ALL PROCESSES MUST HAVE SAFETY THROUGH …€¦ · BPCS Strength in Reserve • BPCS - Basic...
Transcript of ALL PROCESSES MUST HAVE SAFETY THROUGH …€¦ · BPCS Strength in Reserve • BPCS - Basic...
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ALL PROCESSES MUST HAVE SAFETYTHROUGH AUTOMATION
• SAFETY MUST ACCOUNT FOR FAILURES OFEQUIPMENT (INCLUDING CONTROL) & PERSONNEL
• MULTIPLE FAILURES MUST BE COVERED
• RESPONSES SHOULD BE LIMITED, TRY TOMAINTAIN PRODUCTION, IF POSSIBLE
• AUTOMATION SYSTEMS CONTRIBUTE TOSAFE OPERATION
(if they are designed and maintained properly!)
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LET’S CONSIDER A FLASH DRUM
Is this process safe and ready to operate?Is the design compete?
F1
hint
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• Four Layers in the Safety Hierarchy
• Methods and equipment required at all fourlayers
• Process examples for every layer
• Workshop
What’s in this topic?
SAFETY THROUGH AUTOMATION
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ALARMS
SIS
RELIEF
CONTAINMENT
EMERGENCY RESPONSE
BPCS
Strength in Reserve
• BPCS - Basic process control
• Alarms - draw attention
• SIS - Safety interlock systemto stop/start equipment
• Relief - Prevent excessivepressure
• Containment - Preventmaterials from reaching,workers, community orenvironment
• Emergency Response -evacuation, fire fighting,health care, etc.
SAFETY INVOLVES MANY LAYERS TO PROVIDEHIGH RELIABILITY
Control
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SAFETY STRENGTH IN DEPTH !
PROCESS
RELIEF SYSTEM
SAFETY INTERLOCK SYSTEM
ALARM SYSTEM
BASIC PROCESSCONTROL SYSTEM Closed-loop control to maintain process
within acceptable operating region
Bring unusual situation to attentionof a person in the plant
Stop the operation of part of process
Divert material safely
KEY CONCEPT IN PROCESS SAFETY -REDUNDANCY!
Seriousnessof event
Fourindependentprotectionlayers (IPL)
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CATEGORIES OF PROCESS CONTROLOBJECTIVES
1. Safety2. Environmental Protection3. Equipment Protection4. Smooth Operation & Production Rate5. Product Quality6. Profit7. Monitoring & Diagnosis
We are emphasizing these topics
Since people are involved, this isalso important
Control systems are designed to achieve well-definedobjectives, grouped into seven categories.
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1. BASIC PROCESS CONTROL SYSTEM (BPCS)
• Technology - Multiple PIDs, cascade, feedforward, etc.
• Always control unstable variables (Examples in flash?)
• Always control “quick” safety related variables
- Stable variables that tend to change quickly (Examples?)
• Monitor variables that change very slowly
- Corrosion, erosion, build up of materials
• Provide safe response to critical instrumentation failures
- But, we use instrumentation in the BPCS?
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1. BASIC PROCESS CONTROL SYSTEM (BPCS)
Where could we use BPCS in the flash process?
F1
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The level is unstable;it must be controlled.
The pressure willchange quickly andaffect safety; it must becontrolled.
F1
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1. BASIC PROCESS CONTROL SYSTEM (BPCS)
How would we protect against an error in the temperaturesensor (reading too low) causing a dangerously high reactortemperature?
TC
Coldfeed
Highly exothermic reaction.We better be sure that
temperature stays withinallowed range!
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How would we protect against an error in the temperaturesensor (reading too low) causing a dangerously high reactortemperature?
Use multiple sensors and select most conservative!
T1
Coldfeed
T2
TYTC
Measured valueto PID controller
Controlleroutput
>
TY>
Selects thelargest of allinputs
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2. ALARMS THAT REQUIRE ANALYSIS BYA PERSON
• Alarm has an annunciator and visual indication
- No action is automated!
- A plant operator must decide.
• Digital computer stores a record of recent alarms
• Alarms should catch sensor failures
- But, sensors are used to measure variables for alarmchecking?
