CN104109078A - 一种安乃近生产中乙醇回收的方法 - Google Patents
一种安乃近生产中乙醇回收的方法 Download PDFInfo
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- CN104109078A CN104109078A CN201410290166.1A CN201410290166A CN104109078A CN 104109078 A CN104109078 A CN 104109078A CN 201410290166 A CN201410290166 A CN 201410290166A CN 104109078 A CN104109078 A CN 104109078A
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- ethanol
- sulpyrine
- production
- mother liquor
- reclaims
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N ethanol Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 229
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- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicium dioxide Chemical compound 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O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- 238000009834 vaporization Methods 0.000 claims description 5
- 235000019422 polyvinyl alcohol Nutrition 0.000 claims description 4
- 229920002451 polyvinyl alcohol Polymers 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 30
- 238000011084 recovery Methods 0.000 abstract description 17
- 239000012530 fluid Substances 0.000 abstract description 11
- 230000000149 penetrating Effects 0.000 abstract description 11
- 238000005406 washing Methods 0.000 abstract description 8
- 239000002699 waste material Substances 0.000 abstract description 6
- 238000005373 pervaporation Methods 0.000 abstract description 5
- 239000002904 solvent Substances 0.000 abstract description 3
- 239000012141 concentrate Substances 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 17
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- 238000000895 extractive distillation Methods 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 230000001754 anti-pyretic Effects 0.000 description 2
- 239000002221 antipyretic Substances 0.000 description 2
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- 238000005265 energy consumption Methods 0.000 description 2
