ISSUED BY DEP-VSL-00002 RPP-WTP PDC...DEP-VSL-00002 is equipped with mixing eductors to homogenize...

24590-BOF-NlD-DEP-00002 Rev.1 I

CORROSION EVALUATION ISSUED BY Ill I llllll 111111111111111111

DEP-VSL-00002 Evaporator Feed Vessel

RPP-WTP PDC Appurtenances

DEP-EDUC-00001 NB/C

Contents of this document are Dangerous Waste Permit affecting

Results

Materials Considered: Material

(UNS No.) Carbon Steel Type 304L (S30403) Type 316L (S31603) Al-6XN® 6% Mo (N08367l Hastellov® C-22® (N06022)

Recommended Material Type:

Minimum Corrosion Allowance:

Inputs and References

Acceptable Material

X X

Vessel - Al-6XN® 6% Mo (N08367) Eductors - Al-6XN® 6% Mo (N08367)

0.04 inch (includes 0.024 inch corrosion allowance and 0.004 inch general erosion allowance)

• Operating Temperature (°F) (nom/max): 124/166 (24590-BOF-MVC-DEP-00003) • Design corrosion allowance (inch): 0.04 (24590-WTP-M0C-50-00004) • Uniform corrosion allowance (inch): 0.024 (24590-WTP-M0E-50-00012) • Uniform erosion allowance (inch): 0.004 (24590-WTP-M0C-50-00004) • Location: Room E-0105 (24590-BOF-Pl-25-00001)

R11873325

• Operating conditions are as stated in the applicable section of Direct Feed LAW Process Corrosion Data (24590-BOF-RPT-PR- l 5-00 I)

Assumptions and Justification (refer to Section I 9-References) • Source data presented on the Process Corrosion Datasheet (PCDS) are conservative with respect to corrosion. 3

• The liquid in the vessel is assumed to have the physical properties of water 1

• Sampling capability is provided; mixing of the vessel contents is done prior to sampling. 1

• SM sodium hydroxide is added to DEP-VSL-00002 from SHR-TK-00013 to achieve a pH of 12 in DEP-VSL-00002. 1

Operating Restrictions • To protect against localized corrosion in the vessel and transfer piping, develop procedure to bring the vessel contents to within the

limits defined for AL-6XN® in 24590-WTP-RPT-M-11-002, WTP Materials Localized Corrosion Design Limits, in the event that temperature, pH, or chloride concentration exceeds those limits.

• Develop a procedure to control, at a minimum, cleaning, rinsing, and flushing of vessel and internals, as applicable. • Develop procedure to control lay-up and storage; includes both before plant is operational arid during inactive periods after start-up. • Procedures are to be reviewed and accepted by MET prior to use.

Concurrence TD Operations

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forward to the next revision DLAdler APRangus RBDavis TErwin 0 9/22/16 Initial Issue DLAdler APRangus RBDavis TErwin

REV DATE REASON FOR REVISION ORIGINATE CHECK REVIEW APPROVE

Sheet: 1 of 15

24590-BOF-NlD-DEP-00002 Rev.1

CORROSION EVALUATION

Please note that source, special nuclear and byproduct materials, as defined in the Atomic Energy Act of 1954 (AEA), are regulated at the U.S. Department of Energy (DOE) facilities exclusively by DOE acting pursuant to its AEA authority. DOE asserts, that pursuant to the AEA, it has sole and exclusive responsibility and authority to regulate source, special nuclear, and byproduct materials at DOEowned nuclear facilities. Information contained herein on radionuclides is provided for process description purposes only.

DEP-VSL-00002: Sheet: 2 of 15

This bound document contains a total of 15 sheets.


Corrosion/Erosion Detailed Discussion

24590-BOF-NlD-DEP-00002 Rev. I

DEP-VSL-00002 receives filtered effluent from DEP-FIL T-00003, sodium hydroxide from SHR-TK-00013 for pH adjustment, off-spec recycled concentrate from DEP-VSL-00003A/B/C, off-spec recycled condensate from DEP-VSL-00004A/B, and off-spec secondary condensate from the Reboiler Condensate Collection Vessel (DEP-VSL-00008). DEP-PMP-00002A/B are used to transfer DEP-VSL-00002 contents to DEP-EVAP-00001. In the event of an overflow, the liquid will flow by gravity into DEP-VSL-00001.

DEP-VSL-00002 is equipped with mixing eductors to homogenize the contents and allow a representative sample to be taken. The eductors receive fluid from DEP-PMP-00012A/B/C and will operate during mixing. If necessary, DEP-PMP-00012A/B/C are also used to return the contents ofDEP-VSL-00002 to the Tank Farms passing through DEP-HX-00001.

The vessel contents can be sampled and pH can be adjusted by adding sodium hydroxide. The vessel is monitored for level, pressure, and temperature. This vessel will have capability to add demineralized water for washing.

1 General/Uniform Corrosion Discussion

a Background General or uniform corrosion is corrosion that is distributed uniformly over the surface of a material without appreciable localization. This leads to relatively uniform thinning on sheet and plate materials and general thinning on one side or the other (or both) for pipe and tubing. It is recognized by a roughening of the surface and usually by the presence of corrosion products. The mechanism of the attack typically is an electrochemical process that takes place at the surface of the material. Differences in composition or orientation between small areas on the metal surface create anodes and cathodes that facilitate the corrosion process.

b Component-Specific Discussion The vessel normally contains filtered effluent at nominal operating temperature range of 124 °F (166 °F max) at pH 12. Based on the expected normal operating conditions, the 300 series stainless steels are not suitable. A more corrosion-resistant 6% Mo alloy, such as AL-6XN®, is recommended. The contents are not left stagnant; eductors are used to provide mixing of the vessel contents. Under these conditions, the uniform corrosion rate is low.

