WO2013067918A1 - 醋酸乙烯生产过程乙烯回收方法及装置 - Google Patents

醋酸乙烯生产过程乙烯回收方法及装置 Download PDF

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Publication number
WO2013067918A1
WO2013067918A1 PCT/CN2012/084164 CN2012084164W WO2013067918A1 WO 2013067918 A1 WO2013067918 A1 WO 2013067918A1 CN 2012084164 W CN2012084164 W CN 2012084164W WO 2013067918 A1 WO2013067918 A1 WO 2013067918A1
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Prior art keywords
vinyl acetate
ethylene
acetic acid
absorption liquid
section
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PCT/CN2012/084164
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English (en)
French (fr)
Inventor
张敏华
董秀芹
刘成
陶敏莉
李永辉
吕惠生
余英哲
耿中峰
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天津大学
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Priority to US14/356,602 priority Critical patent/US9636627B2/en
Priority to EP12848642.0A priority patent/EP2778149A4/en
Priority to JP2014540303A priority patent/JP5864770B2/ja
Priority to SG11201402168QA priority patent/SG11201402168QA/en
Priority to BR112014011092A priority patent/BR112014011092A2/pt
Publication of WO2013067918A1 publication Critical patent/WO2013067918A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1406—Multiple stage absorption
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1418—Recovery of products
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1487—Removing organic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B01D53/185—Liquid distributors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/205—Other organic compounds not covered by B01D2252/00 - B01D2252/20494
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/50—Combinations of absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/50—Combinations of absorbents
    • B01D2252/504—Mixtures of two or more absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons

