003 - Syngas Generation for GTL.pdf

7/25/2019 003 - Syngas Generation for GTL.pdf

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forforas to Liqui s TLas to Liqui s TL

XTL Fundamentals

- ,


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PRESENTERPRESENTER :: SANJIVSANJIV RATANRATAN

-Technologies, TECHNIP Group

Technip is among the top 5 global engineering contractingcompany

-

23,000 employees worldwide in 21 locations

HQ in Paris, other main operating centres for onshore businessinclude Rome, Houston, Claremont, The Netherlands, Kuala-Lumpur,

Abu-Dhabi, Delhi

Built the first commercial GTL lant at Or x atar which started uin 2007 and operating successfully

Built the Statoil pilot plant at PetroSA

2XTL Fundamentals, 1-3 Dec, 2009, Cape town


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PRESENTATION OVERVIEWPRESENTATION OVERVIEW

Introduction

Specifics of Syngas for GTL / XTL

Syngas Generation Routes and Technologies Challenges and Options in optimizing Syngas

generation

Brief Scouting Comparison Innovative Developments

Conclusions



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Introduction

Syngas specifics for GTL

Syngas Routes and Technologies Challenges and Options in optimizing Syngas

generation


Conclusions



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INTRODUCTIONINTRODUCTION

The Gas in Gas-to-Liquid connotation has transitioneds nce s ncep on

Originally in the 50s, Gas basically signified SynGas (derived

In recent GTL terms, Gas refers to Natural Gas as being thestarting source for producing the Syngas

Within its portfolio, distinctive domains of Coal-to-Liquid (CTL)and Biomass-to -Liquid (BTL) have evolved based on their starting

,

Also presently liquid tends to include, apart from more customaryF-T roducts also Methanol and other derivatives like DME



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SYNGASSYNGAS--BASEDBASED PRODUCTSPRODUCTS OVERVIEWOVERVIEW

Typical

World Scale

Plant Ca acit

Equivalent

Natural Gas

MMSCFD

30 years NG

requirement

TCF

Large H2 Plant 100 mmscfd 45 0.5

Ammonia 2000 mtpd 55 0.6

Methanol 3000 5000 mtpd 100 -160 1.1 - 1.8

GTL 30 150 K bpd 300 1400 3.0 14.0

LNG 5 - 8 mm tpy 800 -1200 8.5 - 13.0



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GTL (& GTC) SPECTRUMGTL (& GTC) SPECTRUM

Ca tive owerCa tive ower

Methanol

MTBEMTBE

Fuel CellsFuel Cells

DMEDMECoalCoal

SyngasNat.Nat.

GasGas

MTOMTO

GTL

ap aap a

Diesel / GasoilDiesel / Gasoil

LubesLubes--Waxes /

Specialties

Waxes /

Specialties

Total Chain Emissions (CO2, NOx & PM10)

per KM ( Well to Wheel )

7

XTL Fundamentals, 1-3 Dec, 2009, Cape town


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GTLGTL PROCESS SECTIONSPROCESS SECTIONS

AirAirAir

Oxygen

Carbon

eparat onOxygen

Carbon

eparat onOxygen

Carbon

eparat on

Natural Gas Monoxide

Syngas

Generation

Fischer-Tropsch

SynthesisNatural Gas Monoxide

Syngas

Generation

Fischer-Tropsch

Synthesis

Monoxide

Syngas

Generation

Fischer-Tropsch

Synthesis

HydrogenSteam

WaxyF-T Products

U radin

HydrogenSteam

WaxyF-T Products

U radin

HydrogenSteam

WaxyF-T Products

U radinIntermediates

Power

Plant SteamExcessPower

Intermediates

Power


Intermediates

Power


Jet Fuel DieselWater

Jet Fuel DieselWaterWater

8

NaphthaNaphtha



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Introduction


Syngas Routes and Technologies Challenges and Options in optimizing Syngas

generation


Conclusions



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SYNGASSYNGAS SPECIFICS FOR GTLSPECIFICS FOR GTL

Syngas denotes mixture of H2 and CO in variousproportions

For a given NG feedstock, the H2/CO ratio can vary in therange of 1.8 to 5.0, depending upon the process /technology applied

