WO2014067239A1 - 一种scr板式脱硝催化剂连续生产装置及生产工艺 - Google Patents

一种scr板式脱硝催化剂连续生产装置及生产工艺 Download PDF

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Publication number
WO2014067239A1
WO2014067239A1 PCT/CN2013/001327 CN2013001327W WO2014067239A1 WO 2014067239 A1 WO2014067239 A1 WO 2014067239A1 CN 2013001327 W CN2013001327 W CN 2013001327W WO 2014067239 A1 WO2014067239 A1 WO 2014067239A1
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Prior art keywords
machine
catalyst
stage
leveling
pinch
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PCT/CN2013/001327
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English (en)
French (fr)
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张景文
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北京华电光大新能源环保技术有限公司
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Priority to KR1020157013200A priority Critical patent/KR101706881B1/ko
Publication of WO2014067239A1 publication Critical patent/WO2014067239A1/zh
Priority to IN3945DEN2015 priority patent/IN2015DN03945A/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/30—Tungsten
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0215—Coating
    • B01J37/0225—Coating of metal substrates
    • 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
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8628—Processes characterised by a specific catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst

Definitions

  • the invention belongs to the field of environmental protection and environmental catalysis, and particularly relates to a continuous production device and a production process of an SCR plate type denitration catalyst.
  • the SCR denitration catalysts are mainly of honeycomb type, plate type and corrugated board type.
  • the main components of the three types of catalysts are the same as the catalytic reaction principle, but the structural forms are different.
  • Corrugated plate catalysts although large in surface area but light in weight, are not compatible with other catalysts and limit their application, and are generally only used in low-ash gas-fired power plants.
  • coal-fired power stations mainly use plate catalysts and honeycomb catalysts.
  • the plate catalysts have strong anti-clogging, anti-wear and anti-poisoning properties under the high dust arrangement conditions of coal-fired power stations.
  • the required volume of the plate catalyst is even smaller than that of the honeycomb catalyst, which helps to reduce the investment capital. China's coal quality is complex and generally has a large ash content, so the plate catalyst has great market potential.
  • an SCR plate type denitration catalyst continuous production apparatus which comprises a stainless steel mesh plate unwinding and pinching system, a catalyst paste preparation system, a catalyst paste cloth system, and a plate catalyst roll-crease-shear System, sample assembly station, dry roasting system (14), wherein
  • the stainless steel stencil unwinding and pinching system includes an unwinding device, a leveling device, a centering device and a pinching device, and the devices are sequentially connected; wherein the leveling device comprises a multi-level leveling machine serially connected in series in the horizontal direction, the first level school The flat machine is connected to the unwinding device, and the outlet end of the final leveling machine is connected with the centering device; the pinching device comprises a multi-stage pinch machine serially connected in series in the horizontal direction, and the first stage pinch feeder is connected with the centering device. The outlet end of the final pinch feeder is connected to the inlet end of the cloth equipment;
  • the catalyst paste preparation system comprises a mixing device and an extrusion molding device; wherein the mixing device comprises a plurality of mutually independent mixing machines, and the discharge opening of each mixing machine is connected with the inlet of the extrusion molding device, and is extruded
  • the discharge port of the molding device is connected to the hopper of the cloth device;
  • the catalyst paste cloth system comprises a cloth distributing device, a screeding device and a material recycling device; wherein the screeding device comprises a multi-stage screeding machine serially connected in series in a horizontal direction, and the inlet end of the first level screeding machine is connected to the outlet end of the distributing device The outlet end of the final screed is connected to the inlet end of the first stage roller press in the rolling equipment; the material recovery equipment is located at the lower part of the cloth equipment and the screeding apparatus;
  • the plate catalyst roll-pinch-shearing system comprises a rolling device, a pleating device and a shearing device; wherein the rolling device comprises a multi-stage rolling press connected in series in the horizontal direction, the inlet end of the first-stage rolling press Connected to the screeding device, the outlet end of the final roller press is connected to the inlet end of the pleating device, and the outlet end of the pleating device is connected to the inlet end of the shearing device;
  • the outlet end of the sample assembly station is connected to a dry roasting system.
  • the leveling device comprises at least two leveling machines, and the leveling machine is a double roller leveling machine or a quadruple roller leveling machine or a six-roll type roller leveling machine.
  • the pinching device comprises at least two pinch machines, and the pinch machine is a roller pinch machine.
  • the mixing device comprises at least two mixers, and the mixer is a vertical or horizontal slow premixer.
  • the extrusion molding apparatus is a spiral granulator.
  • the cloth distributing device is a gravity classifying scraper type cloth distributing machine.
  • the screeding device comprises at least two screeders.
  • the rolling device comprises at least two roller presses.
