WO2016204588A1 - Système de réduction catalytique sélective à basse pression et procédé de commande de celui-ci - Google Patents

Système de réduction catalytique sélective à basse pression et procédé de commande de celui-ci Download PDF

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Publication number
WO2016204588A1
WO2016204588A1 PCT/KR2016/006515 KR2016006515W WO2016204588A1 WO 2016204588 A1 WO2016204588 A1 WO 2016204588A1 KR 2016006515 W KR2016006515 W KR 2016006515W WO 2016204588 A1 WO2016204588 A1 WO 2016204588A1
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Prior art keywords
bypass
urea
gas
temperature
bypass line
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PCT/KR2016/006515
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English (en)
Korean (ko)
Inventor
김대희
양희성
김규종
김건호
김정래
한주석
Original Assignee
현대중공업 주식회사
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Priority claimed from KR1020160075484A external-priority patent/KR101784614B1/ko
Application filed by 현대중공업 주식회사 filed Critical 현대중공업 주식회사
Priority to CN201680035498.2A priority Critical patent/CN107787397B/zh
Priority to EP16812001.2A priority patent/EP3312399B1/fr
Publication of WO2016204588A1 publication Critical patent/WO2016204588A1/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
    • F01N3/08—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous
    • F01N3/10—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust
    • F01N3/18—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by methods of operation; Control
    • F01N3/20—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for rendering innocuous by thermal or catalytic conversion of noxious components of exhaust characterised by methods of operation; Control specially adapted for catalytic conversion ; Methods of operation or control of catalytic converters
    • 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
    • F01N5/00—Exhaust or silencing apparatus combined or associated with devices profiting by exhaust energy
    • F01N5/02—Exhaust or silencing apparatus combined or associated with devices profiting by exhaust energy the devices using heat
    • 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
    • F01N9/00—Electrical control of exhaust gas treating apparatus
    • 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
    • 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
    • Y02T10/40—Engine management systems

Definitions

  • the present disclosure relates to an SCR system and a control method thereof, and more particularly, to a low pressure SCR system in which an SCR reactor is installed downstream of an engine supercharger and a control method thereof.
  • exhaust gases emitted after combustion from engines such as ships, automobiles, and power plants include a plurality of suspended particulates and hazardous substances such as nitrogen oxides (NOx) and sulfur oxides (SOx).
  • NOx nitrogen oxides
  • SOx sulfur oxides
  • the exhaust line of the engine is equipped with a diesel particulate filter (DPF), a selective catalytic reduction (SCR), and a scrubber (SCRubber, SOx removal) to remove harmful components in the exhaust gas.
  • DPF diesel particulate filter
  • SCR selective catalytic reduction
  • SOx removal SOx removal
  • the SCR system chemically reacts nitrogen oxides (NOx) in the exhaust gas with a reducing agent such as ammonia (NH3) and urea (Urea) in the catalyst layer to decompose and discharge water and nitrogen that are harmless to the human body. to be.
  • a reducing agent such as ammonia (NH3) and urea (Urea)
  • the SCR catalyst is composed of a porous catalyst filter formed by extrusion or metallic coating, and one or several SCR catalysts are continuously installed in the SCR reactor installed in the exhaust line.
  • the SCR system of the marine engine requires a high temperature of about 250 °C or more SCR reaction temperature to prevent the generation of ABS (Ammonium Bisulfate: NH4HSO4), decomposition and NOx removal. Accordingly, the engine temperature is increased through engine tuning, or the SCR reactor is installed upstream of the engine supercharger having a high exhaust gas temperature.
  • ABS Ammonium Bisulfate: NH4HSO4
  • the SCR reactor when installed upstream of the supercharger, it is called a 'high pressure SCR system' because the pressure and temperature of the exhaust gas flowing into the SCR reactor are high.
  • the SCR reactor should be installed very close to the engine. This makes it difficult to place the SCR system due to the narrow engine room and limits the layout design of peripherals or piping.
  • the SCR system can be installed downstream of the supercharger.
  • the SCR system can be installed outside the engine room.
  • the SCR system can be arranged freely without space constraints while at the same time freeing the layout design of the engine room.
  • the temperature of the exhaust gas entering the SCR reactor is lower than the normal SCR reaction temperature (or catalyst activation temperature) as the exhaust gas is first deprived of heat as it passes through the supercharger.
  • the normal SCR reaction temperature or catalyst activation temperature
  • due to the low temperature of the exhaust gas flowing into the SCR it is difficult to secure effective NOx removal performance, and also causes problems of catalyst poisoning and degradation of reducing agent decomposition performance.
  • a separate heating device is additionally installed in the exhaust line on the inlet side of the SCR reactor.
  • the heating device By heating the exhaust gas flowing into the SCR reactor through the heating device to the normal SCR reaction temperature.
  • the fuel consumption is high, the thermal efficiency of the entire system is reduced, and the energy is wasted.
  • the decomposition of the reducing agent is smoothly performed because the temperature of the exhaust gas flowing into the SCR reactor is maintained higher than the normal SCR reaction temperature.
  • the temperature of the exhaust gas flowing into the SCR reactor is lower than the normal SCR reaction temperature, thereby reducing decomposition of the reducing agent. Therefore, instead of inducing decomposition by injecting a reducing agent such as urea (UREA) near the inlet of the SCR reactor, it must be previously decomposed using a urea decomposition apparatus. That is, ammonia generated through urea decomposition is injected near the inlet of the SCR reactor.