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- 238000004064 recycling Methods 0.000 description 1
- LIVNPJMFVYWSIS-UHFFFAOYSA-N silicon monoxide Inorganic materials 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[Si-]#[O+] LIVNPJMFVYWSIS-UHFFFAOYSA-N 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
本发明涉及一种安乃近生产中乙醇回收的方法,步骤如下:以安乃近缩合反应工段获得的母液先过滤、结晶,再蒸馏浓缩;浓缩液经乙醇洗涤离心后返回缩合反应釜,废乙醇送入蒸馏塔,塔顶产物经冷凝后进入中间罐;将蒸馏回收的乙醇溶液蒸发后进入渗透汽化膜分离机组脱水,渗透汽化膜分离机组料液侧获得高纯度乙醇,作为溶剂返回安乃近缩合反应工段循环使用;膜分离机组渗透侧与真空系统相连接,料液侧溶液中的水以及少量乙醇以蒸汽形式透过渗透汽化膜,渗透液冷凝后进一步返回蒸馏塔。本发明回收过程中除水外无其他废弃物排放,回收率高,工艺过程简单,能量利用率高,无第三组分加入。
Description
技术领域
[0002] 本发明涉及一种安乃近生产中乙醇回收的方法,尤其涉及一种渗透汽化法回收安 乃近生产中乙醇的方法,属渗透汽化膜应用领域。
[0003]
背景技术
[0004] 安乃近为吡唑酮类解热镇痛药,具有较显著的解热、镇痛及消炎抗风湿作用,广泛 用于发热、急性关节炎、头痛、风湿痛、神经痛、痛经、牙痛及肌肉痛等症的治疗。
[0005] 在安乃近缩合反应工段中先将原料4-甲胺基安替比林溶解在乙醇中,再加入焦 亚硫酸钠、碳酸钠、活性炭和甲醛,缩合反应后料液进入结晶罐结晶得到安乃近成品,母液 经初蒸、乙醇洗涤、离心后固体返回缩合反应釜。上述过程中乙醇与水及其他微量组分形成 溶液,如果不进行乙醇回收,将无法循环使用,直接卖掉造成成本升高,如直接排放造成乙 醇损失,同时污染环境。为了使乙醇循环利用,必须将水除去,要求回用乙醇的水含量小于 千分之五以下。
[0006] 目前,安乃近生产中乙醇回收方法多采用加盐萃取精馏,一般以乙二醇作为萃取 齐U,加盐萃取精馏为双塔工艺,蒸汽消耗量大,设备占地面积大,环境污染严重,且产品易引 入第三组分,导致产品纯度低,第三组分用量大、回收成本高。
[0007]
发明内容
[0008] 本发明的目的在于提出一种安乃近生产中乙醇回收的方法。该方法具有工艺过程 简单,设备占地面积小,安全系数高,能耗低,乙醇回收率高,清洁无污染的特点。
[0009] 技术方案: 一种安乃近生产中乙醇回收的方法,包括如下步骤: 第1步、将安乃近缩合反应工段获得的反应料液进行过滤、结晶,得到乙醇母液,将乙 醇母液进行蒸馏浓缩,得到第一浓缩液和第一馏出液; 第2步、将第1步得到的第一浓缩液用乙醇进行洗涤、离心,得到第二浓缩液和洗涤液, 洗涤液再经过蒸馏得到的第二馏出液; 第3步、将第1步所得的第一馏出液和第2步所得的第二馏出液作为进料送入渗透汽 化装置进行分离,渗透侧得到水,料液侧得到回收乙醇。
[0010] 优选地,所述的第1步中经过过滤之后的乙醇母液中的含水量(质量百分比)是在 2〜20%。
[0011] 优选地,所述的第1步中的蒸馏浓缩中,将料液体积浓缩至159Γ30% ;最优是20%。
[0012] 作为优选,按重量计,第2步的洗涤过程中,乙醇的用量是第一浓缩液和重量的 0. l~〇. 3倍,更优是0.2倍。
[0013] 作为改进,在第3步中,对进料做渗透汽化分离时,先将进料用蒸发器加热之后, 再将蒸发器蒸出的含水乙醇送入渗透汽化分离。作为优选,含水乙醇的温度是5(T150°C。 作为改进,所述的进料送入蒸发器之前,可以通过与渗透汽化分离器料液侧的乙醇蒸汽进 行换热,使进料温度升高至5(Tl00°C。
[0014] 作为优选,在第3步中,渗透汽化膜的料液侧的表压为0〜0. 5MPa ;渗透侧与真空 系统相连,绝压10(T3000Pa。
[0015] 所述的渗透汽化膜分离器采用的膜为优先透水膜,可以为分子筛膜、无定形二氧 化硅膜、PVA膜,最优是分子筛膜。渗透汽化膜分离机组是由1~100个渗透汽化膜分离器串 联、并联或混联连接,以达到不同的处理要求和生产能力。
