1.0 GASIFICATION _Gasifiers_ Gas Cooling_ Rectisol_ Gas Liquor

Document Sample
1.0 GASIFICATION _Gasifiers_ Gas Cooling_ Rectisol_ Gas Liquor Powered By Docstoc
					TRI-STATE S Y N F U E ~   COMPANY                              F L U O R ENGINESRS A N D CONSTRUCTORS, I N ~
I~irec't C ~   Liq~facdon P1~¢                                                                Con~ac¢ 83S5~
WestlCn K ~ y
                                  1.0   GASIFICATION
                    (Gasifiers, Gas Cooling, Rectisol, Gas Liquor
                    Separation, Phenosolvan, Ammonia Recovery, POX)


        1.1        PROCESS DESCRIPTIONS


        I.!.!         Unit l0 - Lurgi Gasification


        This Unit consists of 12 parallel Lurgi gasifiers, 9 operat-
        ing and 3 spare, to gasify sized coal (2-1/2" x I/4").    A
        flow sheet illustrating general configuration is included in
        Section 1.2. Material balances are given in Section 1.3.

        The Lurgi gasifier is a moving bed reactor in which coal
        moves downward under gravity countercurrent to the upward
        flowing gasification agent, a mixture of superheated steam
        and 98.5 percent pure oxygen.   The coal bed is supported by
        a revolving grate through which superheated steam and oxygen
        are added and ash is removed.   The gasifier is operated at a
        pressure of about 450 psia.   The gasifier is jacketed with
        about I0 percent of the feed stea~ for the gasification
        agent being generated in the jacket.

        Coal feeding is done on a batch mode of operation.       The
        sized coal required in the Lurgi gasifiers is transported by
        conveyor belts from the coal preparation buil.ding to the
        coal bunkers located on top of the gasifiers.     Coal from the
        coal bunker is charged into the gasifier via a lock hopper
        arrangement.   Coal is fed to the lock hopper by first
        depressurizing the hopper and then filling the unit w i t h
        coal.  The gas released during depressurization is utilized
        in the plant as a fuel gas.     Any residual gas left in coal
        lock after depressurization is removed by eductors and
        vented to the atmosphere.   Depressurization of the coal lock
        is followed by the opening of the coal feed valve at the top
        of the lock hopper.    After filling the lock hopper with
        coal, the top valve is closed, and the lock hopper is
        pressurized with raw gas to a pressure equal to that inside
        the gasifier.   Next, the b o t t o m valve on the coal lock
        hopper is opened and the coal is introduced into the gasi-
        iier.   h~en the coal lock hopper is empty, the refilling
        procedure is repeated.

        The coal passes slowly through the gasifier, continuously
        changing chemical composition as it goes through four
        distinct zones.  From top to bottom, these zones are: coal
        preheat and devolatilization, gasification, combustion, and
        ash zones.  Coal is fed in the top section of the reactor
        countercurrent to the upward flowing gas stream which dries
        and devolatizes the coal in the top zone.  Devolatilization
        of coal is followed by gasification of the resulting char at


               USE OR DISCLOSURE OF REPORT DATA IS SUBJECT TO THE RESTRICTION ON THE NOTICE PAGE
                                         AT THE FRONT OF THIS REPORT
                                                                                  II
                                                                                  I
        T R I S T A T E S Y N F U E ~ COMPAN~                             FLUOR ENGINEERS AND CONSTRUCTORS, I N ~
        i ~ i m c t Coal I.~lum~'d~ ~ant                                                           Contact 835804
        Wesurn Km~ucky
    .
                i.I.I         Unit     I0 - L u r ~ i    Gasification           (Continued)

               t e m p e r a t u r e s r a n g i n g from 1150°F to 1600"F.                  Chemical
               r e a c t i o n s t h a t o c c u r in the g a s i f i e r are d e s c r i b e d below:

                I)      The g a s i f i c a t i o n     of   the   carbon      takes      place      by   the
                        reaction:

                         C + H20        (steam)       + Heat                   ~   CO + H 2

                2)       H y d r o g e n is p r o d u c e d by the "water gas reaction";

                         CO + H=O                        •   CO 2 + H 2 + H e a t

                3)       Some c a r b o n also          reacts     with    carbon       dioxide      to   form
                         carbon monoxide:

                         C ÷ CO 2 + H e a t                    L   2 CO

                4)       Methane       is p r o d u c e d by the h y d r o g a s i f i c a t i o n   reaction:

                         C + 2H~                .        •   CH~ + Heat

                5)       The net h e a t input for the above r e a c t i o n s is s u p p l i e d
                         by the c o m b u s t i o n of c a r b o n w i t h o x y g e n in the c o m b u s -
                         tion zone.
!


