Roads to Olefins -Sinopec [兼容模式] - Platts · Technical Solutions Major Solutions to Olefin...

Petroleum, Gas, or CoalRoads to OlefinsRoads to OlefinsWANGChaosheng,RegionalRepresentative,Technology&Marketing

AsianRefiningSummit,Singapore,March,2016

Outline

Ⅰ Olefin/Polyolefin Demand and Capacity in China

Ⅱ Technical Solutions to Olefin Production



Ⅲ Review of ProjectsⅢ Review of Projects

Ⅳ Sinopec Olefin TechnologiesⅣ Sinopec Olefin Technologies

Ⅴ SINOPEC T h l C LtdⅤ SINOPEC Technology Co., Ltd.

Outline


Ⅱ Technical Solutions to Olefin Supply


Ⅱ Technical Solutions to Olefin Supply



Ⅴ Si T h l C LtdⅤ Sinopec Technology Co., Ltd.

Olefin/Polyolefin Demand in China

Ethylene Demand and Capacity


Propylene Demand and Capacity


Propylene in 2015Ethylene in 2015

• Capacity growth 11% in 2015- No steam cracking

• Capacity growth 2% in 2015- No steam cracking g

- FCC: 130 K MTA- PDH: 1300 K MTA- CTO /MTO: 880 K MTA

gprofitability improved

- CTO + MTO new capacity: 300+450 K MTA

- Paraffin DH: 325 K MTA

• Demand continues to grow f

low operation ratedue to operation problem

and high cost - Balanced by 2.8 m MT of import

• Demand continues to grow - Driven by downstream.

B l d b 1 5 MT f i t- Balanced by1.5 m MT of import


Butadiene Capacity and Growth


Butadiene

• On-purpose capacity 14.3% of the total, low operation rate of oxidative dehydrogenation units due to low BD y gprice and high cost.

• Demand affected by the shrink auto industry rubber. Oversupply.

• Refinery / naphtha cracking C4 extraction will remain mainstream.


Olefin Demand Continues Grow in the Future

• 2014 PE consumption per capita: China: 16 4 kg developed countries: 36~38 kgChina: 16.4 kg, developed countries: 36 38 kgPar by 2035 @4% growth

• 2014 PP consumption per capita: p p pChina: 14 kg, developed countries: 17~18 kgPar by 2022 @4% growth

Olefin capacity investment: moderate and rationalOlefin capacity investment: moderate and rational

Outline

Ⅰ Olefin and Polyolefin Demand in China







Technical Solutions

Major Solutions to Olefin Production

Steam CrackingFeedstock flexibility, product spectrum ,

downstream integration

Naphtha, LPG, ethane, propane

Maximize

FCC (DCC, CPP)

Maximizepropylene/ethylene gain, Competing with gasoline,

production cost

Access to Resid, VGO

production cost

PDHLow investment, on

purpose product Access to propane

MTO/MTP

Alternative resources, High investment,

environment, competing Methanol from Coal, Natural Gas,

Biomass, p guses

Others

Light hydrocarbon cracking,

Maximum utilization of materialOthersdehydrogenation, disproportionation

Maximum utilization of material

Technical Solutions

Economic Comparison

Scale (KTA)

FeedstockInvestment

(billionYuan)

Pre-tax Return

Rate(%)Mat OP

) ( )

S.CR 1000 Naphtha 4 13.8 94

CPP 1500*Paraffinic

3 17 8 91 +CPP 1500AR

3 17.8 91 +

DCC 1700* VGO 1.2 15.8 95 -

PDH 450 Propane 1.9 15.3 88

MTO 1800* Methanol 2.5 17.9 89 -

MTP 1660* Methanol 2 15.2 91 -

* Feedstock** Price prediction based on historical data,

*** Brent oil $80 / bbl

Technical Solutions

Watershed: 2010, Oil price 70 – 90 USD/bbl

• Before 2010, olefin/polyolefin expansion based crude feedstock

• 2010, first coal polyolefin plant in operation2010, first coal polyolefin plant in operation• After 2010, almost all olefin/polyolefin projects are coal

based, or MTO, PDH

• 2015～2019: New PP 12.23 m MTA, 73% of world total. Mainly coal or PDH basedMainly coal or PDH based.- Coal PP share: 10% in 2014, 30% in 2019

