1. SIMPLE WAY TOSIMPLE WAY TO
UNDERSTAND AMMONIAUNDERSTAND AMMONIA
PLANTPLANT
BYBY
PREM BABOOPREM BABOO
SR. MANAGER(PROD)SR. MANAGER(PROD)
NATIONAL FERTILIZERS LTD,VIJAIPUR, INDIANATIONAL FERTILIZERS LTD,VIJAIPUR, INDIA
2. SIMPLE WAY TO UNDERSTANDSIMPLE WAY TO UNDERSTAND
AMMONIA PLANTAMMONIA PLANT
TECHNOLOGY HALDOR TOPSOETECHNOLOGY HALDOR TOPSOE
CAPACITY 1750/1864 TPDCAPACITY 1750/1864 TPD
FEED NG AND NEPTHAFEED NG AND NEPTHA
ENERGY 7.2GCAL/TON OF AMMONIAENERGY 7.2GCAL/TON OF AMMONIA
ON NGON NG
7.36 GCAL/TON OFAMMONIA IN7.36 GCAL/TON OFAMMONIA IN
CASE OF MIXED FEEDCASE OF MIXED FEED
3.
4. INGREDIENT FOR AMMONIAINGREDIENT FOR AMMONIA
TO PRODUCE AMMONIA WE REQUIRETO PRODUCE AMMONIA WE REQUIRE
HH22 AND NAND N22
HH22 WE GET FROM NG AND WATERWE GET FROM NG AND WATER
NN22 WE GET FROM AIRWE GET FROM AIR
NG CONTAINS ABOUT 92%CHNG CONTAINS ABOUT 92%CH44
NEPTHA CONTAINS HIGHERNEPTHA CONTAINS HIGHER
HYDROCAREBONHYDROCAREBON
5. BLOCK DIGRAM OF AMOONIABLOCK DIGRAM OF AMOONIA
PLANTPLANT
DESULPHERISATION REFORMING
SHIFT REACTION CO2 REMOVAL AREA
SYNTHESIS
COMP HOUSE
CO2 TO UREA
AMM TO UREA
AND METHNATION
6. DESULPHERISATIONDESULPHERISATION
AIMAIM
TO REMOVE ALL SULPHERTO REMOVE ALL SULPHER
COMING WITH NG AND NEPTHACOMING WITH NG AND NEPTHA
SULPHER IS POISIONOUS FOR THESULPHER IS POISIONOUS FOR THE
DOWNSTREAM CATALAYSTDOWNSTREAM CATALAYST
IT CONSISTS OF TWO STEPSIT CONSISTS OF TWO STEPS
7. HYDROGENATIONHYDROGENATION
IN THIS VESSLE NG AND NEPTHA AREIN THIS VESSLE NG AND NEPTHA ARE
BROUGHT IN CONTACT WITHBROUGHT IN CONTACT WITH
HYDROGEN SO THAT ORGANICHYDROGEN SO THAT ORGANIC
SULPHER GETS CONVERTED INTOSULPHER GETS CONVERTED INTO
INORGANIC SULPHER WHICH ISINORGANIC SULPHER WHICH IS
SUBSEQUENTLY REMOVED IN ZNOSUBSEQUENTLY REMOVED IN ZNO
ABSORBERABSORBER
CATALYST NIMO –FOR NGCATALYST NIMO –FOR NG
COMO -FOR NAPHTHACOMO -FOR NAPHTHA
9. ZnO ABSORBERZnO ABSORBER
TWO BEDS ARE INSTALLED IN SERIESTWO BEDS ARE INSTALLED IN SERIES
CATALYST USED IS = ZnOCATALYST USED IS = ZnO
ZnO+HZnO+H22S = ZnS + HS = ZnS + H22OO
SULPHER AT THE OUTLET OF THESE VESSLE ARESULPHER AT THE OUTLET OF THESE VESSLE ARE
LESS THAN .01PPMLESS THAN .01PPM
INCREASING SULPHER CONTENT GIVE THEINCREASING SULPHER CONTENT GIVE THE
INDICATION THAT BEDS ARE GETTING EXHUSTEDINDICATION THAT BEDS ARE GETTING EXHUSTED
AND THEY REQUIRE CHANGEAND THEY REQUIRE CHANGE
FIRST BED CAN BE BYPASSED AND CATALYST CANFIRST BED CAN BE BYPASSED AND CATALYST CAN
BE CHANGED ON LINE A SPECIAL BED OF CopperBE CHANGED ON LINE A SPECIAL BED OF Copper
BASEDCATALYST IS INSTALLED AT THE BOTTOM OFBASEDCATALYST IS INSTALLED AT THE BOTTOM OF
THE FIRST BED TO ADSORB ANY ORGANIC SULPHERTHE FIRST BED TO ADSORB ANY ORGANIC SULPHER
IF IT SLIPS FROM HYDROGEATION BEDIF IT SLIPS FROM HYDROGEATION BED
11. REFORMINGREFORMING
AIMAIM
