Process Maddah

8/10/2019 Process Maddah

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Process Engineering Procedure

In

Oil, Gas & Petrochemical Projects

By A.R.Maddah

f a r a go st a r a nf a r a go st a r a n


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TERMINOLOGY

Company or Employer/Owner:

Refers to one of the related and/or affiliated companies of the Iranian ministryof petroleum such as National Iranian Oil Company (NIOC), National Iranian

Gas Company (NIGC), National Petrochemical Company (NPC), etc.


2:\Engineering Company


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2:\Engineering Company Accounting

Budget-&-Control

Construction Supervision

Engineering

Estimating

HR-Communication

Information Technology

Management

Procurement

Projects Proposals

Support-Services



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2:\Engineering Company



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2:\Engineering CompanyEngineering

Process

Mechanic

HSE

Civil-Structure-Architecture

Piping

Electrical

Instrument



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3:\Process DepartmentProcess

Process Dept.Manager

Process Senior Engineer

Process Engineer

Process Senior Draftsman

Process Draftsman



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3:\Process Department

Process Departments Activities in the following engineering stages:

1. Proposal Preparation (PP)

2. Feasibility Study (FS)

3. Basic Engineering (BE)

4. Detail Engineering (DE)



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A- Documented ActivitiesA- Documented Activities

B- Non Documented ActivitiesB- Non Documented Activities


Process Departments Activities



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A- Documented Activities (BE & DE)

Design Basis & Criteria

P&ID

BFD,PFD, UFD

Chemical & Utility Summary Table

Control Philosophy

Electrical Load Summary Table

Equipment Process D/S

CV, BDV, PSV Process D/S

ESD Concept / Block Diagram

Flare Load Summary TableBasic Design Package

Preliminary Operating Manual

Equipment List

Trip & Alarm Set Point

Stream Process Condition List




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A- Documented Activities Continued (DE only)

Preparation ofInsulation Schedule

Preparation of

Relief & Drainage Diagram

Preparation ofInterconnecting Diagrams

Preparation of

As Built P&IDs

Technical Bid Evaluation




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B- Non Documented Activities (BE & DE)

Hazop Study

Cooperation in Preparing

of Plot Plan

Project Information Gathering, site visit

Attending Project Meeting with ClientForeign Partner & Licensor

Process Simulation

Line Sizing &

Hydraulic Calculation

Equipment Sizing & Rating

Tie-in List

Information

Completion of LDT




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B- Non Documented Activities Continued (DE only)

Basic Package Endorsement

Cooperation with Inst. Dep.

For DCS / PLC Design

Completion of Equipment

and Instrument D/S

Heat Tracing Calculation

Vendors Bid Evaluation

Checking & Incorporating

Equipment Sizing & RatingModel Review

Cooperation with Piping Dep.

For Tie-in List, Special Items,




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ProjectEngineering

Procurement

Construction

Commissioning

EPCC




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4:\Standards

1.Whatre standards?

2.Why do we apply standards?

-Improvement in qualification of design and operating condition-Increase of safety

-Decrease of design and selection of material

-Selection of proper way for procurement

-Work Uniformity



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4:\Standard\International Standards

ANSI

AmericanNational StandardInstitute

API

American Petroleum Institute ASME

The American Society ofMechanical Engineers

ASTM

The American Society forTesting andMaterial

ISAThe Instrumentation System andAutomation Society

NACE

National Association ofCorrosion Engineers



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NFPA

National Fire Protection Association

DIN

Deutshes Institute furNormung BSI

British Standards Institution

ISO

International Organization forStandardization

TEMATubularExchangerManufactures

AWWA

American WaterWorks Association

4:\Standard\International Standards



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4:\Standard\International Standards\Iranian Standards

IPSIranian Petroleum Standard

NPCS

National Petrochemical Company Standard



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API-RP-520: Sizing, Selection, and Installation Of Pressure-Relieving Devices

in Refinery

API-RP-521: Guide For Pressure-Relieving and Depressuring System

API-STD-2000: Venting Atmospheric and Low-Pressure Storage Tanks

API-RP-14E: Recommend Practice for Design and Installation of Offshore

Production Platform Piping System

API-STD-530: Calculation of Heat-Tube Thickness in Petroleum

API-TP-555: Process Analyzer

4:\Standard\International Standards\API



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IPS-E-PR-750: Engineering Standard For Process Design of Compressor

IPS-E-PR-330: Engineering Standard For Process Design of Compressor Air

System

IPS-E-PR-440: Engineering Standard For Process Design of Piping System

IPS-E-PR-308: Engineering Standard For Process Design for Numbering

System

IPS-E-PR-700: Engineering Standard For Process Design for Process Design

of Crude Oil Electrostatic Desalter

4:\Standard\International Standards\IPS



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NFPA 11: Foam Extinguishing System

NFPA 12: Standard on Carbon Dioxide Extinguishing System

NFPA 13: Standard for the Installation of Sprinkler System

NFPA 15: Standard for Water Spray Fixed System for Fire Protection

NFPA 72E: Automatic Fire Detector

NFPA 20: Standard for the Installation of Centrifugal Fire Pump

4:\Standard\International Standards\NFPA



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4:\Standard\Iranian Standard Codes For Process

Drawing

IPS

IPS-E-PR-170 PFD Symbol Document Numbering

IPS-E-PR-230 P&ID Symbol

NPCS

NPCS-ES-PR-01 PFD/P&ID SYMBOLS



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BFD

Simulation

PFD

UFD

Process Description

Heat & Material Balance

P&ID Process Design Criteria

5:\Process Activities



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Line List

Stream Process Condition

Utility Consumption

Chemical Consumptions Data Summary

Technical bid Evaluation

Instrument Data Sheet

Equipment Data Sheet Process Data For Piping Special Item

5:\Process Activities



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5:\Process Activities\Terminology

Process Units: Units which have direct roles in main process of plant.

Utility Units: Units which dont have direct roles in main process of plant

and are the producers of utility services which are utilized in ProcessUnits.

Operating Condition: It Specifies the Normal Condition (Of Pressure,Temp., Flow, Level,) in Which Equipments, piping and units work.



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Definition:

These diagrams (BFD) are schematic documents representing whole process

of the project generally in different units which are introduced in blocks

containing the title of each unit.

Objective:

The objective of these diagrams is to basically show the sequence of the

process in a simple way.

Process

Engineer

Process Lead

Engineer

5:\Process Activities\BFD(BlockFlowDiagram)



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Block Flow Diagram ofLPG Plant



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BFD

Contract

Technical Proposal

Preliminary Eng. Study




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PROCESS ACTIVITIES

BFD



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Definition:

Process Flow Diagram (PFD) mainly defines:

a) A schematic representation of the sequence of all relevant operations

occurring during a process and includes information considered

desirable for analysis.

b) The process presenting events which occur to the material(s) to convertthe feedstock(s) to the specified products.