Definitions

  • This invention relates to an ethylene recovery process for use in a vinyl acetate production process.
  • it is an ethylene recovery method and apparatus for the production of vinyl acetate in an ethylene process.
  • Vinyl acetate (VAC) is an important organic chemical raw material.
  • PVA polyvinyl alcohol
  • EVA vinyl acetate-ethylene copolymer
  • PVAC polyvinyl acetate
  • a derivative such as vinyl acetate monovinyl chloride copolymer (EVC).
  • China's vinyl acetate production began in the 1960s. In 1965, the Beijing Organic Chemical Plant introduced acetylene fluidized bed technology from Japan, and then built several sets of similar devices in China. These vinyl acetate units are all supplied with Vinylon. In the 1970s and 1980s, about 90% of China's vinyl acetate was used for vinylon and polyvinyl alcohol. In recent years, with the development of polyvinyl alcohol, China's vinyl acetate market has continued to expand. As of the end of 2008, China's total production capacity of vinyl acetate was 1.4 million tons per year. It is expected that the demand for vinyl acetate in China will increase at a rate of 8% in the future.
  • the vinyl acetate production process has two methods: ethylene method and acetylene method. Ethylene production dominates worldwide. Acetylene pollution is serious and has been eliminated in foreign countries. At present, only a few countries such as China adopt the acetylene method.
  • the ethylene vinyl acetate production process is to feed the raw materials of ethylene, oxygen and acetic acid into the reactor, and contact with the catalyst in the reactor, and react at a pressure of 0.1 6-1. IMPa and 130 ⁇ 200 ° C to form VA ( :, water and a small amount of by-products.
  • the high-temperature reaction gas is condensed in multiple stages, the condensate contains vinyl acetate, water and unreacted acetic acid, etc., and the mixed liquid is sent to the fine boring process for VAC refining. Unreacted ethylene gas is returned to the compressor cycle Used, it is called a circulating gas.
  • Ethylene is one of the world's largest chemical products and the most important basic chemical raw material. It plays an important role in the national economy. Ethylene is one of the raw materials for the synthesis of vinyl acetate. In the production process of vinyl acetate to produce vinyl acetate, the single pass conversion of ethylene is only about 10%, and a large amount of unconverted ethylene must be recycled. In order to prevent the inert gas from accumulating and to reduce the ethylene concentration and affect the smooth progress of the reaction, a part of the gas is extracted from the refined gas, and the main component of the purified gas is ethylene, which causes loss of the ethylene raw material. Selecting the appropriate absorption liquid, developing a new process, achieving selective recovery of ethylene gas, reducing ethylene gas emissions, reducing the production cost of vinyl acetate and improving the market competitiveness of the product.
  • the object of the present invention is to provide a method and a device capable of selectively recovering ethylene from a purified gas in a vinyl acetate production process, which can reduce ethylene emissions during the production of vinyl acetate in a gas phase process, reduce raw material consumption, and save acetic acid. Alene production costs.
  • the circulating gas mainly includes inert components such as ethylene, main by-product C0 2 and N 2 in the system.
  • inert components such as ethylene, main by-product C0 2 and N 2 in the system.
  • some gas needs to be extracted for decarburization to remove part of C0. 2 , The decarburized gas is returned to the synthesis section and is called refined gas.
  • the main component of the discharged refined gas is ethylene.
  • different methods have been employed, including the use of the product vinyl acetate as the absorption liquid, the raw material acetic acid as the absorption liquid, and the like.
  • Vinyl acetate has good solubility for ethylene, but at the same time dissolves a large amount of other inert gases.
  • Acetic acid has good selectivity to ethylene, but its solubility is poor.
  • the ethylene recovery process of the vinyl acetate production process of the present invention is carried out in two stages for the ethylene recovery tower, the upper section being the water washing section and the lower section being the absorption liquid washing section.
  • a method for recovering ethylene in a vinyl acetate production process using a double solvent absorption method consisting of an absorbing liquid and a non-ionized water: extracting a stream from an acetic acid column feed plate section of a fine vinyl acetate production section as an absorbing liquid, and an absorbing liquid transfer pump It is sent to the top of the lower part of the ethylene recovery tower.
  • the refined gas is passed from the ethylene recovery tower.
  • the absorption liquid is in countercurrent contact with the refined gas.
  • the absorption liquid is sent to the fine section for treatment.
  • the gas continues to rise to the upper part of the ethylene recovery tower and the top of the tower.
  • the non-ionized water is countercurrently contacted, and the acetic acid is removed by absorption; the remaining inert gas is discharged from the top of the ethylene recovery tower.
