Downloaded 70 times
![MASS AND ENERGY BALANCE – ENERGY BALANCE
(Source: Author’s personal data)
[Energy In] – [Energy Out] = [Accumulation of energy]
∆𝐸 = 𝑚𝑖 𝐻 + 𝐸𝑘 + 𝐸𝑝 − 𝑚𝑜 𝐻 + 𝐸𝑘 + 𝐸𝑝 − 𝑄 + 𝑊
Inlet Stream
Heat Flow
(MJ/h)
Outlet Stream
Heat Flow
(MJ/h)
Seawater 77,423.15 Injected Seawater 17 36,322.63
NaOCl 18 0.01 Oxygen 10 0.06
Pump 1 191.16 Backwash 8 32,783.85
Pump 2 60.19 Utility Water 3 9,313.59
Oxygen
Scavanging
Chemical
12 0.36
Calcium Nitrate 13 2.63
Biocide 14 0.38
Corrosion
Inhibitor
15 2.99
Total 78,427.17 Total 78,421.69
Pump 3 746.28 Sludge 4 1.56](https://image.slidesharecdn.com/pptassgn1-160318060529/75/Ppt-assgn-1-34-2048.jpg)
More Related Content
Ppt assgn 1
- 1. Problem Solving : WaterFlood for Oil Production GROUP 11 ALIF NUZULUL HIDAYAT (1206249832) DIDIK SUDARSONO (1206242555) ENI MULYATININGSIH (1206201971) RAHGANDA (1206261182) SYLVIA AMANDA S (1206241230)
- 2. OUTLINE INTRODUCTION (Background, Project Objective,Plant Condition, Basic Theory) PROCESS SYNTHESIS (Alternative Process, Process Selection, Process Description, BFD, PFD) MASS AND ENERGY BALANCE (Mass Balance, Energy Balance, Simulation)
- 3. INTRODUCTION - BACKGROUND •Reservoir pressure in Kerisi has started to decline Enhanced Oil Recovery (EOR) will be conducted to lift the remaining oil in the well. • Based on studies by ConocoPhillips, EOR method chosen for Kerisi field is waterflood. • Waterflood will be done by injecting seawater taken from well K-14 to K-13 well. • Oil and gas reservoir that will be injected by seawater contains no H2S gas • Waterflood by injecting seawater into the formation will lower the temperature of the reservoir to a temperature level that is conducive to the SRB activity
- 4. INTRODUCTION - BACKGROUND •Two methods of seawater pre-treatment to be considered today are sulphate removal membrane and nitrate injection. • The selection is not only based on its ability to reduce H2S in the product, but also considering the limited space available on the platform and also the cost required to install the pre-treatment facility.
- 5. INTRODUCTION – PROJECTOBJECTIVE • To make a preliminary design of a seawater treatment plant to meet the specifications of seawater injected into the well K-13 in order to perform the waterflood to reservoir. • To choose the most appropriate method to avoid the formation of H2S by SRB which are the main problem that can occur due to the waterflood • To estimate the cost required to install the process facilities which are needed for seawater treatment
- 6. INTRODUCTION – PLANTCONDITION
- 7. INTRODUCTION – PLANTCONDITION
- 8. INTRODUCTION – PLANTCONDITION Component Concentration in raw seawater K1+, mg/l 293 Na1+, mg/l 10493 Mg2+, mg/l 1150 Ca2+, mg/l 351.1 Cl1-, mg/l 18387 SO4 2-, mg/l 2671 HCO3 1-, mg/l 93 TDS, mg/l 33458 pH 8.3 TSS, mg/l 15-20 Temp., °C 20 Oxygen, mg/l 5-8
- 9. INTRODUCTION – BASICTHEORY
- 10. INTRODUCTION – BASICTHEORY
- 11. INTRODUCTION – BASICTHEORY Mechanism of Sulfate Reducing Bacteria (SRB) Dissimilatory sulfate reduction occurs in three steps: • Conversion (activation) of sulfate to Adenosine 5’-phosphosulfate (APS) • Reduction of APS to sulfite • Reduction of sulfite to sulfide
- 12. PROCESS SYNTHESIS Basic Mechanism AlternativeProcess : • Sulfate Removal Membrane • Nitrate Injection
- 13. PROCESS SYNTHESIS -SULFATE REMOVAL MEMBRANE • Objective: reduce sulphate as main food supply for SRB
- 14. PROCESS SYNTHESIS -SULFATE REMOVAL MEMBRANE • The process for removing sulfate ions from seawater is based on nano- filtration (NF) membrane separation. • NF is a membrane process that selectively removes sulfate ions to produce seawater with low concentration sulphate (20-40 ppm).
