Naphtha and Gas Cracking For Production of Olefins (Part - 1) Chemical Engineering Notes | EduRev

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Chemical Engineering : Naphtha and Gas Cracking For Production of Olefins (Part - 1) Chemical Engineering Notes | EduRev

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Naphtha and Gas Cracking For Production of Olefins

Olefins are major building blocks for petrochemicals. Because of their reactivity and versatility, olefins especially the light olefins like ethylene, propylene, butenes, butadiene, etc., there has been tremendous growth in the demand of the olefins. Olefins are finding wide application in the manufacture of polymers, chemical intermediates, and synthetic rubber. Ethylene itself is basic building block for large number of petrochemicals and is quoted as king of chemicals. Some of ethylene manufacturing company and their capacity is given in Table M-VII 2.1. The global ethylene capacity at January 1, 2011, net additions and closings was more than 138 million tones compared with nearly 130 million tones in 2008 .  Global ethylene capacity is given in Table M-VII 2.2.

The steam cracker remains the fundamental unit and is the heart of any petrochemical complex and mother plant and produces large number of products and byproducts such as olefins - ethylene, propylene, butadiene, butane and butenes, isoprene, etc., and pyrolysis gasoline. The choice of the feedstock for olefin production depends on the availability of raw materials and the range of downstream products. Naphtha has made up about 50-55percent of ethylene feedstock sources since 1992. Although basic steam cracking technology remain same for naphtha, gas oil and natural gas, different configuration of steam cracking plant are available from various process licensors. 

Table M-VII 2.1: Top 10 Ethylene Complexes 

 

Company

Location

Capacity, tpy

1

Formosa Petrochemical Corp.

Mailiao, Taiwan, China

2935000

2

Nova Chemicals Corp.

Joffre, Alta

2811792

3

Arabian Petrochemical Co.

Jubai, Saudi Arabia

2250000

4

Exxon Mobi Chemical Co.

Baytown, Tex.

2197000

5

Chevron Philips Chemical Co.

Sweeny, Tex.

1865000

6

Dow Chemical Co.

Terneuzen, Netherlands

1800000

7

Ineos Olifins& Polymers

Chocolate Bayou, Tex.

1752000

8

Equistar Chemicals LP

Channelview, Tex.

1750000

9

Yanbu Petrochemical Co.

Yanbu, Saudi Arabia

1705000

10

Equate Petrochemical Co.

Shuaiba, Kuwait

1650000

Table M-VII 2.2: Regional Capacity Breakdown

Ethylene Capacity, tpy

Asia-Pacific

42631000

Eastern Europe

7971000

Middle East, Africa

23357000

North America

34508000

South America

5083500

Western Europe

24904000

Total Capacity

138454500

Naphtha /Gas Cracking 

Requirement of steam will depend upon the type of feedstock; the lighter hydrocarbon requires less steam as compared to heavier feedstock. Steam cracking relative cost according to feedstock is given in Table M-VII 2.3. Steam requirement in steam cracker is given in Table M-VII 2.4 . Energy requirement pattern for olefin production is given in Table M-VII 2.5 .

Table M-VII 2.3: Steam Cracking Relative Cost according to Feedstock 

Feedstock

Relative Investment

Cost

Ethane

1.00

Propane

1.15

Butane

1.20

Naphtha

1.45

Atmospheric gas oil

1.65

Vacuum gas oil

1.84

Table M-VII 2.4: Steam Requirement in Steam Cracking

Feed

Kg steam/kg of hydrocarbon

Ethane

0.2 - 0.4

Propane

0.3 - 0.5

Naphtha

0.4 - 0.8

Gas Oil

0.8 - 1.0

Table M-VII 2.5: Energy Requirement for Olefin Production 

Feedstock

Specific Energy Consumption

Kcal/kg of Ethylene

Kcal/kg of Olefin

Ethane

310

3,050

Propane

4,100

3,050

Ethane/Propane

3,600

3,300

Naphtha

5,000

3,050

 

Modern ethylene plants incorporate following major process steps : cracking compression and separation of the cracked gas by low temperature fractionation. The nature of the feed stock and the level of pyrolysis severity largely determine the operating conditions in the cracking and quenching section. Various steps involved in the pyrolysis of naphtha and separation of the products are discussed below. In case of gas cracking separation of ethane and propane from natural gas is involved. Flow diagram for pyrolysis of napththa is given in Figure M-VII 2.1. 

Hot Section 

It consists of convection zone and radiant zone. In the convection zone, hydrocarbon feed stock is preheated and mixed with steam and heated to high temperature. In the convection zone the rapid rise in temperature takes place and pyrolysis reaction takes place. The addition of dilution steam enhances ethylene yield and reduces the coking tendency in the furnace coils. The production of the pyrolysis reaction consists of a wide range of saturated and unsaturated hydrocarbons.

 Quench Section 

To avoid subsequent reaction the effluent are fixed in their kinetic development by sudden quench first by indirect quench by water to 400 – 450 oC in transfer line exchanger or quench boiler. This is a large heat exchanger that is a bundle of metal tubes through which the gases pass and around which is circulated water under pressure. The hot water produced is used to generate steam for use in the plant. In the next step the quench is done by heavy product of pyrolysis. 

Naphtha and Gas Cracking For Production of Olefins (Part - 1) Chemical Engineering Notes | EduRev

Figure M-VII 2.1: Typical Naphtha Cracker Plant

HOT SECTION 

Convection Zone    Feed stock is pyrolised and the effluent conditioned

Radiation Zone      The product formed are separated and purified 

Quench                  To avoid subsequent reaction the effluents are fixed in their kinetics development by sudden quench. 

I Indirect                  Indirect quench by water to 400-500oC generation of high pressure steam 

II Direct                    Direct quench by heavy residue by-product of pyrolysis 

Primary Fractionation Column   Separation of light products of pyrolysis as top and bottom as pyrolysis product

Compression                              Compression of light products 

Caustic Scrubbing and Drying     Scrubbing with caustic followed by molecular sieve adsorption to remove sulphur compounds, mercaptan, etc. 

Cold Section

After compression, caustic scrubbing and drying the light effluents enter the cold section of the unit which performs the separation of (I) hydrogen to various concentration (ii) ethyllhene containing 99.4percent (iii) 95percent propylene (iv) A C4 cut containing 25-50percent butadiene (v) pyrolysis gasoline which is rich in aromatic hydrocarbons. The complexity of the separation section of a cracker increases markedly as the feed changes from ethane.  

COLD SECTION               · Hydrogen separation

                                          · Ethylene separation 99.9percent

                                          · Propylene separation

                                          · A C4 cut containing 25-50percent butadiene

                                          · Complementary fraction of pyrolysis gasoline rich in aromatic hydrocarbons

Demethaniser                    Methane condensed at top around – 1000C pressure 32 Pa

Deethaniser                       Separation of C2 cut;(Ethane and ethylene) Acetylene eliminated by selective hydrog-nation Catalyst : Palladium or Nickel 40-80oC, 3 kPa 

Separation of Ethylene       Ethylene is fractionated and unreacted ethane recycled

Depropaniser                     C3+ cut from bottom of deethaniser is fractionated.

                                            C3 cut from top of depropaniser is selectively hydrogenated to remove methyl acetylene and propadience.

                                            Propylene content 95percent.

                                            Separation in supplementary column for more pure propylene.

Removal of propane           Separation in supplementary column for more pure 

from propylene                   propylene   

Debutaniser                        Separation of C4 stream from C5+ stream  

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