  • the absorbing liquid is derived from the acetic acid column feed plate section of the vinyl acetate production finishing section, and is a mixture of acetic acid, vinyl acetate and water, and the weight percentage is acetic acid 50-85%, vinyl acetate 5-30% and water 5-20. %.
  • the apparatus for recovering ethylene in the vinyl acetate production process of the invention is: the acetic acid column feed plate section of the vinyl acetate production finishing section is connected to the inlet of the absorption liquid buffer tank, and the outlet of the absorption liquid buffer tank is connected with the inlet of the absorption liquid transfer pump, the absorption liquid The pump outlet is connected to the lower section of the ethylene recovery tower.
  • the ethylene recovery tower is a composite tower, and the ethylene recovery tower is divided into upper and lower sections, the upper section is a water washing section, and the lower section is an absorption liquid washing section.
  • the operating pressure of the ethylene recovery column is an absolute pressure of 0.5-1.2 MPa and an operating temperature of 25-80 °C.
  • the method for recovering ethylene in the vinyl acetate production process of the invention has the advantages of adopting the double solvent absorption method, and extracting the stream as the absorption liquid from the upper part of the acetic acid column feeding section of the fine-slurry section, combining the high solubility characteristics of vinyl acetate on ethylene and the acetic acid to ethylene
  • the highly selected solubility characteristics enable the addition and synergistic function of the absorption liquid, selectively recover the ethylene gas in the refined gas, reduce the ethylene emission loss, and reduce the consumption of raw materials for the production of vinyl acetate.
  • the selectivity of ethylene recovery is 60-95%, the loss of ethylene is reduced, the production cost of the product is lowered, and the market competitiveness of the vinyl acetate product is improved.
  • Figure 1 Schematic diagram of the ethylene recovery process in the vinyl acetate production process. detailed description
  • the apparatus for recovering ethylene in the vinyl acetate production process of the present invention is as follows:
  • the acetic acid column feed plate section of the vinyl acetate production finishing section is connected to the inlet of the absorption liquid buffer tank, and the absorption liquid buffer tank
  • the outlet is connected to the inlet of the absorption liquid transfer pump, and the outlet of the absorption liquid transfer pump is connected to the lower section of the ethylene recovery tower.
  • the ethylene recovery tower is a composite tower, and the ethylene recovery tower is divided into upper and lower sections, the upper section is a water washing section, and the lower section is an absorption liquid washing section.
  • the operating pressure of the ethylene recovery column is an absolute pressure of 0.5-1.2 MPa and an operating temperature of 25-80 °C.
  • the feed stream from the acetic acid column 4 feed plate section of the self-finishing section is taken as the absorption liquid, and the absorption liquid is sent to the buffer tank 1, and sent to the top of the lower section of the ethylene recovery tower 3 by the absorption liquid transfer pump 2, and the purified gas is recovered from the ethylene recovery tower 3.
  • the tower is opened, and the absorption liquid and the purified gas are countercurrently contacted in the column, and the selective recovery of the ethylene gas is realized according to the solubility characteristics of the purified gas in the absorption liquid.
  • the kettle liquid is sent to the finishing section for degassing treatment, and the unabsorbed ascending gas mainly contains an inert gas such as N 2 and a small amount of acetic acid.
  • the rising gas is in countercurrent contact with the ion-free water passing through the top of the column in the upper portion of the ethylene recovery column to absorb the acetic acid removed therefrom.
  • the inert gas is discharged from the top of the ethylene recovery tower to prevent the accumulation of inert gas.
  • the composition of the absorbent (wt%) was 78% acetic acid, 8% vinyl acetate, 14% water, and an ethylene recovery selectivity of 90%.
  • the method was the same as in Example 1; the composition of the absorbent (wt%) was 85% acetic acid, 5% vinyl acetate, 10% water, and the selectivity of ethylene recovery was 95%.
  • the method was the same as in Example 1; the composition of the absorbent (wt%) was 50% acetic acid, 30% vinyl acetate, 20% water, and the selectivity of ethylene recovery was 60%.
  • the method was the same as in Example 1; the composition of the absorbent (wt%) was 65% acetic acid, 30% vinyl acetate, 5% water, and the selectivity of ethylene recovery was 70%.
  • the method and device for recovering ethylene in the vinyl acetate production process disclosed and proposed by the present invention can be realized by those skilled in the art by appropriately changing the raw materials, process parameters, structural design and the like.
  • the method and technology of the present invention have been described by way of a preferred embodiment, and it will be apparent to those skilled in the ⁇ Desc/Clms Page number> The technology of the present invention. It is to be understood that the various alternatives and modifications are obvious to those skilled in the art and are considered to be included in the spirit, scope and content of the invention.

