WO2021114562A1 - 一种生产焦亚硫酸钠的系统及制备方法 - Google Patents

一种生产焦亚硫酸钠的系统及制备方法 Download PDF

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WO2021114562A1
WO2021114562A1 PCT/CN2020/089516 CN2020089516W WO2021114562A1 WO 2021114562 A1 WO2021114562 A1 WO 2021114562A1 CN 2020089516 W CN2020089516 W CN 2020089516W WO 2021114562 A1 WO2021114562 A1 WO 2021114562A1
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reactor
tank
sodium metabisulfite
output end
gas
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PCT/CN2020/089516
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English (en)
French (fr)
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徐海涛
陈任远
徐延忠
刘大华
李明波
宋静
徐梦
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南京杰科丰环保技术装备研究院有限公司
南京工业大学
江苏德义通环保科技有限公司
南京硫研环保科技有限公司
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Publication of WO2021114562A1 publication Critical patent/WO2021114562A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
    • C01D5/14—Preparation of sulfites
    • C01D5/145—Pyrosulfites or metabisulfites
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
    • C01D5/14—Preparation of sulfites

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  • the invention relates to the field of chemical engineering, in particular to a system for producing sodium metabisulfite and a preparation method.
  • the present invention aims at the defects of the prior art and provides a system and preparation method for producing sodium metabisulfite.
  • a system for producing sodium metabisulfite includes a third reactor, a second reactor and a first reactor.
  • the soda ash storage bin is respectively connected with a soda preparation tank and a lye tank, and the soda ash is connected to the first reactor.
  • the storage bins are respectively connected to the alkali distribution tank and the lye tank, the output end of the alkali distribution tank is connected to the upper part of the third reactor, and the output end of the lower part of the third reactor is connected to the second reactor through the third circulating pump.
  • the jet reactor at the top of the three reactors is connected to the upper part of the second reactor; the output end of the lower part of the second reactor is connected to the jet reactor at the top of the second reactor and the upper part of the first reactor through the second circulation pump.
  • the output end of the lower part of the first reactor is respectively connected to the jet reactor and the elutriation tank at the top of the first reactor through the first circulation pump; the elutriation tank is connected by a centrifuge and
  • the output end of the top of the elutriation tank and the liquid output end of the centrifuge are both connected with the alkali distribution tank.
  • the gas output end of the dryer is connected with the tail gas scrubber;
  • the output end at the bottom of the lye tank is connected with the washing circulation tank, and the output end at the bottom of the washing circulation tank is connected with the tail gas scrubber;
  • the tail gas scrubber The output end of the upper part of the tower is connected with the washing circulation tank, and the output end at the bottom of the tail gas washing tower is respectively connected with the middle part of the tail gas washing tower and the alkali distribution tank.
  • the sulfur dioxide gas output pipeline is connected with the jet reactor located at the upper part of the first reactor, the gas output end at the top of the first reactor is connected with the jet reactor located at the upper part of the second reactor, and the upper part of the second reactor
  • the gas output end of is connected to the jet reactor located on the upper part of the third reactor, and the gas output end on the top of the third reactor is discharged outside the boundary.
  • the third reactor, the second reactor and the first reactor include a crystallizer, the top of the crystallizer is provided with a jet reactor, and the lower part of the crystallizer is connected to the jet reactor through a circulation pump
  • the upper part is connected, and the top of the jet reactor is equipped with a gas input system
  • the bottom of the crystallizer is a crystal discharge section, and the upper part of the crystallizer is also equipped with a raw material liquid interface
  • the top of the crystallizer is also equipped with a washing device for reaction tail gas
  • the lower part of the device is provided with a defoaming device, and a flushing water interface is also arranged above the defoaming device, and the top of the washing device is a discharge outlet for reaction tail gas.
  • the lower part of the crystallizer is a conical structure with a contraction angle of 60 to 100°
  • a settling pipe is connected to the lower part of the conical structure, and the conical structure and the settling pipe constitute the crystal discharge section .
  • the jet reactor is provided with a discharge pipe, an expansion pipe, a throat pipe, a contraction pipe, and an intake pipe from bottom to top.
  • the top of the intake pipe is provided with a raw gas interface, and the lower part of the intake pipe is provided with a discharge pipe.
  • There is a liquid interface; the contraction angle of the shrink tube is 10-60°, and the expansion angle of the expansion tube is 5-30°; the discharge tube of the jet reactor extends out of the top cover of the crystallizer, and its extension length is 1000-4000mm.
