WO2022155777A1 - 用于甘油精制生产工艺的余热回收利用装置 - Google Patents

用于甘油精制生产工艺的余热回收利用装置 Download PDF

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WO2022155777A1
WO2022155777A1 PCT/CN2021/072658 CN2021072658W WO2022155777A1 WO 2022155777 A1 WO2022155777 A1 WO 2022155777A1 CN 2021072658 W CN2021072658 W CN 2021072658W WO 2022155777 A1 WO2022155777 A1 WO 2022155777A1
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condenser
steam drum
steam
pipeline
waste heat
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PCT/CN2021/072658
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English (en)
French (fr)
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滕磊
张新合
张纪万
金博文
周旭
张小乐
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汇智工程科技股份有限公司
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Priority to PCT/CN2021/072658 priority Critical patent/WO2022155777A1/zh
Publication of WO2022155777A1 publication Critical patent/WO2022155777A1/zh

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    • 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
    • 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
    • C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/18—Polyhydroxylic acyclic alcohols
    • C07C31/22—Trihydroxylic alcohols, e.g. glycerol
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/16—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being hot liquid or hot vapour, e.g. waste liquid, waste vapour

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  • the invention relates to the technical field of glycerol refining, in particular to a waste heat recovery and utilization device used in a glycerol refining production process.
  • the crude glycerol is classified according to the origin and source: South American crop biological crude glycerin, Southeast Asian palm crude glycerin, crude glycerol produced by European chemical industry and domestic saponified crude glycerin, etc. Therefore, the source and composition of crude glycerin are complicated, so it is necessary to carry out the crude glycerol. Refined to obtain refined glycerin.
  • the water phase in the shell side of the condenser will be vaporized by the high-temperature crude glycerin gas phase in the tube side, thereby producing low-pressure steam with a large amount of waste heat.
  • This part of the steam contains a lot of heat energy. Recycling can save a lot of energy.
  • the technical problem to be solved by the present invention is: overcoming the deficiencies of the prior art, providing a waste heat recovery and utilization device for the glycerin refining production process, and realizing the high temperature gas in the water phase in the shell side of the first condenser in the glycerin refining production process
  • the recovery and utilization of the waste heat steam generated by the chemical process makes full use of the thermal energy and greatly saves energy.
  • a waste heat recovery and utilization device used in a glycerin refining production process including a first condenser, the air inlet of the first condenser is connected to the air outlet of the distillation kettle through a pipeline, and the air outlet of the first condenser is connected to the second condenser through a pipeline.
  • the inlet of the first condenser and the second condenser are respectively connected with the temporary fraction collecting tank through pipes, and also includes a steam drum, and the outlet of the cooling medium shell side of the first condenser is connected with the steam drum through pipes.
  • the air inlet of the steam drum is connected with the steam distribution table through the pipeline; the liquid inlet of the steam drum is connected with the water replenishment tank of the steam drum through the pipeline, and the liquid outlet of the steam drum is connected with the cooling medium of the first condenser through the pipeline.
  • Shell side inlet connection is connected.
  • a liquid level sensor is provided on the steam drum
  • a pump is provided on the pipeline between the steam drum and the water replenishing tank of the steam drum, and the liquid level sensor and the pump are respectively electrically connected to the controller.
  • a separator is provided in the temporary fraction collection tank.
  • the present invention has the following beneficial effects:
  • the invention realizes the recovery and utilization of the waste heat steam generated by the high-temperature gasification of the water phase in the shell side of the first condenser in the glycerin refining production process, fully utilizes the thermal energy, and greatly saves the energy.
  • Figure 1 is a schematic structural diagram of the present invention.
  • 1-first condenser 2-still still, 3-second condenser, 4-fraction temporary collection tank, 5-steam drum, 6-steam distribution table, 7-steam drum replenishment tank, 8-liquid Position sensor, 9-pump, 10-spacer.
