WO2014040473A1 - Use of tris(2-aminoethyl)amine as carbon dioxide absorbent - Google Patents

Use of tris(2-aminoethyl)amine as carbon dioxide absorbent Download PDF

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WO2014040473A1
WO2014040473A1 PCT/CN2013/081616 CN2013081616W WO2014040473A1 WO 2014040473 A1 WO2014040473 A1 WO 2014040473A1 CN 2013081616 W CN2013081616 W CN 2013081616W WO 2014040473 A1 WO2014040473 A1 WO 2014040473A1
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amine
carbon dioxide
aminoethyl
tris
absorption
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PCT/CN2013/081616
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French (fr)
Chinese (zh)
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梁志武
刘贺磊
那艳清
童柏栋
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湖南大学
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/103—Sulfur containing contaminants
    • 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
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • 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
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20415—Tri- or polyamines
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the present invention is in the field of carbon dioxide capture and separation, and specifically provides the use of tris(2-aminoethyl:)amine as a carbon dioxide absorber.
  • the organic amine compound absorption method appeared in the 1930s, and has become one of the main methods for industrial gas purification because of its advantages of faster absorption rate, larger absorption capacity, and lower economic cost.
  • the existing organic amine absorbent has a fast absorption rate, but a small absorption capacity and a high desorption energy consumption; or a slow absorption rate, a large absorption capacity, and a low desorption energy consumption.
  • primary amine MEA has a fast absorption rate, but its aqueous solution is easy to foam and degrade.
  • the product formed by the reaction of MEA and CO 2 is stable, the solution regeneration temperature is high, and the steam consumption is large; the carbamate corrosion Stronger, especially when C0 2 load is high.
  • the tertiary amine N-methyldiethanolamine (MDEA) is a tertiary alcohol amine. It has no active hydrogen atoms in the molecule, so it has good chemical stability and is not easy to degrade.
  • the MDEA aqueous solution has lower foaming tendency and corrosivity than primary amines.
  • MEA and secondary amine (DEA); form a metastable hydrogen carbamate with C0 2 , so regeneration is easy and energy consumption is low.
  • the MDEA solution reacts slowly with C0 2 and requires the addition of certain additives to increase its rate of absorption of C0 2 .
  • the disadvantage of sterically hindered amines compared to the amines commonly used in production is that the vapor pressure is high and the price is relatively high. Therefore, the existing organic amine solution cannot meet the high rate, high capacity, and low cost requirements of industrialization for absorbing solvents. Therefore, a new research trend in the field of co 2 capture has been developed for new solvents with high absorption rates, high capacity, and low desorption energy consumption.
  • the molecular formula of tris(2-aminoethyl:)amine is C 6 H 18 N 4 , which is currently mainly used in pharmaceutical intermediates, and other uses are unknown.
  • the present invention aims to provide a new use of tris(2-aminoethyl)amine, that is, the use of tris(2-aminoethyl)amine as a carbon dioxide absorber.
  • the tris(2-aminoethyl)amine proposed by the invention has better CO 2 absorption performance than the existing absorption solvent such as monoethanolamine (MEA); has a larger absorption capacity and is faster. Absorption rate.
  • Tris(2-aminoethyl:)amine (TAEAM® is a carbon dioxide absorber application.
  • Tris(2-aminoethyl:)amine (TAEAM® is a carbon dioxide absorber application, and tris(2-aminoethyl:)amine is formulated into an aqueous solution having a concentration of 0.5 mol/L to 4 mol/L as a carbon dioxide absorption liquid. And control the temperature of the carbon dioxide absorbing solution to be 20 ° C - 90 ° C.
  • the concentration of the carbon dioxide absorber is preferably from 1 mol/L to 3 mol/L, more preferably 2 mol/L.
  • the temperature of the carbon dioxide absorber is from 20 ° C to 60 ° C.
  • the pressure of the absorbed gas is 0.1-3 MPa.
  • the volume fraction of C0 2 in the absorbed gas is preferably 0.5% to 99%. More preferably, the volume fraction of C0 2 in the gas is 5% to 60%.
