WO2017067087A1 - 锅炉排烟海水填料洗涤脱硫方法及洗涤装置 - Google Patents

锅炉排烟海水填料洗涤脱硫方法及洗涤装置 Download PDF

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WO2017067087A1
WO2017067087A1 PCT/CN2015/100083 CN2015100083W WO2017067087A1 WO 2017067087 A1 WO2017067087 A1 WO 2017067087A1 CN 2015100083 W CN2015100083 W CN 2015100083W WO 2017067087 A1 WO2017067087 A1 WO 2017067087A1
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washing
seawater
flue gas
filler
packing
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PCT/CN2015/100083
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English (en)
French (fr)
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彭斯干
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彭斯干
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact

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  • the invention relates to a method and a washing device for washing and desulfurizing a boiler seawater filling seawater, and uses the seawater washing to reduce atmospheric sulfur pollutants mainly composed of sulfur dioxide in the flue gas of the boiler, and belongs to the technical field of clean energy of flue gas desulfurization of a coal-fired power plant.
  • seawater washing and desulfurization process In the past 20 years, with the increasing global environmental resources, the demand for seawater washing and desulfurization process has been increasing year by year. This is because the seawater washing process can reduce the cost of high-efficiency and low-efficiency industrial combustion devices, especially coal-fired power plants. Air pollutants and friendly to the marine ecosystem.
  • the seawater-only desulfurization process also known as “seawater flue gas desulfurization technology", “NSW FGD”, or simply “seawater desulfurization”, etc., is characterized by the use of seawater to wash industrial flue gas.
  • the seawater includes natural seawater directly extracted from the ocean, and also includes seawater extracted from the ocean for use in industrial facility cooling but still having a certain alkalinity.
  • seawater is used as a washing desulfurization medium
  • it is used in a conventional desulfurization process flow using an alkaline chemical raw material as a washing desulfurization medium, and a spray tower dedicated to a conventional desulfurization process is used.
  • a seawater washing unit even in the same way as the conventional desulfurization process, an aeration process is provided inside the washing unit, thus causing the following problems:
  • a cooling/reheating device is provided to pre-cool the flue gas, resulting in an increase in operating energy consumption and maintenance costs, and a loss of low-cost economic advantages of seawater washing technology;
  • the invention aims to overcome the deficiencies of the prior art, and provides a seawater washing desulfurization method and a washing device for a boiler exhaust gas, and further optimizes the filler washing and desulfurization technical scheme by improving and upgrading a plurality of technical parameters of the filler washing device.
  • the technical proposal of the method for washing and desulfurization of the boiler flue gas seawater filler of the invention comprises the following steps:
  • a method for washing and desulfurizing a boiler flue gas seawater filling which comprises introducing boiler flue gas and sea water to a washing device, washing flue gas with seawater in the washing device, discharging the purified flue gas and washing seawater after washing, and discharging the acidity
  • the seawater is transported to the seawater quality recovery device and finally discharged to the sea;
  • the washing of the flue gas by seawater in the washing device is the washing of the filler by the packing layer in the packing washing device, and the packing washing device comprises a dry packing factor of 20
  • the washing layer of ⁇ 1000/m, the washing time of the flue gas passing through the packing layer is 0.5-10 seconds;
  • the washing of the filler by the packing layer is to directly introduce the boiler flue gas with the temperature of 100° C. to 190° C. into the packing layer.
  • the washing is carried out, and the washing of the filler is carried out under the condition that the external atmosphere is sealed with a water seal.
  • the filler layer is provided with a temperature resistance section at the inlet end of the flue gas, the height of the temperature resistant section is greater than 5 ⁇ of the total height of the filler layer, and the temperature resistant section filler and the structural material withstand temperature ⁇ 100 °C.
  • the seawater washing desulfurization method is introduced into the seawater of the packing washing device, and the flow rate is selected in a range of a ratio of the boiler flue gas flow rate to the seawater flow rate of 30 to 1000, wherein the unit of the boiler flue gas flow rate is Nm 3 /h, sea water The flow unit is m 3 /h.
  • the filler washing is an efficient low pressure drop washing in which the pressure of the flue gas passes through the packing layer is less than 1500 Pa.
