WO2014023137A1 - 一种压缩式热泵精馏装置及工艺 - Google Patents

一种压缩式热泵精馏装置及工艺 Download PDF

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Publication number
WO2014023137A1
WO2014023137A1 PCT/CN2013/077862 CN2013077862W WO2014023137A1 WO 2014023137 A1 WO2014023137 A1 WO 2014023137A1 CN 2013077862 W CN2013077862 W CN 2013077862W WO 2014023137 A1 WO2014023137 A1 WO 2014023137A1
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Prior art keywords
feed
rectification
port
column
heat pump
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PCT/CN2013/077862
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English (en)
French (fr)
Inventor
许松伟
于星
陆庆权
沈贵文
张�杰
崔磊
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南通醋酸纤维有限公司
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Publication of WO2014023137A1 publication Critical patent/WO2014023137A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/007—Energy recuperation; Heat pumps
    • 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
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency

Definitions

  • the invention belongs to the field of chemical separation process and energy-saving technology, and relates to a compression heat pump rectification device and a process. Background technique
  • the rectification process of solvent purification and separation is often involved.
  • the overhead vapor is usually directly condensed, part of the condensate is refluxed as a rectification column, and part is taken as a product. This process not only increases the cooling cycle water consumption, but also loses the condensation of the overhead steam.
  • Latent heat Compressed heat pump rectification processes such as external working type, tower kettle flashing or overhead vapor direct compression can be used to recover latent steam condensation overhead, such as propane-propylene separation and triphenyl separation.
  • Heat pump technology is a new energy technology that has received worldwide attention in recent years.
  • a heat pump is a device that transfers thermal energy from a low temperature heat source to a high temperature heat source.
  • heat pump technology is gradually used in the field of chemical rectification.
  • Supranto S. et al. studied the use of two-stage vapor compression, and the use of heat pump distillation in the rectification unit for separating ethanol and water (Heat pump assisted distillation. IX: Acceptance trials on a system for separating ethanol and water, International Journal Of Energy Research, 1988, 12, p 413-422 Gaspillo P. et al.
  • Chinese patent 200810231613.0 introduces a diethyl carbonate heat pump rectification device and a process, and introduces the steam material at the top of the rectification column into a compressor to be used as a heat source for the refiller of the column.
  • Deng Renjie et al. studied the new process of butyl acetate heat pump distillation (Chemical Engineering, 2006, issue 6). In view of the high energy consumption of the conventional butyl acetate production process, it is proposed to apply heat pump distillation to the production of butyl acetate to develop acetic acid.
  • New process for butyl ester heat pump distillation The process also compresses the vapor at the top of the column and uses it for the heat source of the column reboiler.
  • the temperature difference between the column of the esterification column and the distillation column in the apparatus is 13 °C and 18 °C, respectively.
  • the heat pump technology is applied to the rectification process in the chemical industry.
  • the temperature difference of the top column of the distillation column is large (especially when it is greater than 30 ° C)
  • the compression ratio is very high, resulting in compression.
  • the power of the machine is improved, the energy saving effect is not obvious, and the energy utilization is insufficient.
  • Summary of the invention In order to solve the heat pump rectification process in the chemical industry, when the temperature difference of the top of the distillation column tower is large (especially when it is greater than 30 ° C), the compression ratio is very high, the energy saving effect is not obvious, and the energy utilization is insufficient; It is an object of the present invention to provide a compression heat pump rectification apparatus.
  • Another object of the present invention is to provide a compression heat pump rectification process.
  • the present invention provides a compression heat pump rectification apparatus comprising a feed evaporator, a feed steam compressor, a rectification column, an overhead condensing cooler, and a reflux tank, which are in turn connected by piping.
  • the feed evaporator is provided with a feed evaporator feed port, a feed evaporator discharge port, a feed evaporator heating medium feed port, and a feed evaporator heating medium discharge port, and a feed evaporator
  • the heating medium feed port is located at the side of the feed evaporator, and the feed evaporator heating medium discharge port is located at the other side corresponding to the feed evaporator heating medium feed port; the feed evaporator discharge port and the compression
  • the feed inlet of the machine is connected, the heating medium discharge port of the feed evaporator is connected with the inlet of the overhead condensing cooler, and the feed medium of the feed evaporator is connected with the steam outlet of the top of the distillation column.
  • the feed steam compressor is provided with a compressor feed port and a compressor discharge port, and the compressor feed port is connected with the feed evaporator discharge port, and the compressor discharge port is connected with the rectification column feed port. .
  • the rectification column is provided with a rectification column feed port, a rectification column overhead steam outlet, a rectification column tower cavage outlet and a reflux liquid feed port, and the rectification column feed port is located at the side of the rectification column In the middle side, the reflux feed port is located on the other side corresponding to the rectification column feed port, the rectification column overhead steam outlet is located at the top of the rectification column, and the rectification column bottom coke outlet is located at the bottom of the rectification column
  • the distillation column feed port is connected to the compressor discharge port, the distillation column top steam outlet is connected to the feed evaporator heating medium feed port, and the reflux liquid feed port is connected to the reflux liquid outlet.
  • the tower top condensing cooler is provided with a cooler inlet and a cooler outlet, and the cooler inlet is connected with the feed evaporator heating medium outlet, and the cooler outlet and the return tank are fed. Port connection.
  • the reflux tank is provided with a return tank inlet, a reflux outlet and a top product outlet, and the reflux tank inlet is connected to the cooler outlet, and the reflux outlet is connected to the reflux inlet.