5:\Process Activities\PFD(ProcessFlowDiagram)



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Contents of PFD:

Including:

PFD shall comprise but not limited to the following items:

1. All process lines, utilities and operating conditions including item numberessential for material balance and heat and material balance.

2. Type and utility flow lines which are used continuously within the battery

limits.

3. Equipment diagrams to be arranged according to process flow, designation,

and equipment number.4. Simplified control instrumentation pertaining to control valves and the likes

to be involved in process flows

5:\Process Activities\PFD



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5. Major process analyzers

6. Operating conditions around major equipment.

7. Heat duty for all heat transfer equipment.

8. Changing process conditions along individual process flow lines, such asflow rates, operating pressure & temperature, etc.

9. Material balance table.




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Excluding:

The following items are generally not be shown on PFD, except in specialcases:

1. Minor process lines which are not usually used in normal operation andminor equipment, such as block valves, safety/relief valves, etc.

2. Elevation of equipment.

3. All spare equipment.

4. Heat transfer equipment, pumps, compressor, etc., to be operated in parallelshall be shown as one unit.

5. Piping information such as size, orifice plates, strainers, and classificationinto hot or cold insulated of jacket piping.




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6. Pressure condition which must be determined by hydraulic calculation,such as discharge pressure of pump and compressor.

7. Instrumentation not related to automatic control.

8. Drivers of rotating machinery except where they are important for controlline of process condition.

9. Any dimensional information on equipment, such as internal diameter,height, length, and volume. Internals of equipment shall be shown only ifrequired for a clear understanding of the working of the equipment.




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GENERAL DRAFTING INSTRUCTIONS

1. ScalePFDs should not be drafted to scale. However, their size should be

compatible with that of equipment drawings.

2. Flow Direction

As a rule, PFDs should be drawn from the left to the right in accordancewith process flows.

5:\Process Activities\PFD\Drafting



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c)All electrical, computer and instrument

signals

Thickness = 0.3 m

b) Secondary process lines and utility line

Thickness = 0.5 mm

a) Main process lines

Thickness = 0.8 mm

4. Kind Of Lines

As a rule, Process lines, utility lines, and loop lines for instrument should be

drawn according to IPS-E-PR-230 as follows:




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5. Line Crossover

Where two lines cross each other, the horizontal line should be drawn as a

continuous line in all cases. This shall not apply to loop lines for instruments.

c) Where one main line crosses one loop linefor an instrument

b) Where one main line crosses onesecondary process and utility lines

a) Where two main process lines cross




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6. Denotation of Lines at Battery Limit Tie-In Points

a) Process lines

From Item No. and/ To Item No. and/

or Dwg. No. or Dwg. No.

b) Utility lines COOLING WATER

Names of fluids should be given in parentheses above the utility lines.

Name of these fluids should be as abbreviation according to IPS-E-PR-308




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7. Direction of Flow

The direction of flow should be indicated by arrows. In principle all flow

lines should be denoted by arrows located at the inlet of equipment, and at

the corners of the lines. Where a process line is long, however, the process

flow may be denoted by arrows located at intermediate points.

The number of arrows used to denote one process flow line is not

restricted. However, care should be taken not to clutter the drawing with

excessive arrows.




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8. Division of PFD

Where a PFD must be divided into two or more sheets, it should be

divided at portions where division is easiest from the process standpoint

and each divided section should be drawn on a separate sheet.

9. Other Trains

Where there are two or more identical trains of process flows, one

representative train may be given in the PFD and the others omitted.

However, notations pointing out such omissions must be clearly indicated

in the titles of all relevant PFDs to avoid confusion.




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10. Title

The title should be given in the title block at the lower right-hand corner of

the PFD.

11. Legend

The legend may be given in separate schematic drawing to which reference

shall be made if necessary.

12. SizeThe size of PFD should normally be A1 (594 mm 841 mm).




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Minimum Information Requirements For Equipments

1. Designated streams

a) Stream numbers should be serially denoted by Decimal numbers.b) Fluid name.

c) Total flow rate.

d) Density and/or molecular mass (weight) if required.

e) Operating pressure and temperature if required.




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2. Heat exchangers

a) Identification number and service name.

b) Operating heat duty.

c) Inlet and outlet temperatures on both shell and tube sides.

3. Furnaces


b) Operating absorbed heat duty.

c) Inlet and outlet operating temperatures on tube side.



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4. Reactors


b) Inlet and outlet operation temperature.

c) Inlet and/or outlet pressure.

5. Columns


b) Tray numbers, operating temperature and pressure for top and bottom trays

and also for special trays such as feed and draw-off, etc.

c) Trays shall be numbered from bottom to top.




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6. Drums


b) Operating temperature.

c) Operating pressure.

7. Pumps


b) Normal operating capacity and differential pressure.




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8. Compressors and blowers


b) Normal operating capacity and differential pressure.

9. Tanks


b) Operating temperature.

c) Operating pressure.



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PFD Modification

1. First Issue (FI):

Release for proposal (Conclusion of estimate, study)

-Main equipment (Tagged)

-Main Process Lines

-Battery Limit

-Main control concept (control & switch)

-Package unit Limits

5:\Process Activities\PFD Modification



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2. Issued For Approval (IFA):

Release for Basic Engineering (Conclusion of fixed price bid)

In addition to contents 1.-Important valve ( isolation, manual control)

-Essential process shutdown circuits

-Important start up lines

-Definition of heat exchanger type




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3. Issued For Design (IFD):

Release for Basic Engineering Development (Conclusion of verification

Phase and Basic Eng.)

-Content as 1. & 2. however adjusted to the contract conditions



4. Approved For Design (AFD):

Release for Detail Engineering (End of Basic Eng.)

-Crosscheck with P&ID, release detail engineering


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5. Issued For Construction (IFC):

Release for Detail Engineering Development

-Crosscheck with P&ID, release for purchase of bulk material



6. Approved For Construction (AFC):

Release for Construction phase (End of Detail Eng)

-Final issue of PFD in Detail phase

7. As Built (ASB):

End of construction

-Includes all of the changes in commissioning and construction phase


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PROCESS ACTIVITIES

BFD

PFD



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Heat and Material Balance Table:

The basis for preparation of this Table is process description accompanied by

the specified contract requirements such as separation percent or outlet

required pressure or any other specification of Feed and Products. This table is

generally prepared by process simulation soft wares like HYSYS, PROII and

etc.

5:\Process Activities\PFD\H&M Balance



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Contents :

Stream information: Stream No., name of stream, flow rate, composition.

Operating conditions: Operating temperature and pressure.

Basic physical properties: Molecular mass (weight), API gravity, Relative

Mass Density (Specific Gravity) or (Sp.Gr.), etc.