  • a reducing agent such as urea (UREA)
  • the temperature of the flame generated as the fuel burns in the heating portion (eg, the heating chamber) of the urea cracker is very high, reaching 1500 ° C. Therefore, a cooling device for lowering the flame gas to a temperature suitable for urea decomposition is further required before the heated gas which has received the flame temperature is introduced into the urea decomposition chamber.
  • the addition of a cooling device not only complicates the system but also increases the running costs.
  • further driving of the cooling system reduces the efficiency of the entire system, increases energy waste and increases operating costs. At the same time, precise control of the temperature of the urea decomposition chamber to an appropriate level is not guaranteed.
  • the present invention has been proposed to solve the above-mentioned problems with the low pressure SCR system in which the SCR reactor is installed downstream of the supercharger.
  • An object of the present invention by using a portion of the exhaust gas from the engine to bypass the supercharger as a gas for temperature control of the urea cracker, a heat source for increasing the temperature of the exhaust gas flowing into the SCR reactor above the normal SCR reaction temperature It is to be used as a. It can supply the heat source for exhaust gas urea cracking and the heat source (or heat source for cooling the urea cracking unit) without additional energy supply to the SCR reactor, thereby reducing energy consumption and improving the thermal efficiency of the entire system.
  • An object of the present invention is to provide an SCR system and a control method thereof.
  • Another object of the present invention according to the temperature of the SCR reactor and the temperature of the urea cracker when utilizing the exhaust gas extracted before entering the supercharger as two heat sources for the temperature control of the SCR reactor and the temperature control of the urea cracker It is an object of the present invention to provide a low pressure SCR system capable of effective and precise control and a control method thereof.
  • Another object of the present invention is to supply a bypass gas to the urea cracking device to utilize as a heat source for urea cracking, so that the flow rate of the bypass gas supplied to the urea cracking device does not become excessive and flows on an appropriate scale, thereby urea cracking It is an object of the present invention to provide a low pressure SCR system and a method of controlling the same so that the size of the device can be optimized not too large.
  • Low pressure SCR system SCR reactor 30; An exhaust line 11 for guiding the low temperature exhaust gas passing through the supercharger 20 to the SCR reactor 30; A urea decomposition apparatus 40 having urea decomposition chamber 41 to decompose urea to generate ammonia, and send the generated ammonia to the SCR reactor 30; A first bypass line (13) for extracting a part of the high-temperature exhaust gas before flowing into the supercharger (20) from the engine to guide the urea cracker (40); The first exhaust line 11 is connected to the exhaust line 11 to distribute the high temperature exhaust gas flowing through the first bypass line 13 to the exhaust line 11.
  • Control unit 60 to perform; It includes.
  • the distribution ratio of the bypass gas flow rate between the first bypass line 13 and the second bypass line 14 may be set according to the exhaust gas temperature of the inlet of the SCR reactor 30. have.
  • the supply of additional gas through the third bypass line 16 is cut off, and the first bypass line
  • the bypass gas flow rate supplied to the urea cracker 40 through 13 is increased, and the bypass gas flow rate exiting the exhaust line 11 through the second bypass line 14 is set to decrease.
  • the increase in the flow rate of the bypass gas supplied to the urea cracker 40 it may be set to increase the amount of fuel flowing into the urea cracker 40.
  • the supply of additional gas for cooling the urea cracker 40 through the third bypass line 16 is lower than the target SCR temperature;
  • the second bypass line 14 is blocked so that the high temperature bypass gas is introduced into the urea cracker 40 through the first bypass line 13. It can be set to start when the heating gas temperature of the device 40 exceeds the target temperature.
  • the supply of additional gas for cooling through the third bypass line 16 may be set to increase until the heating gas temperature of the urea decomposition device 40 drops to a target temperature.
  • the third bypass line 16 is branched from the exhaust line 11 and the first bypass line downstream of the branch point P1 of the second bypass line 14. 13, additional gas extracted from the exhaust line 11 may be configured to join the bypass gas entering the urea cracking device 40 through the first bypass line 13.
  • Low pressure SCR system control method the step of determining the exhaust gas temperature of the SCR reactor 30 inlet; According to the determination result, the first bypass line 13 connected to the urea cracker 40 side and the upstream side of the SCR reactor 30 with respect to the high temperature bypass gas extracted before entering the supercharger 20. Setting a distribution ratio between the second bypass lines 14 connected to the exhaust gas line 11; According to the set distribution ratio, the opening degree of the first bypass line 13 and the second bypass line 14 is adjusted to the bypass gas flow rate supplied to the urea cracker 40 and the SCR reactor 30. Adjusting the discharged gas flow rate discharged; Determining whether to supply additional gas for cooling the urea cracker 40 through the third bypass line 16 and adjusting the flow rate according to the temperature of the heating gas of the urea cracker 40; It includes.
  • the exhaust gas temperature of the inlet of the SCR reactor 30 is lower than the SCR target temperature
  • the supply of additional gas for cooling through the third bypass line 16 is blocked.
  • the bypass gas flow rate discharged to the exhaust line 11 through the second bypass line 14 is reduced, and the bypass supplied to the urea cracker 40 through the first bypass line 13 is reduced.
  • the pass gas flow rate can be controlled to increase.
  • the third bypass line 16 is opened to exhaust the low-temperature exhaust gas from the supercharger 20. Control to supply as additional gas for cooling can be performed.
  • the exhaust gas temperature of the inlet of the SCR reactor 30 is lower than the target SCR temperature, by blocking the second bypass line 14 and opening the first bypass line 13.
  • the temperature of the heating gas of the urea cracker 40 is set to a target value.
  • the third bypass line 16 is opened to further extract a portion of the low temperature exhaust gas passing through the exhaust line 11, and through the first bypass line 13. It is possible to join the hot bypass gas entering the urea decomposition device 40.