  • the invention also provides a compression heat pump rectification process, the process comprising the following steps:
  • the organic mixed solution to be separated is added to the feed evaporator, and the feed evaporator is heated under reduced pressure with the top steam of the distillation column as a heat source to completely vaporize the feed, and the vaporized feed is fed.
  • the steam compressor is compressed to increase the feed pressure, it enters the rectification column; after the rectification of the rectification column is completed, the liquid in the rectification column reaches the production standard and is directly produced, and the steam at the top of the column is passed to the feed evaporator as
  • the heat source performs heat exchange, and the overhead steam and part of the condensate after the heat exchange enters the overhead condensing cooler to be condensed into a liquid into the reflux tank; the condensate portion of the reflux tank is passed to the rectification column to continue to reflux, and the rest is taken as a product.
  • the organic mixed solution is a mixture of an organic compound and water or a mixture of two organic compounds.
  • the organic compound is selected from the group consisting of an alcohol, a ketone, an aldehyde or an ester organic compound, for example: methanol, ethanol, and n-propyl Alcohol, isopropanol, formaldehyde, acetaldehyde, propionaldehyde, acetone, methyl ethyl ketone, methyl formate or ethyl formate.
  • an alcohol a ketone
  • an aldehyde or an ester organic compound for example: methanol, ethanol, and n-propyl Alcohol, isopropanol, formaldehyde, acetaldehyde, propionaldehyde, acetone, methyl ethyl ketone, methyl formate or ethyl formate.
  • the organic mixed solution has a light component mass concentration of 25 to 75%.
  • the feed evaporator is selected from the group consisting of a plate heat exchanger, a tube heat exchanger, a tube plate heat exchanger or a spiral plate heat exchanger, and the heat exchange temperature difference ranges from 10 to 60 °C.
  • the feed steam compressor is selected from the group consisting of a positive displacement compressor, a reciprocating compressor, and a centrifugal compressor, and has a temperature rise range of 20 to 60 ° C and a compression ratio of 1.5 to 5.0.
  • the rectification column is selected from the group consisting of a sieve tray tower, a float valve tower or a packed tower, and the reflux ratio of the column top is 1.0 to 5.0.
  • the present invention has the following advantages and beneficial effects:
  • the present invention discloses a novel heat pump rectification process for rectification of a large temperature difference (greater than 30 ° C) in a column tower.
  • the steam at the top of the rectification column is used as a heat source for heating the feed, and the feed can be heated not only to the feed. Dew point or above, and significantly reduce the compression ratio of the overhead steam, reducing compression power consumption, thereby reducing energy consumption.
  • the present invention can greatly reduce the required cooling cycle water consumption of steam condensation at the top of the tower by recovering the latent heat of condensation of the steam at the top of the tower and effectively increasing the heat utilization efficiency.
  • the invention is applicable to all heat pump rectification processes satisfying the conditions, and has a wide application range.
  • the present invention relates to a novel compression heat pump rectification process for a temperature difference of a tower overhead tank exceeding 30 °C.
  • the process uses the steam at the top of the distillation column as a heat source, and the steam at the top of the column is condensed while heating the feed to a vaporization condition under reduced pressure.
  • the vaporized feed is compressed by the compressor and passed to the rectification column.
  • the present invention saves the heat consumed by the vaporization of the feedstock; if the prior art rectification column is a liquid phase feed
  • the invention transforms the rectification column into a gas phase feed, and the energy consumption required for the rectification process is greatly saved due to the increase of the feed energy.
  • the cooling cycle water consumption for the steam at the top of the condensation tower but also the latent heat of condensation of the top steam can be recovered, and the heat utilization efficiency can be improved, and the energy consumption can be reduced.
  • Figure 1 is a flow chart showing the heat pump rectification process of the embodiment of the present invention.
  • 1 is feed evaporator
  • 2 is feed steam compressor
  • 3 is rectification tower
  • 4 is tower top condensation cooler
  • 5 is reflux tank
  • 11 is feed evaporator inlet
  • 12 is feed evaporator
  • the discharge port, 13 is the feed evaporator heating medium feed port
  • 14 is the feed evaporator heating medium discharge port
  • 21 is the compressor feed port
  • 22 is the compressor discharge port
  • 31 is the rectification column.
  • the feed port, 32 is the steam outlet of the distillation column overhead
  • 33 is the distillation column
  • 34 is the reflux feed inlet
  • 41 is the cooler feed port
  • 42 is the cooler discharge port
  • 51 is the reflux
  • the tank feed port, 52 is the reflux liquid outlet
  • 53 is the top product production outlet.
  • Fig. 2 is a flow chart showing the conventional rectification process of Comparative Example 1.
  • 6 is a feed evaporator
  • 7 is a rectification column
  • 8 is a column top condensation cooler
  • 9 is a reflux tank.
  • Fig. 1 is a flow chart showing the heat pump rectification process according to the embodiment of the present invention; the rectification column adopts a gas phase feed.
  • the feed amount of 10T / h is 50 ° C calculation
  • the distillation column 3 uses 45 actual trays
  • the reflux ratio of the top of the tower is 3.0
  • the steam from the top of the distillation tower 3 is used as the feed evaporator
  • the heat source of 1 is heated under reduced pressure to vaporize the feed, and then pressurized by the feed steam compressor 2 to increase the feed pressure and then enter the rectification column 3.
  • methanol having a water content of less than 100 ppm is obtained, and the methanol concentration in the column reactor is also less than 100 ppm.
  • the overhead vapor after heat exchange through the feed evaporator 1 is cooled to a liquid phase in the overhead condensing cooler 4, and the heat exchange amount is 1.38 Gcal/h.