TO REFORM NG AND NEPTHA IN TO HTO REFORM NG AND NEPTHA IN TO H22
CO AND COCO AND CO22 REFORMING IS DONE WITHREFORMING IS DONE WITH
THE HELP OF STEAM THATIS WHY IT ISTHE HELP OF STEAM THATIS WHY IT IS
CALLED STEAM REFORMING ITCALLED STEAM REFORMING IT
CONSIST OF THREE STEPSCONSIST OF THREE STEPS
12. STEPS OF REFORMINGSTEPS OF REFORMING
PREREFORMERPREREFORMER
PRIMARY REFORMERPRIMARY REFORMER
SECONDRY REFORMERSECONDRY REFORMER
13. CONDITION OF REFORMINGCONDITION OF REFORMING
REFORMING IS AN ENDOTHERMIC REACTIONREFORMING IS AN ENDOTHERMIC REACTION
IT MEANS THAT HEAT WILL HAVE TO BEIT MEANS THAT HEAT WILL HAVE TO BE
SUPPLIED TO MOVE THE REACTION INSUPPLIED TO MOVE THE REACTION IN
FORWARD DIRECTIONFORWARD DIRECTION
MAJOR PORTION OF REFORMING IS DONE INMAJOR PORTION OF REFORMING IS DONE IN
PRIMARY REFORMER THIS REACTION ISPRIMARY REFORMER THIS REACTION IS
CARRIED OUT IN A FURNACE OPERATINGCARRIED OUT IN A FURNACE OPERATING
CONDITIONS ARE VERY INTENCECONDITIONS ARE VERY INTENCE
15. HOW OPERATING CONDIONSHOW OPERATING CONDIONS
ARE DECIDEDARE DECIDED
AS PER LE CHATERLIERS PRINCIPLE THEAS PER LE CHATERLIERS PRINCIPLE THE
REACTION OF REFORMING REQUIRESREACTION OF REFORMING REQUIRES
HIGH TEMERATUTRE CONDITIONSHIGH TEMERATUTRE CONDITIONS
LOW PRESSURE CONDITIONSLOW PRESSURE CONDITIONS
OPTIMUM PRESSURE IS SET ARROUNDOPTIMUM PRESSURE IS SET ARROUND
34KGCM34KGCM22
PRESSURE BELOW THIS SUITS REFORMIGPRESSURE BELOW THIS SUITS REFORMIG
REACTION BUT THIS IS NOT SUITABLE FORREACTION BUT THIS IS NOT SUITABLE FOR
DOWNSREAM REACTIONSDOWNSREAM REACTIONS
16. CATALYST USED INCATALYST USED IN
REFORMINGREFORMING
CATALYST USED IS NICKLECATALYST USED IS NICKLE
IN VARIOUS REFORMING STEPS ONLYIN VARIOUS REFORMING STEPS ONLY
THE CONTENT OF NICKLE VARRIESTHE CONTENT OF NICKLE VARRIES
BESIDES THIS BASE OF THE CATALYSTBESIDES THIS BASE OF THE CATALYST
ALSO VARRIESALSO VARRIES
CONDENSATION OF STEAM IS TO BECONDENSATION OF STEAM IS TO BE
AVOIDED IN CATALYST BEDAVOIDED IN CATALYST BED
BECAUUSE IT MAY SPOIL THE ENTIREBECAUUSE IT MAY SPOIL THE ENTIRE
CATALYSTCATALYST
17. PRE REFORMERPRE REFORMER
PRE REFORMER IS ISTALLED IN AMMONIAPRE REFORMER IS ISTALLED IN AMMONIA
EXPANSIONEXPANSION
ITS PURPOSE IS TO REFORM HIGER HYDROCARBONITS PURPOSE IS TO REFORM HIGER HYDROCARBON
TO LOWER HYDROCARBONTO LOWER HYDROCARBON
TO BE KEPT IN LINE WHEN NEPTHA IS BEING USEDTO BE KEPT IN LINE WHEN NEPTHA IS BEING USED
IN FEEDIN FEED
WITHOUT PREREFORMER NEPTHA CAN NOT BEWITHOUT PREREFORMER NEPTHA CAN NOT BE
USED IN FEEDUSED IN FEED
IT CAN BE KEPT IN LINE WITH NG ALSO BUT NOTIT CAN BE KEPT IN LINE WITH NG ALSO BUT NOT
WITH GREAT DEAL OF ADVANTAGEWITH GREAT DEAL OF ADVANTAGE
ITS CATALYST IS ONE OF THE COSLIEST INITS CATALYST IS ONE OF THE COSLIEST IN
AMMONIA PLANTAMMONIA PLANT
19. PRIMARY REFORMERPRIMARY REFORMER