  • the technical scheme of the seawater washing device for the boiler flue gas seawater washing and desulfurization method of the invention comprises: a casing, wherein the casing is provided with a packing layer with a dry packing factor of 20-1000/m, and a lower temperature end of the packing layer is provided,
  • the temperature resistance section is composed of It is composed of packing or / and structural parts with temperature ⁇ 100 °C.
  • the height of the temperature resistant section is greater than 5 ⁇ of the total height of the packing layer.
  • the material of the temperature resistant section is selected from metals, ceramics and plastics.
  • the total height of the packing layer is the product of the time when the boiler flue gas passes through the packing layer and the filling point gas velocity, and the time is 0.5 to 10 seconds.
  • the technical effect of the invention is remarkable, and the boiler flue gas with a smoke temperature of 100 ° C to 190 ° C can be directly treated, and the sulfur dioxide emission in the flue gas is reduced by 99%, and the cooling/reheating system is omitted, and there is no chemical additive and harmful by-products, so that the system Cost and operating costs have been reduced overall, while the reliability and operating rates of abatement facilities have increased significantly.
  • FIG. 1 is a schematic view showing the process flow of a method for washing a smoked seawater filler of the present invention.
  • Fig. 2 is a schematic view showing an embodiment of the smoke exhausting seawater washing apparatus of the present invention.
  • Figure 3a is a schematic diagram of a flat ring packing, the packing factor of the packing into a packing layer is 80 ⁇ 800;
  • Figure 3b is a schematic diagram of a stepped ring packing having a packing factor of 50 to 300 in the packing layer.
  • FIG. 4 is a schematic diagram of a prior art seawater washing technical solution, including: washing seawater lifting pump and pipeline, flue gas pre-cooling/reheating device (GGH), spray tower of traditional process, and tower aeration facility of traditional process Wait.
  • GGH flue gas pre-cooling/reheating device
  • Embodiment 1 It is a basic embodiment of the method for washing and desulfurizing the seawater filling of the boiler of the present invention, the steps of which are to introduce boiler flue gas and sea water to the washing device, and to wash the flue gas with seawater in the washing device, and to purify the purified flue gas after washing.
  • the gas and washing seawater are discharged from the washing device, and the discharged acidic seawater is sent to the seawater quality recovery device and finally discharged to the sea; the washing of the flue gas by seawater in the washing device is the washing of the filler through the packing layer in the filling washing device.
  • the filler washing device comprises a packing layer with a dry packing factor of 20-1000/m, the washing time of the flue gas passing through the packing layer is 0.5-10 seconds; the dry packing factor is a/ ⁇ 3 , wherein a is a packing layer Total specific surface area, the unit is m 2 /m 3 , ⁇ is the ratio of the void volume of the filler layer to the volume of the filler layer, the unit is m 3 /m 3 ; the washing of the filler by the filler layer is the temperature of 100 ° C
  • the boiler flue gas to 190 ° C is directly introduced into the washing of the packing layer, which is washing under the condition that the external atmosphere is sealed with a water seal. Since the dry filler factor and the washing time affect the filler washing effect, the present invention proposes parameters for the dry filler factor and washing time.
  • the main difference between the prior art solution represented by FIG. 4 and the technical solution of the present invention is as follows: 1.
  • the traditional desulfurization process relying on alkaline chemical raw materials, in order to avoid fouling blockage, the special washing tower must adopt a large void ratio and gas.
  • the effect of the invention is fully considered; and the technical solution of the invention proposed by the seawater washing process mechanism is fully realized, and the technical effect of absorbing sulfur dioxide by ultra-low cost and high efficiency is realized; 2.
  • the prior art of the prior art is aerating the inside of the washing device by a conventional process.
  • the sulfur dioxide product dissolved in the washed seawater is reversely reacted, and as a result, the newly absorbed sulfur dioxide is driven out again, and the absorption effect is further deteriorated.
  • the washing of the filler according to the present invention is carried out under the condition that the external atmosphere is sealed by a water seal, thereby ensuring the high absorption efficiency of sulfur dioxide; 3.
  • the conventional process washing unit adopted in the prior art such as FIG.
  • Embodiment 2 It is a further embodiment based on Embodiment 1.