                         C + O~ . . . . . .           CO~ ÷ Heat
                                                                                                                        i

                O x y g e n and steam enter as a m i x t u r e n e a r the b o t t o m of the                           i
                g a s i f i e r and the m i x t u r e p a s s e s u p w a r d t h r o u g h the ash zone
                                                                                                                            ]
                to the c o m b u s t i o n zone.      The steam to o x y g e n ratio, d i c t a t e d                       !
                by the coal c o m p o s i t i o n , d e t e r m i n e s the t e m p e r a t u r e in the
                c o m b u s t i o n zone.  The t e m p e r a t u r e m u s t be ,maintained b e l o w                       t
                                                                                                                            +
                the ash m e l t i n g p o i n t but h i g h e n o u g h to ensure the g a s i f i -
                c a t i o n of the coal.                                                                                    t

                 The raw gas l e a v i n g the g a s i f i e r w i l l be at a t e m p e r a t u r e of
                 a b o u t 1000°F and a p r e s s u r e of about 45C p s i a                   The raw gas
                                                                                                                            !
                 is q u e n c h e d by d i r e c t c o n t a c t in a w a s h cooler w h e r e it is                            i
                                                                                                                                i

                 r a p i d l y cooled.         The q u e n c h e d gas if f u r t h e r c o o l e d in w a s t e                !
                 h e a t b o i l e r s by h e a t e x c h a n g e w i t h b o i l e r feed w a t e r thus
                 r e c o v e r i n g w a s t e h e a t as steam.       The gas is then fed to the                                   I
                 Gas C o o l i n g U n i t for further c o o l i n g a n d h e a t recovery..               As
                 the raw gas is cooled, water, tars and oils, and e n t r a i n e d
                 coal fines c o n d e n s e and are r o u t e d to the Gas Liquor S e p a r a -
                 tion U n i t for f u r t h e r processing.

                 A s h r e m o v a l is a c c o m p l i s h e d on a b a t c h m o d e of o p e r a t i o n
                 t h r o u g h a lock h o p p e r a r r a n g e m e n t s i m i l a r to the coal feed
                 operation.             The ash is r e m o v e d by a r o t a t i n g grate and
C                d i s c h a r g e d v i a a s e m i - a u t o m a t i c a l l y o p e r a t i n g ash lock w h i c h
                 is p r e s s u r i z e d w i t h s u p e r h e a t e d steam.           The o p e r a t i o n


                     USE OR DISCLOSURE OF REPoI~r DATA IS SUilJECT TO THE RESTRICTION ON THE NOTICE FAGE
                                                AT THE FRONT OF THIS REPOR-
         T R I S T A T E $ Y N F U E ~ COMPANY                           F L U O R ENGINEERS A N D C O N S T R U C T O R ~ I N ~
         I~irec~ ~        LiQ~fac~on ~                                                                      Conlxac¢ 8 3 5 5 ~
         Westc,cn K~Cucky
                I.I.I         Unit      l0., Lurgi G a s i f i c a t i o n     (Continued)

                closely parallels the o p e r a t i o n of a coal lock.                       The ash
                leaving the ash lock drops into a s l u i c e w a y to be carried to
                the ash dewatering plant.                        Any steam p r o d u c e d b y the
                q u e n c h i n g of the hot ash is routed t h r o u g h a w e t cyclone
                separater for p a r t i c u l a t e and condensate removal and any
                n o n - c o n d e n s a b l e s are v e n t e d to the atmosphere.


                1.1.2         Unit      II - Gas C o o l i n ~

                The raw gas leaving the g a s i f i c a t i o n unit is further cooled
                in the Gas Cooling Unit. The Gas C o o l i n g Unit consists of
                two p a r a l l e l trains.      The gas is first c o o l e d in a t e m p e r e d
                w a t e r system to about 305°F and then in air coolers to about
                130°F.           Final cooling to about 95°F is a c c o m p l i s h e d by w a t e r
                cooling.             The cooled gas is then fed to the R e c t i s o l Gas
                P u r i f i c a t i o n Unit.