  • the bypass gas by using the bypass gas at the same time as a heat source for raising the temperature of the SCR reactor, a heat source for urea decomposition, a heat source for cooling the urea cracking device, It can reduce consumption and improve the overall thermal efficiency of the system.
  • the urea cracker when supplying the bypass gas to the urea cracking device as a heat source for urea cracking, it is appropriately distributed to each bypass line to urea cracking
  • the urea cracker can be optimized to a relatively small size by allowing the flow rate of the bypass gas supplied to the device to be introduced at an appropriate scale without excessive flow.
  • FIG. 1 is a system diagram of a low pressure SCR system according to a first embodiment of the present invention.
  • FIG. 2 is a view showing the flow of exhaust gas and bypass gas when performing control of the low pressure SCR system according to the first embodiment of the present invention.
  • FIG 3 is a view for explaining a control process of the low-voltage SCR system according to a first embodiment of the present invention.
  • FIG. 4 is a system diagram of a low pressure SCR system according to a second embodiment of the present invention.
  • FIG. 5 is a view showing the flow of exhaust gas and bypass gas when performing control of the low-pressure SCR system according to the second embodiment of the present invention.
  • 6 is a comparison table showing simulation results of the bypass gas flow rate according to whether the bypass gas flow rate adjustment is possible.
  • FIG. 9 is a comparison diagram of three cases for the configuration of the third bypass line.
  • FIG. 10 is a graph comparing response characteristics of Case 2 and Case 3 of FIG. 9.
  • FIG. 11 is a schematic diagram illustrating a low pressure SCR system according to a third embodiment of the present invention.
  • FIG. 12 is a graph illustrating a comparison of the amount of additional gas for cooling according to the position of the branch point of the third bypass line.
  • FIG. 13 is a system diagram of a low pressure SCR system according to a fourth embodiment of the present invention.
  • FIG. 14 is a view showing the flow of exhaust gas and bypass gas when performing control of the low pressure SCR system according to the fourth embodiment of the present invention.
  • 15 is a view for explaining a control process of the low-voltage SCR system according to a fourth embodiment of the present invention.
  • the 'SCR target temperature' is the lower limit of the temperature range set to normally induced catalytic reaction for removing nitrogen oxides in the SCR reactor. Therefore, the temperature of the exhaust gas flowing into the SCR reactor must be maintained above the 'SCR target temperature'. For example, if the temperature range in which the catalytic reaction is normally induced is 250 ° C. to 400 ° C., the SCR target temperature is 250 ° C., its lower limit.
  • the 'target temperature of the heating gas' is a temperature or temperature range that the heating gas for urea decomposition introduced into the urea decomposition chamber should have. That is, the urea decomposition temperature is optimally maintained and urea decomposition is normally performed in the urea decomposition chamber by allowing the heating gas to maintain the 'target temperature of the heating gas'.
  • the urea decomposition target temperature is the optimum atmosphere in which the urea solution is decomposed into ammonia and carbon dioxide in the urea decomposition chamber.
  • the ammonia oxidation rate is increased, and when it is lower than that, the residence time for decomposition into ammonia is increased and the size of the urea decomposition chamber must be increased.
  • the target temperature of the heating gas can be set to 500 ° C, for example.
  • the target temperature of the heating gas is maintained at 500 ° C.
  • the endothermic reaction during urea decomposition causes the urea decomposition chamber to exit and enter the inlet side of the SCR reactor, where the temperature of the ammonia-containing heating gas is weak.
  • FIG. 1 is a schematic diagram of a low pressure SCR system according to a first embodiment of the present invention.
  • the low pressure SCR system includes an exhaust gas receiver 10, a supercharger 20, an SCR reactor 30, a urea cracker 40, a controller 60, An exhaust line 11, an SCR bypass line 12, a first bypass line 13, a second bypass line 14 and an ammonia injection line 15.
  • the exhaust gas receiver 10 collects exhaust gas discharged from each cylinder of an engine (not shown) and sends it to the supercharger 20.
  • the exhaust gas generated from the engine is supplied to the supercharger 20 through the exhaust gas receiver 10 to drive the turbine T of the supercharger 20 and then discharged through the exhaust line 11.
  • Exhaust gas discharged through the exhaust line 11 enters the SCR reactor 30 or is discharged into the flue without passing through the SCR reactor 30 through the SCR bypass line 12.
  • the selection of the exhaust line 11 and the SCR bypass line 12 is performed by the selective opening and closing of the open / close valve 61 and the open / close valve 62 provided in each line.
  • the on-off valve 62 is closed and the on-off valve 61 is opened.
  • the ammonia-containing heating gas generated in the urea cracker 40 flows into the inlet of the SCR reactor 30 along with the exhaust gas from the supercharger 20, and passes through the catalyst layer installed therein to provide nitrogen in the exhaust gas. Remove the oxide.
  • the temperature detector TC1 measures the exhaust gas temperature at the inlet of the SCR reactor 30 and applies the measured temperature to the controller 60.
  • the temperature detector TC1 may be installed at an inlet of the SCR reactor 30 or inside the SCR reactor 30.
  • the urea decomposing device 40 is to decompose urea to generate ammonia, which is a reducing agent.
  • the urea decomposing device 40 provides a space where a urea decomposing reaction takes place, and a heating unit 42 for heating the urea decomposing chamber 41. ).
  • the heating unit 42 may be a burner. As the fuel is burned through the burner in the heating part 42, a heating gas is provided to provide urea decomposition heat.
  • the fuel consists of oil or gas and air. Oil or gas and air can be provided in one supply line or in separate lines for each.
