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Purification of Carbon Dioxide

Inactive Publication Date: 2015-04-30
AIR PROD & CHEM INC
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Benefits of technology

The present invention provides a more efficient process for removing impurities from carbon dioxide, particularly the "light" impurities. The overall recovery of carbon dioxide is improved while maintaining or even improving purity. Additionally, the simplified process eliminates the need for external refrigerant systems, reducing energy consumption and improving efficiency.

Problems solved by technology

Some of these sources contain hydrogen sulfide, which is undesirable for pipeline transport since hydrogen sulfide is toxic and corrosive in the presence of water.
In addition, it is not desirable to introduce hydrogen sulfide to the crude oil that is being extracted by the EOR process.

Method used

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  • Purification of Carbon Dioxide
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  • Purification of Carbon Dioxide

Examples

Experimental program
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example 1

[0434]The process depicted in FIG. 3 was modeled by computer using ASPEN™ Plus software (version 7.2; © Aspen Technology, Inc.) using measured vapor-liquid equilibrium data in the composition and pressure / temperature range of interest. The heat and mass balance data for key streams are provided in Table 2.

[0435]According to the modeling, the exemplified process recovers 99% of the carbon dioxide in the feed at a purity of 91.1 mol. %, and consumes about 20,013 kW of power in total. This figure represents the sum of the power required for compressors CP1 and CP3 (19,915 kW) and pumps P3 and P4 (98 kW). The exemplified process therefore saves 16.2% of the power of the comparative example (or 15.6% on a specific power basis).

[0436]It should be noted that these figures do not take into account the power consumed by the conventional “light” impurity removal process depicted in FIG. 1B. Therefore, the total and specific power savings of FIG. 3 would actually be significantly more than tha...

example 2

[0437]The process depicted in FIG. 4 was modeled by computer using ASPEN™ Plus software (version 7.2; © Aspen Technology, Inc.) using measured vapor-liquid equilibrium data in the composition and pressure / temperature range of interest. The heat and mass balance data for key streams are provided in Table 3.

[0438]According to the modeling, the exemplified process recovers 99% of the carbon dioxide in the feed at a purity of 91.1 mol. %, and consumes about 18,527 kW of power in total. This figure represents the sum of the power required for compressors CP1 and CP3 (18,428 kW) and pumps P3 and P4 (100 kW). The exemplified process therefore saves 22.5% of the power of the comparative example (or 21.9% on a specific power basis).

[0439]It should be noted that these figures do not take into account the power consumed by the conventional “light” impurity removal process depicted in FIG. 1B. Therefore, the total and specific power savings of FIG. 4 would actually be significantly more than th...

example 3

[0440]The process depicted in FIG. 5 was modeled by computer using ASPEN™ Plus software (version 7.2; © Aspen Technology, Inc.) using measured vapor-liquid equilibrium data in the composition and pressure / temperature range of interest. The heat and mass balance data for key streams are provided in Table 4.

[0441]According to the modeling, the exemplified process recovers 94.9% of the carbon dioxide in the feed at a purity of 97.3 mol. %, and consumes about 17,801 kW of power in total. This figure represents the sum of the power required for compressors CP1 and CP3 (17,511 kW) and pumps P1, P3 and P4 (290 kW). The exemplified process therefore saves 26.7% of the power of the comparative example (or 16.3% on a specific power basis).

[0442]It should be noted that these figures do not take into account the power consumed by the conventional “light” impurity removal process depicted in FIG. 1B. Therefore, the total and specific power savings of FIG. 5 would actually be significantly more t...

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PUM

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Abstract

In a process for separating “heavy” impurities such as hydrogen sulfide from crude carbon dioxide comprising significant quantities of “light” impurities such as non-condensable gases, involving at least one heat pump cycle using as working fluid a fluid from the “heavy” impurity separation, the “light” impurities are removed from carbon dioxide-enriched gas generated in the “heavy” impurity separation. The carbon dioxide-enriched gas, or a compressed carbon dioxide-enriched gas produced therefrom, is at least partially condensed by indirect heat exchange against intermediate liquid also generated in the “heavy” impurity separation. Total and specific energy consumption is reduced compared to conventional processes in which “light” impurities are removed from carbon dioxide product gas.

Description

BACKGROUND OF THE INVENTION[0001]The present invention relates to processes and apparatus for the purification of carbon dioxide. In particular, the invention relates to processes and apparatus for the removal of at least one “heavy” impurity from crude carbon dioxide by mass transfer separation at sub-ambient temperatures and super-atmospheric pressures. The invention has particular application to the purification of crude carbon dioxide comprising significant amounts of at least one “light” impurity.[0002]By “light” impurity, the Inventors are referring to an impurity that is more volatile than carbon dioxide. Examples of “light” impurities include nitrogen (N2), oxygen (O2), argon (Ar), hydrogen (H2), helium (He); methane (CH4); carbon monoxide (CO), neon (Ne), xenon (Xe), krypton (Kr), nitric oxide (NO) and nitrous oxide (N2O).[0003]By “heavy” impurity, the Inventors are referring to an impurity that is less volatile than carbon dioxide. Examples of “heavy” impurities include hy...

Claims

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Application Information

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IPC IPC(8): F25J3/08C01B32/50
CPCF25J3/08B01D53/002C01B17/167F25J2200/02F25J2200/04F25J2200/40F25J2200/50F25J2200/74F25J2200/76F25J2200/78F25J2205/02F25J2215/80F25J2220/82F25J2220/84F25J2230/80F25J2235/02F25J2235/80F25J2240/40F25J2245/02F25J2260/20F25J2260/80F25J2270/02F25J2270/80F25J2270/88F25J2290/40B01D53/75B01D2257/302B01D2257/304B01D2257/306B01D2257/308B01D2257/404B01D2257/406B01D2257/7022C01B32/50Y02P20/129Y02P20/151
Inventor HIGGINBOTHAM, PAULGUVELIOGLU, GALIP HAKANPALAMARA, JOHN EUGENEWHITE, VINCENT
Owner AIR PROD & CHEM INC