  • the filler layer is provided with a temperature resistance section at the inlet end of the flue gas, the height of the temperature resistant section is greater than 5 ⁇ of the total height of the filler layer, and the temperature resistant section filler and the structural material withstand temperature ⁇ 100° C.
  • the seawater introduced into the packing washing device is selected in the range of the ratio of the boiler flue gas flow to the seawater flow rate of 30 to 1000, wherein the unit of the boiler flue gas flow is Nm 3 /h, and the seawater flow unit is m 3 / h.
  • the filler washing is carried out under the condition that the external atmosphere is sealed by a water seal, and the pressure drop of the flue gas through the packing layer is less than 1500 Pa.
  • Embodiment 3 A preferred embodiment based on Embodiment 2.
  • the washing desulfurization method introduces the boiler flue gas into the washing device by directly introducing the flue gas having a flue temperature of 130 ° C into the packing layer of the washing device, and the flow rate of the flue gas introduced into the boiler is 2800000 Nm 3 /h, the flue gas flow rate and the sea water flow rate.
  • the ratio is selected to be 200; the flue gas and seawater are passed through the packing layer 8 in a countercurrent manner in the packing washing device; the packing factor of the packing layer 8 is 30-900/m, the height is 5 m, and the height of the temperature-resistant section 9 is 40 cm.
  • the packing layer 8 It consists of a polytetrafluoroethylene Pall ring with a temperature of 160 ° C; the time for the flue gas to pass through the packing layer 8 is 2 seconds.
  • the filler factor is 40 to 800 / m, or 50 to 600 / m, there are two other different embodiments.
  • Embodiment 4 is a basic embodiment of a seawater washing device for a boiler flue gas seawater washing and desulfurization method of the present invention. As shown in Figures 2, 3a and 3b, it comprises a casing 1 having a dry packing factor set therein. 20 to 1000 packing layer 8, the lower end of the packing layer 8 is provided with a temperature resistant section 9, which is composed of a packing or / and structural member with a temperature ⁇ 100 ° C, and the height of the temperature resistant section is greater than the total height of the packing layer 5 ⁇ , the temperature resistant section material is selected from metals, ceramics and plastics.
