脱硫装置中的洗涤器 3的又一个实施例结构示意图： 进气 管 3.1从洗涤器 3下部侧壁导入的高温烟气 3.2，适用于烟气横向进入洗涤器，然后烟气 向上的实施场合。
图 5、 是本发明海船排烟脱硫装置的脱硫控制器流程方框示意图。
图 6、是现有技术"艾克赛勒海水洗涤系统" (EcoSilencer sea water scrubbing system ) 示意图， 其洗涤器采用美国 US7056367号专利技术方案， 包括： 同轴嵌入的进气导管、 热导管， 和排出管道， 逆向通过的排气， 装载洗涤液的水箱； 其热导管的末端和出口导 管相互联通并沉浸在水箱的洗涤液内， 热导管具有星形截面， 加大其导热面积以使更多 的热量再加热排气， 目标是提升排气温度超过露点至少 30 V。
附图中所示的图号标记对应的相关部件或结构的名称为：
图 1、 图 2中： 1-船舶发动机， 2-洗涤进气管， 3-洗涤器； 图 3、 图 4中： 3.1-壳体， 3.2-冷却层， 3.3-填料洗涤层， 3.4-烟气进口， 3.5--排出干净烟气， 3.6-洗涤海水入口管， 3.7-集液池； 图 1、 图 2中： 4-洗涤排气管， 5-洗涤海水泵， 6-洗涤调速电机， 7-分离器， 8-分离器排污管， 9-掺混海水泵， 10-省水除酸器， 11-风机， 12-排气管， 13-总进水管， 14-总排水管， 15-脱硫控制器; 图 5中： 15.1-指令器， 15.2-传感器， 15.3-中央处理器， 15.4-执行器， 15.5-全球海区定位器。 图 6中： 16.1洗涤并再加热废气， 16.2洗涤气体再 热区， 16.3洗涤器内混合排气和海水， 16.4海水进入， 16.5海水排往分离器和换热器， 16.6废气， 16.7分离和过滤装置， 16.8排放清洁水， 16.9排放污泥。 具体实施方式
结合附图和实施例对本发明海船排烟脱硫方法、海船排烟脱硫装置作进一步说明如 下： A: 对本发明海船排烟脱硫方法作进一步说明如下：
实施例 1 : 如图 1所示， 具有脱硫控制器。本实施例的海船排烟脱硫方法步骤如下： a、 洗涤： 将船舶发动机排出的含有 302的高温烟气冷却后进行洗涤， 然后将洗涤 净化后的烟气排放； 所述的洗涤是在洗涤器中用海水洗涤； b、 转出酸性海水： 将洗涤 过程吸收了 S02形成的酸性海水从洗涤器内转出到省水除酸器中； c、 除酸处理： 向进 入省水除酸器的酸性海水中掺入碱性海水， 使成为混合海水， 并对混合海水鼓入空气； d、 排水： 将经过除酸处理的适排海水排放至海域； 所述的洗涤步骤中的在洗涤器中用 海水洗涤， 是在具有填料洗涤层的洗涤器中进行洗涤；
为了适应船舶航行移动中海域的条件变化、不同批次燃油含硫量的差异以及排烟和 排水要符合不同国家和地区的排放限制环境要求，本发明除酸处理步骤中向省水除酸器 中掺入的碱性海水， 其流量由调节器调节， 所述的调节器调节， 是通过出力能够调节的 泵调节， 也可以选为开度能够调节的阀门调节， 还可以是通过开度能够调节的阀门和出 力能够调节的泵调节； 对省水除酸器中的混合海水鼓入的空气， 其流量由调节器调节， 所述的调节器调节， 是通过出力能够调节的风机调节， 也可以选为开度能够调节的阀门 调节， 或挡板调节， 还可以选为阀门和风机调节， 或挡板和风机调节； 洗涤步骤中所用 的洗涤海水，其流量由调节器调节；所述的调节器调节，是通过出力能够调节的泵调节， 也可以通过开度能够调节的阀门调节，还可以通过开度能够调节的阀门和出力能够调节 的泵调节；所述的调节器调节是脱硫控制器根据船舶所在海区的烟气和海水排放的环境 要求控制调节； 人工手动控制调节则是又一种实施例； 洗涤步骤与除酸处理步骤之间有 一个分离杂质步骤， 是用分离器分离杂质并将所分离出的杂质经排污管排出。