IT IS THE MOST IMPORTANT STEP INIT IS THE MOST IMPORTANT STEP IN
THE REFORMING PROCESSTHE REFORMING PROCESS
IT COSIST OF A FURNACEIT COSIST OF A FURNACE
FURNACE IS SIDE FIREDFURNACE IS SIDE FIRED
IT CONTAINS 288 TUBES AND 576IT CONTAINS 288 TUBES AND 576
BURNERSBURNERS
CATALYST IS FILLED INSIDE THE TUBECATALYST IS FILLED INSIDE THE TUBE
FIRING IS DONE ON BOTH THE SIDESFIRING IS DONE ON BOTH THE SIDES
OF THE TUBEOF THE TUBE
21. IMPORTANT PARAMETER OFIMPORTANT PARAMETER OF
PRIMARY REFORMERPRIMARY REFORMER
FURNACE INSIDE PRESSURE SHOULD BEFURNACE INSIDE PRESSURE SHOULD BE
SLIHTLY BELOW ATMOSPHERIC PRESSURESLIHTLY BELOW ATMOSPHERIC PRESSURE
ARROND -5MMWCARROND -5MMWC
TUBES SKIN TEMP SHOULD NOT EXCEEDTUBES SKIN TEMP SHOULD NOT EXCEED
905DEGREE CENTRIGADE OTHRWISE TUBE905DEGREE CENTRIGADE OTHRWISE TUBE
LIFE WOULD BE SHORTENEDLIFE WOULD BE SHORTENED
S/C RATIO IS ONE OF THE MOST IMPS/C RATIO IS ONE OF THE MOST IMP
PARAMETE ITS KEPT ARROUND 3.3 LOWERPARAMETE ITS KEPT ARROUND 3.3 LOWER
S/C RATIO MAY RESULT IN CARBONS/C RATIO MAY RESULT IN CARBON
FORMATIONFORMATION
22. SECONDRY REFORMINGSECONDRY REFORMING
AIMAIM
TO COMLETE THE REMAININGTO COMLETE THE REMAINING
REFORMINGREFORMING
TO INTRODUCE AIR SO THAT WE CANTO INTRODUCE AIR SO THAT WE CAN
GET N2 REQUIRED FOR THE AMMONIAGET N2 REQUIRED FOR THE AMMONIA
PRODUCTIONPRODUCTION
24. WHAT HAPPENS IN SECONDRYWHAT HAPPENS IN SECONDRY
REFORMERREFORMER
PRIMARY REFORMER OUTLET GASPRIMARY REFORMER OUTLET GAS
WHICH CONTAINS ABOUTWHICH CONTAINS ABOUT
11%METHANE AT ATEMP OF ABOUT11%METHANE AT ATEMP OF ABOUT
765DEGREE IS BROGHT IN CONTACT765DEGREE IS BROGHT IN CONTACT
WITH AIR AT A TEMP OF 575 DEGREEWITH AIR AT A TEMP OF 575 DEGREE
FIRST REACTION IN SR IS EXOTHERMICFIRST REACTION IN SR IS EXOTHERMIC
REACTION IN WHICH APART OF GASREACTION IN WHICH APART OF GAS
BURNS WITH AIR O2 GETS CONSUMEDBURNS WITH AIR O2 GETS CONSUMED
25. WHAT HAPPENS IN SECONDRYWHAT HAPPENS IN SECONDRY
REFORMERREFORMER
TEMERATURE OF GAS IN TOP PAERT OFTEMERATURE OF GAS IN TOP PAERT OF
REFORMER REACHES TO ARROUNDREFORMER REACHES TO ARROUND
1200 DEGREE1200 DEGREE
THIS HEAT IS USED FOR FURTHERTHIS HEAT IS USED FOR FURTHER
REFORMINGREFORMING
METHANE AT OUTLET OF SR BECOMESMETHANE AT OUTLET OF SR BECOMES
ABOUT .3%ABOUT .3%
SR OUTLET TEMP BECOMES 940SR OUTLET TEMP BECOMES 940
DEGREEDEGREE
26. SHIFT REACTIONSHIFT REACTION
AIMAIM
GAS AT THE OUTLET OF SR CONTAINSGAS AT THE OUTLET OF SR CONTAINS
BOTH CO AND CO2BOTH CO AND CO2
CO IS OF NO USECO IS OF NO USE
CO2 IS REQUIRED FOR THECO2 IS REQUIRED FOR THE
PRODUCTION OF UREAPRODUCTION OF UREA
IN SHIFT REACTORS ALL CO ISIN SHIFT REACTORS ALL CO IS
CONVERTED IN TO CO2CONVERTED IN TO CO2
27. SHIFT REACTIONSHIFT REACTION
SHIFT REACTION IS TWO STEPSHIFT REACTION IS TWO STEP
PROCESSPROCESS
FIRST STEP IS CARRIED OUT AT HIGHFIRST STEP IS CARRIED OUT AT HIGH
