Amendment 3_Attachment 2 - FEL2 Hydroprocessor Information Package Revision 2.pdf

PDF 3 MB Posted Dec 16, 2025

Attached to: Integrated Biorefinery Facility North High Bay Revitalization Custom Equipment
Solicitation number: SUB-2025-10354
Issued by: Department of Energy Office of Science

About this file

Written by GovTribe AI · Dec 16, 2025

This document is a Process Design Basis for a Hydroprocessing Unit at the National Laboratory of the Rockies, detailing specifications for a hydrotreater designed to process 1 barrel per day of Fats, Oils, and Grease (FOG) feeds. The hydrotreater will utilize hydrogen compression in three stages to an outlet pressure of 2075 psig, with the combined feed preheated from 100°F to 700°F. The reactor system will operate at up to 2015 psig and an outlet temperature of 765°F, with a liquid recycle volumetric ratio of 10:1 to maintain the desired exotherm.

The design includes two reactors in series with a 3-inch inner diameter, a catalyst height of 5 ft per reactor, and specific requirements for internals such as a distribution tray and catalyst support. The reactor effluent will be cooled using an air cooler and a cooling water trim cooler, with the air cooler designed to cool to 175°F and the trim cooler to 100°F. The system will also feature high-pressure and low-pressure flash drums for hydrogen recycling and product separation, with provisions for aqueous and organic phase handling. The document provides detailed specifications for equipment, instrumentation, and process conditions, including assumptions about operating parameters, materials, and future engineering requirements.

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RFP Amendment 3.pdf	PDF	Dec 16, 2025
Amendment 3_Attachment 3 - FEL2 Distillation Column Information Package Revision 2.pdf	PDF	Dec 16, 2025
RFP Amendment 2.pdf	PDF	Nov 12, 2025
RFP Amendment 1.pdf	PDF	Nov 3, 2025
Attachment 5 - Revised Proposed Payment Schedule .xlsx	XLSX spreadsheet	Nov 3, 2025
Attachment 5 - Proposed Payment Schedule.xlsx	XLSX spreadsheet	Oct 16, 2025
Attachment 1 - Statement of Work.pdf	PDF	Oct 16, 2025
NREL Request for Proposal (RFP) No. SUB-2025-10354.pdf	PDF	Oct 16, 2025
Attachment 3 - FEL 2 Distillation Column Information Package.pdf	PDF	Oct 16, 2025
Attachment 4 - Sample Subcontract.pdf	PDF	Oct 16, 2025
Attachment 2 - FEL2 Hydroprocessor Information Package .pdf	PDF	Oct 16, 2025

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To: National Laboratory of the Rockies Procurement and Subcontract Vendors

From:

Date: 12/11/2025

Subject: Process Design Basis – FEL II – IBRF Pilot Plant Revamp – Hydroprocessing Unit

Unit Operation: Hydroprocessor

Feed Rate(s): 1 BBL/DAY of Fats, Oils and Grease (FOG) feeds and 435 SCFH of circulating H2, including a hydrogen recycle stream.

Assumptions:

• The hydrodeoxygenation reaction occurs in two reactors in series. The reactor is modeled as one with no interbed hydrogen injection.

o The P&IDs reflect the capability of doing interbed hydrogen injection.

• The reactor mass flux is 4000 lb/hr/sq ft

• The unit is designed to operate with a maximum of 1 BPD production, and processing rates are likely to be lower.

• Standard conditions are 60 deg F and 12.2 psia on South Table Mountain Campus

• Cooling water supply is available at 24 deg C (approx. 75 deg F) at approximately 60 psig

• BBL/DAY = 42 gal/day

• Control valve dP = 25 psi, when it is NOT a pressure control valve

• Hydrogen supply is 430 psig

• LHSV calculations were completed with fresh feed, not the total hydrocarbon feed rate

• The liquid recycle is assumed to be 100% converted at the reactor outlet

• All electrical components must be NRTL certified. If they are not, they must be field verified.

o If additional cost is necessary to complete this task, please include the cost in the bid.

• One-line drawings are not complete and need to be done as the detailed engineering.

• Relief valve sizing is not complete and is considered a deliverable of detailed engineering.

Process Design Basis:

A hydrotreater is designed to process approximately 1 bbl/day, or 42 gal/day, of a FOG feed.

Hydrogen is compressed from the house hydrogen system. The compressor stages are minimized to an outlet temperature of 210 deg F to limit seal damage and prolong equipment life and reliability. Because of the limit, there are three stages of compression necessary to achieve an outlet pressure of 2075 psig. A spillback is required to control flow to the reactors for high turndown cases. Three separate compressors could be used instead of a single three stage compressor if the cost is lower or if the size of compressor prevents a three-stage configuration.

The combined feed is preheated from approximately 100 deg F up to 700 deg F. The reactor(s) exotherm is approximately 65 deg F. To maintain this exotherm, a liquid recycle volumetric ratio of 10 to 1 versus fresh triolein feed is necessary. The combined feed also includes a hydrogen recycle.

The hydrogen is recycled as much as possible to minimize the fresh hydrogen needed from the house utility. A small purge of approximately 10 SCFD of recycled hydrogen is necessary to purge any buildup of non-condensables and impurities. Both the high-pressure flash drum and the low-pressure flash drum recycle the flashed hydrogen back to the compressor.

The reactors are operated up to 2015 psig and an outlet temperature of 765 deg F. The pressure is controlled via a back pressure control valve on the high-pressure flash drum. The exotherm is minimized to ensure that there is enough hydrogen in the reactors to prevent coking the catalyst quickly.