  • the total height of the packing layer 8 is the product of the time during which the boiler flue gas passes through the packing layer and the filling point gas velocity, which is 0.5 to 10 seconds.
  • Still another embodiment is the use of an embodiment of a flat ring packing as shown in Figure 3a, the packing factor of the packing into a packing layer is 80-800 / m; the application of a step ring packing as shown in Figure 3b
  • the filler has a filler layer of 50 to 300/m.
  • Embodiment 5 A preferred embodiment based on Embodiment 4.
  • the seawater washing device, the non-temperature resistant section filler of the packing layer 8 is formed by stacking a step ring packing with a packing factor of 300 selected in the chemical design manual, and the temperature resistant section is formed.
  • the modified polystyrene Raschig ring is piled up; the general part design of the washing device of the present invention is carried out according to the chemical design manual regarding the packed tower design part.

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  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
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Abstract

一种利用海水和填料对锅炉排烟洗涤脱硫的方法及洗涤装置。方法包括向洗涤装置导入锅炉烟气和海水，在洗涤装置中用海水洗涤烟气，将洗涤后的净化烟气和洗涤海水排出洗涤装置，排出的酸性海水经海水水质恢复装置（16）后排往大海；在洗涤装置中用海水洗涤烟气是在填料洗涤装置中通过填料层（8）进行的填料洗涤，填料洗涤装置包括干填料因子为20～1000/m的填料层（8）。

Description

锅炉排烟海水填料洗涤脱硫方法及洗涤装置 技术领域
本发明涉及锅炉排烟海水填料洗涤脱硫方法及洗涤装置，使用海水洗涤减排锅炉烟气中以二氧化硫为主的大气污染物，属于燃煤电厂烟气脱硫的清洁能源技术领域。
背景技术
近20年来，随着全球环境资源问题的日益突出，对于海水洗涤脱硫工艺的需求逐年提升，这是由于海水洗涤工艺可以超低成本高效减排工业燃烧装置特别是燃煤电厂以二氧化硫为主的大气污染物，并对海洋生态环境友好。所述的仅用海水洗涤脱硫工艺，也称为“海水法烟气脱硫技术”、“NSW FGD”，甚至被简称为“海水脱硫”等等，其关键特征是使用海水洗涤工业烟气。所述的海水，包括从海洋直接提取的天然海水，也包括从海洋提取用于工业设施冷却等用途但仍有一定碱度的海水。
但在如附图4所示的现有技术中，虽然使用海水作为洗涤脱硫介质，却沿用以碱性化工原料作为洗涤脱硫介质的传统脱硫工艺流程，并采用传统脱硫工艺专用的喷淋塔用作海水洗涤单元，甚至和传统脱硫工艺一样，在洗涤单元内部设置曝气工序，因而造成以下问题：
1)吸收二氧化硫效果不佳，污染减排达不到要求，丧失海水洗涤工艺高效减排的环保优势；