TEMP IT IS CALLED HT SHIFTTEMP IT IS CALLED HT SHIFT
REACTION TO INCREASE THE RATE OFREACTION TO INCREASE THE RATE OF
REACTIONREACTION
SECOND STEP IS CARRIED OUT AT LOWSECOND STEP IS CARRIED OUT AT LOW
TEMP CALLED LT SHIFT REACTION ITTEMP CALLED LT SHIFT REACTION IT
IS TO ACHIVE HIGH EQULIBIRIUMIS TO ACHIVE HIGH EQULIBIRIUM
CONVERSIONCONVERSION
28. HT SHIFT CONVERTORHT SHIFT CONVERTOR
CATALYST USED IRON OXIDECATALYST USED IRON OXIDE
INLETTEMP 355 DEGREEINLETTEMP 355 DEGREE
OUTLET TEMP 423DEGREEOUTLET TEMP 423DEGREE
OUTLET CO 2.8%OUTLET CO 2.8%
CO+HCO+H22O = COO = CO22 +H+H22
29. HT SHIFT CONVERTORHT SHIFT CONVERTOR
HT SHIFT
CATALYST
IRON OXIDE
SR OULET GAS
GAS TO LT
355
423
CO 2.8%
CO 12.77
30. LT CONVERTORLT CONVERTOR
CATALEST USED MIANLY CUCATALEST USED MIANLY CU
INLET TEMP 195 DEGREEINLET TEMP 195 DEGREE
OUTLET 212 DEGREEOUTLET 212 DEGREE
OUTLET CO .17%OUTLET CO .17%
CO +HCO +H22O = COO = CO22 + H+ H22
POISON FOR THE CATALYST AREPOISON FOR THE CATALYST ARE
S AND CHLORIDES AND CHLORIDE
31. LT SHIFT CONVERTORLT SHIFT CONVERTOR
LT CONVERTOR
HT OUUTLET
LT OUTLET
CO .17%
CO 2.8%
32. CO2 REMOVALCO2 REMOVAL
TWO MAIN PROCESS FOR THIS ARETWO MAIN PROCESS FOR THIS ARE
BENFIELD PROCESS USED IN LINE 1BENFIELD PROCESS USED IN LINE 1
GV PROCESS USED IN LINE 2GV PROCESS USED IN LINE 2
GV PROCESS USED IN LINE 2 HAS SOMEGV PROCESS USED IN LINE 2 HAS SOME
ADVANTAGE OVER BENFIELD PROCESSADVANTAGE OVER BENFIELD PROCESS
33. GV PROCESSGV PROCESS
AIMAIM
TO REMOVE ALL CO2 FROM THETO REMOVE ALL CO2 FROM THE
PROCESS GAS BY ABSORBING IN HOTPROCESS GAS BY ABSORBING IN HOT
POTTASIUM CARBONATE SOLUTIONPOTTASIUM CARBONATE SOLUTION
AND THEN REGENERATING THEAND THEN REGENERATING THE
SOLUTIONSOLUTION
CO2 PRODUCED IS SENT TO UREACO2 PRODUCED IS SENT TO UREA
PLANTPLANT
34. GV PROCESSGV PROCESS
SOLUTION IS MADE OF POTTASSIUMSOLUTION IS MADE OF POTTASSIUM
CARBONATECARBONATE
TWO ACTIVATORS USED ARETWO ACTIVATORS USED ARE
GLYCENE AND DEAGLYCENE AND DEA
COMPOSITIONCOMPOSITION
KK22COCO33 27%27%
GLYCENE 1.2%GLYCENE 1.2%
DEA 1.0%DEA 1.0%
VANADIUM .4%VANADIUM .4%
36. TWO STAGE REGENERATION & USE OF FLASH STEAM OF HP IN LPTWO STAGE REGENERATION & USE OF FLASH STEAM OF HP IN LP
REGENERATOR & REDUCTION IN LP STEAMREGENERATOR & REDUCTION IN LP STEAM
REDUCTION CO2 SLIP by 1000PPMREDUCTION CO2 SLIP by 1000PPM
IMPROVED HEAT RECOVERYIMPROVED HEAT RECOVERY
38. BLOCK DIGRAMBLOCK DIGRAM
CO2 FREE GASCO2 FREE GAS
ABSORBER
GAS
SOLUTION
LOADED SOL
REGENERATOR
CO2
REGENERATED SOL
LOADED SOL
STEAM
39. METHNATIONMETHNATION
AIMAIM
TO CONVERT ALL CO AND COTO CONVERT ALL CO AND CO22 TOTO
METHANEMETHANE
OUTLET GAS FROM COOUTLET GAS FROM CO22 REMOVALREMOVAL
AREA CONTAINS BOTH C0 AND C0AREA CONTAINS BOTH C0 AND C022
BOTH THESE GAS ARE NOT REQUIREDBOTH THESE GAS ARE NOT REQUIRED