For F-T, the required ratio is ~ 2.0 with minimized level of CO2and inerts

e syngas components 2 an prov e t e an

elements required for producing the straight chain, 2 2



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SYNGASSYNGAS SPECIFICS FOR GTLSPECIFICS FOR GTL

Choice of Syngas technology for GTL gets critical in view of : Economy of scale v/s cost-effective scale-up

Steam-power / energy integration (energy efficiency)

eve o nves men cap a e c ency

For 10,000 bpd, it needs ~ 250 mmscfd Syngas

Syngas generation for GTL is energy and capital intensive

Syngas dictates ~ 2/3rd of the specific energy usage

Accounts for more than half of the total investment



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INFLUENCE OF FINFLUENCE OF F--TT CATALYST ONCATALYST ON SYNGASSYNGAS

Fe catal st In-situ WGS activity more suitable for heavier HC feeds

(lower H2/CO syngas) on-regenera e

CO catalyst

higher H2/CO Higher selectivity for linear HC

Temperature (and pressure) sensitivity

Operating conditions Higher T and lower P favors lighter product slate



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TYPICAL GTLTYPICAL GTL SCHEME AND CSCHEME AND C--BALANCEBALANCE

WaterWaterAirAir Steam

SteamSteam Steam-Power

system Power

ue gasue gas

Separation

System

OO22Tail gasTail gas

Fuel gas / wash purgeFuel gas / wash purge

Q

SyngasGeneration

F-T Synthesis& Separation

ProductsWork-Up

Natural gas Synfuels

HH22 *HH22PSA* Proc.Proc. CondCond

Reac. waterReac. waterH2 plant

~ 300 ~ 70 ~ 230C, tph (50 kbpd)



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GTL INTEGRATION SUBGTL INTEGRATION SUB--SYSTEMS (SMDS)SYSTEMS (SMDS)

Ai r

CO-Shift

Air Separation

Unit H2/CO = 2.30

Reformingand

PSA Units

H2/CO = 3.36

Natural

Gas Oxygen(99.5% vol)

C5+

ExtractionHydrogen

(99.9% vol)C5+ cut

Light Ends

to Fuel

Natural Gas

Partial

Raw Gas

Scrubbing and Products Hydrocracking

H2/CO = 1.76

Water & Oxygenates

sc er- ropsc

ReactorH2/CO = 2.10

Distillate



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Introduction


Syngas Routes and Technologies

Brief Scouting Comparison

Conclusions



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SYNGASSYNGAS ROUTES AND TECHNOLOGIESROUTES AND TECHNOLOGIES

Steam route Steam-methane reformin SMR

Catalytic, endothermic process ( upto 950 C) CH

4

+ H2

O = 3 H2

+ CO (NG feed ; 206 kJ/mole)

y rogen on r u or ; e c en or -

[ C6H12 + 6H2O = 12 H2 + 6 CO for Naphtha feed ]

Oxygen route Traditionally non-catalytic Partial oxidation (POx)

-Steam + O2

at much higher temps (1200-1400 C)

CH4 + O2 = 2 H2 + CO (NG feed ; - 39 kJ/mole)

Recent developments over catalytic POx (CPO)

CO Contributor ; Hydrogen deficient for F-T



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SYNGASSYNGAS ROUTES AND TECHNOLOGIESROUTES AND TECHNOLOGIES

- Partial oxidation with oxygen and steam carrying in-situ SMR

Catalytic with 900-1100 C outlet (typically 1050 C) 2 CH4 + H2O + O2 = 5 H2 + 2 CO H2/CO =2.5

3.74 + . 2 + . 2 + . 2 = . 2 + . + . 2 + . 2

Combination / Hybrid Routes

Combination of SMR with POx and ATR in parallel or series to getthe specific benefits for GTL (syngas) applications



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WAYS TO ADJUST H2/CO RATIO INWAYS TO ADJUST H2/CO RATIO IN SYNGASSYNGAS