• 2015～2019: New PE 7.72 m MTA, 35% of world total.2015 2019: New PE 7.72 m MTA, 35% of world total. Mainly coal based.- Coal PE share: 4% in 2014, 26% in 2019

Technical Solutions

Ethylene + Propylene Capacity in 2015

• 48~50 m MTA• About 25% from CTO/MTOAbout 25% from CTO/MTO

C2 about 15% from none-crude

• PDH PP: 4.4 m MTA• CTP/MTO PP: 4.2 m MTA• PP Total: 28 m MTA

30%+ from none-crude

Technical Solutions

Cost Comparison

Outline








Review of Projects

PDH Built:

Project Scale (KMTA) Process Start Site

1 天津渤化 600 Oleflex 2013 天津

2 绍兴三圆 450 Oleflex 2014 绍兴绍兴圆绍兴

3 卫星石化 450 Oleflex 2014 嘉兴

4 海越股份 600 Catofin 2014 宁波

5 烟台万华 750 Oleflex 2015 烟台烟台万华烟台

6 扬子江石化 600 Oleflex 2015 张家港

7 宁波福基 660 Oleflex 2015 宁波

8 山东京博(混合烷烃) 125 Oleflex 2015 山东8 山东京博(混合烷烃) 125 Oleflex 2015 山东

9 山东神驰(混合烷烃) 200 Oleflex 2015 东营

小计 4435

Review of Projects

PDH Planned:

10 扬子江石化（二期） 600 Oleflex 2017 张家港

11 宁波福基(二期) 660 Oleflex 2017 宁波

12 山东海力 600 C t fi 东营12 山东海力 600 Catofin 东营

13 长江天然气化工 650 Oleflex 南通

14 中国软包装 800 Oleflex 福清

15 石大胜华 200 Oleflex 东营

16 卫星石化(二期) 600 Oleflex 嘉兴

17 鹏尊能源 300 Oleflex 湛江17 鹏尊能源 300 Oleflex 湛江

18 盘锦和运 600 盘锦

19 上海华谊 600 上海

M f th l d PDH MTO j t ill b t d l d

小计 5610

• Many of the planned PDH, MTO projects will be postponed or canceled

Review of Projects

CTO/MTO Built + 4 more:

Startup ProjectMathanol Cpty

(KMTA)M OP Rate

Olefin Cpty (KMTA)

O OP Rate

2010年8月神华包头一期 1800 95% 600 100%

2010年9月神华宁煤一期 1680 95% 500 100%

2011年6月大唐多伦 1680 0% 460 35%2011年11月中原石化 600 -- 200 100%2013年1月宁波富德 -- -- 600 65%2013年9月南京惠生 -- -- 300 100%2014年7月寿光鲁清 -- -- 200 0%

2014年7月延长中煤榆林 1800 80% 600 110%

2014年8月神华宁煤二期 -- -- 500 100%

2014年8月中煤榆林一期 1800 95% 600 106%2014年8月中煤榆林期 1800 95% 600 106%

2014年9月山东玉皇 -- -- 100 80%2014年11月宁夏宝丰 1800 95% 600 100%2014年11月神达化工 -- -- 340 80%2014年12月陕西蒲城 1800 92% 680 84%2014年12月陕西蒲城 1800 92% 680 84%

2014年12月东营瑞昌一期 -- -- 100 0%

2014年12月沈阳蜡化 -- -- 100 95%2015年3月齐成华滨 -- -- 200 30%2014年4月浙江兴兴 -- -- 690 100%2014年4月浙江兴兴 690 100%2015年4月鲁深发 -- -- 200 30%

7570

Review of Projects

CTO/MTO Planned:

• By 2017, 14 MMTA new MTO capacity approved, with 5 MMTA PE and 5 8 MMTA PP5 MMTA PE and 5. 8 MMTA PP

• Another 10 MMTA CTO are proposed

Many of these projects will be postponed or canceledMany of these projects will be postponed or canceled though, the impact on market will be huge.

to die or to change the game?to die or to change the game?

