Flexible hydrocarbon gas separation process and apparatus

• US 7,856,848 B2
• Filed: 03/05/2007
• Issued: 12/28/2010
• Est. Priority Date: 07/19/2006
• Status: Expired due to Fees

• Current Assignee: Yingzhong Lu
• Original Assignee: Yingzhong Lu
• Inventors: Lu, Yingzhong
• Primary Examiner(s): Tyler; Cheryl J
• Assistant Examiner(s): BALDRIDGE, LUKAS M
• Application Number:
  US11/713,757
• Publication Number:
  US 20080016909A1
• Time in Patent Office: 1,394 Days
• Field of Search: 626/23, 626/18, 626/20, 626/30, 629/12, 951/49, 951/56, 951/72
• US Class Current: 62/623
• CPC Class Codes: C10L 3/10 Working-up natural gas or synthetic natural gas

Abstract

The present invention related to a flexible hydrocarbon gas separation process that could dehydrate the water-saturated hydrocarbon gas mixture and recover thereof the required higher hydrocarbons (NGL) therein with a controllable ethane recovery rate (ranging from >95% to <2%) while keeping high recovery rate of all other heavier components. The flexible process comprises the following steps: deep-cooling and dehydrating the raw gas and get the NGL condensate; flowing the deep-dehydrated gas into the flexible absorber to get the rich oil with desirable ethane content; completely demethanizing and partially deethanizing as desired the rich oil and the NGL condensate to get purified rich oil and purified NGL condensate, respectively; separating the NGL vapor from the purified rich oil; cooling and compressing the NGL vapor; mixing the NGL vapor with the purified NGL condensate; and liquefying the mixture to get the final NGL product. The present invention also provides a flexible apparatus with highly efficient components for the flexible process.

Claims

1. A flexible hydrocarbon gas separation process that could dehydrate a water-saturated hydrocarbon gas (“

raw gas”

hereafter) and recover thereof the higher hydrocarbon liquid (“

NGL”

hereafter) with controllable ethane recovery rate ranging from >

95% to <

2% while keeping high recovery rate of all other heavier hydrocarbon components comprises the following steps;

(a) Pre-cooling and pre-dehydrating the raw gas by directly contacting a counter-flowing liquid coolant comprising an aqueous solution of a gas hydrate inhibitor to get a pre-cooled pre-dehydrated gas and a partial NGL condensate;

(b) Deep-cooling and deep-dehydrating the pre-cooled pre-dehydrated gas with a refrigerant from an external refrigerator to get a deep-cooled deep-dehydrated gas and a deep-cooled NGL condensate;

(c) Flowing the NGL condensate into a condensate pre-demethanizer and a flexible condensate deethanizer in tandem to remove all the methane content therein and simultaneously reduce the ethane content therein to any desirable level to get a deep-cooled purified NGL condensate;

(d) Flowing the deep-cooled deep-dehydrated gas into a flexible absorber and contacting the gas with a counter-flowing liquid absorbent (“

lean oil”

hereafter) to get a cold residue gas and a cold rich absorbent (“

rich oil”

hereafter) with a desirable level of ethane content;

(e) Flowing the cold rich oil into a rich oil pre-demethanizer and a flexible rich oil deethanizer in tandem to remove all the methane content therein and simultaneously reduce the ethane content therein to any desirable level to get a purified rich oil;

(f) Depressurizing the purified rich oil and distilling the purified rich oil in a rich oil fractionator to get an NGL vapor and a regenerated lean oil;

(g) Cooling the NGL vapor with a heat transport medium to transport the heat energy from the NGL vapor to the deep-cooled rich oil in the flexible rich oil deethanizer;

(h) Compressing the NGL vapor and mixing the compressed NGL vapor with the deep-cooled purified NGL condensate to get a low-temperature NGL vapor-liquid mixture; and

(i) Liquefying the low-temperature NGL vapor-liquid mixture to get a final NGL product.

2. The flexible hydrocarbon gas separation process of claim 1 wherein in step (a) the liquid coolant comprising an aqueous solution of a gas hydrate inhibitor is pre-cooled with the cold residue gas and the cold rich oil before being used as the coolant in step (a).