Decreases Increases Application

at o rat o

Lower S/C ratio /

X

NG-SMR

H2 skimming using

Membranes XNG-SMR

Recycle Process CO2 X NG-SMRNG-ATR (partial)

Import CO2 /

F-T tail gas recycleX

NG-SMR

X

CTL

Process combination NG: SMR + POx



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H2/CO RATIO REGIMESH2/CO RATIO REGIMES

Feed : Natural Gas; CN =1.05

POx O2 / C

ratio

ATR

COMB

w 2 a on

3CH4 + 3H2O = 3CO + 9H2CO2 + H2 = CO + H2O

SMR

4 2 2 = 2

1 2 3 4 5

H2 / CO ratio

with import CO2



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SYNGASSYNGAS TECHNOLOGIESTECHNOLOGIES OVERVIEWOVERVIEW

Steam Reforming Autothermal Reforming (ATR)

Conventional SMR

Compact reforming

Oxygen blown

Air blown Regenerative reforming* Fluidised

Partial Oxidation (POx)

Combination Routes Combi reforming

Non catalytic

Catalytic

+ n sp t -para e

2-step reforming

SMR + ATR (OBS) in series

GHR* + ATR/OBS in series

Combi Pox

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POx / ATR + EHTR* in parallelXTL Fundamentals, 1-3 Dec, 2009, Cape town


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Conventional SMR

Compact reforming

Oxygen blown




Non catalytic

Catalytic

+ n sp t -para e

2-step reforming



Combi Pox

22



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CONVENTIONAL STEAM REFORMINGCONVENTIONAL STEAM REFORMING

Flue gas

Fuel

180

Steam Reforming duty

Steam

1100 C150 C

Air880 C

Steam

300 C Syngas

30

Feed

Excess S/H steam

45

23

10



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STEAM REFORMING (SMR)STEAM REFORMING (SMR)

Combustion AirCombustion Air

Feed inlet systemFeed inlet system

BurnersBurners

Catalyst tubesCatalyst tubes

Flue GasOutlet systemOutlet system

Transfer LineTransfer Line

unne sReformedReformed

gasgas



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STEAM REFORMING PRINCIPLESSTEAM REFORMING PRINCIPLES

800C

gas/

steamFuel / ai r

600

eratureDeg

CH4 + H2O CO + 3H2 Endo

+ +

0 0.2 0.4 0.6 0.8 1200

400

Temp

Fraction down tube

Gas Temp Eq'm Temp

Nat. gas + steam flow down vertical tubes at pressure

Fuel combusted at atm. pressure in external furnace

Radiant Heat transfer to tubes

Catalyst shaped to enhance inside-tube heat transfer

Furnaces can be cylindrical (small), top-fired or side-fired(terrace- wall)

catalyst

flame

Close approach to methane-steam equilibrium at highexit temperature



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Conventional SMR

Compact reforming

Oxygen blown




Non catalytic

Catalytic

+ n sp t -para e

2-step reforming



Combi Pox

27



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PARTIAL OXIDATION PROCESSESPARTIAL OXIDATION PROCESSES

Conventional (non-catalytic) partial oxidation (POx)

Catalytic partial oxidation Non-equilibrium based

Equi i rium ase



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CONVENTIONAL PARTIAL OXIDATIONCONVENTIONAL PARTIAL OXIDATION ((POXPOX))

Non-catal tic

Gasifier at 1200-1400C

Feed gas preheated with little

feed gas

O2

or no steam addition

Large oxidant consumption

-Gasifier

2 . .

