H2A Case Study: Future Distributed Natural Gas Steam Reformer

Project Summary

Full Title:	H2A Case Study: Future (2025) Natural Gas Steam Reformer (SMR) at Forecourt 1500 kg/day
Project ID:	243
Principal Investigator:	Brian James
Keywords:	Hydrogen production; forecourt; distributed; ethanol; steam reforming

Purpose

The purpose of this analysis is to determine a baseline delivered cost of hydrogen for the forecourt production of hydrogen from ethanol steam reforming.

Performer

Principal Investigator:	Brian James
Organization:	Directed Technologies, Inc. (DTI)
Address:	3601 Wilson Blvd., Suite 650 Arlington, VA 22201
Telephone:	703-243-3383
Email:	Brian_James@DirectedTechnologies.com

Sponsor(s)

Name:	Fred Joseck
Organization:	DOE/EERE/HFCIT
Telephone:	202-586-7932
Email:	Fred.Joseck@ee.doe.gov

Period of Performance

Start:	February 2008
End:	May 2008

Project Description

Type of Project:	Analysis
Category:	Hydrogen Fuel Pathways

Methodology/Approach:	The delivered cost of hydrogen was determined using a discounted cash flow analysis on the total capital investment and the periodic expenditures for repair, maintenance, and replacement. Hysys simulation of the reformer system was conducted to confirm mass flows and electrical power requirements. Capital cost of the steam reformer system was estimated by a combination of scaling, industry quotes, and ground-up component cost estimation.

Methodology/Approach:

The delivered cost of hydrogen was determined using a discounted cash flow analysis on the total capital investment and the periodic expenditures for repair, maintenance, and replacement. Hysys simulation of the reformer system was conducted to confirm mass flows and electrical power requirements. Capital cost of the steam reformer system was estimated by a combination of scaling, industry quotes, and ground-up component cost estimation.

Models Used:	H2A Production Model

Timeframe Studied:	2025

Products/Deliverables

	Description: Spreadsheet Analysis Publication Title: Future (2025) Natural Gas Steam Reformer (SMR) at Forecourt 1500kg/day Publisher: National Renewable Energy Laboratory Author Name(s): James, Brian D. http://www.hydrogen.energy.gov/h2a_prod_studies.html Publication Date: May 2008

Notes/Comments:	The natural gas reforming process is based on 20-atm integrated membrane stream reformer (reforming catalyst, water gas shift catalyst, Pd-alloy membrane tubes integrated into a single vessel). A 1:7.5 (by volume)admixture of reforming catalyst (Ni-Al-Ru at $150/kg, 2g/cc) and water gas shift catalyst(Fe/Cr Ox at $7.0/kg, 1 g/cc) is assumed. Gas hourly specific space velocity (GHSV) of the reactor catalyst system is 1344 per hour and is based on a 50% reduction of combined reformer/WGS catalyst volume compared to a non-integrated natural gas steam reforming configuration. The reactor vessel is based on a 4-pass annular heat exchange reformer configuration. Maximum process gas temperature is 550C.

Notes/Comments:

The natural gas reforming process is based on 20-atm integrated membrane stream reformer (reforming catalyst, water gas shift catalyst, Pd-alloy membrane tubes integrated into a single vessel). A 1:7.5 (by volume)admixture of reforming catalyst (Ni-Al-Ru at $150/kg, 2g/cc) and water gas shift catalyst(Fe/Cr Ox at $7.0/kg, 1 g/cc) is assumed. Gas hourly specific space velocity (GHSV) of the reactor catalyst system is 1344 per hour and is based on a 50% reduction of combined reformer/WGS catalyst volume compared to a non-integrated natural gas steam reforming configuration. The reactor vessel is based on a 4-pass annular heat exchange reformer configuration. Maximum process gas temperature is 550C.

Date Last Updated: 10/01/2008