WO2022160742A1 - 一种从含溴粗盐中回收高纯溴化钠的方法 - Google Patents

一种从含溴粗盐中回收高纯溴化钠的方法 Download PDF

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WO2022160742A1
WO2022160742A1 PCT/CN2021/119297 CN2021119297W WO2022160742A1 WO 2022160742 A1 WO2022160742 A1 WO 2022160742A1 CN 2021119297 W CN2021119297 W CN 2021119297W WO 2022160742 A1 WO2022160742 A1 WO 2022160742A1
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bromine
extraction
sodium bromide
acidified
water
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PCT/CN2021/119297
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French (fr)
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潘德安
李冠军
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北京工业大学
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Priority to US17/626,805 priority Critical patent/US20240010507A1/en
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/10—Bromides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B01D11/0488—Flow sheets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B01D11/0492—Applications, solvents used
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0018—Evaporation of components of the mixture to be separated
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/80—Compositional purity

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  • the invention relates to the field of resource recovery of bromine in the treatment process of waste circuit boards, in particular to a process of recovering high-purity sodium bromide from bromine-containing crude salt.
  • Circuit boards are an important part of electronic appliances, accounting for about 4%-7% of the total electronic waste, and their output shows an increasing trend.
  • the basic composition includes 40% metal, 30% resin and plastic and 30% glass fiber, which contains various elements, such as heavy metal elements copper, lead, tin, precious metal elements gold, silver and non-metallic elements bromine, etc. , with high-value recycling potential.
  • Fire disposal of waste circuit boards is mainly to treat waste circuit boards by incineration, heating and melting, etc., which can effectively reduce the volume of waste circuit boards and obtain metal rich bodies, which has the advantages of large processing capacity and high recovery degree.
  • pyrolysis technology, collaborative smelting technology and self-heating smelting technology are commonly used fire disposal technologies, but because the brominated flame retardants in waste circuit boards will decompose during the disposal process and escape in the form of flue gas or pyrolysis gas Therefore, the bromine-containing crude salt or the soot of the products of the tail gas absorption link exists in the bromide, which will pollute the environment and lose resources such as bromine if it is not treated.
  • sodium bromide is a widely used chemical, which can be used in photosensitive industry, perfume industry, printing and dyeing industry, etc. It can also be used for trace determination of cadmium, manufacture of bromide, inorganic and organic synthesis, photographic paper, etc.
  • the preparation method of sodium mainly includes neutralization method and reduction method, but all need the supply of raw material bromine or hydrogen bromide, and the cost is high, so reclaiming high-purity sodium bromide from bromine-containing crude salt has considerable economic value.
  • CN107138036A proposes to reduce the content of acid gas and dioxin in the molten pool smelting flue gas through quenching, dynamic wave washing, lye absorption and activated carbon adsorption, but does not pay attention to the subsequent recovery and treatment of bromine-containing crude salt, which is likely to cause secondary pollution.
  • Shen Chao used chlorine gas oxidation to enrich the bromine resources in the molten pool smelting soot alkali leaching solution, but there were problems such as high chlorine gas toxicity, untreated excess chlorine gas, and difficult operation control. And the product contains a large amount of urea impurities, and the product purity is low.
  • the invention proposes to use hydrochloric acid and sodium chlorate for acidification and oxidation, effectively control the acidification and oxidation process by adjusting the added amount of hydrochloric acid and sodium chlorate, and absorbs and reuses the exhaust gas, thereby avoiding secondary pollution and waste of resources.
  • Sodium carbonate synergistic stripping achieves high stripping rate under alkaline conditions, greatly reduces the amount of urea, and improves the purity of the product.
  • the purpose of the present invention is to solve the problems of difficult control of bromine salt conversion, low recovery rate and low product purity in the recovery process of bromine-containing crude salt, and proposes a combined process such as acidification oxidation, multi-stage extraction and synergistic stripping from bromine-containing salts.
  • the new method of directly recovering and preparing high-purity sodium bromide from crude salt realizes the efficient conversion and enrichment of bromine resources in bromine-containing crude salt, and has the characteristics of high product purity, simple operation and environmental friendliness.