NG and 0.4 - 0.6 on Coal Low CO2, very low CH4slip in

steam

syngas

Pressures can be upto 70 bar

syngas



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PARTIAL OXIDATIONPARTIAL OXIDATION

S/C Overall : 0.2

O2/C : 0.64Reactor

WH Boiler

1350C, 60 barO2 + Steam

NG feed

H2/CO : 1.9Steam

yngas




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PROs

2

Not limited by catalyst temperature limits (higher temp --> higherCO/H

2)

Can an e variety o eavier ee s

Residues, petroleum coke, coal

Allows hi her ressure s n as u to 60 bar

CONs Large Oxygen usage (~3500 tpd for 15,000 bpd)

Reliability (especially on heavier feeds)

-

Capital efficiency

Limited scale-up compared to SMR

31

Need for more trains


CATALYTICCATALYTIC PARTIALPARTIAL OXIDATIONOXIDATION


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CATALYTICCATALYTIC PARTIALPARTIAL OXIDATIONOXIDATION

CPO operates at 900-1000Cvery ig space ve ocity an

flameless)

Feed gas preheated (possiblyfeed gas

oxygen

pre-reformed)

Little or no steam additionCPOfuel gas

(usually O2) Theoretical H2/CO ratio 2steam

2, 4

Better selectivity than non-

catalytic Pox Non-equilibrium reforming

No commercial scaleapplication so far

syngas



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SYNGASSYNGAS GENERATION TECHNOLOGIESGENERATION TECHNOLOGIES

Steam reforming (SMR)

Conventional SMR

Autothermal reforming (ATR)

Fixed Bed Adiabatic

Compact Reforming

-

Oxygen blown

Air blown


Non catalytic

Hybrid processes

Combined Reforming Catalytic Gas Heated Reforming (GHR)*

EHTR Post Reforming

34TL Fundamentals, 1-3 Dec, 2009, Cape town

AUTOTHERMAL REFORMINGAUTOTHERMAL REFORMING


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AUTOTHERMAL REFORMINGAUTOTHERMAL REFORMING

2

NG Feed

Steam

.

S/C overall : 0.8

CO2/C : 0.3

Sulphur1050C , 35 bar

H2/CO : 2.0

FT

synthesis

Tail gas Recycle

35

100 MMSCFD feed gas ~ 265 MMSCFD H100 MMSCFD feed gas ~ 265 MMSCFD H22 + CO+ CO



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AUTOAUTO--THERMAL REFORMERTHERMAL REFORMER

oxygen

~1.15 te/te natural as

ee gas rom re ea er

~700

C

steam

syngas

1020

C

~


//


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ATR: S/C RATIO SENSITIVITYATR: S/C RATIO SENSITIVITY

O2/C ratio : 0.64

Outlet pressure : 35 bar abs

No CO2 rec cle

S/C ratio (molar) 1.7 1.2 0.6

Residual methane 0.30 0.48 1.05

2 . . .

H2/CO 2.65 2.31 2.08

Severity Low Medium High


AUTOTHERMALAUTOTHERMAL REFORMINGREFORMING


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AUTOTHERMALAUTOTHERMAL REFORMINGREFORMING

PROs Provides H2/CO ~2.0

with partial CO2 recycle and reduced S/C ratio

Well proven in ammonia and methanol

CONs Need for oxygen (3,600 tpd for 20,000 bpd)

Heat integration in important

Limited references on GTL conditions (burner design)

,


ORYX ATRORYX ATR BASEDBASED SYNGASSYNGAS SECTIONSECTION


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ORYX ATRORYX ATR--BASEDBASED SYNGASSYNGAS SECTIONSECTION



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FLUIDISEDFLUIDISED AUTOTHERMALAUTOTHERMAL REFORMINGREFORMING


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FLUIDISEDFLUIDISED AUTOTHERMALAUTOTHERMAL REFORMINGREFORMING

PROs Scaleable to high capacities

Based on FCC experience

CONs Severe catal st o eratin re ime

Possibly complex operation and controls

Complications of dust, attrition, erosion etc

Process believed to have been abandoned


H2/CO RATIO V/S CO YIELDH2/CO RATIO V/S CO YIELD


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H2/CO RATIO V/S CO YIELDH2/CO RATIO V/S CO YIELD

%

C0

YIELD SMR ATR POX COPOX IDEAL

70 3

.