Data concerning hydraulic calculation: Density, viscosity, etc. if required



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PROCESS ACTIVITIES

H&M BALANCE

BFD

PFD

5:\Process Activities\H&M Balance


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Definition:

These diagrams (UFD) are generally similar to Process Flow Diagrams but theyare related to the Utility parts (streams) of the process which give services to themain process lines for different purposes.

These diagrams are normally not simulated by softwares to reach the above-mentioned specifications of streams (To prepare Heat and Material Balance).

The Symbol Diagram of UFDs are the same as PFDs.

5:\Process Activities\UFD

(UtilityFlowDiagram)



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1.ModificationModification and revision is defined separately for every sheet of a UFD

FI , IFA , IFD , AFD , IFC , AFC , ABS

2.Revision

A new revision indicates the change of a document. The revision is defined by

number & alphabets, which by subsequent revision shall be consecutively raised

from a starting point.

Numbers Rev.1,2,

Alphabets Rev.A,B,

5:\Process Activities\UFD Modification



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PROCESS ACTIVITIES

H&M BALANCE

BFD

PFD

UFD

5:\Process Activities\UFD


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Output ofSimulation by

Process

Engineer

It is drawn

byDraftsman

Checked byProcess

Senior

Engineer

Approved by

Process Dep.

Manager

Process Lead Engineer

5:\Process Activities\PFD & UFD



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PFD, UFD, H&M Balance

Contract (Symbol & Legend)

Codes/ Std./ Eng. Practice

Licensor Comments

Final Doc. Of Equipment Vendor

Technical Proposal

Simulation ResultsBasic Design


Preliminary Eng. Study


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Purposes:

Decreasing of calculation time

Heat & Material Balance Table

Prediction of optimum arrangement of equipment for PFD

production

Pinch study

Designing of equipment

5:\Process Activities\Simulation (ND)



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Applications Cases:

Proposal Preparation (PP)

Feasibility Study (FS)

Basic Engineering (BE)

Detail Engineering (DE)




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Terminology:

Simulation

Design

Rating




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Simulations Software:o PRO /II

o HYSYS

o HEXTRAN

o HX-NET

o HTRI

o Visual Flow

o INPLANT

o PIPE-PHASEo Pipe Sys

o PROMAX




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PROCESS ACTIVITIES

H&M BALANCE

BFD

PFD

UFD

SIMULATION

5:\Process Activities\Simulation


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5:\Process Activities\Process Description


Objective:

Process Description , describes technical information, that determines

operating conditions and explains major principles of plant process

Process Description is prepared at two stages :

1.Proposal Preparation (PP)

2.Basic Engineering (BE)


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1.Proposal Preparation (PP)

-After the study of bid documents from client, a short process descriptionwill prepared.

-This process description should be based on BFD

-In this stage , process description covers the minimum requirement toexplain major principles, operating condition and purpose of each defined

block in BFD


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2.Basic Engineering (BE)

-Preliminary process description (from client) will be completed during thisstage

-In order to prepare detailed process description , PFD,UFD and H&MBalance should be used to extract necessary data such as temperature,

pressure, operating condition and main process loop control.

-In addition , process description includes duty of each equipment, majorprinciples of plant or sub unit , feed and product condition to/from each unit.


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Process Description

Contract

Licensor Basic Design

Technical ProposalBFD , PFD ,UFD


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PROCESS ACTIVITIES

H&M BALANCE

BFD

PFD

UFD

SIMULATION

PROCESS DESCRIPTION



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5:\Process Activities\Basic Design


Basic Design (Design Basis)

This document shows the basic parameters that process engineers apply in

designing of plant.


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Basic Design (Design Basis) Consists of below items,

1. Feed and Product Specification

- General Specification

- Plant Capacity

- Feed

- Product


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2. Utility Specification

- HP,MP,LP Steam

- Plant & Instrument Air

- Nitrogen

- Water (Potable,Plant,DEMIN,)

- Fuel (Oil,Gas)


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4. Emissions and Waste

- List of Expected Gaseous Emissions

- List of Expected Liquid Effluents

- List of Expected Solid Wastes


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6. Environmental Data

- Site Data

Location, Elevation above Sea Level, Earthquake Spec.

and

- Climatic Data

Air Temperature, Air Humidity, Barometric Pressre,

Wind, Rain and Snow Fall


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Process Design Basic

Contract Licensor Basic Design

Technical Proposal


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PROCESS ACTIVITIES

H&M BALANCE

BFD

PFD

UFD

SIMULATION

PROCESS DESCRIPTION

DESIGN BASIS

5:\Process Activities\Design Basis


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Definition:

The Piping and Instrument Diagram (P&ID), based on the Process Flow

Diagram (PFD), represents the technical realization of a process by means ofgraphical symbols for equipment and piping together with graphical symbols

for process measurement and control functions.

5:\ Process Activities \P&ID

(Piping & Instrument Diagram)



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Terminology:

Design Conditions: Design Pressure and Temperature are used to determine theminimum permissible thickness or Physical characteristics of each Equipment

or Piping item.

Low Level: A condition (Press,Temp, Flow, Liq. Level) in a process componentless than the minimum operating condition.

High Level: A condition (Press,Temp, Flow, Liq. Level) in a processcomponent in excess of the maximum operating condition.

5:\ Process Activities \P&ID\TerminologyTerminology



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Control Valve: These are automatic valves used for controlling parameters like

Press., Temp., Flow rate, Their power medium is normally Instrument Air

(pneumatic actuators)

Failure: Improper performance of a device or equipment item that prevents

completion of its design function.

Fail Open / Closed (Control Valve): The safe position of a valve which will shift

to upon loss of the power medium.

Normal Position (Valve): The position of a valve in Normal Condition of the

process (N.O. , N.C.)




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Plant Shutdown: The shutting in of all process stations of a Plant Production

process and all support equipment for the process.

Process Shutdown: The isolation of a given process station from the process

by closing appropriate SDVs to shut-in flow to the process station or divert

flow to another process station.

Shutdown Valve (SDV): An automatically operated Normally Closed valve

used for isolating a process station.

Emergency Shutdown System (ESD): A system of stations which when

activated initiate plant shutdown.



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Flare: A means of safety disposing of waste gases through the use of

combustion. With a flare the combustion is carried out at the top of a pipe or

stack where a the burner and igniter are located.

Relief System: A system containing mechanical overpressure protection

devices (press. safety valves) on the equipment, relieving in to a collection /

disposal system.




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Pressure Safety Valve (PSV): A pressure relief device designed to open andrelieve excess pressure and to reclose and prevent the further flow of fluidafter normal conditions have been restored.

Depressurization: When metal exposed to fire on one side with vapor on theother side, the metal temp. may reach a level at which metal rupture due tostress may occur, even though the press. does not exceed the allowableoverpressure. An emergency depressurization (blow down) system is providedto avoid such an occurrence.