The reactor is designed to maintain plug flow and adiabatic operation. A mass flux of 4000 lbs/hr/sq ft was chosen as the basis based on other commercial HDO hydrotreater reactors. To maintain that flux, the reactor inner diameter needs to be 3 inches. The other important reactor sizing criteria is space velocity. For this unit operation, a liquid hourly space velocity (LHSV) of 1 hr-1 leads to a catalyst height of 5 ft tall per reactor. The total height of the vessel is 6 ft tall. Internals should be installed to allow for proper feed distribution and disengaging space. A distribution tray should be installed at the top of the reactor. A catalyst support should be installed at the bottom of each reactor. The reactor head and bottom for each vessel need to be able to be removed to load and dump catalyst before and after each run. There needs to be approximately 2 to 3 feet below the reactors for maintenance activities such as catalyst collection.

The reactor effluent coolers are comprised of an air cooler and a cooling water trim cooler. The air cooler is directly downstream of the second reactor outlet and is designed to cool to 175 deg F and the trim cooler is designed for an outlet temperature of 100 deg F. The air cooler is to be exhausted outside directly and a blower for forced air circulation has been specified with this design package.

The air cooler should be something like the Xchanger brand.

Downstream of the coolers is the high-pressure flash drum controlled by a back pressure control valve on the vapor outlet. The vapor, which consists of mostly hydrogen, is recycled back to the second stage compressor to decrease the overall hydrogen need. The recycle flow is approximately 335 SCFH and is 83 mol% hydrogen. The high-pressure flash drum has an aqueous phase draw and the organic phase is split into a low-pressure flash drum feed stream and a large liquid organic phase recycle to the reactor feed. The recycle stream is approximately 10 to 1 volumetric ratio versus fresh feed. The recycle can be adjusted to limit the exotherm needed for the research.

The low-pressure flash drum pressure is approximately 375 psig. A control valve between the high pressure and low-pressure flash drums controls the pressure drop.

The low-pressure flash drum pressure is controlled with a back pressure control valve on the vapor outlet. The vapor outlet is routed to the thermal oxidizer, where it is later burned. There is a flow meter on that stream for mass balance closure. A sample station on that stream will be added in the future. The aqueous phase from the low-pressure flash drum is metered and routed to a holding tank. The organic phase is level controlled from the drum to the downstream stripper for fuel finishing. A separate process design basis is provided for the distillation column/stripper in a separate bid package.

As an alternative design case, a hydrocracker should be considered. The hydrocracker reactors would operate at 2000 psig. The temperature profile would be nearly the same, as far as exotherm expected, and there would need to be a liquid and hydrogen recycle loop, as there is in the current hydrotreater design.

Additional Considerations

• Additional detailed engineering including but not limited to the following items needs to be included in this bid.

o Details regarding specific equipment selection o Relief valve sizing o Control valve selection o Equipment layout, particularly for taller items and maintenance needs o Rotating equipment selection o Finalized specification sheets o Electrical one-line drawings o Control hardware selection o PHA outcomes

• This package includes o Instrumentation specification sheets o Vessel specification sheets o Heat exchanger specification sheets o Pump and compressor specification sheets o Blower specification sheet o Piping and instrumentation diagrams (P&IDs) o Heat and material balance o Equipment lists o Instrumentation list

• The process hazard analysis (PHA/HAZOP) has not been completed on this design. This will be completed with the National Laboratory of the Rockies before construction begins.

• Four identical reactor vessels should be purchased as a part of this bid. Two installed on the skid. The other two are spare reactors.

• All pumps need to be mounted so that any NPSH requirements are met at start up conditions – meaning low to no levels.

• Maintenance access is required for rotating equipment and reactors. Cooling water exchangers need to be able to be removed periodically for cleaning.

• The feed tank will be provided by owner, but the feed pump should be included in the quote for this unit.

• The equipment may be mounted on multiple structures if that helps ease construction. The pilot plant is divided into bays and are approximately 10 ft by 15 ft and 20 – 23 ft tall. The center of the building is taller than the outer perimeter.

Material Balance Tables

Feeds Description Mass Flow, lb/day Density, lb/ft3 Volumetric

Flow, SCF/H or

GPD

Fresh Hydrogen 12.42 0.1232 95.2 SCFH Soybean Oil 80.49 56.51 10.5 GPD Canola Oil 241.4 56.46 31.5 GPD

GPD – gallons per day (24 hours at standard conditions); SCF – standard cubic foot; lb – pound mass

Products Description Mass Flow, lb/day Density, lb/ft3 Volumetric

Flow, SCF/H or

GPD

H2 Water 0.126 53.35 0.015 GPD Reactor Effluent Water 39.55 61.93 4.75 GPD H2 Purge on LPFD 0.348 0.026 0.42 SCFH Stripper Feed 294.2 5.943 46.2 GPD

GPD – gallons per day (24 hours at standard conditions); SCF – standard cubic foot; lb – pound mass; LPFD – low pressure flash drum

Utility Usage Utility Amount Necessary Note 1 Note 2 Cooling Water 0.36 gpm (actual) Supply temperature –

75 ° F Supply pressure – 60 psig

Pump/Compressor Motor Electrical Needs

0.43 kWh 3 pumps 3 compressor stages

Low Pressure Steam Usage

386.2 BTU/hr 30 psi steam

Clamshell Heater Electrical Needs

16.4 kWh

All utility needs will be met by the National Laboratory of the Rockies.