  • the present embodiment provides a waste heat recovery and utilization device for glycerin refining production process, including a first condenser 1, the air inlet of the first condenser 1 is connected to the air outlet of the distillation still 2 through a pipeline Connection, the air outlet of the first condenser 1 is connected with the air inlet of the second condenser 3 through the pipeline, the fraction outlets of the first condenser 1 and the second condenser 3 are respectively connected with the temporary fraction collection tank 4 through the pipeline, and the fraction
  • the temporary collection tank 4 is provided with a partition 10 to separate the condensed fractions of the first condenser 1 and the second condenser 3; it also includes a steam drum 5, and the outlet of the cooling medium shell side of the first condenser 1 is separated.
  • the air port is connected with the air inlet of the steam drum 5 through the pipeline, and the air outlet of the steam drum 5 is connected with the steam distribution platform 6 through the pipeline; the liquid inlet of the steam drum 5 is connected with the steam drum replenishment tank 7 through the pipeline, and the outlet of the steam drum 5
  • the liquid port is connected to the liquid inlet of the cooling medium shell side of the first condenser 1 through a pipeline.
  • the crude glycerol is first preheated, pumped into the crude glycerin pretreatment tank, heated and air-mixed under the action of acid to carry out hydrolysis reaction to obtain fatty acid, and then the preliminary separation of fatty acid and crude glycerol is carried out. .
  • the crude glycerol after separation of fatty acids is then pumped into the alkali adjusting tank, and the remaining trace fatty acids in the crude glycerol are neutralized to generate fatty acid sodium salts, which are converted into high-boiling components.
  • the crude glycerin treated with alkali adjustment is pumped to the heat exchanger for heat exchange, and the crude glycerol after heat exchange is pumped to the flash tank for vacuum flash evaporation to remove moisture.
  • the crude glycerin after flash dehydration is pumped to the heat exchanger for heat exchange, and then pumped to the distillation still 2 for distillation.
  • the first condenser 1 condenses and recovers the fraction at 140-200°C, after the high-temperature crude glycerin gas phase in the first condenser 1 tube side exchanges heat with the shell-side hot water, part of the hot water is vaporized at high temperature into steam, and this part of the steam Contains thermal energy and should be recycled.
  • a steam drum 5 is added on one side of the shell side of the cooling medium of the first condenser 1, and the low-pressure waste heat steam generated by the high temperature gasification of the water phase in the shell side of the cooling medium of the first condenser 1 first enters through the pipeline In the steam drum 5, and finally into the steam distribution table 6, it can be used for the preheating of crude glycerin at room temperature, the temperature adjustment of the crude glycerin pretreatment tank, the temperature adjustment of the decolorization kettle, and the flash dehydration and other devices.
  • the liquid level of the shell side will drop.
  • water is supplied to the steam drum 5 through the steam drum water replenishment tank 7, and the water in the steam drum 5 is then supplemented to the shell side through the pipeline connected to the shell side of the first condenser 1, so that The continuous cycle is carried out to condense the high boiling point glycerin in the gas phase tube side of the first condenser 1, and the low boiling point gas phase such as uncondensed water vapor enters the subsequent stage condenser.
  • the device of this embodiment realizes the recovery and utilization of the waste heat steam generated by the high temperature gasification of the water phase in the shell side of the first condenser 1 in the glycerol refining production process, fully utilizes the thermal energy, and greatly saves energy.
  • the steam drum 5 is provided with a liquid level sensor 8, and the pipeline between the steam drum 5 and the steam drum replenishment tank 7 is provided with a pump 9, and the liquid level sensor 8 and the pump 9 are respectively connected with the control electrical connection.
  • the controller controls to start the pump 9 to automatically replenish water to the steam drum 5; when the liquid level of the steam drum 5 is high, the controller controls to turn off the pump 9 and stops supplying water to the steam drum 5 , so as to realize the automatic replenishment of hot water in the steam drum 5 and the first condenser 1 .