                Tarry gas liquor and oily gas liquor are s e p a r a t e d from the
                gas stream during the c o o l i n g process. The gas liquor
                streams are sent to the Gas Liquor S e p a r a t i o n U n i t for
                further processing.


                 1.1.3         Uni~     12 - Rectisol

                The raw gas leaving the Gas Cooling Unit is fed to the
                Rectisol Unit to remove sulfur compounds and COa from the
                gas s~ream.  The R e c t i s o l Unit w h i c h consists of two paral-
                lel trains, utilizes cold m e t h a n o l to p u r i f y the gas.

                First, the gas in the u n i t is w a s h e d w i t h m e d i u m - c o l d
                m e t h a n o l to remove gas n a p h t h a components, i.e., pentanes,
                hexanes, benzene, toluene,                and h e a v i e r aromatics.              The
                prewash m e t h a n o l stream is then flashed to release d i s s o l v e d
                gases and naphtha.            This r e c o v e r e d n a p h t h a is m i x e d w i t h the
                t~r and oil recovered in the Gas L i q u o r S e p a r a t i o n Unit for
                g a s i f i c a t i o n in POX (partial oxidation)                gasifiers.         The
                flashed gases are routed to the Sulfur R e c o v e r y Unit.

                The p r e w a s h e d gas exiting the p r e w a s h c o l u m n is routed to
                the main w a s h column w h e r e the b u l k of the H2S and CO~ are
                removed by w a s h i n g w i t h v e r y cold methanol.        A f t e r the m a i n
                wash col~mn, the gas is finally w a s h e d in the fine w a s h
                column w h e r e the H2S c o n t e n t of the gas is r e d u c e d to less
                than 0.i ppmV.




    b-


                     USE OR DISCLOSURE OF REPORT DATA IS SUBJECT TO THE RESTRICTION ON THE NOTICE PAGE
                                               AT THE FRONT OF THIS REPORT

|
    TRI-,~rATE SYNFUELS COMPANY                                 F L U O R ENGINEERS A N D CONSTRUCTORS, INC.
                                                                                               C o m n m 83SS04
    Indir~.:~
            ~   l.iqud~-tion l~m~t
    W~m':~ Kemz~Icy

(         1. i. 3      Unit     12 - R e c t i s o l   (Continued)

          L o a d e d m e t h a n o l from the m a i n and fine w a s h systems is
          r e g e n e r a t e d by flashing in several s~ages.            Part of the
          flashed m e t h a n o l is hot r e g e n e r a t e d by steam stripping the
          H=S and sulfur compounds for use in the fine w a s h section.
          Flashed gas from the first stage is r e c y c l e d for recovery of
          CO, H 2, and CH ~.             Gas from subsequent flashes and hot
          r e g e n e r a t o r off gas, containing HzS and CO 2 are sent to the
          Sulfur R e c o v e r y Unit for R2S removal.            Gas c o n d e n s a t e from
          the Rectisol Unit is routed to the Gas L i q u o r Separation
          Unit.


           1.1.4       Unit     13 - Gas L i q u o r   Separation

          The Gas Liquor Separation Unit which c o n s i s t s of one train,
          processes the various gas liquor streams p r o d u c e d in the
          cool down of the raw gas.               These gas liquor streams contain
          dissolved gases such as crude gas components, ammonia, and
          h y d r o c y a n i c acid, as w e l l as tar, oil, phenols, chlorine,
          fluorine, fatty acids, and some amounts of coal and ash
          dust.

           The gaseous components are separated by flashing to atmo-
           spheric pressure.  The liquids (aqueous and non-aqueous) and
/          solid components are s e p a r a t e d by gravity separation.
\
           The Gas Liquor fed to this unit is cooled and d e p r e s s u r i z e d
           using control valves and a specially d e s i g n e d e x p a n s i o n
           drum.  The r e l e a s e d gases are routed to the Sulfur Recovery_
           Unit for H:S removal.

           Gas liquor then flows into the primary separators w h e r e the
           h e a v y c o m p o n e n t tar is separated. P r e s e n t in this tar is a
           small amount of coal dust carried over in the gasifier.                   Tar
           c o n t a i n i n g the b u l k of this dust settles to the b o t t o m of
           the conical separator, and there it is p u m p e d b a c k into the
           top of the gasifier.