  • the shearing device is a pneumatic shear or a hydraulic shear.
  • the dry roasting system is a temperature programmed tunnel kiln.
  • a continuous production process of an SCR plate type denitration catalyst using the above production apparatus characterized in that a rolled stainless steel mesh plate is unwound by a coiling device, and a leveling device is multi-staged. After the centering and centering equipment is automatically centered, it is continuously fed into the pinch feeding device, and continuously advances at a uniform speed under the action of the multi-stage pinch feeder of the pinch device; at the same time, the catalyst raw material is sufficiently mixed after the mixing device is fed.
  • the extrusion molding apparatus obtains the formed catalyst paste particles and arranges on the stainless steel mesh plate through the hopper of the distribution device; the stainless steel mesh plate coated with the catalyst paste particles is smoothed by the multi-stage smoothing machine to make the catalyst paste particles Evenly arranged, the material spilled during the cloth and smoothing process is collected by the material recovery equipment; the stainless steel mesh plate uniformly coated with the catalyst paste particles enters the rolling equipment, and the catalyst paste is evenly coated on the stainless steel after multi-stage rolling On the stencil, and then into the pleating device to suppress the corrugation, and then enter the shearing device to shear to obtain the bulk plate catalyst; The obtained bulk plate catalyst is assembled into a specific module on a sample assembly stage, and finally sent to a dry calcination system for drying and calcination to obtain a finished plate type denitration catalyst.
  • the catalyst raw materials include anatase type nano titanium dioxide, ammonium metavanadate, ammonium metatungstate, oxalic acid, water, kaolin, polyvinyl alcohol,
  • the mixing process of the catalyst raw materials includes the following steps:
  • Step (1) According to the mass ratio (4 ⁇ 5): (18-25): (6-7): 100 weigh ammonium metavanadate, ammonium metatungstate, oxalic acid and deionized water, metavanadic acid Ammonium, ammonium metatungstate and oxalic acid are dissolved in deionized water, and all of them are dissolved by stirring to obtain an active component solution;
  • Step (2) In the active component solution obtained in the step (1), anatase-type nano-titanium dioxide is added, the mass ratio of the two is (75-85): 100, and the titanium dioxide is fully wetted for 3 hours to obtain catalyst activity.
  • Step (3) Weigh kaolin, polyvinyl alcohol and methyl cellulose according to a mass ratio of (10 ⁇ 11): 1:1, mechanically mix them to obtain a mixed powder; and add the above mixed powder to the catalyst activity in the step (2)
  • the mass ratio of the components, the two is 1: (5.5 ⁇ 6.0) ; the catalyst paste is obtained by thorough stirring.
  • the stainless steel mesh has a thickness of 0.15-0.3 mm.
  • the pinch feeder and the stainless steel mesh plate have an operating speed of from 1 to 15 m/min.
  • the plate catalyst has a thickness of from 0.5 to 0.8 mm.
  • the temperature of the plate catalyst in the dry calcination system is 80-120 ° C, and the drying time is preferably, the calcination temperature of the plate catalyst in the dry calcination system is 450-600 ° C, and the temperature programming rate is 0.5-10 ° C / min, holding time is l-4h.
  • the invention has the beneficial effects that the SCR plate type denitration catalyst continuous production device of the invention is based on the multilevel leveling machine of the leveling device, realizes complete leveling of the stainless steel mesh plate, and prepares for the subsequent uniform cloth; Centering equipment, automatic centering of stainless steel stencils to prevent the deviation of stainless steel stencils and affect fabric uniformity and rolling
  • the multi-stage troweling machine of the equipment realizes the uniform distribution of the catalyst paste on the stainless steel stencil and controls the thickness of the material layer; the multi-stage roller press based on the rolling equipment realizes the effective forming of the catalyst paste on the stainless steel stencil
  • the drying and calcination conditions of the catalyst are strictly controlled by a dry calcination system.
  • Fig. 1 is a schematic view showing the production apparatus of the SCR plate type denitration catalyst.
  • the present invention provides an apparatus and method for producing an SCR plate type denitration catalyst, which will be further described below in conjunction with specific embodiments.
  • the apparatus for producing an SCR plate type denitration catalyst of the present invention comprises a stainless steel mesh plate unwinding and pinching system, a catalyst paste preparation system, a catalyst paste cloth system, a plate catalyst roll-pressure pleating-shearing system, Sample assembly station and dry roasting system.
