Ship flue gas purification system

Abstract

The utility model relates to the technical field of ship flue gas purification, and discloses a ship flue gas purification system which comprises a flue gas introduction device, a liquid introduction device, a micro-interface oscillation absorber, a settling tank and a controller, the flue gas introducing device comprises a main pipe, a branch pipe, an induced draft fan, an intelligent flue gas regulating valve and an intelligent air regulating valve, the main pipe and the branch pipe are respectively connected with the induced draft fan, and the induced draft fan is connected with the micro-interface oscillation absorber; the intelligent flue gas regulating valve is arranged on the main pipe, and the intelligent air regulating valve is arranged on the branch pipe; the liquid introduction device comprises an absorption liquid pump which is connected with the micro-interface oscillation absorber; the controller is respectively connected with the intelligent flue gas regulating valve, the intelligent air regulating valve and the absorption liquid pump. The system provided by the utility model can effectively solve the problem that the ship flue gas purification effect is unstable.

Description

TECHNICAL FIELD

[0001] The utility model relates to ship flue gas purification technical field, concretely relates to a ship flue gas purification system. BACKGROUND

[0002] The flue gas discharged by the ship contains SO X , NO X , and carbon black, which are one of the main pollution sources in the atmosphere. With the increasing global environmental awareness, many countries have formulated strict emission standards. For example, China issued the "General Requirements for Monitoring of Ship Atmospheric Pollutants" in 2021 to reduce the pollution of ship exhaust gas to the atmosphere.

[0003] In order to reduce the harm of ship flue gas to the environment, the shipping industry is actively developing and applying ship flue gas removal technology to achieve ultra-low emission targets. At the same time, the micro-liquid droplet interface oscillation technology can effectively improve the reaction rate due to its high mass and heat transfer efficiency, fast reaction speed, etc., which also provides a new possibility for improving the efficiency of ship flue gas treatment.

[0004] However, the cutting and atomization effect of the absorption liquid in the micro-interface oscillation absorber developed by using the micro-liquid droplet interface oscillation technology is easily affected by the gas flow and gas temperature. When the ship travels on the river and the sea, the working condition is complex and changeable, resulting in large fluctuations in flue gas flow. Sometimes the ship emits less flue gas, which makes the cutting and atomization effect of the micro-interface oscillation absorber poor, resulting in poor purification effect of the ship flue gas. Sometimes the ship emits more flue gas, although it can ensure the cutting and atomization effect of the micro-interface oscillation absorber, but the operable space on the ship is small, and it is difficult to cool when the flue gas is more. When the flue gas enters the micro-interface oscillation absorber with a high temperature, the absorption liquid evaporates greatly during the gas-liquid contact process, resulting in a decrease in the purification effect of the flue gas.

[0005] Therefore, it is urgent to provide a ship flue gas purification system that can cope with the fluctuation of flue gas flow and stabilize the purification effect of flue gas. SUMMARY

[0006] The utility model discloses a kind of ship flue gas purification systems to solve the problems that the cutting and atomization effect of the micro-interface oscillation absorber is unstable due to the large fluctuation of flue gas flow in prior art.

[0007] To achieve the above-mentioned purpose, the utility model provides a kind of ship flue gas purification system, wherein the system includes: flue gas introduction device 1, liquid introduction device 2, micro-interface oscillation absorber 3, sediment tank 4 and controller 5;Wherein the flue gas introduction device 1 and liquid introduction device 2 are connected with the micro-interface oscillation absorber 3 respectively, and the micro-interface oscillation absorber 3 is connected with the sediment tank 4;

[0008] The flue gas introduction device 1 comprises a main pipe 11, a branch pipe 12, a flue fan 13, a flue gas intelligent regulating valve 14 and an air intelligent regulating valve 15. The main pipe 11 and the branch pipe 12 are connected with the flue fan 13 respectively. The flue fan 13 is connected with the micro-interface oscillation absorber 3. The flue gas intelligent regulating valve 14 is arranged on the main pipe 11. The air intelligent regulating valve 15 is arranged on the branch pipe 12.

[0009] The liquid introduction device 2 comprises an absorption liquid pump 22. The absorption liquid pump 22 is connected with the micro-interface oscillation absorber 3.

[0010] The controller 5 is connected with the flue gas intelligent regulating valve 14, the air intelligent regulating valve 15 and the absorption liquid pump 22 respectively.

[0011] Preferably, the branch pipe 12 is arranged on the main pipe 11 and connected with the flue fan 13 through the main pipe 11.

[0012] Preferably, the flue gas intelligent regulating valve 14 is used for measuring the flow and temperature of the flue gas. The air intelligent regulating valve 15 is used for adjusting the flow of air.

[0013] Preferably, the liquid introduction device 2 further comprises an absorption liquid storage tank 21. The absorption liquid storage tank 21 is connected with the absorption liquid pump 22.

[0014] Preferably, the liquid introduction device 2 further comprises a solvent pump 23. The solvent pump 23 is connected with the absorption liquid storage tank 21.

[0015] Preferably, the micro-interface oscillation absorber 3 comprises a gas phase inlet and a liquid phase inlet. The gas phase inlet is arranged higher than the liquid phase inlet in the micro-interface oscillation absorber 3.