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Blow down Valve :

An automatically operated normally

open valve used to vent the pressure

from a process station on shutdown.

5:\Process Activities \P&ID\TerminologyTerminology



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Drain System:

This is the configuration which drains liquids

from vessels or piping systems after

depressurization (via valves) in to a system

of vessel and piping.




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Vent: A pipe or hatch on a vessel that opens to the atmosphere.

Battery Limit: Generally is used for showing the exact margin of a specific unit.

(Process or Utility Units)




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Contents:

Piping System

Equipments

Control Items

Automatic and Manual Valves

All Item Numbers

All Item Required Information

Vent and Drain Systems

Notes

Packages

Tie-In Points

5:\Process Activities \P&ID\Contents



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P&ID Symbols:P&ID Symbols:

P&ID Equipment SymbolsP&ID Equipment Symbols

P&ID General SymbolsP&ID General Symbols

P&ID Instrument Symbols (Typical HookP&ID Instrument Symbols (Typical Hook--Up)Up)

P&ID Instrument Symbols (Valve Symbol)P&ID Instrument Symbols (Valve Symbol)

5:\Process Activities \P&ID\Symbols



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Gate valve (basic symbol)

Globe valve

Check valve (general)

Gate valve behind off

Angle valveBall valve

Four way valve

Gate valve with body bleed

Butterfly valve

Hydraulic control

Metering cock

Needle valve

Plug valveS=solenoid valve

R= Manual reset when indicated

Diaphragm valve

DESCRIPTIONSYMBOL




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Main process line (arrow indicates Direction of flow )

Heat traced pipe line

Underground pipeline

Existing line

Future line

Vendor package

Jackated or double containment pipeline

Line crossing (connected )

DescriptionSymbol




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Drafting

1. General rules

Drafting shall be in accordance with the requirements outlined in this Standard.The drafting must be of sufficiently high quality to maintain legibility when

the drawing is reduced to an A3 size sheet.

2. Drawings sheet sizes

Diagrams shall be shown on A0 size (841 mm 1189 mm) tracing paper. A1

size (591 mm 841 mm) may be used for simple P&IDs as per Companys

approval.

5:\Process Activities \P&ID\Drafting



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3. Drawing title block

The following requirements shall be shown on the title block of each drawing (Next

Page):

- revision table;

- main Companys name (e.g., National Iranian Oil Company);

- name of Company Relevant Organization, (if any), (e.g., Refineries Engineering and

Construction);

- name of refinery or plant (in English and Persian words);

- Contractors name;

- drawing title;

- Companys project No.;

- Contractors job No. (optional);

- Contractors drawing No. (optional);

- Companys drawing No.




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Title block sizes and drawing dimensions shall be as follows

180 190

130 175

100 155

75 120

A0 = 841 1189

A1 = 594 841

A2 = 420 594

A3 = 297 420

TITLE BLOCK SIZE (INCLUDING REVISION

TABLE)WIDTH (mm) LENGTH (mm)

DRAWING DIMENSIONS

(mm mm)




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4. Line widths

To obtain a clear representation, different line widths shall be used. Main flow

lines or main piping shall be highlighted.

The following line widths shall be applied:

0.8 mm for main process lines;

0.5 mm for other process lines; utility lines, and underground lines;

0.5 mm for graphical symbols for equipment and machinery, except valves

and fittings and piping accessories; 0.5 mm for rectangular boxes for illustrating Unit operations, process

equipment, etc.;




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0.5 mm for subsidiary flow lines or subsidiary product lines and

for energy carrier lines and auxiliary system lines;

0.4 mm for class changes designation;

0.3 mm for graphical symbols for valves and fittings and pipingaccessories and for symbols for process measurement and

control functions, control and data transmission lines;

0.3 mm for all electrical, computer and instrument signals;

0.3 mm for reference lines;

Line widths of less than 0.3 mm shall not be used.




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5. Line spacing

The space between parallel lines shall not be less than twice the width of the

heaviest of these lines. A spacing of 10 mm and more is desirable between

flow lines.




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6. Direction of flow

In general, the main direction of flow proceeds from left to right and from

top to bottom. Inlet and outlet arrows are used for indicating the inlet and

outlet of flows into or out of the diagram.

Arrows are incorporated in the line for indicating the direction of the flows.If necessary for proper understanding, arrows may be used at the inlets to

equipment and machinery (except for pumps) and upstream of pipe

branches. If a diagram consists of several sheets, the incoming and outgoing

flow lines or piping on a sheet may be drawn in such a manner that the lines

continue at the same level when the individual sheets are horizontally

aligned.




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7. Connections

Connections between flow lines or pipelines shall be drawn as shown in

Figs. 1 and 2below:

Figs. 3 and 4 show two flow lines or pipelines, which are not connected:

Fig1 Fig2

Fig3 Fig4




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8. Equipment Location Index

Piping & Instrument Diagrams shall be divided intoequivalent intervals (each in 50 mm) eitherin length or width.The intervals shall be designated with numbers from 1 to 23 in

length and alphabets from "A" to "P" in width. Equipmentlocation on each diagram shall be addressed by the relevantcoordinates where required. In upper right-hand area of theflow diagram under title of "Item Index" all main equipmentshall be listed by equipment number, alphabetically andnumerically and equipment location coordinates. In a separate

sheet apart from P&IDs, an "Item Index" shall be prepared tosummarize all equipment of the Unit/Plant with referenceP&IDs and equipment location.




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9. MINIMUM INFORMATION TO BE SHOWN ON P&ID DIAGRAMS

General

Each P&ID shall present all information as required herein below during

implementation of a project in detailed design phase. Extent of information

shown on each P&ID in the basic design stage shall be agreed by Company inadvance.

Vendor supplied packages with an outline of the main components shall be

shown in a dashed/dotted box. Letter "PK" referring to package shall be

indicated adjacent to each equipment and instrument of the package.




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Equipment, instruments or piping which are traced or jacketed, shall be shown.

The identification number and service presentation shall be shown for eachpiece of equipment. This information shall be indicated in or adjacent to

towers, drums, heaters, tanks and heat exchangers, etc.




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A .Fixed Equipments, TanksThe following requirements shall be shown:

Drawing

a) all nozzles, manways, instrument connections, drains, vents, vortex breakers, and

safety/relief valve connections;b) all internals such as steam coils, air spargers, tank heaters and etc.

Equipment descriptiona) equipment item number (this number also appears adjacent to the tank);

b) service;

c) inside diameter and height;

d) nominal capacity, in (m);e) design pressure and temperature;f) indication of insulation.




