Foundation Fieldbus End User Council

FCS & Modern Technologies_ Iran

Foundation Fieldbus End User Council

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به اطلاع کليه اعضا محترم مجمع کاربران فيلدباس ايران مي رساند:

دانلود برنامه سمينار مجمع كاربران خاورميانه در بحرين

Air Blowing

Air Blowing

در‌این روش از‌انرژی جنبشی وحرکتی‌جریان هوا‌برای تمیزکاری‌داخل خطوط‌ و Piping استفاده‌می‌شود.بسته به شرایط شرایط سایت ازنظرامکانات خدماتی‌تولیدهوا،دستگاههای‌تولیدهواوسایزخطوط این عملیات به‌سه‌روش مختلف انجام می گردد :

1) روش Air Accumulation

دراین ‌روش هوا درسیستم جمع‌آوری کرده‌ و مقدارمعینی فشارایجاد می‌کنیم.سیستم با تخلیه سریع ‌هوا بوسیله ولو یا Rupture Disk موادخارجی داخل لوله ها‌بیرون رانده شده وتمیزمی‌گردد.

2) روش Disect Blowing method

دراین روش هوا را بطورمستقیم واردسیستم‌کرده و ازطرف دیگرخارج می‌کنیم‌که ازهوای‌ شبکه هوای Utility استفاده می‌شود.

3) روش Scavenging Run of Process

دراین روش از‌کمپرسورهوای واحداستفاده می‌شود.

OLEFINS

OLEFINS

Olefins are the basic building blocks for many chemical syntheses. These

unsaturated materials enter into polymers, rubbers, and plastics, and react to

form a wide variety of chemical compounds such as alcohols, amines, chlorides

and oxides.

Steam Cracking is the thermal crachg and reforming of hydrocarbons in

the presence of steam at high temperature, short contact time, and rather low

pressure in a fired tubular furnace. From the standpoint of both the amount and

variety of compounds produced, steam cracking of gas oils and naphthas is one

of the most important petroleum process for producing a wide range of chemical

raw materials. Ethane and propane cracking are used widely by others but

relatively few products other than ethylene result.

In a typical gas oil design, the lighter products overhead from the quench

tower/primary fractionator are compressed to 210 psi, and cooled to about

100°F. Some C, plus material is recovered from the compressor knockout

drums. The gases are ethanolamine and caustic washed to remove acid gases:

sulfur compounds and carbon dioxide, and then desiccant dried to remove last

traces of water. This is to prevent ice and hydrate formation in the low

temperature section downstream.

In the depropanizer tower the propane and lighter gases are taken overhead

to become feed to the ethylene and propylene recovery facilities. Separation is

accomplished at a relatively low overhead temperature of -25 "F to minimize

reboiler fouling by olefin polymerization.

Butane and heavier bottoms from the depropanizer flow to the debutanizer

where the C, stream (almost entirely olefins and diolefins) is taken overhead and

sent to butadiene and isobutylene recovery facilities.

Depending upon the refinery needs, the raw C, plus steam cracked naphtha

may be sent to isoprene extraction, treated to remove gum forming diolefins and

sent to the refinery gasoline pool, or else completely hydrogenated and then fed

to an aromatics extraction unit.

The principal function of the ethylene recovery facilities is to recover high

purity ethylene (Figure 2). Ethylene recovery consists basically of a low

temperature, relatively high pressure distillation process to separate ethylene

from other hydrocarbons and hydrogen. In addition, acetylene conversion and

caustic treating steps are employed to reduce contaminants which would not be

adequately removed by the distillation process.

The depropanizer overhead, C, and lighter feed is compressed to about 300

psi and then passed over a fixed bed of acetylene removal catalyst, generally

palladium on alumina. Because of the very large amount of hydrogen contained

in this stream, the operating conditions are critical to selectively hydrogenate the

acetylene without degrading the valuable ethylene to ethane.

The gases are again dried and then further compressed to about 550 psi.

Separation of hydrogen and methane take place in the demethanizer and in its

preflash system. Three successive Golder preflash steps are used in this

separation, with propylene as refrigerant, then ethylene, and finally a selfgenerated

methane refrigerant at -200°F.