  • the principle of the present invention is:
  • the present invention utilizes tris(2-aminoethyl) (TAEA) having three primary amine nitrogen atoms and one tertiary amine nitrogen atom, and one nitrogen atom is bonded to three relatively large groups, having a certain The steric hindrance effect. Not only make up for the deficiency of a single organic amine solution, but also improve the absorption efficiency of C0 2
  • Tris(2-aminoethyl:) as a carbon dioxide absorber has a faster absorption rate, a larger absorption capacity, a higher cycle utilization rate, and a lower desorption energy consumption.
  • Figure 1 is a schematic diagram of the experimental apparatus for measuring the absorption capacity of 0 2 ; wherein 1 0 2 gas cylinder gas, 2 - N 2 gas cylinder, 3 - mass flow meter, 4 a valve, 5 - electric heater, 6 - saturation device, 7—reaction device, 8—temperature controller, 9-condenser, 10—constant water tank;
  • FIG 2 shows the CO 2 absorption capacity of an aqueous solution of tris(2-aminoethyl) (TAEA) at different C0 2 partial pressures.
  • Figure 3 C0 2 absorption capacity of aqueous solution of tris(2-aminoethyl) (TAEA) at different temperatures and monoethanolamine (MEA)
  • the device used is shown in Figure 1.
  • the saturation device and the reaction device are all placed in a constant temperature water tank.
  • Tris(2-aminoethyl)amine is formulated into a certain concentration of aqueous solution (0.5 mol/L to 4 mol/L) as a carbon dioxide absorption liquid.
  • N 2 , C0 2 gas from the cylinder through the pressure reducing valve, mass flow meter mixed into the saturation device for saturation is a certain degree of wetting of the gas to a certain saturated vapor pressure.
  • the saturated gas enters the reaction apparatus containing the absorption liquid, and is then condensed by the condenser and vented.
  • a temperature controller controlling the temperature (20 ° C-90 ° C ) of the absorption process, while using a mass flow meter and control ⁇ C0 2 ratio (i.e. the concentration of 0.023 gas is absorbed in the simulation).
  • the CO 2 capacity of TAEA was measured once every 1-2 hours with a 0 2 content analyzer in the liquid phase until the measured adjacent 0 2 capacities were the same or differed by ⁇ 0.05, at which time the reaction reached equilibrium and the absorption process was completed.
  • the tris(2-aminoethyl:)amine was formulated into an aqueous solution having a concentration of 2 mol/L as a carbon dioxide absorbing solution, and the volume fraction of C0 2 was controlled under a normal pressure of 0.1 MPa. 15% (ie, the partial pressure of C0 2 is 15 kPa), the relationship between the absorption capacity of TAEA and temperature is measured, and the absorption equilibrium is reached in 8-10 hours, compared with the absorption capacity of MEA under the same conditions, as shown in Fig. 3. .
  • FIG 3 is a C0 2 absorption capacity of the aqueous solution at different temperatures and TAEA C0 2 MEA solution absorption capacity compared to * MEA, so as TAEA. It can be seen from Fig. 3 that when TAEA is used as the CO 2 absorbent, it is feasible at 20 ° C to 90 ° C, and has a larger absorption capacity than MEA at different temperatures. And under the condition that the two reach the equilibrium of absorption, the absorption capacity of TAEA is large, and the absorption rate is fast.
  • Example 3 Investigation of absorbent concentration
  • the volume fraction of C0 2 is controlled to be 15% (that is, the partial pressure of 0 2 is 15 kPa), the temperature of the absorbent is 40 ° C, and different molar concentrations are prepared.
  • the aqueous solution of tris(2-aminoethyl)amine was used as a carbon dioxide absorbing solution: 0.5 mol/L, 1 mol/L, 2 mol/L, 3 mol/L, and 4 mol/L to measure the absorption capacity of TAEA.
  • the final result shows that the greater the concentration of TAEA in the carbon dioxide absorbing solution, the greater the 0 2 absorption capacity per unit volume of absorbing liquid.
  • the comprehensive economic factor is preferably 1 mol/L -3 mol/L, and more suitable at 2 mol/L under the other conditions mentioned above.
  • the tris(2-aminoethyl:)amine was formulated into an aqueous solution having a concentration of 2 mol/L as a carbon dioxide absorbing solution, and the temperature of the absorbent was controlled to be 40 ° C at a normal pressure of 0.1 MPa.
  • the relationship between the CO 2 absorption capacity of TAEA and the C0 2 partial pressure is measured, and compared with the CO 2 absorption capacity of the MEA under the same conditions, as shown in FIG. 2 .
