CN113926290A - CO2Phase change absorption system of - Google Patents

CO2Phase change absorption system of Download PDF

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Publication number
CN113926290A
CN113926290A CN202010611225.6A CN202010611225A CN113926290A CN 113926290 A CN113926290 A CN 113926290A CN 202010611225 A CN202010611225 A CN 202010611225A CN 113926290 A CN113926290 A CN 113926290A
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phase change
absorption system
change absorption
absorption
mass
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CN113926290B (en
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陆诗建
李清方
李孟杰
刘建武
张新军
刘海丽
王翀
史林青
林名桢
江克金
毛彦辉
陆胤君
陈宏福
范振宁
梁海宁
于惠娟
刘海燕
柳亭
闫广宏
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China Petrochemical Corp
Sinopec Oilfield Service Corp
Sinopec Petroleum Engineering Corp
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Sinopec Petroleum Engineering Corp
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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
    • B01D53/1456—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
    • B01D2252/2041—Diamines
    • 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

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  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
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Abstract

The invention discloses CO2The phase change absorption system comprises the following components in percentage by mass: a base fluid comprising: hydroxyethyl ethylenediamine and tetraethylenepentamine, 15 wt.% to 25 wt.%; a delaminating agent comprising: ethyl ethylene diamine and 1, 4-butanediamine, 5 wt.% to 10 wt.%; an activator, comprising: piperazine or diethanolamine, 1 wt.% to 5 wt.%; nanoparticles, 0.01 wt.% to 0.08 wt.%; and, the balance water. The phase change absorption system of the invention is used for absorbing CO2Has high absorption load and absorption/desorption rate, and can alleviate solvent loss caused by regeneration heating.