  • a method for producing sodium metabisulfite using the above system comprising the following steps:
  • Reactive crystallization the sodium sulfite slurry passes through the third reactor, the second reactor, and the first reactor in sequence, and the sulfur dioxide-containing gas passes through the first reactor, the second reactor and the third reactor in sequence, in the first reactor All the internal sodium sulfite reacts to produce supersaturation to generate a large amount of sodium metabisulfite crystals, the tail gas is discharged from the third reactor, and the slurry containing sodium metabisulfite crystals is extracted from the first reactor and sent to the elutriation tank;
  • Crystal separation the crystal slurry of the first reactor realizes the coarse and fine separation of crystals and the concentration of crystals in the elutriation tank, and the high-quality crystals are extracted from the lower part of the elutriation tank and sent to the centrifuge; the fine crystals discharged from the upper part of the elutriation tank And the mother liquor of centrifugation is sent to the alkali tank, and it reacts with soda ash to transform into a slurry containing sodium sulfite crystals; the high-quality crystals that are centrifuged are sent to the dryer for drying;
  • the soda ash is discharged to the soda ash tank for storage, is fed quantitatively to the alkali preparation tank, and reacts with the centrifugal mother liquor, the elutriation tank discharge liquid, and the tail gas washing liquid in the alkali preparation tank, after defoaming and degassing Sent to the third reactor;
  • Exhaust gas treatment the exhaust gas discharged from each equipment and the dry exhaust gas produced by drying are sent to the tail suction tower, after the alkali liquid washing, the sulfur dioxide concentration in the exhaust gas will be discharged below 10ppm, and the washing liquid produced by the washing is sent to the alkali distribution tank for reuse .
  • the solid content of the circulating slurry of the first reactor, the second reactor, and the third reactor is 5-30%, and the temperature is 40-60°C.
  • the volume of the elutriation tank is 3-6 times the volume of the first reactor.
  • the concentration of the sulfur dioxide-containing gas is greater than 3%, and may be one or several combinations of sulfur incineration flue gas, pyrite incineration flue gas, organic amine desulfurization regenerated sulfur dioxide gas, and activated carbon desulfurization regenerated sulfur dioxide gas.
  • the first reactor, the second reactor, and the third reactor adopt a tower structure, the lower part of the reactor is a slurry zone, and the upper part is a mixing section.
  • Each reactor has a corresponding circulating pump to circulate The pump draws the slurry containing sodium sulfite from the lower part of the reactor.
  • the slurry and sulfur dioxide are in gas-liquid contact in the mixing section.
  • the sodium metabisulfite slurry produced by absorbing the sulfur dioxide gas falls into the lower part of the reactor, and the residual tail gas is discharged from the exhaust port on the upper part of the reactor.
  • the first reactor, the second reactor, and the third reactor the sodium sulfite slurry and the sulfur dioxide gas are in cocurrent contact, and the reactor resistance is 3-8kpa.
  • the elutriation tank is a vertical cylindrical structure, and the liquid discharged from the first-stage reactor enters tangentially from the bottom of the elutriation tank to produce a turbulent flow effect. Under the action of gravity and liquid recoil, the coarse and fine crystals are separated, The crystals are concentrated, the high-concentration coarse crystal slurry is discharged from the lower side to the centrifuge, and the low-concentration fine crystal slurry is discharged from the upper part to the mixing tank.
  • the dryer adopts an airflow drying type, and the inlet air temperature of the dryer is 130-160°C.
  • the alkali distribution tank is equipped with a stirrer and a defoaming device, the soda ash is neutralized with the centrifugal mother liquor, the elutriation tank drain, and the tail gas washing liquid to produce sodium sulfite, which is sent to the third after defoaming and degassing.
  • the solid content of the alkali distribution tank is 5-30%, and the pH is 5.0-7.0.
  • the present invention is suitable for the preparation of sodium metabisulfite from a variety of sulfur dioxide-containing gases, and provides a more economical and low-cost sulfur dioxide gas preparation process for sodium metabisulfite, with good by-product quality; compared with the prior art, the overall production cost is reduced by about 10% %, the main component content of by-products> 97.5%, far higher than the 96.5% required by the national standard for premium products.
  • the first reactor, the second reactor, and the third-party reactor of the present invention adopt a tower structure, which has low resistance, complete reaction, stability and reliability, and is especially suitable for large-scale production, while the traditional bubble reactor is used for intermittent operation. , The bubbling liquid level is high and the resistance is large.
  • Figure 1 is a schematic diagram of the system of the present invention.
  • Figure 1 101-product; 102-soda ash; 103-sulfur dioxide gas; 104-reaction tail gas; 1-third reactor; 2-third circulation pump; 3-second reactor; 4-second circulation pump ; 5-first reactor; 6-first circulating pump; 7-refill pump; 8-alkali tank; 9-first soda ash conveyor; 10-lye tank; 11-lye pump; 12-second Soda ash conveyor; 13-soda ash storage bin; 14-second exhaust gas washing circulating pump; 15-washing circulating tank; 16-first exhaust gas washing circulating pump; 17-tail gas washing tower; 18-washing tank; 19-centrifuge ; 20-dryer; 21-packaging machine; 22-jet reactor.