  • the stainless steel stencil unwinding and pinching system comprises an unwinding device 1, a leveling device 2, a centering device 3 and a pinching device 4, wherein the devices are sequentially connected; wherein the leveling device 2 comprises a multi-level leveling machine, the multi-stage school
  • the flat machines are connected in series in the horizontal direction, and the first level leveling machine is connected to the unwinding device 1, and the second leveling machine is followed by the second leveling machine, ..., the final leveling machine; the exit of the first level leveling machine
  • the end is connected to the inlet end of the secondary leveling machine, The end is connected to the centering device 3;
  • the pinch device 4 includes a multi-stage pinch machine, the multi-stage pinch machine is connected in series in the horizontal direction, and the first stage pinch machine is connected to the centering device 3, After that, it is a secondary pinch feeder, ..., a final pinch feeder; the outlet end of the first pinch feeder is connected to the inlet end of the secondary pinch feeder; the outlet end of the secondary pinch feeder and
  • the catalyst paste preparation system comprises a mixing device 5 and an extrusion molding device 6; wherein the mixing device 5 comprises a plurality of mixing machines, each of which is independent of each other, a discharge port and an extrusion molding device of each mixing machine
  • the feed port of the 6 is connected, the discharge port of the extrusion molding device 6 is connected to the hopper of the cloth device 7;
  • the catalyst paste cloth system comprises a cloth device 7, a smoothing device 8 and a material recovery device 9; wherein the smoothing device 8 comprises The multi-stage troweling machine, the multi-stage screeding machine is connected in series in the horizontal direction, and the first-stage screeding machine is connected with the cloth-laying device 7, and the second-level screeding machine is sequentially followed, ..., the last-stage smearing
  • the inlet end of the first level trowel is connected to the outlet end of the cloth device 7, the outlet end of the first level trowel is connected to the inlet end of the secondary screed machine, and the outlet end of the secondary screed machine
  • the plate catalyst roll-pinch-shearing system includes a rolling apparatus 10, a pleating apparatus 11 and a shearing apparatus 12; wherein the rolling apparatus 10 includes a multi-stage rolling press, and the multi-stage rolling press is horizontally In series, in series with the screeding device 8, the first stage roller press, followed by the secondary roller press, ..., the final roller press; the outlet end of the first stage roller press and the second stage
  • the inlet end of the roller press is connected, the outlet end of the secondary roller press is connected to the inlet end of the tertiary roller press, and so on, the outlet end of the final roller press is connected to the inlet end of the crimping device 11, pleating
  • the outlet end of the device 11 is connected to the inlet end of the shearing device 12.
  • the outlet end of the sample assembly station 13 is connected to a dry calcination system 14.
  • Prepare SCR plate denitration catalyst 4kg, 18kg, 6kg and 100kg of ammonium metavanadate, ammonium metatungstate, oxalic acid and deionized water were weighed into the mixer 5, and ammonium metavanadate, ammonium metatungstate and oxalic acid were all dissolved by stirring.
  • the active component solution is obtained; 160 kg of anatase-type nano titanium dioxide is added to the above active component solution, and the titanium dioxide is fully infiltrated for 3 hours to obtain the active component of the catalyst; 42 kg, 4.2 kg and respectively are weighed.
  • 4.2 kg of kaolin, polyvinyl alcohol and methyl cellulose were mechanically mixed and added to the above active component of the catalyst, and stirred sufficiently to obtain a catalyst paste.
  • the rolled stainless steel stencil having a thickness of 0.2 mm is continuously fed into the two-stage pinch machine 2 via the unwinding device 1, the two-stage leveling machine 2, and the centering device 3, and the pinch speed is lOm/min;
  • the catalyst paste in the mixer 5 is fed into the extrusion molding apparatus 6 to obtain columnar catalyst paste particles having a diameter of 2 mm, and is disposed on the stainless steel mesh plate via the hopper of the distribution device 7; the catalyst paste particles are disposed.
  • the stainless steel mesh plate is evenly arranged by the two-stage screeding machine 8 to uniformly arrange the catalyst paste particles, and the materials spilled during the cloth and the smoothing process are collected by the material recovery device 9; the stainless steel mesh plate uniformly distributing the catalyst paste particles After the third-stage rolling, the catalyst paste is evenly coated on the stainless steel mesh plate, and then into the crimping device 11 to suppress the corrugation, and then enters the shearing device 12 to be sheared to obtain a bulk plate catalyst having a thickness of 0.6 mm;
  • the obtained bulk plate catalyst was assembled into a specific module on the sample assembly stage 13, and finally sent to the dry calcination system 14, first dried at 100 ° C for 3 h, and then heated at 2 ° C / min. Ratio was raised to 550 ° C, and kept for 2h at 550 ° C, to obtain a finished slab denitration catalyst.
  • the denitration performance of the above-mentioned finished plate catalyst was evaluated, and the denitration efficiency at a typical flue gas (NOx 500 ppm, S0 2 1000 ppm, NH 3 500 ppm) and a space velocity of ⁇ 1 was 95%.
