NOVEL SCHEME FOR SMALL SCALE LNG PRODUCTION in POLAND. W.H. Isalski
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1 NOVEL SCHEME FOR SMALL SCALE LNG PRODUCTION in POLAND W.H. Isalski
2 Presentation Overview The history of gas de-nitrogenation in Poland Changes in feed gas Changes in market conditions Expanding market for small scale liquefaction Land-based remote locations The technical challenges The results of modifications and their effects
3 The KRIO Nitrogen Rejection Plant Location
4 History of Polish KRIO Nitrogen Rejection Plant Located South-Western Poland Constructed in the 1970s Original design feed gas composition : Helium 0,4 vol% Nitrogen 42,7 vol% ( now 30 35%) Methane 56,0 vol% Ethane 0,5 vol% Propane+ 0,1 vol% CO2 0,3 vol% Water Saturated at inlet conditions Pressure 5,1-5,6 Mpa Temperature C deg Flow NCMH
5 Process Elements in Nitrogen Rejection Units (NRUs) Nitrogen contaminated gas / low BTU gas undergoes pre-treatment : CO2 removal (amine unit) H2O removal (molecular sieve) aromatics & C5+ removal (activated carbon) Filtration of dust & mole sieve particles A typical NRU is a highly integrated process comprising : plate-fin heat exchangers pumps cryogenic distillation columns Joule-Thomson (J-T) valves for refrigeration Product Compression
6 Block Flow Diagram for Nitrogen Rejection Plant
7 History of Polish KRIO Nitrogen Rejection Plant Product Requirements : product gas < 4% N2 at 1,8MPa compressed to grid downstream waste gas < 1% CH4 vented to atmosphere crude helium > 85% He pure helium > 99,999% Flexibility to produce some liquid CH4 & N2 Base load Product is pipeline quality gas.
8 Changes in Feed Gas & Waste Gas Nitrogen content : 43% 33-35% Helium content : 0,4% 0,18% Pressure : 5,6 MPa 5,3 MPa CO2 content : 0,3 % 0,4% Waste gas CH4 <1% 3 4 % Original Plant lost flexibility.
9 Main effects of changes in feed composition The environmental impact of increased methane content in the waste gas The economic loss as the consequence of methane emissions Inability to produce liquid products. Reduced flexibility when changing from LNG to liquid nitrogen by-product. Less helium in feed means reduced revenue from liquid helium Less stable operation of the cryogenic unit
10 Growing Market for Small LNG liquefiers Small gas reserves in remote areas can be monetised. Countries with un-reliable or non-existent gas network need gas supplies. Scotland, Poland, China, USA, Norway Rising cost of gas/lng. Greater volatility in prices. LNG transport vessels produce boil-off gas (BOG covered in previous paper).
11 History of natural gas liquefaction Cryogenic industry started in early 1900s Liquefaction of LNG began in the 1940s First base load Plant in the 1960s LNG Peak Shaving plants in the 1970s Base load train size increased dramatically Ship BOG re-liquefaction patents in 1970s Stranded gas exploitation gathers momentum in late 1990s GTL, mid-sized LNG plants, small scale units Machinery well developed with high efficiencies Mature technology. Innovations still possible. Modifications to existing plants.
12 LNG Liquefaction Train Capacities Type of LNG Liquefier Capacity Gas Input Plants & tonnes/day MMSCFD Location Peak Shaving Units Over 100 units,usa, UK, Europe, since 1940s. Mid-sized units Less than 10 Kenai, Algeria, China. Base Load Plants Over 100 units worldwide. Newer Base Load Plants several built, worldwide, a few planned even larger at >20000 tonnes/day. Under development Planned
13 Variety of LNG liquefaction Cycles Classical APCI C3 pre-cooled MRC. Dual MRC, Shell, TEAL & Linde. Cascade Cycle, Phillips. Single Fluid, multi-stage Mixed Refrigerant. Single Stage Mixed Refrigerant, Prico. Gas expander cycles & Nitrogen Expander cycles. Novel systems: Acoustic, Vortex Tubes. Modifications added to existing processes gas expanders, additional cycles bolted on to existing facilties.
