Patent Application
20120067079
The invention relates to the integration of a liquefied natural gas (LNG) liquefier system with a nitrogen rejection unit (NRU) so as to minimize the capital and operating costs while maintaining liquefied natural gas product purity requirements.
Renewable methane can be recovered from a number of sources, such as anaerobic digestion of municipal or industrial waste streams, the degradation of biomass in landfills, the gasification of waste and biomass streams, amongst others. In many instances, this renewable methane require purification before it can be used and/or sold into higher valued markets, such as injection into the pipeline grid, as a feedstock for liquefied natural gas, as a vehicle fuel, or as a feedstock for the production of hydrogen. Further, the energy that is required to purify the renewable methane is significant.
The cleanup of biogas/landfill gas is both capital and power intensive because it contains a large number of trace and bulk contaminants in fairly large concentrations. Various methods are employed to remove these including chilling, cryogenic methods and various adsorption and scrubbing processes. However, these processes can be expensive in both capital and operating costs and it is important to minimize these costs to achieve an economically viable process.
A typical process for the purification of the methane from biogas/landfill gas requires several steps. Sulfur removal is generally followed by drying. The dried gas stream is then treated for contaminants such a volatile organic compounds by process such as adsorption, CO2 washing or by cryogenic methods. The stream is then treated for bulk carbon dioxide removal by a membrane or adsorption process and then is treated for removal of nitrogen. All these purification steps are necessary before the biogas/landfill gas can be liquefied and stored in anticipation of being dispensed, or directed towards other uses, such as pipeline injection, energy production with fuel cells or small-scale hydrogen production. LNG production is particularly challenging since all condensable contaminants including carbon dioxide must be removed to low ppm levels.
The invention will allow for maximizing the methane recovery while maintaining high liquefied natural gas product purity. The operator can utilize a smaller nitrogen rejection unit and can optimize power consumption. The process of using the nitrogen rejection unit integrated with the liquefied natural gas liquefier system achieves greater product purity (>96 mol % methane) and greater than 89% methane recovery than conventional non-integrated combinations.
By integration of the liquefied natural gas liquefier system with a nitrogen rejection unit, the overall system becomes more compact and efficient. This further enables the operator to maximize methane recovery while maintaining high liquefied natural gas product purity while enable a smaller nitrogen rejection unit. The invention further allows the operator to optimize power consumption while allowing for significantly higher product purity and methane recovery than conventional or unitegrated NRU and liquefier combinations which are limited to 96 mol % methane and 80% methane recovery.
The invention is a method for recovering liquefied natural gas comprising the steps:
Feeding a natural gas stream containing impurities to a nitrogen rejection unit;
Feeding the purified natural gas stream to a liquefier heat exchanger;
Expanding the liquefied natural gas and feeding the expanded liquefied natural gas to a flash vessel;
Flashing the liquid natural gas and separating the liquefied natural gas from the flash gas;
Feeding the liquefied natural gas to storage and the flash gas to said nitrogen rejection unit.
Alternatively, the invention is a method for recovering liquefied natural gas comprising the steps:
Feeding a natural gas stream containing impurities to a nitrogen rejection unit;
Feeding the purified natural gas stream to a liquefier heat exchanger;
Expanding the liquefied natural gas and feeding the expanded liquefied natural gas to a flash vessel;
Flashing the liquid natural gas and separating the liquefied natural gas from the flash gas;
Recovering refrigeration from said flash gas; and
Feeding the liquefied natural gas to storage and the flash gas to said nitrogen rejection unit.
The invention further comprises an apparatus comprising a nitrogen rejection unit, a liquefier heat exchanger and a flash vessel.
The raw feed gas is first compressed and pre-conditioned which entails the removal of water, carbon dioxide, non-methane organic compounds (NMOCs) and sulfur compounds by known methods. The partially purified gas is fed to the nitrogen rejection unit where much of the nitrogen is rejected. Since product purity and methane recovery are inversely related, nitrogen rejection is limited to maximize the methane recovery for the smallest equipment cost. The resulting gas which contains significantly lower amounts of inerts is fed to the liquefier heat exchanger where it is liquefied at pressure to a subcooled state. Typical pressures range from 30 bar to 6 bar with a tradeoff between mixed refrigeration compressor power and compression power for the purification system. This liquid is expanded through a valve whereby further cooling is effected to about 2 bar (range is 1 to 5 bar).