2 Pitting Corrosion Analysis

Pitting is localized corrosion of a metal surface that is confined to a point or small area and takes the form of cavities. According to Dillon (2000), in alkaline solutions, pH > 12, chlorides are likely to promote pitting only in tight crevices. Normally the vessel is to operate at 124 °F (166 °F max); pH 12 is maintained. Material localized corrosion design limits to protect against localized corrosion by other constituents (like fluoride) are not required because of their lower potential for life limiting corrosion in WTP application (24590-WTP-RPT-M-11-002, WTP Materials Locali=ed Corrosion Design Limits). The vessel is operated such that conditions do not promote pitting corrosion; the solution in the vessel is not left stagnant.

The chemistry and operating conditions in this vessel fall within the limits established for AL-6XN®, in Table 1-3 24590-WTP-RPT-M-11-002. For convenience, this comparison is documented on page 6 of this corrosion evaluation.

3 Crevice Corrosion Analysis

Crevice corrosion is a form of localized corrosion of a metal or alloy surface at, or immediately adjacent to, an area that is shielded from full exposure to the environment because of close proximity of the metal or alloy to the surface of another material or an adjacent surface of the same metal or alloy. Crevice corrosion is similar to pitting in mechanism.

Crevices in this vessel are limited by the design and fabrication practice. All welding uses butt welds and crevices are limited to wash ring hangers and other internals. With the stated operating conditions, a 6% Mo alloy would be the minimum acceptable.

The expected chemistry and temperature in this vessel fall within the limits for localized corrosion established for AL-6XN® in Table 1-3 of24590-WTP-RPT-M-l l-002.

4 Stress Corrosion Cracking Analysis

Stress corrosion cracking (SCC) is the cracking of a material produced by the combined action of corrosion and sustained tensile stress (residual or applied). The exact amount of chloride required to cause SCC is unknown. In part this is because the necessary concentration varies with temperature, metal sensitization, and the environment; also, chloride tends to concentrate under heat transfer conditions and by evaporation. Hence, even concentrations as low as IO ppm can lead to cracking under some conditions. With the proposed normal conditions, a 6% Mo alloy is expected to be the minimum acceptable.

The chemistry and operating conditions in this vessel fall within the limits established for 6% Mo alloy (AL-6XN®) in Table 1-3 of24590-WTP-RPT-M-l l-002.

5 End Grain Corrosion Analysis

End grain corrosion is preferential corrosion which occurs along the cold working direction of wrought stainless steels when exposed to highly oxidizing acidic conditions. Such conditions are not present in the pressure boundary design and nozzles; vessels are all butt-weld joints. End grain corrosion is not a concern for the vessel pressure boundary materials.

DEP-VSL-00002: Sheet: 3 of15


6 Weld Corrosion Analysis


The welds used in the fabrication will follow the WTP specifications and standards for quality workmanship. The materials selected for this fabrication are compatible with the weld filler metals and ASME/ A WS practice. Using the welding practices specified for the project, there should not be gross micro-segregation, precipitation of secondary phases, formation of unmixed zones, or volatilization of the alloying elements that could lead to localized corrosion of the weld. The low carbon materials specified for WTP prevent base metal sensitization during welding. Controls on the cover gas, heat input, and interpass temperature limit the heat tint. Welding procedure review will confirm appropriate weld filler metal is specified. Corrosion at welds is not considered a problem in the proposed environment. No additional allowance is made for weld bead corrosion.

7 Microbiologically Influenced Corrosion Analysis

Microbiologically influenced corrosion (MIC) refers to corrosion affected by the presence or activity, or both, of microorganisms. Typically, with the exception of cooling water systems, MIC is not observed in operating systems. The proposed operating conditions are not ideal for microbial growth; therefore, the potential for MIC in the vessel is small.

8 Fatigue/Corrosion Fatigue Analysis

Fatigue is the process of progressive localized permanent structural change occurring in a material subjected to fluctuating stresses less than the ultimate tensile strength of the material. Corrosion fatigue is the process wherein a metal fractures prematurely under conditions of simultaneous corrosion and repeated cyclic loading at lower stress levels or fewer cycles than would be required to cause fatigue of that metal in the absence of the corrosive environment. Corrosion fatigue is a function of the cyclic loading and corrosive conditions. The vessel design is such that fatigue loads adhere to design code limitations.

Based on the anticipated low mechanical and thermal cycling, it can be stated that conditions which leads to fatigue or corrosion fatigue are not present in this vessel.

9 Vapor Phase Corrosion Analysis

Conditions in the vapor phase and at the vapor/liquid interface can be different than those present in the liquid. The vapor space corrosion is self-limiting due to the passive film. Also, the layers of deposited corrosion product on top of the passive film act as barriers that reduce mass transport necessary for corrosion. Corrosion rates of materials exposed to vapors in the headspace are never greater than the corrosion during immersion service. The corrosion at the liquid air interface (LAI) is an oxygen-concentration cell resulting from the alternate wetting and drying occurring at the interface. Vessels that operate at the same liquid level and form a surface crust are more susceptible to LAI corrosion. Corrosion at the LAI could be similar to immersion service and not greater. WTP vessels also have the protective passive film at the LAI which reduces corrosion. Further, the liquid level fluctuates between the minimum and maximum level, rather than maintaining a constant level. As compared to the corrosion in the immersion section, the corrosion rates in the vapor space are lower. Vapor phase corrosion is not a concern.

10 Erosion Analysis

Erosion is the progressive loss of material from a solid surface resulting from mechanical interaction between that surface and a fluid, a multi-component fluid, or solid particles carried with the fluid. The concentration of particles, particle size, and particle velocity are key considerations when considering erosion degradation. Based on the low concentrations, small size, and low velocities in the stream received from the offgas submerged bed scrubber and associated condensate collection vessels through DEP-FIL T-00003, it can be concluded that the erosion losses are bounded by the 0.004 erosion allowance.