  • the denitration performance of the above-mentioned finished plate catalyst was evaluated, and the denitration efficiency at a typical flue gas (NOx 500 ppm, S0 2 1000 ppm, NH 3 500 ppm) and a space velocity of 1000 h' 1 was 96%.
  • the denitration performance of the above-mentioned finished plate catalyst was evaluated, and the denitration efficiency at a typical flue gas (NOx 500 ppm, S0 2 1000 ppm N3 ⁇ 4 500 ppm) and a space velocity of 1000 h' 1 was 96%.

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  • Organic Chemistry (AREA)
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Abstract

一种SCR板式脱硝催化剂连续生产装置，包括不锈钢网板开卷夹送系统、催化剂膏体布料系统、板式催化剂辊压-压褶-剪切系统、样品组装台、干燥焙烧系统。生产时，不锈钢网板经开卷、校平、对中后，由夹送设备连续夹送运行；与此同时，脱硝催化剂原料经混合、挤压成型后由布料设备和抹平设备将其均匀布置于不锈钢网板上，而后将多级辊压、压褶、剪切后获得块状板式催化剂；所获得的块状板式催化剂，在样品组装台上组装成特定模块，最后送入干燥焙烧系统中经干燥和焙烧获得成品板式脱硝催化剂。本发明通过引入多级校平机、对中设备、多级夹送机、多级抹平机、多级辊压机等设备，实现了板式脱硝催化剂的连续生产。

Description

一种 SCR板式脱硝催化剂连续生产装置及生产工艺
技术领域
本发明属于环境保护与环境催化领域， 具体涉及一种 SCR板式脱硝催化剂 连续生产装置及生产工艺。
背景技术
2011年 7月 29日， 环境保护部正式发布《火电厂大气污染物排放标准》， 该 标准严格规定了火电厂氮氧化物排放限值。 在现有的各类脱硝技术中， 氨选择性 催化还原 （SCR) 法由于其高效的脱硝效率、 选择性好， 且技术成熟， 是目前主 要的燃煤电站脱硝技术。
SCR脱硝催化剂主要有蜂窝式、 板式、 波纹板式三种， 三种形式的催化剂的 主要成份与催化反应原理是相同的， 只是结构形式有差别。 波纹板式催化剂虽比 表面积大但重量轻， 不能与其他催化剂兼容， 限制了其应用， 一般只用于低灰的 燃气电站。 目前燃煤电站使用的主要是板式催化剂和蜂窝式催化剂， 板式催化剂 在燃煤电站的高尘布置条件下具有很强的防堵灰、 耐磨损和抗中毒的性能， 在极 高尘烟气条件下板式催化剂所需体积甚至比蜂窝式催化剂小有助于降低投资资 本。 我国煤质复杂， 一般灰分较大， 因此板式催化剂具有很大的市场潜力。
目前国内外在 SCR板式脱硝催化剂生产工艺方面己有一些报道， 但在如何 实现连续生产的工艺和装置方面鲜有报道， 而且也仅有极少数单位实现了 SCR 板式脱硝催化剂的工业化生产； 基于已有的报道材料， 现有连续生产工艺存在着 集成度不高、 生产效率较低、 废品率较高、 生产成本高等问题， 不利于量产。 发明内容
本发明的目的在于克服现有技术的不足， 提供一种 SCR板式脱硝催化剂的 根据本发明的一方面， 提供了一种 SCR板式脱硝催化剂连续生产装置， 包 括不锈钢网板开卷夹送系统、 催化剂膏体制备系统、 催化剂膏体布料系统、 板式 催化剂辊压 -压褶 -剪切系统、 样品组装台、 干燥焙烧系统 （14)， 其中，
不锈钢网板开卷夹送系统包括开卷设备、 校平设备、 对中设备和夹送设备， 各设备依次相连； 其中校平设备包括在水平方向上依次串联的多级校平机， 第一 级校平机与开卷设备相连， 末级校平机的出口端与对中设备相连； 夹送设备包括 在水平方向上依次串联的多级夹送机， 第一级夹送机与对中设备相连， 末级夹送 机的出口端与布料设备的入口端相连；
催化剂膏体制备系统包括混料设备和挤压成型设备； 其中混料设备包括多个 互相独立的混料机， 各混料机的出料口与挤压成型设备的入料口相连， 挤压成型 设备的出料口与布料设备的料斗相连；