  • Fig. 2 is a comparison of the CO 2 absorption capacity of the aqueous solution of TAEA under different partial pressures with the 0 2 absorption capacity of the MEA aqueous solution, which is the input of the country.
  • the TAEA absorbent can be applied to a wide C0 2 volume fraction (0.5%-99%, preferably 5%-60%), and at different C0 2 partial pressures, compared with MEA. Have a large suction

Abstract

Provided is use of tris(2-aminoethyl)amine as a carbon dioxide absorbent. Comparing with the existing absorbents (such as monoethanolamine), tris(2-aminoethyl)amine has a larger absorption capacity and a faster absorption rate.

Description

三 (2-氨乙基)胺作为二氧化碳吸收剂方面的应用 技术领域  Application of tris(2-aminoethyl)amine as carbon dioxide absorber
本发明属于二氧化碳捕获与分离领域， 具体提供了三 (2-氨乙基:)胺作为二 氧化碳吸收剂方面的应用。  The present invention is in the field of carbon dioxide capture and separation, and specifically provides the use of tris(2-aminoethyl:)amine as a carbon dioxide absorber.
背景技术 Background technique
近年来， 臭氧层的损耗、 温室效应的加剧和酸雨等全球性环境问题日趋严 重， 使人类环境与经济可持续发展面临着严峻的挑战。 特别是， 由大量化石燃 料燃烧导致排放的 co2增加引起的温室效应加剧是引起国际争论的全球性环境 污染热门课题， 因而减排问题引起了全球范围的广泛关注； 同时， co2又是一 种潜在的化学资源， 在工业生产中有非常重要的应用。 如何能够高效、 经济地 回收 co2 具有重要的经济和社会意义， 并已成为世界各国特别是发达国家十分 关注的问题。 In recent years, global environmental problems such as the depletion of the ozone layer, the intensification of the greenhouse effect, and acid rain have become increasingly serious, making the human environment and economic sustainable development facing severe challenges. In particular, the increase in greenhouse effect caused by the increase in co 2 emissions caused by the burning of large amounts of fossil fuels is a hot topic of global environmental pollution that has caused international controversy. Therefore, the issue of emission reduction has caused widespread concern worldwide; at the same time, co 2 is a A potential chemical resource has a very important application in industrial production. How to efficiently and economically recycle co 2 has important economic and social significance, and has become a matter of great concern to all countries in the world, especially developed countries.
有机胺化合物吸收法出现于 20世纪 30年代， 因其具有吸收速率较快、 吸收 容量较大、 经济成本较低等优点， 已成为工业气体净化的主要方法之一。  The organic amine compound absorption method appeared in the 1930s, and has become one of the main methods for industrial gas purification because of its advantages of faster absorption rate, larger absorption capacity, and lower economic cost.
而现有的有机胺吸收剂要么是吸收速率快， 但吸收容量小， 解吸耗能高； 要么是吸收速率慢， 吸收容量大， 解吸耗能低。 比如伯胺 MEA 吸收速率快， 但其水溶液容易发泡、 降解； MEA 与 C02 反应生成的产物氨基甲酸盐较稳 定， 溶液再生温度较高， 蒸汽耗量大； 氨基甲酸盐的腐蚀性较强， C02 负荷较 高时腐蚀尤为严重。 叔胺 N-甲基二乙醇胺 （MDEA) ， 是叔醇胺， 分子中不存 在活泼氢原子， 因而化学稳定性好， 不易降解变质； MDEA 水溶液的发泡倾 向和腐蚀性均低于伯胺 (MEA) 和仲胺 (DEA); 与 C02 生成亚稳定的氨基甲酸氢 盐， 故再生容易， 能耗低。 但是 MDEA 溶液与 C02 反应速率较慢， 需要加入 某些添加剂才能提高其吸收 C02 的速率。 空间位阻胺与生产上常用的胺相比， 其缺点是蒸汽压高， 价格较贵。 因此现有的有机胺溶液并不能够满足工业化对 吸收溶剂的高速率、 高容量、 低成本的要求。 因此， 开发出具有高吸收速率， 高容量， 低解吸能耗的新溶剂未来 co2捕 获领域的一大研究趋势。 