  • a kind of method of reclaiming high-purity sodium bromide from bromine-containing crude salt of the present invention is carried out as follows:
  • (1) water leaching filtration the bromine-containing coarse salt is soaked and filtered with tap water, wherein the volume of tap water and bromine-containing coarse salt: mass ratio is 3:1-5:1 liter/kg, and the water immersion time is 10-20min , the water immersion temperature is 25-35 °C, and the water leaching solution and the water leaching slag are obtained, and the water leaching slag is processed in a centralized manner;
  • step (2) acidification and oxidation: the water infusion solution obtained in step (1) is acidified with 36% concentrated hydrochloric acid, and the addition amount of concentrated hydrochloric acid is 0.4-0.8L/L water infusion solution, then sodium chlorate is added and fully stirred, and the chloric acid
  • the amount of sodium added is 10-20g/L water leaching solution, during which concentrated hydrochloric acid is used to maintain the pH of the system at 0-1, the reaction time is 30-60min, and the reaction temperature is 25-35°C to obtain the acidified and oxidized liquid and the acidified and oxidized tail gas, The acidified oxidation tail gas is absorbed by the lye and returned to the acidified oxidation process;
  • step (3) multistage extraction the acidified and oxidized liquid obtained in step (2) adopts carbon tetrachloride to carry out multistage extraction, wherein the volume ratio of carbon tetrachloride to the acidified and oxidized liquid is 1.5:1-2.5:1, The number of extraction stages is 2-5, the extraction time is 2-8min, and the extraction temperature is 25-35°C to obtain an extract and a raffinate, and the raffinate is evaporated and crystallized to obtain crude sodium bromide for centralized treatment;
  • Evaporative crystallization Evaporate and crystallize the back extract obtained in step (4) to obtain sodium bromide, wherein the evaporative crystallization temperature is 110°C-140°C.
  • the bromine resources in the bromine-containing crude salt are enriched and purified by the combined processes of acidification oxidation, multi-stage extraction and synergistic stripping, and high-efficiency conversion of bromine resources is directly recovered and prepared. Pure sodium bromide, and no waste liquid is generated during the implementation process, and has the characteristics of high product purity, simple operation, and environmental friendliness.
  • Fig. 1 represents a kind of method flow chart that reclaims high-purity sodium bromide from bromine-containing crude salt
  • (1) water leaching filtration the bromine-containing coarse salt is soaked and filtered with tap water, wherein the volume of tap water and bromine-containing coarse salt: mass ratio is 3:1 liter/kg, and the water immersion time is 10min, and the water immersion temperature is 25 °C to obtain water leaching solution and water leaching residue, and the water leaching slag is centrally treated;
  • step (2) acidification and oxidation: the water infusion solution obtained in step (1) is acidified with 36% concentrated hydrochloric acid, and the addition amount of concentrated hydrochloric acid is 0.4L/L water infusion solution, then sodium chlorate is added and fully stirred, and sodium chlorate is added Amount is 10g/L, utilizes concentrated hydrochloric acid to maintain the pH of the system to be 1 during the period, the reaction time is 30min, and the reaction temperature is 25 ° C to obtain the acidified oxidation back liquid and the acidified oxidation tail gas, and the acidified oxidation tail gas is returned to the acidified oxidation process after being absorbed by the lye;
  • step (3) multistage extraction the acidified and oxidized liquid obtained in step (2) adopts carbon tetrachloride to carry out multistage extraction, wherein the volume ratio of carbon tetrachloride to the acidified and oxidized liquid is 1.5:1, and the extraction stage number is 2, the extraction time is 2min, and the extraction temperature is 25°C to obtain an extract and a raffinate, and the raffinate is evaporated and crystallized to obtain crude sodium bromide for centralized treatment;
  • Evaporative crystallization Evaporate and crystallize the back extract obtained in step (4) to obtain high-purity sodium bromide, wherein the evaporative crystallization temperature is 110°C.
  • the recovery rate of sodium bromide is 98.4%, and the obtained sodium bromide crystal has a purity of 99.1%, which meets the standard of high-quality sodium bromide (NaBr ⁇ 99.0%) in the national Ministry of Chemical Industry standard HG/T3809-2006.
  • (1) water leaching filtration the bromine-containing coarse salt is soaked and filtered with tap water, wherein the volume of tap water and bromine-containing coarse salt: mass ratio is 5:1 liter/kg, and the water immersion time is 20min, and the water immersion temperature is 35 °C to obtain water leaching solution and water leaching residue, and the water leaching slag is centrally treated;
  • step (2) acidification and oxidation: the water infusion solution obtained in step (1) is acidified with 36% concentrated hydrochloric acid, and the addition amount of concentrated hydrochloric acid is 0.8L/L water infusion solution, then sodium chlorate is added and fully stirred, and the sodium chlorate adds Amount is 20g/L, utilizes concentrated hydrochloric acid to maintain the pH of the system to be 0 during the period, the reaction time is 60min, and the reaction temperature is 35 ° C to obtain the acidified oxidation back liquid and the acidified oxidation tail gas, and the acidified oxidation tail gas is returned to the acidified oxidation process after being absorbed by the lye;
  • step (3) multistage extraction the acidified and oxidized liquid obtained in step (2) adopts carbon tetrachloride to carry out multistage extraction, wherein the volume ratio of carbon tetrachloride to the acidified and oxidized liquid is 2.5:1, and the number of extraction stages is 5, the extraction time is 8min, and the extraction temperature is 35°C to obtain an extract and a raffinate, and the raffinate is evaporated and crystallized to obtain crude sodium bromide for centralized treatment;
  • Evaporative crystallization Evaporate and crystallize the back extract obtained in step (4) to obtain high-purity sodium bromide, wherein the evaporative crystallization temperature is 140°C.