催化剂膏体布料系统包括布料设备、 抹平设备和物料回收设备； 其中抹平设 备包括在水平方向依次串联的多级抹平机， 第一级抹平机的入口端与布料设备的 出口端相连末级抹平机的出口端与辊压设备中的第一级辊压机的入口端相连； 物 料回收设备位于布料设备和抹平设备的下部；
板式催化剂辊压 -压褶 -剪切系统包括辊压设备、 压褶设备和剪切设备； 其中 辊压设备包括在水平方向依次串联的多级辊压机， 第一级辊压机的入口端与抹平 设备相连， 末级辊压机的出口端与压褶设备的入口端相连， 压褶设备的出口端与 剪切设备的入口端相连；
样品组装台的出口端与干燥焙烧系统相连。
优选地， 所述的校平设备至少包括两个校平机， 所述校平机为二重式辊式校 平机或四重式辊式校平机或六重式辊式校平机。 优选地， 所述的夹送设备至少包括两个夹送机， 所述夹送机为辊式夹送机。 优选地， 所述的混料设备至少包括两个混料机， 所述混料机为立式或卧式慢 速预混机。
优选地， 所述的挤压成型设备为螺旋造粒机。
优选地， 所述的布料设备为重力分级刮板式布料机。
优选地， 所述的抹平设备至少包括两个抹平机。
优选地， 所述的辊压设备至少包括两个辊压机。
优选地， 所述的剪切设备为气压剪切机或者液压剪切机。
优选地， 所述的干燥焙烧系统为程序升温隧道窑。
根据本发明的另一方面， 还提供了一种利用上述生产装置的 SCR板式脱硝 催化剂的连续生产工艺， 其特征在于， 将卷状的不锈钢网板经由幵卷设备开卷、 校平设备多级校平、 对中设备自动对中后， 连续送入夹送设备中， 在夹送设备的 多级夹送机作用下连续匀速前进；与此同时，催化剂原料在混料设备充分混合后， 送入挤压成型设备， 获得成型的催化剂膏体颗粒， 并经由布料设备的料斗布置于 不锈钢网板上； 布有催化剂膏体颗粒的不锈钢网板经多级抹平机抹平后使催化剂 膏体颗粒均匀布置， 布料和抹平过程中洒落的物料则由物料回收设备收集； 均布 催化剂膏体颗粒的不锈钢网板进入辊压设备中， 经多级辊压后使催化剂膏体均匀 涂覆于不锈钢网板上， 而后进入压褶设备中压制波纹， 之后再进入剪切设备中剪 切获得块状板式催化剂； 所获得的块状板式催化剂， 在样品组装台上组装成特定 模块， 最后送入干燥焙烧系统中经干燥和焙烧获得成品板式脱硝催化剂。
优选地， 所述的 SCR板式脱硝催化剂的连续生产工艺中， 催化剂原料包括 锐钛矿型纳米二氧化钛、 偏钒酸铵、 偏钨酸铵、 草酸、 水、 高岭土、 聚乙烯醇、 进一步地， 所述的 SCR板式脱硝催化剂的连续生产工艺中， 催化剂原料的 混料过程包括如下步骤：
步骤 （1 ): 按质量比为 (4〜5)： (18-25)： (6-7)： 100称取偏钒酸铵、 偏钨酸 铵、 草酸和去离子水， 将偏钒酸铵、 偏钨酸铵和草酸溶于去离子水中， 通过搅拌 使其全部溶解， 获得活性组分溶液；
步骤 （2): 在步骤 （1 )获得的活性组分溶液中， 加入锐钛型纳米二氧化钛， 两者的质量比为 (75〜85)： 100， 充分搅拌 3h使二氧化钛充分浸润， 获得催化剂活 性组分；
步骤 （3): 按质量比为 (10〜11)： 1： 1称取高岭土、 聚乙烯醇和甲基纤维素， 将其机械混合得到混合粉末； 将上述混合粉末加入步骤（2) 中催化剂活性组分， 两者的质量比为 1 : (5.5~6.0); 充分搅拌获得催化剂膏体。
优选地， 所述不锈钢网板的厚度为 0.15-0.3mm。
优选地， 所述夹送机和不锈钢网板的运行速度为 l-15m/min。
优选地， 所述板式催化剂的厚度为 0.5-0.8mm。
优选地， 所述板式催化剂在干燥焙烧系统中的温度为 80-120°C， 干燥时间为 优选地， 所述板式催化剂在干燥焙烧系统中的焙烧温度为 450-600°C， 程序 升温速率为 0.5-10°C/min， 保温时间为 l-4h。
本发明的有益效果为- 本发明所述的 SCR板式脱硝催化剂连续生产装置， 基于校平设备的多级校平 机， 实现不锈钢网板的完全校平， 为后续的均匀布料做好准备； 基于对中设备， 实现不锈钢网板的自动对中， 以防止不锈钢网板跑偏从而影响布料均匀性及辊压 设备的多级抹平机， 实现催化剂膏体在不锈钢网板上的均匀布料， 并控制料层厚 度； 基于辊压设备的多级辊压机， 实现催化剂膏体在不锈钢网板上的有效成型； 通过干燥焙烧系统严格控制催化剂的干燥和焙烧条件。通过上述设备和工艺的运 用， 实现优质板式脱硝催化剂的连续生产。
附图说明
图 1一一 SCR板式脱硝催化剂的生产装置示意图。
图中标号：
( 1 ) 开卷设备； （2) 校平设备； （3 ) 对中设备； （4) 夹送设备； （5) 混料 设备； （6) 挤压成型设备； （7) 布料设备； （8) 抹平设备； （9) 物料回收设备；