AS THESE ARE POISON FOR THE SYNAS THESE ARE POISON FOR THE SYN
CATALYSTCATALYST
40. METHNATIONMETHNATION
CATALYST USED NICKLECATALYST USED NICKLE
C0 + HC0 + H22 = CH= CH44 + HEAT+ HEAT
COCO22 +H+H22 =CH=CH44 + HEAT+ HEAT
METHANE FORMED ACTS AS A INERTMETHANE FORMED ACTS AS A INERT
GAS IN SYN REACTION AND IT ISGAS IN SYN REACTION AND IT IS
REMOVED IN PURGE TAKEN OUT FROMREMOVED IN PURGE TAKEN OUT FROM
THE SYN LOOPTHE SYN LOOP
42. COMP HOUSECOMP HOUSE
COMP HOUSE CONTAINS THREE COMPCOMP HOUSE CONTAINS THREE COMP
AIR COMPAIR COMP
REFRIGRATION COMPREFRIGRATION COMP
SYNTHESIS COMPSYNTHESIS COMP
43. AIR COMPAIR COMP
AIMAIM
AIR COMPRESSOR COMPRESSES AIR UPAIR COMPRESSOR COMPRESSES AIR UP
TO 34KGCM2 PRESSURETO 34KGCM2 PRESSURE
AIR IS USED IN SECONDRY REFORMERAIR IS USED IN SECONDRY REFORMER
H2/N2 RATIO DETERMINES FLOW OFH2/N2 RATIO DETERMINES FLOW OF
AIR TO SECONDRY REFORMERAIR TO SECONDRY REFORMER
45. REFRIGRATION COMPRESSORREFRIGRATION COMPRESSOR
AIMAIM
IT IS USED TO COMPRESS AMMONIAIT IS USED TO COMPRESS AMMONIA
WHICH IS USED AS A REFRIGRENT INWHICH IS USED AS A REFRIGRENT IN
SYNTHESIS LOOPSYNTHESIS LOOP
REFIGRATION IS DONE AT THREEREFIGRATION IS DONE AT THREE
PRESSURE LEVELPRESSURE LEVEL
ITS FINAL DISCHARGE PRESSURE ISITS FINAL DISCHARGE PRESSURE IS
14KG CM214KG CM2
46. SYNTHESIS COMPSYNTHESIS COMP
AIMAIM
AMMONIA SYNTHESIS REACTION ISAMMONIA SYNTHESIS REACTION IS
CARRIED OUT AT HIGH PRESSURECARRIED OUT AT HIGH PRESSURE
CONDITIONS AT ABOUT 180KGCM2CONDITIONS AT ABOUT 180KGCM2
SYN COMP IS USED TO COMPRESS GASSYN COMP IS USED TO COMPRESS GAS
UP TO THAT PRESSUREUP TO THAT PRESSURE
48. AMMONIA SYNTHESISAMMONIA SYNTHESIS
AIMAIM
TO PRODUCE AMMONIA WITH THETO PRODUCE AMMONIA WITH THE
HELP OF SYN GAS COMING FROMHELP OF SYN GAS COMING FROM
METHNATORMETHNATOR
SYN GAS CONTAINS MAINLY HSYN GAS CONTAINS MAINLY H22 AND NAND N22
49. AMMONIA SYN REACTIONAMMONIA SYN REACTION
3H3H22 +N+N22 = 2NH= 2NH33 +HEAT+HEAT
CATALYST USED IRONCATALYST USED IRON
REACTION CONDITIONREACTION CONDITION
HIGH PRESSURE AND LOW TEMPHIGH PRESSURE AND LOW TEMP
50. AMMONA SYN REACTIONAMMONA SYN REACTION
AMMONIA SYN REACTION IS A REVERSIBILEAMMONIA SYN REACTION IS A REVERSIBILE
REACTION AND EQULIBIRIUM CONDITION ISREACTION AND EQULIBIRIUM CONDITION IS
DETERMINED BY TEMP AND PRESSUREDETERMINED BY TEMP AND PRESSURE
CONDITIONSCONDITIONS
IN ONE PASS THROUGH THE CONVERTORIN ONE PASS THROUGH THE CONVERTOR
ONLY 30% OF THE REACTANTS GETSONLY 30% OF THE REACTANTS GETS
CONVERTED TO THE PRODUCT SOCONVERTED TO THE PRODUCT SO
REMAINING GAS KEEPS ON CIRCULATINGREMAINING GAS KEEPS ON CIRCULATING
53. BLOCK DIGRAM OF SYNBLOCK DIGRAM OF SYN
SECTIONSECTION
AMM CONVERTOR BFW HEATER
GAS GAS EX WATER COOLER GAS GAS EX
PRI CHIL SEC CHILL AMM SEP LET DOWNVESSLE
LOOP BOILER
STEAM
PURGE GAS
AMM TO UREA
TO
STORAGE
SYN GAS
54.