[0016] Preferably, the flue fan is connected with the gas phase inlet. The absorption liquid pump is connected with the liquid phase inlet.

[0017] Preferably, the precipitation tank 4 is connected with the absorption liquid storage tank 21.

[0018] Preferably, the precipitation tank 4 further comprises a control valve. The control valve is arranged at the liquid phase outlet.

[0019] Preferably, the controller 5 is used for transmitting the volume flow and temperature of the ship flue gas monitored by the flue gas intelligent regulating valve 14, the switch state of the air intelligent regulating valve 15 and the volume flow of the air inlet to the computer control terminal in real time. The mass flow of the absorption liquid output by the absorption liquid pump 22 is adjusted in combination with the concentration of the absorbent and the activator in the absorption liquid.

[0020] By the technical scheme, the ship flue gas purification system has the beneficial technical effects as follows:

[0021] 1. The ship flue gas purification system provided by the utility model can introduce air in time to make up for the shortage of flue gas flow when the flue gas discharged by the ship is small, so that the airflow entering the micro-interface oscillation absorber can be kept stable, and the absorption liquid in the micro-interface oscillation absorber can be fully cut and atomized, thereby making the flue gas of the ship still be efficiently purified when the discharge amount is small; the discharged purified flue gas can always meet the international and domestic environmental protection standards, the ultra-low discharge of flue gas can be realized, air pollution can be effectively reduced, and the marine ecological system and human health are protected.

[0022] 2. The ship flue gas purification system provided by the utility model can effectively solve the problem of the decline of the purification effect of the micro-interface oscillation absorber caused by the excessively high temperature of the ship flue gas by linking the intelligent flue gas regulating valve and the absorption liquid pump and timely adjusting the mass flow and concentration of the absorption liquid.

[0023] 3. The ship flue gas purification system provided by the utility model can realize on-site water taking, can timely adjust the composition of the absorption liquid and the types of additives (absorbent, activator, defoaming agent, etc.) according to specific conditions, is economical and environmentally friendly, and is also helpful to improve the flexibility of the flue gas purification system.

[0024] 4. The ship flue gas purification system provided by the utility model is simple in device operation, compact in overall design, convenient to maintain, does not need special equipment and skills, has higher removal efficiency, has lower operation cost, is especially suitable for flue gas treatment on the ship, can better adapt to the operation requirements of the ship in a complex and changeable environment, and will not affect the normal operation and performance of the ship. BRIEF DESCRIPTION OF DRAWINGS

[0025] Figure 1 is a structural schematic view of the ship flue gas purification system provided by the utility model.

[0026] MARKS

[0027] DETAILED DESCRIPTION

[0028] The endpoints of the ranges and any values disclosed herein are not limited to the precise values stated. The endpoints of the ranges and any values should be interpreted as approximately the value so stated. With respect to the numerical ranges, the endpoints of the ranges are included in the ranges, the endpoints of the ranges are not included in the ranges, and the individual points are included in the ranges. The ranges can be combined to form new ranges.

[0029] The maximum gas feeding amount, also referred to as a maximum gas treatment amount, refers to the maximum material amount of the gas that can be treated by the micro-interface oscillation absorber in a unit time. In the utility model, the cutting and atomizing effect of the micro-interface oscillation absorber on the absorption liquid is closely related to the actual feeding amount of the gas. When the actual feeding amount of the gas is 70-100% of the maximum gas treatment amount, the absorption liquid in the micro-interface oscillation absorber can be fully cut and atomized, so that the ship flue gas can be efficiently purified. When the actual feeding amount of the gas is ≤70% of the maximum gas treatment amount of the micro-interface oscillation absorber, the cutting and atomizing effect of the absorption liquid in the micro-interface oscillation absorber is obviously poor, so that the ship flue gas is difficult to be efficiently purified.

[0030] The utility model provides a kind of ship flue gas purification system, wherein, the system includes: flue gas introduction device 1, liquid introduction device 2, micro-interface oscillation absorber 3, sediment tank 4 and controller 5;Wherein, the flue gas introduction device 1 and liquid introduction device 2 are connected with the micro-interface oscillation absorber 3 respectively, and the micro-interface oscillation absorber 3 is connected with the sediment tank 4;

[0031] Wherein, the flue gas introduction device 1 includes main pipe 11, branch pipe 12, air draught fan 13, flue gas intelligent regulating valve 14 and air intelligent regulating valve 15, and the main pipe 11 and branch pipe 12 are connected with the air draught fan 13 respectively, and the air draught fan 13 is connected with the micro-interface oscillation absorber 3;The flue gas intelligent regulating valve 14 is arranged on the main pipe 11, and the air intelligent regulating valve 15 is arranged on the branch pipe 12;

[0032] The liquid introduction device 2 includes absorption liquid pump 22, and the absorption liquid pump 22 is connected with the micro-interface oscillation absorber 3;

[0033] Wherein, the controller (5) is connected with the flue gas intelligent regulating valve (14), air intelligent regulating valve (15) and absorption liquid pump (22) respectively, and the like Figure 1 As shown in the figure.