本实施例应用的船舶安装有 12MW柴油发动机， 排放烟温 200 490 V， 排放烟气 量约为 67,095Nm3/h; 实施本发明脱硫方法， 在燃油含硫量 3%的条件下， 减排二氧化 硫到脱硫等效燃油含硫量为 0.1%， 排水 pH 6.5， 在不同海区时的耗用海水量为： 波罗的海 洗涤海水量 300m3 /h 掺混海水量 1100m3 /h
北 海 洗涤海水量 280m3 /h 掺混海水量 950m3 /h
实施例 2: 如图 2所示， 本实施例与实施例 1不同的是洗涤器 3有并联旁路排烟管， 即船舶发动机 1与洗涤排气管 4有直接联通的排烟管， 便于切换洗涤器 3。 脱硫控制是 用人工手动控制。 本实施例应用的船舶吨位较大， 安装有 60MW柴油发动机， 排放烟温 200 430 °C， 排放烟气量约为 310,100Nm3/h; 实施本发明脱硫方法， 在燃油含硫量 3%的条件下， 减 排二氧化硫到脱硫等效燃油含硫量满足 SECA控制标准（2005年）的 1.5%， 排水 pH 6.5， 在不同海区时的耗用海水量为：
波罗的海 洗涤海水量 980m3 /h 掺混海水量 3600m3 /h
太 平 洋 洗涤海水量 880m3 /h 掺混海水量 2600m3 /h
B: 对本发明海船排烟脱硫装置的技术方案作进一步说明如下：
实施例 3:
如图 1、图 3所示是一种用于本发明所述方法的海船排烟脱硫装置，洗涤器 3的进气 管 3.1从洗涤器 3下部导入的高温烟气 3.2，适用于烟气垂直向上进入洗涤器的实施场合。 一种海船排烟脱硫装置， 它有一个洗涤器 3， 省水除酸器 10; 所述的洗涤器 3， 其上部 为洗涤层 3.3， 与洗涤海水泵 5通过管道连通； 下部为冷却层 3.2; 洗涤器 3的一端与船 舶发动机 1的排烟管通过洗涤进气管 2连通， 另一端连接有洗涤排气管 4; 洗涤器 3下 部与省水除酸器 10连通；省水除酸器 10与掺混海水泵 9、风机 11以及经除酸处理后的 适排海水总排水管 14连接； 其省水除酸器 10有掺入碱性海水通道， 该通道设置有碱性 海水流量调节器， 它是出力能够调节的泵， 也可以是开度能够调节的阀门， 还可以是阀 门和出力能够调节的泵同时设置； 省水除酸器 10有空气注入通道， 该通道设置有空气 流量调节器， 它是出力能够调节的风机， 也可以为开度能够调节的阀门， 或挡板， 还可 以为阀门和风机， 或挡板和风机； 所述洗涤器 3有洗涤海水注入通道， 该通道设置有洗 涤海水流量调节器， 它是出力能够调节的泵， 也可以是开度能够调节的阀门， 还可以是 阀门和出力能够调节的泵同时设置； 上述耐阀门、 挡板上设置有控制杆， 所述的泵和风 机上设置有电机调速器； 所述的控制杆、 电机调速器与脱硫控制器 15相连接； 所述的 洗涤器 3包括壳体 3.1， 冷却层 3.2， 填料洗涤层 3.3， 集液池 3.7; 其中， 冷却层 3.2在 填料洗涤层 3.3的下方;所述的洗涤器 3与省水除酸器 10之间安装一分离杂质的分离器 7； 所述的脱硫控制器 15包括有指令 15.1、 传感器 15.2、 中央处理器 15.3、 执行器 15.4 和全球海区定位器 15.5。
实施例 4:
如图 2、 图 4所示， 是另一种用于本发明所述方法的海船排烟脱硫装置， 与上述实施 例不同的是高温烟气从侧面烟气进口 3.4水平方向进入洗涤器 3， 适用于烟气横向进入 洗涤器， 然后烟气向上流动的实施场合。 另外， 脱硫控制调节是手动操作。
本发明的保护范围不限于上述实施例。

Claims

权 利 要 求 书
1、 一种海船排烟脱硫方法， 其特征在于， 它包括下述步骤：
a、 洗涤： 将船舶发动机排出的含有 302的高温烟气冷却后进行洗涤， 然后将洗 涤净化后的烟气排放； 所述的洗涤是在洗涤器中用海水洗涤；
b、 转出酸性海水： 将洗涤过程吸收了 S02形成的酸性海水从洗涤器内转出到省 水除酸器中；