55. What is purgeWhat is purge
AS AMMONIA SYN REACTION IS NOTAS AMMONIA SYN REACTION IS NOT
COMPLETED IN ONE STEP AND GAS IS KEPTCOMPLETED IN ONE STEP AND GAS IS KEPT
ON CIRCULATING INERTS BUILDS UP IN THEON CIRCULATING INERTS BUILDS UP IN THE
LOOPLOOP
INERT MEANS CH4, Ar NH3 AT INLET OFINERT MEANS CH4, Ar NH3 AT INLET OF
CONV THEIR CONCENTRATION SHALL NOTCONV THEIR CONCENTRATION SHALL NOT
INCREASE BEYOND 14%INCREASE BEYOND 14%
SO A SMALL AMMOUNT OF GAS ISSO A SMALL AMMOUNT OF GAS IS
CONTTIOUSLY WITHDRAWN FROM THECONTTIOUSLY WITHDRAWN FROM THE
LOOP THIS STREAM OF THE GAS IS CALLEDLOOP THIS STREAM OF THE GAS IS CALLED
PUGE GASPUGE GAS
56. PURGE GAS RECOVERYPURGE GAS RECOVERY
PURGE GAS CONTAINS HPURGE GAS CONTAINS H22, CH, CH44 ANDAND
AMMONIAAMMONIA
AMMONIA IS RECOVERED BYAMMONIA IS RECOVERED BY
WASHING THE GAS WITH WATER ANDWASHING THE GAS WITH WATER AND
REMAINING GAS WHICH CONTAINS CHREMAINING GAS WHICH CONTAINS CH44
AND HAND H22 IS USED IN REFORMER FIRINGIS USED IN REFORMER FIRING
SYSTEMSYSTEM
57. PURGE GAS RECOVERYPURGE GAS RECOVERY
ABSORBER REGENERATIONR
PUURGE
WATER
STEAM
GAS TO REF
LOADED SOL
AM TO STORAGE
58. Installation of Plate type Combustion airInstallation of Plate type Combustion air
preheaterpreheater
Facilitate reduction in reformer stack temperature toFacilitate reduction in reformer stack temperature to
125125°C°C
Energy saving: 0.055 Gcal /MT NH3Energy saving: 0.055 Gcal /MT NH3
Energy saving due toEnergy saving due to
a) NG saving due to increase in combustion aira) NG saving due to increase in combustion air
temperaturetemperature
B) Reduction in steam consumption in ID FanB) Reduction in steam consumption in ID Fan
59. Conversion of Benfield process to GVConversion of Benfield process to GV
processprocess
To increase capacity and improve energyTo increase capacity and improve energy
effciencyeffciency
GV 2 stage process has a lower specificGV 2 stage process has a lower specific
regeneration heat requirement and henceregeneration heat requirement and hence
reduction in low pressure steam consumption byreduction in low pressure steam consumption by
utilizing flash steam of HP regenerator &utilizing flash steam of HP regenerator &
utilization heat by LP steam reboiler instead ofutilization heat by LP steam reboiler instead of
loosing to atmosphere through air coolerloosing to atmosphere through air cooler
Energy savings: 0.18 Gcal/MT NH3Energy savings: 0.18 Gcal/MT NH3
Existing Amm-II is based on GV ProcessExisting Amm-II is based on GV Process
60. New equipment in conversion from Benfield to GVNew equipment in conversion from Benfield to GV
sectionsection
Separator OH 2Separator OH 2ndnd
regenerator (B-1307)regenerator (B-1307)