[0034] The utility model discloses a ship flue gas purification system, which comprises a main pipe 11, an air intelligent regulating valve 15, an air liquid introducing device 2 and a micro-interface oscillation absorber 3.

[0035] In a preferred embodiment of the utility model, the branch pipe 12 is arranged on the main pipe 11 and connected with the air draught fan 13 through the main pipe 11.

[0036] In the utility model, the main pipe is used for introducing the ship flue gas, the branch pipe is used for introducing air, the branch pipe is arranged on the main pipe, and the main pipe and the branch pipe share a pipeline, so that the number of inlet settings of the air draught fan can be reduced, and the size of the flue gas purification system is further reduced.

[0037] In a preferred embodiment of the utility model, the flue gas intelligent regulating valve 14 is used for measuring the flow and temperature of the flue gas, and the air intelligent regulating valve 15 is used for adjusting the flow of air.

[0038] In the utility model, the flue gas intelligent regulating valve and the air intelligent regulating valve are not specially limited, and any valve capable of realizing the above functions can be used in the utility model, for example, an American standard pneumatic flange ball valve (BSQ641) and a feedback pneumatic regulating valve (American VTON).

[0039] In a preferred embodiment of the utility model, the liquid introducing device 2 further comprises an absorbent liquid storage tank 21, and the absorbent liquid storage tank 21 is connected with the absorbent liquid pump 22.

[0040] In the utility model, the absorbent liquid storage tank can be used for configuring and storing the absorbent liquid and recycling the regenerated absorbent liquid. The absorbent liquid pump can introduce the absorbent liquid and / or the regenerated absorbent liquid in the absorbent liquid storage tank into the micro-interface oscillation absorber through the water inlet of the micro-interface oscillation absorber.

[0041] In a preferred embodiment of the utility model, the liquid introducing device 2 further comprises a solvent pump 23, and the solvent pump 23 is connected with the absorbent liquid storage tank 21.

[0042] In the utility model, the solvent pump can be placed in the water area where the ship actually travels, for example, a river, a lake or a sea, so that water can be taken locally, and then mixed with the additives such as the activator and the absorbent carried by the ship to configure the absorption liquid. Such a configuration can significantly improve the flexibility of the flue gas purification system.

[0043] In the utility model, the ship flue gas and the absorption liquid are contacted in the micro-interface oscillation absorber, SO X and NO X can enter the absorption liquid from the ship flue gas by chemical reaction with the absorbent in the absorption liquid, and the carbon black can be removed from the ship flue gas under the action of the activator in the absorption liquid. After the ship flue gas is purified in the micro-interface oscillation absorber, the purified gas formed by the ship flue gas can be directly discharged into the atmosphere from the top of the micro-interface oscillation absorber. After the absorption liquid absorbs SO X , NO X and carbon black in the micro-interface oscillation absorber, the impurity removal liquid is formed and discharged from the bottom of the micro-interface oscillation absorber.

[0044] In a preferred embodiment of the utility model, the material of the precipitation tank 4 is selected from wear-resistant and corrosion-resistant materials, preferably one or more of 304, 316L and polytetrafluoroethylene.

[0045] In the utility model, the precipitation tank is used for separating the impurity removal liquid to remove solid impurities and recycle the regenerated absorption liquid. The wear-resistant and corrosion-resistant material can prevent chemical corrosion when the precipitation tank contacts the impurity removal liquid.

[0046] In a preferred embodiment of the utility model, the precipitation tank 4 is further connected to the liquid introduction device 2, and further preferably connected to the absorption liquid storage tank 21.

[0047] In the utility model, the impurity removal liquid contacts the flocculating agent in the precipitation tank, and under the action of the flocculating agent, the carbon black and other particulate matters in the impurity removal liquid can be removed to obtain the regenerated absorption liquid and the sediment. Since the concentrations of the absorbent and the activator in the absorption liquid are much higher than the concentrations of the pollutants in the ship flue gas, the regenerated absorption liquid still has a high absorption state and can be returned to the micro-interface oscillation absorber for recycling. This not only saves resources, but also reduces wastewater discharge, which meets the requirements of environmental protection and sustainable development.

[0048] In a preferred embodiment of the utility model, the micro-interface oscillation absorber (3) comprises a gas phase inlet and a liquid phase inlet; the gas phase inlet is higher than the liquid phase inlet in the position of the micro-interface oscillation absorber (3).

[0049] In a preferred embodiment of the utility model, the air guide fan 13 is connected with the gas phase inlet, and the absorption liquid pump 22 is connected with the liquid phase inlet.

[0050] In a preferred embodiment of the utility model, the precipitation tank 4 further comprises a control valve, wherein the control valve is arranged at the liquid phase outlet.

[0051] In the utility model, the control valve is arranged, so that the precipitate can be conveniently discharged, and the loss of supernatant (i.e. regenerated absorption liquid) in the precipitation tank is avoided.