Screwed Connection for Mixing Nozzle

Need to Determine Possibility of using 25mm Ingold Connection

12" Hatch

6" Agitator Connection

3" Sight Glass

3" Light Glass

3" CIP Port

NATIONAL RENEWABLE ENERGY LABORATORY

National Renewable Energy Laboratory

15013 Denver West Parkway

Golden, CO 80401

Operated for the US Department of Energy by

The Alliance for Sustainable Energy, LLC

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NATIONAL RENEWABLE ENERGY LABORATORY

National Renewable Energy Laboratory

15013 Denver West Parkway

Golden, CO 80401

Operated for the US Department of Energy by

The Alliance for Sustainable Energy, LLC

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National Renewable Energy Laboratory

15013 Denver West Parkway

Golden, CO 80401

Operated for the US Department of Energy by

The Alliance for Sustainable Energy, LLC

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15013 Denver West Parkway

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Operated for the US Department of Energy by

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14"-PF-003126-316SS

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14"-PF-003125-316SS

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14"-PF-003121-316SS

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14"-PF-003113-316SS

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14"-PV-003124-316SS

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14"-PV-003123-316SS

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EMC

AutoCAD SHX Text 11/26/2025

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IBRF - 278

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P&ID

AutoCAD SHX Text n/a

AutoCAD SHX Text PID - Hydrotreater Flash Drums

12/11/25

15013 Denver West Parkway

Golden, CO 80401

Operated for the US Department of Energy by

The Alliance for Sustainable Energy, LLC

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Note 2 - Sample stations can include vendor packages if all functionality is present.

REVEQUIPMENT LIST Project: IBRF Revitalization - Hydroprocessing Unit Site: STM - IBRF

DocumentNumber

National Laboratory of the Rockies PRIMARY PIPING SYSTEMS Project No.: Revision: 0 Date: 12/11/2025

Client:

By: Chk'd: Appr'd:

National Laboratory of the Rockies Page 1

PRESSURE DROP

DESCRIPTION

Total Liquid Vapour Temperature Pressure Density

ITEM NUMBER

FLUID

MASS FLOWS VOLUMETRIC

FLOWRATE

FLUID CONDITIONS NOMINAL

Viscosity OD Thickness Velocity lb/ft3 cP inch inches ft/sec psi/100 ftlb/day lb/day lb/day gph/scfh °F psig

Hydrogen feed

1/4"-PF-003106-316SS

Reactor Effluent Off Gas 3.129 -- 3.129

100 350 0.12 0.009058 1/4" 0.035

1/4"-H2-UTILXX101-316SS

Dry Hydrogen 12.4 -- 12.4 95.3 SCF/HR

0.035Low pressure flash drum recycle 0.38 SCF/HR 111 350 0.7921 0.01202 1/4"

Pre-Compression Knockout Pot Drain 1/4" 0.049100 350 62.1 0.6817

1/4"-PD-001110-316SS

Water with trace hydrocarbon 0 0 -- 0

0.035Hydrogen to Stage 1 Compression 99 SCF/HR 100 350 0.1484 0.008988 1/4"

1/4"-H2-001101-316SS

Hydrogen 15.56 -- 15.56

Stage 1 Compressed Hydrogen

1/4"-H2-001103-316SS

Hydrogen 15.56 0.1252 15.4

209 639.6 0.222 0.01502 1/4" 0.035

1/4"-H2-001102-316SS

Hydrogen 15.56 -- 15.56 99 SCF/HR

0.035Cooled Hydrogen Downstream of 1st Stage of Compression 2100.D.00198.9 SCF/HR 100 634.6 0.2636 Mixed Phase 1/4"

1st Stage Knockout Pot Drain

1/4"-H2-001104-316SS

Hydrogen 15.43 -- 15.43

100 634.6 62.1 0.6817 1/4" 0.049

1/4"-PD-001112-316SS

Water with trace hydrocarbon 0.1252 0.1252 -- 0.00062 gph

0.0352nd Stage Compression Feed 98 SCF/HR 100 634.6 0.2615 0.009043 1/4"

2nd Stage Compressed Hydrogen 1/4" 0.035209 1152 0.3894 0.0106

1/4"-H2-001105-316SS

Hydrogen 15.43 -- 15.43 98 SCF/HR

0.0352nd Stage Compressed Cooled Hydrogen 98 SCF/HR 100 1147 0.4627 Mixed Phase 1/4"

1/4"-H2-001106-316SS

Hydrogen 15.43 0.07194 15.36

High Pressure Flash Drum Recycle

1/4"-PD-001114-316SS

Water with trace hydrocarbon 0.0006 0.0006 --

97 1147 1.113 Mixed Phase 1/4" 0.035

1/4"-PF-003121-316SS

Hydrogen with other light end vapors 123.9 0.0006 123.9 135 SCF/HR

0.0492nd Stage Knockout Pot Drain 0.0000036 97 1147 62.1 2.03 1/4"

3rd Stage Compression Feed 1/4" 0.035 2100.D.00197 1147 0.9631 0.009482

1/4"-H2-001108-316SS

Hydrogen 139.3 -- 139.3 434.4 SCF/HR

0.0353rd Stage Compressed Hydrogen 434.4 SCF/HR 197 2074 1.432 0.01106 1/4" 2100.D.001/2100.D.002

1/4"-H2-001107-316SS

Hydrogen 139.3 -- 139.3

316SS

Hydrogen Vent to Flare

1/4"-PD-001111-316SS

Water with trace hydrocarbon 0 0 --

197 2074 1.432 0.01106 1/4" 0.035

1/4"-H2-001109-316SS

Hydrogen 0 -- 0 0 SCF/HR

0.049Low pressure drain of waste water to aqueous collection (pre KO Pot) 0 107 0 62.1 0.6817 1/4"

Low pressure drain of waste water to aqueous collection (1st Stage KO)

LegalDisclaimer Version 2 4/7/2004

AZ Equipment List Piping System.xls

316SS101.7 0 62.1 0.6694 1/4" 0.049

1/4"-PD-001113-316SS

Water with trace hydrocarbon 0.1252 0.1252 -- 0.00062 gph 2100.D.001

P&ID Page Number

2100.D.001

316SS

Materials of Construction

316SS

2100.D.001

316SS

2100.D.001

DocumentNumber

National Laboratory of the Rockies PRIMARY PIPING SYSTEMS Project No.: Revision: 0 Date: 12/11/2025