  • Figure 2 is a schematic structural diagram of a gas-liquid two-phase continuous reaction crystallization device
  • 23-crystal discharge section 23-crystal discharge section, 24-material liquid interface, 25-defoaming device, 26-washing water interface, 27-reaction tail gas outlet.
  • Figure 3 is a schematic diagram of the structure of a jet reactor.
  • a system for producing sodium metabisulfite includes a third reactor 1, a second reactor 3, and a first reactor 5.
  • the soda ash storage silo 13 is connected to the alkali tank 8 and the lye tank 10, respectively.
  • the output end of the lye tank 10 is connected to the upper part of the third reactor 1, and the output end of the lower part of the third reactor 1 is respectively reacted with the jet at the top of the third reactor 1 through the third circulation pump 2
  • Reactor 22 is connected to the upper part of the second reactor 3; the output end of the lower part of the second reactor 3 is respectively connected to the jet reactor 22 at the top of the second reactor 3 and the upper part of the first reactor 1 through the second circulating pump 4
  • the output end of the lower part of the first reactor 5 is connected to the jet reactor 22 and the elutriation tank 18 at the top of the first reactor 5 through the first circulation pump 6; the elutriation tank 18 passes through the centrifuge 19 and The dryer 20 is connected.
  • the output end of the top of the elutriation tank 18 and the liquid output end of the centrifuge 19 are both connected to the alkali distribution tank 8.
  • the gas output end of the dryer 20 is connected to the tail gas washing tower 17; the output end at the bottom of the lye tank 10 is connected to the washing circulation tank 15, and the output end at the bottom of the washing circulation tank 15 is connected to the tail gas washing tower 17;
  • the upper output end of the tower 17 is connected to the washing circulation tank 15, and the output end at the bottom of the tail gas washing tower 17 is connected to the middle part of the tail gas washing tower 17 and the alkali distribution tank 8 respectively.
  • the sulfur dioxide gas output pipeline is connected to the jet reactor 22 located in the upper part of the first reactor 5, and the gas output end at the top of the first reactor 5 is connected to the jet reactor 22 located in the upper part of the second reactor 3.
  • the upper part of the second reactor 3 The gas output end of is connected to the jet reactor 22 located on the upper part of the third reactor 1, and the gas output end on the top of the third reactor 1 is discharged outside the boundary.
  • the third reactor 1, the second reactor 3 and the first reactor 5 include crystallizers.
  • the top of the crystallizer is provided with a jet reactor 22, and the lower part of the crystallizer is connected to the upper part of the jet reactor 22 through a circulation pump.
  • the top of the jet reactor 22 is equipped with a gas input system; the bottom of the crystallizer is the crystal discharge section 23, the upper part of the crystallizer is also provided with a raw material liquid interface 24; the top of the crystallizer is also equipped with a reaction tail gas scrubber Device, the lower part of the device is provided with a defoaming device 25, and above the defoaming device 25 is also provided with a flushing water interface 26, and the top of the scrubbing device is a discharge outlet 27 for the reaction tail gas.
  • the lower part of the crystallizer is a conical structure with a contraction angle of 60-100°.
  • a settling pipe is connected to the lower part of the conical structure, and the conical structure and the settling pipe constitute the crystal discharge section 23.
  • the jet reactor 22 is provided with a discharge pipe 33, an expansion pipe 32, a throat pipe 31, a contraction pipe 30, and an inlet pipe 29 from bottom to top.
  • the top of the inlet pipe is provided with a raw gas interface 28, and the inlet pipe 29
  • the lower part is provided with a liquid interface 34;
  • the contraction angle of the contraction tube is 10-60°, and the expansion angle of the expansion tube is 5-30°;
  • the discharge tube 33 of the jet reactor 22 extends out of the top cover of the crystallizer, and its extension length It is 1000 ⁇ 4000mm.
  • a method for producing sodium metabisulfite using the above system comprising the following steps:
  • Reactive crystallization the sodium sulfite slurry passes through the third reactor 1, the second reactor 3, and the first reactor 5 in sequence, and the sulfur dioxide-containing gas passes through the first reactor 5, the second reactor 3 and the third reactor 1 in sequence , In the first reactor 5, all the sodium sulfite reacts to produce supersaturation to generate a large amount of sodium metabisulfite crystals.