[0052] In a preferred embodiment of the utility model, the controller (5) is used for transmitting the volume flow and temperature of the ship flue gas monitored by the flue gas intelligent regulating valve (14), the on-off state of the air intelligent regulating valve (15) and the volume flow of the air inlet to the computer control terminal in real time, and adjusting the mass flow of the absorption liquid output by the absorption liquid pump (22) in combination with the concentration of the absorbent and the activator in the absorption liquid.

[0053] In a preferred embodiment of the utility model, the system adopts modular design, is convenient to disassemble and replace, and reduces the maintenance cost.

[0054] In a preferred embodiment of the utility model, the utility model further provides a ship flue gas purification method, wherein the method is carried out in the system of the first aspect of the utility model, and comprises the following steps.

[0055] (1) contacting the ship flue gas raw gas and the absorption liquid in the micro-interface oscillation absorber, carrying out micro-liquid drop interface oscillation absorption, obtaining purified flue gas and impurity removal liquid;

[0056] In the process of introducing the ship flue gas raw gas into the micro-interface oscillation absorber, the flow of the ship flue gas discharged by the ship is monitored in real time.

[0057] When the flow of the ship flue gas discharged by the ship is ≤70% of the maximum gas treatment capacity of the micro-interface oscillation absorber, the air intelligent regulating valve is started, air is introduced into the ship flue gas, and the ship flue gas and the air are used as the ship flue gas raw gas; the introduction amount of the air is such that the flow of the ship flue gas raw gas is 70-100% of the maximum gas treatment capacity of the micro-interface oscillation absorber.

[0058] When the flow of the ship flue gas discharged by the ship is 70-100% of the maximum gas treatment capacity, the air intelligent regulating valve is closed, the ship flue gas is used as the ship flue gas raw gas, and the concentration of the absorbent and the activator in the absorption liquid and the mass flow of the absorption liquid are adjusted according to the monitoring result of the flue gas intelligent regulating valve.

[0059] (2) optionally, the impurity removal solution is contacted with a flocculant in a sedimentation tank to perform sedimentation separation to obtain a regenerated absorption liquid and a sediment;

[0060] (3) optionally, the regenerated absorption liquid is returned to the absorption liquid.

[0061] In step (1):

[0062] In a preferred embodiment of the present application, the absorption liquid comprises an absorbent, an activator and a solvent; wherein the absorbent is used to absorb SO X and NO X in the flue gas, and the activator is used to remove carbon black.

[0063] In a preferred embodiment of the present application, the absorbent is selected from an oxidizing absorbent, and is further preferably selected from one or more of NaClO, NaClO2, KMnO4 and H2O2, and is more preferably NaClO.

[0064] In the present application, the oxidizing absorbent is selected to avoid the consumption of absorbent by carbon dioxide in the flue gas, thereby further improving the removal effect of the absorption liquid on SO X and NO X .

[0065] In a preferred embodiment of the present application, the activator is selected from one or more of sodium dodecyl benzene sulfonate, cetyl trimethyl ammonium bromide, lauryl alcohol polyoxyethylene (9) ether and nonylphenol polyoxyethylene ether, and is preferably lauryl alcohol polyoxyethylene (9) ether.

[0066] In the present application, the activator can increase the wettability of carbon black, reduce the surface tension and viscosity of the absorption liquid, make the absorption liquid more easily broken and atomized, improve the gas-liquid mass transfer coefficient and reaction rate, and further improve the removal efficiency of carbon black.

[0067] In a preferred embodiment of the present application, the solvent is selected from one or more of river water, lake water and sea water.

[0068] In the present application, the water in the water area where the ship travels is used as the solvent, which can realize on-site water collection, can timely adjust the type and amount of the absorbent and the activator in the absorption liquid according to the specific situation, and helps to improve the flexibility of the flue gas purification system.

[0069] In a preferred embodiment of the present application, the outlet temperature of the flue gas discharged by the ship is 100-400℃, and is preferably 100-300℃.

[0070] In an optimal embodiment of the utility model, when the flow of the ship flue gas discharged by the ship is less than or equal to 70% of the maximum gas treatment capacity of the micro-interface oscillation absorber, the concentration of the absorbent is 5-15wt%, preferably 8-12wt%; the concentration of the activator is 0.1-0.5wt%, preferably 0.2-0.3wt%; the ratio of the volume flow rate of the ship flue gas raw gas to the mass flow rate of the absorption liquid is 1Nm 3 / h: 0.1-1.2Kg / h, preferably 1Nm 3 / h: 0.3-0.7Kg / h.

[0071] In the utility model, the introduction of air can reduce the temperature of the ship flue gas discharged by the ship, realize low-temperature feeding of the micro-interface oscillation absorber, and make up for the deficiency of small discharge amount of the ship flue gas discharged by the ship, so that the absorption liquid in the micro-interface oscillation absorber can be fully cut and atomized; however, air can dilute the concentration of the components to be removed (SO X , NO X and carbon black) in the ship flue gas, resulting in a decrease in the gas-liquid mass transfer coefficient and a decrease in the removal efficiency of the components to be removed. The inventors of the utility model have found that after the introduction of air, timely adjustment of the concentration of the absorbent and the activator in the absorption liquid, and limitation of the volume flow rate of the ship flue gas raw gas to the mass flow rate of the absorption liquid within the above range can eliminate the disadvantages caused by air and further improve the removal effect of the micro-interface oscillation absorber on SO X , NO X and carbon black when the discharge amount of the ship flue gas is small.