( 10) 辊压设备； （11 ) 压褶设备； （12) 剪切设备； （13 ) 样品组装台； （14) 干 燥焙烧系统。
具体实施方式
本发明提供了一种 SCR板式脱硝催化剂的生产装置和方法， 下面结合具体 实施方式对本发明做进一步说明。
实施例 1
如图 1所示， 本发明的 SCR板式脱硝催化剂的生产装置， 包括不锈钢网板 开卷夹送系统、 催化剂膏体制备系统、 催化剂膏体布料系统、 板式催化剂辊压- 压褶 -剪切系统、 样品组装台与干燥焙烧系统。
不锈钢网板开卷夹送系统包括开卷设备 1、 校平设备 2、 对中设备 3和夹送 设备 4， 各设备依次相连； 其中校平设备 2包括多级校平机， 所述的多级校平机 在水平方向上依次串联， 与开卷设备 1相连的为第一级校平机， 向后依次为二级 校平机， ……，末级校平机；第一级校平机的出口端与二级校平机的入口端相连， 端与对中设备 3相连； 夹送设备 4包括多级夹送机， 所述的多级夹送机在水平方 向上依次串联， 与对中设备 3 相连的为第一级夹送机， 向后依次为二级夹送 机， ……， 末级夹送机； 第一级夹送机的出口端与二级夹送机的入口端相连； 二 级夹送机的出口端与三级夹送机的入口端相连； 依次类推； 末级夹送机的出口端 与布料设备 7的入口端相连。
催化剂膏体制备系统包括混料设备 5和挤压成型设备 6; 其中混料设备 5包 括多个混料机， 每个混料机互相独立， 各混料机的出料口与挤压成型设备 6的入 料口相连， 挤压成型设备 6的出料口与布料设备 7的料斗相连； 催化剂膏体布料 系统包括布料设备 7、 抹平设备 8和物料回收设备 9; 其中抹平设备 8包括多级 抹平机， 所述的多级抹平机在水平方向依次串联， 与布料设备 7相连的为第一级 抹平机， 向后依次为二级抹平机， ……， 末级抹平机； 第一级抹平机的入口端与 布料设备 7的出口端相连， 一级抹平机的出口端与二级抹平机的入口端相连， 二 级抹平机的出口端与三级抹平机的入口端相连， 依次类推， 末级抹平机的出口端 与辊压设备 10中的第一级辊压机的入口端相连；物料回收设备 9位于布料设备 7 和抹平设备 8的下部。
板式催化剂辊压-压褶-剪切系统包括辊压设备 10、 压褶设备 11 和剪切设备 12； 其中辊压设备 10包括多级辊压机， 所述的多级辊压机在水平方向依次串联， 与抹平设备 8相邻的为第一级辊压机， 向后依次为二级辊压机， ……， 末级辊压 机； 第一级辊压机的出口端与二级辊压机的入口端相连， 二级辊压机的出口端与 三级辊压机的入口端相连， 依次类推， 末级辊压机的出口端与压褶设备 11 的入 口端相连， 压褶设备 11的出口端与剪切设备 12的入口端相连。
样品组装台 13的出口端与干燥焙烧系统 14相连。 备 SCR板式脱硝催化剂。 分别称取 4kg、 18kg、 6kg和 100kg的偏钒酸铵、 偏钨 酸铵、 草酸和去离子水置于混料机 5中， 通过搅拌使偏钒酸铵、 偏钨酸铵和草酸 全部溶解于去离子水中，获得活性组分溶液；在上述活性组分溶液中，加入 160kg 的锐钛型纳米二氧化钛， 充分搅拌 3h使二氧化钛充分浸润， 获得催化剂活性组 分； 分别称取 42kg、 4.2kg和 4.2kg的高岭土、 聚乙烯醇和甲基纤维素， 将其机 械混合后加入上述催化剂活性组分中， 充分搅拌获得催化剂膏体。
将厚度为 0.2mm的卷状不锈钢网板经由开卷设备 1、 两级校平机 2、 对中设 备 3后， 连续送入两级夹送机 2中， 夹送速度为 lOm/min; 与此同时， 将混料机 5中的催化剂膏体送入挤压成型设备 6获得直径为 2mm的柱状催化剂膏体颗粒， 并经由布料设备 7的料斗布置于不锈钢网板上； 布有催化剂膏体颗粒的不锈钢网 板经两级抹平机 8抹平后使催化剂膏体颗粒均匀布置， 布料和抹平过程中洒落的 物料则由物料回收设备 9收集； 均布催化剂膏体颗粒的不锈钢网板经三级辊压后 使催化剂膏体均匀涂覆于不锈钢网板上， 而后进入压褶设备 11 中压制波纹， 之 后再进入剪切设备 12中剪切获得块状板式催化剂， 厚度为 0.6mm; 所获得的块 状板式催化剂， 在样品组装台 13上组装成特定模块， 最后送入干燥焙烧系统 14 中， 首先在 100°C下干燥 3h， 而后采用 2°C/min的升温速率升温至 550°C， 并在 550°C下保持 2h， 从而得到成品板式脱硝催化剂。
对上述成品板式催化剂的脱硝性能进行评价， 在典型烟气 （NOx 500 ppm、 S02 1000 ppm、 NH3 500 ppm) 以及空速为 ΙΟΟΟΟΙι·1下的脱硝效率为 95%。