However, the existing organic amine absorbent has a fast absorption rate, but a small absorption capacity and a high desorption energy consumption; or a slow absorption rate, a large absorption capacity, and a low desorption energy consumption. For example, primary amine MEA has a fast absorption rate, but its aqueous solution is easy to foam and degrade. The product formed by the reaction of MEA and CO 2 is stable, the solution regeneration temperature is high, and the steam consumption is large; the carbamate corrosion Stronger, especially when C0 2 load is high. The tertiary amine N-methyldiethanolamine (MDEA) is a tertiary alcohol amine. It has no active hydrogen atoms in the molecule, so it has good chemical stability and is not easy to degrade. The MDEA aqueous solution has lower foaming tendency and corrosivity than primary amines. MEA) and secondary amine (DEA); form a metastable hydrogen carbamate with C0 2 , so regeneration is easy and energy consumption is low. However, the MDEA solution reacts slowly with C0 2 and requires the addition of certain additives to increase its rate of absorption of C0 2 . The disadvantage of sterically hindered amines compared to the amines commonly used in production is that the vapor pressure is high and the price is relatively high. Therefore, the existing organic amine solution cannot meet the high rate, high capacity, and low cost requirements of industrialization for absorbing solvents. Therefore, a new research trend in the field of co 2 capture has been developed for new solvents with high absorption rates, high capacity, and low desorption energy consumption.
三 (2-氨乙基：)胺的分子式为 C6H18N4， 目前主要应用于医药中间体， 其它用 途不明。 The molecular formula of tris(2-aminoethyl:)amine is C 6 H 18 N 4 , which is currently mainly used in pharmaceutical intermediates, and other uses are unknown.
发明内容  Summary of the invention
针对现有技术的不足， 本发明旨在提供一种三 (2-氨乙基)胺的新用途， 也 就是三 (2-氨乙基)胺作为二氧化碳吸收剂方面的应用。 与现有的吸收溶剂相 比， 本发明提出的三 (2-氨乙基)胺吸收 C02性能优于现有的吸收溶剂如单乙醇 胺 （MEA); 具有较大的吸收容量， 较快的吸收速率。 In view of the deficiencies of the prior art, the present invention aims to provide a new use of tris(2-aminoethyl)amine, that is, the use of tris(2-aminoethyl)amine as a carbon dioxide absorber. Compared with the existing absorption solvent, the tris(2-aminoethyl)amine proposed by the invention has better CO 2 absorption performance than the existing absorption solvent such as monoethanolamine (MEA); has a larger absorption capacity and is faster. Absorption rate.
为实现上述目的， 本发明的技术方案是：  In order to achieve the above object, the technical solution of the present invention is:
三 (2-氨乙基：)胺 (TAEAM乍为二氧化碳吸收剂方面的应用。  Tris(2-aminoethyl:)amine (TAEAM® is a carbon dioxide absorber application.
三 (2-氨乙基：)胺 (TAEAM乍为二氧化碳吸收剂方面的应用， 将三 (2-氨乙基：)胺 配制成浓度为 0.5mol/L-4mol/L的水溶液作为二氧化碳吸收液， 并控制二氧化碳 吸收液的温度为 20°C-90°C。  Tris(2-aminoethyl:)amine (TAEAM® is a carbon dioxide absorber application, and tris(2-aminoethyl:)amine is formulated into an aqueous solution having a concentration of 0.5 mol/L to 4 mol/L as a carbon dioxide absorption liquid. And control the temperature of the carbon dioxide absorbing solution to be 20 ° C - 90 ° C.
所述二氧化碳吸收剂的浓度优先为 lmol/L-3 mol/L, 更优选为 2mol/L。  The concentration of the carbon dioxide absorber is preferably from 1 mol/L to 3 mol/L, more preferably 2 mol/L.
所述二氧化碳吸收剂的温度为 20°C-60°C。  The temperature of the carbon dioxide absorber is from 20 ° C to 60 ° C.
其中， 被吸收的气体压力为 0.1-3MPa。 被吸收气体中 C02的体积分数优先为 0.5%-99%。， 更优为所述气体中 C02的体积分数为 5%-60%。 Among them, the pressure of the absorbed gas is 0.1-3 MPa. The volume fraction of C0 2 in the absorbed gas is preferably 0.5% to 99%. More preferably, the volume fraction of C0 2 in the gas is 5% to 60%.