A high purity hydrogen and a low purity methane stream result. The 95%

hydrogen may be used directly to hydrogenate steam cracked naphtha or directly

consumed elsewhere in the refinery. The methane stream goes to fuel.

The C, plus bottoms from the demethanizer then go to the deethanizer. A

propylene-propane bottoms product containing 90-92 % propylene is obtained

which may either be sold, used directly as propylene- 90, or further purified. The

ethylene-ethane overhead from the deethanizer is separated in the splitter tower

yielding a 99.8% overhead ethylene product at -25°F. The ethane bottoms at + 18°F may either be sent to fuel gas or used as feed to an ethane craclung

furnace. Overall ethylene recovery in these facilities is about 98 % . The product

is of very high purity with less than 50 parts per million of non-hydrocarbon

contaminants and a methane plus ethane level below 250 ppm.

Propylene Recovery

The propylene-90 bottoms product from the deethanizer may be upgraded to high

polymer grade 99.8 % purity by superfractionation. Propane bottoms are used

elsewhere in the refinery.

Butenes

N o d butenes and isobutylene are separated by a selective reaction-extraction

process which takes advantage of differences in reactivity with dilute sulfuric

acid to form butyl alcohols. Because of differences in olefin structure,

isobutylene reacts much more rapidly than normal butenes with weak acid. In

fact, reaction of normal butenes in acids weaker than 65% is negligible at

commercial conditions. Reaction products are soluble in dilute acid. The unreacted

feed is only slightly soluble.

The acid extract phase is separated, diluted with water, and heated to

regenerate isobutylene. The isobutylene is then caustic and water washed to

remove traces of acid, distillation dried, and rerun. The unreacted C, stream,

containing normal butenes, is also caustic washed before further processing.

C, cuts, after extraction of butadiene, are preferred as feed to isobutylene

extraction units because the isobutylene concentration (about 30-40%) is higher

than in C, streams from catalytic cracking. The basic reaction in isobutylene

extraction is the reversible hydration of isobutylene to tertiary butyl alcohol in the

presence of sulfuric acid.

Polymerization to C, and C;, olefins is the chief side reaction.

Polymerization increases with extraction temperature and with the hold-up time

in the extraction section. It limits the temperature used to obtain high extraction

rates.

The extraction is carried out in a staged countercurrent system for good

recovery of isobutylene. Temperature is maintained by refrigeration, since heat

is evolved in the hydration. Normal (2,'s are rejected as the raffinate from the

lean stage. The stream, typically containing 70 mol% normal butenes, can be

used as feedstock for dehydrogenation to butadiene. The rich acid extract is

flashed to about 2 psig and blown with a small amount of steam to remove

butylenes and butanes physically dissolved in the extract. Isobutylene is then

recovered from the acid extract by direct injection of steam in the regenerator

tower.

Enough steam is used to reduce the acid concentration from 65 % to 45 % .

The heat supplied by the steam is used in: (a) regeneration of isobutylene from

t-butyl alcohol (an endothermic reaction) (b) raising the acid temperature to

250°F and (c) distilling out isobutylene, polymer, and residual tertiary butyl

alcohol. High temperature and low acid strength allow regeneration of the

isobutylene with minimal polymerization. Acid strength in the regenerator tower

is critical. Too low values result in separation of unwanted alcohol while high

concentrations increase polymerization rates.

The regenerator overhead is caustic and water washed, yielding a 95-96%

isobutylene product. The 45% acid taken as bottoms from the regenerator is

concentrated to 57% for steam cracked C, cuts (65% for cat cracked C,'s) and

recycled to the lean stage of the extraction section.

High purity 99+ % isobutylene can be made by rerunning, with a recovery

of over 85% of the isobutylene in the feed.

When hgh purity isobutylene is not required, the acid extract from the rich

stage may be heated for a few minutes to 250-300"F, and then quickly cooled.

Under these conditions the isobutylene dimerizes to form largely 2,4,4, trimethyl

pentene- 1. This is known as the dimer process and may be used to concentrate

1-butenes for dehydrogenation feed, the isobutylene dimer being added to the

motor gasoline pool. Trimers, as well as codimers with normal butenes are also

produced.

 

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ChemOffice Ultra 2008

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