Description

CO2Phase change absorption system of
Technical Field
The invention relates to CO2In particular, to a chemical absorbent having a high CO content2Supported amount of CO2The phase change absorption system of (1).
Background
At present, CO is captured by low partial pressure flue gas2Method (2)There are chemical absorption, physical adsorption and membrane separation methods, but the chemical absorption method is undoubtedly the best choice at present in terms of application time, technical maturity and prospect. The chemical absorption method is to selectively mix CO in the flue gas with the absorbent2Chemical reaction to realize CO2Separated from other gases and regenerated by means of the reverse reaction of this reaction, releasing high-purity CO2And (4) carrying out enrichment. The reaction principle is that weak base and weak acid react to form water soluble salt which absorbs or releases CO2Is controlled by the chemical reaction equilibrium. However, the most important bottleneck limiting the large-scale application of the chemical absorption method is that the energy consumption is large and the wood formation is high. In order to reduce energy consumption, researchers have developed new phase change absorbents.
The hot point of research on phase change absorbents at present is focused on absorption systems (first type of phase change absorption systems) which are layered after absorption and absorption systems (second type of phase change absorption systems) which are layered after desorption. For the second type of phase-change absorption system, the current main method is to add an extracting agent to extract organic amine in the rich solution to promote CO2The compounds formed by the reaction decompose to CO2Quickly released, reduced regeneration temperature and full utilization of low-grade steam. From a technological point of view, the process is basically consistent with a typical chemical absorption process, but the process needs to add an extracting agent for extracting the organic amine before regeneration.
Researchers at the reaction engineering institute of Dotmond university of Germany constructed a series of phase change absorbents for CO using various lipophilic amine reagents2They found that the lipophilic amine solution absorbs CO2The solution is homogeneous, during regeneration, the regenerated lipophilic amine forms an organic phase above the solution, and the regenerated amine is continuously extracted from the lower layer solution, so that the chemical balance during regeneration is broken, and the reaction is pushed to proceed towards the regeneration direction. Such absorbents can use low heating or waste heat to achieve CO due to self-extraction during regeneration2The desorption greatly reduces the regeneration energy consumption of the amine absorbent. The researchers further found that the addition of an activator to a lipophilic amine phase change absorbent promotes CO2Is suckedAnd (6) harvesting. As described by the university of zhejiang's king mingxi activation of lipophilic amines 2, 2-Dimethylcyclopropanecarboxamide (DMCA) and di-sec-butylamine (DSBA) with two activators, N-Methylcyclohexylamine (MCA) and Piperazine (PZ), found that 15 wt.% DMCA +15 wt.% MCA, 25 wt.% DMCA +25 wt.% PZ and 15 wt.% DSBA +15 wt.% MCA had good CO2Trapping performance, where the absorption rate of 15 wt.% DMCA +15 wt.% MCA is comparable to a 30 wt.% ethanolamine (MEA) solution and the regeneration efficiency is 69% higher than 30 wt.% MEA. The regeneration energy consumption of the absorbent is evaluated by a simple regeneration tower model, and the regeneration energy consumption can be reduced to 2.48GJ/ton CO after the activator is added2The regeneration energy consumption is 36% lower than that of 30 wt.% MEA. However, the phase change absorbents containing lipophilic amine solutions are ubiquitous with CO2The loading capacity is low, and the lipophilic amine liquid is easy to volatilize and lose.
Disclosure of Invention
Aiming at CO in the prior art2CO in phase change absorption system2The invention provides a CO with low load capacity2The phase change absorption system comprises the following components in percentage by mass:
a base fluid comprising: hydroxyethyl ethylenediamine and tetraethylenepentamine, 15 wt.% to 25 wt.%;
a delaminating agent comprising: ethyl ethylene diamine and 1, 4-butanediamine, 5 wt.% to 10 wt.%;
an activator, comprising: piperazine or diethanolamine, 1 wt.% to 5 wt.%;
nanoparticles, 0.01 wt.% to 0.08 wt.%;
the balance of water.
In some embodiments, the composition further comprises, in mass fraction: 0.025 wt.% to 0.05 wt.% of corrosion inhibitor; and/or, antioxidant 0.025 wt.% to 0.05 wt.%.
In some embodiments, the corrosion inhibitor comprises: imidazoline benzoate-dimethyl sulfate quaternary ammonium salt, or imidazoline benzoate-methyl chloride quaternary ammonium salt; the antioxidant includes: carbohydrazide, or pyrogallol.
In some embodiments, the mass ratio of hydroxyethylethylenediamine to tetraethylenepentamine is between 4:1 and 1: 1.
In some embodiments, the mass ratio of ethylethylenediamine to 1, 4-butanediamine is between 4:1 and 1: 2.
In some embodiments, the sum of the mass amounts of base fluid, delaminating agent and activating agent is 30 wt.%.
In some embodiments, the nanoparticles have a particle size ranging from 5 to 14 nm.
In some embodiments, the nanoparticles are metal oxides.
In some embodiments, the metal oxide comprises Fe2O3、Fe3O4MgO, ZnO or CuO.
In some embodiments, the metal oxide is present in an amount between 0.04 wt.% and 0.05 wt.%.
The invention has the beneficial technical effects that: CO of the invention2In the phase-change absorption system, the para-CO is added2The absorption of the base liquids AEEA and TETA has rapid reaction and good absorption selectivity, the content of the base liquids AEEA and TETA reaches 15 wt.% to 25 wt.%, and the phase change absorption system can ensure that the phase change absorption system of the invention can absorb CO2Has high absorption load and absorption/desorption rate; meanwhile, AEEA and TETA have higher boiling points (the boiling points under normal pressure are 240 ℃ and 340 ℃) respectively, and the two base liquid components are not easy to volatilize under the regeneration temperature (< 100 ℃), so that the solvent loss caused by regeneration heating can be relieved.