[0072] In an optimal embodiment of the utility model, when the flow of the ship flue gas discharged by the ship is 70-100% of the maximum gas treatment capacity, the mass flow rate (Q L ) of the absorption liquid and the outlet temperature (T 气 ) of the ship flue gas discharged by the ship, the volume flow rate (Q 气 ) of the ship flue gas raw gas, the concentration (C1) of the absorbent in the absorption liquid and the concentration (C2) of the activator in the absorption liquid satisfy the relationship shown in formula 1: Q L = Q 气 ×K×[1+(T 气 -60℃)×2×10 -3 / ℃]+ m×Q 气 (T 气 -30℃)×C1×C2 formula 1;

[0073] Wherein, the unit of Q L is kg / h, and the unit of Q 气 is Nm 3h, K is a correction coefficient of the ratio of the unit flow rate of the absorption liquid to the unit flow rate of the ship flue gas raw gas, and is 0.45-0.55, and the unit is kg / Nm 3 ; T 气 The unit is ℃, and m is a compensation coefficient of evaporation of the absorption liquid, and the unit is kg / Nm 3 * ℃, and the value range is 0.09-0.11; C1 is 5-15wt%, and C2 is 0.2-0.5wt%.

[0074] In the utility model, the inventor finds that the way of increasing the mass flow of the absorption liquid alone can not solve the problem of the too high feed temperature of the ship flue gas raw gas, and the evaporation loss of the absorption liquid is large in the gas-liquid contact process of the ship flue gas raw gas and the absorption liquid, which can easily lead to the decline of the purification effect. According to the outlet temperature of the ship flue gas and the volume flow of the ship flue gas, and the concentration of the absorbent and the concentration of the activator in the absorption liquid, the mass flow of the absorption liquid is adjusted according to the relationship shown in formula 1, which can effectively solve the problem of the too high feed temperature of the ship flue gas raw gas, and improve the removal effect of SO X , NO X and carbon black of the micro-interface oscillation absorber when the ship flue gas emission is large.

[0075] In a preferred embodiment of the utility model, the K is 0.49-0.51, and the unit is kg / Nm 3 ; the m is 0.095-0.105.

[0076] In a preferred embodiment of the utility model, the content of SO X in the purified flue gas is ≤550 ppm, the content of NO X is ≤350 ppm, and the content of carbon black is ≤500 mg / m 3 .

[0077] The purification method of the ship flue gas provided in the utility model has good removal effects on SO X , NO X and carbon black, the removal rate of SO X is above 96%, the removal rate of NO X is above 95%, and the removal rate of carbon black is above 93%.

[0078] In step (2):

[0079] In a preferred embodiment of the utility model, the mass ratio of the impurity removal liquid to the flocculating agent is 100:0.2-0.8, and preferably 100:0.3-0.5.

[0080] In an optimal embodiment of the present application, the flocculating agent is selected from polyaluminum chloride and / or polyacrylamide. In the present application, the flocculating agent can promote the separation of carbon black.

[0081] In an optimal embodiment of the present application, the operating conditions of the sedimentation separation include: 10-60 min of static state at room temperature after stirring, and then solid-liquid separation.

[0082] In step (3):

[0083] In an optimal embodiment of the present application, the regenerated absorbent is added to the absorbent in whole, and the amount of the absorbent is correspondingly reduced, so that the mass of the mixture of the regenerated absorbent and the absorbent is the same as that when the absorbent is used alone.

[0084] In an optimal embodiment of the present application, the method is performed in the ship flue gas purification system of the first aspect of the present application.

[0085] The present application will be described in detail below through examples. In the examples, the ship flue gas purification system shown in Figure 1 is used. The model of the micro-interface oscillation absorber is XP-200, and the maximum gas treatment capacity is 3000 Nm 3 / h.

[0086] Example 1

[0087] (1) The intelligent flue gas regulating valve monitors the flow rate and temperature of the ship flue gas discharged by the ship in real time. When the ship is running at low speed in the port, the discharge amount of the ship flue gas is 500 Nm 3 / h, and the outlet temperature is 180℃. The air intelligent regulating valve is opened to introduce air into the ship flue gas. After the air and the ship flue gas are mixed, the ship flue gas raw material gas is formed, and the temperature of the ship flue gas raw material gas is 70℃. The ship flue gas raw material gas is introduced into the micro-interface oscillation absorber by the induced draft fan at a flow rate of 3000 Nm 3 / h.

[0088] The solvent pump is started to pump seawater into the absorbent storage tank. The absorbent (NaClO) and the activator (lauryl alcohol polyoxyethylene (9) ether) are added to the absorbent storage tank to obtain an absorbent with an absorbent content of 10wt% and an activator content of 0.2wt%. The absorbent is pumped into the micro-interface oscillation absorber by the absorbent pump at a flow rate of 1500 Kg / h. The ratio K of the flow rate of the ship flue gas raw material gas to the flow rate of the absorbent is 1 Nm 3 / h: 0.5 Kg / h.