Review of Projects

Future investment in coal chemical

• Utilization of Coal• Feedstock availability for fuels and chemicals• Government policy change on coal chemical

- Local GDP- Environment concern, public awareness- Water problem- Carbon emission international commitment - Taxation

• Crude / propane / ethane price• Downstream market: location, demand and price

• Economics: Pre-tax return rate btw. 5%~10% at 50~60 USD/bbl Brent - UBS

Review of Projects

Future investment in olefins

Steam CrackingFeedstock flexibility: naphtha, LPG,

ethane, propaneDownstream integration

FCC (DCC CPP)Maximum utilization

FCC (DCC, CPP)Upstream integration

PDH etcOpportunity feedstock

PDH etcIndependent players

CTO/MTO …

Outline








Sinopec Olefin Technologies

Related Technologies

CBLSteam Cracking, Flexible to feedstock, unique tube technologyunique tube technology

DCC Deep Catalytic CrackingCPP Catalytic Pyrolysis Process

OCC Olefin Catalytic CrackingOCC Olefin Catalytic Cracking

SMTO Methanol to Olefin

….


SINOPEC has a complete system for technology R&D, engineering and operation, from oil E&P, refining, to petrochemicals.

8 Research Institutes Sinopec Engineering Group

FRIPP-Fushun Research Institute of Petrochemical ProcessingPEPRIS-Exploration &

SRIPE- Research Institute of Petroleum Engineering

Processing

BRICI-Beijing Research Institute of Chemical Industry

Production Research Institute

Institute of Chemical Industry

QDSEI-Qingdao Safety

RIPP-Research Institute of Petroleum Processing

SGRI G h i lSRIPT-Shanghai Research Institute of Petrochemical Tech

Q Q g yEngineering Institute SGRI- Geophysical

Research Institute

Sinopec Olefin Technologies: CBL

CBL Steam Cracking Technology

• Sinopec has rich experience in cracking furnace design

to realize value cracking and increase feedstock flexibility

and development (CBL technology). Single furnace max

capacity is 200 KTA.

300 KTA furnace under design.

• Spectrum of feedstock: from light feedstock, such as

fethane and light hydrocarbons, to heavy feedstock as

diesel and HVGO.

• Till now 113 furnaces have been built by using CBL• Till now, 113 furnaces have been built by using CBL

technology. The total capacity is 11.3 Mt.

Gas furnaces: 23. Total gas capacity is 2.7 Mt.g p y

Sinopec Olefin Technologies : CBL

Enhanced heat transfer technology

High temperature(780~900℃), short residence time and lower hydrocarbon partial pressure

H t i t d t th fl b d l Ch ll Heat resistance due to the flow boundary layer and coking, resulting in over temp. and shortened run length

Challenges

Quick heat transfer through tube wall into the fluid body

Reduce cokingTargets

g Extend run length

Solution: Swirling Element Radiant Tube technology (SERT)

Enhance heat transfer, reduce coking and extending run lengthEnhance heat transfer, reduce coking and extending run length

Sinopec Olefin Technologies: CBL

To change the flow pattern of the

SERT for Steam Cracking Furnace Tube

To change the flow pattern of the fluid body

Thinner boundary layerThinner boundary layer

Reduced coking rate

Reduce Tube Metal Temperature (TMT)

Extend run length

To change feedstock flow pattern: from plug flow to swirl flow- increase flow velocity along the tube perimeter, and reduce the laminar boundary layer. Turbulent flow to enhance heat transfer y y- the scouring force of the feedstock flow reduces the coke formation

Sinopec Olefin Technologies : CBL

SERT for Steam Cracking Furnace

The influence of SERT on the cracking furnaceitem Without SERT With SERT

P d t i ld BASE N t ti

The influence of SERT on the cracking furnace

Product yields BASE Not negative

TMT BASE Reduce at least 20℃

Run length BASE Increase at least 40%

Capacity BASE Increase about 7%

Operation BASE No additional workload

* Under the same operation conditions with insertion of the tube with twisted-tape Under the same operation conditions, with insertion of the tube with twisted-tape

• Lower cost! (comparing with other heat transfer enhancing technologies)• Can be installed on incumbent tubes

Tubes with SERT insertion can handle flexible feeds (naphtha propane etc )• Tubes with SERT insertion can handle flexible feeds (naphtha, propane, etc.)