- 15. PROCESS SYNTHESIS -SULFATE REMOVAL MEMBRANE Advantages Disadvantages • High quality injection ion sulphate from water • Reduction in need for biocides • Reduction of scaling • More effective squeeze treatments • Assists control of bacterial (sulphate reducing bacteria) well souring • Lower operating costs and increases productivity • Degrade very quickly upon exposure to free chlorine • Use of DBNPA or equivalent biocide be considered to prevent biological fouling. • Must add anti-scale to prevent calcium scaling. • Need high CAPEX to buy the sulphate removal membrane. • < 40 mg/L ion sulphate CAPEX is $20MM USD • < 30 mg/L ion sulphate incremental CAPEX $103,000 USD; need higher spec membrane.
- 16. PROCESS SYNTHESIS –NITRATE INJECTION Facilities Process 1. Added NaOCl in order 2. Passing through course filter (range 50 - 2000 μm. 3. Passing through Multimedia filter (<40 micron) 4. Oxygen Scavenger or de-aeration 5. Injection of chemical compounds: • Nitrate • Biocide • Corrosion inhibitor • Objective : bio-competition, to reduce food supply for SRB
- 17. PROCESS SYNTHESIS –NITRATE INJECTION Advantages Disadvantages • Cheap nitrate price, around 30 US Dollar per ton to get 45% of Ca(NO3)2. • Can clean soured reservoir with gradually injection up to 100 ppm nitrate ion to facilities. • Simple usage, • Safe to use, not caused damage to environment and potential for microbial EOR. • Water treatment facilities need to be constructed with non-iron material. • Reservoir performance can be lower as there is permeability reduction to bacterial colonies in critical flow passages. • There are no significant dosage of nitrate for injection and also every well will has different dosage depend on condition
- 18. PROCESS SYNTHESIS –PROCESS SELECTION Rating Criteria Performance to Prevent H2S Production Space Required Corrosion Effect to Sub-Surface Facilities Easy to Operate Investment Cost Environment Effect Weight (%) 30 25 15 10 15 5 1 More than 600 ppm H2S concentration in 10 year Require very large spacing ( > 4000 m2), so must require expansion platform Contain corrodent (O2, acid, bacteria) and electrolyte with high concentration Cannot operate automatic, always change parameter of composition in chemical injection and often maintenance More than $40 million Very dangerous for environment, chemical injection is strongly hazardous and explosive 2 600 ppm-300 ppm H2S concentration in 10 year Require large spacing (4000 - 3000 m2), so must require expansion platform Contain corrodent (O2, acid, bacteria) with low concentration and electrolyte with high concentration Cannot operate automatic, sometime change parameter of composition in chemical injection and often maintenance $40 million - $30 million Dangerous for environment, chemical injection is strongly hazardous 3 300 ppm -100 ppm H2S concentration in 10 year Require middle spacing (3000- 2000 m2), so must require expansion platform Contain corrodent (O2, acid, bacteria) and electrolyte with low concentration Cannot operate automatic, sometime change parameter of composition in chemical injection and seldom maintenance $30 million - $20 million Less dangerous for environment, chemical injection is bit hazardous