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

一种用于甘油精制生产工艺的余热回收利用装置，包括第一冷凝器（1），第一冷凝器（1）的进气口通过管道与蒸馏釜（2）的出气口连接，第一冷凝器（1）的出气口通过管道与第二冷凝器（3）的进气口连接，第一冷凝器（1）和第二冷凝器（3）的馏分出口分别通过管道与馏分暂收罐（4）连接，还包括汽包（5），第一冷凝器（1）的冷却介质壳程的出气口通过管道与汽包（5）的进气口连接，汽包（5）的出气口通过管道与蒸汽分配台（6）连接；汽包（5）的进液口通过管道与汽包补水罐（7）连接，汽包（5）的出液口通过管道与第一冷凝器（1）的冷却介质壳程的进液口连接，实现了甘油精制中第一冷凝器（1）壳程中的水相高温气化产生的余热蒸汽的回收利用，充分利用了热能，大大节约了能源。

Description

用于甘油精制生产工艺的余热回收利用装置 技术领域
本发明涉及甘油精制技术领域，具体涉及一种用于甘油精制生产工艺的余热回收利用装置。
背景技术
得益于生物化工技术快速的发展，各国积极发展生物柴油工业，随之水解产生大量副产粗甘油。据资料显示：每生产10吨生物柴油，就会产生1吨的粗甘油副产品。将粗甘油按产地和来源分类分别为：南美农作物生物粗甘油、东南亚棕榈粗甘油、欧洲化工生产的粗甘油及国内皂化粗甘油等，因此粗甘油来源和成分较复杂，因此需要对粗甘油进行精制得到精甘油。
而在粗甘油的蒸馏冷凝工序中，冷凝器壳程中的水相会被管程中的高温粗甘油气相气化，从而产生带有大量余热的低压蒸汽，这部分蒸汽含有大量热能，若能够回收利用，则可以节约大量能源。
发明内容
本发明要解决的技术问题是：克服现有技术的不足，提供一种用于甘油精制生产工艺的余热回收利用装置，实现了甘油精制生产工艺中第一冷凝器壳程中的水相高温气化产生的余热蒸汽的回收利用，充分利用了热能，大大节约了能源。
本发明的技术方案为：
用于甘油精制生产工艺的余热回收利用装置，包括第一冷凝器，第一冷凝器的进气口通过管道与蒸馏釜的出气口连接，第一冷凝器的出气口通过管道与第二冷凝器的进气口连接，第一冷凝器和第二冷凝器的馏分出口分别通过管道与馏分暂收罐连接，还包括汽包，第一冷凝器的冷却介质壳程的出气口通过管道与汽包的进气口连接，汽包的出气口通过管道与蒸汽分配台连接；汽包的进液口通过管道与汽包补水罐连接，汽包的出液口通过管道与第一冷凝器的冷却介质壳程的进液口连接。
优选地，所述汽包上设置有液位传感器，汽包与汽包补水罐之间的管道上设置有泵，液位传感器和泵分别与控制器电连接。
优选地，所述馏分暂收罐内设置有隔板。
本发明与现有技术相比，具有以下有益效果：
本发明实现了甘油精制生产工艺中第一冷凝器壳程中的水相高温气化产生的余热蒸汽的回收利用，充分利用了热能，大大节约了能源。
附图说明
图1是本发明的结构示意图。
图中，1-第一冷凝器、2-蒸馏釜、3-第二冷凝器、4-馏分暂收罐、5-汽包、6-蒸汽分配台、7-汽包补水罐、8-液位传感器、9-泵、10-隔板。
具体实施方式
实施例1