Velocities within the vessel are expected to be below 12 ft/s. The erosion allowance of0.004 inch for Type 304L and 3 I 6L stainless steel components with low solids content(< 2 wt%) at velocities up to 12 ft/sis based on 24590-WTP-M0C-50-00004, Wear Allowance for WTP Waste Slurry Systems. Since the AL-6XN® alloy is stronger and harder than the austenitic stainless steels, the erosive wear allowance used for the austenitic stainless steel is conservative when used for AL-6XN® (24590-WTP-M0E-50-000I2, Calculation of Wear Rates for Piping Containing Waste Streams of Weighted Mean Particle Diameter of 2 4 Microns).

11 Galling of Moving Surfaces Analysis

Where two metals are moving in contact with each other without lubrication, there is a risk of damage to their surfaces. No moving unlubricated surfaces are present within the vessel; therefore, galling is not a concern.

12 Fretting/Wear Analysis

Fretting corrosion refers to corrosion damage caused by a slight oscillatory slip between two surfaces. Similar to galling but at a much smaller movement, the corrosion products and metal debris break off and act as an abrasive between the surfaces, producing a classic three body wear problem. This damage is induced under load and repeated relative surface motion. Conditions which lead to fretting are not present in this vessel.

13 Galvanic Corrosion Analysis

Galvanic corrosion is accelerated corrosion caused by the potential difference between the two dissimilar metals in an electrolyte. A potential difference of greater than 200 m V is necessary to drive corrosion. One material becomes the anode and the other the cathode. Corrosion occurs on the anode material at the interface where the potential gradient is the greatest. The potential difference for any




combination of alloys used in these vessels is not sufficient for galvanic currents to overcome the passive protective film. Therefore, it can be stated that conditions which lead to galvanic corrosion are not present in this vessel.

14 Cavitation Analysis

Cavitation is the formation and rapid collapse of cavities or bubbles of vapor or gas within a liquid resulting from mechanical or hydrodynamic forces. Cavitation is typically associated with pumps and orifice plates; this vessel has neither. The alloys selected display a superior resistance to cavitation, and WTP vessel design limits conditions which lead to cavitation; therefore, cavitation is not a concern.

15 Creep Analysis

Creep is time-dependent strain occurring under stress and is described as plastic flow, yielding at stresses less than the yield strength. Creep is only experienced in plants operating at high temperatures. Temperatures much greater than one half the absolute melting temperature of the alloy are necessary for thermally activated creep to become a concern. The vessel operating and design temperatures are too low to lead to creep; therefore, creep is not a concern.

16 Inadvertent Nitric Acid Addition

At this time, the design does not provide for the regular use of nitric acid reagent in this system. Addition of nitric acid into the system would require operator intervention to complete the routing. Nitric acid is a known inhibitor solution for austenitic stainless steels and nickel-based alloys. The presence of nitric acid is not a concern for the stainless steel; especially at the operating temperatures listed.

17 Conclusion and Justification

The conclusion of this evaluation is that DEP-VSL-00002 can be fabricated from AL-6XN® and is capable of providing 40 years of service. Based on the expected operating conditions, AL-6XN® is expected to be satisfactorily resistant to uniform and localized corrosion. The recommended corrosion allowance of0.024 inch and the recommended erosion allowance of0.004 inch provide sufficient protection against uniform corrosion and erosion of the vessel. A design corrosion allowance of0.04 inch is recommended, which exceeds the corrosion and erosion allowances identified in 24590-WTP-M0C-50-00004 and 24590-WTP-RPT-M-04-0008, Evaluation of Stainless Steel and Nickel Alloy Wear Rates in WTP Waste Streams at Low Velocities.

Based on comparison of the process conditions documented in 24590-WTP-RPT-PR-04-0001-07 against the limits for AL-6XN® documented in 24590-WTP-RPT-M-11-002. The PCDS values, which take into account conditions at contract maximum values, are within the applicable limits.

Sections of the issued Process Corrosion Data report (PCDS) (attached to the corrosion evaluation) include several references to the Process Inputs Basis of Design (PI BOD) for LAW and EMF. 24590-WTP-DB-PET-17-001 which was not issued at the time the PCDS was issued. The PIBOD for LAW and EMF has been issued. Any variance in the values between the PIBOD and PCDS associated with streams and stream characteristics used to evaluate corrosion and erosion have been reviewed and evaluated. The evaluation concluded that the analysis described in this corrosion evaluation was bounding and the material selection recommendations remain as initially issued.

Conditions leading to localized erosion are not present; therefore, no localized erosion allowance is identified.

18 Margin

The system is designed with a total design corrosion allowance of0.04 inch based on the range of inputs, system knowledge, handbooks, literature, and engineering judgment/experience. The service conditions described above result in a predicted loss due to uniform corrosion and erosion of0.028 inches. The specified design corrosion allowance (0.04 inch) exceeds the minimum required corrosion allowance specified in the input calculations; therefore, margin is provided. The uniform corrosion design margin for the operating conditions is sufficient to expect a 40 year operating life and is justified in the referenced calculations.

The recommended general erosion wear allowance of0.004 inch provides sufficient protection for erosion of the vessel shell. The margin in the erosive wear allowances used above is contained in the referenced calculations (24590-WTP-M0C-50-00004 and 24590-WTP-M0E-50-00012). No additional localized erosion requirement has been identified for these vessels.

The maximum operating parameters for these vessels are defined in the PCDS. As shown in the table on the next page, the PCDS calculated pH, chemistry, and temperature are bounded by the materials localized corrosion design limits documented in the WTP Materials Localized Corrosion Design Limits report. The difference between the design limits and the operating maximums (PCDS value) is the localized corrosion design margin and, based on the operating conditions, is sufficient to expect a 40 year operating life. The Evaporator Feed Vessel, DEP-VSL-00002, is protected from localized corrosion (pitting, crevice, and stress corrosion) by operating within the acceptable range of the design limits. Operational and process restriction will be used to ensure the limits are maintained.