  • the flow rate of the fuel supplied to the heating part 42 is adjusted by controlling the opening degree of the fuel amount control valve 43 by the control part 60. If oil or gas and air are provided in separate lines, the flow control valve 44 and the flow control valve 45 installed in each line are controlled.
  • the heating gas generated by the combustion of the fuel in the heating unit 42 flows into the urea decomposition chamber 41 and becomes a heat source for decomposing urea injected into the urea decomposition chamber 41.
  • the heating gas coexists with the decomposed ammonia.
  • the ammonia-containing heating gas is supplied to the exhaust line 11 adjacent to the inlet of the SCR reactor 30 through the ammonia injection line 15, mixed with the exhaust gas flowing through the exhaust line 11, and introduced into the SCR reactor 30. .
  • the temperature detector TC3 measures the temperature of the heating gas flowing into the urea decomposition chamber 41 from the heater 42 and transmits the measured temperature value to the controller 60.
  • the exhaust line 15 guides the exhaust gas passing through the supercharger 20 to the SCR reactor 30 side.
  • the first bypass line 13 extracts a part of the exhaust gas before the high temperature exhaust gas discharged from the engine flows into the supercharger 20, that is, upstream of the supercharger 20, so that the urea cracker 40 is removed.
  • the on-off valve 63 opens or closes the first bypass line 13.
  • the on-off valve 63 is kept open at all times during normal operation.
  • the first bypass flow regulating valve 64 adjusts the flow rate of the bypass gas entering the urea decomposition device 40 through the first bypass line 13 under the control of the control unit 60.
  • the bypass gas supplied to the urea cracker 40 through the first bypass line 13 flows into the heating part 42 to adjust the temperature of the heating gas by the flame of the burner (for example, the temperature of 1000 to 1500 ° C.).
  • Ammonia injection line 15 as ammonia-containing heating gas after urea decomposition, with the role of controlling (ie lowering to a target temperature suitable for urea decomposition (eg 500 ° C.) or heating to the target temperature faster with less fuel).
  • the second bypass line 14 is connected between the first bypass line 13 and the exhaust line 11.
  • the second bypass line 14 branches at the branch point P1 of the first bypass line 13 and is connected to the exhaust line 11 at the joining point P2.
  • bypass gas provided by extracting a part of the high-temperature exhaust gas before flowing into the supercharger 20 from the engine is supplied to the urea cracker 40 through the first bypass line 13 and the second gas is supplied. 2 is distributed at the bypass gas flow rate discharged to the exhaust line 11 through the bypass line 14.
  • the temperature of the exhaust gas discharged from the engine is high (eg, 300 ° C. to 450 ° C.), while the exhaust gas passing through the supercharger 20 is relatively low temperature (eg, about 230 ° C.).
  • the temperature of the SCR reactor 30 must be raised to the SCR target temperature (eg, 250 ° C.) through the bypass gas.
  • the SCR target temperature eg, 250 ° C.
  • a part of the bypass gas is transferred to the urea cracker 40.
  • the ammonia-containing heating gas after decomposing urea in the urea cracker 40 maintains a high temperature (for example, 300 to 400 ° C.)
  • the temperature of the SCR reactor 30 is increased by using a high temperature of the bypass gas. Raising to the target temperature can play the original role together.
  • the first bypass flow regulating valve 64 is provided in the first bypass line 13, and the second bypass flow regulating valve 65 is provided in the second bypass line 14.
  • the urea decomposition apparatus 40 By adjusting the opening degree of the 1st bypass flow regulating valve 64 and the 2nd bypass flow regulating valve 65 by the control part 60, the urea decomposition apparatus 40 through the 1st bypass line 13 is carried out.
  • the distribution ratio of the bypass gas flow rate supplied to) and the bypass gas flow rate discharged to the exhaust line 11 through the second bypass line 14 is changed (adjusted).
  • the controller 60 transmits the temperature of the SCR reactor 30 inlet port (in the present specification, which includes the inside of the SCR reactor 30) transmitted through the temperature detector TC1, and is transmitted through the temperature detector TC2.
  • Bypass gas temperature the temperature of the heating gas flowing into the urea decomposition chamber 41 transmitted through the temperature detector TC3, and the ammonia-containing heating gas of the ammonia injection line 15 transmitted through the temperature detector TC4. Comparing and determining the temperature of the bypass gas distribution ratio of the first bypass line 13 and the second bypass line 14 is set. Distribution ratios referred to in this specification and claims are defined to include 0: 100 or 100: 0.
  • bypass gas flow rate entering the urea cracker 40 through the first bypass line 13 or the bypass gas flow rate discharged to the exhaust line 11 through the second bypass line 14. Is to include a distribution situation that shuts off and sends all bypass gas to the other side.
  • the controller 60 may set a bypass gas distribution ratio of the first bypass line 13 and the second bypass line 14 according to the exhaust gas temperature of the inlet of the SCR reactor 30.
  • controller 60 increases the bypass gas flow rate supplied to the urea cracker 40 through the first bypass line 13 when the exhaust gas temperature at the inlet of the SCR reactor 30 is lower than the SCR target temperature.
  • the distribution ratio can be set to
  • the controller 60 increases the amount of fuel flowing into the urea cracker 40, while the first bypass line 13 is closed.
  • the distribution ratio may be set to increase the bypass gas flow rate supplied to the urea cracker 40 through.
  • FIGS. 2 and 3 A control process of the low pressure SCR system according to the first embodiment will be described with reference to FIGS. 2 and 3.
  • 2 is a diagram illustrating the flow of exhaust gas and bypass gas
  • FIG. 3 is a diagram illustrating a process of performing control.