[0089] Ship flue gas feedstock and absorbent liquid come into full contact in a micro-interface oscillating absorber, where micro-droplet interface oscillation occurs to obtain purified flue gas and impurity removal liquid. The purified flue gas is discharged directly into the air from the top of the micro-interface oscillating absorber, while the impurity removal liquid is discharged into a settling tank from the bottom of the micro-interface oscillating absorber.

[0090] (2) Add the impurity removal liquid and flocculant (polyaluminum chloride) to the sedimentation tank at a mass ratio of 100:0.3. After stirring, let it stand at room temperature for 30 minutes. Then, open the control valve at the bottom of the sedimentation tank to remove the lower sediment and obtain the upper clear liquid, which is the regeneration absorption liquid.

[0091] (3) All of the above-mentioned regenerated absorbent is returned to the absorbent added in step (1) for recycling.

[0092] Example 2

[0093] (1) The intelligent flue gas regulating valve monitors the flow rate and temperature of the ship's flue gas in real time. When the ship is sailing at high speed on the high seas, the emission amount Q of the ship's flue gas is... 气 2500 Nm 3 / h, outlet temperature T 气 Set the temperature to 350℃; close the intelligent air regulating valve and use the ship's exhaust gas as the raw material gas for ship exhaust gas, at a rate of 2500 Nm³. 3 A flow rate of / h is introduced into the micro-interface oscillation absorber via an induced draft fan;

[0094] Start the solvent pump to pump seawater into the absorbent storage tank. Add absorbent (NaClO) and activator (lauryl alcohol polyoxyethylene (9) ether) to the absorbent storage tank to obtain an absorbent with absorbent content of 12wt% C1 and activator content of 0.5wt% C2. Based on the monitoring results of the flue gas intelligent regulating valve and the concentration of absorbent and activator in the absorbent, adjust the feed rate of the absorbent pump to 2000Kg / h according to the following formula.

[0095] Q L = Q 气 ×K×[1+(T 气 - 60℃) × 2 × 10 -3 ]+ m×Q 气 (T) 气 -30℃) × C1 × C2; where K is 0.5 kg / Nm 3 m is 0.1 kg / Nm 3 *℃; The absorbent is pumped to the micro-interface oscillating absorber at a flow rate of 2023Kg / h via the absorbent pump;

[0096] Ship flue gas feedstock and absorbent liquid come into full contact in a micro-interface oscillating absorber, where micro-droplet interface oscillation occurs to obtain purified flue gas and impurity removal liquid. The purified flue gas is discharged directly into the air from the top of the micro-interface oscillating absorber, while the impurity removal liquid is discharged into a settling tank from the bottom of the micro-interface oscillating absorber.

[0097] (2) Add the impurity removal liquid and flocculant (polyaluminum chloride) to the sedimentation tank at a mass ratio of 100:0.3, and carry out sedimentation separation under normal temperature and pressure conditions to obtain supernatant absorbent liquid and sludge;

[0098] (3) Return all of the above-mentioned regenerated absorbent to the absorbent added in step (1).

[0099] Example 3

[0100] (1) The intelligent flue gas regulating valve monitors the flow rate and temperature of the ship's flue gas in real time. When the ship is sailing at high speed on the high seas, the emission amount Q of the ship's flue gas is... 气 3000 Nm 3 / h, outlet temperature T 气 Set the temperature to 300℃; close the intelligent air regulating valve and use the ship's exhaust gas as the raw material gas for ship exhaust gas, at a rate of 3000 Nm³. 3 A flow rate of / h is introduced into the micro-interface oscillation absorber via an induced draft fan;

[0101] Start the solvent pump to pump seawater into the absorbent storage tank. Add absorbent (NaClO) and activator (lauryl alcohol polyoxyethylene (9) ether) to the absorbent storage tank to obtain an absorbent with absorbent content of 12wt% C1 and activator content of 0.5wt% C2. Based on the monitoring results of the flue gas intelligent regulating valve and the concentration of absorbent and activator in the absorbent, adjust the feed rate of the absorbent pump to 2268 Kg / h according to the following formula.

[0102] Q L = Q 气 ×K×[1+(T 气 - 60℃) × 2 × 10 -3 ]+ m×Q 气 (T) 气 -30℃) × C1 × C2; where K is 0.5 kg / Nm 3 m is 0.1 kg / Nm 3 *℃; The absorbent is pumped to the micro-interface oscillating absorber at a flow rate of 2268Kg / h via the absorbent pump;

[0103] Ship flue gas feedstock and absorbent liquid come into full contact in a micro-interface oscillating absorber, where micro-droplet interface oscillation occurs to obtain purified flue gas and impurity removal liquid. The purified flue gas is discharged directly into the air from the top of the micro-interface oscillating absorber, while the impurity removal liquid is discharged into a settling tank from the bottom of the micro-interface oscillating absorber.