The two-phase mixture is separated in a flash vessel and the resulting liquid is directed to the storage tanks, while the flash gas which is richer in nitrogen is recycled back to the nitrogen rejection unit. The flash gas can also be combined with the raw natural gas/biogas at the front end of the overall process if the nitrogen rejection unit does not have a recycle compressor. Clearly additional flash gas from the storage tank will be produced. This too is recycled back to the nitrogen rejection unit or to the front end of the cleanup process. The only methane that will be lost is the nitrogen rejection unit waste stream which is nitrogen-rich but otherwise very pure and can be flared or converted into power using a gas engine or a fuel cell.
The end flash from the flash vessel has an additional advantage in that the liquid outlet of a flash is at equilibrium which implies that it will produce some more gas inside the line between the end flash and storage tank because of product line pressure drop. Therefore, it is best practice that the flash pressure be lower than the storage pressure. To maximize liquefied natural gas production and minimize product flash losses, the first flash within the flash vessel is effected at a pressure lower than the storage tank pressure, whence, the liquid coming down from the end-flash tank will be sub-cooled at storage pressure. A cryogenic pump can be utilized to overcome this concern, but involves additional cost, maintenance and potential reliability issues. Therefore it is advisable to have horizontal storage tanks, and a cold box layout so that the liquid level inside the end flash will be higher by a few hundreds of mbar of equivalent liquefied natural gas head that the top of the storage and to use that additional head to pressurize
a is an integrated mixed refrigerant liquefied natural gas liquefier.
b depicts a different embodiment of an integrated mixed refrigerant liquefied natural gas liquefier.
c depicts another embodiment of an integrated mixed refrigerant liquefied natural gas liquefier.
a shows a liquefier having a lower cost to operate.
b shows a different embodiment of a lower cost to operate liquefier.
Landfill gas is purified and all the water, sulfur compounds, NMOCs and carbon dioxide are removed in a pre-purification process. The purified gas contains methane, nitrogen and oxygen and has the following composition:
The gas is further purified in an adsorption system so that the carbon dioxide level is reduced below 50 ppmv and a large portion of the nitrogen is removed. Oxygen usually does not adsorb appreciably and about 50% of the oxygen is removed in each case.
Turning to the figures,
A cold water stream (CWS) is fed through line 11 to heat exchanger E as well as through valve V6 and line 13 to line 12 as cold water return (CWR). The cold mixed refrigerant is fed through line 9 to knockout drum B where it will proceed through line 7A to refrigerant pump C and through open valve V4 to contact line 3 in heat exchanger A. When valve V4 is closed and valve V5 is open the mixed refrigerant will re-enter knock out drum B through line 7. The overhead from knockout drum B will travel through line 3 to heat exchanger A and enter valve V2 to column unit D where it will exit unit D through overhead line 4 as well as through the bottom of unit D through line 5A. This will exit heat exchanger A through line 5 and connect to inlet separator G where the bottoms will travel through line 8 and transfer pump H to line 6 which will enter the knockout drum B. The refrigerant will leave the inlet separator G through line 8A and connect to mixed refrigerant column unit F where the mixed refrigerant will travel through line 10 back to heat exchanger E.
In
The nitrogen recovery unit product/liquefier feed natural gas is fed through line 24 into heat exchanger I where it will pass through valve V12 and enter flash tank J. The now liquefied natural gas will exit through valve V11 and line 25 to line 26 where it will enter storage tank K and can be accessed through line 21 and valve V10 for later use. Vent gas from the storage tank K will exit through line 20 where it will join line 22 and be fed back through the recycle compressor Q to the nitrogen containing biogas feed line 23.
Heat exchanger T is fed cold water through line 35A to provide a cooling medium which will also feed to the cold water return line 35 through valve V16. Line 24A directs warm water leaving heat exchanger T. The cold refrigerant is fed through line 36 to knock out drum P which feeds the cold refrigerant to the heat exchanger I through line 28 and which passes through valve V13 to the column unit L where refrigerant from the top exits through line 31 and through the bottom through 31A which joins line 31 and passes through heat exchanger I and line 31 will be fed to inlet separator M where refrigerant exits through line 33 and is fed to mixed refrigerant column unit U which feeds mixed refrigerant, now warmer to the heat exchanger T through line 24. The bottoms from the inlet separator M is fed through line 32 and transfer pump N back to knock out drum P. The bottoms from the knockout drum P are fed through line 30 and refrigerant pump O to valve V15 for reentry back into the knockout drum P. BZ designates the cold box boundary.
The refrigerant from the knockout drum P may also enter line 29 and open valve V14 where it will feed into line 31 and entry into the inlet separator M.
b is a similar version of the integrated mixed refrigerant liquefied natural gas liquefier system of
c is another embodiment of the invention showing an integrated mixed refrigerant liquefied natural gas liquefier. Natural gas such as that from landfill gas or biogas from a nitrogen recovery unit, not shown, is fed through line 40 into heat exchanger V. The natural gas is liquefied and its pressure is higher as it exits through line 40A through temperature control valve V17. The liquefied natural gas enters end flash unit W where the flashed liquefied natural gas is fed through line 41 and open pressure control valve V18 and recycled back to heat exchanger V where it will exit and be fed through line 42 to a nitrogen recovery unit, not shown.