  • the on-off valve 63 is normally opened to supply the bypass gas.
  • the opening degree of the first bypass flow adjustment valve 64 and the second bypass flow adjustment valve 65 is controlled to a predetermined standard value (or an initial operation value) to control the first bypass line 13 and the second.
  • the distribution ratio of the bypass line 14 is kept at a standard value.
  • the opening amount of the fuel amount control valve 43 is controlled to a predetermined standard value (or initial operation value) to maintain the fuel amount supplied to the urea cracker 40 at a standard value.
  • the control unit 60 determines the exhaust gas temperature of the inlet SCR reactor 30 in order to effectively implement urea decomposition and exhaust gas heating according to the exhaust gas temperature of the inlet SCR reactor 30 (S10). . That is, it is determined whether or not the temperature of the exhaust gas flowing into the SCR reactor 30 is greater than or equal to the 'SCR target temperature (eg, 250 ° C.)' in which a catalytic reaction for removing nitrogen oxides from the SCR reactor is normally induced.
  • the 'SCR target temperature eg, 250 ° C.
  • the bypass gas distribution ratio of the first bypass line 13 and the second bypass line 14 is set (S20).
  • the flow rate of the first bypass line 13 is set to increase compared to the second bypass line 14.
  • bypass gas flow rates of the first bypass line 13 and the second bypass line 14 are controlled according to the set distribution ratio (S30). Control of the gas flow rate is performed by increasing or decreasing the opening value of the first bypass flow regulating valve 64 and the second bypass flow regulating valve 65.
  • the opening value of the second bypass flow regulating valve 65 is decreased and the first bypass flow regulating valve 64 is closed. The opening value is increased. Then, the bypass gas flow rate discharged to the exhaust line 11 through the second bypass line 14 is reduced and the bypass gas flow rate supplied to the urea cracker through the first bypass line 13 is increased. .
  • the flow rate and temperature of the heating gas are increased together, and as a result, the flow rate and temperature of the ammonia-containing heating gas exiting from the urea decomposition chamber 41 are increased, and the exhaust gas temperature of the inlet portion of the SCR reactor 30 is increased more quickly. .
  • the heat capacity of the heating unit 42 is increased with the increase of the amount of fuel flowing into the urea cracker 40, which is too high due to the high flame temperature (for example, 1000 ⁇ 1500 °C) generated by the combustion of the fuel
  • the temperature of the heating gas is lowered to the urea decomposition target temperature (eg 500 ° C.) by the bypass gas supplied in a large amount through the first bypass line 13 and not the cooling air provided by any other apparatus. .
  • the flow rate of the bypass gas through the first bypass line 13 is gradually increased until the temperature of the heating gas reaches the target temperature.
  • the exhaust gas temperature at the inlet of the SCR reactor 30 reaches or exceeds the SCR target temperature
  • an additional heat supply for raising the exhaust gas temperature at the inlet of the SCR reactor 30 is not necessary, and the urea cracker ( In 40) only the heat for urea decomposition is needed. Therefore, the amount of fuel supplied to the urea cracker 40 can be maintained at the minimum amount to provide only heat for urea cracking, and the minimum ratio of bypass gas flow rate required to lower the temperature of the heating gas to the urea cracking target temperature. May be supplied through the first bypass line 13.
  • FIG. 4 and 5 are views for explaining a low pressure SCR system according to a second embodiment of the present invention.
  • FIG. 4 is a schematic diagram
  • FIG. 5 is a diagram illustrating a flow of exhaust gas and bypass gas when performing control.
  • the second embodiment differs only from the first embodiment in that it further comprises a third bypass line 16 which extracts a portion of the exhaust gas passing through the exhaust line 11 and supplies it to the urea cracker 40.
  • the rest of the configuration is the same.
  • the third bypass line 16 is branched at the branch point P3 of the exhaust line 11 and connected to the first bypass line 13 at the joining point P4.
  • the third bypass line 16 may be provided with a blower 50 for extracting exhaust gas flowing through the exhaust line 11.
  • the exhaust gas flowing into the blower 50 is controlled by the on-off valve 66, and the flow rate of the additional gas exiting the blower 50 is controlled by the controller 60 by adjusting the third bypass flow regulating valve 67. Controlled.
  • the controller 60 may control the flow rate of the additional gas flowing into the urea decomposition device 50 through the third bypass line 16 by adjusting the rotational speed of the blower 50.
  • the supply of additional gas through the third bypass line 16 is performed under the condition that the exhaust gas temperature at the inlet of the SCR reactor 30 is lower than the SCR target temperature, and the second bypass flow control valve 65 is closed.
  • the bypass flow regulating valve 64 see FIG. 5
  • the heating gas flowing into the urea decomposition chamber 41 of the urea decomposition apparatus 40 may be set to be performed when the temperature exceeds the target temperature.
  • a target temperature of the heating gas that has received a high flame temperature of the heating part 42 is urea decomposition target temperature. It can be used as a cooling gas to lower the furnace.
  • control to increase the amount of fuel flowing into the urea cracker 40 can also be performed.
  • the heat capacity of the heating unit 42 is increased with the increase of the amount of fuel flowing into the urea cracker 40, which is too high due to the high flame temperature (for example, 1000 ⁇ 1500 °C) generated by the combustion of the fuel
  • the temperature of the heating gas is lowered to the urea decomposition target temperature (eg, 500 ° C.) by the bypass gas supplied in a large amount through the first bypass line 13.
  • the flow rate of the bypass gas through the first bypass line 13 is gradually increased until the temperature of the heating gas reaches the target temperature.