Client:

By: Chk'd: Appr'd:

National Laboratory of the Rockies Page 2

PRESSURE DROP

P&ID Page Number Materials of Construction

DESCRIPTION

Total Liquid Vapour Temperature Pressure

ITEM NUMBER

FLUID

MASS FLOWS VOLUMETRIC

FLOWRATE

FLUID CONDITIONS NOMINAL

Density Viscosity OD Thickness Velocity lb/day ft/sec psi/100 ft

1/4"-PD-001122-316SS

Water with trace hydrocarbon 0.1252 0.1252 -- 0.00062 gph 100 lb/day lb/day gph/scfh °F psig lb/ft3 cP inch inches

316SS1st Stage KO Drain Combining with Pre KO Pot Drain

1/4"-PD-001115-316SS

Water with trace hydrocarbon 0.000545 0.00001671 0.000532

0 62.1 0.6817 1/4" 0.049

2100.D.001 316SSMixed Phase 99 0 1.797 Mixed Phase2nd Stage KO Drain Downstream of LCV-003

1/4"-PD-001116-316SS

Water with trace hydrocarbon 0.1257 0.1252 0.0005Total drain flow to aqueous collection

0.049

2100.D.001

0.049 2100.D.001 316SSMixed Phase 101.7 0 53.35 Mixed Phase 1/4"

1/4"

2100.D.001 316SSPSV-001 Relief Vent Line Dependent on governing relief case 550 1/2" 0.035

1/2"-PV-001117-316SS

Hydrogen and light hydrocarbon vapor

Dependent on governing relief case

2100.D.001 316SSPSV-002 Relief Vent Line Dependent on governing relief case 850 1/4" 0.035

1/4"-PV-001118-316SS

Hydrogen and light hydrocarbon vapor

Dependent on governing relief case

2100.D.001 316SSPSV-001 and PSV-002 combined relief vent line Dependent on governing relief case 850 1" 0.065

1"-PV-001119-316SS

Hydrogen and light hydrocarbon vapor

Dependent on governing relief case

2100.D.001 316SSPSV-003 Relief Vent Line Dependent on governing relief case 1750 1/4" 0.035

1/4"-PV-001120-316SS

Hydrogen and light hydrocarbon vapor

Dependent on governing relief case

2100.D.001 316SSCombined relief valve outlets for hydrogen compression system Dependent on governing relief case 1750 2" 0.12

2"-PV-001121-316SS

Hydrogen and light hydrocarbon vapor

Dependent on governing relief case

2100.D.002 316SSLiquid I Feed Line 113 2040 56.55 1.328 1/4" 0.035

1/4"-PF-######-316SS

Vegetable Oil 321.9 321.9 -- 1.75

2100.D.002 316SSCombined feed to Reactor 1 108 2040 21.32 Mixed Phase 1/4" 0.035

1/4"-PF-002201-316SS

Vegetable Oil, reactor effluent, and hydrogen 3140 2995 145.5

Liquid - 19.75 gph

Vapor - 429.3 scfh

2100.D.002 316SSHydrogen Feed to Reactor 1 197 2074 1.432 0.01106 1/4" 0.035

1/4"-H2-002100-316SS

Hydrogen and light hydrocarbon vapor 139.3 -- 139.3 434.3 scfh

2100.D.002 316SSHydrogen Feed to Reactor 2 (normally no flow) 197 2074 1.432 0.01106 1/4" 0.035

1/4"-H2-002102-316SS

Hydrogen and light hydrocarbon vapor 32.08 -- 32.08 100 scfh

2100.D.002 316SSBypass around 2100-FCV-003 (normally no flow) 197 2074 1.432 0.01106 1/4" 0.035

1/4"-H2-002110-316SS

Hydrogen and light hydrocarbon vapor 32.08 -- 32.08 100 scfh

2100.D.002 316SS2100-P-002 Pump discharge 100.1 2065 46.66 1.486 1/4" 0.035

1/4"-PF-002115-316SS

Reactor Effluent 2679 2679 -- 18 gph

2100.D.002 Hastelloy C276Feed bypass around Reactor 1 (normally no flow) 300 MAX (due to heat tracing) 2040 21.32 Mixed Phase 1/4" 0.035

1/4"-PF-002103-C276

Vegetable Oil, reactor effluent, and hydrogen 3140 2995 145.5

Liquid - 19.75 gph

Vapor - 429.3 scfh

2100.D.002/2100.D.003 316SSLiquid Recycle for Exotherm Control 100 2000 46.63 1.486 1/4" 0.035

1/4"-PF-003113-316SS

Reactor Effluent 2679 2679 -- 18 gph

LegalDisclaimer Version 2 4/7/2004

AZ Equipment List Piping System.xls

2100.D.002 316SSBypass around 2100-TCV-022 (normally no flow) 100.1 2065 46.66 1.486 1/4" 0.035

1/4"-PF-002111-316SS

Reactor Effluent 2679 2679 -- 18 gph

DocumentNumber

National Laboratory of the Rockies PRIMARY PIPING SYSTEMS Project No.: Revision: 0 Date: 12/11/2025

Client:

By: Chk'd: Appr'd:

National Laboratory of the Rockies Page 3

PRESSURE DROP

P&ID Page Number Materials of Construction

DESCRIPTION

Total Liquid Vapour Temperature Pressure

ITEM NUMBER

FLUID

MASS FLOWS VOLUMETRIC

FLOWRATE

FLUID CONDITIONS NOMINAL

Density Viscosity OD Thickness Velocity lb/day ft/sec psi/100 ft

1/4"-PF-002109-316SS

Reactor Effluent 2679 2679 -- 18 gph 100.1 lb/day lb/day gph/scfh °F psig lb/ft3 cP inch inches