实施例 2
在与实施例 1完全相同的设备和工艺，仅将干燥焙烧条件改为：首先 80°C下 干燥 4h， 而后采用 2°C/min的升温速率升温至 500°C， 并在 500Ό下保持 3h， 从 对上述成品板式催化剂的脱硝性能进行评价， 在典型烟气 （NOx 500 ppm、 S02 1000 ppm、 NH3 500 ppm) 以及空速为 lOOOOh'1下的脱硝效率为 95%。
实施例 3
在与实施例 1完全相同的设备和工艺， 仅将偏钒酸铵的用量改为 4.5kg制备 获得成品板式脱硝催化剂。
对上述成品板式催化剂的脱硝性能进行评价， 在典型烟气 （NOx 500 ppm、 S02 1000 ppm、 NH3 500 ppm) 以及空速为 lOOOOh'1下的脱硝效率为 96%。
实施例 4
在与实施例 1完全相同的设备和工艺， 仅将偏钒酸铵和偏钨酸铵的用量改为 4.5kg和 20kg制备获得成品板式脱硝催化剂。
对上述成品板式催化剂的脱硝性能进行评价， 在典型烟气 （NOx 500 ppm、 S02 1000 ppm N¾ 500 ppm) 以及空速为 lOOOOh'1下的脱硝效率为 96%。
以上所述仅为本发明的较佳实施例而已， 并不用以限制本发明， 凡在本发明 的精神和原则之内， 所做的任何修改、 等同替换、 改进等， 均应包含在本发明的 范围之内。

Claims

1. 一种 SCR板式脱硝催化剂连续生产装置，包括不锈钢网板幵卷夹送系统、 催化剂膏体制备系统、 催化剂膏体布料系统、 板式催化剂辊压 -压褶 -剪切系统、 样品组装台、 干燥焙烧系统 （14)， 其特征在于，
不锈钢网板开卷夹送系统包括开卷设备 （1 )、 校平设备 （2)、 对中设备（3 ) 和夹送设备 （4)， 各设备依次相连； 其中校平设备 （2) 包括在水平方向上依次 串联的多级校平机， 第一级校平机与幵卷设备 （1 ) 相连， 末级校平机的出口端 与对中设备（3 )相连； 夹送设备（4)包括在水平方向上依次串联的多级夹送机， 第一级夹送机与对中设备 （3 )相连， 末级夹送机的出口端与布料设备（7) 的入 口端相连；
催化剂膏体制备系统包括混料设备 （5) 和挤压成型设备 （6); 其中混料设 备（5)包括多个互相独立的混料机， 各混料机的出料口与挤压成型设备（6) 的 入料口相连， 挤压成型设备 （6) 的出料口与布料设备 （7) 的料斗相连；
催化剂膏体布料系统包括布料设备（7)、抹平设备（8)和物料回收设备（9); 其中抹平设备 （8) 包括在水平方向依次串联的多级抹平机， 第一级抹平机的入 口端与布料设备 （7) 的出口端相连末级抹平机的出口端与辊压设备 （10) 中的 第一级辊压机的入口端相连； 物料回收设备 （9)位于布料设备（7) 和抹平设备 (8) 的下部；
板式催化剂辊压-压褶-剪切系统包括辊压设备（10)、 压褶设备（11 )和剪切 设备 （12); 其中辊压设备 （10) 包括在水平方向依次串联的多级辊压机， 第一 级辊压机的入口端与抹平设备相连， 末级辊压机的出口端与压褶设备（11 ) 的入 口端相连， 压褶设备 （11 ) 的出口端与剪切设备 （12) 的入口端相连；
样品组装台 （13 ) 的出口端与干燥焙烧系统 （14) 相连。 所述校平设备 （2) 至少包括两个校平机， 所述校平机为二重式辊式校平机或四 重式辊式校平机或六重式辊式校平机。
3. 根据权利要求 1所述的 SCR板式脱硝催化剂的生产装置， 其特征在于： 所述对中设备 （3 ) 为具有自动纠偏功能的辊式对中机。
4. 根据权利要求 1所述的 SCR板式脱硝催化剂连续生产装置，其特征在于: 所述夹送设备 （4) 至少包括两个夹送机， 所述夹送机为辊式夹送机。
5. 根据权利要求 1所述的 SCR板式脱硝催化剂连续生产装置，其特征在于: 所述混料设备（5)至少包括两个混料机， 所述混料机为立式或卧式慢速预混机。
6. 根据权利要求 1所述的 SCR板式脱硝催化剂连续生产装置，其特征在于: 所述挤压成型设备 （6) 为螺旋造粒机。
7. 根据权利要求 1所述的 SCR板式脱硝催化剂连续生产装置，其特征在于: 所述布料设备 （7) 为重力分级刮板式布料机。
8. 根据权利要求 1所述的 SCR板式脱硝催化剂连续生产装置，其特征在于: 所述抹平设备 （8) 至少包括两个抹平机。
9. 根据权利要求 1所述的 SCR板式脱硝催化剂连续生产装置，其特征在于: 所述辊压设备 （10) 至少包括两个辊压机。
10. 根据权利要求 1所述的 SCR板式脱硝催化剂连续生产装置，其特征在于: 所述剪切设备 （12) 为气压剪切机或者液压剪切机。