[0016] 作为改进,第3步中汽化冷凝后的渗透液返回蒸馏塔,馏出含一定水量的乙醇,再 返回至第1步中的乙醇母液。
[0017] 作为改进,在第1步中得到乙醇母液后,在乙醇母液中加入双氧水,所述的双氧水 的体积是乙醇母液的5〜10%,所述的双氧水的浓度是10〜20 wt%。
[0018] 有益效果 与加盐萃取精馏法回收安乃近生产中乙醇相比,本发明的方法具有如下特点: 1. 本发明采用渗透汽化膜分离机组脱水,不受共沸限制,工艺过程简单; 2. 本发明渗透汽化膜分离机组自动化程度高,操作简便,设备占地面积少; 3. 本方法采用先蒸馏再渗透汽化的方式,不引入第三组分,既节约了试剂消耗,又保证 产品纯度; 4. 本发明将渗透液返至蒸馏塔回收处理,减少了乙醇的排放量,增加了乙醇的回收 率; 5. 本发明利用产品热量对进入蒸发器前的含水乙醇料液进行预热,提高了系统内能量 利用率,进一步降低了生产能耗; 6. 本发明提供的乙醇回收方法,乙醇中的水含量小,可以降低至0.05%,能耗降低 30〜60%。
[0019]
附图说明
[0020] 图1是安乃近生产中乙醇回收工艺流程图; 其中1是缩合反应釜,2是压滤机,3是结晶罐,4是蒸馏釜,5是离心机,6是蒸馏塔,7 是中间罐,8是预热器,9是蒸发器,10是渗透汽化分离机组,11是渗透液冷凝器,12是真空 泵,13是产品冷凝器,14是产品罐。
[0021]
具体实施方式
[0022] 本发明的目的是针对安乃近生产中缩合工艺产生的乙醇母液进行乙醇脱水回收, 在安乃近的缩合工艺中,采用的溶剂是乙醇,在结晶、离心分离过程中,也采用的乙醇作为 溶剂,因此,在尚心后广生的母液中含有大量的未反应完全的原料(例如:焦亚硫fe纳、碳fe 钠、活性炭和甲醛)、副产物、杂质、水。利用蒸馏-渗透汽化工艺,可以将母液中的乙醇进行 脱水分尚。
[0023] 本发明采用的技术方案是:首先,要将安乃近缩合反应工段获得的反应料液进行 结晶、过滤,得到乙醇母液,将乙醇母液进行蒸馏浓缩,得到第一浓缩液和第一馏出液;得到 的第一浓缩液用乙醇进行洗涤、离心,得到第二浓缩液和洗涤液,洗涤液再经过蒸馏得到第 二馏出液;将第一馏出液和第二馏出液作为进料送入渗透汽化装置进行分离,渗透侧得到 水,料液侧得到回收乙醇。
[0024] 在该步骤中,对乙醇母液进行蒸馏浓缩的最主要的目的是对其进行初步提纯,可 以使未反应完全的原料、副产物等重组分和一部分水留在蒸馏釜底,这样一方面可以避免 重组分进入至渗透汽化分离器的料液侧,影响到最终的回收乙醇的纯度,还可以脱除一部 分水,减轻渗透汽化膜的面积,使其处理量、产品含水量得到提高。一般来说,乙醇母液中的 含水量是在2~20wt. %左右,更适合于该工艺的是在15wt%左右。另外,在这个蒸馏的过程 中,如果浓缩率不高的话,会导致在一部分乙醇不能完全被蒸出,影响到工艺的收率;但是, 如果浓缩率过高时,会导致蒸馏釜的釜底料液过浓,一些重组分、杂质或者溶解于乙醇中的 甲醛等也会随着蒸馏的过程进入至蒸汽中,最终会影响到回收乙醇的纯度。最好是将料液 体积浓缩至15~30% ;在最优的实施例中为20%。
[0025] 为了使上述的过程中得到的回收乙醇产品纯度更高、渗透汽化膜的性能能够得到 提高,可以通过将蒸馏釜底的第一浓缩液用乙醇进行洗涤,由于第一浓缩液中的溶解物的 浓度提高,在将其降温后,其溶解度会发生下降,会产生固体物的析出,用乙醇对其进行洗 涤,再将洗涤液进行蒸馏后得到的第二馏出液进行渗透汽化分离,一方面可以使固体物进 一步地被提纯,另一方面,洗涤液与第一馏出液混合后,可以降低混合液中重组分、杂质的 浓度,防止釜底液过度蒸馏后产生的副产物、杂质进入渗透汽化料液侧的问题,可以提高产 品纯度、渗透汽化膜的性能。洗涤过程中的乙醇的用量是第一浓缩液重量的〇. 1~〇. 3倍,在 一个最优实施例中是0.2倍。
[0026] 根据本发明的另一个改进的实施方式,对于从蒸馏釜中蒸馏产生的馏出物(第一 馏出液和/或第二馏出液),最好是将其用蒸发器进行加热之后,以蒸汽形式进入至渗透汽 化分离器,这主要是可以提高渗透汽化膜的分离效率,蒸汽的温度优选是5(T150°C,为了更 好地利用余热,可以在将其送入蒸发器之前,先与渗透汽化分离器料液侧的乙醇蒸汽进行 预热,升温至5(n〇〇°c。
[0027] 根据本发明的一个优选的实施方式,采用的渗透汽化膜是分子筛膜,相对于其它 类似的膜材料,例如:无定形二氧化硅膜、PVA膜,分子筛膜分离后得到的回收乙醇的纯度 高而且分离过程中的膜通量较大。