92 1.8

96 1.9

100 2.1




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Steam reforming (SMR)

Conventional SMR

Autothermal reforming (ATR)

Fixed Bed Adiabatic

Compact Reforming

-

Oxygen blown

Air blown


Non catalytic

Hybrid processes

Combined Reforming Catalytic Gas Heated Reforming (GHR)*

EHTR Post Reforming

43L Fundamentals, 1-3 Dec, 2009, Cape town

HYBRIDHYBRID PROCESSESPROCESSES


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HYBRIDHYBRID PROCESSESPROCESSES

Combi reforming : SMR + ATR in split - parallel

2-step reforming : SMR + ATR (OBS) in series


Combi POx : POx + SMR in independent modePOx / ATR + EHTR* in split-parallel

and offer higher integration potential

44

.


COMBICOMBI REFORMINGREFORMING


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reformer

Around 1/3rd of the reforming duty is done on the steamreformer and the balance on the ATR. This maximizes

production compared to an ATR on its own and the steamreformer is relatively small

Since combined reforming has both an ASU and a steamre ormer t e overa system is more comp ex an t is canaffect reliability




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PROs Established technology for methanol

g s ng e s ream capac y ~ , p

s More complex than steam reforming or ATR alone

Steam ratio and therefore H2 : CO ratio higher than ideal for GTL


LURGI'SLURGI'S COMBICOMBI--REFORMINGREFORMING


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LURGI SLURGI S COMBICOMBI REFORMINGREFORMING



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TWO STEPTWO STEP REFORMINGREFORMING


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TWO STEPTWO STEP REFORMINGREFORMING

Process

Steam

ue gas

Steam

to and fromFeedstock

Recycle

Oxygen + steam

Combustion air

By-pass

Feed

Hydro-

desulphurizerZnO bed

Fuel gas

49

to Heat Recovery

L Fundamentals, 1-3 Dec, 2009, Cape town

SYNGASSYNGAS ROUTE AND PLAYERS OVERVIEWROUTE AND PLAYERS OVERVIEW


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SYNGASSYNGAS ROUTE AND PLAYERS OVERVIEWROUTE AND PLAYERS OVERVIEW

Syngas Route Regime : Provider

Steam Reforming (SMR)

Combi : Lurgi* / Petro SA

Compact : BP-Davy* / One SynergySevere : Rentech

Non-Catalytic : Shell (SGP*) + SMR /

Catalytic : Conoco (CoPOx)*Fixed bed : Topsoe*-Sasol-Chevron

*-

(ATR)

Fluidised : ExxonMobil *

Combi : Lurgi * / GTL F-1

Regenerative reforming +

O2-based

(A)GHR* + OBS : Johnson Matthey

EHTR* + Pox : Technip-Air Products +

XTL Fundamentals, 1-3 Dec, 2009, Cape town 50

ADVANCESADVANCES IN SMRIN SMR SYNGASSYNGAS ROUTESROUTES


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Regenerative reforming se o process gas g - eve ea or par re orm ng

Substantial reduction in reformer duty and firing

Smaller reformer and steam system

Configurations

n - ou

Enhanced Heat Transfer Reformer (EHTR )

-Advanced Gas Heated reformer (AGHR)


REGENERATIVEREGENERATIVE REFORMING : EHTRREFORMING : EHTR


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Feed + Steam

Transfer Reformer

n - ou

Hot reformed gas

Source

Total reformed gas to


EHTREHTR DESIGN ANDDESIGN AND FABRICATIONFABRICATION


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POXPOX + EHTR+ EHTR


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2Natural Gas /(CO2)Oxygen

Syngas

Advanced EHTRGasifier

toEHTR



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GAS HEATED REFORMING + ATR IN SERIESGAS HEATED REFORMING + ATR IN SERIES


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Heat recycle to feed

Process wit out power export & ow CO2 emissions

Being developed at steam ratio of 1.0 with recycle CO2an or a -gas

oxygen

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CO2 UTILIZATIONCO2 UTILIZATION


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3.03.0

2.02.0

1.01.00.8

0 0.5 1 1.5 2

CO2

/C Ratio in Feed (mol / mol)


COCO22 REMOVAL (BASFREMOVAL (BASFAA--MDEAMDEA PROCESS)PROCESS)