Drawings
FIG. 1 CO of the present invention2Application of phase change absorption system in absorbing CO from coal-fired flue gas2Schematic diagram of the simulation test device.
Symbolic illustration in the drawings:
100 of flue gas;
200 of a decarbonizing gas;
1, an absorption tower;
2, a regeneration tower;
3, a lean-rich liquid heat exchanger;
4 an absorption heat pump system;
5, a flash tower;
61. 62 a rich liquid pump;
63 a barren liquor pump;
7, a dehydrator;
8 CO2a storage tank;
9 lean liquid cooler.
Detailed Description
Example 1
This example provides a CO2The phase change absorption system comprises the following components in percentage by mass:
a base fluid comprising: hydroxyethylethylenediamine (AEEA) and tetraethylenepentamine (TETA), 15 wt.% to 25 wt.%;
a delaminating agent comprising: ethyl ethylene diamine (N-ELDE) and 1, 4-butanediamine (TETA), 5 wt.% to 10 wt.%;
an activator, comprising: piperazine (PZ) or Diethanolamine (DEA), 1 wt.% to 5 wt.%;
nanoparticles, 0.01 wt.% to 0.08 wt.%;
the balance of water.
In some embodiments, the CO of the present invention2The phase change absorption system further comprises the following components in percentage by mass: 0.025 wt.% to 0.05 wt.% of corrosion inhibitor; and/or, antioxidant 0.025 wt.% to 0.05 wt.%. Wherein corrosion inhibitors are used to reduce the CO of the present invention2The corrosivity of the phase change absorption system to steel (reactors, heat exchange equipment, various storage tanks, pipelines and the like); antioxidants are used to reduce thermal and oxidative degradation of the base fluid, delaminating agents and activators, ensuring the CO of the present invention2Stability of the phase change absorber system throughout the process cycle.
In some embodiments, the CO of the present invention2The corrosion inhibitor in the phase change absorption system is selected from benzoic acid imidazoline-dimethyl sulfate quaternary ammonium salt (IBDSQAS) or benzoic acid imidazoline-chloromethane quaternary ammonium salt (ICQAB).
In some embodiments, the CO of the present invention2The antioxidant in the phase change absorption system is Carbohydrazide (CD) or pyrogallol (OTP).
In some embodiments, the base fluid has a mass ratio of hydroxyethylethylenediamine (AEEA) to tetraethylenepentamine (TETA) between 4:1 and 1: 1.
In some embodiments, the mass ratio of the ingredients ethylethylenediamine (N-ELDE) to 1, 4-butanediamine (TETA) of the base layering agent is between 4:1 and 1: 2.
In some embodiments, the CO of the present invention2The nanoparticles in the phase-change absorption system are preferably metal oxides, and the nanoparticles of the metal oxides have stable performance, rich raw materials and easy preparation.
In some embodiments, the nanoparticles preferably have a particle size of 5 to 14 nm.
In some embodiments, the nanoparticles of metal oxide comprise: fe2O3、Fe3O4MgO, ZnO or CuO.
CO of the invention2The content of the base liquid in the phase change absorption system is at most 15-25 wt.%, and the component of the base liquid is selected to CO2The absorption has AEEA and TETA with rapid reaction and good absorption selectivity, wherein the TETA has good CO2Adsorption performance, while AEEA shows better CO2The desorption performance, the base liquid formed by matching the two amine liquids can ensure that the phase change absorption system of the invention can absorb CO2With absorption loading and absorption/desorption rates. Meanwhile, AEEA and TETA have higher boiling points (the boiling points under normal pressure are 240 ℃ and 340 ℃) respectively, and the two base liquid components are not easy to volatilize under the regeneration temperature (< 100 ℃), so that the solvent loss caused by regeneration heating can be relieved.
CO of the invention2In the components of the phase-change absorption system, the layering agent forms organic phase layering above the solution during regeneration, regenerated amine can be continuously extracted from the lower-layer solution, the chemical balance during regeneration is broken, the reaction is promoted to be carried out in the regeneration direction, and the autonomous self-extraction of the organic phase is realized.
CO of the invention2In the components of the phase-change absorption system, the activator is used for improving the absorption of CO by the absorption system2Reaction rate and desorption of CO2The rate of reaction.
CO of the invention2Among the components of the phase-change absorption system, the nano particles are used for strengthening mass transfer and improving CO2And increase the mass transfer absorption load. Selecting metal oxide nanoparticles as the nanoparticles of the metal oxideStable performance, rich raw materials and easy preparation.
Optimization experiments show that the content of the nanoparticles influences the mass transfer enhancement effect, because when the content of the nanoparticles in the solution is less than a certain proportion, the nanoparticles are distributed in the solution more uniformly to form a series of dispersed active centers. Because the nano particles have large specific surface area, micro-vortex is formed when fluid passes through the nano particles, the reduction of the thickness of a gas-liquid reaction liquid film and the rapid surface updating are realized on the surfaces of the particles, and the mass transfer rate is increased. When the content of the nano particles in the solution is more than a certain proportion, the nano particles collide with each other in the fluid and are agglomerated under the action of chemical bond force and Van der Waals attractive force to form the nano large particles, so that the effect of self-enhanced mass transfer is reduced. CO of the invention2In the phase change absorption system, the preferable content of the nanoparticles is 0.01 wt.% to 0.08 wt.%, and when the particle size of the nanoparticles is selected to be in the range of 5 to 14nm, the preferable content is 0.04 wt.% to 0.05 wt.%.
Example 2
Table 1 shows the CO of the present invention2Exemplary formulations of phase change absorbing systems, it should be understood that the formulations are given merely to illustrate the technical content of the present invention, which is not limited to the specific formulations exemplified.