  • the recovery rate of sodium bromide is 99.3%, and the purity of the obtained sodium bromide crystal is 99.7%, which reaches the standard of excellent sodium bromide product (NaBr ⁇ 99.0%) in the national Ministry of Chemical Industry standard HG/T3809-2006.
  • (1) water leaching filtration the bromine-containing coarse salt is soaked and filtered with tap water, wherein the volume of tap water and bromine-containing coarse salt: mass ratio is 4:1 liter/kg, and the water immersion time is 15min, and the water immersion temperature is 30 °C to obtain water leaching solution and water leaching residue, and the water leaching slag is centrally treated;
  • step (2) acidification and oxidation: the water infusion solution obtained in step (1) is acidified with 36% concentrated hydrochloric acid, and the addition amount of concentrated hydrochloric acid is 0.6L/L water infusion solution, then sodium chlorate is added and fully stirred, and the sodium chlorate is added The amount is 15g/L, and the pH of the system is maintained at 0.5 using concentrated hydrochloric acid, the reaction time is 45min, and the reaction temperature is 30 ° C to obtain the acidified oxidation back liquid and the acidified oxidation tail gas, and the acidified oxidation tail gas is absorbed by the lye and returns to the acidification oxidation process;
  • step (3) multistage extraction the acidified and oxidized liquid obtained in step (2) adopts carbon tetrachloride to carry out multistage extraction, wherein the volume ratio of carbon tetrachloride to the acidified and oxidized liquid is 2:1, and the extraction stage is 4, the extraction time is 5min, and the extraction temperature is 30°C to obtain an extract and a raffinate, and the raffinate is evaporated and crystallized to obtain crude sodium bromide for centralized treatment;
  • Evaporative crystallization Evaporate and crystallize the back extract obtained in step (4) to obtain high-purity sodium bromide, wherein the evaporative crystallization temperature is 125°C.
  • the recovery rate of sodium bromide is 99.0%, and the obtained sodium bromide crystal has a purity of 99.5%, which meets the standard of excellent sodium bromide product (NaBr ⁇ 99.0%) in the national Ministry of Chemical Industry standard HG/T3809-2006.
  • (1) water leaching filtration the bromine-containing coarse salt is soaked and filtered with tap water, wherein the volume of tap water and bromine-containing coarse salt: mass ratio is 3.5:1 liter/kg, and the water immersion time is 13min, and the water immersion temperature is 28 °C to obtain water leaching solution and water leaching residue, and the water leaching slag is centrally treated;
  • step (2) acidification and oxidation: the water infusion solution obtained in step (1) is acidified with 36% concentrated hydrochloric acid, and the addition amount of concentrated hydrochloric acid is 0.5L/L water infusion solution, then sodium chlorate is added and fully stirred, and the sodium chlorate adds The amount is 13g/L, and the pH of the system is maintained at 0.6 by using concentrated hydrochloric acid during the period, the reaction time is 40min, and the reaction temperature is 28 ° C to obtain the acidified oxidation back liquid and the acidified oxidation tail gas, and the acidified oxidation tail gas is returned to the acidification oxidation process after being absorbed by the lye;
  • step (3) multi-stage extraction the acidified and oxidized liquid obtained in step (2) adopts carbon tetrachloride to carry out multi-stage extraction, wherein the volume ratio of carbon tetrachloride to the acidified and oxidized liquid is 1.8:1, and the number of extraction stages is 4, the extraction time is 5min, and the extraction temperature is 28° C. to obtain an extract and a raffinate, and the raffinate is evaporated and crystallized to obtain crude sodium bromide for centralized treatment;
  • Evaporative crystallization Evaporate and crystallize the back extract obtained in step (4) to obtain high-purity sodium bromide, wherein the evaporative crystallization temperature is 120°C.
  • the recovery rate of sodium bromide is 98.8%, and the purity of the obtained sodium bromide crystal is 99.3%, which reaches the standard of excellent sodium bromide product (NaBr ⁇ 99.0%) in the national Ministry of Chemical Industry standard HG/T3809-2006.