本发明的原理是： 本发明利用三 (2-氨乙基） （TAEA) 具有三个伯胺氮原子 和一个叔胺氮原子， 而且一个氮原子上连接了三个比较大基团， 具有一定的空 间位阻效应。 不但弥补了单一的有机胺溶液的不足， 同时会提高 C02吸收效 The principle of the present invention is: The present invention utilizes tris(2-aminoethyl) (TAEA) having three primary amine nitrogen atoms and one tertiary amine nitrogen atom, and one nitrogen atom is bonded to three relatively large groups, having a certain The steric hindrance effect. Not only make up for the deficiency of a single organic amine solution, but also improve the absorption efficiency of C0 2
与现有技术相比， 本发明的优势在于： The advantages of the present invention over the prior art are:
三 (2-氨乙基：)作为二氧化碳吸收剂具有较快的吸收速率， 较大的吸收容量， 较高的循环利用率， 较低的解吸能耗。  Tris(2-aminoethyl:) as a carbon dioxide absorber has a faster absorption rate, a larger absorption capacity, a higher cycle utilization rate, and a lower desorption energy consumption.
附图说明  DRAWINGS
图 1是 02吸收容量测定的实验装置图； 其中 1一 02气体钢瓶气体， 2— N2气钢瓶， 3—质量流量计， 4一阀门， 5—电加热器， 6—饱和装置， 7—反应 装置， 8—控温仪， 9一冷凝器， 10—恒温水槽； Figure 1 is a schematic diagram of the experimental apparatus for measuring the absorption capacity of 0 2 ; wherein 1 0 2 gas cylinder gas, 2 - N 2 gas cylinder, 3 - mass flow meter, 4 a valve, 5 - electric heater, 6 - saturation device, 7—reaction device, 8—temperature controller, 9-condenser, 10—constant water tank;
图 2为不同 C02分压下三 (2-氨乙基） （TAEA) 的水溶液的 C02吸收容量与 单乙醇胺 （MEA) 水溶液的 C02吸收容量对比； 为^^ ， 國为 1 £ ； 图 3不同温度下三 (2-氨乙基） （TAEA) 的水溶液的 C02吸收容量与单乙醇 胺 （MEA) 水溶液的 C02吸收容量对比； *为^^ ， 令为1 。 下面结合具体实施方式， 对本发明做进一步的解释和发明， 但本发明并不 限于实施例所述的范围。 Figure 2 shows the CO 2 absorption capacity of an aqueous solution of tris(2-aminoethyl) (TAEA) at different C0 2 partial pressures. Comparison of C0 2 absorption capacity of monoethanolamine (MEA) aqueous solution; ^^, country 1 £; Figure 3 C0 2 absorption capacity of aqueous solution of tris(2-aminoethyl) (TAEA) at different temperatures and monoethanolamine (MEA) The comparison of the C0 2 absorption capacity of the aqueous solution; * is ^^, and the order is 1. The invention is further explained and invented with reference to the specific embodiments, but the invention is not limited to the scope of the embodiments.
实施例 1 : 实验过程  Example 1 : Experimental procedure
所用装置如图 1所示。 其中饱和装置和反应装置均放入恒温水槽中。 将三 (2-氨乙基)胺配制成一定浓度的水溶液 （0.5mol/L-4mol/L) 作为二氧化碳吸收 液。  The device used is shown in Figure 1. The saturation device and the reaction device are all placed in a constant temperature water tank. Tris(2-aminoethyl)amine is formulated into a certain concentration of aqueous solution (0.5 mol/L to 4 mol/L) as a carbon dioxide absorption liquid.