  • the heat loss of the rectification column 3 column kettle reboiler is 1.55 Gcal/h.
  • the overhead condensing cooler 4 condensed liquid enters the reflux tank 5; the condensate portion of the reflux tank 5 is passed to the rectification column 3 to continue the reflux, and the rest is taken as a product.
  • the 50 wt% methanol-water solution separation process is shown in Figure 2.
  • the rectification column uses a gas phase feed with a feed rate of ⁇ /h and a feed temperature of 50 °C.
  • the rectification process uses 45 actual trays, and the reflux ratio of the rectification column 7 is 3.0, and the methanol at the top of the column is less than 100 ppm, and the methanol concentration in the column is also less than 100 ppm.
  • the heat required for the feed evaporator 6 to heat the feed to gasification was 4.43 Gcal/h.
  • the overhead condenser cooler 8 has a cooling capacity of 5.20 Gcal/h.
  • the heat loss of the 7 column kettle reboiler is 1.55 Gcal/h.
  • Example 1 Compared with Comparative Example 1, the feed steam compressor 2 compresses the feed steam from about 0.3 Bar to 1.3 Bar (compression ratio 4.3), and the required effective shaft power is 793 KW, which is calculated according to the motor efficiency of 0.7. The increased power consumption is 1135 kW, which is 0.98 Gcal/h. The entire process saves heating energy consumption 4.43Gcal/h, saving cooling energy consumption 3.82Gcal/h, saving 7.27Gcal/h.
  • the heat pump rectification process is shown in Figure 1, and the rectification column uses gas phase feed. According to the feed amount of 10T / h, the feed temperature is 50 ° C calculation, the distillation column 3 uses 23 actual trays, the reflux ratio of the top of the tower is 5.0, the steam from the top of the distillation tower 3 is used as the feed evaporator
  • the heat source of 1 is heated under reduced pressure to vaporize the feed, and then pressurized by the feed steam compressor 2 to increase the feed pressure and then enter the rectification column 3.
  • ethanol having a water content of less than 15% by weight is obtained, and the ethanol concentration of the column is less than 0.5% by weight.
  • the 25 wt% ethanol-water solution separation process is shown in Figure 2.
  • the rectification column uses a gas phase feed with a feed rate of ⁇ /h and a feed temperature of 50 °C.
  • the rectification process uses 23 actual trays, the rectification column 7 operates at a reflux ratio of 5.0, the top of the column obtains ethanol having a water content of less than 15 wt%, and the column kettle produces an ethanol concentration of less than 0.5 wt%.
  • the heat required for the feed evaporator 6 to heat the feed to gasification was 5.07 Gcal/h, based on the feed amount of 10 T/h and the feed temperature of 50 °C.
  • the overhead condensing cooler 8 has a cooling capacity of 5.17 Gcal/h.
  • the heat loss of the rectification tower crucible reboiler was 0.49 G C al/h.
  • Example 2 Compared with Comparative Example 2, the feed steam compressor 2 compresses the feed steam from about 0.3 Bar to 1.5 Bar (compression ratio 5.0), and the required effective shaft power is 1050 KW, which is calculated according to the motor efficiency of 0.7.
  • the increased power consumption is 1500 KW, which is 1.29 Gcal/h.
  • the entire process saves heating energy consumption by 5.07Gcal/h, saving cooling energy consumption by 4.89Gcal/h, and saving 8.67Gcal/h.
  • the process of the heat pump rectification process of the 75 wt% acetone-water solution separation process is shown in Fig. 1, and the rectification column uses the gas phase feed.
  • the feed amount of 10T / h the feed temperature is 50 ° C calculation
  • the distillation column 3 uses 28 actual trays
  • the reflux ratio of the top of the tower is 1.5
  • the steam from the top of the distillation tower 3 is used as the feed evaporator
  • the heat source of 1 is heated under reduced pressure to vaporize the feed, and then pressurized by the feed steam compressor 2 to increase the feed pressure and then enter the rectification column 3.
  • acetone having a water content of less than 3% by weight is obtained, and the acetone concentration of the column is less than 1% by weight.
  • the overhead vapor after heat exchange by the feed evaporator 1 is cooled to a liquid phase in the overhead condensing cooler 4, and the heat exchange amount is 0.31 G C a /h.
  • the heat loss of the rectification column 3 column kettle reboiler was 0.37 G C al/h.
  • the liquid condensed by the overhead condensing cooler 4 enters the reflux tank 5; the condensate portion of the reflux tank 5 is passed to the rectification column 3 to continue the reflux, and the remainder is produced as a product.
  • the 75 wt% acetone-water solution separation process is shown in Figure 2.
  • the rectification column uses a gas phase feed with a feed rate of ⁇ /h and a feed temperature of 50 °C.
  • the rectification process uses 28 actual trays, the rectification column 7 operates at a reflux ratio of 1.5, the top of the column obtains acetone having a water content of less than 3 wt%, and the column kettle produces an acetone concentration of less than 1 wt%.
  • the heat required for the feed evaporator 6 to heat the feed to gasification was 2.63 Gcal/h.
  • the overhead condensing cooler 8 has a cooling capacity of 2.79 Gcal/h.
  • the heat loss of the rectification column 7 column kettle reboiler was 0.37 G C al/h.
  • Example 3 Compared with Comparative Example 3, the feed steam compressor 2 compresses the feed steam from about 0.35 Bar to 1.3 Bar (compression ratio 3.7), and the required effective shaft power is 620 KW, which is calculated according to the motor efficiency of 0.7. The increased power consumption is 886 kW, which is 0.76 Gcal/h. The entire process saves heating energy consumption 2.63Gcal/h, saving cooling energy consumption 2.48Gcal/h, saving a total of 4.35Gcal/h.