           Gas liquor and oil with some tar flows from the top of the
           p r i m a r y separator into the secondary separator.     Oil is
           d r a w n from the top of the secondary separator, w a t e r from
           the middle, and a small q u a n t i t y of tar is drawn p e r i o d i c -
           ally from the bottom.

           The gas liquor flowing out of the secondary separators flows
           into t e r t i a r y separators for the separation of light oils
           and tars still present.            The aqueous phase then goes into
           the P h e n o s o l v a n Unit for additional processing.  The oils
           and tars separated are sent to POX Unit for g a s i f y i n g to
           synthesis gas.
6
                USE OR DISCLOSURE OF REPORT DATA IS SUBJECT TO THE RESTRICTION ON THE NOTICIE PAGE
                                          ATTHE FRONT OF THiS REPORT
T R I - S T A T E SYN FUELS COMPANY                           F L U O R ENGINEERS A N D CONSTRUCTORS, INC.
Indirect Coal LiQuef-ac~on Plane                                                             Conxrac~ 835504
Wer~rn Kent~ckv
       I. 1.5       Unit     16 - P h e n o s o l v a n

      The   Phenosolvan Unit, consisting of one train p r o c e s s e s the
       gas liquor from the Gas Liquor S e p a r a t i o n Unit to recover
       phenols.   A storage tank to a c c o m m o d a t e gas liquor p r o d u c -
       tion for 14 days is installed at the inlet of this unit.
       The liquor storage is p r o v i d e d so m a i n t e n a n c e w o r k on the
       unit can be p e r f o r m e d w i t h o u t s h u t t i n g down the entire
       facility.    The unit, licensed by Lurgi, consists of three
       main parts:    filtration, extraction, and solvent recovery.

       Gas liquor from the Gas Liquor S e p a r a t i o n Unit w i l l be
       filtered to remove any suspended particles.                        The liquor then
       enters a five stage c o u n t e r - c u r r e n t extractor, w h e r e p h e n o l s
       are e x t r a c t e d from the liquor by c o u n t e r - c u r r e n t contact
       with isopropyl e t h e r solvent.           The e x t r a c t c o n t a i n i n g the
       solvent and phenols is d i s t i l l e d to separate the solvent.
       The d i s t i l l e d solvent is recycled to the extractors.                       The
       solvent c o n t a i n e d in the p h e n o l after d i s t i l l a t i o n        is
       recovered by steam stripping and r e c y c l e d to a d i s t i l l a t i o n
       column.         The crude phenols are m i x e d w i t h tar, oil, and
       naphtha r e c o v e r e d from the L u r g i G a s i f i c a t i o n Process for
       charging into the POX gasifiers to p r o d u c e synthesis gas.
       The d e p h e n e l i z e d gas liquor is next s t r i p p e d w i t h Na in a
       stripping column to remove the r e s i d u a l isopropyl ether
       solvent dissolved in the liquor.                 The N2/ isopropyl ether is
       w a s h e d w i t h p h e n o l to recover the so~vent for recycle.
       After N= stripping, the d e p h e n o l i z e d gas liquor is fed to
       the Ammonia Recovery Unit for r e c o v e r i n g ammonia.


       1.1.6         Unit ! 7 ~       Ammonia      Recovery

       The d e p h e n o l i z e d gas liquor is fed to the Cyam p r o c e s s to
       recover ammonia.                  This process is l i c e n s e d by U.S. Steel
       Corporation.             L i c e n s i n g agreements have not b e e n m a d e w i t h
       them.     The USS C y a m process recovers b o t h free and fixed
       ammonia from w a s t e water.                 The gas liquor stream is fed into
       a free ammonia st~ll w h e r e the free a m m o n i a and acid gases
       are r e c o v e r e d by live steam injection.               The liquid leaving
       the b o t t o m s of the free ammonia still are fed to a lime
       mixing vessel w h e r e a lime slurry is a d d e d to free the f i x e d
       ammonia.        The m i x t u r e from the lime slurry v e s s e l is fed to
       a fixed ammonia still to recover the r e m a i n i n g a m m o n i a u s i n g
       steam stripping.                 The ammonia v a p o r s leaving the top of the
       fixed a m m o n i a still are c o m b i n e d w i t h the vapor leaving the
       free ammonia still and fed to a P h o s a m - W a b s o r b e r for
       recovering ammonia.