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  • Engineering & Computer Science (AREA)
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Abstract

一种醋酸乙烯生产过程乙烯回收方法及装置，采用吸收液和无离子水组成的双溶剂吸收法：自醋酸乙烯生产精镏工段的醋酸塔进料板上段引出流股作为吸收液，由吸收液输送泵送至乙烯回收塔下段顶部，精制气由乙烯回收塔塔釜通入，吸收液与精制气逆流接触；吸收釜液送至精镏工段处理，气体继续上升至乙烯回收塔上段与塔顶部通入的无离子水逆流接触，吸收脱除其中的醋酸；剩余的N2等惰性气体由乙烯回收塔塔顶排出。所述的吸收液为乙酸、醋酸乙烯及水的混合物，重量百分比为乙酸50-85%、醋酸乙烯5-30%和水5-20%。

Description

醋酸乙烯牛产过稈乙烯回收方法及装置
技术领域
本发明涉及用于醋酸乙烯生产过程的乙烯回收方法。 特别是用于乙烯法生产醋酸乙烯生 产过程的乙烯回收方法及装置。 背景技术
醋酸乙烯 (VAC)是一种重要的有机化工原料， 通过自身聚合或与其它单体共聚， 可以生成 聚乙烯醇 (PVA)、 醋酸乙烯一乙烯共聚物 (EVA)、 聚醋酸乙烯 (PVAC)、 醋酸乙烯一氯乙烯共聚 物 (EVC)等衍生物。 这些衍生物的用途十分广泛， 一般可用于粘接剂， 纸张或织物的上胶剂、 油漆、 墨水、 皮革加工、 乳化剂、 水溶性膜、 土壤改良剂等方面。 醋酸乙烯作为中间体， 随 着聚乙烯醇非纤维领域应用的拓展， 使得醋酸乙烯的需求不断增长， 提高。
我国醋酸乙烯生产开始于 20世纪 60年代。 1965年北京有机化工厂从日本引进乙炔法流化 床技术， 之后在国内建成多套同类装置。 这些醋酸乙烯装置均为维尼纶配套， 在 20世纪 70〜 80年代， 中国醋酸乙烯约有 90%用于维尼纶及聚乙烯醇。 近年来随着聚乙烯醇的发展， 中国 醋酸乙烯市场不断扩大。 截至到 2008年底， 中国醋酸乙烯总生产能力 140万吨 /年， 预计未来 我国醋酸乙烯的需求量将以 8%的速率增长。
醋酸乙烯生产工艺路线有乙烯法和乙炔法两种。 在世界范围内乙烯法生产占主导地位。 乙炔污染严重， 在国外已被淘汰， 目前只有我国等少数国家采用乙炔法。 乙烯法醋酸乙烯生 产过程是将原料乙烯、 氧、 醋酸气体通入反应器， 在反应器内与催化剂接触， 在绝对压力 0. 6-1. IMPa和 130〜200°C温度下反应生成 VA (：、水及少量副产物。高温反应气体经多级冷凝， 冷凝液中含有醋酸乙烯、 水及未反应的醋酸等， 混合液送精镏工序进行 VAC的精制。 未反应 乙烯气体返回压缩机循环使用， 被成为循环气体。
乙烯是世界上产量最大的化学产品之一， 也是最重要的基本化工原料， 在国民经济中占 有重要的地位。 乙烯是合成醋酸乙烯的原料之一。 在乙烯法生产醋酸乙烯的生产过程中， 乙 烯的单程转化率仅为 10%左右， 大量未转化的乙烯必须循环使用。为防止氮气等惰性气体累积 后降低乙烯浓度影响反应的顺利进行， 需从精制气体中抽出一部分气体排放， 排出的精制气 体的主要组成为乙烯， 这样就造成乙烯原料的损失。选择适宜的吸收液， 开发新的工艺过程, 实现乙烯气体的选择性回收， 减少乙烯气体的排放， 能够降低醋酸乙烯生产成本， 提高产品 的市场竞争力。
发明内容
本发明的目的在于提供一种能够从醋酸乙烯生产过程精制气中选择性回收乙烯的方法及 装置， 该工艺能够减少气相法醋酸乙烯生产过程中乙烯的排放， 降低原料消耗， 节约醋酸乙 烯生产成本。
在乙烯法醋酸乙烯的生产过程中， 原料的单程转化率较低， 乙烯的单程转化率仅为 10% 左右， 并且受到爆炸限的限制， 实际生产中乙烯总是大量过剩， 大量的乙烯必须循环使用。 循环气体主要包括乙烯、 主要副产物 C02以及系统中的 N2等惰性组分， 为了保持系统中乙烯 浓度和循环气中 C02浓度恒定， 需抽出部分气体进行脱碳处理， 以除去部分 C02， 脱碳后的气 体返回合成工段使用， 被称为精制气体。 为了防止惰性气体积累， 需要从精制气体中再抽出 一部分气体排放， 排出的精制气体的主要组成为乙烯。 为了回收这部分乙烯气体， 人们采用 了不同的方法， 包括使用产品醋酸乙烯作为吸收液、 以原料醋酸作为吸收液等等。 醋酸乙烯 对乙烯具有较好的溶解性， 但同时溶解大量其它惰性气体。 醋酸对乙烯的选择性较好， 但溶 解度较差。