3. The flexible hydrocarbon gas separation process of claim 1 wherein in step (b) the pre-cooled pre-dehydrated gas is mixed with the partial NGL condensate before being deep-cooled with a refrigerant to get the deep-cooled deep-dehydrated gas and the NGL condensate.

4. The flexible hydrocarbon gas separation process of claim 1 wherein in step (b) the pre-cooled pre-dehydrated gas is mixed with a spray of concentrated gas hydrate inhibitor solution before being deep-cooled with a refrigerant to get the deep-cooled deep-dehydrated gas and the NGL condensate.

5. The flexible hydrocarbon gas separation process of claim 1 wherein in step (b) the pre-cooled pre-dehydrated gas is further deep-dehydrated with a solid desiccant to get the deep-dehydrated gas before further deep-cooled with a refrigerant.

6. The flexible hydrocarbon gas separation process of claim 5 wherein the solid desiccant is calcium chloride or other deliquesce solid desiccants that would be liquefied when absorbing sufficient water, and the deliquescent liquid is then used as the concentrated hydrate inhibitor solution.

7. The flexible hydrocarbon gas separation process of claim 1 wherein in step (c) and (e) the working pressure and bottom temperature of the deethanizer is controlled to precisely reduce the ethane content of the purified condensate to desirable level.

8. The flexible hydrocarbon gas separation process of claim 1 wherein in step (c) and (e) the tandem process with the pre-demethanizer and the deethanizer is replaced with the integrated process of a integrated cascade flexible deethanizer.

9. The flexible hydrocarbon gas separation process of claim 1 wherein in step (d) the absorbent used in the absorber could be either heavy oils (i.e., hydrocarbon mixture with molecular weight higher than 100) or other organic compounds with hydrocarbon gas solubility higher than 20 scf/gal.

10. The flexible hydrocarbon gas separation process of claim 1 wherein in step (d) the ethane recovery rate in the flexible absorber is precisely controlled by changing the lean oil flow rate.

11. The flexible hydrocarbon gas separation process of claim 1 wherein in step (f) the regenerated lean oil is recycled as a heating medium.

12. The flexible hydrocarbon gas separation process of claim 1 wherein in step (g) the heat transport medium is a cooled recycling lean oil.

13. A flexible hydrocarbon gas separation process that could dehydrate a water-saturated raw hydrocarbon gas under high pressure and recover thereof the NGL with controllable ethane recovery rate ranging from >

95% to <

2% while keeping high recovery rate (over 90%) of all other heavier hydrocarbon components comprises the following steps;

(a) Pre-cooling and pre-dehydrating the raw gas by directly contacting a counter-flowing liquid coolant comprising an aqueous solution of a gas hydrate inhibitor to get a pre-cooled pre-dehydrated gas and a partial NGL condensate;

(b) Deep-dehydrating the pre-cooled pre-dehydrated gas with a solid desiccant to get a pre-cooled deep-dehydrated gas;

(c) Expanding the pre-cooled deep-dehydrated gas to a lower pressure and temperature to get a deep-cooled deep-dehydrated gas and an NGL condensate;

(d) Flowing the NGL condensate and the partial NGL condensate into a condensate pre-demethanizer and a flexible condensate deethanizer in tandem to remove all the methane content therein and simultaneously reduce the ethane content therein to any desirable level to get a deep-cooled purified NGL condensate;

(e) Flowing the deep-cooled deep-dehydrated gas into a flexible absorber and contacting the gas with a counter-flowing liquid absorbent (“

lean oil”

hereafter) to get a cold residue gas and a cold rich oil with a desirable level of ethane content;

(f) Flowing the cold rich oil into a rich oil pre-demethanizer and a flexible rich oil deethanizer in tandem to remove all the methane content therein and simultaneously reduce the ethane content therein to any desirable level to get a purified rich oil;

(g) Depressurizing the purified rich oil and distilling the purified rich oil in a rich oil fractionator to get an NGL vapor and a regenerated lean oil;

(h) Cooling the NGL vapor with a heat transport medium to transport the heat energy from the NGL vapor to the deep-cooled rich oil in the flexible rich oil deethanizer;

(i) Compressing the NGL vapor and mixing the compressed NGL vapor with the deep-cooled purified NGL condensate to get a low-temperature NGL vapor-liquid mixture; and

(j) Liquefying the low-temperature NGL vapor-liquid mixture to get a final NGL product.