  • (1) water leaching filtration the bromine-containing coarse salt is soaked and filtered with tap water, wherein the volume of tap water and bromine-containing coarse salt: mass ratio is 4.5:1 liter/kg, and the water immersion time is 17min, and the water immersion temperature is 30 °C to obtain water leaching solution and water leaching residue, and the water leaching slag is centrally treated;
  • step (2) acidification and oxidation: the water infusion solution obtained in step (1) is acidified with 36% concentrated hydrochloric acid, and the addition amount of concentrated hydrochloric acid is 0.7L/L water infusion solution, then sodium chlorate is added and fully stirred, and the sodium chlorate adds The amount is 17g/L, the pH of the system is maintained at 0-1 by using concentrated hydrochloric acid during the period, the reaction time is 50min, and the reaction temperature is 30 ° C to obtain the acidified oxidation liquid and acidified oxidation tail gas, and the acidified oxidation tail gas is absorbed by the lye and returned to the acidified oxidation process;
  • step (3) multistage extraction the acidified and oxidized liquid obtained in step (2) adopts carbon tetrachloride to carry out multistage extraction, wherein the volume ratio of carbon tetrachloride to the acidified and oxidized liquid is 2.5:1, and the number of extraction stages is 4.
  • the extraction time is 7min, and the extraction temperature is 30°C to obtain the extract and the raffinate, and the raffinate is evaporated and crystallized to obtain crude sodium bromide for centralized treatment;
  • Evaporative crystallization Evaporate and crystallize the back extract obtained in step (4) to obtain high-purity sodium bromide, wherein the evaporative crystallization temperature is 130°C.
  • the recovery rate of sodium bromide is 99.2%, and the obtained sodium bromide crystal has a purity of 99.6%, which meets the standard of high-quality sodium bromide (NaBr ⁇ 99.0%) in the national Ministry of Chemical Industry standard HG/T3809-2006.
  • (1) water leaching filtration the bromine-containing coarse salt is soaked and filtered with tap water, wherein the volume of tap water and bromine-containing coarse salt: mass ratio is 4:1 liter/kg, and the water immersion time is 16min, and the water immersion temperature is 30 °C to obtain water leaching solution and water leaching residue, and the water leaching slag is centrally treated;
  • step (2) acidification and oxidation: the water infusion solution obtained in step (1) is acidified with 36% concentrated hydrochloric acid, and the addition amount of concentrated hydrochloric acid is 0.6L/L water infusion solution, then sodium chlorate is added and fully stirred, and the sodium chlorate is added The amount is 17g/L, the pH of the system is maintained at 0-1 by using concentrated hydrochloric acid during the period, the reaction time is 50min, and the reaction temperature is 25°C to obtain acidified oxidation liquid and acidified oxidation tail gas. process;
  • step (3) multistage extraction the acidified and oxidized liquid obtained in step (2) adopts carbon tetrachloride to carry out multistage extraction, wherein the volume ratio of carbon tetrachloride to the acidified and oxidized liquid is 2:1, and the extraction stage is 3, the extraction time is 4min, and the extraction temperature is 25°C to obtain an extract and a raffinate, and the raffinate is evaporated and crystallized to obtain crude sodium bromide for centralized treatment;
  • Evaporative crystallization Evaporate and crystallize the back extract obtained in step (4) to obtain high-purity sodium bromide, wherein the evaporative crystallization temperature is 135°C.
  • the sodium bromide recovery rate is 99.1%, and the obtained sodium bromide crystal has a purity of 99.4%, which meets the standard of high-quality sodium bromide (NaBr ⁇ 99.0%) in the national Ministry of Chemical Industry standard HG/T3809-2006.