The bottoms from the flash unit W exit through line 43 and open valve V19 where it will enter horizontal cryogenic storage tank Y. Additional static head is maintained between the liquid level in the end flash unit W and the horizontal cryogenic storage tank Y such that it is equivalent to subcooling at storage level and pressure. Line BZ represents the cold box boundary.
Cold water is fed through line 60 into heat exchanger AI to provide a cooling medium and also fed through line 61 and open valve V25 to the cold water return line 62. Refrigerant will exit through line 64 and be fed through to a knockout drum AD where refrigerant is fed through line 51 and refrigerant pump AE through open valve V24 to line 52 passing through heat exchanger AA. When valve V24 is closed and valve V24A is open, the refrigerant is fed through line 55 back to knockout drum AD. Refrigerant is also fed through line 56 from the top of the knockout drum AD to line 52 passing through heat exchanger AA. Line 52 will deliver the refrigerant through open valve V21 to a column unit AC where the bottoms from said unit are fed through line 53 to rejoin with the tops which exit unit AC through line 54. Line 54 passes through heat exchanger AA where it will be fed to inlet separator AF.
The refrigerant in line 54 is occasionally supplemented from the knockout drum AD through open valve V23 and line 57 which connects with the tops from the knockout drum AD through line 56. Line 54 will enter the inlet separator AF where its bottoms are transferred through line 58A and transfer pump AG to line 50 which returns to the knockout drum AD. The tops from the inlet separator AF exit through line 58 and enter mixed refrigerant column unit AH where mixed refrigerant will enter the heat exchanger AI for cooling and reentry into the knockout drum AD for entry into heat exchanger AA.
a shows a lower cost embodiment liquefier. Natural gas such as that found in landfill gas or biogas is fed through line 79 and open valve V30 where it will enter flash tank BA. Liquefied natural gas exits through line 77 and open valve V33 to storage, not shown. Natural gas will exit the flash tank BA through line 78 where it will pass through economizer BC and exit to a nitrogen recovery unit, not shown. Valve V32 can be opened and excess nitrogen can be recovered through line 78A, unit TIC back into flash tank BA.
Part of the natural gas feed from line 78 is fed through open valve V31 to line 76 which passes through heat exchanger BD and open valve V34 back to the flash tank BA as liquefied natural gas.
Cold water is fed through line 83 to heat exchanger BJ and through line 85 and open valve V39 to cold water return line 84. Refrigerant will exit through line 85A and be fed to knockout drum BH where it will exit through the bottom of the knockout drum through open valve V36 and refrigerant pump BI to be fed to line 74 passing through heat exchanger BD. Valve V36 can be closed and valve V38 open such that refrigerant will pass through line 75 back to knockout drum BR
The tops from the knockout drum BH will be fed through line 70 to line 74 passing through heat exchanger BD. The refrigerant will pass through open valve V35 and be fed to column unit BE where the bottoms from the unit exit through line 71 and join with the tops from the unit BE line 72 which passes refrigerant through heat exchanger BD. This refrigerant will enter inlet separator BG through line 72 where the bottoms from the inlet separator BG are fed through line 80 and transfer pump BF back to the knockout drum BH.
The tops from the inlet separator will exit through line 81 to mixed refrigerant unit BK. The mixed refrigerant from unit BK is fed back to heat exchanger BJ as a warm fluid through line 82 where it will be cooled down and ultimately fed back into heat exchanger BD after passing through knockout drum BH. Line BZ designates the cold box boundary.
b is virtually identical to
Typical nitrogen rejection performance is shown in
In addition, the relative power for all 3 cases is compared in Table 3 which shows that the extra power needed for liquefaction and recycle with higher inerts (case 1) is compensated by the vacuum pump power needed for higher NRU purity (case 3). Hence, there is no appreciable net power penalty.
Other embodiments of the invention are illustrated in
While this invention has been described with respect to particular embodiments thereof, it is apparent that numerous other forms and modifications of the invention will be obvious to those skilled in the art. The appended claims in this invention generally should be construed to cover all such obvious forms and modifications which are within the true spirit and scope of the invention.
This application claims priority from U.S. provisional patent application Ser. No. 61/317,466, filed Mar. 25, 2010.
| Number | Date | Country | |
|---|---|---|---|
| 61317466 | Mar 2010 | US |