LP steam boiler (E-1301)LP steam boiler (E-1301)
DMW pre-heater (E-1305 A/B)DMW pre-heater (E-1305 A/B)
Condenser OH 2Condenser OH 2ndnd
regenerator (E-1309)regenerator (E-1309)
22ndnd
Regenerator (F-1303)Regenerator (F-1303)
Steam Ejector (X-1301)Steam Ejector (X-1301)
Aeration Injection tank (T-1305)Aeration Injection tank (T-1305)
Sealing water heater (E-1315)Sealing water heater (E-1315)
Cooler for Aeration tank (E-1324)Cooler for Aeration tank (E-1324)
Activated carbon filter and 2Activated carbon filter and 2ndnd
Mechanical filterMechanical filter
61. New machinery in conversion from Benfield to GVNew machinery in conversion from Benfield to GV
sectionsection
CO2 blower (K-1301)CO2 blower (K-1301)
Semi-lean solution pump (P-1301D)Semi-lean solution pump (P-1301D)
Lean solution pump (P-1302 A/B)Lean solution pump (P-1302 A/B)
22ndnd
condensate pump (P-1308 A/B)condensate pump (P-1308 A/B)
Aeration Injection pump (P-1309 A/B)Aeration Injection pump (P-1309 A/B)
Sealing water pump (P-1310 A/B)Sealing water pump (P-1310 A/B)
62. Modifications in 1Modifications in 1stst
regeneratorregenerator
New take off trays are installed below bed 2New take off trays are installed below bed 2
and above bed 3and above bed 3
New liquid re-distributors above bed 1 and 3New liquid re-distributors above bed 1 and 3
Bed limiters over beds 1 and 3Bed limiters over beds 1 and 3
11stst
bed height reduced by 2195 mmbed height reduced by 2195 mm
DemisterDemister
New nozzles and instrumentation for newNew nozzles and instrumentation for new
take-off traystake-off trays
63. Modification in CO2 absorberModification in CO2 absorber
Liquid distributor over Bed 2 and 4Liquid distributor over Bed 2 and 4
Liquid redistributor over beds 1,2,3 & 4Liquid redistributor over beds 1,2,3 & 4
Gas distributor under bed 1Gas distributor under bed 1
Packing : Bed 1: IMTP 50 Bed 4: IMTP25Packing : Bed 1: IMTP 50 Bed 4: IMTP25
64. Installation of S-50 converterInstallation of S-50 converter
To increase the energy efficiency of the ammoniaTo increase the energy efficiency of the ammonia
synthesis loop, an S-50 converter R-1502 is installedsynthesis loop, an S-50 converter R-1502 is installed
downstream of the existing converter.downstream of the existing converter.
The increase in ammonia concentration exit the newThe increase in ammonia concentration exit the new
converter results in a decrease in loop pressure and aconverter results in a decrease in loop pressure and a
lower circulation rate, which gives savings on thelower circulation rate, which gives savings on the
synthesis gas compressor and the refrigerationsynthesis gas compressor and the refrigeration
compressor.compressor.