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2. ALARMS THAT REQUIRE ANALYSIS BY APERSON
• Common error is to design too many alarms
- Easy to include; simple (perhaps, incorrect) fix toprevent repeat of safety incident
- One plant had 17 alarms/h - operator acted on only 8%
• Establish and observe clear priority ranking
- HIGH = Hazard to people or equip., action required
- MEDIUM = Loss of $$, close monitoring required
- LOWLOW = investigate when time available
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2. ALARMS THAT REQUIRE ANALYSIS BY APERSON
F1
Where could we use alarms
in the flash process?
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A low level coulddamage the pump; ahigh level couldallow liquid in thevapor line.
The pressure affectssafety, add a high alarm
F1
PAH
LAHLAL
Too much light keycould result in a largeeconomic loss
AAH
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3. SAFETY INTERLOCK SYSTEM (SIS)
• Automatic action usually stops part of plant operation toachieve safe conditions
- Can divert flow to containment or disposal- Can stop potentially hazardous process, e.g.,combustion
• Capacity of the alternative process must be for “worstcase”
• SIS prevents “unusual” situations
- We must be able to start up and shut down- Very fast “blips” might not be significant
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3. SAFETY INTERLOCK SYSTEM (SIS)
• Also called emergency shutdown system (ESS)
• SIS should respond properly to instrumentation failures
- But, instrumentation is required for SIS?
• Extreme corrective action is required and automated
- More aggressive than process control (BPCS)
• Alarm to operator when an SIS takes action
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3. SAFETY INTERLOCK SYSTEM (SIS)
• The automation strategy is usually simple, for example,
If L123 < L123min; then, reduce fuel to zero
steam
water
LC
PC
fuel
How do we automate this SIS
when PC is adjusting the valve?
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If L123 < L123min; then, reduce fuel to zero
steam
water
LC
PC
fuel
LS s s
fc fc
15 psig
LS = level switch, note that separate sensor is used
s = solenoid valve (open/closed) fc = fail closed
Extra valve with tight shutoff
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3. SAFETY INTERLOCK SYSTEM (SIS)
• The automation strategy may involve several variables,any one of which could activate the SIS
If L123 < L123min; orIf T105 > T105max…….then, reduce fuel to zero
SIS100
L123T105…..
s
Shown as “box” in drawing with details elsewhere
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3. SAFETY INTERLOCK SYSTEM (SIS)
• The SIS saves us from hazards, but can shutdown theplant for false reasons, e.g., instrument failure.
1 out of 1 must indicate
failure
T100s
2 out of 3 must indicate
failure
T100T101T102
Same variable,multiple sensors!
s
Falseshutdown
Failureondemand
5 x 10-35 x 10-3
2.5 x 10-6 2.5 x 10-6
Betterperformance,more expensive
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Medium2
Major3
Major3
Minimal1
Medium2
Major3
Minimal1
Minimal1
Medium2
low moderate high
Event Likelihood
Eve
nt S
ever
ity
extensiveseriousminor
Table entriesword = qualitative risk description
number = required safety integrity level (SIL)
Safety Integrity Levels(Prob. Of failure on demand)
1 = .01 to .1
2 = .001 to .01
3 = .0001 to .001
RISK MATRIX FOR SELECTING SIS DESIGN
Selectiondocumented forlegalrequirements
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3. SAFETY INTERLOCK SYSTEM (SIS)
• We desire independent protection layers, withoutcommon-cause failures - Separate systems
sensors
SIS system
i/o i/o………….
sensors
Digital control system
i/o i/o………….
BPCS and AlarmsSIS and Alarmsassociated with SIS
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SAFETY STRENGTH IN DEPTH !
PROCESS
RELIEF SYSTEM
SAFETY INTERLOCK SYSTEM
ALARM SYSTEM
BASIC PROCESSCONTROL SYSTEM Closed-loop control to maintain process
within acceptable operating region
Bring unusual situation to attentionof a person in the plant
Stop the operation of part of process
Divert material safely
These layers requireelectrical power,computing,communication, etc.
KEY CONCEPT IN PROCESS SAFETY -REDUNDANCY!