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A .Fixed Equipments Vessels, Towers, DrumsThe following requirements shall be shown:

Drawing

a) changes of shell diameter (if any); b) top and bottom trays, and those trays which are necessary to locate feed, reflux and

product lines;

c) all draw-off trays with tray number;

d) all nozzles, manholes, instrument connections, drains, vents, pump-out and steam-out, vortex breakers, and safety/relief valve connections,sample connection

e) skirt or legs, top and bottom tangent lines;

f) elevations above base line to bottom tangent line of column or to bottom of horizontaldrum;




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Drawing (For Vessels, Towers, Drums) :

g) the position of high high liquid level (HHLL), high liquid level (HLL), normal liquid

level (NLL), low liquid level (LLL) and low low liquid level (LLLL);

h) all flanged connections; [all connections whose purpose is not readily evident shallindicate the purpose (e.g., spare inlet, catalyst draw-off, etc.).];

i) catalyst beds, packings, demisters, chimney trays, distributors, grids, rotating discs,mixers, cyclones, tangential inlet and all other internals;

j) water drop-out boots;

k) maintenance blinds for the vessel nozzles.




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Important Notes (For Vessels, Towers, Drums) :

a) All nozzles and connections indicated on the equipment data sheet shall be shownin their correct positions.

b) All indications shall be such that the consistency in the dimensions is considered,although not necessarily to scale.

c) Numbering of the trays shall be from bottom to top.

d) Height of the vessel bottom tangent line shall be indicated.

Self standing : Skirt heightElevated vessel: Minimum required height shall be shown as "min. ....".

e) A valved drain for all columns and vessels shall be indicated.




119/263


120/263

Equipment Description (For Vessels, Towers, Drums) :

The following requirements shall be described under equipment description:

a) vessel item number (this number will also appear adjacent to the vessel);

b) service; c) size [inside diameter(s) and tangent to tangent length];

d) design pressure (internal/external) and design temperature;

e) indication of insulation;

f) line number of vessel trim (this applies to LG & LC connections, vents, sample

connections, etc.);




121/263

A .Fixed EquipmentsFired Heaters, Boilers, Incinerators

The following requirements shall be shown:

Drawing

a) all nozzles, instrument connections, drains, vents and damper(s);

b) ducting arrangement including damper actuators where required;

c) waste heat recovery system (if present), such as economizer, air preheater,

forced draft fan, induced draft fan,etc.;

d) decoking connections;




122/263

Drawing

e) detail of one complete set of burners for each cell and total burner number requiredfor each type of burner;

f) tube coils schematically in correct relative positions and all skinpoint thermocouples;

h) logic diagram of shut down system (heat off sequence);

i) number of passes and control arrangement;

j) blow-down and steam-out connections;

k) testing facilities;

l) convection section (where applicable).




123/263

A .Fixed Equipments,Heat Exchangers, Coolers, ReboilersThe following requirements shall be shown:

a) all nozzles, instrument connections, drains and vents, chemical cleaning

connections and safety/relief valves as indicated on the equipment data sheet;

b) spectacle blinds for the isolation;

c) elevations required for process reason (e.g., reboilers, condensers, etc.);

d) the position of high liquid level (HLL), normal liquid level (NLL) and lowliquid level (LLL) for kettle type reboilers;

f) direction of flow in each side of exchanger.




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Important notes (For Heat Exchangers, Coolers, Reboilers)

Due considerations should be made for proper indication in the following requirements:

a) Generally, direction of flow shall be downflow for cooled media and upflow forheated media.

b) Isolation valves shall be provided on inlet and outlet lines where maintenance canbe performed on the exchanger with the Unit operating. Provision of by-passing isrequired for this case.

c) Shell and channel piping shall be provided with a valved vent connection and a drainconnection unless venting and draining can be done via other equipment.




125/263

Important notes (For Heat Exchangers, Coolers, Reboilers)

e) An inlet and outlet, temperature indicator shall be provided on each exchanger (oneither shell or tube side) so that to facilitate checking of heat balance aroundexchanger.

Type of temperature indicator shall be as follows:

- A board mounted temperature indicator (TI) shall be provided at the inlet and outletof all shell and tube process/process exchanger.

- For water coolers, the water side outlet shall be provided with a local TI only. Theshell side in and out shall be provided with board mounted TIs.

- Thermowells (TWs) shall be provided between each shell side and tube side of thesame services when the exchangers are in series.




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Equipment description (For Heat Exchangers, Coolers, Reboilers)

a) equipment item number (this number also appears adjacent to the equipment);

b) service;

c) duty (kJ/s);

d) shell side design pressure and temperature;

e) tube side design pressure and temperature;

f) indication of insulation.




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B. Rotary MachineriesPumps


Drawing

a) all nozzles including instrument connections;

b) pump suction valve and strainer, and discharge valve and check valve. Provision of

wafer type check valve should be avoided unless otherwise specified;

c) pump drains and vents piping.

d) the type of pump;

e) pump auxiliary system connections such as, cooling water, seal oil and lube oil, steam,etc.;

h) pressure gage located on the discharge of each pump; the gage shall be installed

between the pump discharge nozzle and the check valve;




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Equipment description (For pumps)

a) pump item number (this number also appears below the pump);

b) service;

c) capacity, (m/h, dm/h for injection pumps);

d) differential pressure, (kPa);

e) relative density (specific gravity) of pumped fluid at pumping temperature;

f) indication of insulation and tracing;

g) miscellaneous auxiliary piping (CW, seal oil, etc.).




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B. Rotary Machineries, Air Fin Coolers


Drawing a) all nozzles and instrument connections;

b) blinds for the isolation;

c) any automatic control (fan pitch control or louver control) and any alarm (vibrationalarm, etc.);

d) configuration of inlet and outlet headers and the branches. Only one bundle andfan shall be shown; total number of fans and bundles shall be indicated. When

multiple bundles are required, headers arrangement as separate detailed sketchshall be indicated;




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e) steam coil and condensate recovery system (if required);

f) isolation valves (if required); isolation valves shall be provided in corrosive andfouling services where individual bundles can be repaired and maintained with theUnit operating;.

g) valved vent and valved drain connection for each header, vent header should beconnected to closed system for volatile services;

h) a board mounted TI at inlet and outlet, (the TI will monitor the process side of eachair fin service). If multiple bundles to be used for fouled services, provide TWs on theoutlet of each bundle.




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Equipment description (For Air Fin Cooler)

a) equipment item number (this number will also appear adjacent to the equipment);

b) service;

c) duty (kJ/s);

d) tube side design pressure (internal and external) and design temperature.




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B. Rotary Machineries Compressors and BlowersDrawing

a) type of compressor or blower;

b) start-up facilities (i.e., inert gas purge system);

c) safety/relief valves;

d) suction and discharge valves;

e) suction strainer (filter) and discharge check valve;

f) suction and discharge pulsation dampener where required;

g) valved vents and casing drains;




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Drawing (For Compressor and Blowers)

h) winterization (steam or electrical tracing on suction piping) where required;

i) lube and seal oil / sealing system and cooling water systems detail arrangement;

j) interstage coolers where required;

k) surge protection (where required);

l) inlet and outlet nozzles;

m)all instrument connections.