Energy saving: 0.18 Gcal/MT NH3Energy saving: 0.18 Gcal/MT NH3
65. Advantages of addition of S-50 LoopAdvantages of addition of S-50 Loop
Ammonia concentration at the outlet of S-50 =Ammonia concentration at the outlet of S-50 =
24.35% as compared to 20.02% in S-20024.35% as compared to 20.02% in S-200
Higher conversion 35.5 % as compared to 28.3% in S-200Higher conversion 35.5 % as compared to 28.3% in S-200
Lower circulation rate as compared to S-200 for sameLower circulation rate as compared to S-200 for same
loadload
Higher steam generation 82 T/hr as compared to 70 T/hr in S-Higher steam generation 82 T/hr as compared to 70 T/hr in S-
200200
Lower synthesis loop pressureLower synthesis loop pressure
Lower compressor power due to less circulation and lowLower compressor power due to less circulation and low
pressurepressure
Possible to achieve higher plant load with same equipmentsPossible to achieve higher plant load with same equipments
68. Parallel Air compressorParallel Air compressor
Addition of Parallel air compressorAddition of Parallel air compressor
(reciprocating type) to meet the additional(reciprocating type) to meet the additional
process air requirementprocess air requirement
Process air from Existing PAC: 59152Process air from Existing PAC: 59152
Nm3/hrNm3/hr
Process air from New Compressor: 6030Process air from New Compressor: 6030
Nm3/hrNm3/hr
Total air requirement for 1750 MTPDTotal air requirement for 1750 MTPD
ammonia as per PFD: 65181 Nm3/hrammonia as per PFD: 65181 Nm3/hr
69. Ammonia-II CEP: Process airAmmonia-II CEP: Process air
As per PFD of Ammonia-II CEP, the totalAs per PFD of Ammonia-II CEP, the total
requirement of process air from PAC ofrequirement of process air from PAC of
Ammonia-II shall be 75683 Nm3/hr withAmmonia-II shall be 75683 Nm3/hr with
distribution as follows:distribution as follows:
Process air for Ammonia-II CEP : 69234Process air for Ammonia-II CEP : 69234
Nm3/hrNm3/hr
Instrument air : 3924 Nm3/hrInstrument air : 3924 Nm3/hr
Export to Ammonia-I : 2525 Nm3/hrExport to Ammonia-I : 2525 Nm3/hr
6969
70. Ammonia-II CEP: HTAS report & OEM reviewAmmonia-II CEP: HTAS report & OEM review
The capacity of existing PAC in Ammonia-II is : Normal:The capacity of existing PAC in Ammonia-II is : Normal:
59275 Nm³/h , Rated : 64900 Nm³/h59275 Nm³/h , Rated : 64900 Nm³/h
Based on overall performance curve of PAC, HTAS hasBased on overall performance curve of PAC, HTAS has
confirmed that the desired load shall remain within theconfirmed that the desired load shall remain within the
operating range of the compressor.operating range of the compressor.
OEM of PAC of Ammonia-II has confirmed that it shouldOEM of PAC of Ammonia-II has confirmed that it should
be possible to operate the machine with 75372 Nm³/hbe possible to operate the machine with 75372 Nm³/h
without modifications.without modifications.
It was practically observed that the machine is in positionIt was practically observed that the machine is in position
to deliver the desired load with no limitation on driverto deliver the desired load with no limitation on driver
side.side.
7070
71. LINE1 AND LINE2 DIFFERENCELINE1 AND LINE2 DIFFERENCE
LINE 1 DOES NOT HAVE MIXED FEEDLINE 1 DOES NOT HAVE MIXED FEED
CAPABILITY ONLY NG CAN BE USEDCAPABILITY ONLY NG CAN BE USED
AS FEEDAS FEED
IN LINE1 AIR COMP IS RUN BY STEAMIN LINE1 AIR COMP IS RUN BY STEAM
TURBINE IN LINE 2 GT IS USED FORTURBINE IN LINE 2 GT IS USED FOR
RUNNING AIR COMPRUNNING AIR COMP
72. LINE1 AND LINE2 DIFFERENCELINE1 AND LINE2 DIFFERENCE
IN LINE 1 STRIPPING OF CONDENSATEIN LINE 1 STRIPPING OF CONDENSATE
IS DONE BY LOW PREESURE STEAMIS DONE BY LOW PREESURE STEAM
AND ALL THE STEAM IS VENTED TOAND ALL THE STEAM IS VENTED TO
ATMOSPHEREATMOSPHERE
IN LINE 2 STRIIPING IS DONE BY MPIN LINE 2 STRIIPING IS DONE BY MP
STEAM AND STEAM IS REUSED INSTEAM AND STEAM IS REUSED IN
REFORMER THUS SAVING THE ENERGYREFORMER THUS SAVING THE ENERGY
73. LINE1 AND LINE2 DIFFERENCELINE1 AND LINE2 DIFFERENCE
IN LINE 1 BENFIELD PROCESS IS USEDIN LINE 1 BENFIELD PROCESS IS USED
FOR CO2 STRIPPINGFOR CO2 STRIPPING
IN LINE 2 GV PROCESS IS USED FORIN LINE 2 GV PROCESS IS USED FOR
CO2 REMOVALCO2 REMOVAL
LINE 1 DOES NOT HAVE PRELINE 1 DOES NOT HAVE PRE
REFORMERREFORMER
74. LINE1 AND LINE2 DIFFERENCELINE1 AND LINE2 DIFFERENCE
IN LINE 1 BENFIELD PROCESS IS USEDIN LINE 1 BENFIELD PROCESS IS USED
FOR CO2 STRIPPINGFOR CO2 STRIPPING
IN LINE 2 GV PROCESS IS USED FORIN LINE 2 GV PROCESS IS USED FOR
CO2 REMOVALCO2 REMOVAL
LINE 1 DOES NOT HAVE PRELINE 1 DOES NOT HAVE PRE
REFORMERREFORMER