  • Fig. 1 is a flow chart showing the heat pump rectification process of the embodiment of the present invention.
  • a compression heat pump rectification apparatus comprising a feed evaporator 1, a feed steam compressor 2, a rectification column 3, a column top condensing cooler 4, and a reflux tank 5, which are sequentially connected through a pipeline.
  • the feed evaporator 1 is provided with a feed evaporator feed port 11, a feed evaporator discharge port 12, a feed evaporator heating medium feed port 13 and a feed evaporator heating medium discharge port 14, feeding
  • the evaporator heating medium feed port 13 is located at the side of the feed evaporator 1, and the feed evaporator heating medium discharge port 14 is located at the other side corresponding to the feed evaporator heating medium feed port 13;
  • the discharge port 12 is connected to the compressor feed port 21, and the feed evaporator heating medium discharge port 14 is connected to the overhead condensing cooler feed port 41.
  • the feed evaporator heats the medium feed port 13 and the rectification column.
  • the overhead steam outlet 32 is connected.
  • the feed steam compressor 2 is provided with a compressor feed port 21 and a compressor discharge port 22, and the compressor feed port 21 is connected to the feed evaporator discharge port 12, the compressor discharge port 22 and the rectification column
  • the feed port 31 is connected.
  • the rectification column 3 is provided with a rectification column feed port 31, a rectification column overhead steam outlet 32, a rectification column bottom coke outlet 33 and a reflux feed port 34, and the rectification column feed port 31 is located in the rectification column In the middle of the side of the column 3, the reflux feed port 34 is located on the other side corresponding to the rectification column feed port 31, and the rectification column overhead vapor outlet 32 is located at the top of the rectification column 3, and the rectification column bottoms
  • the production outlet 33 is located at the bottom of the rectification column 3; the rectification column feed port 31 is connected to the compressor discharge port 22, and the rectification column overhead steam outlet 32 is connected to the feed evaporator heating medium feed port 13, the reflux liquid
  • the feed port 34 is connected to the reflux outlet 52.