MATERIALS LOCALIZED CORROSION DESIGN LIMITS-AL-6XN® Temperature C°F) Chloride (ppm)

DESIGN LIMIT 212 max 25,000 max

166 12.0 8793

DESIGN LIMIT 160 max lto5 25,000 Filtered Effluent from

DEP-FILT-00003 EP03a 166 0.23 9945

Sodium Hydroxide Addition DEPII 113 14.7 0

Inlet vessels to DEP-VSL-00002 based on 24590-BOF-RPT-PR-15-001 , Section 4.3 and Figure 4.

References sources for this table:

1) Design limits-24590-WfP-RPT-M-ll-002, Table 1-3 -2) DEP-VSL-00002 (DEP02)-24590-BOF-RPT-PR-15-001, Figure A-3 3) DEP-FILT-00003 (DEP03a)-24590-BOF-RPT-PR-15-001, Figure A-2 4) Sodium hydroxide addition (DEPl 1)-24590-BOF-RPT-PR-15-001, Figure A-3



19 References:


I. 24590-BOF-MVC-DEP-00003, Process Data for the Evaporator Feed Vessel (DEP-VSL-00002), Transfer Pumps (DEP-PMP-00002AIB), and Recirculation Pumps (DEP-PMP-00012AIBIC).

2. 24590-BOF-Pl-25-00001, Balance of Facilities LAW EjJluent Process Bldg & LAW EjJluent Drain Tank Bldg General Arrangement Plan at Elev 0 Ft - 0 in.

3. 24590-BOF-RPT-PR-l 5-00I, Direct Feed LAW Process Corrosion Data. 4. 24590-WfP-DB-PET-17-001, Process Inputs Basis of Design (PJBOD)for LAW and EMF. 5. 24590-WfP-M0C-50-00004, Wear Allowance for WTP Waste Slurry Systems with ECCN 24590-WTP M0E-50-00012. 6. 24590-WfP-RPT-M-11-002, WTP Vessel locali=ed Corrosion limit Analysis Report. 7. CCN 130173, Dillon, CP (Nickel Development Institute), Personal Communication to JR Divine (ChemMet, Ltd., PC), 3 Feb 2000.

Additional Reading

• 24590-BOF-M6-DEP-00002001, P&JD - BOFIEMF - Direct Feed LAW EMF - Process System - Evaporator Feed Vessel - DEP-VSL-00002.

• 24590-BOF-MVD-DEP-00003, Mechanical Datasheetfor 24590-BOF-MV-DEP-VSL-00002 - Evaporator Feed Vessel. • 24590-WTP-RPT-M-04-0008, Evaluation of Stainless Steel and Nickel Alloy Wear Rates in WTP Waste Streams at low Velocities. • Agarwal, DC, Nickel and Nickel Alloys, In: Revie, WW, 2000. Uhlig's Corrosion Handbook, 2nd Edition, Wiley-Interscience, New

York, NY 10158 • Allegheny Technologies Incorporated. AL-6XN (UNS N08367) Technical Bulletin. Allegheny Technologies Incorporated, Pittsburgh,

PA 15222. • Berhardsson, S, R Mellstrom, and J Oredsson, 1981, Properties of Two Highly corrosion Resistant Duplex Stainless Steels, Paper 124,

presented at Corrosion 81, NACE International, Houston, TX 77218 • Blackbum, LD to PG Johnson, Internal Memo, Westinghouse Hanford Co, Evaluation of 240-AR Chloride limit, August 15, 1991. • Borenstein, SW, 1988. Microbiologically Influenced Corrosion Of Austenitic Stainless Steel, Materials Selection & Design August

1988 • Danielson, MJ & SG Pitman, 2000, Corrosion Tests of 316l and Hastelloy C-22 in Simulated Tank Waste Solutions, PNWD-3015

(BNFL-RPT-019, Rev 0), Pacific Northwest Laboratory, Richland WA. • Davis, JR (Ed), 1987, Corrosion, Vol 13, In "Metals Handbook", ASM International, Metals Park, OH 44073 • Davis, JR (Ed), 1994, Stainless Steels, In ASM Metals Handbook, ASM International, Metals Park, OH 44073 • Hamner, NE, 1981, Corrosion Data Survey, Metals Section, 5th Ed, NACE International, Houston, TX 77218 • Jones, RH (Ed.), 1992, Stress-Corrosion Cracking, ASM International, Metals Park, OH 44073 • Koch, GH, 1995, locali=ed Corrosion in Halides Other Than Chlorides, MTI Pub No. 41, Materials Technology Institute of the

Chemical Process Industries, Inc, St Louis, MO 63141 • Ohl, PC & WC Carlos, 1994, Hariford High-level Evaporator/Crystalli=er Corrosion Evaluation, Presented at Corrosion 94, NACE

International, Houston TX 77218 • Phull, BS, WL Mathay, & RW Ross, 2000, Corrosion Resistance of Duplex and 4-6% Mo-Containing Stainless Steels in FGD

Scrubber Absorber Slurry Environments, Presented at Corrosion 2000, Orlando, FL, March 26-31, 2000, NACE International, Houston TX 77218.

• Revie, WW, 2000. Uhlig's Corrosion Handbook, 2nd Edition, Wiley-Interscience, New York, NY IO 158 • Sedriks, AJ, 1996, Corrosion of Stainless Steels, John Wiley & Sons, Inc., New York, NY 10158 • Smith, H. D. and M. R. Elmore, 1992, Corrosion Studies of Carbon Steel under Impinging Jets of Simulated Slurries of Neutrali=ed

Current Acid Waste (NCA W) and Neutrali=ed Cladding Removal Waste (NCRW), PNL-7816, Pacific Northwest Laboratory, Richland, Washington.