What do we do if a major incident occurs that causes
• loss of power or communication• a computer failure (hardware or software)
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4. SAFETY RELIEF SYSTEM
• Entirely self-contained, no external power required
• The action is automatic - does not require a person
• Usually, goal is to achieve reasonable pressure
- Prevent high (over-) pressure- Prevent low (under-) pressure
• The capacity should be for the “worst case” scenario
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4. SAFETY RELIEF SYSTEM
• Two general classes of devices
- Self-Closing: design provides forclosing of flow path when the systempressure returns within its acceptablerange; operation can resume
Example: Spring safety valve
- Non-self-closing: Remains open.Typically, the process must beshutdown and the device replaced
Example: Burst diaphragm
Next lesson covers these in more detail
Copyrights by CCPS/American Institute ofChemical Engineers and copied with thepermission of AIChE
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GOOD PRACTICES IN CONTROL FOR SAFETY
1) never by-pass the calculation (logic) for the SIS, i.e., never turn it off2) never mechanically block a control, SIS valve so that it can not close3) never open manual by-pass values around control and shutdown valves4) never "fix" the alarm acknowledgement button so that new alarms will not
require the action of an operator5) avoid using the same sensor for control, alarm, and SIS. Also, avoid
using the same process connection (thermowell, tap, etc.) for all sensors.6) avoid combining high and low value alarms into one indication7) critically evaluate the selection of alarms, do not have too many alarms8) use independent equipment for each layer, including computing
equipment9) select emergency manipulated variables with a fast effect on the key
process variable10) use redundant equipment for critical functions11) provide capability for maintenance testing, since the systems are normally
in "stand-by” for long times - then must respond as designed!
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SAFETY AUTOMATION SYSTEMS,WHAT HAVE WE LEARNED?
• Typically, four layers are designed for a process
• Each layer has special technology and advantages
• Layers must be part of process design
• Layers contribute to safety, but if incorrect, can beunsafe
We are now ready to gain experience in designing andevaluating safety automation systems.
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SAFETY STRENGTH IN DEPTH !
PROCESS
RELIEF SYSTEM
SAFETY INTERLOCK SYSTEM
ALARM SYSTEM
BASIC PROCESSCONTROL SYSTEM Closed-loop control to maintain process
within acceptable operating region
Bring unusual situation to attentionof a person in the plant
Stop the operation of part of process
Divert material safely
By the way, whichof the four layersuses the feedback
principle?
SAFETY THROUGH AUTOMATION
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REFERENCES
AIChE, Guidelines for Engineering Design for Process Safety, American Institute of Chemical Engineers,New York, 1993, Chapter 9.
AIChE, Guidelines for Safe Automation of Chemical Processes, American Institute of Chemical Engineers,Research Triangle Park, NC, 1994
AIChE, International Symposium and Workshop on Safe Chemical Process Automation, American Instituteof Chemical Engineers, New York, 1994
Englund, S. and D. Grinwis, Provide the Right Redundancy for Control Systems, CEP, Oct. 1992, 36-44.
Fisher, T. (Ed), AControl System Safety@, ISA Transactions, 30, 1, (special edition), 1991
Goble, W., Evaluating Control System Reliability, Instrument Society of America, Research Triangle Park,1992
International Symposium and Workshop on Safe Chemical Process Automation, Sept 27-29, 1994,American Institute of Chemical Engineers, New York, 1994
Marlin, T., Process Control: Designing Processes and Control Systems for Dynamic Performance 2nd Ed.,McGraw-Hill, New York, 2000, Section 24.8 - p. 794-799.
Summers, A., Techniques for Assigning a Target Safety Integrity Level, ISA Transactions, 37, 1998, 95-104.
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SAFETY THROUGH AUTOMATION WORKSHOP 1
1. Review the distillation process on the next slide.
2. Locate at least one example of each of the fourlayers of safety automation
3. Evaluate each example that you find.
(Remember, the example is for educationalpurposes which could include errors forworkshops.)
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1
2
3
15
16
17LC-1
LC-3
LC-2
Feed drum attenuatescompositiondisturbances
Averaging level controlattenuates flow ratedisturbances
dP-1
dP-2
To flare
T5
T6
TC-7
AC-1
LAHLAL
LAHLAL
PAH
PC-1
P3
F3F4
F7
F8
F9
Feed flow rate andcompositiondisturbances
PV-3
TAL
T10
L4
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SAFETY THROUGH AUTOMATION WORKSHOP 1
1. Review the fired heater process on the next slide.
2. Equipment would be damaged and personnelcould be injured if the combustion continuedwhen the process is not operating properly.
Determine a mal-operation that could lead tounsafe operation.
3. Determine the sensors, the final element(s) andSIS logic to provide a safe system.
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FT1
FT2
PT1
PIC1
AT1
TI1
TI2
TI3
TI4
PI2
PI3
PI4
TI5
TI6
TI7
TI8
TI9
FI3
TI10
TI11
PI5
PI6