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Abstract

一种从含溴粗盐中回收高纯溴化钠的方法，属于废线路板处理过程中溴的资源化回收领域，特别涉及从含溴粗盐中回收高纯溴化钠的方法。主要包括酸化氧化、多级萃取、协同反萃等步骤。与传统氯气氧化、单一尿素反萃技术相比，通过合理调节盐酸和氯酸钠的加入量有效控制酸化氧化过程，且对尾气进行吸收回用，避免了二次污染和资源浪费，同时采用尿素和碳酸钠进行协同反萃，实现了高反萃率，并且大大减少了尿素的用量，得到了高纯度的溴化钠晶体，实现了含溴粗盐中溴资源的高效回收。本发明具有产品纯度高、操作简单、环境友好等特点。

Description

一种从含溴粗盐中回收高纯溴化钠的方法 技术领域
本发明涉及废线路板处理过程中溴的资源化回收领域，特别涉及从含溴粗盐回收高纯溴化钠的过程。
背景技术
线路板是电子电器的重要组成部分，约占电子废弃物总量的4％-7％，且其产量呈现递增趋势。线路板种类繁多，但基本组成包括40％金属，30％树脂和塑料以及30％玻璃纤维，其中含有多种元素，如重金属元素铜、铅、锡，贵金属元素金、银以及非金属元素溴等，具有高值化回收潜力。
火法处置废线路板主要是通过焚烧、加热熔融等方法处理废线路板，能够实现废线路板处理的有效减容并获得金属富集体，具有处理量大、回收程度高的优点。其中热解技术、协同熔炼技术以及自热熔炼技术是常用的火法处置技术，但由于废线路板中的溴化阻燃剂在处置过程中会分解并以烟气或热解气的形式逸出，因而导致尾气吸收环节的产物含溴粗盐或烟灰中存在溴化物，如果不经处理将会污染环境同时损失了其中的溴等资源。同时，溴化钠是用途广泛的化学药品，可用于感光工业，香料工业，印染工业等工业，还可用于微量测定镉，制造溴化物，无机和有机合成，照相纸版等方面，目前溴化钠的制备方法主要有中和法与还原法，但都需要原料溴素或溴化氢的供应，成本高，因此从含溴粗盐中回收高纯溴化钠具有可观的经济价值。
CN107138036A提出将熔池熔炼烟气通过急冷、动力波洗涤、碱液吸收与活性炭吸附降低其中酸性气体与二噁英含量，但未关注到含溴粗盐的后续回收处理，易造成二次污染。沈超对熔池熔炼烟灰碱浸液采用氯气氧化的方法富集其中的溴资源，但存在氯气毒性大、多余氯气未处理以及操作难以控制等问题，同时采用单一尿素反萃，反萃效率低且产物中含有大量尿素杂质，产物纯度低。本发明提出利用盐酸和氯酸钠进行酸化氧化，通过调节盐酸和氯酸钠的加入量有效控制酸化氧化过程，且对尾气进行吸收回用，避免了二次污染和资源浪费，同时采用尿素和碳酸钠协同反萃，在碱性条件下实现了高反萃率，并且大大减少了尿素的用量，提高了产物的纯度。
发明内容
本发明的目的是解决含溴粗盐回收过程中溴盐转化难以控制、回收率低、产物纯度不高等问题，提出了一种通过酸化氧化、多级萃取和协同反萃等组合工艺从含溴粗盐中直接回收制备得到高纯溴化钠的全新方法，实现了含溴粗盐中溴资源的高效转化与富集，具有产品纯度高、操作简单、环境友好等特点。
本发明所述的一种从含溴粗盐中回收高纯溴化钠的方法如下步骤进行：
(1)水浸过滤：将含溴粗盐用自来水水浸并过滤，其中自来水与含溴粗盐的体积：质量比为3:1-5:1升/公斤，水浸时间为10-20min，水浸温度为25-35℃，得到水浸液和水浸渣，水浸渣集中处理；
(2)酸化氧化：将步骤(1)得到的水浸液用36％浓盐酸进行酸化，浓盐酸加入量为0.4-0.8L/L水浸液，然后加入氯酸钠并充分搅拌，氯酸钠加入量为10-20g/L水浸液，期间利用浓盐酸维持体系pH为0-1，反应时间为30-60min，反应温度为25-35℃，得到酸化氧化后液和酸化氧化尾气，酸化氧化尾气经碱液吸收后返回酸化氧化工序；
(3)多级萃取：将步骤(2)得到的酸化氧化后液采用四氯化碳进行多级萃取，其中四氯化碳与酸化氧化后液的体积比为1.5:1-2.5:1，萃取级数为2-5，萃取时间为2-8min，萃取温度为25-35℃，得到萃取液和萃余液，萃余液经蒸发结晶得到粗溴化钠进行集中处理；