  • the tower top condensing cooler 4 is provided with a cooler feed port 41 and a cooler discharge port 42, and the cooler feed port 41 is connected to the feed evaporator heating medium discharge port 14, the cooler discharge port 42 and the reflux
  • the tank feed port 51 is connected.
  • the return tank 5 is provided with a return tank inlet port 51, a reflux liquid outlet 52 and an overhead product outlet port 53, and the return tank inlet port 51 is connected to the cooler discharge port 42, the reflux liquid outlet 52 and the reflux liquid feed port. 34 connections.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

提供了一种压缩式热泵精馏塔装置及工艺，装置包括进料蒸发器（1）、进料蒸汽压缩机（2）、精馏塔（3）、塔顶冷凝冷却器（4）和回流槽（5），依次经过管路连接。还提供了一种压缩式热泵精馏工艺，将精馏塔顶蒸汽作为加热进料的热源。

Description

明 书 一种压缩式热泵精馏装置及工艺 技术领域
本发明属于化工分离过程和节能技术领域， 涉及一种压缩式热泵精馏装置及工艺。 背景技术
在化工生产过程中， 经常涉及溶剂提纯和分离的精馏工艺过程。 在精馏过程中， 通常直 接将塔顶蒸汽冷凝后， 部分冷凝液作为精馏塔回流， 部分作为产品采出， 此种工艺不但增加 了冷却循环水消耗， 而且也损失了塔顶蒸汽的冷凝潜热。 通常可采用外部工质型、 塔釜闪蒸 式或塔顶蒸汽直接压缩式等压缩式热泵精馏工艺， 回收塔顶蒸汽冷凝潜热， 比如丙烷一丙烯 分离， 三苯分离等。
热泵技术是近年来在全世界倍受关注的新能源技术。 热泵是一种将低温热源的热能转移 到高温热源的装置。 作为一种余热利用的有效工具， 热泵技术逐渐运用在化工精馏领域。 Supranto S.等人研究了涉及两级蒸汽压缩， 在分离乙醇和水的精馏装置中采用了热泵精馏技 术 (Heat pump assisted distillation. IX: Acceptance trials on a system for separating ethanol and water, International Journal of Energy Research, 1988， 12， p 413-422 Gaspillo P.等人介绍了 在脱氢异丙醇反应精馏塔采用化学热泵精馏技术 (Dehydrogenation of 2-propanol in reactive distillation column for chemical heat pump, Journal of Chemical Engineering of Japan, 1998， 31， p440-444)o 中国专利 200680023637.6介绍了一种使用热泵的精馏设备， 用于精馏含水混合物 中易汽化成分。
中国专利 200810231613.0介绍了碳酸二乙酯热泵精馏装置及工艺， 将精馏塔顶蒸汽物料 引入压缩机加压后用于塔釜再沸器热源。 邓仁杰等人研究醋酸丁酯热泵精馏新工艺 (化学工 程， 2006年 6期)， 针对常规醋酸丁酯生产工艺能耗高的特点， 提出将热泵精馏应用于醋酸丁 酯生产， 开发出醋酸丁酯热泵精馏新工艺。 该工艺同样将塔顶蒸汽压缩后用于塔釜再沸器热 源， 装置中酯化塔和精馏塔的塔顶塔釜温差分别为 13 °C和 18°C。
将热泵技术应用于化工行业精馏工艺， 当精馏塔塔顶塔釜温差较大时 (特别是大于 30°C 时)， 如果采用上述热泵精馏工艺， 则存在压缩比非常高， 造成压缩机的功率提高， 节能效果 不明显， 能源利用不够充分的问题。 发明内容 为了解决化工行业中热泵精馏工艺中， 当精馏塔塔顶塔釜温差较大时 (特别是大于 30°C 时)， 压缩比非常高， 节能效果不明显， 能源利用不够充分的问题； 本发明的目的是提供一种 压缩式热泵精馏装置。
本发明的另一个目的是提供一种压缩式热泵精馏工艺。
本发明的技术方案如下：
本发明提供了一种压缩式热泵精馏装置， 该装置包括进料蒸发器、 进料蒸汽压缩机、 精 馏塔、 塔顶冷凝冷却器和回流槽， 依次经过管路连接。
所述的进料蒸发器上设有进料蒸发器进料口、 进料蒸发器出料口、 进料蒸发器加热介质 进料口和进料蒸发器加热介质出料口， 进料蒸发器加热介质进料口位于进料蒸发器的侧边， 进料蒸发器加热介质出料口位于进料蒸发器加热介质进料口相对应的另一侧边； 进料蒸发器 出料口与压缩机进料口连接， 进料蒸发器加热介质出料口与塔顶冷凝冷却器进料口连接， 进 料蒸发器加热介质进料口与精馏塔塔顶蒸汽出口连接。
所述的进料蒸汽压缩机上设有压缩机进料口和压缩机出料口， 压缩机进料口与进料蒸发 器出料口连接， 压缩机出料口与精馏塔进料口连接。
所述的精馏塔上设有精馏塔进料口、 精馏塔塔顶蒸汽出口、 精馏塔塔釜采出口和回流液 进料口， 精馏塔进料口位于精馏塔的侧边中部， 回流液进料口位于精馏塔进料口相对应的另 一侧边， 精馏塔塔顶蒸汽出口位于精馏塔的顶部， 精馏塔塔釜采出口位于精馏塔的底部； 精 馏塔进料口与压缩机出料口连接， 精馏塔塔顶蒸汽出口与进料蒸发器加热介质进料口连接， 回流液进料口与回流液出口连接。