  • a portion of the low temperature exhaust gas is extracted from the exhaust line 11 through the third bypass line 16 and further supplied to the urea cracker 40 as an additional gas to urea crack the temperature of the heating gas.
  • the target temperature can be lowered.
  • FIGS. 6 to 10 show the energy saving effect and the urea decomposition chamber 41 according to the configuration of the first, second and third bypass lines 13, 14 and 16 of the present invention, and the flow rate control of each line.
  • the results of the simulation are performed on the possibility of size reduction and the response characteristic to the control of the third bypass line 16.
  • the engine used for the simulation was an eight-cylinder two-stroke, a piston diameter of 95 cm, a maximum output of 41.6 MW / 75 rpm, and an displacement of 306,396 kg / h.
  • the urea decomposition chamber 41 used what consists of 1.5 m in diameter.
  • FIG. 6 shows a case where the bypass gas flow rate flowing into the urea cracker 40 cannot be adjusted (conventionally), and the second bypass line 14 is branched from the first bypass line 13 to separate the urea cracker (
  • the urea decomposition target temperature of the urea decomposition chamber 41 was calculated at 500 ° C., and the fuel consumption of the burner of the urea decomposition apparatus for this purpose was calculated.
  • the bypass gas flow rate of 10% from the engine always flows into the urea cracker 40 as it is. Due to this, burner fuel consumption increases to 80 to 135 kg / h in the engine load range of 40 to 100.
  • the height of the urea decomposition chamber 41 should be made as high as about 4.7 m.
  • the present invention has a second bypass line 14 and the gas flowing into the urea cracker 40 through the first bypass line 13 by the control of the first bypass flow control valve 64. Since the flow rate can be optimally controlled, the gas flow rate flowing into the urea cracker 40 can be reduced to 5% of the engine displacement. The remaining 5% is discharged to the exhaust line 11 through the second bypass line 14. Due to this, the fuel consumption of the burner is reduced to 40 to 65 kg / h in the engine load region of 40 to 100. In addition, the height of the urea decomposition chamber 41 for accommodating the entire bypass gas flow rate of 5% and heating to the urea decomposition target temperature (500 ° C.) is sufficient to ensure only about 2.4 m.
  • the gas flow rate flowing into the urea cracker 40 cannot be adjusted, the gas flow rate flowing into the urea cracker 40 is set to a maximum value, while corresponding to the worst condition in which the flow rate may be insufficient. Therefore, it was necessary to secure an additional bypass gas flow rate, and therefore, it is necessary to design a bypass gas flow rate that is too much larger than the actual required flow rate.
  • the increase in burner fuel consumption and the increase in size of the urea decomposition chamber 41 are accompanied by this reason.
  • the gas flow rate flowing into the urea cracker 40 can be optimally controlled by the control of the second bypass line 14 and the first bypass flow regulating valve 64, the additional bypass It is not necessary to ensure too much pass gas flow rate.
  • the burner fuel consumption and the size of the urea decomposition chamber 41 can be reduced by that.
  • FIG. 7 to 8 show the case where the flow rate of the third bypass line 16 cannot be adjusted, and the additional gas for cooling is provided by the third bypass flow control valve 67 with the third bypass line 16.
  • FIG. 7 shows a third bypass gas flow rate
  • FIG. 8 is a graph comparing the supply amount of the third bypass gas flow rate according to the engine load.
  • the flow rate of the bypass gas (EGB) coming out of the engine from the engine to the first bypass line 13 is 10% of the total flow rate (exhaust amount) of the engine, and the first bypass flow control valve 64 is used. ), The bypass gas flow rate entering the urea cracker 40 was adjusted to 4%.
  • FIG. 9 to 10 compare the response characteristics when the blower 50 is provided in the third bypass line 16 and the flow rate adjustment is possible by the third bypass flow regulating valve 67.
  • a comparison diagram of the three cases with respect to the configuration of the third bypass line 16 is shown, and FIG. 10 shows a graph comparing the response characteristics of the case 2 and the case 3.
  • case 1 (CASE 1) includes only the opening / closing valve or the flow regulating valve in the third bypass line 16
  • case 2 CASE 2 is blower 50 in the third bypass line 16.
  • the case 3 (CASE 3) is a case where the blower 50 and the third bypass flow control valve 67 are provided together with the third bypass line 16.
  • the exhaust line 11 flows through the supercharger 20 while exhaust gas having a reduced pressure and temperature flows.
  • the pressure of the exhaust line 11 is about 1 bara or less.
  • the first bypass line 13 the high-temperature, high-pressure exhaust gas before passing through the supercharger 20 flows.
  • the pressure of the first bypass line 13 is about 3 bara or less. Therefore, when only the on-off valve or the flow regulating valve is provided without a blower as in Case 1, it is very difficult to introduce the exhaust gas from the low pressure exhaust line 11 into the high pressure first bypass line 13.
  • the gas may be forcibly extracted from the low pressure exhaust line 11 to the high pressure first bypass line 13 through the blower, but the flow rate should be controlled only by adjusting the output of the blower. Therefore, as shown in FIG. 10, even when a flow rate change command is applied by the controller 60 when the engine load suddenly changes, a large delay time is required until the target flow rate is reached.
  • the blower 50 and the third bypass flow regulating valve 67 are provided together in the third bypass line 16 so that the blower 50 is operated at the maximum allowable load.
  • the flow rate is controlled by the control of the third bypass flow regulating valve 67 at the time of sudden change, when the flow rate change command is applied from the controller 60, the flow rate can be quickly adjusted to the target flow rate.
  • FIG. 11 is a schematic diagram illustrating a low pressure SCR system according to a third embodiment of the present invention.