            USE OR DISCLOSURE QF REPORT DATA IS SUBJECT TO THE RESTRICTION ON THE NOTICE PAGE
                                      ATTHE FRONT OF THIS REPORT
    TRI-,STATE $YNFUEI.S COMPANY                                  FLUOR ENGINEERS AND CONSTRUCTORS, INC.
    Indimc~ Cmd Licmefac~on Plant                                                          C o n m ~ 838804
    Vhnmm K m ~
          1.1.6       Unit         17 -   Ammonia   Recovery        {Continued)

         The fixed ammonia still b o t t o m s are cooled and fed to a
         clarifier.  The lime sludge from the clarifier is fed to a
         sludge filtration system to dewater the sludge, w h i c h is
         then sent to the landfill site for disposal.         The w a t e r
         removed from the clarifier and sludge filtration system is
         then sent to w a s t e w a t e r treatment.

          The c o ~ i n e d   a m m o n i a vapors from the free ammonia still and
          fixed ammonia still enter at the b o t t o m of the P h o s a m - w
          absorber, where an a m m o n i u m p h o s p h a t e solution removes the
          ammonia.         The vapors leaving the top of the ammonia a b s o r b e r
          contain less than 100 ppmv of NH 3.                 This stream is sent to
          the Sulfur Recovery Unit (Unit 18).                  The a m m o n i a is removed
          from the rich b o t t o m s solution by stripping ~ i t h h i g h
          p r e s s u r e steam in the P h o s a m - W stripper.

          Aqu_eous vapor c o n t a i n i n g 10 to 20 w e i g h t p e r c e n t ammonia
          e x i t i n g the top of the stripper is condensed and c o l l e c t e d
          in a f r a c t i o n a t o r feed tank.     This aqueous ammonia is p u m p e d
          from the f r a c t i o n a t o r feed tank into an ammonia f r a c t i o n a t o r
          column.        Pure ammonia w i t h at least 99.5 wt % of ~ n i a
          leaves the top of the fractionator and water c o n t a i n i n g less
          than i00 p p m by wt.               of ammonia leaves the bottom.        This
          w a t e r is c o m b i n e d w i t h the stripped gas liquor from the lime
          sludge c l a r i f i e r for waste w a t e r treating.


          1.1.7        Unit 82 - L.ur~i Liquids               POX G a s i f i c a t i o n

          Lurgi liquids are g a s i f i e d to make more synthesis gas in a
          p a r t i a l o x i d a t i o n unit.    The p a r t i a l o x i d a t i o n gasifier
          o p e r a t e s in the s l a g g i n g mode.    The liquids d e r i v e d from the
          Lurgi Coal G a s i f i c a t i o n process, i.e., tar, oils, naphtha,
          and p h e n o l s are fed to the g a s i f i e r burners along w i t h steam
          and o x y g e n and u n d e r g o partial o x i d a t i o n r e s u l t i n g in r.he pro-
          d u c t i o n of m e d i u m Btu gas.      The g a s i f i c a t i o n t e m p e r a t u r e m u s t
          be s u f f i c i e n t l y a b o v e the ash flow p o i n t to e n s u r e free flow-
          ing m o l t e n slag w h i c h falls into the water q u e n c h chamber at
          the b o t t o m of the gasifier.            The m o l t e n slag is c o l l e c t e d in
          a lock hopper and p e r i o d i c a l l y discharged.

          The hot crude gas leaving the ga_~ifier p a s s e s t h r o u g h a
          radiant type w a s t e h e a t b o i l e r g e n e r a t i n g 600 psig s a t u r a t e d
          steam, and then is scrubbed w i t h w a t e r to remove p a r t i c u -
          lates from the gas stream.                        F o l l o w i n g the s c r u b b i n g opera-
          tion, the remaining w a s t e heat of the                           gas is r e c o v e r e d in a
          w a s t e h e a t b o i l e r g e n e r a t i n g 60 psig steam.            The gas is then
          c o o l e d to about 100°F in w a t e r cooled shell and tube heat
          exchangers.


w




                       °




                  OR D I S C ~ E     OF REPORT DATA I$ SUBJECTTO THE RESTRICTIONON THE NOTICE PAGE
                                             ATTHE FRONT OF THIS REPORT
                                                                                                                 L
TRI-STATE SYNFUELS COMPANY                                 FLUOR ENGINEERS A N D CONSTRUCTORS, I N C .
Indirect Coal ticluefac'tlon Plans                                                    Co nu-a~ 835504
Western Kentucky


i. 2     FLOW SHEETS

         F l o w sheets for the G a s i f i c a t i o n area are p r o p r i e t a r y w i t h
         the l i c e n s o r s involved.      D e t a i l s of the p r o c e s s e s c a n n o t
         be r e v e a l e d until a l i c e n s i n g a g r e e m e n t is signed.