所述的塔顶冷凝冷却器上设有冷却器进料口和冷却器出料口， 冷却器进料口与进料蒸发 器加热介质出料口连接， 冷却器出料口与回流槽进料口连接。
所述的回流槽上设有回流槽进料口、 回流液出口和塔顶产品采出口， 回流槽进料口与冷 却器出料口连接， 回流液出口与回流液进料口连接。
本发明还提供了一种压缩式热泵精馏工艺， 该工艺包括以下步骤：
首先将待分离的有机混合溶液加入到进料蒸发器中， 进料蒸发器在减压条件下以精馏塔 塔顶蒸汽做为热源将进料加热至完全汽化， 汽化后的进料经进料蒸汽压缩机压缩提高进料压 力后进入精馏塔； 进料经精馏塔精馏后， 精馏塔塔釜液体达到采出标准后直接采出， 塔顶蒸 汽通入进料蒸发器作为热源进行热交换， 换热之后的塔顶蒸汽及部分冷凝液进入塔顶冷凝冷 却器冷凝成液体进入回流槽； 回流槽中冷凝液部分通入精馏塔继续回流， 其余作为产品采出。
所述的有机混合溶液为一种 ^〜 有机化合物与水的混合液或者两种 ^〜 有机化合 物的混合液。
所述的 〜 有机化合物选自醇、 酮、 醛或酯类有机化合物， 例如： 甲醇、 乙醇、 正丙 醇、 异丙醇、 甲醛、 乙醛、 丙醛、 丙酮、 甲乙酮、 甲酸甲酯或甲酸乙酯。
所述的有机混合溶液的轻组分质量浓度为 25~75%。
所述的进料蒸发器选自板式换热器、 管式换热器、 管板式换热器或者螺旋板式换热器中 的一种， 换热温差范围在 10~60°C。
所述的进料蒸汽压缩机选自容积式压缩机， 往复式压缩机， 离心式压缩机中的一种， 升 温范围在 20~60°C， 压缩比为 1.5~5.0。
所述的精馏塔选自筛板塔， 浮阀塔或者填料塔中的一种， 塔顶回流比为 1.0~5.0。
本发明同现有技术相比， 具有如下优点和有益效果：
1、本发明公开了一种针对塔顶塔釜大温差 (大于 30°C)精馏的新型热泵精馏工艺， 将精馏 塔顶蒸汽作为加热进料的热源， 不但可以将进料加热至露点或以上温度， 而且明显降低塔顶 蒸汽的压缩比， 减少压缩动力消耗， 从而减少能源消耗。
2、本发明通过回收塔顶蒸汽的冷凝潜热， 有效提高热量利用效率可大大减少塔顶蒸汽冷 凝的所需冷却循环水消耗。
3、 本发明适用于一切满足条件的热泵精馏工艺， 应用范围广阔。
4、 本发明涉及一种针对塔顶塔釜温差超过 30°C的新型压缩式热泵精馏工艺。 该工艺以 精馏塔塔顶蒸汽为热源， 将进料在减压条件下加热至汽化的同时， 塔顶蒸汽被冷凝。 汽化后 的进料经压缩机压缩后进入精馏塔。 与现有的精馏技术进行比较， 如果现有技术的精馏塔采 用外部热源加热的气相进料， 本发明则节约原料汽化所消耗热量； 如果现有技术的精馏塔为 液相进料， 本发明将精馏塔改造为气相进料， 由于进料能量提高， 大大节约精馏过程的需要 的能耗。 对于传统精馏塔顶塔釜温差大的精馏工艺， 不但可节约用于冷凝塔顶蒸汽的冷却循 环水消耗， 也可回收塔顶蒸汽的冷凝潜热， 提高热量利用效率， 节能降耗。 附图说明
图 1表示本发明实施例的热泵精馏工艺流程图。
1为进料蒸发器、 2为进料蒸汽压缩机、 3为精馏塔、 4为塔顶冷凝冷却器、 5为回流槽、 11为进料蒸发器进料口、 12为进料蒸发器出料口、 13为进料蒸发器加热介质进料口、 14为 进料蒸发器加热介质出料口、 21为压缩机进料口、 22为压缩机出料口、 31为精馏塔进料口、 32为精馏塔塔顶蒸汽出口、 33为精馏塔塔釜采出口、 34为回流液进料口、 41为冷却器进料 口、 42为冷却器出料口、 51为回流槽进料口、 52为回流液出口、 53为塔顶产品采出口。
图 2表示比较例 1普通精馏工艺流程图。
6为进料蒸发器、 7为精馏塔、 8为塔顶冷凝冷却器、 9为回流槽。 具体实施方式
以下结合附图所示实施例对本发明作进一步的说明。
实施例 1
50wt%甲醇-水溶液分离过程热泵精馏工艺的流程如图 1所示， 图 1表示本发明实施例的 热泵精馏工艺流程图； 精馏塔采用气相进料。
按照进料量 10T/h， 进料温度为 50°C计算， 精馏塔 3采用 45块实际塔板， 塔顶回流比为 3.0, 将精馏塔 3塔顶采出蒸汽作为进料蒸发器 1的热源， 在减压条件下加热使进料气化， 然 后利用进料蒸汽压缩机 2压缩提高进料压力后进入精馏塔 3。 精馏塔 3塔顶得到水含量小于 lOOppm的甲醇， 塔釜采出中甲醇浓度同样小于 100ppm。 经过进料蒸发器 1换热后的塔顶蒸 汽在塔顶冷凝冷却器 4中冷却为液相， 换热量为 1.38Gcal/h。 精馏塔 3塔釜再沸器的热量消 耗为 1.55Gcal/h。塔顶冷凝冷却器 4冷凝的液体进入回流槽 5 ; 回流槽 5中冷凝液部分通入精 馏塔 3继续回流， 其余作为产品采出。
比较例 1
50wt%甲醇-水溶液分离过程普通精馏工艺如图 2 所示， 精馏塔采用气相进料， 进料量 ΙΟΤ/h, 进料温度为 50°C。
该精馏过程采用 45块实际塔板，精馏塔 7塔顶回流比为 3.0，塔顶得到水含量小于 lOOppm 的甲醇， 塔釜采出甲醇浓度同样小于 100ppm。 按照进料量 10T/h， 进料温度为 50°C计算， 进 料蒸发器 6 将进料加热至气化所需要的热量为 4.43Gcal/h。 塔顶冷凝冷却器 8 冷量为 5.20Gcal/h。 精馏塔 7塔釜再沸器的热量消耗为 1.55Gcal/h。
实施例 1与比较例 1相比， 进料蒸汽压缩机 2将进料蒸汽由约 0.3Bar压缩至 1.3Bar (压 缩比 4.3 )， 所需要的有效轴功率为 793KW, 按照电机效率 0.7 计算， 需要增加的电耗为 1135KW, 即 0.98Gcal/h。 整个工艺过程节约加热能量消耗 4.43Gcal/h， 节约冷却能量消耗 3.82Gcal/h, 合计节约 7.27Gcal/h。