具体实验过程： N2， C02气体由钢瓶依次经减压阀、 质量流量计混合后进 入饱和装置进行饱和 （是将气体进行一定的润湿， 达到一定的饱和蒸汽压） 。 饱和之后的气体进入装有吸收液的反应装置， 之后经过冷凝器冷凝后放空。 通 过控温仪控制吸收过程的温度 （20°C-90°C ) ， 同时利用质量流量计来控制 C02 与^的配比 （也就是模拟被吸收的气体中。02的浓度） 。 每隔 1-2小时用液相中 02含量分析装置测量一次 TAEA的 C02容量， 直到测得的相邻的 02容量相同 或者相差 ±0.05， 此时反应达到平衡， 完成吸收过程。 The specific experimental process: N 2 , C0 2 gas from the cylinder through the pressure reducing valve, mass flow meter mixed into the saturation device for saturation (is a certain degree of wetting of the gas to a certain saturated vapor pressure). The saturated gas enters the reaction apparatus containing the absorption liquid, and is then condensed by the condenser and vented. By a temperature controller controlling the temperature (20 ° C-90 ° C ) of the absorption process, while using a mass flow meter and control ^ C0 2 ratio (i.e. the concentration of 0.023 gas is absorbed in the simulation). The CO 2 capacity of TAEA was measured once every 1-2 hours with a 0 2 content analyzer in the liquid phase until the measured adjacent 0 2 capacities were the same or differed by ± 0.05, at which time the reaction reached equilibrium and the absorption process was completed.
实施例 2: 吸收剂温度考察  Example 2: Investigation of absorbent temperature
用实施例 1 所述的方法， 将三 (2-氨乙基：)胺配制成浓度为 2mol/L 的水溶 液作为二氧化碳吸收液， 在常压 O.lMPa的条件下， 控制 C02体积分数为 15% (即 C02的分压为 15kPa)， 测量 TAEA 的吸收容量与温度之间的关系， 8-10 小时达到吸收平衡， 与相同条件下的 MEA的吸收容量的对比， 如图 3所示。 Using the method described in Example 1, the tris(2-aminoethyl:)amine was formulated into an aqueous solution having a concentration of 2 mol/L as a carbon dioxide absorbing solution, and the volume fraction of C0 2 was controlled under a normal pressure of 0.1 MPa. 15% (ie, the partial pressure of C0 2 is 15 kPa), the relationship between the absorption capacity of TAEA and temperature is measured, and the absorption equilibrium is reached in 8-10 hours, compared with the absorption capacity of MEA under the same conditions, as shown in Fig. 3. .
图 3为不同温度下 TAEA的水溶液的 C02吸收容量与 MEA水溶液的 C02 吸收容量对比， *为 MEA, 令为 TAEA。 由图 3可见， TAEA作为 C02吸收剂 时， 在 20°C-90°C下均是可行的， 且在不同的温度下， 与 MEA相比都具有较大 的吸收容量。 且在两者达到吸收平衡的时间差不多的条件下， TAEA 的吸收容 量大， 可见其吸收速率快。 实施例 3: 吸收剂浓度考察 FIG 3 is a C0 2 absorption capacity of the aqueous solution at different temperatures and TAEA C0 2 MEA solution absorption capacity compared to * MEA, so as TAEA. It can be seen from Fig. 3 that when TAEA is used as the CO 2 absorbent, it is feasible at 20 ° C to 90 ° C, and has a larger absorption capacity than MEA at different temperatures. And under the condition that the two reach the equilibrium of absorption, the absorption capacity of TAEA is large, and the absorption rate is fast. Example 3: Investigation of absorbent concentration
用实施例 1所述的方法， 在常压 O.lMPa的条件下， 控制 C02体积分数为 15% (即 02的分压为 15kPa)， 吸收剂温度为 40°C， 配制不同摩尔浓度的三 (2-氨乙基)胺水溶液作为二氧化碳吸收液： 0.5 mol/L , lmol/L , 2mol/L， 3mol/L， 4mol/L测量 TAEA的吸收容量。 最终结果显示， 二氧化碳吸收液中的 TAEA 浓度越大， 单位体积吸收液的 02吸收容量增加。 综合经济因素， 以 lmol/L -3mol/L较为适宜， 其中在上述其它条件下， 以 2mol/L更为适合。 Using the method described in Example 1, under the condition of normal pressure O.lMPa, the volume fraction of C0 2 is controlled to be 15% (that is, the partial pressure of 0 2 is 15 kPa), the temperature of the absorbent is 40 ° C, and different molar concentrations are prepared. The aqueous solution of tris(2-aminoethyl)amine was used as a carbon dioxide absorbing solution: 0.5 mol/L, 1 mol/L, 2 mol/L, 3 mol/L, and 4 mol/L to measure the absorption capacity of TAEA. The final result shows that the greater the concentration of TAEA in the carbon dioxide absorbing solution, the greater the 0 2 absorption capacity per unit volume of absorbing liquid. The comprehensive economic factor is preferably 1 mol/L -3 mol/L, and more suitable at 2 mol/L under the other conditions mentioned above.