  • the tail gas is discharged from the third reactor 3, and the slurry containing sodium metabisulfite crystals is extracted from the first reactor 5 and sent to the elutriation tank 18. ;
  • the solid content of the circulating slurry in the first reactor 5, the second reactor 3, and the third reactor 1 is 5-30%, and the temperature is 40-60°C.
  • the sodium sulfite slurry is in cocurrent contact with the sulfur dioxide gas, and the resistance of the reactor is 3 to 4 kpa.
  • Crystal separation the crystal slurry in the first reactor 5 realizes coarse and fine crystal separation and crystal concentration in the elutriation tank 18, and high-quality crystals are extracted from the lower part of the elutriation tank 18 and sent to the centrifuge 19; the elutriation tank 18 The fine crystals discharged from the upper part and the centrifugal mother liquor are sent to the alkali distribution tank 8, where they react with soda ash and are converted into a slurry containing sodium sulfite crystals; the high-quality centrifugal crystals are sent to the dryer 20 for drying; the volume of the elutriation tank 18 is the first reactor 5. 3 to 6 times the volume.
  • the soda ash is discharged to the soda ash tank for storage, is fed quantitatively to the alkali preparation tank, and reacts with the centrifugal mother liquor, the elutriation tank discharge liquid, and the exhaust gas washing liquid in the alkali preparation tank 8, and undergoes defoaming and degassing. Then it is sent to the third reactor 1; the alkali distribution tank is equipped with a stirrer and a defoaming device.
  • the soda ash is neutralized with the centrifugal mother liquor, the elutriation tank drain, and the tail gas washing liquid to generate sodium sulfite, which is defoamed and degassed It is sent to the third reactor, the solid content of the alkali distribution tank is 5-30%, and the pH is 5.0-7.0.