[0028] 根据本发明的一个改进的实施方式,在第1步中得到乙醇母液之后,最好是在其 中加入一些双氧水,双氧水的体积最好是乙醇母液的5〜10%,其浓度优选是10〜20 wt. % ; 这主要是由于双氧水的加入可以分解掉母液中的一些例如甲醛这样的杂质,避免了这些杂 质对渗透汽化过程产生影响,其可以提高渗透汽化膜的性能,回收乙醇的纯度也是可以得 到提高。在一个最优的实施例中,双氧水的加入量是乙醇母液的8%,其浓度是15 wt %。
[0029] 实施例1 安乃近生产中乙醇回收的方法,采用的装置如图1所示,操作过程包括下列步骤:将来 自安乃近缩合反应工段得到的母液,先进入压滤机2过滤,再进入结晶罐3结晶,上层母液 (含水量20wt%左右)送入蒸馏釜4浓缩,蒸馏乙醇收集于中间罐7,蒸馏过程中母液体积减 小至25%左右,得到第一浓缩液,再用其重量0. 3倍的乙醇洗涤后进入离心机5中离心,将 离心机得到了固体或胶状物返回缩合反应釜1,而洗涤液(废乙醇)送入蒸馏塔6,蒸馏乙醇 (第二馏出液)进入中间罐7,中间罐7中水含量为15wt%的乙醇溶液。将中间罐7中的料液 控制流量分别为l〇〇〇、775、325kg/h输送到预热器8,通过产品蒸汽对该料液预热至80°C, 然后进入蒸发器9中加热,料液被加热到11(TC以蒸汽形式进入到分别由12个分子筛膜、 Si02膜和PVA膜组件(每级膜组件面积为10m2)串联构成的渗透汽化膜分离机组10进行脱 水分离。料液侧压力为〇. 2MPa,渗透侧压力控制在1500Pa。料液水含量通过渗透汽化膜分 离机会明显地降低,得到回收乙醇,其流经预热器8对料液预热后再经产品冷凝器13冷凝 进入产品罐14。渗透侧得到的渗透液冷凝后,返回至蒸馏塔6处理。
[0030] 在采用不同的膜材料时,所得的回收乙醇、渗透液、通量等数据如表1所示。
[0031] 表 1
从表中可以看出,分子筛膜特别适合于该回收乙醇的脱水处理,所得的处理量、渗透通 量优于其它种类的膜材料,渗透液的水含量也优于其它的几种膜材料。
[0032] 实施例2 安乃近生产中乙醇回收的方法,采用的装置如图1所示,操作过程包括下列步骤:将来 自安乃近缩合反应工段得到的母液,先进入压滤机2过滤,再进入结晶罐3结晶,上层母液 (含水量20wt%左右)送入蒸馏釜4浓缩,蒸馏乙醇收集于中间罐7,蒸馏过程中第一浓缩液 浓缩液体积分别减小至1〇%、15%、20%、25%、30%、35%左右(质量百分比),再用其重量0. 1 倍的乙醇洗涤后进入离心机5中离心,将离心机得到了固体或胶状物返回缩合反应釜1,而 洗涤液(废乙醇)送入蒸馏塔6,蒸馏乙醇(第二馏出液)进入中间罐7,中间罐7中水含量为 12wt%的乙醇溶液。将中间罐7中的流量控制为1500kg/h输送到预热器8,通过产品蒸汽 对该料液预热至70°C,然后进入蒸发器9中加热,料液被加热到125°C以蒸汽形式进入到由 14个NaA分子筛渗透汽化膜组件(每级膜组件面积为10m 2)串联构成的渗透汽化膜分离机 组10进行脱水分离。料液侧压力为〇.4MPa,渗透侧压力控制在800Pa。料液水含量通过渗 透汽化膜分离机会明显地降低,得到回收乙醇,其流经预热器8对料液预热后再经产品冷 凝器13冷凝进入产品罐14。渗透侧得到的渗透液冷凝后,返回至蒸馏塔6处理。
[0033] 在采用不同的浓缩百分比时,所得的回收乙醇、渗透液、通量等数据如表2所示。
[0034] 表 2
从表中可以看出,将蒸馏釜的浓缩比控制在合适的范围时,可以有效地使母液中杂质 等进入至蒸汽中,可以提高水通量和回收乙醇的纯度。
[0035] 实施例3 安乃近生产中乙醇回收的方法,采用的装置如图1所示,操作过程包括下列步骤:将来 自安乃近缩合反应工段得到的母液,先进入压滤机2过滤,再进入结晶罐3结晶,结晶之后 可以通过离心等方式将固体物进行固液分离去除,上层母液(含水量15wt%左右)送入蒸馏 釜4浓缩,蒸馏乙醇收集于中间罐7,蒸馏过程中离心母液体积分别减小至20%左右(质量 百分比),得到第一浓缩液,再用其重量0. 2倍的乙醇洗涤后进入离心机5中离心,将离心机 得到了固体或胶状物返回缩合反应釜1,而洗涤液(废乙醇)送入蒸馏塔6,蒸馏乙醇(第二馏 出液)进入中间罐7,中间罐7中水含量为llwt%的乙醇溶液。将中间罐7中的乙醇控制流 量为1000kg/h输送到预热器8,通过产品蒸汽对该料液预热至85°C,然后进入蒸发器9中 加热,料液被加热到1 l〇°C以蒸汽形式进入到由15个NaA分子筛渗透汽化膜组件(每级膜组 件面积为l〇m2)串联构成的渗透汽化膜分离机组10进行脱水分离。料液侧压力为0. 2MPa, 渗透侧压力控制在l〇〇〇Pa。料液水含量通过渗透汽化膜分离机会明显地降低,得到回收乙 醇的纯度大约为98wt%,其通量约为1. 30 kg/m2 *h,含水量约为0. 2wt%,其流经预热器8对 料液预热后再经产品冷凝器13冷凝进入产品罐14。渗透侧得到的渗透液冷凝后,水含量为 93. 7%,返回至蒸馏塔6处理。