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Description for Compressors and Blowers

a) equipment item number and stage (this number also appears below thecompressor);

b) service:

c) capacity, (Nm/h);

d) suction pressure, and temperature, [kPa (g)], (C);

e) discharge pressure, and temperature, [kPa (g)], (C);

f) miscellaneous auxiliary piping (CW, lube, oil, seal oil / sealing system, etc.);

g) gas horse power, (kW).




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B. Rotary Machineries Steam and Gas Turbine Drivers

Drawing

a) all nozzles and connections;

b) detail of all auxiliary systems for steam turbine drivers such as steam supply,condensate return, surface condenser and etc.;

c) detail of lube oil, cooling water, etc.;

d) all instrumentations such as PI, TI, etc.;

e) safety/relief valves; relief valves shall be located between the discharge nozzle andthe outlet isolation valve;

h) vent line to atmosphere at turbine exhaust; the vent is required for the start-up/testoperation of the turbine.




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1.ModificationModification and revision is defined separately for every sheet of a P&ID

FI, IFD , AFD , IFC , AFC , ABS

2.RevisionA new revision indicates the change of a document. The revision is defined by

number & alphabets, which by subsequent revision shall be consecutively raised

from a starting point.

Numbers Rev.1,2,

Alphabets Rev.A,B,

5:\Process Activities\P&ID Modification



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GeneralAs the P&I Diagram contains a large amount of plant design information, its revision

will have a great effect on the subsequent engineering works.

Accordingly for the purpose of minimizing the revisions and avoiding unnecessary

works, the steps for preparing the P&I Diagrams shall be established. The followingsteps should be realized in preparing the P&I Diagrams. Upon the information which

can be prepared as engineering work proceeds, steps 2, 3 and 4 may be combinedor extended to more steps as required.




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PFD Modification

1.First Issue (FI):

Through step 1, the basic design philosophy concerning those basic items for the

preparation of P&IDs such as mode of indication, applicable standards, numberingsystem, valve arrangement and those other basic items on which agreements

shall be made by the Company prior to the preparation of the P&ID should be

clarified.




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The basic items which should be taken into consideration in step 1 are listed hereinbelow but should not be limited to the following items:

a) Vellum and drafting

- size and vellum of drawing;

- title;- drafting;

- arrangement;- equipment description;

- interconnection.

b) Numbering System

- drawing No.;

- equipment No.;

- instrument tag No.;

- line No.




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c) Symbol

- equipment;

- piping components;- instrument symbol;

- process stream symbol;

- utility symbol.

d) Valve arrangement around equipment

- valve arrangement for drain, vent and purge;

- valve arrangement for steam-out;- sizes of the nozzles for installing the instruments;

- valve arrangement around the heater and exchanger;- valve arrangement around the pump and compressor;

- valve arrangement around the steam turbine.




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e) Piping

- piping classification standards;

- valve arrangement at the battery limit;- valve arrangement for drain, vent, purge and steam-out on piping;

- valve arrangement around the steam trap;

- valve arrangement around the sample point/sample connections;- blow-down;

- valve type selection criteria/standards;- strainer type selection standards;

- pipe line sizing




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f) Instrumentation

- valve arrangement around the control valve;

- valve arrangement around the safety/relief valve;

- valve arrangement around other instruments;

- instrument type selection standards;- software linkage and DCS presentation.

g) Miscellaneous

- winterizing and heat conservation;

- recovery of steam condensate;

- disposal of drains and waste water effluent




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\ A i i i


144/263

Results of hazard analysis and operability (HAZOP) study (if any) note :contractor shall

perform the HAZOP study (if required by the owner) using PFD, P&ID and plot plantogether with equipment data sheets and related safety equipment checklist.

Contractor shall provide information about the reported accidents in similar processunits in the world during HAZOP meetings.

The Contractor should prepare both the draft of the basic items for preparation of the P&IDiagrams and all necessary operation and safety features as mentioned above to

Companys review and approval before issuance of official revision of P&I Diagram forengineering start.



5 \P A i i i


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2. Issued For Design (IFD):

Release for Basic Engineering

Step 2,

The following information as minimum requirement shall be reviewed and completed at this

stage:

1) Equipment

- number of equipment;

- type of equipment;- equipment No. and name



5 \P A i i i


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2) Piping

- size of main piping;

- winterizing/heat conservation requirement;- valve type;

- provision of drain and vent;

- provision of purge, steam-out, chemical injection and water injection connections andvalving;

- line No.;- utility services connected to each equipment, piping and packaged Unites.

3) Instrumentation

- type of instrument and location of the primary element;

- location and discharge destination of the safety/relief valve;- location, type and valve functioning (failure action) of the control valve;

- measurement and control method;- instrument tag No.




147/263

5 \P A ti iti \ difi i


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3. Approved For Design (AFD):

Release for End of Basic Engineering

Step 3,

The purpose of issuing the P&I Diagrams , is the Companys approval on the basis of

detailed design for piping layout.The minimum information which should be added on the P&ID at this stage shall be as

follows:

1) Equipment

- elevation of equipment;

- size of equipment;

- internal of equipment.



5 \P A ti iti \P&ID M difi i


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2) Piping

- line class;

- miscellaneous piping size (except around the safety/relief valve and control valve);- thermal and cold insulation;

- correct orientation of piping around equipment.

3) Instrumentation

- size of main control valves;

- additions and revisions on the basis of detailed design.

4) Vendors packaged uni ts

- The details of some available information concerning the Vendors shall be indicated.




150/263

5 \P A ti iti \P&ID M difi i


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2) Instrumentation

- sizes of the safety/relief valves;

- sizes of the control valves;- details concerning level transmitters and level gages;

- logic diagram for heaters, incinerators, compressors, and all other main equipment(where applicable).

- Consequences of details of cause and effect tables.

3) Vendors information

- The necessary information concerning the Vendors, equipment shall be indicated.

5 \P A ti iti \P&ID M difi ti


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5. Approved For Construction (AFC):

End of Detail EngineeringStep 5,

The P&I Diagram shall be issued for construction after completion of the followingactivities:

- piping material table;- piping class and all relevant job specifications;

- all job specifications and standard drawings in relation to the preparation of P&I

Diagrams;- logic diagram of the main equipment;

- hydraulic of system;- size of all piping, valves and instrumentation components;

- vendors information.



5 \P A ti iti \P&ID M difi ti


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6. As Built (ASB):

End of construction

Step 6,

- The P&I Diagram as-built shall be prepared in accordance with the results of linechecking and the final edition of the field sketches.