  • the comprehensive production cost is reduced by about 10%, and the main component content of the by-product is greater than 97.5%, which is much higher than the 96.5% required by the national standard for superior products.

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Abstract

本发明提供一种生产焦亚硫酸钠的系统及制备方法，属于化工领域。该方法是含二氧化硫气体依次通过第一反应器、第二反应器、第三反应器，过饱和的亚硫酸钠溶液依次通过第三反应器、第二反应器、第一反应器，在第一反应器中生成大量焦亚硫酸钠；当亚硫酸钠全部反应，达到反应终点，将含有焦亚硫酸钠的晶浆从第一反应器采出送至淘洗罐，粗晶体浆液进入离心机分离，离心母液经加入纯碱生成亚硫酸钠浆液送至第三反应器，离心分离的固态湿料送至干燥机干燥，再经过包装成焦亚硫酸钠产品；干燥产生的尾气经尾气塔碱洗除尘后排放，尾气水洗产生的洗涤液送至配碱槽，返回反应器。本发明制得的焦亚硫酸钠品质好，且工艺流程新颖、能耗低，具有广泛的推广和使用价值。

Description

一种生产焦亚硫酸钠的系统及制备方法 技术领域
本发明涉及化工领域，具体涉及一种生产焦亚硫酸钠的系统及制备方法。
背景技术
我国是一个资源生产和消费大国，然而在生产和消费的同时，也产生了重大的环境问题。近年来，资源回收型脱硫技术得到大规模应用，如有机胺脱硫技术、活性炭脱硫技术，其脱硫副产物为SO 2。传统方法是将SO 2制成硫酸，由于国内现阶段硫酸产能过剩，市场需求受区域性影响较大，且硫酸难以贮存和运输，存在胀库风险，经济价值较低，而利用SO 2生产焦亚硫酸钠可以实现良好的经济效益，不失为一种好方法。
化学工业出版社出版的《无机盐工业手册》(下册)介绍了一种传统生产焦亚硫酸钠的技术为，其过程为含二氧化硫气体依次通过三级鼓泡反应釜，生成焦亚硫酸钠晶体，再经离心分离，母液加纯碱制成碱液返回三级反应器，晶体去干燥即制得产品。由于传统工艺采用鼓泡反应器，气体阻力大，动力消耗较大；每个反应釜需要定期投切，气体压力波动大，操作繁琐；产品品质不稳定，结晶均匀度不佳；设备SO 2散排量大，生产环境差。
发明内容
本发明是针对现有技术存在的缺陷，提供一种生产焦亚硫酸钠的系统及制备方法。
本发明的目的可以通过以下技术方案实现：
一种生产焦亚硫酸钠的系统，该系统包括第三反应器，第二反应器和第一反应器，纯碱储仓分别与配碱槽和碱液槽相连，所述器和第一反应器，纯碱储仓分别与配碱槽和碱液槽相连，所述配碱槽的的输出端与第三反应器的上部相连，所述第三反应器下部的输出端通过第三循环泵分别与位于第三反应器顶部的喷射反应器和第二反应器的上部相连；第二反应器下部的输出端通过第二循环泵分别与位于第二反应器顶部的喷射反应器和第一反应器的上部相连；第一反应器下部的输出端通过第一循环泵分别与位于第一反应器顶部的喷射反应器和淘洗罐相连；所述的淘洗罐依次通过离心机以及干燥机相连。
本发明技术方案中：淘洗罐顶部的输出端以及离心机的液体输出端均与配碱槽相连。
本发明技术方案中：干燥机的气体输出端与尾气洗涤塔相连；碱液槽底部的输出端与洗涤循环槽相连，所述洗涤循环槽底部的输出端与尾气洗涤塔相连；所述尾气洗涤塔中上部的输出端与洗涤循环槽相连，所述尾气洗涤塔底部的输出端分别与尾气洗涤塔中部以及配碱槽相连。
本发明技术方案中：二氧化硫气体输出管道与位于第一反应器上部的喷射反应器相连，第一反应器顶部的气体输出端与位于第二反应器上部的喷射反应器相连，第二反应器上部的气体输出端与位于第三反应器上部的喷射反应器相连，所述第三反应器顶部的气体输出端排出界外。
本发明技术方案中：第三反应器，第二反应器和第一反应器包括结晶器，所述结晶器的顶部设有喷射反应器，所述结晶器的下部通过循环泵与喷射反应器的上部相连，且所述喷射反应器的顶部设有气体输入系统；结晶器的底部为晶体排出段，结晶器的上部还设有原料液接口；结晶器的顶部还设有反应尾气的洗涤装置，该装置中下部设有除沫装置，且除沫装置的上方还设有冲洗水接口，洗涤装置的顶部为反应尾气的排出口。
本发明技术方案中：所述结晶器下部为收缩的锥面结构，其收缩的夹角为60～100°，锥面结构下部连接有一段沉降管，锥面结构和沉降管构成了晶体排出段。
本发明技术方案中：所述喷射反应器从下到上依次设有排出管，扩张管、喉管、收缩管和进气管，所述进气管的顶部设有原料气接口，进气管的下部设有液体接口；收缩管的收缩角度为10～60°，扩张管的扩张角度为5～30°；所述喷射反应器的排出管伸出结晶器顶盖，其伸出长度为1000～4000mm。