(4)协同反萃：向步骤(3)得到的萃取液中加入反萃剂并不断搅拌，当反萃液pH为6-7时，停止加入反萃剂，再反应5-10min，得到有机相和反萃液，有机相返步骤(3)多级萃取工序，其中反萃剂由碳酸钠和尿素混合溶液组成，碳酸钠与尿素的摩尔比为3:1，反萃剂浓度为20-40g/L，反应温度为25-35℃；
(5)蒸发结晶：将步骤(4)得到的反萃液进行蒸发结晶，得到溴化钠，其中蒸发结晶温度为110℃-140℃。
与现有技术相比，本发明采用酸化氧化、多级萃取与协同反萃等组合工艺将含溴粗盐中的溴资源进行了富集提纯，通过溴资源的高效转化直接回收制备得到了高纯溴化钠，且实施过程中无废液产生，具有产品纯度高、操作简单、环境友好等特点。
附图说明
图1表示一种从含溴粗盐中回收高纯溴化钠的方法流程图
具体实施方式
实施例1
按照如下步骤进行：
(1)水浸过滤：将含溴粗盐用自来水水浸并过滤，其中自来水与含溴粗盐的体积：质量比为3:1升/公斤，水浸时间为10min，水浸温度为25℃，得到水浸液和水浸渣，水浸渣集中处理；
(2)酸化氧化：将步骤(1)得到的水浸液用36％浓盐酸进行酸化，浓盐酸加入量为0.4L/L水浸液，然后加入氯酸钠并充分搅拌，氯酸钠加入量为10g/L，期间利用浓盐酸维持体系pH为1，反应时间为30min，反应温度为25℃，得到酸化氧化后液和酸化氧化尾气，酸化氧化尾气经碱液吸收后返回酸化氧化工序；
(3)多级萃取：将步骤(2)得到的酸化氧化后液采用四氯化碳进行多级萃取，其中四氯化碳与酸化氧化后液的体积比为1.5:1，萃取级数为2，萃取时间为2min，萃取温度为25℃，得到萃取液和萃余液，萃余液经蒸发结晶得到粗溴化钠进行集中处理；
(4)协同反萃：向步骤(3)得到的萃取液中加入反萃剂并不断搅拌，当反萃液pH为6时，停止加入反萃剂，再反应5min，得到有机相和反萃液，有机相返步骤(3)多级萃取工序，其中反萃剂由碳酸钠和尿素混合溶液组成，碳酸钠与尿素的摩尔比为3:1，反萃剂浓度为20g/L，反应温度为25℃；
(5)蒸发结晶：将步骤(4)得到的反萃液进行蒸发结晶，得到高纯溴化钠，其中蒸发结晶温度为110℃℃。
溴化钠回收率98.4％，得到的溴化钠晶体纯度为99.1％，达到国家化工部标准HG/T3809-2006中溴化钠优等品(NaBr≥99.0％)的标准。
实施例2
按照如下步骤进行：
(1)水浸过滤：将含溴粗盐用自来水水浸并过滤，其中自来水与含溴粗盐的体积：质量比为5:1升/公斤，水浸时间为20min，水浸温度为35℃，得到水浸液和水浸渣，水浸渣集中处理；
(2)酸化氧化：将步骤(1)得到的水浸液用36％浓盐酸进行酸化，浓盐酸加入量为0.8L/L水浸液，然后加入氯酸钠并充分搅拌，氯酸钠加入量为20g/L，期间利用浓盐酸维持体系pH为0，反应时间为60min，反应温度为35℃，得到酸化氧化后液和酸化氧化尾气，酸化氧化尾气经碱液吸收后返回酸化氧化工序；
(3)多级萃取：将步骤(2)得到的酸化氧化后液采用四氯化碳进行多级萃取，其中四氯化碳与酸化氧化后液的体积比为2.5:1，萃取级数为5，萃取时间为8min，萃取温度为35℃，得到萃取液和萃余液，萃余液经蒸发结晶得到粗溴化钠进行集中处理；
(4)协同反萃：向步骤(3)得到的萃取液中加入反萃剂并不断搅拌，当反萃液pH为7时，停止加入反萃剂，再反应10min，得到有机相和反萃液，有机相返步骤(3)多级萃取工序，其中反萃剂由碳酸钠和尿素混合溶液组成，碳酸钠与尿素的摩尔比为3:1，反萃剂浓度为40g/L，反应温度为35℃；
(5)蒸发结晶：将步骤(4)得到的反萃液进行蒸发结晶，得到高纯溴化钠，其中蒸发结晶温度为140℃。
溴化钠回收率99.3％，得到的溴化钠晶体纯度为99.7％，达到国家化工部标准HG/T3809-2006中溴化钠优等品(NaBr≥99.0％)的标准。
实施例3
按照如下步骤进行：