Sinopec Olefin Technologies : SERT

Comparison between furnaces with and without SERT

SERT for Steam Cracking Furnace

• TMT • Pressure drop

1100

1120

1140

1100

1120

1140

TMT NO SERT280

290 no SERT with SERT

1040

1060

1080

1040

1060

1080

ubew

all t

emp

260

270

essu

re (K

pa)

with SERT

980

1000

1020

980

1000

1020

tu

With SERT240

250

inle

t pr

0 20 40 60 80 100980 980

runlength(day) 0 10 20 30 40 50 60 70230

run length (day)


ZHENHAI 1,000 KTA Ethylene complex (SERT used)

– Feed：HVGO, NAP, C2/C3, LPG, C5– Thermal Eff.: 93.8-94.5%– Run length g

• NAP: more than 119 days • C2: 133 days

HVGO: 121 days• HVGO: 121 days– Liquid furnace: CBL-Ⅲ– Gas furnace: CBL-R– Capacity:

• 120 kta gas feed• 100 kta liquid feed (9 furnaces)100 kta liquid feed (9 furnaces)• 150 kta liquid feed, double firebox

– Feed in on Apr. 20, 2010


SERT for any kind cracking furnace tube

B 2013 SERT h b i t ll d i

Commercial Experience Commercial Experience

By 2013, SERT has been installed in 113 ethylene cracking furnaces, including installations in Malaysia, Thailand and USA.

The SERT in the online furnace

Applicable, when • Revamp: replace the radiant coils

• Revamp: modify the incumbent coils

• Build new cracking furnace

Sinopec Olefin Technologies: DCC

DCC (Deep Catalytic Cracking)

1. Maximum propylene and butylenes production2. Riser reactor plus fluid bed reactor with p

continuous reaction/regeneration circulation operation. Reaction temperature is much lower than that of steam cracking.

3. Recracking a portion of DCC part range or full k d hth li ith ith trange cracked naphtha coupling with or without

C4 cut in the DCC operation will increase the yield of propylene and BTX at a naphthayield of propylene and BTX at a naphtha expense.

4 Proprietary catalyst4. Proprietary catalyst


Block flow diagram of DCC/CPP plant & integration

To diesel blending

GasPurificate

EthyleneRecovery

Unit

Light

Ethylene to plant

Propylene to storageEnds Unit

C3 & C4Purification Split

C3Spliter

C

To storageC3 cut

Propylene to storage

LPG to storage

FractionatorGasolineSelective

Hydrogenation

Vacuum

H2 Otherfeeds

C4cut

H2

Gasoline

C cut to MTBE PlantVGOHTU

DCC/CPP reactor& Regenerator

gasoil C4 cut to MTBE Plant

Decanted oil to fuel


DCC Commercial Mode

Two DCC operation modes in commercial prunning:DCC-IDCC-I

Riser plus fluidized dense bed reactor Manxumum proplyene operation modep p y p

DCC-IIRiser reactorRiser reactorManxumum isoolefins operation mode


Light olefin yields from the representatives feedstock for DCC-I

Number 1 2 3 4

VGO VGO + Resid VGO + DAO VGO Feedstock VGO

Paraffinic baseVGO + Resid Paraffinic base

VGO + DAO interm base Naphthenic

base

Density, g/cm3 0.8449 0.8621 0.9085 0.9249

UOP K 12.7 12.6 12.0 11.4

Hydrogen, w% 14.23 13.62 12.52 12.24

Olefin yields, w%

Ethylene 5.8 3.6 3.5 3.6

Propylene 23.7 22.9 18.3 13.2

Butylenes 17.8 17.4 14.0 10.6


Light olefin yields from representative feedstock for DCC-II

Number 1 2 3 4

Feedstock VGO VGO + Resid VGO + DAO VGO NaphthenicFeedstock Paraffinic base Paraffinic base interm base Naphthenic