一种利用上述的系统实现生产焦亚硫酸钠的方法，该方法包括如下步骤：
(1)反应结晶：亚硫酸钠浆液依次通过第三反应器、第二反应器、第一反应器，含二氧化硫气体依次通过第一反应器、第二反应器和第三反应器，在第一反应器内亚硫酸钠全部反应，生产过饱和生成大量焦亚硫酸钠晶体，尾气从第三反应器排出，从第一反应器采出含有焦亚硫酸钠晶体的浆液送至淘洗罐；
(2)晶体分离：第一反应器的晶体浆液在淘洗罐内实现晶体粗细分离、晶体提浓，从淘洗罐下部采出优质的晶体送至离心机；淘洗罐上部排出的细小晶体和离心母液送至配碱槽，与纯碱反应转化为含亚硫酸钠晶体的浆液；离心出的优质晶体被送至干燥机干燥；
(3)干燥和包装：离心出的焦亚硫酸钠晶体在干燥机内与热风换热，将晶体表面水分蒸干，之后固体粉料送入包装机包装成袋装产品；
(4)配碱，纯碱经卸料至纯碱罐储存，定量进料至配碱槽，在配碱槽内与离心母液、淘洗罐排液、尾气洗涤液反应，经消泡、脱气后送至第三反应器；
(5)尾气处理，各设备排放的尾气与干燥产生的干燥尾气送至尾吸塔，经过碱液洗涤，尾气中二氧化硫浓度将至10ppm以下排放，洗涤产生的洗涤液送至配碱槽重新利用。
上述方法中：所述第一反应器、第二反应器、第三反应器的循环浆液的固含量为5～30％，其温度为40～60℃。
上述方法中：淘洗罐容积为第一反应器容积的3～6倍。
上述方法中：所述含二氧化硫气体其浓度大于3％，可以是硫磺焚烧烟气、硫铁矿焚烧烟气、有机胺脱硫再生二氧化硫气体、活性炭脱硫再生二氧化硫气体中的一种或几种组合。
上述方法中：所述第一反应器、第二反应器、第三反应器采用塔式结构，反应器下部是浆液区，上部为混合段，每个反应器有与之对应的循环泵，循环泵从反应器下部抽取含亚硫酸钠的浆液，浆液与二氧化硫在混合段进行气液接触，吸收二氧化硫气体生成的焦亚硫酸钠浆液落入反应器下部，残余尾气从反应器上部排气口排出。
上述方法中：所述第一反应器、第二反应器、第三反应器，亚硫酸钠浆液与二氧化硫气体为顺流接触，反应器阻力为3～8kpa。
上述方法中：所述淘洗罐为立式圆筒结构，一级反应器排液从淘洗罐底部切向进入产生扰流效果，在重力和液体反冲力的作用下，实现晶体粗细分离、晶体提浓，高浓度粗晶体浆液从下部侧面排出到离心机，低浓度细晶体浆液从上部排出到配液槽。
上述方法中：所述干燥机采用气流干燥型式，干燥机进风温度为130～160℃。
上述方法中：所述配碱槽配有搅拌器、消泡装置，纯碱与离心母液、淘洗罐排液、尾气洗涤液进行中和反应生成亚硫酸钠，经消泡、脱气后送至第三反应器，配碱槽固含量为5～30％，pH为5.0～7.0。
本发明的有益效果：
1)本发明适用于多种含二氧化硫气体制备焦亚硫酸钠，提供了一种较经济的低成本的二氧化硫气体制备焦亚硫酸钠工艺，副产物品质好；与现有技术相比，综合生产成本降低约10％，副产物主成分含量＞97.5％，远高于国标优等品要求的96.5％。
2)本发明工艺过程新颖且安全可靠，环境友好；所采用装置结构简单、维修方便；
3)本发明第一反应器、第二反应器、第三方反应器采用塔式结构，阻力小，反应彻 底，稳定可靠，特别适用于大规模生产，而传统采用鼓泡式反应釜，间歇操作，鼓泡液位高阻力大。
4)本发明所有设备排气均收集到尾气洗涤塔，进行碱洗处理，回收了二氧化硫，厂房内无二氧化硫溢出，环境好，无二次污染。
附图说明
图1为本发明系统的示意图。
其中：图1：101-产品；102-纯碱；103-二氧化硫气体；104-反应尾气；1-第三反应器；2-第三循环泵；3-第二反应器；4-第二循环泵；5-第一反应器；6-第一循环泵；7-补液泵；8-配碱槽；9-第一纯碱输送器；10-碱液槽；11-碱液泵；12-第二纯碱输送器；13-纯碱储仓；14-第二尾气洗涤循环泵；15-洗涤循环槽；16-第一尾气洗涤循环泵；17-尾气洗涤塔；18-淘洗罐；19-离心机；20-干燥机；21-包装机；22-喷射反应器。
图2为气液两相连续反应结晶装置的结构示意图；
其中：23-晶体排出段，24-原料液接口，25-除沫装置，26-冲洗水接口，27-反应尾气的排出口。
图3为喷射反应器的结构示意图。
其中：28-原料气接口，29-进气管，30-收缩管，31-喉管，32-扩张管，33-排出管，34-液体接口。
具体实施方式
下面结合实施例对本发明做进一步说明，但本发明的保护范围不限于此：
如图1～3，一种生产焦亚硫酸钠的系统，该系统包括第三反应器1，第二反应器3和第一反应器5，纯碱储仓13分别与配碱槽8和碱液槽10相连，所述碱液槽10的输出端与第三反应器1的上部相连，所述第三反应器1下部的输出端通过第三循环泵2分别与位于第三反应器1顶部的喷射反应器22和第二反应器3的上部相连；第二反应器3下部的输出端通过第二循环泵4分别与位于第二反应器3顶部的喷射反应器22和第一反应器1的上部相连；第一反应器5下部的输出端通过第一循环泵6分别与位于第一反应器5顶部的喷射反应器22和淘洗罐18相连；所述的淘洗罐18依次通过离心机19以及干燥机20相连。