c、 除酸处理： 向进入省水除酸器的酸性海水中掺入碱性海水， 使成为混合海水， 并对混合海水鼓入空气；
d、 排水： 将经过除酸处理的适排海水排放至海域。
2、 根据权利要求 1所述的海船排烟脱硫方法， 其特征在于， 所述的洗涤步骤中的 在洗涤器中用海水洗涤， 是在具有填料洗涤层的洗涤器中进行洗涤。
3、 根据权利要求 1所述的海船排烟脱硫方法， 其特征在于， 所述的除酸处理步骤 中向省水除酸器中掺入的碱性海水， 其流量由调节器调节， 所述的调节器调节， 是通过 开度能够调节的阀门或 /和出力能够调节的泵调节;对省水除酸器中的混合海水鼓入的空 气， 其流量由调节器调节， 所述的调节器调节， 是通过开度能够调节的阀门、 挡板或 / 和出力能够调节的风机调节。
4、 根据权利要求 1所述的海船排烟脱硫方法， 其特征在于， 所述的洗涤步骤中所 用的洗涤海水， 其流量由调节器调节； 所述的调节器调节， 是通过开度能够调节的阀门 或 /和出力能够调节的泵调节。
5、 根据权利要求 3或 4所述的海船排烟脱硫方法， 其特征在于， 所述的调节器调 节是由人工或 /和脱硫控制器根据船舶所在海区的烟气和海水排放的环境要求控制调节。
6、 根据权利要求 1所述的海船排烟脱硫方法， 其特征在于， 洗涤步骤与除酸处理 步骤之间有一个分离杂质步骤， 是用分离器分离杂质并将所分离出的杂质经排污管排 出。
7、 一种用于权利要求 1所述方法的海船排烟脱硫装置， 其特征在于， 它包括洗涤 器 （3) ， 省水除酸器 （10) ； 所述的洗涤器 （3) ， 其上部为洗涤层 （3.3) ， 与洗涤海 水泵 （5)通过管道连通； 下部为冷却层 （3.2) ； 洗涤器 （3) 的一端与船舶发动机 （1 ) 的排烟管通过洗涤进气管（2)连通， 另一端连接有洗涤排气管 （4)； 洗涤器（3 )下部 与省水除酸器 （10) 连通； 省水除酸器 （10) 与掺混海水泵 （9) 、 风机 （11 ) 以及经 除酸处理后的适排海水总排水管 （14) 连接。
8、根据权利要求 7所述的海船排烟脱硫装置，其特征在于，所述的省水除酸器（10) 有掺入碱性海水通道， 该通道设置有碱性海水流量调节器， 选自于开度能够调节的阀门 或 /和出力能够调节的泵； 省水除酸器（10)有空气注入通道， 该通道设置有空气流量调 节器， 选自于开度能够调节的阀门、 挡板或 /和出力能够调节的风机。
9、 根据权利要求 7所述的海船排烟脱硫装置， 其特征在于， 洗涤器 （3 )有洗涤海 水注入通道，该通道设置有洗涤海水流量调节器，选自于开度能够调节的阀门或 /和出力 能够调节的泵。
10、 根据权利要求 8或 9所述的海船排烟脱硫装置， 其特征在于， 所述的阀门、 挡 板上设置有控制杆， 所述的泵和风机上设置有电机调速器； 所述的控制杆、 电机调速器 与脱硫控制器 （15 ) 相连接。
11、 根据权利要求 7所述的海船排烟脱硫装置， 其特征在于， 所述洗涤器 （3 ) 包 括壳体（3.1 )， 冷却层（3.2)， 填料洗涤层（3.3 )， 集液池（3.7 )； 其中， 冷却层（3.2) 在填料洗涤层 （3.3 ) 的下方。
12、 根据权利要求 Ί所述的海船排烟脱硫装置， 其特征在于， 洗涤器 （3 ) 与省水 除酸器 （10) 之间安装一分离杂质的分离器 （7 ) 。
13、 根据权利要求 10所述的海船排烟脱硫装置， 其特征在于， 脱硫控制器 （15 )包 括有指令器 （15.1 ) 、 传感器 （15.2) 、 中央处理器 （15.3 ) 、 执行器 （15.4) 和全球海 区定位器 ( 15.5 ) 。
PCT/CN2008/071307 2008-06-13 2008-06-13 海船排烟脱硫方法及装置 WO2009149603A1 (zh)

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