base

Density, g/cm3 0.8579 0.8939 0.8983 0.9249

UOP K 12.4 12.5 12.0 11.4

Hydrogen, w% 13.45 12.87 12.63 12.24

Olefin yields, w%

Propylene 14.3 11.8 12.5 7.9

Isobutylene 6.1 5.3 4.6 3.5

Isoamylenes 6.8 5.5 5.8 4.1

Sinopec Olefin Technologies: CPP

CPP (Catalytic Pyrolysis Process)

1. Maximum ethylene and propylene

2. Riser reactor with continuous reaction/ regeneration circulation operation. Reaction temperature is much lower than that of steam cracking.

3. Catalyst: Proprietary catalyst

4 Feedstock: VGO and heavier4. Feedstock: VGO and heavier


CPP Commercial Mode

Three test modes were carried out during gcommercial trial of CPP technology:

CPP-P is for max propylene production,

CPP-E is for max ethylene production.

CPP-P&E is for max ethylene & propylene production.p


CPP Demonstration unit- feedstock properties

Test mode CPP‐P CPP‐P&E CPP‐E

Density(20℃)/g cm‐3 0 9002 0 9015 0 9012Density(20℃)/g.cm 3 0.9002 0.9015 0.9012CCR, wt% 4.7 4.9 4.7H, wt% 12.82 12.86 12.84S, wt% 0.16 0.16 0.16N, wt% 0.29 0.26 0.25Ni ppm 5 8 6 2 6 3Ni, ppm 5.8 6.2 6.3Group composition, wt%

Saturates 56.3 54.8 55.5Aromatics 27.2 28.4 28.0Resin 15.7 16.0 15.7Asphaltene 0.8 0.8 0.8Asphaltene 0.8 0.8 0.8


CPP Demonstration unit- Products yield

Test Mode CPP‐P CPP‐P&E CPP‐E

Products yield, wt%

Dry gas 17.64 26.29 37.13

LPG 43.72 36.55 28.46

C5+Naphtha 17.84 17.61 14.825 p

LCO 11.75 8.98 7.93

Coke 8.41 9.67 10.66Coke 8.41 9.67 10.66

Losses 0.64 0.90 1.00


CPP Demonstration unit- olefins yield

Olefins yield，wt% CPP‐P CPP‐P&E CPP‐EOlefins yield，wt% CPP P CPP P&E CPP E

C2= 9.77 13.71 20.37

C3= 24.60 21.45 18.23

C4= 13.19 11.34 7.52

Total olefins yield, wt% 46.96 46.50 46.12y ,


CPP Demonstration unit- Naphtha

Test modes CPP‐P CPP‐P&E CPP‐E

D it / 3 0 8158 0 8261 0 8315Density，g/cm3 0.8158 0.8261 0.8315

RON 97.8 101.6 102.5

MON 82.1 87.6 87.8MON 82.1 87.6 87.8

Group(GC), wt %

n‐Paraffins 6.30 3.76 1.24

i‐Paraffins 3.77 2.96 2.63

Naphthenes 1.73 1.51 0.76

Olefins 9.28 12.79 16.25

Aromatics 78.92 78.98 79.12

Sinopec Olefin Technologies: DCC/CPP

Light olefin Yield Comparison among FCC,DCC &CPP

25 FCC DCC CPP

15

20

d, m

%

5

10

Ole

fin y

iel

0Ethylene Propylene Butylenes

O


CPP/DCC operation parameters

Technology F C C D C C C P P

Reaction Temp. oC Base +0‐50oC +80‐150 oC

/CTO, M/M Base 1.5‐2 times 2‐4 times

Reaction Time, s Base longer longerg g

Reaction Pressure Base Lower Lower

Steam Base More Much More


Jinan Company SINOPEC

SINOPEC DCC Technology Commercial Experience

Jinan Company, SINOPEC Start up November 1990 First DCC unit in the world

Jinan

TPI Thailand’s TPI Start up May1997 First DCC unit outside China

Petro Rabigh

Rabigh Refining & Petrochemical Co.