淘洗罐18顶部的输出端以及离心机19的液体输出端均与配碱槽8相连。
干燥机20的气体输出端与尾气洗涤塔17相连；碱液槽10底部的输出端与洗涤循环槽15相连，所述洗涤循环槽15底部的输出端与尾气洗涤塔17相连；所述尾气洗涤塔17中上部的输出端与洗涤循环槽15相连，所述尾气洗涤塔17底部的输出端分别与尾气洗涤塔17中部以及配碱槽8相连。
二氧化硫气体输出管道与位于第一反应器5上部的喷射反应器22相连，第一反应器5顶部的气体输出端与位于第二反应器3上部的喷射反应器22相连，第二反应器3上部的气体输出端与位于第三反应器1上部的喷射反应器22相连，所述第三反应器1顶部的气体输出端排出界外。
第三反应器1，第二反应器3和第一反应器5包括结晶器，所述结晶器的顶部设有喷射反应器22，所述结晶器的下部通过循环泵与喷射反应器22的上部相连，且所述喷射反应器22的顶部设有气体输入系统；结晶器的底部为晶体排出段23，结晶器的上部还设有原料液接口24；结晶器的顶部还设有反应尾气的洗涤装置，该装置中下部设有除沫装置25，且除沫装置25的上方还设有冲洗水接口26，洗涤装置的顶部为反应尾气的排出口27。
所述结晶器下部为收缩的锥面结构，其收缩的夹角为60～100°，锥面结构下部连接有一段沉降管，锥面结构和沉降管构成了晶体排出段23。
所述喷射反应器22从下到上依次设有排出管33，扩张管32、喉管31、收缩管30和进气管29，所述进气管的顶部设有原料气接口28，进气管29的下部设有液体接口34；收缩管的收缩角度为10～60°，扩张管的扩张角度为5～30°；所述喷射反应器22的排出管33伸出结晶器顶盖，其伸出长度为1000～4000mm。
一种利用上述系统生产焦亚硫酸钠的方法，该方法包括以下步骤：
(1)反应结晶：亚硫酸钠浆液依次通过第三反应器1、第二反应器3、第一反应器5，含二氧化硫气体依次通过第一反应器5、第二反应器3和第三反应器1，在第一反应器5内亚硫酸钠全部反应，生产过饱和生成大量焦亚硫酸钠晶体，尾气从第三反应器3排出，从第一反应器5采出含有焦亚硫酸钠晶体的浆液送至淘洗罐18；
其中：所述第一反应器5、第二反应器3、第三反应器1的循环浆液的固含量为5～30％，其温度为40～60℃。所述第一反应器、第二反应器、第三反应器，亚硫酸钠浆液与二氧化硫气体为顺流接触，反应器阻力为3～4kpa。
(2)晶体分离：第一反应器5的晶体浆液在淘洗罐18内实现晶体粗细分离、晶体提浓，从淘洗罐18下部采出优质的晶体送至离心机19；淘洗罐18上部排出的细小晶体和 离心母液送至配碱槽8，与纯碱反应转化为含亚硫酸钠晶体的浆液；离心出的优质晶体被送至干燥机20干燥；淘洗罐18容积为第一反应器5容积的3～6倍。
(3)干燥和包装：离心出的焦亚硫酸钠晶体在干燥机20内与热风换热，将晶体表面水分蒸干，之后固体粉料送入包装机21包装成袋装产品；所述干燥机采用气流干燥型式，干燥机进风温度为130～160℃。
(4)配碱，纯碱经卸料至纯碱罐储存，定量进料至配碱槽，在配碱槽8内与离心母液、淘洗罐排液、尾气洗涤液反应，经消泡、脱气后送至第三反应器1；所述配碱槽配有搅拌器、消泡装置，纯碱与离心母液、淘洗罐排液、尾气洗涤液进行中和反应生成亚硫酸钠，经消泡、脱气后送至第三反应器，配碱槽固含量为5～30％，pH为5.0～7.0。
(5)尾气处理，各设备排放的尾气与干燥产生的干燥尾气送至尾吸塔17，经过碱液洗涤，尾气中二氧化硫浓度将至10ppm以下排放，洗涤产生的洗涤液送至配碱槽重新利用。
与现有技术相比，综合生产成本降低约10％，副产物主成分含量＞97.5％，远高于国标优等品要求的96.5％。

Claims (10)

  1. 一种生产焦亚硫酸钠的系统，其特征在于：该系统包括第三反应器(1)，第二反应器(3)和第一反应器(5)，纯碱储仓(13)分别与配碱槽(8)和碱液槽(10)相连，所述配碱槽(8)的输出端与第三反应器(1)的上部相连，所述第三反应器(1)下部的输出端通过第三循环泵(2)分别与位于第三反应器(1)顶部的喷射反应器(22)和第二反应器(3)的上部相连；第二反应器(3)下部的输出端通过第二循环泵(4)分别与位于第二反应器(3)顶部的喷射反应器(22)和第一反应器(1)的上部相连；第一反应器(5)下部的输出端通过第一循环泵(6)分别与位于第一反应器(5)顶部的喷射反应器(22)和淘洗罐(18)相连；所述的淘洗罐(18)依次通过离心机(19)以及干燥机(20)相连。