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CW

LP Flash

2

Purified Syngas

CO2Stripper Absorber

MP FlashRawSyngas

CW




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Introduction



Challenges and Options in optimizing Syngasgeneration

Brief Scouting Comparison

Innovative Developments

Conclusions


CHALLENGES ON SYNGAS FOR GTLCHALLENGES ON SYNGAS FOR GTL


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Process optimization for achieving the required H2/CO ratio

Minimized level of inerts and contaminants

. Level of CO2 removal / recycle and its integration

Other contaminants anal sis and handlin when usin solidfeedstocks

Environmental aspects CO2 Management

Process and effluent water treatment / reuse

vera wa er a ance an rea men esp. w so ee s



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CHALLENGESCHALLENGES FOR EQUIPMENTFOR EQUIPMENT


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Very large capacity equipment Building block approach

Benchmark scale-up limits

Combating potential metal dusting Combined severit of com osition hi h % CO with hi h Tem &

pressure

Multiplicity of equipment against economy of scale andc us er ayou


HYDRAULICS USING CFD MODELINGHYDRAULICS USING CFD MODELING


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No Stagnation

Flue gas tunnelEnsuring better performance

Higher plant reliability

Lower life cycle costs


MODULARIZATION AND PREMODULARIZATION AND PRE--FABRICATIONFABRICATION


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Considerations

Site conditions

Overall schedule

Site labor situation

Transport

Cost-effectiveness



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GTL ENERGY (MIS) MATCH : SMRGTL ENERGY (MIS) MATCH : SMR


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Power

export

Waste heat recovery

Process gas and Flue gas Reaction heat recovery

SyngasGeneration F-TSynthesisNG SynfuelsSyngas

Endothermic

(external combustion)

Endothermic

(external combustion) ExothermicExothermic



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TYPICAL REACTION WATERTYPICAL REACTION WATERTREATMENT SYSTEMTREATMENT SYSTEM


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Off-gas fuel

Distillation unit

FT

reaction

water

Secondarytreatment

Tertiarytreatment Cooling

Effluent

water

make-upAir




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Introduction

Specifics of Syngas for GTL


a enges an p ons n op m z ng yngas genera on Brief Scouting Comparison

Conclusions


COMPARATIVE SUMMARYCOMPARATIVE SUMMARYFEED : LIGHT NG CN =104FEED : LIGHT NG CN =104


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POxATRSMR +SMR

0.21.41.52.7Steam / Carbon (molal)

1.92.33.04.8H2/CO

0.640.640.48NAOxygen / Carbon (molal)

NoPartial

(


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ATRPOx +

SMRSMR +

OBS

POx +

EHTR

GHR +

OBS

S/C for SMR 0.9 1.4 2.2

Oxygen kg/bbl 210 170 190

2.5

230

0.9

160

, . . .

Syngas 1), kg/bbl 605 590 570

.

550

.

600C-efficiency % 75 78 76 80 81

CO2

impact, kg/bbl 150 120 105190 100

Relative ranking2)

3 2Base 4 1-21-2

1) H2/CO ~2, max. inerts ~8% vol. dry

+ Full Heat Integration

74




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Introduction

Specifics of Syngas for GTL



Conclusions


INNOVATIVE DEVELOPMENTSINNOVATIVE DEVELOPMENTS


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Syngas CO2 - methane (dry) reforming

Compact Reformer

Catalytic POx (CPO)

Ion-transport ceramic membranes (ITM) for O2 generation as well

GTL More active and selective F-T catal sis

FPSO systems for localized (smaller) scale units

Direct liquids from hydrocarbon pyrolysis


BPBP--DAVY COMPACT REFORMERDAVY COMPACT REFORMER


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Steam raising eliminated

Modular fabrication andtransportation

Bundle fits standardcontainer

Small footprint (25% ofconventional SteamReformer)

Maximum ca acit 2500bpd


CATALYTICCATALYTIC POXPOX


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PROs

Small reactors and catalyst volumes

Lower tem eratures with low CH and CO in s n as High efficiency

CONs

Not commercially proven (COP pilot unit)