实施例 2
25wt%乙醇-水溶液分离过程热泵精馏工艺的流程如图 1所示， 精馏塔采用气相进料。 按照进料量 10T/h， 进料温度为 50°C计算， 精馏塔 3采用 23块实际塔板， 塔顶回流比为 5.0， 将精馏塔 3塔顶采出蒸汽作为进料蒸发器 1的热源， 在减压条件下加热使进料气化， 然 后利用进料蒸汽压缩机 2压缩提高进料压力后进入精馏塔 3。 精馏塔 3塔顶得到水含量小于 15wt%的乙醇， 塔釜采出乙醇浓度小于 0.5wt%。 经过进料蒸发器 1换热后的塔顶蒸汽在塔顶 冷凝冷却器 4 中冷却为液相， 换热量为 0.28GCal/h。 精馏塔 3 塔釜再沸器的热量消耗为 0.49GCal/h。 塔顶冷凝冷却器 4冷凝的液体进入回流槽 5 ; 回流槽 5中冷凝液部分通入精馏塔 3继续回流， 其余作为产品采出。 比较例 2
25wt%乙醇-水溶液分离过程普通精馏工艺如图 2 所示， 精馏塔采用气相进料， 进料量 ΙΟΤ/h, 进料温度为 50°C。
该精馏过程采用 23块实际塔板，精馏塔 7操作回流比为 5.0，塔顶得到水含量小于 15 wt% 的乙醇， 塔釜采出乙醇浓度小于 0.5wt%。 按照进料量 10T/h， 进料温度为 50°C计算， 进料蒸 发器 6将进料加热至气化所需要的热量为 5.07Gcal/h。 塔顶冷凝冷却器 8冷量为 5.17Gcal/h。 精馏塔 Ί塔釜再沸器的热量消耗为 0.49GCal/h。
实施例 2与比较例 2相比， 进料蒸汽压缩机 2将进料蒸汽由约 0.3Bar压缩至 1.5Bar (压 缩比 5.0)， 所需要的有效轴功率为 1050KW, 按照电机效率 0.7 计算， 需要增加的电耗为 1500KW, 即 1.29Gcal/h。 整个工艺过程节约加热能量消耗 5.07Gcal/h， 节约冷却能量消耗 4.89Gcal/h， 合计节约 8.67Gcal/h。
实施例 3
75wt%丙酮-水溶液分离过程热泵精馏工艺的流程如图 1所示， 精馏塔采用气相进料。 按照进料量 10T/h， 进料温度为 50°C计算， 精馏塔 3采用 28块实际塔板， 塔顶回流比为 1.5， 将精馏塔 3塔顶采出蒸汽作为进料蒸发器 1的热源， 在减压条件下加热使进料气化， 然 后利用进料蒸汽压缩机 2压缩提高进料压力后进入精馏塔 3。 精馏塔 3塔顶得到水含量小于 3wt%的丙酮， 塔釜采出丙酮浓度小于 lwt%。 经过进料蒸发器 1换热后的塔顶蒸汽在塔顶冷 凝冷却器 4中冷却为液相，换热量为 0.31GCal/h。精馏塔 3塔釜再沸器的热量消耗为 0.37GCal/h。 塔顶冷凝冷却器 4冷凝的液体进入回流槽 5 ; 回流槽 5中冷凝液部分通入精馏塔 3继续回流， 其余作为产品采出。
比较例 3
75wt%丙酮-水溶液分离过程普通精馏工艺如图 2 所示， 精馏塔采用气相进料， 进料量 ΙΟΤ/h, 进料温度为 50°C。
该精馏过程采用 28块实际塔板，精馏塔 7操作回流比为 1.5，塔顶得到水含量小于 3wt% 的丙酮， 塔釜采出丙酮浓度小于 lwt%。 按照进料量 10T/h， 进料温度为 50°C计算， 进料蒸发 器 6将进料加热至气化所需要的热量为 2.63Gcal/h。 塔顶冷凝冷却器 8冷量为 2.79Gcal/h。 精 馏塔 7塔釜再沸器的热量消耗为 0.37GCal/h。
实施例 3与比较例 3相比，进料蒸汽压缩机 2将进料蒸汽由约 0.35Bar压缩至 1.3Bar (压 缩比 3.7)，所需要的有效轴功率为 620KW,按照电机效率 0.7计算，需要增加的电耗为 886KW, 即 0.76Gcal/h。 整个工艺过程节约加热能量消耗 2.63Gcal/h， 节约冷却能量消耗 2.48Gcal/h， 合计节约 4.35Gcal/h。
实施例 4 如图 1所示， 图 1表示本发明实施例的热泵精馏工艺流程图。
一种压缩式热泵精馏装置， 该装置包括进料蒸发器 1、 进料蒸汽压缩机 2、 精馏塔 3、 塔 顶冷凝冷却器 4和回流槽 5， 依次经过管路连接。
进料蒸发器 1上设有进料蒸发器进料口 11、进料蒸发器出料口 12、进料蒸发器加热介质 进料口 13和进料蒸发器加热介质出料口 14， 进料蒸发器加热介质进料口 13位于进料蒸发器 1的侧边， 进料蒸发器加热介质出料口 14位于进料蒸发器加热介质进料口 13相对应的另一 侧边； 进料蒸发器出料口 12与压缩机进料口 21连接， 进料蒸发器加热介质出料口 14与塔顶 冷凝冷却器进料口 41连接， 进料蒸发器加热介质进料口 13与精馏塔塔顶蒸汽出口 32连接。
进料蒸汽压缩机 2上设有压缩机进料口 21和压缩机出料口 22， 压缩机进料口 21与进料 蒸发器出料口 12连接， 压缩机出料口 22与精馏塔进料口 31连接。
精馏塔 3上设有精馏塔进料口 31、 精馏塔塔顶蒸汽出口 32、 精馏塔塔釜采出口 33和回 流液进料口 34， 精馏塔进料口 31位于精馏塔 3的侧边中部， 回流液进料口 34位于精馏塔进 料口 31相对应的另一侧边， 精馏塔塔顶蒸汽出口 32位于精馏塔 3的顶部， 精馏塔塔釜采出 口 33位于精馏塔 3的底部； 精馏塔进料口 31与压缩机出料口 22连接， 精馏塔塔顶蒸汽出口 32与进料蒸发器加热介质进料口 13连接， 回流液进料口 34与回流液出口 52连接。
塔顶冷凝冷却器 4上设有冷却器进料口 41和冷却器出料口 42， 冷却器进料口 41与进料 蒸发器加热介质出料口 14连接， 冷却器出料口 42与回流槽进料口 51连接。