如图1所示，本实施例提供了一种用于甘油精制生产工艺的余热回收利用装置，包括第一冷凝器1，第一冷凝器1的进气口通过管道与蒸馏釜2的出气口连接，第一冷凝器1的出气口通过管道与第二冷凝器3的进气口连接，第一冷凝器1和第二冷凝器3的馏分出口分别通过管道与馏分暂收罐4连接，馏分暂收罐4内设置有隔板10，将第一冷凝器1和第二冷凝器3的冷凝出的馏分分隔开；还包括汽包5，第一冷凝器1的冷却介质壳程的出气口通过管道与汽包5的进气口连接，汽包5的出气口通过管道与蒸汽分配台6连接；汽包5的进液口通过管道与汽包补水罐7连接，汽包5的出液口通过管道与第一冷凝器1的冷却介质壳程的进液口连接。
在对粗甘油进行预处理时，首先将粗甘油预热，泵送至粗甘油预处理槽中，在酸的作用下加热气混进行水解反应得到脂肪酸，随后再进行脂肪酸和粗甘油的初步分离。分离脂肪酸后的粗甘油再泵入调碱罐中，将粗甘油中剩余的微量脂肪酸中和反应生成脂肪酸钠盐，转化为高沸点的组分。经调碱处理后的粗甘油泵送至换热器中进行换热，换热后的粗甘油泵送至闪蒸釜内对其进行真空闪蒸脱出水分。闪蒸脱水后的粗甘油泵送至换热器中进行换热，随后泵送至蒸馏釜2进行蒸馏，从蒸馏釜2顶部蒸出的高温气相逐级进入后续的冷凝器中进行冷凝。
在第一冷凝器1冷凝回收140-200℃的馏分时，第一冷凝器1管程中的高温粗甘油气相与壳程热水换热后，部分热水高温汽化变为蒸汽，这部分蒸汽含有热能，应加以回收利用。因此本实施例在第一冷凝器1的冷却介质壳程一侧加设一只汽包5，第一冷凝器1冷却介质壳程中的水相高温气化产生的低压余热蒸汽先通过管道进入汽包5中，并最终进入到蒸汽分配台6中，可用于常温粗甘油的预热、粗甘油预处理槽的温度调节、脱色 釜的温度调节和闪蒸脱水等装置。
第一冷凝器1壳程中的部分热水汽化变为蒸汽后，会使壳程的液位下降。为了填补这部分缺失的热水，本实施例通过汽包补水罐7向汽包5补水，汽包5中的水再通过与第一冷凝器1壳程连通的管道补充到壳程中，如此连续循环进行，将第一冷凝器1气相管程中的高沸点甘油冷凝下来，未被冷凝的水汽等低沸点气相进入后级冷凝器。
本实施例的装置实现了甘油精制生产工艺中第一冷凝器1壳程中的水相高温气化产生的余热蒸汽的回收利用，充分利用了热能，大大节约了能源。
实施例2
在实施例1的基础上，所述汽包5上设置有液位传感器8，汽包5与汽包补水罐7之间的管道上设置有泵9，液位传感器8和泵9分别与控制器电连接。当汽包5的液位低时，控制器控制启动泵9，向汽包5中自动补水；当汽包5的液位高时，则控制器控制关闭泵9，停止向汽包5中补水，从而实现了汽包5和第一冷凝器1中热水的自动补充。
尽管通过参考附图并结合优选实施例的方式对本发明进行了详细描述，但本发明并不限于此。在不脱离本发明的精神和实质的前提下，本领域普通技术人员可以对本发明的实施例进行各种等效的修改或替换，而这些修改或替换都应在本发明的涵盖范围内/任何熟悉本技术领域的技术人员在本发明揭露的技术范围内，可轻易想到变化或替换，都应涵盖在本发明的保护范围之内。因此，本发明的保护范围应所述以权利要求的保护范围为准。

Claims (3)