  • the third bypass line 16 is branched at the branch point P3 of the exhaust line 11 and connected at the joining point P4 to the first bypass line 13.
  • the branch point P3 of the third bypass line 16 is located at the exhaust line 11 upstream of the confluence point P2 of the second bypass line 14,
  • the confluence point P4 is located in the first bypass line 13 downstream of the branch point P1 of the second bypass line 14.
  • the branch point P3 of the third bypass line 16 is provided upstream of the confluence point P2 of the second bypass line 14, so that it is less than the second embodiment.
  • the urea decomposition target temperature can be achieved by the exhaust gas at the flow rate, and the urea decomposition chamber 41 can be optimized and the energy consumption of the blower 50 can be further reduced.
  • the branch point P3 of the third bypass line 16 is provided upstream of the confluence point P2 of the second bypass line 14 as in the third embodiment of the present invention, the high temperature bypass gas is joined. Since the low-temperature exhaust gas can be added, the amount of cooling gas required by the urea cracking apparatus 40 can be reduced by that much.
  • FIG. 12 illustrates a case where the branch point P3 of the third bypass line 16 is located downstream of the confluence point P2 of the second bypass line 14 as in the second embodiment, and the third bypass as in the third embodiment.
  • the branch point P3 of the pass line 16 must be supplied to the urea cracker 40 through the third bypass line 16 when the branch point P3 is located upstream of the joining point P2 of the second bypass line 14.
  • a graph showing a comparison of the amount of additional gas for cooling is shown.
  • the engine used for the simulation was an 11-cylinder two-stroke, a piston diameter of 95 cm, a maximum output of 59.8 MW / 78 rpm and a displacement of 439,200 kg / h.
  • the additional gas bleed flow towards the urea cracker 40 was based on 2% of the total displacement.
  • FIGS. 13 to 15 are diagrams for describing a low pressure SCR system according to a fourth embodiment of the present invention.
  • FIG. 13 is a schematic diagram
  • FIG. 14 is a diagram illustrating a flow of exhaust gas and bypass gas when performing control
  • FIG. 15 is a diagram for explaining a process of performing control.
  • bypass gas line extracts a part of the exhaust gas before flowing into the supercharger 20 from the engine and guides it to the urea cracker 40.
  • a bypass line 13 and a third bypass line 16 branched from the exhaust line 11 and connected to the first bypass line 13.
  • the third bypass line 16 passes through the supercharger 20 and supplies a part of the exhaust gas passing through the exhaust line 11 as an additional gas to the urea cracker 40.
  • the on-off valve 63 is installed in the first bypass line 13.
  • the third bypass line 16 may be provided with a blower 50 for extracting exhaust gas flowing through the exhaust line 11.
  • the exhaust gas flowing into the blower 50 is controlled by the on-off valve 66, and the flow rate of the additional gas exiting the blower 50 is controlled by the controller 60 by adjusting the third bypass flow regulating valve 67. Controlled.
  • the controller 60 may control the flow rate of the additional gas flowing into the urea decomposition device 50 through the third bypass line 16 by adjusting the rotational speed of the blower 50.
  • the SCR reactor 30 is supplied to the SCR reactor 30 by supplying a bypass gas, i.e., ammonia-containing heating gas, which is heated to 40 while passing through 40, to the exhaust line 11 on the inlet side of the SCR reactor 30.
  • a bypass gas i.e., ammonia-containing heating gas
  • the target temperature was raised.
  • the role of lowering the temperature of the heating gas of the urea cracker 40 by the bypass gas supplied through the first bypass line 13 is also performed.
  • a part of the low temperature exhaust gas is extracted from the exhaust line 11 through the third bypass line 16 and further supplied to the urea cracker 40 as additional gas, thereby heating the gas of the urea cracker 40. This is to reduce the temperature of the urea to the target temperature for urea decomposition.
  • the ratio of the flow rate of the additional gas entering the urea cracker 40 through the third bypass line 16 to the flow rate of the bypass gas entering the urea cracker 40 through the first bypass line 13 is The controller 60 controls the temperature of the heating gas generated by the heating unit 42 to effectively lower the urea decomposition target temperature.
  • the first flow is increased in response to the increase in the fuel flow rate.
  • the bypass gas flow rate supplied through the pass line 13 the temperature of the heating gas according to the increase in the heat capacity of the heating portion of the urea cracker 40 is cooled so as not to exceed the target temperature.
  • Such control may be performed in a state where the supply of the exhaust gas through the third bypass line 16 is cut off.
  • the third bypass line 16 may be opened to supply the low temperature exhaust gas flowing through the supercharger 20 and flowing through the exhaust line 11 as an additional gas to assist the cooling operation.
  • FIG. 15 is a diagram for describing performing control according to the fourth embodiment. See FIG. 14 in parallel.
  • the control method of FIG. 15 can be used as the control method of the second to third embodiments of the present invention.
  • the on-off valve 63 is normally opened to supply the bypass gas (S100).
  • the on-off valve 66 and the third bypass flow adjustment valve 67 are closed to keep the supply of additional gas shut off.
  • the control unit 60 determines the exhaust gas temperature of the inlet SCR reactor 30 in order to effectively implement urea decomposition and exhaust gas heating according to the exhaust gas temperature of the SCR reactor 30 inlet (S110). . That is, it is determined whether or not the temperature of the exhaust gas flowing into the SCR reactor 30 is greater than or equal to the 'SCR target temperature (eg, 250 ° C.)' in which a catalytic reaction for removing nitrogen oxides from the SCR reactor is normally induced.
  • the 'SCR target temperature eg, 250 ° C.
  • the increase or decrease of the fuel flow rate flowing into the urea cracker 40 is determined.