Sophisticated reactor designs

ove ca a ys s; nconven ona reg me


ION TRANSPORT MEMBRANE (ITM)ION TRANSPORT MEMBRANE (ITM)


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ION TRANSPORT MEMBRANEION TRANSPORT MEMBRANE


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10000

ivity Membrane

Uto ia

100

2

Selec

O2

/N

Polymer Upper Bound

1

1 100 10000 1000000

Relative Oxygen Flux

80


ITM FORITM FOR SYNGASSYNGAS FROMFROM NGNG ::


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O2 (air)e-

O2-CO + 2H2

yngas Depleted Air

O2 + 4e- 2O2-

e-CH4 + O

2- CO + 2H2 +

2e-

2 a rO2-

CH4

Steamee

Reduction

catalyst

Reforming

catalyst

US DOE Project (1997US DOE Project (1997--2005) involving Air Products, ARCO, Chevron, Babcock2005) involving Air Products, ARCO, Chevron, Babcock

[Oxygen Transport Membrane (OTM) alliance of[Oxygen Transport Membrane (OTM) alliance of SasolSasol, BP Amoco, Praxair,, BP Amoco, Praxair, StatoilStatoil is dissolved]is dissolved]


ITMITM SYNGASSYNGAS CAPITAL COST REDUCTIONCAPITAL COST REDUCTION


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Syngas

Air Products & Chemicals Inc.


NOVELNOVEL SYNGASSYNGAS PROCESSESPROCESSES


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Ceramic membranes Potential for reduced cost air separation

Combined directly with partial oxidation/reforming

Plasma process

At small scale

Direct oxidation to products (e.g. methanol, gasoline) Bypasses syngas formation step completely

Yields and selectivities very low

If low temperature process then heat utilisation difficulties


NOVEL GTL PROCESSESNOVEL GTL PROCESSES


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Com actGTL Compact multi-channel reactors

Steam reforming

Compact integrated processes for offshore use

Aimed at associated gases to facilitate oil productionopera ons w ou ar ng

Velocys

Nippon GTL

CO2 reforming Aimed at natural gas feedstocks with high CO2 levels


MATERIALS OF CONSTRUCTIONMATERIALS OF CONSTRUCTION


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Corrosion has always been a problem with syngas plants Limited or manageable with conventional plants at high

steam ratios

r v r r u Can be very severe at steam ratios of 1 or less

reformers S ecific o eratin conditions are im ortant

Development programmes continuing to find improvedsolutions New a oys

Better understanding of existing materials


SYNGASSYNGAS PROCESS DEVELOPMENT NEEDSPROCESS DEVELOPMENT NEEDS


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Lab facilities Catal sts

Process conditions

Materials of construction

Feed conversion and yield

Recycle effects and options

Demo scale units Catalysts and equipment

erformance

Operational testing

Material feedback

New lessons learned


CARBONCARBON EMISSIONSEMISSIONS


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87

ource: ray



I t d ti


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Introduction Specifics of Syngas for GTL



Conclusions


CONCLUSIONSCONCLUSIONS

C t ff ti ti ti f t d d NG i k d i GTL


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Cost-effective monetization of stranded NG is key driver GTL Syngas generation constitutes a major portion of a GTL

complex

ap a cos Energy input

GTL units above 17-22,000 bpd generally exceed current-

Though syngas technology is mature, advanced and

innovative solutions are still bein develo ed to res ondeffectively to the emerging needs and challenges


CONCLUSIONSCONCLUSIONS

S t h l th h t d ll f d d


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Syngas technology though matured, calls for advancedsolutions, esp. for larger units for effectively responding tothe emerging needs and challenges.

Even with relatively cheap gas, it requires judicious steam-power synergy for improving the capital efficiency, economicvia i ity an H E comp iance

Future innovations are poised towards lower cost Oxygen,higher C and energy efficiencies and lower CO2 footprintSyngas


ORYX ATARORYX ATAR


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0.32 Bcfd Natural gas

, p

0.8 Bcfd Syngas


003 - Syngas Generation for GTL.pdf

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