[0104] (2) Add the impurity removal liquid and flocculant (polyaluminum chloride) to the sedimentation tank at a mass ratio of 100:0.3, and carry out sedimentation separation under normal temperature and pressure conditions to obtain supernatant absorbent liquid and sludge;

[0105] (3) Return all of the above-mentioned regenerated absorbent to the absorbent added in step (1).

[0106] Example 4

[0107] (1) The intelligent flue gas regulating valve monitors the flow rate and temperature of the ship's flue gas in real time. When the ship is sailing at high speed on the high seas, the emission amount Q of the ship's flue gas is... 气 2200 Nm 3 / h, outlet temperature T 气 Set the temperature to 280℃; close the intelligent air regulating valve and use the ship's exhaust gas as the raw material gas for ship exhaust gas, at a temperature of 2200 Nm³. 3 A flow rate of / h is introduced into the micro-interface oscillation absorber via an induced draft fan;

[0108] Start the solvent pump to pump seawater into the absorbent storage tank. Add absorbent (NaClO) and activator (lauryl alcohol polyoxyethylene (9) ether) to the absorbent storage tank to obtain an absorbent with absorbent content of 11wt% C1 and activator content of 0.4wt% C2. Based on the monitoring results of the flue gas intelligent regulating valve and the concentration of absorbent and activator in the absorbent, adjust the feed rate of the absorbent pump to 1608 Kg / h according to the following formula.

[0109] Q L = Q 气 ×K×[1+(T 气 - 60℃) × 2 × 10 -3 ]+ m×Q 气 (T) 气 -30℃) × C1 × C2; where K is 0.5 kg / Nm 3 m is 0.1 kg / Nm 3 *℃; The absorbent is pumped to the micro-interface oscillating absorber at a flow rate of 1608 Kg / h via the absorbent pump;

[0110] The ship flue gas raw material gas and the absorption liquid are fully contacted in the micro-interface oscillation absorber, micro-liquid droplet interface oscillation is carried out, purified flue gas and impurity removal liquid are obtained; wherein, the purified flue gas is directly discharged into the air from the top of the micro-interface oscillation absorber, and the impurity removal liquid is discharged into the sedimentation tank from the bottom of the micro-interface oscillation absorber;

[0111] (2) The impurity removal liquid and the flocculating agent (polyaluminum chloride) are added into the sedimentation tank at a mass ratio of 100:0.3, and the sedimentation separation is carried out at normal temperature and pressure, to obtain supernatant absorption liquid and sediment;

[0112] (3) The above regenerated absorption liquid is all returned and added into the absorption liquid in step (1).

[0113] Comparative Example 1

[0114] Compared with Example 1, the difference lies in that air is not introduced.

[0115] (1) The ship flue gas intelligent regulating valve monitors the flow and temperature of the ship flue gas discharged by the ship in real time. When the ship is running at low speed in the port, the discharge amount of the ship flue gas is 500 Nm 3 / h, and the outlet temperature is 170℃; the ship flue gas is taken as the ship flue gas raw material gas, and is introduced into the micro-interface oscillation absorber by the induced draft fan at a flow rate of 500 Nm 3 / h;

[0116] The solvent pump is started, and seawater is pumped into the absorption liquid storage tank. The absorbent (NaClO) and the activator (lauryl alcohol polyoxyethylene (9) ether) are added into the absorption liquid storage tank, to obtain the absorption liquid with the absorbent content of 10wt% and the activator content of 0.2wt%. The absorption liquid is pumped into the micro-interface oscillation absorber by the absorption liquid pump at a flow rate of 1500 Kg / h, wherein the ratio of the flow rates of the ship flue gas raw material gas and the absorption liquid is 1 Nm 3 / h:0.5 Kg / h;

[0117] The ship flue gas raw material gas and the absorption liquid are fully contacted in the micro-interface oscillation absorber, micro-liquid droplet interface oscillation is carried out, purified flue gas and impurity removal liquid are obtained; wherein, the purified flue gas is directly discharged into the air from the top of the micro-interface oscillation absorber, and the impurity removal liquid is discharged into the sedimentation tank from the bottom of the micro-interface oscillation absorber;

[0118] (2) The impurity removal liquid and the flocculating agent (polyaluminum chloride) are added into the sedimentation tank at a mass ratio of 100:0.3, and the sedimentation separation is carried out at normal temperature and pressure, to obtain supernatant absorption liquid and sediment;

[0119] (3) The above regenerated absorption liquid is all returned and added into the absorption liquid in step (1).

[0120] Comparative Example 2

[0121] Compared with Example 2, the difference lies in that the mass flow rate (Q L ) of the absorption liquid does not satisfy the relationship shown in formula 1, and the absorption liquid is pumped to the micro-interface oscillation absorber by the absorption liquid pump at a flow rate of 1500 Kg / h.

[0122] Test Example 1

[0123] According to the “GB 15097-2016 standard”, the contents of SO X , NO X and carbon black in the ship flue gas and the purified flue gas discharged in Examples 1-2 and Comparative Examples 1-2 are measured, and the removal rates of the respective are calculated, and the calculation results are shown in Table 1:

[0124] Table 1

[0125]

[0126] It can be known from Comparative Examples 1-4 that the system in the utility model is used for purifying the ship flue gas, which can effectively solve the problem of unstable purification effect of the micro-interface oscillation absorber on the ship flue gas caused by large fluctuation of the flue gas flow, so that the ship flue gas can be effectively purified at all times.

