PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
(OP)
How do you determine whether to pump or compress 97% co2 into a pipeline, when it is in supercritical region?
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PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
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RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
For example, we have 3-3000 horsepower electric drive IR HHE 2 throw (8" by 14" stroke") compressors on C2=, suction 850 psig at 60F and discharge 2400 psig. There were time we needed a lower rate so we installed a Bingham MSD split case pump with 8 impellars. suction 850 psig 60F (on the same header as the reciprocating compressors), discharge 1650 psig.
The pump was far cheaper than a reciprocating unit, but its eff is lower. NOW, the impellars are not a stainless steel as in most pump operations, they are aluminum alloy to dissapate heat better.
We also has booster pumps on the ethylene, suction from 850 to 1250 psig, discharge 1300 to 2000 psig.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
How does one determine to pump or use a compressor?
From your example, it seems to me capacity is one factor. Correct?
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
But the real test will come when looking at the conditions. If the pipeline pressure goes from 1600 to 2100 psig, you will waste a lot of horsepower using the pump. The pumps tend to have lower maintenance isssues.
So you should do a little life cycle cost for the first 15 years (after 15 years, the NPV values don't show much influance). My gut says use a pump along the pipeline, but if this is at the same location where you are gathering and compressing in the first few stages, then just continue with the compressor...
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
What is the issue with density in determing whether to use a pump or a compressor?
I have to compress it until I get to the critical pressure of 950 psig in my case, and then pump it. Is that a good assumption? My flowrate is only 1 MMscfd and my final pressure is 1800 psig.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
- compositional changes can change your critical point and play havoc with your design.
- having a pump and compressor in series slaves them to each other with maintenance and makes each of them a critical piece of equip.
- If you have a compressor already, I'd limit myself to a single piece of rotating equipment to limit leaks and seals.
just my opinion...
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
a 1 MMSCFD unit is a cake walk....
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
Be aware of compressor bypass arrangements, obviously liquid or subcooled CO2 going through a compressor bypass valve will hit cryogenic temp's. We've had good success with a dual-stage bypass to minimize the potential for hydrates and freezing temps.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
Could you please explain your dual-stage bypass to minimize the potential for hydrates and freezing temps? Thanks.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
Setpoints and loop ramping speeds are important, especially during startup, but overall, we're really happy with the performance. Note that the compressor blowdown MUST also be on the hot 5th stage discharge gas.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
The distinction between a pump and a compressor is largely semantic, but pumping a gas IS compressing it.
Maddocks demonstrated impressive in-depth knowledge of a multistage centrifugal compressor.
I once had interaction with a company called Compressor Controls Corp. Their Compressor management technology and surge control technology are both state-of-the-art. Expensive, but not as expensive as a ruined compressor.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
Is this system variable speed drive? You need a way to vary your system capacity, either through auto-bypassing or through speed control or preferably both for maximum control. Do you have a way to bypass the dehydration unit? You will also need some startup bypass assembly to get the system up and running. Ideally, its nice to have a hot discharge to flare so you can run the system and pretend you're injecting - it allows for a really nice startup and you can play with your loops and tune effectively.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
1.) Cascading water dumps can allow for some excellent degassing of water so that when it finally dumps to the tank, it has been degassed to a great degree. if you dump from stage 4 suction direct to a tank, there some considerable risks including ripping the tank apart when the dump valve sticks open. As well, if you overcool 4th stage suction, you can send condensed CO2 to the tank where it expands and...well, you get the picture.
2.) I described the bypass pretty well on one of the above postings.
3.) I've written this up in a couple of recent design papers - let me know if you can't track them down with google.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
I will add one by pass from last to 1st, the rest will be designed by the compressor vendor.
Thanks for the dump valve issue, good point.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
Here is another tip. Put a sweet gas purge system in place. If the unit ESD'd, the suction and discharge lines are closed and a sweet natural gas source is sent through the compressor to a flare. You could even use N2.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
1) Why do I need to purge it out after ESD? My vents all go to atmosphere.
2) I have recipe compressors with automatic clearance pockets for capacity control. Why should I use bypasses for capacity control?
3) Do you know for thh scrubber liquid-out what kind of a vessel I need? I mean does the sump need to be lined with????
Regards.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
If you have reviewed the capacity curves with the pockets open, and you are haeppy with the capacity, then you do not need to have auto-bypasses. However, I've never come across an acid gas machine that functions within pocket limits. As well, changing VVCP pocket settings tends to be a less than great way to vary recip capacity as it changes volumetric efficiency of the cylinder and modifies interstage pressures and temperatures.
The acid gas water sump vessel should be resistant to carbonic acid attack - you may wish to consider either a coated tank, FRP, or stainless steel.
Does your system contain H2S as well?
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
1. Great point about the purge issue.
2. Where do I add the bypasses (4 stages) for capacity control? I thought for recipes you don't add bypasses.
3. Yes, I do have H2S.
Regards.
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
You'd better get yourself a qualified consultant with some acid gas experience and review the system with them. As well, you should be talking with your compressor vendor - if they have any acid gas experience, they should be assisting you in your efforts to create a safe, operable system with maximum flexibility.
dcasto - your thoughts?
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
RE: PUMP OR COMPRESSOR CO2 AT SUPERCRITICAL CONDITIONS
Yes, you are getting to the ponit where ratash can select a qualifies design person. On eng-tips we all like to help kick start ideas and get the poster to think about it. Then they can use basics and ideas to assist them.
Also, ratash, you have enough data to go get budgetary fiquires, the size of the equipment, the basic materials of construction, the ned or no need for driers, safety systems, capacity control needs, there should be very little ommissions onan RFP/RFQ.
If after ratash gets some info back from the vendors and they don't make sense, ratash could ask opinions here too I suppose.