• Uhlig, HH, 1948, Corrosion Handbook, John Wiley & Sons, New York, NY 10158 • Van Delinder, LS (Ed), 1984, Corrosion Basics, NACE International, Houston, TX 77084 • Wilding, MW and BE Paige, 1976, Survey on Corrosion of Metals and Alloys in Solutions Containing Nitric Acid, ICP-1107, Idaho

National Engineering Laboratory, Idaho Falls, ID • Zapp, PE, 1998, Preliminary Assessment of Evaporator Materials of Construction, BNF---003-98-0029, Rev 0, Westinghouse

Savannah River Co., Inc for BNFL Inc.



24590-BOF-N I D-DEP-00002 Rev. I

PROCESS CORROSION DATA SHEET (extract)

Component(s) (Name/ID#) Evaporator Feed -Vessel {DEP-VSL-00002)

Facility EMF

In Black Cell? NO

Stream ID l DEP02 Chemicals Unit AQUEOUS Cations (oom)

Al+3 (Aluminum) ppm 179

Fe+3 (Iron) DDm 194

Hg+2 (Mercury) oom 0

Pb+2 (Lead) DDm 10

Anions fnnm)

er (Chloride) oom 8793

co3-2 (Carbonate) ppm 276

F- (Fluoride) DDm 14,883

No2- (Nitrite) ppm 59

NO3- (Nitrate) ppm 264

po4-3 (Phosphate) ppm 27

s o 4-2 (Sulfate) ppm 1093

OH(aqr ppm 166

OH(sf ppm 49

pH 12.00

Suspended Solids wt% 0

Temperature Of 166.00

Liquid Density (normal) I lb/ft3 61.7


Figure A-3 DEP-VSL-00002 Aqueous PCDS

L DDIJa DD'll --..-Slll-:pc,dad Solids [wt ', J 0

) 0

Tow s.Jt, (1" '•l 1BD (2) UOE+ol

Sodium ::l<!oanl)· [Ml IllD {2) 5.00

Rmm"I Hmmi!uy l~•l , .. (2) ,u

pH 0 . .?3 (2) JUO

Alln-Fomi AJmt [ppm] 1BD (2) 0

TOC (!b:nbr] 1BD (2) TBD

~"''" [psir] 0 (2) 0

T-rure (C1 4 (2)

43

Tm,;,on""" !Fl 166 (2)

113

\\~IE Fl.o1l• lt.L., mh:r] IllD (2) TBD

Tow Aqutom Flow ltm [lbm.h:rJ TIID (2) TBD

Toal Flow R.o.te rlbm. !Jrl 1BD (

TBD

·-DE.P-nL-0000? »dlam h ·dnmdt

UwtNott C-ombmtd ,nams. oddidcm fI=I SHR-

E.P03 ad RI..D1l TK-OOOlJ.

--

DENJa D£Pll

Aqiaous-•---C•-

A,- 0 0 AH I 7ll 0

Am.+3 0 0 A,~5 0 0

S-3 6_:_ 0

Ba--e-:! 0 0 :S.,...:! 0 0

3 t-3 0 0

C1- :! I~ 0 Cd+~ 0 0

c- 2 0

Co-~ 0 0

Cr---3 20 0

C'M ~ 0

c,- 0 0

(a. ..... :! 0 0

En+-3 0 0

Fe--J 0 0

f ~3 1!4 0

H- 5~ 0

Hg-1 0 0 K~ l~S 0

l!.rJ 0 0

L:i+ 510 0

:'>lg.-? i 0 ).ill.-! . 0 '.\l.o-<S 0 0

i,:,... 10406 03332 Nd-+3 0 0 Ni- ~ ~ 0

Pb-+-1 10 0 Pd+-~ 0 0

~ 0 0 ~ 0 0

Rs- ~ 0 0 R~ 0 0

R!r.- 3 0 0

Rl:l--1 0 0 Sb+3 0 0 ~ 3 0 Si.-! 3 17 0 ~r+:! 0 0 r..-.5 0 0 I c--1 0 0 Ie-4 0 0 Tlr-1 0 0 Ti..-4 68 0

TI- 5 ! 0 U--1 0 0 V- 3 0 0

W41 0 0 y ..... 3 0 0

Z,,...2 2 17 0

Zr-I 12 0

AaialU B(OR}I- 4P 0 C Ol-? 0

Cl- 9145 0 Cl\"- 0 0

COJ-2 216 0 F- 16&3_ 0

=- 9~ 0 H2Si0l-2 118 0 H3Si04- 613 0

HC-O3- 0 0 HP04-2 IS 0

HSO3- 2i:S 0

HSOl- 920 0 l- 0 0

10:;. 0 0 K H+.- 0 0 NO l • 59 0

NO3- 265 0 0-2 2-149 0

02~~ 0 0 OK(tq)- 3S 76-H3

OH(•)- 50 0 P04-3 2 0 503•::? 376 0 SOl-1 1094 0

Or1Mics AFA_ DC:'-il' 7 0 AFA_NVOC' 0 0

N\"OC 98 0 SlltIO>t I 0 5\"0C !Oil 0 voe I 0

DEP-VSL-00002: Sheet: 9ofl5

24590-BOF-N 1 D-DEP-00002 Rev. I


DDtl

t• ) 0 (4

(5) TBI) (1)

(7) TBI) (1)

.:a (S) ll.00 (t)

(' ) TBD (I)

[1) TBD (I)

(3) 0 (])

(0) 74 (J)

0) 11141

(])

(1) TBD (I)

(1) TBD

(I)

(1) TBD

(I)

Enp<n.tor Fetd 5ttum

CS) DEN! (9 )

.