  • the third bypass line 16 is opened to supply the low-temperature exhaust gas that has passed through the supercharger 20 as an additional gas to the urea cracker. Help the cooling of the heating gas of (40).
  • the flow rate of the additional gas is increased by increasing the opening degree of the third bypass line 16 until the heating gas temperature of the urea cracker 40 is lowered to the urea cracking target temperature (S160).
  • the configuration of the low pressure SCR system and the control method thereof according to the present invention can be implemented without various modifications within the range allowed by the technical idea of the present invention.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Toxicology (AREA)
  • Exhaust Gas After Treatment (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

La présente invention concerne un système de réduction catalytique sélective à basse pression comprenant : un réacteur de réduction catalytique sélective (30) ; un tuyau d'échappement (11) permettant de guider le gaz d'échappement à basse température, qui est passé à travers un compresseur de suralimentation (20), jusqu'au réacteur de réduction catalytique sélective (30) ; un dispositif de décomposition d'urée (40) présentant une chambre de décomposition d'urée (41) permettant de décomposer l'urée pour produire de l'ammoniac, et d'envoyer l'ammoniac produit vers le réacteur de réduction catalytique sélective (30) ; une première conduite de dérivation (13) permettant d'extraire, à partir d'un moteur, une partie du gaz d'échappement à haute température avant d'être introduit dans le compresseur de suralimentation (20) et de guider le gaz d'échappement à haute température jusqu'au dispositif de décomposition de l'urée (40) ; une deuxième conduite de dérivation (14) capable de changer le débit de gaz de dérivation fourni au dispositif de décomposition de l'urée (40) à travers la première conduite de dérivation (13), en raccordant le tuyau d'échappement (11) à la première ligne de dérivation (13) de sorte que le gaz d'échappement à haute température s'écoulant à travers la première conduite de dérivation (13) est distribué au tuyau d'échappement (11) ; une troisième conduite de dérivation (16) permettant d'extraire une partie du gaz d'échappement à basse température, qui est passée à travers le compresseur de suralimentation (20) et s'écoule à travers le tuyau d'échappement (11), et de fournir, au dispositif de décomposition d'urée (40), le gaz d'échappement à basse température en tant que gaz supplémentaire pour refroidir le gaz chauffé pour décomposer l'urée ; et un ventilateur (50) et une soupape de régulation de débit de dérivation (67) installée sur la troisième conduite de dérivation (16) pour ajouter de manière forcée le gaz d'échappement s'écoulant à travers le tuyau d'échappement (11).
PCT/KR2016/006515 2015-06-18 2016-06-20 Système de réduction catalytique sélective à basse pression et procédé de commande de celui-ci WO2016204588A1 (fr)

Priority Applications (2)

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CN201680035498.2A CN107787397B (zh) 2015-06-18 2016-06-20 低压scr系统及其控制方法
EP16812001.2A EP3312399B1 (fr) 2015-06-18 2016-06-20 Système de réduction catalytique sélective à basse pression et procédé de commande de celui-ci

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KR20150086744 2015-06-18
KR10-2015-0086723 2015-06-18
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KR20150100654 2015-07-15
KR10-2015-0100654 2015-07-15
KR10-2016-0075484 2016-06-17
KR1020160075484A KR101784614B1 (ko) 2015-06-18 2016-06-17 저압 scr 시스템 및 그 제어 방법

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2280155A2 (fr) * 2009-07-30 2011-02-02 MAN Nutzfahrzeuge AG Procédé et dispositif de nettoyage d'un flux de gaz d'échappement d'un moteur à combustion interne
JP2013130072A (ja) * 2011-12-20 2013-07-04 Mitsubishi Motors Corp 内燃機関の排ガス浄化装置及び浄化方法
KR20140000556A (ko) * 2012-06-25 2014-01-03 두산엔진주식회사 선택적 촉매 환원 시스템을 포함한 선박용 동력 장치
KR20140094645A (ko) * 2010-01-15 2014-07-30 미츠비시 쥬고교 가부시키가이샤 배기 가스 탈초 시스템 및 이것을 구비한 선박과 배기 가스 탈초 시스템의 제어 방법
US20140223902A1 (en) * 2013-02-13 2014-08-14 Ford Global Technologies, Llc Internal combustion engine with selective catalytic converter for the reduction of nitrogen oxides and method for operating an internal combustion engine of said type
KR20160006516A (ko) * 2014-07-09 2016-01-19 엘지전자 주식회사 이동단말기 및 그 제어방법

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2280155A2 (fr) * 2009-07-30 2011-02-02 MAN Nutzfahrzeuge AG Procédé et dispositif de nettoyage d'un flux de gaz d'échappement d'un moteur à combustion interne
KR20140094645A (ko) * 2010-01-15 2014-07-30 미츠비시 쥬고교 가부시키가이샤 배기 가스 탈초 시스템 및 이것을 구비한 선박과 배기 가스 탈초 시스템의 제어 방법
JP2013130072A (ja) * 2011-12-20 2013-07-04 Mitsubishi Motors Corp 内燃機関の排ガス浄化装置及び浄化方法
KR20140000556A (ko) * 2012-06-25 2014-01-03 두산엔진주식회사 선택적 촉매 환원 시스템을 포함한 선박용 동력 장치
US20140223902A1 (en) * 2013-02-13 2014-08-14 Ford Global Technologies, Llc Internal combustion engine with selective catalytic converter for the reduction of nitrogen oxides and method for operating an internal combustion engine of said type
KR20160006516A (ko) * 2014-07-09 2016-01-19 엘지전자 주식회사 이동단말기 및 그 제어방법

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