  1. 用于甘油精制生产工艺的余热回收利用装置，包括第一冷凝器(1)，第一冷凝器(1)的进气口通过管道与蒸馏釜(2)的出气口连接，第一冷凝器(1)的出气口通过管道与第二冷凝器(3)的进气口连接，第一冷凝器(1)和第二冷凝器(3)的馏分出口分别通过管道与馏分暂收罐(4)连接，其特征在于：还包括汽包(5)，第一冷凝器(1)的冷却介质壳程的出气口通过管道与汽包(5)的进气口连接，汽包(5)的出气口通过管道与蒸汽分配台(6)连接；汽包(5)的进液口通过管道与汽包补水罐(7)连接，汽包(5)的出液口通过管道与第一冷凝器(1)的冷却介质壳程的进液口连接。
  2. 如权利要求1所述的用于甘油精制生产工艺的余热回收利用装置，其特征在于：所述汽包(5)上设置有液位传感器(8)，汽包(5)与汽包补水罐(7)之间的管道上设置有泵(9)，液位传感器(8)和泵(9)分别与控制器电连接。
  3. 如权利要求1所述的用于甘油精制生产工艺的余热回收利用装置，其特征在于：所述馏分暂收罐(4)内设置有隔板(10)。
PCT/CN2021/072658 2021-01-19 2021-01-19 用于甘油精制生产工艺的余热回收利用装置 WO2022155777A1 (zh)

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Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3582472A (en) * 1967-12-21 1971-06-01 Buss Ag Plural stage vacuum distillation apparatus for continuous purification and concentration of glycerine
CN202199147U (zh) * 2011-08-18 2012-04-25 天津大学 带有蒸汽包压力控制的立式可副产蒸汽的冷凝器
KR20140107878A (ko) * 2013-02-28 2014-09-05 (주)신흥유업 글리세린 정제장치
CN107266320A (zh) * 2017-06-26 2017-10-20 安徽省化工设计院 一种硝基氯苯精馏分离中综合能耗回收的工艺方法
CN207600551U (zh) * 2017-12-25 2018-07-10 内蒙古大唐国际托克托发电有限责任公司 一种准确性高的锅炉汽包水位测量修正装置
CN108821946A (zh) * 2018-08-30 2018-11-16 江苏洁丽莱科技有限公司 甘油的连续化生产装置及方法
CN208829570U (zh) * 2018-08-30 2019-05-07 江苏洁丽莱科技有限公司 甘油的连续化生产装置
CN209655277U (zh) * 2019-03-18 2019-11-19 河南济源钢铁(集团)有限公司 一种锅炉汽包补水装置
CN212179661U (zh) * 2020-02-10 2020-12-18 迈瑞尔实验设备（上海）有限公司 外循环汽包取热系统

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3582472A (en) * 1967-12-21 1971-06-01 Buss Ag Plural stage vacuum distillation apparatus for continuous purification and concentration of glycerine
CN202199147U (zh) * 2011-08-18 2012-04-25 天津大学 带有蒸汽包压力控制的立式可副产蒸汽的冷凝器
KR20140107878A (ko) * 2013-02-28 2014-09-05 (주)신흥유업 글리세린 정제장치
CN107266320A (zh) * 2017-06-26 2017-10-20 安徽省化工设计院 一种硝基氯苯精馏分离中综合能耗回收的工艺方法
CN207600551U (zh) * 2017-12-25 2018-07-10 内蒙古大唐国际托克托发电有限责任公司 一种准确性高的锅炉汽包水位测量修正装置
CN108821946A (zh) * 2018-08-30 2018-11-16 江苏洁丽莱科技有限公司 甘油的连续化生产装置及方法
CN208829570U (zh) * 2018-08-30 2019-05-07 江苏洁丽莱科技有限公司 甘油的连续化生产装置
CN209655277U (zh) * 2019-03-18 2019-11-19 河南济源钢铁(集团)有限公司 一种锅炉汽包补水装置
CN212179661U (zh) * 2020-02-10 2020-12-18 迈瑞尔实验设备（上海）有限公司 外循环汽包取热系统

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