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CN106268297B (zh) * 2016-08-05 2021-03-23 韩东吉 一种催化剂板片的回收方法及回收装置
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KR102197079B1 (ko) 2019-08-06 2020-12-30 주식회사 현대기전 고상우레아에 기반한 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템의 용융우레아 공급장치, 이의 공급 운용 방법, 및 이를 포함하는 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템
KR102197077B1 (ko) 2019-08-06 2020-12-30 주식회사 현대기전 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템의 고상우레아 용융장치, 및 이를 포함하는 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템
KR102197078B1 (ko) 2019-08-06 2020-12-30 주식회사 현대기전 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템의 고상우레아 투입공급장치, 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템의 고상우레아 투입공급방법, 및 이를 포함하는 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템
KR102079540B1 (ko) 2019-08-06 2020-02-20 주식회사 현대기전 선택적환원촉매 탈질 설비용 고상 우레아 기반의 암모니아 환원제 공급 설비 시스템 및 그의 운용 방법
KR102211718B1 (ko) 2019-09-09 2021-02-03 주식회사 현대기전 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템의 분체형 고상우레아 뭉침 방지 장치
KR102211708B1 (ko) 2019-09-09 2021-02-03 주식회사 현대기전 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템의 암모니아 환원제 생성용 리액터 장치, 그의 운용 제어 방법, 및 이를 포함하는 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템
KR102211717B1 (ko) 2019-09-09 2021-02-03 주식회사 현대기전 고상 우레아 기반의 암모니아 환원제 공급 설비의 열원 공급 시스템 및 이를 포함하는 암모니아 환원제 공급 설비
KR102211715B1 (ko) 2019-09-09 2021-02-03 주식회사 현대기전 고상 우레아 기반의 암모니아 환원제 공급 설비 시스템의 운전 운용 방법, 이를 포함하는 암모니아 환원제 공급 설비 시스템의 운용 시스템 및 그의 운용 방법
KR102211712B1 (ko) 2019-09-09 2021-02-03 주식회사 현대기전 암모니아 환원제 공급 설비 시스템의 잔류 용융우레아 퍼징 방법과, 이를 포함하는 고상우레아 기반의 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 운용 방법 및 시스템
KR102259720B1 (ko) 2019-09-11 2021-06-01 주식회사 현대기전 암모니아 환원제 공급 설비 시스템의 용융우레아 고착 방지 장치, 이를 포함하는 용융우레아 공급 장치, 및 용융우레아 공급 장치를 포함하는 고상우레아 기반의 선택적환원촉매 탈질 설비용 암모니아 환원제 공급 설비 시스템
CN111256461B (zh) * 2020-02-10 2021-12-28 北京华电光大环境股份有限公司 一种自动分离式红外烘干炉及烘干系统

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