TABLE 1 CO of the invention2Exemplary formulations of phase change absorbing systems
Figure BDA0002560976840000051
Example 3
This example illustrates the CO of the present invention2Application of phase change absorption system in absorbing CO from coal-fired flue gas2The test apparatus is shown in fig. 1, and the test method is as follows:
after the flow of the coal-fired flue gas (simulated flue gas) is adjusted by a flow adjusting valve, alkali washing and water washing are firstly carried out; the flue gas 100 enters from the bottom of the absorption tower 1 after being pretreated, and is uniformly distributed and ascended after passing through a gas distributor at the bottom of the absorption tower 1, and the CO in the invention2Phase change absorption system (lean)Liquid) absorption of CO2Hereinafter referred to as rich liquor. CO removal2The residual gas enters the cyclone separator through the top of the absorption tower 1 to realize the separation of gas phase and liquid phase, and the decarbonized gas 200 is discharged from the top of the separator. The rich solution enters the absorption heat pump system 4 for heating through the lean and rich solution heat exchanger 3 by the rich solution pump 61. After being heated, the rich liquid respectively reaches the regeneration tower 2 from the middle part and the upper part of the regeneration tower 2 through the adjustment of a rich liquid pump 62, and the rich liquid starts to be regenerated in the regeneration tower 2. The regenerated gas is cooled by a water cooler from the top of the tower, reaches a cyclone separator for separation, is discharged from the top, is treated by a dehydrator 7, and then is introduced with CO2 A storage tank 8. The lean solution obtained after regeneration is sent to a flash tower 5 for flash evaporation, the obtained steam returns to the bottom of a regeneration tower 2, and a reboiler 21 provides heat for the solution regeneration process in the tower; the barren solution after flash evaporation is discharged from the bottom of the flash tower 5, is sent to the absorption heat pump system 4 after passing through the barren and rich solution heat exchanger 3, is cooled through the barren solution cooler 9, and the barren solution after cooling is adjusted by a barren solution pump 63 to return to the top of the absorption tower 1, so that the CO in the invention2The phase change absorption system realizes cyclic regeneration.
Wherein the volume fraction of the components of the simulated smoke is CO215％、N280% and O 25 percent. The specification parameters of the absorption tower and the regeneration tower are shown in table 2, and the test operation parameters are shown in table 3:
TABLE 2 specification parameters of absorption and regeneration towers
Figure BDA0002560976840000061
TABLE 3 test run parameters
Figure BDA0002560976840000062
The above-described test apparatus and test method were used to test CO of the present invention, which is listed in example 3 and is numbered from 1 to 102Formulations of phase change absorption systems were tested to illustrate the CO of the present invention2The effective mass concentration of the phase change absorption system is 30 wt% (the effective mass concentration is base liquid + layering agent +)The mass concentration of the activating agent), wherein the particle size of the selected CuO or MgO is in the range of 5-14 nm, and the test results are shown in Table 4:
TABLE 4 CO of the invention2Results of absorption/regeneration test of phase change absorption system
Figure BDA0002560976840000071
As can be seen from the test results in Table 4, the CO of the present invention2The phase-change absorber is under the condition of regeneration temperature of 98-99 ℃, and the loading capacity of the rich solution is 52-54 LCO2the/L solution is higher than the rich solution load (30-35 LCO) of the common absorbent in the industry at present2the/L solution) with the lean solution load of 18-21 LCO2The solution is L solution, which shows that the components of the base liquid, AEEA and TETA, can ensure that the phase change absorption system of the invention can absorb CO2With high absorption load and absorption/desorption rates, examples of CO according to the invention2The regeneration energy consumption of the phase change absorption system is 2.39-2.54 GJ/tCO2The regeneration energy consumption is about 40 percent lower than that of 30 wt.% MEA commonly used in industry, and the regeneration energy consumption reaches a value close to or even lower than that of the two-phase absorbent reported at present. Meanwhile, the base liquid components AEEA and TETA have higher boiling points (the boiling points under normal pressure are 240 ℃ and 340 ℃ respectively), and the two base liquid components are not easy to volatilize at the regeneration temperature, so that the solvent loss caused by regeneration heating can be relieved, the extra cost increased by solvent supplement can be further reduced, and the environmental pollution caused by volatilization of an organic solvent can be reduced.
CO of the invention2The phase change absorption system contains nano particles, and the CO in the invention is subjected to mass transfer enhancement by the nano particles2In the regeneration process, the phase change absorber system does not need to be additionally provided with equipment such as ultrasound, stirring and the like, so that the equipment investment is reduced, the regeneration process is simplified, and the regeneration energy consumption can be reduced.
In conclusion, through test optimization and screening, the invention provides CO with excellent comprehensive performance2Phase change absorption System, CO of the present invention2Phase change absorption system to CO2Has high absorption negativityLoading and absorption/desorption rate, low regeneration energy consumption, easily obtained raw material components, low price, cost advantage when applied to chemical production and industrial practicability.
The above-mentioned embodiments are merely preferred embodiments for fully illustrating the present invention, and the scope of the present invention is not limited thereto. The equivalent substitution or change made by the technical personnel in the technical field on the basis of the invention is all within the protection scope of the invention.