Start up February 2012 The largest capacity 92,000 bbl/d

There are 16 DCC units under designing, construction and

(460 MMT/a)

running in the world10 unitsChina

2 unitsThailand

1 unitsRussia

1 unitsSaudiArabic

2 unitsIndiaChina Thailand Russia ArabicIndia

Sinopec Olefin Technologies: COAT

Recover C2 from refinery off-gas

Refinery off-gas includes

• FCC dry gasFCC dry gas

• The content of ethylene and ethane, about 10~20%

• Coking dry gas & light hydrocarbon dry gas, etc.Coking dry gas & light hydrocarbon dry gas, etc.

• Less ethylene but more ethane

• At present, refinery off-gas are mainly used as fuel gas.At present, refinery off gas are mainly used as fuel gas.

• How to make good use of refinery off-gas and convert low

b h d b i t hi h l dd d d tcarbon hydrocarbons into high value-added products are an

important topic for refining enterprise to enhance their

competitiveness.


Extract the ethylene-rich gas from FCC dry gas


Extract the ethylene rich gas from FCC dry gas

cryogenic separation pressure swing adsorption (PSA) oil absorption

Commercialized• High recovery of ethylene

• Large investment，hi h ti

Commercialized• More equipments，• complicated control,

Commercialized• High recovery of ethylene

• Less equipments,i l ti• high energy consumption,

• complicated operation

p• short operating cycle • simple operation,

• long operating cycle


Fuel gas CO O NOx

Technology Features of COAT

Fuel gas CO2 O2、NOx

t n

C2-rich gasre

ssio

n ni

t

ptio

n U

nit

gena

tion

nitoniz

atio

nU

nitFCC off-gas

53kt/a

Com

pr Un

Abs

orp

Deo

xyg un

Dec

arb U108 kt/a

H2,CH4,N2,O2,NOx,CO,etc. are removed by the process above 0℃. The obtained C2-rich gas is sent to caustic washing tower of ethylene unit. Surplus waste heat in refinery can be used to supply heat and cold sources Surplus waste heat in refinery can be used to supply heat and cold sources. Through lithium bromide water absorption refrigerating equipment, 5℃ cold water can

be obtained to supply cold sources. The propylene refrigeration compressor and dryerare NOT needed.

Refinery C4 fraction is used to absorb C2 fraction. The stable gasoline is used torecover the losing C4 fraction entrained by fuel gas.


Case StudyCase Study


The first COAT unit successfully and safely began in 2011 and is producing high quality C2 gas to the ethylene plant. (oil-in: September 22th, 2011)

Ethylene recovery rate is 93%, with 80%+ ethylene and ethane in the products. Oxygen content is lower than 0.1PPM.

There are 4 new units either in construction or in detailedconstruction or in detailed engineering.

100 kt/a COAT Unit in Qilu, Sinopec


Technology advantagesTechnology advantages

High recovery of ethylene the performance data of Qilu unit is 93% C2 recovery (guaranteed value:

92%).

Simple process use conventional and less equipment no need of adsorbent (Ref use conventional and less equipment, no need of adsorbent (Ref.

technology: complicated process and more equipment)

Stable operation simple operation, stable running, long operation cycle. (Ref. technology:

complicated control, unstable running, short operation cycle)

Less floor area Less floor area Qilu unit covers about 2700m2, the floor area increases a little with scaling

up. (Ref. technology: one unit covers about 3800m2, the floor areai h ith li )increases much more with scaling up)


Technology advantagesTechnology advantagesL i t t Low investment Using less pieces of conventional equipment, and using the refinery’s

surplus waste heat

High quality product

Unique advantages in impurity removal

Less energy consumption: The low grade heat source of refinery is used: Qilu uses the surplus low

pressure steam as the heat source of absorption refrigeration and towerp p greboiler, with no need of high quality steam.