          USE OR DISCLOSURE CF REPORT DATA IS SUBJECT TO THE RESTRICTION ON THE NOTICE PAGE
                                    ,~TTHE FRONT OF THIS REPORT

              u                IImEI
                                     imml
T R I S T A T E SYNFUELS COMPANY                              FLUGR ENGINEERS A N D C o N I r r R ~      INC.
indirect Coal Liquefaction Plant
                                                                                                c~n~m
Wesmm Kentucky


1.3      UNIT M A T E R I A L B A L A N C E S

         S t r e a m c o m p o s i t i o n s for the G a s i f i c a t i o n area are p r o p r i e t a r y
         w i t h the l i c e n s o r s involved.         D e t a i l s of the p r o c e s s e s c a n n o t
         be r e v e a l e d until a l i c e n s i n g a g r e e m e n t is signed.




            USE OR DISCLOSURE OF REPORT DATA IS $1JBjLr~"TTO THE RESTRICTION ON THE NOTICE PAGE
                                      AT ~   FRONT OF THIS REPORT


                    l                                                  I
TRI-STATE SYNFUELS COMPANY                             FLUOR ENGINEERS A N D CONSTRUCTORS, INC.
Indirect Coal Liquefaction Plan~                                                  Contract 835504
         Kent'ucky

       1.4      ACCOMPLISHMENTS        AND DECISIONS

       The current plant d e s i g n uses the results of our p r o c e s s
       alternative study Case 13 (See Volume X).                            This is a pre-
       liminary process d e s i g n that uses data s u p p l i e d by Lurgi for
       g a s i f i c a t i o n and R e c t i s o l yields.   No other licensor designs
       are i n c o r p o r a t e d into the work.          M T G y i e l d s are b a s e d on
       data available in the literature.


       1.5      CURRENT     STATUS

       A process design has been e s t a b l i s h e d on a p r e l i m i n a r y
       basis.   The p r e l i m i n a r y design data on Coal G a s i f i c a t i o n
       Units was furnished by Lurgi b a s e d on data o b t a i n e d d u r i n g
       test runs w i t h K e n t u c k y No. 9 coal at the Sasol plant.

       Mark IV gasifiers, fitted w i t h coal d i s t r i b u t o r s and stir-
       ring devices, will be used to gasify K e n t u c k y No. 9 coal.
       The special stirring device is added to the standard M a r k IV
       gasifier.    The design gas y i e l d per Lurgi m a r k IV g a s i f i e r
       has been e s t a b l i s h e d by Lurgi b a s e d on test results at
       SASOL.    For the design Case 13, the total number of gasi-
       fiers is twelve, w h i c h includes s u f f i c i e n t spare g a s i f i c a -
       tion capacity to ensure desired raw gas d e s i g n output con-
       sistent with a n t i c i p a t e d gasifier m a i n t e n a n c e downtime.

       The gasifiers will operate w i t h a s t e a m / o x y g e n                ratio of
       7.2 kg steam/Nm a of 0 2 for the specified coal.                            The d e s i g n
       s t e a m / o x y g e n ratio will be 7.4.

       A d e c i s i o n has been m a d e to u t i l i z e coal lock gas as a fuel
       gas in the plant.          A process o p t i m i z a t i o n study has shown
       that the recycle of lock gas to the R e c t i s o l Unit is
       uneconomic.

       The coal Gasification,          Gas Cooling, Rectisol, Gas L i q u o r
       Separation, and P h e n o s o l v a n Units w i l l be l i c e n s e d by Lurgi.

       The liquids o b t a i n e d from the g a s i f i c a t i o n process, i.e.,
       tars, oils, phenols, and naphtha w i l l all be c o m b i n e d and
       g a s i f i e d in a T e x a c o Partial O x i d a t i o n U n i t to p r o d u c e more
       gas.        This route w a s found to b e the m o s t e c o n o m i c a l one for
       d i s p o s i t i o n of these liqu~.ds.