实施例 4: 被吸收气体中 02分压考察 Example 4: Investigation of 0 2 partial pressure in absorbed gas
用实施例 1所述的方法， 将三 (2-氨乙基：)胺配制成浓度为 2mol/L的水溶液 作为二氧化碳吸收液， 控制吸收剂的温度为 40°C， 在常压 O.lMPa 下， 测量 TAEA 的 C02吸收容量与 C02分压之间的关系， 并与相同条件下的 MEA 的 C02吸收容量的对比， 如图 2所示。 图 2为不同分压下 TAEA的水溶液的 C02 吸收容量与 MEA水溶液的 02吸收容量对比， 为^^入， 國为 1入£入。 Using the method described in Example 1, the tris(2-aminoethyl:)amine was formulated into an aqueous solution having a concentration of 2 mol/L as a carbon dioxide absorbing solution, and the temperature of the absorbent was controlled to be 40 ° C at a normal pressure of 0.1 MPa. Next, the relationship between the CO 2 absorption capacity of TAEA and the C0 2 partial pressure is measured, and compared with the CO 2 absorption capacity of the MEA under the same conditions, as shown in FIG. 2 . Fig. 2 is a comparison of the CO 2 absorption capacity of the aqueous solution of TAEA under different partial pressures with the 0 2 absorption capacity of the MEA aqueous solution, which is the input of the country.
由图 2可见， TAEA吸收剂可以适用于较宽的 C02体积分数 （0.5%-99%均可 行， 优选 5%-60%)， 且在不同的 C02分压的下， 与 MEA相比都具有较大的吸 As can be seen from Figure 2, the TAEA absorbent can be applied to a wide C0 2 volume fraction (0.5%-99%, preferably 5%-60%), and at different C0 2 partial pressures, compared with MEA. Have a large suction

Claims

权 利 要 求 Rights request
1. 三（2-氨乙基）胺作为二氧化碳吸收剂方面的应用。 1. Tris(2-aminoethyl)amine as a carbon dioxide absorber.
2. 根据权利要求 1所述三（2-氨乙基)胺作为二氧化碳吸收剂方面的应用， 其特征是，将三（2-氨乙基）胺配制成浓度为 0. 5mol/L-4mol/L的水溶液作 为二氧化碳吸收液， 并控制二氧化碳吸收液的温度为 20°C-90°C。  5摩尔/L-4摩尔。 The concentration of 0. 5mol / L - 4mol, the concentration of 0. 5mol / L - 4mol The aqueous solution of /L is used as the carbon dioxide absorbing liquid, and the temperature of the carbon dioxide absorbing liquid is controlled to be 20 ° C to 90 ° C.
3. 根据权利要求 2所述应用， 其特征是， 所述二氧化碳吸收液中三（2-氨乙 基）胺的浓度为 lmol/L- 3 mol/Lo  3. The use according to claim 2, wherein the concentration of tris(2-aminoethyl)amine in the carbon dioxide absorbing solution is 1 mol/L - 3 mol/Lo
4. 根据权利要求 2所述应用， 其特征是， 所述二氧化碳吸收液中三（2-氨乙 基）胺的浓度为 2mol/L。  The use according to claim 2, wherein the concentration of tris(2-aminoethyl)amine in the carbon dioxide absorbing liquid is 2 mol/L.
5. 根据权利要求 2所述应用， 其特征是， 所述二氧化碳吸收液的温度为 20°C-60°C。  The use according to claim 2, characterized in that the temperature of the carbon dioxide absorbing liquid is from 20 ° C to 60 ° C.
6. 根据权利要求 1所述应用，其特征是，被吸收的气体压力为 0. l-3MPa。 l-3MPa。 The application of the gas is 0. l-3MPa.
7. 根据权利要求 6所述应用， 其特征是， 所述气体中 C02的体积分数为 0. 5%- 99%。 5%至99%。 The volume fraction of C0 2 in the gas is from 0.5% to 99%.
8. 根据权利要求 6所述应用， 其特征是， 所述气体中 C02的体积分数为 5%— 60%。 8. The use according to claim 6, characterized in that the volume fraction of C0 2 in the gas is from 5% to 60%.
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