0 I l'IP

I 0

0 QI

I 0 0

0

I 186

0

2

I 0

20

M

I 0

0

0

I 0

1M 0

I 0

148

0

I SOP 7 2

I 0

21163 0

I 4

10 0

I 0 0 0

I 0 0 0

I 0 J

JIG

I 0 0 0

I 0 0 di

i 2 0 0

I 0 0

2 UI

L_ u

I 49 7

17113

I 0

2711 14113

I Ill

117 412

I 0 15

274

I PII 0 0

I 0 59

204

I 2-WS

0 14141 11D)

I 49 27 376

L 1093

I 7 0 ,.

r I

109 I

DEP03a

otes:

24590-BOF-RPT-PR-15-001 , Rev 0 Direct Feed LAW Process Corrosion Data2

0 m ~

DEP-VSL--00002

(1) Values marl<ed as 'TBD" will be provided in the revis ion o 24590 -8 OF-M4C-V1 H -00004 (Ref. 5. 1.4(2)) based on APPS model runs for oorroslon (2) DEP03a values from DEP-FIL T -00003 PCDS reported in Figure A-2 including aqueous concentrations (3) Maximum vessel property per 24590-BOF-MVC-DEP-00003 (Ref. 5.1 .4(3). Section 8) (4) Only trace solids are expected downstream of DEP-FIL T--00003 and are negligible in the sodium hydroxide reagent Anti-foam agent is also not expected in the sodium hydroxide reagent. (5) Value from "DFLAW_High CI_F Feed Vectors - Leach Case.xls.x" ResultS (Ref. 5.1 .4(2), 245~RMCD-04948) (6) pH of governing stream calculated as described in Section 3.2.2 based on composite stream concentrations. The pH calculation uses the stream density from "DFLAW _High CI_F Feed Vectors - Leach Case.xlsx• Results (Ref. 5.1.4(2), 24590-RMCD-04948) (7) Sodium hydroXide concentration per Ref. 5.1.3(3) (8) Maximum outside ambient air temperature per 24590-WTP-DB -E G-01-001 (Ref. 5.1.1(1 ), Table 4-4) (9) Maximum concentrations of all COCs except OH-(aQ) in govern ing stream DEP02 per Ref. 5.1.4(2) Table 8-2 (10) MINIMUM OH-(aq) value for governing stream DEP02 per Ref. 5.1 .4(2) Table 8-2

,ENER-IL .\ OTE FOR USE OF PCDS:

• Tlie 11iformo11011 p1·01·1d<.>d i,, , th , PCDS I·ep o l'l H 11/ /(!11ded .rn f P~1·. o,· m;, i ll wpp(lrf o/ rlw , ·,•s.H>I ,, ar.,,-inl .~PIPrrion

µmu? ·s m ,d 0I-,-osI01I En1l11m io11s . T/1e i11p111s. ns I1111pno11 • and co111p111n t i o1Jn! e 11g meen11g 111odeT. 11 ed 111 ge11emrl11g rlie r s11hs prese,11erl herein nre spec{ffc ro this eJ/orr. Lse of I/re r,i/oml(l//o/J prNe11red lienm, for "''·' u1!1er purpust< 11·ill req1,il e. eptrrare ron., iderario,

mid ,wn~1·sis ro s11pponj11srificc11io11 (~fit. m,• for fl',, des,r d. nltc1·11ntn· purpose.

• n, •. pron· dt.•scriptio11s i11 1/ris repo1T corer ro111i1 e p,·ocess oper<11io11s <1110 11011-,·,m1i11 (i11{,· q11e1/t/ proce -s operotionr, 11·he11 s 11 r l, exis 1. thnr could impncr co1-ros io11

01· er osio11 of p r oC<' ~S eq11iJl'IWIII

• Tfr,, proces!> df'scrtprio11s pro1•ided in this r l?pon an• or g i>nernl i1!fomwrio11 a11d rejlecm v e> rh<' corrosio ,1 e11gi11 eer ·s a11n~1·s is for rrm1spnre11cy. rl,e i1!fon11n1io11 is c11rrc111 011~ · at the' trmc th rs do 11111 111 ,s 1ss11C'd. T/1esC'

pn:,c,>. ·s de ·c1·ip1iom· ho11ld 11ot be refer"1W dfor desig11 .



24590-BOF-RPT-PR-15-001, Rev 0 Direct Feed LAW Process Corrosion Data

4.3 Evaporat01· Fttd \'\-sstl (DEP-VSL-00002)

4.3.1 Dtsniption ofVtsstl

DEP-VSL-00002 receiYes filtered effluent from DEP-Fll T-00003. sodium hydroxide from SHR-TK-000 U for pH adjustment. off-spec recycled concentrate from DEP-VS1-00003A/B/C. off-spec recycled condensate from DEP-VSL-00004A;B. and off-spec secondary condensate from the Reboiler Condensate Collection Vessel (DEP-VSL-00008).

DEP-Pl\lP-00002A.,.B are used to transfer DEP-VSL-00002 contents to DEP-EVAP-00001. In the event of an oYertlow. the liquid will flow by graYity into DEP-VSL-00001.

DEP-VSL-00002 is equipped with an Ernporator Feed Vessel :Mixing Eductors (DEP-EDUC-0000 lA,.B/C) to homogenize the contents and allow a representatiYe sample to be taken. The eductors recei,·e fluid from the EYaporator Feed Vessel Recirculation Pumps (DEP-Pl\lP-00012.A,.BiC) and will operate during mixing. If necessary. DEP-Pl\lP-00012A/B/C are ah,o used to renllll the contents ofDEP-VSL-00002 to the Tank Fanm, passing through DEP-HX-00001.

The Yessel contents can be sampled and pH can be adjusted by adding sodium hydroxide. The Yessel is monitored for leYel. pressiu·e. and temperan1re.

DEP-VSL-00002 is purged with air drawn through the Yessel head space and is Yented to the Vessel Vent Header. Vessel Yent streams are described in Section 4.10. This Yessel will haYe capability to add DIW for washing.