本发明的醋酸乙烯生产过程乙烯回收方法， 针对乙烯回收塔分为两段进行， 上段为水洗 段， 下段为吸收液洗涤段。
本发明的技术方案如下：
一种醋酸乙烯生产过程乙烯回收方法， 采用吸收液和无离子水组成的双溶剂吸收法： 自 醋酸乙烯生产精镏工段的醋酸塔进料板上段引出流股作为吸收液， 由吸收液输送泵送至乙烯 回收塔下段顶部， 精制气由乙烯回收塔塔釜通入， 吸收液与精制气逆流接触； 吸收釜液送至 精镏工段处理， 气体继续上升至乙烯回收塔上段与塔顶部通入的无离子水逆流接触， 吸收脱 除其中的醋酸； 剩余的惰性气体由乙烯回收塔塔顶排出。
所述的吸收液来自醋酸乙烯生产精镏工段的醋酸塔进料板上段， 为乙酸、 醋酸乙烯及水 的混合物， 重量百分比为乙酸 50-85%、 醋酸乙烯 5-30%和水 5-20%。
本发明的醋酸乙烯生产过程乙烯回收方法的装置为： 醋酸乙烯生产精镏工段的醋酸塔进 料板上段与吸收液缓冲罐入口相连， 吸收液缓冲罐出口与吸收液输送泵入口相连， 吸收液输 送泵出口与乙烯回收塔下段相连。
所述的乙烯回收塔为复合塔， 乙烯回收塔分为上下两段， 上段为水洗段， 下段为吸收液 洗涤段。
所述的乙烯回收塔的操作压力为绝对压力 0.5-1.2MPa， 操作温度为 25-80°C。
本发明的醋酸乙烯生产过程乙烯回收方法， 其优点在于采用双溶剂吸收法， 从精镏工段 醋酸塔进料板上段引出流股作为吸收液， 结合醋酸乙烯对乙烯的高溶解特性及乙酸对乙烯的 高选择的溶解特性， 实现吸收液的加和增效功能， 选择性回收精制气中的乙烯气体， 减少乙 烯排放损失， 降低醋酸乙烯生产的原料消耗。
采用本发明的醋酸乙烯生产过程乙烯回收方法， 乙烯回收选择性为 60-95%， 减少了乙烯 的损失， 降低产品生产成本， 提高醋酸乙烯产品的市场竞争力。 附图说明
图 1 : 醋酸乙烯生产过程乙烯回收方法流程示意图。 具体实施方式
以下结合附图对本发明作进一步详细说明， 本发明的醋酸乙烯生产过程乙烯回收方法的 装置为： 醋酸乙烯生产精镏工段的醋酸塔进料板上段与吸收液缓冲罐入口相连， 吸收液缓冲 罐出口与吸收液输送泵入口相连， 吸收液输送泵出口与乙烯回收塔下段相连。 所述的乙烯回 收塔为复合塔， 乙烯回收塔分为上下两段， 上段为水洗段， 下段为吸收液洗涤段。 其中乙烯 回收塔的操作压力为绝对压力 0.5-1.2MPa， 操作温度为 25-80°C。
实施例 1 :
自精镏工段的醋酸塔 4进料板上段引出流股作为吸收液， 吸收液送至缓冲罐 1， 由吸收液 输送泵 2送至乙烯回收塔 3下段的顶部， 精制气由乙烯回收塔 3塔釜通入， 吸收液与精制气 在塔内逆流接触， 依据精制气在吸收液中的溶解特性， 实现对乙烯气体的选择性回收。 釜液 送至精镏工段进行脱气处理， 未被吸收的上升气体中主要含有 N2等惰性气体， 还含有少量醋 酸。 上升气体在乙烯回收塔上段与塔顶部通入的无离子水逆流接触， 吸收脱除其中的醋酸。 等惰性气体由乙烯回收塔塔顶排出， 防止了惰性气体的积累。 吸收液组成 （wt%) 为乙酸 78%, 醋酸乙烯 8%， 水 14%， 乙烯回收选择性为 90%。
实施例 2:
方法同实施例 1 ; 吸收液组成 （wt%) 为乙酸 85%， 醋酸乙烯 5%， 水 10%， 乙烯回收选 择性为 95%。
实施例 3:
方法同实施例 1 ; 吸收液组成（wt%) 为乙酸 50%， 醋酸乙烯 30%， 水 20%， 乙烯回收选 择性为 60%。
实施例 4:
方法同实施例 1 ; 吸收液组成 （wt%) 为乙酸 65%， 醋酸乙烯 30%， 水 5%， 乙烯回收选 择性为 70%。 本发明公开和提出的醋酸乙烯生产过程乙烯回收方法及装置， 本领域技术人员可通过借 鉴本文内容， 适当改变原料、 工艺参数、 结构设计等环节实现。 本发明的方法与技术已通过 较佳实施例子进行了描述， 相关技术人员明显能在不脱离本发明内容、 精神和范围内对本文 所述的方法和技术进行改动或适当变更与组合， 来实现本发明技术。 特别需要指出的是， 所 有相类似的替换和改动对本领域技术人员来说是显而易见的， 他们都被视为包括在本发明精 神、 范围和内容中。