- 19. PROCESS SYNTHESIS –PROCESS SELECTION Rating Criteria Performance to Prevent H2S Production Space Required Corrosion Effect to Sub-Surface Facilities Easy to Operate Investment Cost Environment Effect Weight (%) 30 25 15 10 15 5 4 100 ppm -50 ppm H2S concentration in 10 year Require narrow spacing (2000- 1000 m2), not require expansion platform Not contain corrodent (O2, acid, bacteria), but contain electrolyte Can operate automatic, sometime change parameter of composition in chemical injection and seldom maintenance $20 milion - $10 milion No-negative environmental . chemical injection is less hazardous 5 Less than 50 ppm H2S concentration in 10 year Require very narrow spacing (< 1000 m2), not require expansion platform Not contain corrodent (O2, acid, bacteria) and electrolyte Can operate automatic, seldom change parameter of composition in chemical injection and seldom maintenance Less than $10 milion No-negative environmental . chemical injection is not hazardous
- 20. PROCESS SYNTHESIS –PROCESS SELECTION Parameter Weight (%) Sulphate Removal Membran Weight Score Nitrate Injection Weight Score Performance to prevent H2S production 30 5 1.5 4 1.2 Space required 25 2 0.5 4 1 Prevent corrosion on sub-surface Facilities 15 4 0.6 2 0.3 Investment Cost 15 2 0.3 4 0.6 Ease to Operate 10 2 0.2 4 0.4 Environment Effect 5 4 0.2 5 0.25 Total 100 3.3 3.75
- 21. PROCESS SYNTHESIS -BLOCK FLOW DIAGRAM Figure 2.17. Vacuum Stripping De-aeration
- 22. PROCESS SYNTHESIS -PROCESS DESCRIPTION Capacity waterflood : 50.000 barrel or 339000 kg/h Capacity seawater : 741000 kg/h Waterflood Characteristic
- 23. PROCESS SYNTHESIS -PROCESS DESCRIPTION 1. Pre-Primary Filtration • Basin is a reservoir of seawater to be pumped. • Basin serves to prevent floating dirt is not carried into seawater lift pump. • A deeper intake is aim to get sea- water that contain low TSS, low oxygen, low temperature and consistent water quality • In basin, seawater is injected sodium hypochlorite (𝑁𝑎𝑂𝐶𝑙) that is produced in hypochlorite generator. Figure 2. 8. Basin Structure for Pre-Primary Filtration
- 24. PROCESS SYNTHESIS -PROCESS DESCRIPTION 1. Pre-Primary Filtration • Raw material : Seawater • Process : Electrolysis (In Situ) Anode : 2𝐶𝑙− → 𝐶𝑙2 + 2𝑒− Cathode : 2𝑁𝑎+ + 2𝐻2 𝑂 + 2𝑒− + 𝐶𝑙2 → 2𝑁𝑎𝑂𝐶𝑙 + 2𝐻2 Overall : 𝑁𝑎𝐶𝑙 + 𝐻2 𝑂 → 𝑁𝑎𝑂𝐶𝑙 + 𝐻2 Figure 2. 9. Hypochlorite Generator
- 25. PROCESS SYNTHESIS -PROCESS DESCRIPTION 2. Primary Solid Removal • Remove suspended solid (> 100 µm) with 98% efficiency. • Type : Dead End Filtration • Flow capacity up to 2270 GPM (619 m3/h) • If pressure drop is high, flush process start to clean the solid that is restrained. • Flush process can operate automatic. Raw Water Inlet Filtered Water Outlet Sludge Outlet Figure 2.10. Coarse Strainer Unit
- 26. PROCESS SYNTHESIS -PROCESS DESCRIPTION 3. Secondary Solid Removal • Remove suspended solid (> 2 µm) with 98% efficiency. (high turbidity in seawater) • Type : Granular Filtration • Flow capacity up to 425 m3/h • Backwash : Clean the bed, High pressure drop • The ideal backwash rate is 250-450 m3/h. Figure 2.11. Multi Media Unit Raw Water Inlet Filtered Water Outlet Sludge Outlet Backwash Inlet Anthracite Fine Garnet Coarse Garnet