(1)水浸过滤：将含溴粗盐用自来水水浸并过滤，其中自来水与含溴粗盐的体积：质量比为4:1升/公斤，水浸时间为15min，水浸温度为30℃，得到水浸液和水浸渣，水浸渣集中处理；
(2)酸化氧化：将步骤(1)得到的水浸液用36％浓盐酸进行酸化，浓盐酸加入量为0.6L/L水浸液，然后加入氯酸钠并充分搅拌，氯酸钠加入量为15g/L，期间利用浓盐酸维持体系pH为0.5，反应时间为45min，反应温度为30℃，得到酸化氧化后液和酸化氧化尾气，酸化氧化尾气经碱液吸收后返回酸化氧化工序；
(3)多级萃取：将步骤(2)得到的酸化氧化后液采用四氯化碳进行多级萃取，其中四氯化碳与酸化氧化后液的体积比为2:1，萃取级数为4，萃取时间为5min，萃取温度为30℃，得到萃取液和萃余液，萃余液经蒸发结晶得到粗溴化钠进行集中处理；
(4)协同反萃：向步骤(3)得到的萃取液中加入反萃剂并不断搅拌，当反萃液pH为6.5时，停止加入反萃剂，再反应8min，得到有机相和反萃液，有机相返步骤(3)多级萃取工序，其中反萃剂由碳酸钠和尿素混合溶液组成，碳酸钠与尿素的摩尔比为3:1，反萃剂浓度为30g/L，反应温度为30℃；
(5)蒸发结晶：将步骤(4)得到的反萃液进行蒸发结晶，得到高纯溴化钠，其中蒸发结晶温度为125℃。
溴化钠回收率99.0％，得到的溴化钠晶体纯度为99.5％，达到国家化工部标准HG/T3809-2006中溴化钠优等品(NaBr≥99.0％)的标准。
实施例4
按照如下步骤进行：
(1)水浸过滤：将含溴粗盐用自来水水浸并过滤，其中自来水与含溴粗盐的体积：质量比为3.5:1升/公斤，水浸时间为13min，水浸温度为28℃，得到水浸液和水浸渣，水浸渣集中处理；
(2)酸化氧化：将步骤(1)得到的水浸液用36％浓盐酸进行酸化，浓盐酸加入量为0.5L/L水浸液，然后加入氯酸钠并充分搅拌，氯酸钠加入量为13g/L，期间利用浓盐酸维持体系pH为0.6，反应时间为40min，反应温度为28℃，得到酸化氧化后液和酸化氧化尾气，酸化氧化尾气经碱液吸收后返回酸化氧化工序；
(3)多级萃取：将步骤(2)得到的酸化氧化后液采用四氯化碳进行多级萃取，其中四氯化碳与酸化氧化后液的体积比为1.8:1，萃取级数为4，萃取时间为5min，萃取温度为28℃，得到萃取液和萃余液，萃余液经蒸发结晶得到粗溴化钠进行集中处理；
(4)协同反萃：向步骤(3)得到的萃取液中加入反萃剂并不断搅拌，当反萃液pH为6.5时，停止加入反萃剂，再反应7min，得到有机相和反萃液，有机相返步骤(3)多级萃取工序，其中反萃剂由碳酸钠和尿素混合溶液组成，碳酸钠与尿素的摩尔比为3:1，反萃剂浓度为25g/L，反应温度为28℃；
(5)蒸发结晶：将步骤(4)得到的反萃液进行蒸发结晶，得到高纯溴化钠，其中蒸发结晶温度为120℃。
溴化钠回收率98.8％，得到的溴化钠晶体纯度为99.3％，达到国家化工部标准 HG/T3809-2006中溴化钠优等品(NaBr≥99.0％)的标准。
实施例5
按照如下步骤进行：
(1)水浸过滤：将含溴粗盐用自来水水浸并过滤，其中自来水与含溴粗盐的体积：质量比为4.5:1升/公斤，水浸时间为17min，水浸温度为30℃，得到水浸液和水浸渣，水浸渣集中处理；
(2)酸化氧化：将步骤(1)得到的水浸液用36％浓盐酸进行酸化，浓盐酸加入量为0.7L/L水浸液，然后加入氯酸钠并充分搅拌，氯酸钠加入量为17g/L，期间利用浓盐酸维持体系pH为0-1，反应时间为50min，反应温度为30℃，得到酸化氧化后液和酸化氧化尾气，酸化氧化尾气经碱液吸收后返回酸化氧化工序；
(3)多级萃取：将步骤(2)得到的酸化氧化后液采用四氯化碳进行多级萃取，其中四氯化碳与酸化氧化后液的体积比为2.5:1，萃取级数为4，萃取时间为7min，萃取温度为30℃，得到萃取液和萃余液，萃余液经蒸发结晶得到粗溴化钠进行集中处理；
(4)协同反萃：向步骤(3)得到的萃取液中加入反萃剂并不断搅拌，当反萃液pH为6.5时，停止加入反萃剂，再反应8min，得到有机相和反萃液，有机相返步骤(3)多级萃取工序，其中反萃剂由碳酸钠和尿素混合溶液组成，碳酸钠与尿素的摩尔比为3:1，反萃剂浓度为35g/L，反应温度为30℃；