If the waste hot oil of refinery is used as the heat source, the energyconsumption of the unit will be further decreasedconsumption of the unit will be further decreased.

The successful running of the off-gas recovery unit using Cold OilAbsorption Technology shows that it is reliable and can be widelyAbsorption Technology shows that it is reliable and can be widelyapplied.

Sinopec Olefin Technologies: LECT

Proprietary technology

Low Energy Ethylene Separation Technology

Proprietary technology minimum energy consumption easy operation high reliability.

Front-end Depropanization & Hydrogenation Quench Quench Compression, Front-end depropanization & hydrogenation, Cold separation, Hot separation and refrigeration systems.


Process Process Scheme Scheme Low Energy Ethylene Separation Technology

QO TowerQW TowerCGC1~4

HP DeC3 C2 Hydrogenation

C3 Washer

Propylene LP DeC3

Alkaline Tower

pyFractionatorDeC1 Tower

Pre-demethanizerEthylene Fractionator

Cold Box

DeethanizerFractionator

C3 Hydrogenation

C2 Washer


C1/C2/C3 Catalysts & Processes

C1 - Low Temperature Methanation

C2 - Selective Hydrogenation Technology

C2 - Selective Hydrogenation Technology

C3 - Selective Hydrogenation Technology Methanation

Catalyst• High activity in low

temperature 150 ~ 200℃

Technology• Front-end Selective

Hydrogenation Technology for Removal of Acetylene

Technology• Tail-end Selective

Hydrogenation Technology for Removal of Acetylene

Technology • Liquid-phase Selective

Hydrogenation Process and Catalyst for the Removal of Methyl200℃

• Adapting to various reactor and process

• Excellent operation flexibility & low cost

Removal of Acetylene in DepropanizerProcess

Removal of Acetylene in C2 Fraction

Removal of Methyl Acetylene and Propadiene in C3 Fractions

flexibility & low cost


• DCC/CPP

SummarySummary

- Leading technology for producing light olefins with heavy feedstock, which bridge refining with petrochemical industry.

CBL Steam Cracking ith SERT• CBL Steam Cracking with SERT- Leading technology for enhancing heat transfer and preventing coking.

COAT• COAT- Low investment to recover C2 from dry gas from FCC and other source.

LECT• LECT- A low energy ethylene separation technology, front-end depropanation

Sinopec Sinopec Technology Co. Ltd.Technology Co. Ltd.

Sinopec Technology Co. Ltd. is a subsidiary of SINOPEC Corp, in h f th li i d t f i f SINOPEC’ P i tcharge of the licensing and transferring of SINOPEC’s Proprietary

technologies and involved actively in global licensing market.

Process Design Package

Note: Providing the PDP is the main

Basic Engineering Design

ote o d g t e s t e abusiness of Sinopec Technology

Detailed Engineering Design Technical Service EPC Contractor Turn-key Project


Operating Model of Business Activities

SinopecTechProject Management

Technical Resources

Technical Business Activities

Business Team

Cooperation

Support

Partners Research Inst.

Cooperation Licensing Clients

Engineering Support

Engineering Corp.


SINOPEC Regional Representatives of Technology & MarketingSINOPEC Regional Representatives of Technology & Marketing

Offices in:• New York

Main Responsibilities

• Frankfurt• Hong Kong • Technology licensing

• Seeking cooperation opportunities with partnersopportunities with partners

• Quick response to alliances and clients

Contact Information Contact Information

For more information:For more information:For more information:For more information:http://www.sinopectech.com/english

Contact: Contact: WANG ChaoshengRegional Representative, Technology & Marketing SINOPEC Hong Kong Representative Office

Email: [email protected] Add.: 20/F., Office Tower, Convention Plaza

1 Harbour Road Wanchai Hong Kong1 Harbour Road, Wanchai, Hong Kong

Roads to Olefins -Sinopec [兼容模式] - Platts · Technical Solutions Major Solutions to Olefin...

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Transcript of Roads to Olefins -Sinopec [兼容模式] - Platts · Technical Solutions Major Solutions to Olefin...