Figme 4 is a sketch of the input and output aITangement of streams for DEP-VSL-00002.

Figure 4- DEP-VSL-00002 Sketch

Filered EfllJent from DEP-FL T-00003

Sodi.m ~•oxide Addition

Contrninaled Reboier Condmsale ~. Iran DEP-VSl.-00008 ~ - - - - - - -

OIHpec Recyded Concentrate Iron, [······ ....... "-. DEP-EVAP-00001 _l:EP05e_,,,,- - - - - - - -

Off-specRecyd~~~ ~-_____ _

- Nonna! Operalioo

- - - • Nor>rrubne operation

DEP-VSL-00002: Sheet: JO of 15

DEP.flJUC-00001NBIC

--

I

' O.,erflow to DEP-VSL-00001

t-------~ - - ··- -EEP02~ Transfer to OEP-HX-00001

Evaporator Feed Strean




4.3.2 Systt'm Functions

The process functions of DEP-VSL-00002 are as follows:

• ReceiYe inlet streams • Mix process fluids • Store proces'> fluids • Transfer process fluids

The equipment perfonuc; additional system fi.mctions beyond the proce<,s fi.mctions. but these additional fi.mctionc; are beyond the c;cope of this document. These fi.mctions are not discussed any ftu1her in this document. howeYer are listed below for completeness.

• Confine collected effluentc;

• Sample collected effluents

• Flush system components

• Rep011 syc;tem conditions

4.3.3

4.3.3.1

Dt'sniption of Proct'ss Functions for DEP-VSL-00002

Rt'ct'ipt Strt'ams

The following: process c;treatm sho\\11 in PFD 24590-BOF-lvl5-Vl 7T-00011 (Ref. 5.1.3(1)) and P&ID 24590-BOF-M6-DEP-00002001 {Ref. 5.1.3(7)) are inputs to DEP-VSL-00002.

• DEP03a - Filtered Effluent from DEP-FIL T-00003

• DEP 11 - Sodium hydroxide addition from SHR-TK-00013 • Off-spec reboiler condensate from DEP-VSL-00008 • DEP05e - Off-spec recycled concentrate from DEP-EVAP-00001 • DEP0 lb - Off-spec recycled conden<,ate from DEP-VSL-00004A/B

4.3.3.1.1 DEP03a - Filtt>rt>d Efflut>ot to DEP-VSL-00002

The filtrate '>tream leaYing DEP-FIL T-00003 is tran<,fell'ed to DEP-VSL-00002. Stream prope11ies for this stream are shown in Section 4.2.3.3. l.

4.3.3.1.2 DEPll - Sodium Hydroxidt> Addition from SHR-TK-00013

The pH in DEP-VSL-00002 can be adjusted using sodimu hydroxide (expected to be 5M) to meet a specified pH.

Sodium :Molarity The nonual Na molarity ofDEPll is 51\f (Ref. 5.1.3(3)).

T t>mpt>1·aturt> TI1e 5M sodium hydroxide is stored in SHR-TK-00013. TI1e tank is located outside. TI1e minimum and maxinuun ambient temperatmes at the Hanford Site are -23cF and l l3°F. respectiYely (24590-\VTP-DB-





ENG-01-001. Ref. 5.1.1(1 ). Table 4-4). The nominal temperanu·e is 68°F. the aYerage of the minimum and maximum temperanrres at the Hanford Site. TI1e maxinuuu temperanrre is 113 °F. the maximmn temperanu·e of the Hanford Site. The mininuuu temperanu-e i'> 40°F. ba:.ed on the mininnun temperanrre (Ref. 5.1.3(3). Note 12).

Solids Conce-ntl'ation

Trace quantitie,;, ofinlpllfities are present in the solution based on the manufacnlfing process. Table 4-3 pro,ide:. the impurities of membrane grade. 50 wt°o (19M) sodimu hydroxide anilable from the Dow Chemical Company (CCN 246826. Attachment 1. Page 1. Ref. 5.1.5(1 )). This sodimu hydroxide is representati,·e of commercially aYailable caustic and will be u:.ed for estimating concentrations of impmities. The WTP selection of caustic reagent is not expected to be lower in quality.

Note: Since 5 molar NaOH is planned for SHR-TK-00013. the concentration of each imptmty decreases per tmit ofrnlume from the 1911 solution. As a result. the imptmties in the table below are bom1ding and com,etTatiYe.

Table- 4-3 - 19M ~aOH lmpmities

lmpuri~· Limit

Sodimu Carbonate O.IO~o

Soditm1 Chlotide lOOppm

Sodium Sulfate lOOppm

Soditm1 Chlorate 65ppm

Iron 5ppm

Liquid De-nsitY TI1e specific graYity of 5M sodium hydroxide is 1.19 at the minimum operating temperanrre 40°F and 1.16 and maximum operating temperanu·es of 113°F (Oxychem Caustic Soda Handbook. Ref. 5.2(4). Graph2).

Liquid pH The pH of 5M ,;odimn hydroxide is 14.7 (pH= 14 - (-log[OH-]) = 14 - (-log(5)) = 14.7).

4.3.3.1.3 Off-spe-c Re-boilel' Conde-nsate- from DEP-VSL-00008

IfDEP-VSL-00008 eftluent is determined to be off-.:,pec/contaminated. the stream can be redirected to DEP-VSL-00002.

TIIis is considered an off-nonnal proces,; that is not modeled in APPS. Therefore. the stream is not discussed any ftuther in this document.

4.3.3.1.4 DEP0Se - Off-spe-c Recycle-d Conce-ntl'ate- from DEP-EV AP-00001

DEP-VSL-00002 has the ability to receiYe the e,·aporator concentrate stream from DEP-EVAP-00001. if the contents do not meet the specifications for ftuther do\\11.:,tream processing.





This sh·eam is considered off-nonnal and is not modeled in APPS. Therefore. it will not be discm,sed ftirther in this docmnent.