(5)蒸发结晶：将步骤(4)得到的反萃液进行蒸发结晶，得到高纯溴化钠，其中蒸发结晶温度为130℃。
溴化钠回收率99.2％，得到的溴化钠晶体纯度为99.6％，达到国家化工部标准HG/T3809-2006中溴化钠优等品(NaBr≥99.0％)的标准。
实施例6
按照如下步骤进行：
(1)水浸过滤：将含溴粗盐用自来水水浸并过滤，其中自来水与含溴粗盐的体积：质量比为4:1升/公斤，水浸时间为16min，水浸温度为30℃，得到水浸液和水浸渣，水浸渣集中处理；
(2)酸化氧化：将步骤(1)得到的水浸液用36％浓盐酸进行酸化，浓盐酸加入量为0.6L/L水浸液，然后加入氯酸钠并充分搅拌，氯酸钠加入量为17g/L，期间利用浓盐酸维持体系pH为0-1，反应时间为50min，反应温度为25℃，得到酸化氧化后液和酸化氧化尾气，酸化氧化尾气经碱液吸收后返回酸化氧化工序；
(3)多级萃取：将步骤(2)得到的酸化氧化后液采用四氯化碳进行多级萃取，其中四氯化碳与酸化氧化后液的体积比为2:1，萃取级数为3，萃取时间为4min，萃取温度为25℃，得到萃取液和萃余液，萃余液经蒸发结晶得到粗溴化钠进行集中处理；
(4)协同反萃：向步骤(3)得到的萃取液中加入反萃剂并不断搅拌，当反萃液pH为7时，停止加入反萃剂，再反应7min，得到有机相和反萃液，有机相返步骤(3)多级萃取工序，其中反萃剂由碳酸钠和尿素混合溶液组成，碳酸钠与尿素的摩尔比为3:1，反萃剂浓度为25g/L，反应温度为25℃；
(5)蒸发结晶：将步骤(4)得到的反萃液进行蒸发结晶，得到高纯溴化钠，其中蒸发结晶温度为135℃。
溴化钠回收率99.1％，得到的溴化钠晶体纯度为99.4％，达到国家化工部标准HG/T3809-2006中溴化钠优等品(NaBr≥99.0％)的标准。

Claims (4)

  1. 一种从含溴粗盐中回收高纯溴化钠的方法，其特征在于，具体步骤如下：
    (1)水浸过滤：将含溴粗盐用自来水水浸并过滤，其中自来水与含溴粗盐的体积：质量比为3:1-5:1升/公斤，水浸时间为10-20min，水浸温度为25-35℃，得到水浸液和水浸渣，其中含溴粗盐溴质量百分含量为5-25％；
    (2)酸化氧化：将步骤(1)得到的水浸液用36％浓盐酸进行酸化，然后加入氯酸钠并充分搅拌，期间利用浓盐酸维持体系pH在0-1，得到酸化氧化后液和酸化氧化尾气；浓盐酸加入量为0.4-0.8L/L水浸液，氯酸钠加入量为10-20g/L水浸液，反应时间为30-60min，反应温度为25-35℃
    (3)多级萃取：将步骤(2)得到的酸化氧化后液采用四氯化碳进行多级萃取，其中四氯化碳与酸化氧化后液的体积比为1.5:1-2.5:1，萃取级数为2-5，萃取时间为2-8min，萃取温度为25-35℃，得到萃取液和萃余液，萃余液经蒸发结晶得到粗溴化钠进行集中处理；
    (4)协同反萃：向步骤(3)得到的萃取液中加入反萃剂并不断搅拌，当pH为6-7时，停止加入反萃剂，反应温度为25-35℃下再继续反应5-10min，得到有机相和反萃液；
    (5)蒸发结晶：将步骤(4)得到的反萃液进行蒸发结晶，得到溴化钠，其中蒸发结晶温度为110℃-140℃。
  2. 如权利要求1所述的一种从含溴粗盐中回收高纯溴化钠的方法，其特征在于，步骤(4)中反萃剂由碳酸钠和尿素混合水溶液组成，碳酸钠与尿素的摩尔比为3:1，反萃剂浓度为20-40g/L。
  3. 如权利要求1所述的一种从含溴粗盐中回收高纯溴化钠的方法，其特征在于，酸化氧化尾气经碱液吸收后返回酸化氧化工序。
  4. 如权利要求1所述的一种从含溴粗盐中回收高纯溴化钠的方法，其特征在于，有机相返步骤(3)多级萃取工序。
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