2)为改善吸收效果而增加海水喷淋密度，以及增加烟气进口压力以抵消增加喷淋密度引起的阻力；而且由于传统洗涤单元不能直接处理烟温高于100℃的锅炉烟气，还另设冷却/再热装置以预先冷却烟气，结果导致运行能耗和维护成本升高，丧失海水洗涤技术的低成本经济优势；
还有类似的现有技术，由于增加喷淋密度仍不解决问题，不得不在海水洗涤系统中添加碱性化工原料，以致失去对海洋生态环境友好的优势，其使用受到限制。
而另有专利号为ZL 95119389.9的中国专利，公开了对锅炉烟气仅用海水进行填料洗涤脱硫的技术方案，但由于较为初步，人们对该类技术方案的提升和优化产生进一步期待。
发明内容
本发明目的在于，克服现有技术的不足，提供一种锅炉排烟使用海水洗涤脱硫方法及洗涤装置，通过对填料洗涤装置多项技术参数的改进、提升，进一步优化填料洗涤脱硫技术方案，实现仅用海水洗涤，高效低成本减排锅炉烟气中以二氧化硫为主的大气污染物，充分发挥海水洗涤工艺减排效果好、成本低的环境及经济优势。
本发明锅炉排烟海水填料洗涤脱硫方法技术方案包括下述步骤：
一种锅炉排烟海水填料洗涤脱硫方法，它包括向洗涤装置导入锅炉烟气和海水，在洗涤装置中用海水洗涤烟气、将洗涤后的净化烟气和洗涤海水排出洗涤装置、排出的酸性海水输往海水水质恢复装置最终排往大海；所述的在洗涤装置中用海水洗涤烟气是在填料洗涤装置中通过填料层进行的填料洗涤，所述的填料洗涤装置包括干填料因子为20～1000/m的填料层，烟气通过填料层的洗涤时间为0.5～10秒；所述的通过填料层进行的填料洗涤，是将温度为100℃至190℃的锅炉烟气直接导入填料层进行的洗涤，所述的填料洗涤是在用水封隔绝外部大气的条件下进行的洗涤。
进一步的技术方案是：
所述的海水洗涤脱硫方法，其填料层在烟气进入端设置耐温段，该耐温段的高度大于填料层总高度的5‰，耐温段填料和结构材料耐受温度≥100℃。
所述的海水洗涤脱硫方法，其导入填料洗涤装置的海水，流量在锅炉烟气流量与海水流量的比值为30～1000的范围内选取，其中锅炉烟气流量的单位为Nm3/h，海水流量单位为m3/h。
所述的海水洗涤脱硫方法，其填料洗涤是烟气通过填料层的压力降小于1500Pa的高效低压降洗涤。
本发明锅炉排烟海水填料洗涤脱硫方法的海水洗涤装置技术方案是：它包括壳体，该壳体内设置有干填料因子为20～1000/m的填料层，填料层下端设置有耐温段，该耐温段由 耐受温度≥100℃的填料或/和结构件组成，耐温段高度大于填料层总高度的5‰，耐温段材质选自于金属、陶瓷及塑料。
进一步的技术方案是：所述的海水洗涤装置，其填料层的总高度为锅炉烟气通过填料层的时间与填料泛点气速的乘积，所述的时间为0.5～10秒。
本发明锅炉排烟海水填料洗涤脱硫方法及洗涤装置的技术效果显著：
本发明的技术效果显著，可以直接处理烟温100℃至190℃的锅炉烟气，减少烟气中99％的二氧化硫排放，同时省略冷却/再热系统，没有化学添加剂和有害副产物，使得系统造价和运行成本全面降低，而减排设施的可靠性和运行率则大幅提高。
附图说明
图1是本发明排烟海水填料洗涤方法的工艺流程示意图。
图2是本发明排烟海水填料洗涤装置的一个实施例示意图。
图3a是一种扁环填料示意图，该填料堆成填料层的填料因子是80～800；
图3b是一种阶梯环填料示意图，该填料堆成填料层的填料因子为50～300。
图4是一种现有海水洗涤技术方案的示意图，包括：洗涤海水提升泵和管线、烟气预冷却/再热装置(GGH)、传统工艺的喷淋塔、传统工艺的塔内曝气设施等。
附图中所示的图号标记对应的相关部件或结构的名称为：
1—壳体，2—烟气导入口，3—洗涤海水注入口，4—净化烟气排出口，5—酸性海水排出口，6—除雾器，7—布水器，8—填料层，9—填料层耐温段，10—水封池，11—锅炉，12—除尘器，13—引风机，14—海水提升泵，15—烟囱，16—水质恢复装置。
具体实施方式
结合附图和实施例对本发明的锅炉排烟海水填料洗涤方法及洗涤装置作进一步说明如下：
实施例1：是本发明锅炉排烟海水填料洗涤脱硫方法的基本实施例，它的步骤是向洗涤装置导入锅炉烟气和海水，在洗涤装置中用海水洗涤烟气、将洗涤后的净化烟气和洗涤海水排出洗涤装置、排出的酸性海水输往海水水质恢复装置最终排往大海；所述的在洗涤装置中 用海水洗涤烟气是在填料洗涤装置中通过填料层进行的填料洗涤，所述的填料洗涤装置包括干填料因子为20～1000/m的填料层，烟气通过填料层的洗涤时间为0.5～10秒；所述干填料因子为a/ε3，其中a为填料层的总比表面积，单位是m2/m3，ε为填料层空隙体积与填料层体积的比值，单位是m3/m3；所述的通过填料层进行的填料洗涤，是将温度为100℃至190℃的锅炉烟气直接导入填料层进行的洗涤，所述的填料洗涤是在用水封隔绝外部大气的条件下进行的洗涤。由于干填料因子和洗涤时间影响填料洗涤效果，本发明提出适用干填料因子和洗涤时间的参数。