[0127] It can be known from Comparative Examples 1 and 2 that when the flow rate of the ship flue gas discharged by the ship is ≤70% of the maximum gas treatment capacity of the micro-interface oscillation absorber, the system in the utility model is used for purifying the ship flue gas, air is introduced, and the concentration of the absorbent and the activator in the absorption liquid and the volume flow rate of the ship flue gas raw gas and the mass flow rate of the absorption liquid are adjusted in time, which can significantly improve the removal effect of the micro-interface oscillation absorber on SO X , NO X and carbon black when the ship flue gas discharge amount is small.

[0128] It can be known from Comparative Examples 2 and 2 that when the flow rate of the ship flue gas discharged by the ship is 70-100% of the maximum gas treatment capacity, the system in the utility model is used for purifying the ship flue gas, and according to the outlet temperature of the ship flue gas discharged by the ship and the volume flow rate of the ship flue gas raw gas, and the concentration of the absorbent and the concentration of the activator in the absorption liquid, the mass flow rate of the absorption liquid is adjusted according to the relationship shown in formula 1, which can effectively solve the problem of too high feed temperature of the ship flue gas raw gas, thereby significantly improving the removal effect of the micro-interface oscillation absorber on SO X , NO X and carbon black when the ship flue gas discharge amount is large.

[0129] The preferred embodiments of the present application are described in detail above, but the present application is not limited thereto. Within the technical concept of the present application, various simple modifications can be made to the technical solution of the present application, including the combination of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as disclosed content of the present application, and all belong to the protection scope of the present application.

Claims

1. A ship exhaust gas cleaning system, characterized in that The system comprises a flue gas introduction device (1), a liquid introduction device (2), a micro-interface oscillation absorber (3), a precipitation tank (4) and a controller (5); wherein the flue gas introduction device (1) and the liquid introduction device (2) are connected with the micro-interface oscillation absorber (3) respectively, and the micro-interface oscillation absorber (3) is connected with the precipitation tank (4); Wherein, the flue gas introduction device (1) comprises a main pipe (11), a branch pipe (12), a draft fan (13), a flue gas intelligent regulating valve (14) and an air intelligent regulating valve (15), the main pipe (11) and the branch pipe (12) are connected with the draft fan (13) respectively, and the draft fan (13) is connected with the micro-interface oscillation absorber (3); the flue gas intelligent regulating valve (14) is arranged on the main pipe (11), and the air intelligent regulating valve (15) is arranged on the branch pipe (12); Wherein, the liquid introduction device (2) comprises an absorption liquid pump (22), and the absorption liquid pump (22) is connected with the micro-interface oscillation absorber (3); Wherein, the controller (5) is connected with the flue gas intelligent regulating valve (14), the air intelligent regulating valve (15) and the absorption liquid pump (22) respectively.

2. Marine exhaust gas cleaning system according to claim 1, characterized in that The branch pipe (12) is arranged on the main pipe (11) and connected with the draft fan (13) through the main pipe (11).

3. Marine exhaust gas cleaning system according to claim 1 or 2, characterized in that, The flue gas intelligent regulating valve (14) is used for measuring the flow and temperature of flue gas, and the air intelligent regulating valve (15) is used for adjusting the flow of air.

4. The marine exhaust gas cleaning system according to claim 1, characterized in that, The liquid introduction device (2) further comprises an absorption liquid storage tank (21); wherein the absorption liquid storage tank (21) is connected with the absorption liquid pump (22).

5. A marine exhaust gas cleaning system according to claim 4, characterized in that, The liquid introduction device (2) further comprises a solvent pump (23); wherein the solvent pump (23) is connected with the absorption liquid storage tank (21).

6. The marine exhaust gas cleaning system according to claim 1, characterized in that, The micro-interface oscillation absorber (3) comprises a gas phase inlet and a liquid phase inlet; the position of the gas phase inlet in the micro-interface oscillation absorber (3) is higher than that of the liquid phase inlet.

7. A marine exhaust gas cleaning system according to claim 6, c h a r a c t e r i s e d in that The draft fan (13) is connected with the gas phase inlet, and the absorption liquid pump (22) is connected with the liquid phase inlet.

8. The marine exhaust gas cleaning system according to claim 4, characterized in that, The precipitation tank (4) is connected with the absorption liquid storage tank (21).

9. The marine exhaust gas cleaning system according to claim 1, characterized in that, The precipitation tank (4) further comprises a control valve, wherein the control valve is arranged at the liquid phase outlet.

10. The marine exhaust gas cleaning system according to claim 1, characterized in that, The controller (5) is used for transmitting the volume flow and temperature of ship flue gas monitored by the flue gas intelligent regulating valve (14), the on-off state of the air intelligent regulating valve (15) and the volume flow of air inlet to a computer control terminal in real time, and adjusting the mass flow of absorption liquid output by the absorption liquid pump (22) in combination with the concentrations of absorbent and activator in the absorption liquid.

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