316SS 0Liquid recycle downstream of temperature control valve 2100-TCV-022

3/8"-PF-002104-C276 Mixed hydrogen, effluent, and unreacted vegetable oil 3140 2995 145.5

2040 46.64 1.483 1/4" 0.035

2100.D.002 Hastelloy C276 0

Liquid - 19.75 gph

Vapor - 429.3 scfh

108 2040 21.32 Mixed PhaseReactor 1 feed

3/8"-PF-002105-C276 Mixed hydrogen, effluent, and unreacted vegetable oil 3140 2995 145.5Reactor 1 outlet

0.035

2100.D.002

0.035 2100.D.002 Hastelloy C276 0

Liquid - 19.75 gph

Vapor - 429.3 scfh

735 2022 21.32 Mixed Phase 3/8"

3/8"

2100.D.002 Hastelloy C276 0Reactor 2 Bypass (normally no flow) 735 2022 21.32 Mixed Phase 3/8" 0.035

3/8"-PF-002106-C276 Mixed hydrogen, effluent, and unreacted vegetable oil 3140 2995 145.5

Liquid - 19.75 gph

Vapor - 429.3 scfh

2100.D.002 Hastelloy C276 0Reactor 2 outlet 765 2015 11.65 Mixed Phase 3/8" 0.035

3/8"-PF-002107-C276

Reactor Effluent 3140 2255 885.9

Liquid - 15.68 gph

Vapor - 356.7 scfh

2100.D.002 316SS 0Reactor Effluent air cooler outlet 175 2005 21.92 Mixed Phase 3/8" 0.035

3/8"-PF-002108-316SS

Reactor Effluent 3140 2985 155 Liquid - 19.9 gph Vapor - 347 scfh

2100.D.002 316SS 0Liquid Feed Tank II to Reactor 2 (normally no flow) 300 MAX (due to heat tracing) 2040 Varies Varies 1/4" 0.035

1/4"-PF-######-316SS Pyrolysis Oil or seed oil or another type of hydrotreatable feed Varies -- 1.75 gph

2100.D.003 316SS 0Cooled reactor effluent with hydrogen to high pressure flash drum 100 2000 24.1 Mixed Phase 3/8" 0.035

3/8"-PF-003100-316SS

Reactor Effluent 3140 3016.1 123.9 Liquid - 20.2 gph Vapor - 124 scfh

2100.D.003 316SS 0High pressure flash drum recycle hydrogen to 2100-PCV-008 100 2000 1.882 0.01014 1/4" 0.035

1/4"-PF-003101-316SS

Hydrogen with light hydrocarbon vapors 123.9 -- 123.9 335.5 SCFH

2100.D.003 316SS 0Bypass around 2100-PCV-008 (normally no flow) 100 2000 1.882 0.01014 1/4" 0.035

1/4"-PF-003114-316SS

Hydrogen with light hydrocarbon vapors 123.9 -- 123.9 335.5 SCFH

2100.D.003 316SS 0Hydrogen vent (normally no flow but if things begin to accumulate, flow of 23 lb/day or 62 SCFH at the same process conditions)

100 2000 1.882 0.01014 1/4" 0.035

1/4"-PF-003102-316SS

Hydrogen with light hydrocarbon vapors 123.9 -- 123.9 335.5 SCFH

2100.D.003 316SS 0Bypass around 2100-FCV-005 (normally no flow but if things begin to accumulate, flow of 23 lb/day or 62 SCFH at the same process conditions)

100 2000 1.882 0.01014 1/4" 0.035

1/4"-PF-003115-316SS

Hydrogen with light hydrocarbon vapors 123.9 -- 123.9 335.5 SCFH

2100.D.003 316SS 0Hydrogen vent downstream of FCV-005 100 0 0.01167 0.01014 1/4" 0.035

1/4"-PV-003112-316SS

Hydrogen with light hydrocarbon vapors 123.9 123.9 335.5 SCFH

2100.D.003 316SS 0High pressure flash drum relief valve outlet (normally no flow) Dependent on governing relief case 2500 1/2" 0.035

1/2"-PV-003109-316SS

Reactor Effluent Dependent on governing relief case

2100.D.003 316SS 0Waterboot Outlet for High Pressure Flash Drum 100 2000 62.37 0.6824 1/4" 0.049

1/4"-PD-003103-316SS

Water with trace hydrocarbon 39.55 39.55 -- 0.2 gph

2100.D.003 316SS 0Bypass around 2100-LCV-009 (normally no flow) 100 2000 62.37 0.6824 1/4" 0.035

1/4"-PF-003116-316SS

Water with trace hydrocarbon 39.55 39.55 -- 0.2 gph

LegalDisclaimer Version 2 4/7/2004

AZ Equipment List Piping System.xls

2100.D.003 316SS 0Liquid Reactor Effluent to low pressure flash drum 100 2000 46.63 1.486 1/4" 0.035

1/4"-PF-003104-316SS

Jet fuel with hydrogen and light hydrocarbon vapors 297.7 297.7 -- 2 gph

DocumentNumber

National Laboratory of the Rockies PRIMARY PIPING SYSTEMS Project No.: Revision: 0 Date: 12/11/2025

Client:

By: Chk'd: Appr'd:

National Laboratory of the Rockies Page 4

PRESSURE DROP

P&ID Page Number Materials of Construction

DESCRIPTION

Total Liquid Vapour Temperature Pressure

ITEM NUMBER

FLUID

MASS FLOWS VOLUMETRIC

FLOWRATE

FLUID CONDITIONS NOMINAL

Density Viscosity OD Thickness Velocity lb/day ft/sec psi/100 ft

1/4"-PF-003117-316SS

Jet fuel with hydrogen and light hydrocarbon vapors 297.7 297.7 -- 2 gph 100 lb/day lb/day gph/scfh °F psig lb/ft3 cP inch inches

316SSBypass around 2100-LCV-008 (normally no flow)

1/4"-PF-003108-316SS

Unstabilized jet fuel 294.2 294.2 --

2000 46.63 1.486 1/4" 0.035

2100.D.003 316SS1.94 gph 112 375 46.71 1.64Low pressure flash drum liquid product

1/4"-PF-003122-316SS

Unstabilized jet fuel 294.2 294.2 --Bypass around 2100-LCV-011 (normally no flow)

0.035

2100.D.003

0.035 2100.D.003 316SS1.94 gph 112 375 46.71 1.64 1/4"

1/4"

2100.D.003 316SSLow Pressure waterboot outlet (normally no flow) 112 375 62.7 0.6022 1/4" 0.049

1/4"-PD-003107-316SS

Water with trace hydrocarbon 24 24 -- 0.12 gph

2100.D.003 316SSBypass around 2100-LCV-010 (normally no flow) 112 375 62.7 0.6022 1/4" 0.049

1/4"-PF-003120-316SS

Water with trace hydrocarbon 24 24 -- 0.12 gph

2100.D.003 316SSLow pressure flash drum vent 112 375 0.8467 0.01205 1/4" 0.035

1/4"-PV-003105-316SS Hydrogen with low molecular weight hydrocarbon vapor

0.3477 -- 0.3477 0.4 SCFH

2100.D.003 316SSLow pressuer flash drum hydrogen recycle 112 375 0.8467 0.01205 1/4" 0.035

1/4"-PF-003106-316SS Hydrogen with low molecular weight hydrocarbon vapor

3.129 -- 3.129 3.76 SCFH

2100.D.003 316SSBypass around 2100-FCV-019 (normally no flow) 112 375 0.8467 0.01205 1/4" 0.035

1/4"-PF-003118-316SS Hydrogen with low molecular weight hydrocarbon vapor

0.3477 -- 0.3477 0.4 SCFH

2100.D.003 316SSHigh Pressure Flash Drum Vent downstream of 2100-PCV-008 96.9 1147 1.13 0.009755 1/4" 0.035

1/4"-PF-003123-316SS Hydrogen with low molecular weight hydrocarbon vapor

123.9 -- 123.9 335.5 SCFH

2100.D.003 316SSHydrocarbon outlet of 2100-V-005 100 2000 46.63 1.486 1/4" 0.035

1/4"-PF-003121-316SS

Reactor Effluent 2977 2977 -- 19.985 gph

2100.D.003 316SSOutlet of 2100-LCV-008 to LPFD 100 375 46.63 1.486 1/4" 0.035

1/4"-PF-003125-316SS

Reactor Effluent 297.7 297.7 -- 2 gph

2100.D.003 316SSAqueous drain downstream of 2100-LCV-009 100 0 61.93 0.6446 1/4" 0.049

1/4"-PD-003124-316SS

Water with trace hydrocarbon 39.55 39.55 -- 0.2 gph

2100.D.003 316SSFeed to distillation column downstream of 2100-LCV-011 112 25 5.943 Mixed Phase 1/4" 0.035

1/4"-PF-003126-316SS

Unstabilized jet fuel 294.2 284.3 9.9 4.3 SCFH & 1.84 gph

2100.D.003 316SSRelief valve outlet of 2100-PSV-005 on 2100-V-006 Dependent on governing relief case 2500 1/2" 0.035

1/2"-PV-003110-316SS

Unstabilized jet fuel Dependent on governing relief case

LegalDisclaimer Version 2 4/7/2004

AZ Equipment List Piping System.xls

REVINSTRUMENTATION LIST Project: IBRF Revitalization - Equipment Site: Integrated BioRefinery Faciltiy

By:

DocumentNumber

PRIMARY PIPING SYSTEMS Project No.: Hydroprocessor Revision: 0 Date: LastIssueDate

Client: National Renewable Energy Laboratory Page 1 5 psig

ITEM NUMBER

FLUID & STATE

MASS FLOWS VOLUMETRIC

FLOWRATE

FLUID CONDITIONS Pressure Remarks Atmospheric Pressure is 12 psiaNormal psig P&ID Page

M.W.

Molecular Weight

Coriolis meter

Chk'd: Appr'd:

DESCRIPTION

Minimum Normal Maximum Temperature Cp/Cv Density Viscosity Max Min

Flow Rate (lb/day)

Flow Rate (SCF/h or BBL/Day)

Operating Temperature (F) Density

(lb/cu ft) Dynamic

(cP) psig Saturated Hydrogen (vapor) 0 12.4 140 92.5 100

2100.D.001

100 1.026 62.1 0.6817

0Hydrogen Feed to Compressor

2100-LIT-001 Water (Liquid)

1.419 0.12 0.009058 450 350 250

2100.D.001 Normal level is predicted to be around 0-5%, low level is 0%, and high level is 75%. This needs to be a continuous level, not a switch.