Claims

权利要求
1. 一种醋酸乙烯生产过程乙烯回收方法，其特征是采用吸收液和无离子水组成的双溶 剂吸收法： 自醋酸乙烯生产精馏工段的醋酸塔进料板上段引出流股作为吸收液，由 吸收液输送泵送至乙烯回收塔下段顶部，精制气由乙烯回收塔塔釜通入， 吸收液与 精制气逆流接触； 吸收釜液送至精馏工段处理，气体继续上升至乙烯回收塔上段与 塔顶部通入的无离子水逆流接触， 吸收脱除其中的醋酸；剩余的惰性气体由乙烯回 收塔塔顶排出。
2. 如权利要求 1所述的乙烯回收方法，其特征是所述的吸收液来自醋酸乙烯生产精馏 工段的醋酸塔进料板上段， 为乙酸、 醋酸乙烯及水的混合物， 重量百分比为乙酸 50-85%、 醋酸乙烯 5-30%禾 B水 5-20%。
3. 一种醋酸乙烯生产过程乙烯回收方法的装置，其特征是醋酸乙烯生产精馏工段的醋 酸塔进料板上段与吸收液缓冲罐入口相连，吸收液缓冲罐出口与吸收液输送泵入口 相连， 吸收液输送泵出口与乙烯回收塔下段相连； 所述的乙烯回收塔为复合塔，乙 烯回收塔分为上下两段， 上段为水洗段， 下段为吸收液洗涤段。
4. 如权利要求 3所述的装置， 其特征是所述的乙烯回收塔的操作压力为绝对压力 0.5-1.2MPa, 操作温度为 25-80°C。
PCT/CN2012/084164 2011-11-11 2012-11-06 醋酸乙烯生产过程乙烯回收方法及装置 WO2013067918A1 (zh)

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