4.3.3.1.5 DEP0lb - Off-spl'c Rl'QTll'd Condl'nsatl' from DEP-VSL--00004A/B

DEP-VSL-00002 has the ability to receiYe the effluent stream from DEP-VSL-00004A/B if the contents of those Yessels do not meet the specifications for further downsh·eam processing.

This stream is considered off-nomial and is not modeled in APPS. Therefore. it will not be discussed further in this document.

4.3.3.2 Ston Liquid Effluents

DEP-VSL-00002 nonnally receh·es effluent filtered through DEP-FIL T-00003 and sodium hydroxide from DEP 11. ~on-routine eYents include the receipt of off-spec reboiler condensate. off-spec recycled concentrate from DEP-EVAP-0000 I. and off-spec recycled condensate from DEP-VSL-00004A·B.

4.3.3.3 l\Ux Liquid Effluents

1fixing is accomplished in DEP-VSL-00002 using eductors (DEP-EDUC-OOOOIA.B/C) connected to a recirculation loop. ]\fixing proYi.des a homogeneous mixmre prior to sampling and transfer from the \·essel.

4.3.3.4 Transfl'r Procl'ss Fluids

The following. process s.treams shown in PFD 24590-BOF-M5-Vl 7T-00011 (Ref. 5.1.3(1 )) and P&IDs 24590-BOF-M6-DEP-00002001 (Ref. 5.1.3(7)). 24590-BOF-~16-DEP-00002002 (Ref. 5.1.3(8)) and 24590-BOF-M6-DEP-00002003 (Ref. 5.1.3(9)) are outputs fromDEP-VSL-00002.

• DEP02- EYaporator Feed Stream • DEP02b - Transfer to Tank Fanm, Yi.a DEP-HX-00001 • OYed1ow to DEP-VSL-00001

4.3.3.4.1 DEP02 - Ernpo1·ato1· Fl'l'd Sfl•l'am

Stream DEP02 is the outlet stream from DEP-VSL-00002 that is h·arn,ferred to the DEP eYaporator systenL entering in the reboiler recirculation loop upstream of the DEP Ernporator Recirculation Pump (DEP-PMP-00017).

Sodium Mola1•ity The range for sodimn molarity in sh·eam DEP02 during nomial operations will be established in the DFL;\ W PIBOD.

Tl'mpuaturl' The minimum. nonnal. and maximum temperan1res for sh·eam DEP02 are 40cf_ 124cf_ and 166cF. respecti.Yely. based on the temperan1res ofDEP-VSL-00002 (Ref. 5.1.4(3). Section 8).

Solids Concl'ntration The solids concentration in sh·eam DEP02 is negligible as the main inlet stream is the filtered effluent from DEP-FIL T-00003.





D('DSitY The minimum. nonual. and maximum density for stream DEP02 is 60.9 lbift>. 61.7 lb/ft>. and 68.6 lbift3

respecti\·ely. based on the densities ofDEP-VSL-00002 (Ref. 5.1.4(3). Section 8).

I!!! The range for pH in stream DEP02 during normal operations will be established in the DFLA W PIBOD.

4.3.3.4.2 DEP02b - Transff'r to Tank Fa1·ms \ia DEP-HX-00001

The contents ofDEP-VSL-00002 can be transferred to the Tank Farms after passing through DEP-HX-00001. This sh·eam is considered off-normal and is not modeled in APPS. Therefore. it \Vill not be discussed ftuther in this doctunent.

4.3.3.4.3 Onrflow to DEP-VSL-00001

DEP-VSL-00002 o\'erflows through a graYity drain line that collllecb to the DEP Yessel o\'erflow collection header. which empties into DEP-VSL-00001. The wssel oyerflow is a non-routine condition that is not included in the APPS model and is not discussed ftuther in this document.

4.3.4 Prnct>SS l\fodt>S

4.3.4.1 ~ormal Opt>rations

Based on the assessment of streams frequently transferred in and out ofYessel DEP-VSL-00002. the following processing modes are considered:

l11/e1 streams: • DEP03a - Filtered Effluent from DEP-FIL T-00003

• DEPll - Sodimn hydroxide addition from SHR-TK-00013

01t1/e1 sn·ea111s:

• DEP02- EYaporator Feed Stream

Section 4.3 .5.1 smlllnarizes these processing modes in tabular fonn.

4.3.4.2 Infrt>qut>nt Opt>rations

Based on an assessment of streams infrequently transfell'ed in and out of DEP-VSL-00002. the following processing modes are not considered.

J11/e1 stremm: • Off-spec reboiler condensate from DEP-VSL-00008 • DEP05e - Off-spec recycled concentrate from DEP-VSL-00003AB/C • DEP0lb- Off-spec recycled condensate fromDEP-VSL-00004A/B

011tle1 sn·eams:

• OYerflow to DEP-VSL-00001


24590-BOF-Nl D-DEP-00002 Rev.1



4.3.5

4.3.5.1

Summary of P.-ocnsing Conditions fo1· DEP-VSL-00002

No.-mal Ope.-ations

The following table summarizes the nonnal processing modes for DEP-VSL-00002.

Table 4-4 - DEP-VSL-00002 ~ormal Ope1·attons Na Molarity (mol/L) TftDJWrahlff {°F)

Stream Number Low Nonnal Upper Low Nom13l Upper Low

DEP03a IBD IBD IBD 59 132 166 0 DEPll N/A 5 N/A 40 68 113 0 DEPO:? IBD IBD IBD 40 124 166 0

UDS(wt%)

Nonnal 0 0 0

NOTE: Properties shown as IBD \\ill be established by values from the DFLA W PIBOD.


Upper

0 0 0

ISSUED BY DEP-VSL-00002 RPP-WTP PDC...DEP-VSL-00002 is equipped with mixing eductors to homogenize...

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