14 Peak Shaving LNG Plants in 1970s - Belgium 240 TPD LNG Peak Shaver using nitrogen Cycle
15 Tractebel project - Mid-sized LNG Plant, China 1200 TPD LNG Plant Urumqi, China Status: Plant in operation since Q4/2004.
16 Cascade Reliquefaction System.
17 Cascade Re-liquefaction System.
18 Cryogenic section of Nitrogen Rejection Unit
19 Plate-fin Heat Exchanger.
20 Process Concept Development Options considered Lowering Pressure in Upper Column with Blower Adding Separate cycle to provide refrigeration Importing liquid Nitrogen to assist in cold production. Modification of methane pump control scheme to VSCF controller. Application of gas expanders in various locations. Application of liquid expanders in various locations.feed to lower column, rich liquid & poor liquid Likely Cost/Benefit High Capital and operating Cost, limited benefit. High Capital and operating Cost, moderate benefit.complex solution. High operating cost. Simple implementation and with good benefit. Low, with good benefits, with limited scope for LNG production. Difficult to provide cold at correct temperature level. Quite expensive. The 2nd & 3rd options provide cold at the appropriate temperature level. Limited sources of machinery. Testing required.
21 LNG Production using turbo-expander. TGE Project to increase cold production in a nitrogen rejection plant. Novel process scheme.
22 Process Concept Development Decided to implement - Two-Phase expander! Reasoning based on: Previous site experience with canned pumps Previous site experience of VSCF control in a pump modification(variable Speed Constant Frequency) Knowledge that trials were done & no cavitation Compact nature of modification. MAIN WORRY WAS CAVITATION
23 Example of Cavitation. Propeller rotation is anticlockwise. Bubbles collapse & erode blades. Odolanow situation is opposite: bubbles form and fluid expands.
24 The challenges in 2-phase turbines. Cavitation in turbine(95% vapour volume after flash). 2-phase flow instability in vertical direction. Bearing fluid. Control of turbine. Local space constraints. Maintaining plant flexibility: LNG & nitrogen production depending on market Varying feed composition & need for low CH 4 loss in waste gas Internal motor or external motor.
25 LNG liquefaction experience in Poland Tractebel Project to increase cold production in two nitrogen rejection plants. Result is 60 TPD LNG. Novel process scheme. A first in the world!! More difficult than BOG re-liquefaction. EBARA Expansion turbine with flashing flow on two units. Successful project with test run completed in 2004.
26 Main Elements of the Expander (EBARA) Generator Submerged generator on a common shaft insulated / superior dielectric Expander nozzle ring (rotational fluid flow) runner (radial flow) two-phase jet exducer symmetrical flow with vertical rotational axis - assures low vibration level lubrication for the bearings from simple internal system Thrust Equalisation Mechanism (TEM) provides complete thrust balance through whole range from 1- to 2-phase flow Full Containment in pressure vessel rated at inlet pressure
27 Exducer wheels in Aluminium (EBARA)
28 Model of initial expansion wheel (EBARA) Expansion across a jet exducer with helical fluid passages for vapour formation
29 3-D View of 2-Phase expander (EBARA) Exducer 1 st Expander Wheel Electric Motor
30 Turbine before insertion into casing (EBARA)
31 Location of Turbine.
32 2-phase flow upwards 30 metres.
33 Assessment of Power/Cold Production. Hydraulic Power available is about 65kW In practice 79kW 85kW extracted at generator terminals. In Two-phase terms vapour expansion also contributes energy. HYSYS simulation suggests potential power available is over 100kW. Therefore, could do even better!
34 Incremental LNG Production Economics. Assumptions: LNG cost is at least 5$/MMBtU 2-trains produce 60 TPD LNG Power Produced is about 80kW per train i.e. 160kW. Investment is less than 4$ million. LNG Production yields over 2 million $/year. Payback in the region of 1 year. Greater Plant flexibility. Reduced emissions.
35 Conclusions. Economics was favourable for LNG production and overall plant flexibility. Several different tests were done for expander wheels to improve efficiency. Gas expansion energy from flashing flow can be effectively converted to power/cold production. TGE has an economic solution and broad technical experience to implement such schemes elsewhere. There is scope for improving the efficiency.
36 Truck loading at small land-based LNG plants.
37 Thank you for your attention. Questions welcome
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