- 27. PROCESS SYNTHESIS -PROCESS DESCRIPTION 4. De-aeration • Remove oxygen in seawater (< 50 ppb) • Type : Vacuum Stripping De-aeration • Equipment : De-oxygenation tower, Ejector, Vacuum Pump, Separator. • Principle : o Partial pressure of oxygen in water is a function of the total pressure of the system. o Vacuum the system can reduce the partial pressure of oxygen and make driving force for mass transfer of oxygen from the liquid to the gas phase. Figure 2.17. Vacuum Stripping De-aeration
- 28. PROCESS SYNTHESIS -PROCESS DESCRIPTION 6. Chemical Injection Package Chemical Dosage Treatment Application Injection Point Scale Inhibitor 20 ppm First, 200.000 bbls of water injection Inhibits CaCO3 scale Discharge seawater lift pump Calcium Nitrate 100 ppm Continuous Microbial control by bio-competition Suction of water injection pump Biocide THPS 200 ppm Batch, Once a week for 4 hours Microbial control Suction of water injection pump Oxygen Scavenger 10 ppm Continuous, Reduce oxygen to low concentration Exit of de-aerator Corrosion Inhibitor 30 ppm Continuous, To prevent corrosion in subsurface facilities Suction of water injection pump
- 29. PROCESS SYNTHESIS -PROCESS FLOW DIAGRAM
- 30. PROCESS SYNTHESIS -PROCESS FLOW DIAGRAM Streams 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 Mass Flow Rate (kg/h) 741,523 741,498 88,979 24.22 339,309 339,308 33,058 33,060 339,305 2.66 339,305 4.79 40.48 1.79 32.41 339,384 339,384 Pressure (bar) 7.10 7.01 7.01 7 7.01 7.01 1.01 1.01 7.10 7.10 17.01 1.01 1.01 1.01 1.01 1.01 125.01 Temperature (C ) 25.06 25.06 25.06 25.10 25.06 25.06 25.00 25.00 25.06 25.06 25.10 25.00 25.00 25.00 25.00 25.10 25.63 Alga (% mass) 0.0005 0.0005 0.0005 0.0003 0.0005 0.0000 - 0.0049 0.0000 - 0.0000 - - - - 0 0 Solid (% mass) 0.0015 0.0000 0.0000 10.9000 0.0000 0.0000 - 0.0003 0.0000 - 0.0000 - - - - 0 0 TDS (% mass) 3.25 3.25 3.25 0.43 3.25 3.25 3.25 3.25 3.25 - 3.25 - - - - 3.24 3.24 NaOCl (% mass) 0.00001 0.00000 1 0.000001 0.000001 0.000001 0.00000 - - 0.00000 - 0.00000 - - - - 0 0 Oxygen (% mass) 0.0008 0.0008 0.0008 0.0000 0.0008 0.0008 0.0008 0.0008 0.0000 100.00 0.0000 - - - - 0 0 Water (% mass) 96.74 96.74 96.74 53.21 96.74 96.74 96.74 96.74 96.74 - 96.74 - - - - 96.74 96.74 Na2SO3 (%mass) - - - - - - - - - - - 40 - - - 0.0006 0.0006 Water (% mass) - - - - - - - - - - - 60 - - - - - Ca(NO3)2 (% mass) - - - - - - - - - - - - 45 - - 0.0054 0.0054 Water (% mass) - - - - - - - - - - - - 55 - - - - THPS (% mass) - - - - - - - - - - - - - 50 - 0.0003 0.0003 Water (% massa) - - - - - - - - - - - - - 50 - - - Cyclo-hexylamine (% mass) - - - - - - - - - - - - - - 13 0.0012 0.0012 Morpholin (% mass) - - - - - - - - - - - - - - 7 0.0007 0.0007 Water (% mass) - - - - - - - - - - - - - - 80 - -
- 31. PROCESS SYNTHESIS -PROCESS FLOW DIAGRAM
- 32. MASS AND ENERGYBALANCE – MASS BALANCE Mass Balance Inlet for Overall Processes Inlet Stream Mass Flow (kg/hr) Inlet Component Mass Flow (kg/hr) Seawater (Feed) 741,522.87 H2O 717,402.61 Oxygen 5.93 Dissolved Solid 24,099.49 Suspended Solid 14.83 NaOCl 18 0.23 NaOCl 0.23 Chemical Injection Package 12 79.47 Oxygen Scavenging Chemical 4.79 Calcium Nitrate Solution 40.4813 Biocide Solution 1.7914 15 Corrosion Inhibitor 32.41 Total 741,602.57 (Source: Author’s personal data)