Magnetic float with a local indication (sight glass or similar such as Rosemount 9930)

0Pre KO Pot Level 450

2.062

18.02 350

2100-FT-001

350 250

2100.D.001 Thermocouple

0Hydrogen Feed Temperature -- 100 1.419 0.262 0.009043 450

2100-TT-001 Saturated Hydrogen (vapor) -- -- -- 2.466

2100.D.001 Pressure Transducer

0Hydrogen Header Pressure

2100-TT-002 Saturated Hydrogen (vapor) -- -- --

100 1.419 0.12 0.0106 450 350

2100-PT-001 Saturated Hydrogen (vapor) -- -- -- --

640 500

2100.D.001 Thermocouple (Type K)

01st Stage Hydrogen Compressor Discharge Temperature -- 209 1.408 0.3894 0.0106 750

2100.D.001 Thermocouple (Type K)

01st Stage Hydrogen Cooler Outlet Temperature

2100-LIT-002 Water (Liquid)

100 1.414 0.3894 0.0106 750 640

2100-TT-003 Saturated Hydrogen (vapor) -- -- -- --

640 500

2100.D.001 Normal level is predicted to be around 0-5%, low level is 0%, and high level is 75%. This needs to be a continuous level, not a switch.

Magnetic float with a local indication (sight glass or similar such as Rosemount 9930)

0 1st Stage KO Pot Level -- 100 1.024 0.3894 0.0106 750

2100.D.001 Something similar to an Ashcroft pressure gauge

01st Stage KO Pot Pressure Gauge

2100-TT-004 Saturated Hydrogen (vapor) -- -- --

100 1.416 0.3894 0.0106 750 640

2100-PG-001 Saturated Hydrogen (vapor) -- -- -- --

1155 1000

2100.D.001 Thermocouple (Type K)

02nd Stage Hydrogen Compressor Discharge Temperature -- 209 1.412 0.3894 0.0106 1275

2100.D.001 Thermocouple (Type K)

02nd Stage Hydrogen Cooler Outlet Temperature

2100-LIT-003 Water (Liquid)

100 1.422 0.3894 0.0106 1275 1155

2100-TT-005 Saturated Hydrogen (vapor) -- -- -- --

1155 1000

2100.D.001 Normal level is predicted to be around 0-5%, low level is 0%, and high level is 75%. This needs to be a continuous level, not a switch.

Magnetic float with a local indication (sight glass or similar such as Rosemount 9930)

02nd Stage KO Pot Level -- 100 1.214 47.4 2.03 1275

2100.D.001 Something similar to an Ashcroft pressure gauge

02nd Stage KO Pot Pressure Gauge

2100-PT-002 Saturated Hydrogen (vapor) -- -- --

100 1.4 0.9691 0.0106 1275 1155

2100-PG-002 Saturated Hydrogen (vapor) -- -- -- --

2075 1900

2100.D.001 Pressure Transducer

03rd Stage Hydrogen Compressor Outlet Pressure -- 197 1.39 1.432 0.011 23005.071

2100.D.001 Thermocouple (Type K)

03rd Stage Hydrogen Compressor Outlet Temperature

2100-LCV-001 Water (Liquid)

0 0.06 0.1252

197 1.39 1.432 0.011 2300 2075

2100-TT-006 Saturated Hydrogen (vapor) -- -- -- --

350 250

2100.D.001 With actuator and positioner (want to be able to see the position readout on the SCADA) 0Pre KO Pot Level Control Valve 0.00036 100 1.026 62.1 0.6817 450

2100.D.001 With actuator and positioner (want to be able to see the position readout on the SCADA) 01st Stage KO Pot Level Control Valve

2100-LCV-003 Water (Liquid)

0 0.0005 0.001

100 1.024 62.1 0.6817 750 640

2100-LCV-002 Water (Liquid)

0 0.1252 0.15 0.00036

LegalDisclaimer Version 2 4/7/2004

AZ Equipment List Piping System.xls

2075 1900

2100.D.002 With actuator and positioner (want to be able to see the position readout on the SCADA) 02nd Stage KO Pot Level Control Valve 0.000002 197 1.214 47.4 2.03 2300

5.071

18.02

198.1

2.062

2.466

198.1

5.071

REV

LegalDisclaimer Version 2 4/7/2004

AZ Equipment List Piping System.xls

M.W.

Molecular Weight

5.071

71.36

2022 1900

2100.D.002 Pressure transducer

0Reactor 1 Outlet Pressure 71.36-- 735 1.057 21.31 -- 2300

2100.D.002 Thermocouple (Type K)