Claims (10)

1. CO (carbon monoxide)2The phase change absorption system is characterized by comprising the following components in percentage by mass:
a base fluid comprising: hydroxyethyl ethylenediamine and tetraethylenepentamine, 15 wt.% to 25 wt.%;
a delaminating agent comprising: ethyl ethylene diamine and 1, 4-butanediamine, 5 wt.% to 10 wt.%;
an activator, comprising: piperazine or diethanolamine, 1 wt.% to 5 wt.%;
nanoparticles, 0.01 wt.% to 0.08 wt.%;
the balance of water.
2. The CO of claim 12The phase change absorption system is characterized by further comprising the following components in percentage by mass: 0.025 wt.% to 0.05 wt.% of corrosion inhibitor; and/or, antioxidant 0.025 wt.% to 0.05 wt.%.
3. CO according to claim 22The phase change absorption system of (1), wherein the corrosion inhibitor comprises: imidazoline benzoate-dimethyl sulfate quaternary ammonium salt, or imidazoline benzoate-methyl chloride quaternary ammonium salt; the antioxidant comprises: carbohydrazide, or pyrogallol.
4. The CO of claim 12The phase change absorption system is characterized in that the mass ratio of the hydroxyethyl ethylenediamine to the tetraethylenepentamine is between 4:1 and 1: 1.
5. The CO of claim 12The phase change absorption system is characterized in that the mass ratio of the ethyl ethylenediamine to the 1, 4-butanediamine is between 4:1 and 1: 2.
6. The CO of claim 12Characterized in that the sum of the mass contents of the base liquid, the delaminating agent and the activating agent is 30 wt.%.
7. The CO of claim 12The phase change absorption system is characterized in that the particle size range of the nano particles is between 5 and 14 nm.
8. The CO of any one of claims 1 to 72The phase change absorption system of (1), wherein the nanoparticles are metal oxides.
9. The CO of claim 82Wherein the metal oxide comprises Fe2O3、Fe3O4MgO, ZnO or CuO.
10. The CO of claim 92The phase change absorption system of (1), wherein the mass content of the metal oxide is between 0.04 wt.% and 0.05 wt.%.
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114405258A (en) * 2021-12-28 2022-04-29 中国矿业大学 Is suitable for low partial pressure CO2Capture purified absorbent system

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1519951A1 (en) * 1964-07-01 1969-06-26 Brown Boveri Krupp Reaktor Device for cleaning a gas stream from CO2
CN109012090A (en) * 2018-07-30 2018-12-18 大连理工大学 It is a kind of can oxidation resistant non-aqueous decarbonizing solution for trap carbon dioxide in gas mixture
CN109331610A (en) * 2018-12-14 2019-02-15 中石化石油工程技术服务有限公司 Trap CO in exhaust gas2Phase transformation absorbent
WO2020063557A1 (en) * 2018-09-25 2020-04-02 天津工业大学 Low energy consumption anhydrous co2 phase change absorption agent, and regeneration method and application thereof

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1519951A1 (en) * 1964-07-01 1969-06-26 Brown Boveri Krupp Reaktor Device for cleaning a gas stream from CO2
CN109012090A (en) * 2018-07-30 2018-12-18 大连理工大学 It is a kind of can oxidation resistant non-aqueous decarbonizing solution for trap carbon dioxide in gas mixture
WO2020063557A1 (en) * 2018-09-25 2020-04-02 天津工业大学 Low energy consumption anhydrous co2 phase change absorption agent, and regeneration method and application thereof
CN109331610A (en) * 2018-12-14 2019-02-15 中石化石油工程技术服务有限公司 Trap CO in exhaust gas2Phase transformation absorbent

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114405258A (en) * 2021-12-28 2022-04-29 中国矿业大学 Is suitable for low partial pressure CO2Capture purified absorbent system

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