- The specified piping and instrument take-off and branch points shall be observed

as strictly as possible and shall be implemented on the P&I Diagram.


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5:\Process Activities\P&ID


155/263


Piping & Inst. Diagram (P&ID)

Contract

Codes/ Std./ Eng. Practice

Licensor Comments

Plot Plan

Technical Proposal

Process Calculation

Inst./Equipment

Piping Material Specification


Licensor Basic Design

PFD


5:\Process A ti iti \P&ID


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PROCESS ACTIVITIES

H&M BALANCE

BFD

PFD

UFD

SIMULATION

PROCESS DESCRIPTION

DESIGN BASIS

P&ID


5:\Process Activities\Design Criteria


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SCOPE

PURPOSE

MECHANICAL DESIGN CONDITIONS

EQUIPMENT DESIGN CRITERIA

PIPING




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1.0 SCOPE

These design criteria cover the general requirements for the process design ofoil, gas

and petrochemical plants.

Cases or applications not specifically covered by these criteria shall be handled on an

individual basis. All applicable codes and standards shall apply to these cases.




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2.0 PURPOSE

Basic Engineering

The purpose of this document in BASIC Engineering is to: Standardize and group preferred options and alternatives.

Establish and correlate a source of basic information of typically multidiscipline interestsfor easy access and common reference.

Serve as minimum basic sizing criteria.

Detailed Engineering

The purpose of this document in DETAILED Engineering is to:

Clarify the options selected for equipment design during BASIC Engineering Define the minimum requirements for completion of DETAILED

Engineering




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3.0 MECHANICAL DESIGN

CONDITIONS

Design Pressure

Design Temperatures




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3.1 Design Pressure

3.1.1 Pressure Vessel

The design pressure for pressure vessel (equipment fabricated according to ASME

VIII) shall generally be as follows:

MOP + 7%>69

MOP + 10%18 to 69

MOP + 1.8 bar1.7 to 18

3.5 barg0 to 1.7

Full Vacuum + 3.5 barg (if external pressure is

Atmosphere)

Under Vacuum

Minimum Design Pressure (barg)Maximum Operating

Pressure MOP(barg)



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3.1.2 Compressors

Suction Side Design Pressure

The design pressure of the equipment and piping at the compressor suction should be

calculated based on table presented for pressure vessel. The MOP is the higherpressure of the following:

MOP = (Suction pressure + Discharge pressure)/2




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Discharge Side Design Pressure

Centrifugal Compressor

At the discharge of a centrifugal compressor:

MOP + 1 bar, for MOP 10 barg,

MOP + 10%, for MOP > 10 barg.

Reciprocating compressor

At the discharge of a reciprocating compressor:MOP + 2 bar, for MOP 20 barg

MOP + 10%, for MOP> 20 barg

*PSVs are required.




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3.1.3 Pumps

Centrifugal Pumps

Generally the pump circuit is designed for the shut-off pressure of the pump and whereno PSVs are provided for protection of the circuit. The shut-off pressure, or design

pressure, is the highest of the following:

Shutoff pressure = Normal suction pressure (NSP) + 1.25 of differential pressure atmaximum specified fluid density.

Or

Shutoff pressure = Maximum suction pressure (MSP) + differential pressure atmaximum specified fluid density.




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Normal and Maximum suction pressure (MSP) is calculated as follows:

NSP = upstream equipment Operating pressure + NLL of upstream equipment

MSP = upstream equipment PSV set pressure (design pressure) + HHLL of upstreamequipment

Notes:

In the case of two pumps in series, the design pressure shall be determined using thedesign pressure of the first pump as the maximum suction pressure of the secondpump.




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b) Positive Displacement Pumps

At discharge of positive displacement pumps:

MOP + 1 bar for MOP 10 barg

MOP + 10% for MOP > 10 barg

PSVs are required.




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3.1.4 Heat Exchangers

The same method used for pressure vessel should be applied for heat exchangers.

If a control valve or block valve is installed downstream of a heat exchanger:

The design pressure of the exchanger = the upstream equipment design pressure.

If a control valve or block valve is installed upstream of an exchanger (No valve ondownstream of exchanger):

The design pressure of the exchanger = design pressure of the downstreamequipment at the entry point + 1.25 times the maximum pressure drop in the systembetween the inlet of the exchanger and the inlet of the downstream equipment + statichead (if any).




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An exchanger on the discharge side of a gas driven compressor shall have a designpressure equal to or greater than the setting of the PSV for the system.

Exchanger operating under a vacuum shall be designed for full vacuum.




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3.1.5 Storage Tanks

Atmospheric and near atmospheric tanks

- If the specific gravity of stored liquid is lower than 1.0, the design pressure ofatmospheric storage tanks with open vent or without gas blanketing shall be designed

full of water + 50 mm water column.

- If the specific gravity of stored liquid is higher than 1.0, the design pressure ofAtmospheric storage tanks (open vent or without gas blanketing) shall be designed fullofproduct + 50 mm product column.

For atmospheric storage tanks with gas blanketing, the design pressure of atmosphericstorage tanks shall be designed full of water + 150 mm water column and -50 mmwater column for vacuum condition.

API STD 2000 also describes the pressure and vacuum design requirement ofatmospheric tanks put in this category.




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Other storage tanks (Spheroid, etc.)

Depending on the type of tank, higher design pressures could be specified. This shall

be treated on a case-by-case basis depending on tank type but if storage tank has a

design pressure higher the 1.0 barg, it categorized as pressure vessel (pressurized

storage tank).




171/263

3.1.6 Pipelines

For pipelines, the design pressure is a function of the MOP and a design factor which

depends on the location. Process Engineer determines the MOP only; normally it is thedesign pressure of the last equipment upstream of the pipeline plus the hydrostatic

pressure due to the pipeline profile.



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173/263

3.2 Design Temperatures

- The design temperatures shall be generally specified as follows, for determination of

design temperature using the following table it is necessary to specify the lower andupper limit of operating temperature of the equipment




174/263


To be specified according to selected material and process

requirements.Above 343 C

Max. Op. Temp. + 25 C

orExceptional operating temp.Between 60 C and 343 C

85 C (min)

or

Exceptional operating temp.

Between 0 C and 60 C

Higher Limit :

Min. Op. Temp.5 CBetween -29 C and 0 C

- 45 CBetween -39 C and -30 C

-100 CBetween -100 C and -40 C

Min. Op. Temp.Less than -100C

Lower Limit:

Design Temperature (C)Operating Temp. (C)



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Notes:

- Exceptional operating temperature is to be considered for operations durationexceeding a total of 100 hours per year.