- 33. MASS AND ENERGYBALANCE – MASS BALANCE Mass Balance Outlet for Overall Processes (Source: Author’s personal data) Outlet Stream Mass Flow (kg/hr) Outlet Components Mass Flow (kg/hr) Injected Seawater 16 339,384.98 H2O 328,329.49 Oxygen 0.05 Dissolved Solid 11,055.34 Suspended Solid 0.09 Oxygen 10 2.66 Oxygen 2.66 Utility Water 3 88,979.86 H2O 86,086.77 Oxygen 0.71 Dissolved Solid 2,891.91 Suspended Solid 0.47 Disposed Seawater 313,235.06 H2O 303,038.31 4 and 8 Oxygen 2.51 Dissolved Solid 10,179.97 Suspended Solid 14.27 Total 741,602.56
- 34. MASS AND ENERGYBALANCE – ENERGY BALANCE (Source: Author’s personal data) [Energy In] – [Energy Out] = [Accumulation of energy] ∆𝐸 = 𝑚𝑖 𝐻 + 𝐸𝑘 + 𝐸𝑝 − 𝑚𝑜 𝐻 + 𝐸𝑘 + 𝐸𝑝 − 𝑄 + 𝑊 Inlet Stream Heat Flow (MJ/h) Outlet Stream Heat Flow (MJ/h) Seawater 77,423.15 Injected Seawater 17 36,322.63 NaOCl 18 0.01 Oxygen 10 0.06 Pump 1 191.16 Backwash 8 32,783.85 Pump 2 60.19 Utility Water 3 9,313.59 Oxygen Scavanging Chemical 12 0.36 Calcium Nitrate 13 2.63 Biocide 14 0.38 Corrosion Inhibitor 15 2.99 Total 78,427.17 Total 78,421.69 Pump 3 746.28 Sludge 4 1.56
- 35. MASS AND ENERGYBALANCE – ENERGY BALANCE Mass Efficiency Energy Efficiency
- 36. NEED FOR MASSAND ENERGY To produce 50,000 BWPD for waterflood, it needs 108,667 barrels water per day in the feed, and 3 pumps with total power 1669 kW
- 37. MASS AND ENERGYBALANCE – SIMULATION • Using SuperPro
- 38. CONCLUSION 1. Process ofEnhanced Oil Recovery (EOR) will be conducted to lift the remaining oil from Kerisi well with water flood method. 2. Design for the process need to meet criteria such as reduce amount of content that may cause problem in well like TSS, sulphate ion, and oxygen from seawater, facilities can be placed on available area and should be as economical as possible. 3. Parameters that will be used in process selection are performance to prevent H2S production, space limited, corrosion effect, investment cost and environment. 4. Process selected for seawater for injection well is nitrate injection process which is used calcium nitrate with concentration 100 ppm to process water. 5. There are several main section of this plant as follow pre-primary filtration, primary solid removal with coarse strainer, secondary solid removal with multimedia filter, de-aeration and chemical injection package. 6. We simulate the overall process using SuperPro Software and processing the data to calculate mass and energy balance. It needs 108,667 barrels water per day or equivalent to 741,522 kg/h to produce 50,000 barrels water per day to fullfill demand of waterfloods in the oil well. For energy needs, we will have three pumps with total power 1669 kW.
- 39. Injection of 50,000bpd of seawater will lik ely increase the H2S level in the productio n system to around 600 ppmv in 10 years. The increase of H2S is caused by several factors: Decrease in Reservoir temperature over time. High (dissolved organic carbons) DOC in produced water. High Sulphate in the Seawater. Bacteria availability from the seawater.
- 40.