  2. 根据权利要求1所述的生产焦亚硫酸钠的系统，其特征在于：淘洗罐(18)顶部的输出端以及离心机(19)的液体输出端均与配碱槽(8)相连。
  3. 根据权利要求1所述的生产焦亚硫酸钠的系统，其特征在于：干燥机(20)的气体输出端与尾气洗涤塔(17)相连；碱液槽(10)底部的输出端与洗涤循环槽(15)相连，所述洗涤循环槽(15)底部的输出端与尾气洗涤塔(17)相连；所述尾气洗涤塔(17)中上部的输出端与洗涤循环槽(15)相连，所述尾气洗涤塔(17)底部的输出端分别与尾气洗涤塔(17)中部以及配碱槽(8)相连。
  4. 根据权利要求1所述的生产焦亚硫酸钠的系统，其特征在于：二氧化硫气体输出管道与位于第一反应器(5)上部的喷射反应器(22)相连，第一反应器(5)顶部的气体输出端与位于第二反应器(3)上部的喷射反应器(22)相连，第二反应器(3)上部的气体输出端与位于第三反应器(1)上部的喷射反应器(22)相连，所述第三反应器(1)顶部的气体输出端排出界外。
  5. 根据权利要求4所述的生产焦亚硫酸钠的系统，其特征在于：第三反应器(1)，第二反应器(3)和第一反应器(5)包括结晶器，所述结晶器的顶部设有喷射反应器(22)，所述结晶器的下部通过循环泵与喷射反应器(22)的上部相连，且所述喷射反应器(22)的顶部设有气体输入系统；结晶器的底部为晶体排出段(23)，结晶器的上部还设有原料液接口(24)；结晶器的顶部还设有反应尾气的洗涤装置，该装置中下部设有除沫装置(25)，且除沫装置(25)的上方还设有冲洗水接口(26)，洗涤装置的顶部为反应尾气的排出口(27)。
  6. 根据权利要求4所述的生产焦亚硫酸钠的系统，其特征在于：所述结晶器下部为收缩的 锥面结构，其收缩的夹角为60～100°，锥面结构下部连接有一段沉降管，锥面结构和沉降管构成了晶体排出段(23)。
  7. 根据权利要求4所述的生产焦亚硫酸钠的系统，其特征在于：所述喷射反应器(22)从下到上依次设有排出管(33)，扩张管(32)、喉管(31)、收缩管(30)和进气管(29)，所述进气管的顶部设有原料气接口(28)，进气管(29)的下部设有液体接口(34)；收缩管的收缩角度为10～60°，扩张管的扩张角度为5～30°；所述喷射反应器(22)的排出管(33)伸出结晶器顶盖，其伸出长度为1000～4000mm。
  8. 一种利用权利要求1所述的系统实现生产焦亚硫酸钠的方法，其特征在于：该方法包括如下步骤：
    (1)反应结晶：亚硫酸钠浆液依次通过第三反应器(1)、第二反应器(3)、第一反应器(5)，含二氧化硫气体依次通过第一反应器(5)、第二反应器(3)和第三反应器(1)，在第一反应器(5)内亚硫酸钠全部反应，生产过饱和生成大量焦亚硫酸钠晶体，尾气从第三反应器(3)排出，从第一反应器(5)采出含有焦亚硫酸钠晶体的浆液送至淘洗罐(18)；
    (2)晶体分离：第一反应器(5)的晶体浆液在淘洗罐(18)内实现晶体粗细分离、晶体提浓，从淘洗罐(18)下部采出优质的晶体送至离心机(19)；淘洗罐(18)上部排出的细小晶体和离心母液送至配碱槽(8)，与纯碱反应转化为含亚硫酸钠晶体的浆液；离心出的优质晶体被送至干燥机(20)干燥；
    (3)干燥和包装：离心出的焦亚硫酸钠晶体在干燥机(20)内与热风换热，将晶体表面水分蒸干，之后固体粉料送入包装机(21)包装成袋装产品；
    (4)配碱，纯碱经卸料至纯碱罐储存，定量进料至配碱槽，在配碱槽(8)内与离心母液、淘洗罐排液、尾气洗涤液反应，经消泡、脱气后送至第三反应器(1)；
    (5)尾气处理，各设备排放的尾气与干燥产生的干燥尾气送至尾吸塔(17)，经过碱液洗涤，尾气中二氧化硫浓度将至10ppm以下排放，洗涤产生的洗涤液送至配碱槽重新利用。
  9. 根据权利要求8所述的方法，其特征在于：所述第一反应器(5)、第二反应器(3)、第三反应器(1)的循环浆液的固含量为5～30％，其温度为40～60℃。
  10. 根据权利要求8所述的方法，其特征在于：淘洗罐(18)容积为第一反应器(5)容积的3～6倍。
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CN108190920A (zh) * 2018-03-13 2018-06-22 铜鼓县湘鸿化工有限公司 一种焦亚硫酸钠的生产系统
CN110255585A (zh) * 2019-07-10 2019-09-20 南京工业大学 一种制备亚硫酸盐的装置及方法

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