回流槽 5上设有回流槽进料口 51、 回流液出口 52和塔顶产品采出口 53， 回流槽进料口 51与冷却器出料口 42连接， 回流液出口 52与回流液进料口 34连接。
上述的对实施例的描述是为便于该技术领域的普通技术人员能理解和应用本发明。 熟悉 本领域技术的人员显然可以容易地对这些实施例做出各种修改， 并把在此说明的一般原理应 用到其他实施例中而不必经过创造性的劳动。 因此， 本发明不限于这里的实施例， 本领域技 术人员根据本发明的揭示， 不脱离本发明范畴所做出的改进和修改都应该在本发明的保护范 围之内。

Claims

权 利 要 求 书
1. 一种压缩式热泵精馏装置， 其特征在于： 该装置包括进料蒸发器 （1)、 进料蒸汽压缩 机 （2)、 精馏塔 （3)、 塔顶冷凝冷却器 （4) 和回流槽 （5)， 依次经过管路连接。
2. 根据权利要求 1 所述的压缩式热泵精馏装置， 其特征在于： 所述的进料蒸发器 （1) 上设有进料蒸发器进料口 （11)、 进料蒸发器出料口 （12)、 进料蒸发器加热介质进料口 （13) 和进料蒸发器加热介质出料口 （14)， 进料蒸发器加热介质进料口 （13)位于进料蒸发器（1) 的侧边， 进料蒸发器加热介质出料口 （14) 位于进料蒸发器加热介质进料口 （13) 相对应的 另一侧边； 进料蒸发器出料口 （12) 与压缩机进料口 （21) 连接， 进料蒸发器加热介质出料 口 （14) 与塔顶冷凝冷却器进料口 （41) 连接， 进料蒸发器加热介质进料口 （13) 与精馏塔 塔顶蒸汽出口 （32) 连接。
3. 根据权利要求 1所述的压缩式热泵精馏装置，其特征在于：所述的进料蒸汽压缩机（2) 上设有压缩机进料口 （21)和压缩机出料口 （22)， 压缩机进料口 （21)与进料蒸发器出料口
(12) 连接， 压缩机出料口 （22) 与精馏塔进料口 （31) 连接。
4. 根据权利要求 1 所述的压缩式热泵精馏装置， 其特征在于： 所述的精馏塔 （3) 上设 有精馏塔进料口 （31)、 精馏塔塔顶蒸汽出口 （32)、 精馏塔塔釜采出口 （33) 和回流液进料 口 （34)， 精馏塔进料口 （31) 位于精馏塔 （3) 的侧边中部， 回流液进料口 （34) 位于精馏 塔进料口 （31)相对应的另一侧边， 精馏塔塔顶蒸汽出口 （32)位于精馏塔 （3) 的顶部， 精 馏塔塔釜采出口 （33) 位于精馏塔 （3) 的底部； 精馏塔进料口 （31) 与压缩机出料口 （22) 连接， 精馏塔塔顶蒸汽出口 （32) 与进料蒸发器加热介质进料口 （13) 连接， 回流液进料口
(34) 与回流液出口 （52) 连接。
5. 根据权利要求 1所述的压缩式热泵精馏装置，其特征在于：所述的塔顶冷凝冷却器（4) 上设有冷却器进料口 （41)和冷却器出料口 （42)， 冷却器进料口 （41)与进料蒸发器加热介 质出料口 （14) 连接， 冷却器出料口 （42) 与回流槽进料口 （51) 连接。
6. 根据权利要求 1 所述的压缩式热泵精馏装置， 其特征在于： 所述的回流槽 （5) 上设 有回流槽进料口 （51)、 回流液出口 （52) 和塔顶产品采出口 （53)， 回流槽进料口 （51) 与 冷却器出料口 （42) 连接， 回流液出口 （52) 与回流液进料口 （34) 连接。
7. 权利要求 1~6任一所述的装置进行的压缩式热泵精馏工艺， 其特征在于： 该工艺包括 以下步骤：
首先将待分离的有机混合溶液加入到进料蒸发器 （1) 中， 进料蒸发器 （1) 在减压条件 下以精馏塔（3)塔顶蒸汽做为热源将进料加热至完全汽化， 汽化后的进料经进料蒸汽压缩机 (2)压缩提高进料压力后进入精馏塔 （3); 进料经精馏塔 （3)精馏后， 精馏塔 （3)塔釜液 体达到采出标准后直接采出， 塔顶蒸汽通入进料蒸发器（1)作为热源进行热交换， 换热之后 的塔顶蒸汽及部分冷凝液进入塔顶冷凝冷却器（4)冷凝成液体进入回流槽（5 ); 回流槽（5 ) 中冷凝液部分通入精馏塔 （3 ) 继续回流， 其余作为产品采出。
8. 根据权利要求 7所述的压缩式热泵精馏工艺， 其特征在于： 所述的有机混合溶液为一 种 ^〜 有机化合物与水的混合液或者两种 ^〜 有机化合物的混合液。
9. 根据权利要求 8所述的压缩式热泵精馏工艺， 其特征在于： 所述的 〜 有机化合 物选自醇、 酮、 醛或酯类有机化合物， 例如： 甲醇、 乙醇、 正丙醇、 异丙醇、 甲醛、 乙醛、 丙醛、 丙酮、 甲乙酮、 甲酸甲酯或甲酸乙酯。
10. 根据权利要求 7所述的压缩式热泵精馏工艺， 其特征在于： 所述的有机混合溶液的 轻组分质量浓度为 25~75%。
11. 根据权利要求 7所述的压缩式热泵精馏工艺， 其特征在于： 所述的进料蒸发器 （1 ) 选自板式换热器、 管式换热器、 管板式换热器或者螺旋板式换热器中的一种， 换热温差范围 在 10~60°C o
12. 根据权利要求 7所述的压缩式热泵精馏工艺， 其特征在于： 所述的进料蒸汽压缩机 (2) 选自容积式压缩机， 往复式压缩机， 离心式压缩机中的一种， 升温范围在 20~60°C， 压 缩比为 1.5~5.0。
13. 根据权利要求 7所述的压缩式热泵精馏工艺， 其特征在于： 所述的精馏塔 （3 ) 选自 筛板塔、 浮阀塔或者填料塔中的一种， 塔顶回流比为 1.0~5.0。
PCT/CN2013/077862 2012-08-06 2013-06-25 一种压缩式热泵精馏装置及工艺 WO2014023137A1 (zh)

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