       For the A m m o n i a R e c o v e r y Unit,   the C y a m p r o c e s s ,   licensed      by
       U.S. Steel, has been selected.




              OR DISCLOSURE OF REPORT DATA iS SUBJECT TO THE RESTRICTION ONTHE NOTICE PAGE
                                    AT THE FRONT OF THIS REPORT
emm~m.--...___.__   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .   .




                        TRISTATE SYNFUE;.,S COMPANY                                                                                                        FLUOR ENGINEERS AND (=ONSTRUCI"ORL INC.
                        mnclirentCoal I.;quefacdon Plant                                                                                                                             Ccmtrmt 113S604
                        Weswm Kentucky

    (                                       1.6                     LZCENSORS

                                            For the synthesis gas p r o d u c t i o n units, Lurgi has been
                                                                                                                    AND E V A L U A T I O N S


                                            selected as the licensor.         L i c e n s i n g a r r a n g e m e n t s have been
                                            made b e t w e e n Lurgi and Tri-State.             Lurgi will provide
                                            licensor p a c k a g e s for the following units:

                                                                NO.                                                                         Description

                                                                    10                                                                      Coal G a s i f i c a t i o n

                                                                    II                                                                      Gas Cooling

                                                                    12                                                                      Rectisol

                                                                    13                                                                      Gas Liquor         Separation

                                                                    16                                                                      Phenosolvan

                                            In addition, Lurgi will p e r f o r m                                                                     the d e t a i l e d   engineering   for
                                            units 10 and 13.

                                            Lurgi has t e n t a t i v e l y b e e n selected as the licensor for the
                                            Methanol Synthesis Unit; however, the licensing agreement
                                            negotiations for this u n i t are not completed.

                                            For the Lurgi Liquids Partial O x i d a t i o n Unit, Texaco was
                                            tentatively              selected       as   the   licensor.          Licensor
                                            n e g o t i a t i o n s b e t w e e n Texaco and Tri-State have not b e e n
                                            started.             The results of the p r o c e s s o p t i m i z a t i o n studies
                                            indicated that the most v i a b l e d i s p o s i t i o n for Lurgi liquids
                                            was to gasify t h e m to make more synthesis gas.                             Several
                                            licensors offer a partial o x i d a t i o n process to gasify
                                            h y d r o c a r b o n liquids.         Texaco and Shell Oil b o t h offer this
                                            process.              The Shell Unit is d e s i g n e d to h a n d l e clean
                                            solids-free liquids while Texaco's design can cope w i t h
                                            solids.            The Lurgi tar w i l l have a v a r y i n g q u a n t i t y of coal
                                            dust in the solution.                   For that reason Texaco was the choice
                                            for the POX Unit.

                                            The U.S. Steel C y a m p r o c e s s w a s selected for the A m m o : i a
                                            R e c o v e r y Unit.     A competing process licensed by Chemie Linz
                                            thru Lurgi was i n s t a l l e d at Sasol II and Sasol TIT.                       On the
                                            basis of the e c o n o m i c e v a l u a t i o n b e t w e e n these two p r o c e s s e s
                                            p e r f o r m e d for the W E S C O project, T r i - S t a ~ e has e l e c t e d to
                                            use the U.S. Steel process.                   Texas Eastern, a p a r t n e r in the
                                            T r i - S t a t e Synfuels Company, was a p a r t n e r in the W E S C O
                                            p r o j e c t and had access to the W E S C O study.                  The C y a m p r o c e s s
                                            was selected.            This p r o c e s s is a v a r i a t i o n of U.S. Steel's
                                            P h o s a m - W process.      Cyam w i l l release all of the fixed
                                            ammonia in the gas liquor.                   This p r e v e n t s h a v i n g a p r o b l e m
                                            w i t h n i t r o g e n in the b i o l o g i c a l t r e a t m e n t of the stripped
      C                                     gas liquor.



                                                        USE OR DISCLOSURE OF P.EPORT DATA IS SUIIJECT TO THE RESTIR.IC'rlON ON TIlE NOTICE PAGE
                                                                                   ATTHE FRONT OF THIS REPOIqT

				
DOCUMENT INFO
Shared By:
Categories:
Tags:
Stats:
views:10
posted:9/14/2011
language:English
pages:10