附图4所代表的现有技术方案与本发明技术方案的主要区别在于：1、依靠碱性化工原料的传统脱硫工艺，为避免结垢堵塞，其专用洗涤塔必须采用空隙率极大、气液接触面很小的空心结构；而海水洗涤的溶解机理则要求很大的气液接触面积，如果与附图4等现有技术一样采用空心喷淋塔，必然造成传质强度不足，二氧化硫吸收效果不佳；而充分考虑海水洗涤工艺机理提出的本发明技术方案，实现了超低成本高效率吸收二氧化硫的技术效果；2、附图4等现有技术将传统工艺在洗涤装置内部曝气的技术方案用于海水洗涤，就会使洗涤海水溶解下来的二氧化硫产物发生逆反应，结果将刚吸收的二氧化硫又赶出来，使吸收效果进一步劣化。而本发明所述的填料洗涤，则是在用水封隔绝外部大气的条件下进行的洗涤，因此保证了二氧化硫的高吸收效率；3、附图4等现有技术采用的传统工艺洗涤单元，不能直接处理烟温高于100℃的锅炉烟气，必须另设冷却/再热装置以预先冷却烟气，结果导致制造和运行成本升高；本发明洗涤装置可将温度为100℃至190℃的锅炉烟气直接导入填料层进行洗涤，因此制造和运行成本低，具有较高的经济优势。
实施例2：是在实施例1基础上的进一步实施例。所述的洗涤脱硫方法，其填料层，在烟气进入端设置耐温段，该耐温段的高度大于填料层总高度的5‰，耐温段填料和结构材料耐受温度≥100℃。所述导入填料洗涤装置的海水，其流量在锅炉烟气流量与海水流量的比值为30～1000的范围内选取，其中锅炉烟气流量的单位为Nm3/h，海水流量单位为m3/h。所述的填料洗涤是在用水封隔绝外部大气的条件下进行的，烟气通过填料层的压力降小于1500Pa。
实施例3：是在实施例2基础上的优选实施例。所述的洗涤脱硫方法，向洗涤装置导入 锅炉烟气是将烟温为130℃的烟气直接导入洗涤装置的填料层，导入锅炉烟气的流量为2800000Nm3/h，烟气流量与海水流量的比值选取为200；使烟气和海水在填料洗涤装置内以逆流方式通过填料层8；填料层8的填料因子为30～900/m，高度为5m，耐温段9的高度为40cm，由耐受温度160℃的聚四氟乙烯鲍尔环组成；烟气通过填料层8的时间为2秒。当填料因子为40～800/m，或50～600/m时，则是另外两个不同的实施例。
实施例4：是本发明锅炉排烟海水填料洗涤脱硫方法的海水洗涤装置的基本实施例，如附图2、3a、3b所示，它包括壳体1，该壳体内设置有干填料因子为20～1000的填料层8，填料层8下端设置有耐温段9，该耐温段由耐受温度≥100℃的填料或/和结构件组成，耐温段高度大于填料层总高度的5‰，耐温段材质选自于金属、陶瓷及塑料。填料层8的总高度为锅炉烟气通过填料层的时间与填料泛点气速的乘积，所述的时间为0.5～10秒。还有实施例是：应用如图3a所示一种扁环填料的实施例，该填料堆成填料层的填料因子为80～800/m；应用如图3b所示一种阶梯环填料的实施例，该填料堆成填料层的填料因子为50～300/m。
实施例5：是在实施例4基础上的优选实施例。如图1、图2所示，所述的海水洗涤装置，填料层8的非耐温段填料，由化工设计手册中选择的一种填料因子为300的阶梯环填料堆积而成，耐温段由改性聚苯乙烯拉西环堆成；本发明洗涤装置通用部分设计，参照化工设计手册有关填料塔设计部分进行。
本发明的权利要求保护范围不限于上述实施例。

Claims (6)

  1. 一种锅炉排烟海水填料洗涤脱硫方法，它包括向洗涤装置导入锅炉烟气和海水，在洗涤装置中用海水洗涤烟气、将洗涤后的净化烟气和洗涤海水排出洗涤装置、排出的酸性海水输往海水水质恢复装置最终排往大海；其特征在于，所述的在洗涤装置中用海水洗涤烟气是在填料洗涤装置中通过填料层进行的填料洗涤，所述的填料洗涤装置包括干填料因子为20～1000/m的填料层，烟气通过填料层的洗涤时间为0.5～10秒；所述的通过填料层进行的填料洗涤，是将温度为100℃至190℃的锅炉烟气直接导入填料层进行的洗涤，所述的填料洗涤是在用水封隔绝外部大气的条件下进行的洗涤。
  2. 根据权利要求1所述的海水洗涤脱硫方法，其特征在于，所述的填料层在烟气进入端设置耐温段，该耐温段的高度大于填料层总高度的5‰，耐温段填料和结构材料耐受温度≥100℃。
  3. 根据权利要求1所述的海水洗涤脱硫方法，其特征在于，所述导入填料洗涤装置的海水，其流量在锅炉烟气流量与海水流量的比值为30～1000的范围内选取，其中锅炉烟气流量的单位为Nm3/h，海水流量单位为m3/h。
  4. 根据权利要求1所述的海水洗涤脱硫方法，其特征在于，所述的填料洗涤，是烟气通过填料层的压力降小于1500Pa的高效低压降洗涤。
  5. 用于权利要求1所述锅炉排烟海水填料洗涤脱硫方法的海水洗涤装置，其特征在于，它包括壳体(1)，该壳体内设置有干填料因子为20～1000/m的填料层(8)，填料层(8)下端设置有耐温段(9)，该耐温段由耐受温度≥100℃的填料或/和结构件组成，耐温段高度大于填料层总高度的5‰，耐温段材质选自于金属、陶瓷及塑料。
  6. 根据权利要求5所述的海水洗涤装置，其特征在于，填料层(8)的总高度为锅炉烟气通过填料层的时间与填料泛点气速的乘积，所述的时间为0.5～10秒。
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