- 85 C is the minimum design temperature due to solar radiation.- The design temperature of equipment located downstream of air cooler or trim coolershall be specified as larger of:

Operating temperature +25 C

Or

Inlet operating temperature of upstream cooler




176/263

5:\ ocess c v es\ es g C e a

4.0 EQUIPMENT DESIGN

CRITERIA

Pump

Compressor

Heater

Vessel

Heat exchanger and Cooler



177/263

g

4.1 Pumps

All pumps, where their failure would cause a plant shutdown or unsafe conditions, shall

have a spare installed. One spare unit of a pump should be considered unless stated

otherwise.



178/263

g

- The minimum margin between the normal and rated flow for a pump shall be asfollows:

+15% of normal flowReciprocating and rotary

+30% of normal flowMetering

+20% of normal flowChemical Injection

+10% of normal flowLoading / Transfer

+10% of normal flowExport (continuous operation)

+10% of normal flowUtility+10% of normal flowOther Process

+25% of normal flowReflux, pump around and reboiler pumps

Rated FlowType of pump



179/263

g

- The static head used in calculating the suction pressure is measured from either:

The lowest operating liquid level in the suction vessel if this will initiate a shutdown ofthe pump when that level is reached (e.g. LSLL),

or,

The bottom tangent line for vertical vessels or the bottom invert line for horizontalvessels if no level-initiated pump shutdown is in place,

to one of the following lower elevations:


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181/263

g

- The equivalent length and frictional line losses may be calculated using theappropriate Line-sizing program. otherwise, the suction line equivalent length may beestimated from the pipe diameter d (inches) as follows:

Pumping temperature < 150 C, Le= 8d + 30 m

Pumping temperature 150 C, Le= 12d + 30 m



182/263

g

- Suction line sizing for reciprocating pumps shall take into account acceleration head

by:

Ha = L V N C / 9.8 K

L suction pipe length, m

V suction velocity, m/s

N,C constant from GPSA

K Cp/Cv

Ha acceleration loss, m

Reciprocating pumps shall have pulsation dampers on the suction and discharge side

where liquid pulsation should be minimized from process and operation view points.



183/263

g

4.2 Compressors

- All compressors, where their failure would cause a plant shut-down or unsafeconditions, shall have a spare installed. One spare unit of a compressor should beconsidered unless stated otherwise.

- Normally a 10% margin on maximum capacity will be used for sizing of compressors.

- The variation of gas compositions, molecular weight, Cp/CV, etc., and the operatingconditions (mainly suction and discharge temperature, pressure, and flowrate) shall betaken into account to determine the sizing case.

- Corrosive compounds in the gas (such as sulfur oxides, hydrogen sulfides, acidiccompounds, chlorides, etc.), are to be specified by the Process Engineer as these may

determine the selection of materials by the vendor.



184/263

g

- The following table gives an approximate value of the polytropic efficiency ofcentrifugal compressors:

0.7712700-340000

0.74850-12700

0.63170-850

Average Polytropic Eff ic iencyNominal Capacity

(m3/hr)



185/263

g

4.3 Heaters

- The design margin on Fired Heaters and Furnaces is 10% on heat duty.



186/263

4.4 Vessels

- The basis of sizing is the critical or terminal velocity VT (m/s), calculated from:

VT = K [(l -g)/ g]

where

l , g = liquid density, vapor density (kg/m3)

For vertical vessel vapor velocity shall be less than terminal velocity. The factor 0.85 isrecommended to calculated vapor velocity from terminal velocity.

For horizontal vessel higher vapor velocity may be used to meet acceptable L/D, butliquid droplet separation shall be checked. The upper limit of vapor velocity forhorizontal vessels is re-entrainment velocity.


187/263



188/263

K = 3.6 m/s

CD = Exp (8.411 2.243 X + 0.273 X2 1.865 10-2 X3 + 5.20110-4 X4)

Where

X = Ln ( )

Dp is assumed as follows:

General services: 200 micron

Flare K.O. drum: 600 micron

Note: Dp, m , kg/m3 , cp

K value without Mist Eliminator:

D

P

C

D

2

V

VL3PV

8 )(D1013.0



189/263

- The following hold up should be considered for vessel sizing:

200 mm minimum, butmust allow for time

required to close ESD orXV or stop pump

200 mm minimum, butmust allow for time

required to close ESD orXV or stop pump

Vessel Tangent

Line to LLLL

at least 2 minutes

with 200 mm minimum

at least 2 minutes

with 200 mm minimumLLLL to LLL

determined by the following table

with a 350 mm

minimum

determined by the following table

with a 350 mm minimumLLL to HLL

at least 2 minutes

with 200 mm minimum

at least 2 minutes

with 200 mm minimumHLL to HHLL

Horizontal VesselsVertical VesselsLevels



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- The minimum liquid hold-up times between LLL and HLL are as follows:

Greater volume of5 (below normal interface level) or10

(between water HLL-LLL)

Water Boot:

5 (with a pump)

3 (without a pump)Other Drums:

10Atmospheric De-Gassing Drum

5 (with or without a pump)c) Product to Exchanger or Storage Tank

5b) Product to other Column

5a) Product to next Process

Fractionation Tower Bottoms:

5Reflux Drum

10 (with or without a pump)b) to other Equipment:

10a) to a Heater

Feed Surge Drum:

Time (minutes)Service



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- The following design criteria shall be used for nozzle sizing:

Inlet Nozzle:Horizontal No demister pad mVm2 1000

Vertical No demister pad mVm2 1500Horizontal / Vertical Demister pad mVm2 6000

Horizontal / Vertical Demister pad gVg2 3750

Gas outlet nozzle:

gVg2 3750Liquid outlet nozzle:

V 1 m/secLiquid outlet nozzle

The minimum nozzle diameter shall be 50 mm (2 in.).

Where:

is fluid density in kg/m3V is fluid velocity in m/sec


192/263



193/263

- Number of Manways shall be determined according to the followings:

Vessels

A single manway shall be provided for vessel length or height less than 6 m.

For other vessels (length or height > 6 m), a minimum of two manways shall be

provided; one manway each 6 m for longer or taller vessel.

If vessel is equipped with internals (baffle, etc.), one manway shall be provided foreach compartment.



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- Number of Manways shall be determined according to the followings:

Trayed Columns

Manways shall be provided at the top, below the bottom tray, at the feed tray and

At any other tray at which removable internals are located.

Manways shall also be provided at intermediate points so that the maximum spacing ofmanways does not exceed 15 trays. This shall be reviewed on a case-by-case basis.Tray spacing with manway between internal shall be at least 900 mm.


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196/263

- The drain specification shall be determined on the following basis:

a) Drain Location

The drain of the vessel shall be connected:

To the outlet line at low point for vertical vessel

Directly on the vessel for horizontal vessel

Directly on the vessel for vertical vessels, where the outlet line extends inside the

vessel



197/263

b) Drain Sizes

Vent and drain diameter shall be determined as follows:

46V>420

44220 < V 420 or D > 6000

4375 &

Documents

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