[0036] 实施例4 安乃近生产中乙醇回收的方法,采用的装置如图1所示,操作过程包括下列步骤:将 来自安乃近缩合反应工段得到的母液,先进入压滤机2过滤,再进入结晶罐3结晶,上层 母液(含水量15wt%左右)中加入双氧水,双氧水的体积是乙醇母液的6%,双氧水的浓度是 15wt%,搅拌均匀,保持2h后,送入蒸馏釜4浓缩,蒸馏乙醇收集于中间罐7,蒸馏过程中离 心母液体积分别减小至20%左右(质量百分比),得到第一浓缩液,再用其重量0. 2倍的乙 醇洗涤后进入离心机5中离心,将离心机得到了固体或胶状物返回缩合反应釜1,而洗涤液 (废乙醇)送入蒸馏塔6,蒸馏乙醇(第二馏出液)进入中间罐7,中间罐7中水含量为llwt% 的乙醇溶液。将中间罐7中的乙醇控制流量为775kg/h输送到预热器8,通过产品蒸汽对 该料液预热至85°C,然后进入蒸发器9中加热,料液被加热到11(TC以蒸汽形式进入到由 12个NaA分子筛渗透汽化膜组件(每级膜组件面积为10m 2)串联构成的渗透汽化膜分离机 组10进行脱水分离。料液侧压力为0. 2MPa,渗透侧压力控制在1000Pa。料液水含量通过 渗透汽化膜分离机会明显地降低,得到回收乙醇的纯度大约为99wt%,其通量约为1. 36 kg/ m2 *h,含水量约为0. 15wt. %,其流经预热器8对料液预热后再经产品冷凝器13冷凝进入产 品罐14。渗透侧得到的渗透液冷凝后,水含量为92. 4%,返回至蒸馏塔6处理。通过实施例 3和实施例4可以看出,通过使用双氧水对乙醇母液处理之后,可以有效地降低其中杂质的 含量,有利于提高回收乙醇的纯度以及使膜通量得到提高。
Claims (9)
1. 一种安乃近生产中乙醇回收的方法,其特征在于,包括如下步骤: 第1步、将安乃近缩合反应工段获得的反应料液进行过滤、结晶,得到乙醇母液,将乙 醇母液进行蒸馏浓缩,得到第一浓缩液和第一馏出液; 第2步、将第1步得到的第一浓缩液用乙醇进行洗涤、离心,得到第二浓缩液和洗涤液, 洗涤液再经过蒸馏得到的第二馏出液; 第3步、将第1步所得的第一馏出液和第2步所得的第二馏出液作为进料送入渗透汽 化装置进行分离,渗透侧得到水,料液侧得到回收乙醇。
2. 根据权利要求1所述的安乃近生产中乙醇回收的方法,其特征在于:所述的第1步 中经过过滤之后的料液中的含水量是在2~20wt. %。
3. 根据权利要求1所述的安乃近生产中乙醇回收的方法,其特征在于:所述的第1步 中的蒸馏浓缩中,将料液体积浓缩至159Γ30%。
4. 根据权利要求3所述的安乃近生产中乙醇回收的方法,其特征在于:按重量计,乙醇 的用量是第一浓缩液重量的〇. 1~〇. 3倍。
5. 根据权利要求1所述的安乃近生产中乙醇回收的方法,其特征在于:在第2步中,对 进料做渗透汽化分离时,进料先用蒸发器加热之后,再送入渗透汽化膜组件进行分离。
6. 根据权利要求5所述的安乃近生产中乙醇回收的方法,其特征在于:加热的温度是 5(Γ150Ό。
7. 根据权利要求5或6所述的安乃近生产中乙醇回收的方法,其特征在于:所述的 进料送入蒸发器之前,可以通过与回收后的成品乙醇蒸汽进行换热,使进料温度升高至 50〜100。。。
8. 根据权利要求1所述的安乃近生产中乙醇回收的方法,其特征在于:在第3步中,渗 透汽化膜的料液侧的表压为0〜0. 5MPa ;渗透侧与真空系统相连,绝压10(T3000Pa ;所述 的渗透汽化膜分离器采用的膜为优先透水膜,可以为分子筛膜、无定形二氧化硅膜、PVA膜; 最优是分子筛膜。
9. 根据权利要求1所述的安乃近生产中乙醇回收的方法,其特征在于:在第1步中 得到乙醇母液后,在乙醇母液中加入双氧水,所述的双氧水的体积是乙醇母液体积的5〜 10%,所述的双氧水的浓度是10〜20 wt%。
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CN105218317B (zh) * | 2015-11-03 | 2017-08-25 | 江苏九天高科技股份有限公司 | 一种六硝基联苄生产中乙醇回收的方法及装置 |
CN108905259A (zh) * | 2018-07-18 | 2018-11-30 | 芜湖青悠静谧环保科技有限公司 | 一种新型制备燃料乙醇的工艺装置 |
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