0Reactor 1 Outlet Temperature

2100-PT-005 Hydrogen and Reactor Feed (mixed phase) -- -- --

735 1.057 21.31 -- 2300 202271.36

2100-TT-015 Hydrogen and Reactor Feed (mixed phase) -- -- -- --

2100.D.002 Clamshell control

0Reactor 1 Clamshell Zone 4 Temperature Control --

2100.D.002 Clamshell control

0Reactor 1 Clamshell Zone 3 Temperature Control

2100-TC-004 Not seeing process (on reactor) -- -- --

2100-TC-003 Not seeing process (on reactor) -- -- -- --

2100.D.002 Clamshell control

0Reactor 1 Clamshell Zone 2 Temperature Control --

2100.D.002 Clamshell control

0Reactor 1 Clamshell Zone 1 Temperature Control

2100-TC-002 Not seeing process (on reactor) -- -- --

2100-TC-001 Not seeing process (on reactor) -- -- -- --

2100.D.002 Multipoint thermocouple

0Reactor 1 Interbed Temperature 71.36-- 735 1.057 21.31 -- 2300

2100.D.002 Multipoint thermocouple

0Reactor 1 Interbed Temperature

2100-TT-014 Hydrogen and Reactor Feed (mixed phase) -- -- --

730 1.057 21.31 -- 2300 202871.36

2100-TT-013 Hydrogen and Reactor Feed (mixed phase) -- -- -- --

2100.D.002 Multipoint thermocouple

0Reactor 1 Interbed Temperature 71.36-- 725 1.057 21.31 -- 2300

2100.D.002 Multipoint thermocouple

0Reactor 1 Interbed Temperature

2100-TT-012 Hydrogen and Reactor Feed (mixed phase) -- -- --

715 1.057 21.31 -- 2300 203571.36

2100-TT-011 Hydrogen and Reactor Feed (mixed phase) -- -- -- --

2100.D.002 Multipoint thermocouple

0Reactor 1 Interbed Temperature 71.36-- 705 1.057 21.31 -- 2300

2100.D.002 Multipoint thermocouple

0Reactor 1 Interbed Temperature

2100-TT-010 Hydrogen and Reactor Feed (mixed phase) -- -- --

700 1.057 21.31 -- 2300 204071.36

2100-TT-009 Hydrogen and Reactor Feed (mixed phase) -- -- -- --

2100.D.002 Pressure transducer

0Reactor 2 Inlet Pressure 71.36-- 730 1.057 21.31 -- 2300

2100.D.002 Thermocouple (Type K)

0Reactor 1 Inlet Temperature

2100-PT-004 Canola & soybean oil (mixed) -- -- --

100 1.057 21.31 -- 2300 2023

2100-TT-008 Canola & soybean oil (mixed) -- -- -- --

2023 1900

2100.D.002 Pressure transducer

0Reactor 1 Inlet Pressure -- 100 1.057 10.59 -- 2300

2100-PT-003 Canola & soybean oil (mixed) -- -- --

0Hydrogen Flow to Reactor 2

2100-FCV-003 Saturated Hydrogen (vapor) 0 55 139 435

1.39 1.432 0.011 2300 2075 1900

2100.D.002 With actuator and positioner (want to be able to see the position readout on the SCADA) 0Hydrogen Flow Control Valve to Reactor 2 2300 2075

2100-FT-003 Saturated Hydrogen (vapor) 0 55 139 435 197

2100.D.002

197 1.39 1.432 0.011

Venturi meter

Chk'd: Appr'd:

DESCRIPTION

Minimum Normal Maximum Temperature Cp/Cv Density Viscosity Max Min

Flow Rate (lb/day)

Flow Rate (SCF/h or BBL/Day)

Operating Temperature (F) Density

(lb/cu ft) Dynamic viscosity psig psig

ITEM NUMBER

FLUID & STATE

MASS FLOWS VOLUMETRIC

FLOWRATE

FLUID CONDITIONS Pressure Remarks

Normal psig P&ID Page

DocumentNumber

PRIMARY PIPING SYSTEMS Project No.: Hydroprocessor Revision: 0 Date: LastIssueDate

Client: National Renewable Energy Laboratory Page 2 5

INSTRUMENTATION LIST Project: IBRF Revitalization - Equipment Site: Integrated BioRefinery Faciltiy

By:

LegalDisclaimer Version 2 4/7/2004

AZ Equipment List Piping System.xls

2000 1200

2100.D.002 Something similar to Ashcroft pressure gauge

0Liquid Recycle Pump Suction Pressure Gauge 100 1.205 46.63 165.6 1.486 2500

2100-PG-003 Canola Oil & Soybean Oil (liquid) -- -- -- --

2065 1200

2100.D.002 Coriolis meter

0Liquid Recycle Flow 100 1.205 46.63 165.6 1.486 2500

2100-FT-004 Canola Oil & Soybean Oil (liquid) 0 2679 3250 10.28

2065 1200

2100.D.002 With actuator and positioner (want to be able to see the position readout on the SCADA) 0Reactor 2 Outlet Temperature Control Valve 100 1.205 46.63 165.6 1.486 2500

2100-TCV-022 Hydrogen and Reactor Feed (mixed phase) 0 2679 3250 10.28

2000 1500

2100.D.002 Thermocouple (Type K)

0Reactor Effluent Air Cooler Outlet Temperature 175 1.05 21.92 75.88 -- 2500

2100-TT-023 Hydrogen and Reactor Feed (mixed phase) -- -- -- --

2000 1500

2100.D.002 Pressure transducer

0Reactor Effluent Air Cooler Outlet Pressure 175 1.05 21.92 75.88 -- 2500

2100-PT-007 Hydrogen and Reactor Feed (mixed phase) -- -- -- --

2022 1900

2100.D.002 Thermocouple (Type K)

0Reactor 2 Outlet Temperature 765 1.086 11.65 75.88 -- 2300

2100-TT-022 Hydrogen and Reactor Feed (mixed phase) -- -- -- --

2022 1900

2100.D.002 Pressure transducer

0Reactor 2 Outlet Pressure 765 1.086 11.65 75.88 -- 2300

2100-PT-006 Hydrogen and Reactor Feed (mixed phase) -- -- -- --

2100.D.002 Clamshell heater

0Reactor 2 Clamshell Heater Zone 4 Temperature Controller

2100-TC-008 Not seeing process (on reactor) -- -- -- --

2100.D.002 Clamshell heater

0Reactor 2 Clamshell Heater Zone 3 Temperature Controller

2100-TC-007 Not seeing process (on reactor) -- -- -- --

2100.D.002 Clamshell heater

0Reactor 2 Clamshell Heater Zone 2 Temperature Controller

2100-TC-006 Not seeing process (on reactor) -- -- -- --

2100.D.002 Clamshell heater

0Reactor 2 Clamshell Heater Zone 1 Temperature Controller

2100-TC-005 Not seeing process (on reactor) -- -- -- --

2022 1900

2100.D.002 Multipoint thermocouple

0Reactor 2 Interbed Temperature 765 1.057 11.65 75.88 -- 2300

2100-TT-021 Hydrogen and Reactor Feed (mixed phase) -- -- -- --

2022 1900

2100.D.002 Multipoint thermocouple

0Reactor…

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File details come from the government source that posted it. Updated Dec 16, 2025.