Production of Distillate Fuels by SRC-II - ACS Publications

4 Production of Distillate Fuels by SRC-II D. M. JACKSON and Β. K. SCHMID Downloaded via TUFTS UNIV on July 10, 2018 at 07:56:01 (UTC). See https://pubs.acs.org/sharingguidelines for options on how to legitimately share published articles.

Gulf Mineral Resources Company, 1720 So. Belaire, Denver, CO 80222

The SRC-II process technology for the production of low -sulfur distillates and light hydrocarbons from coal has been tested and evaluated in laboratory and pilot plant experiments on a variety of high-sulfur coals. Its development has successfully evolved to the point where large scale demonstration of the process and required equipment can be considered. Gulf, through its Pittsburg & Midway Coal Mining Co. Subsidiary, is completing, under contract to the Department of Energy, a preliminary evalua tion of engineering design, site, and market and economic assess ment of an SRC-II demonstration plant. The facility will be located on a site suitable for a subsequent commercial facility near Morgantown, West Virginia. The feed coal for the demonstra tion plant will be a typical high-sulfur Pittsburgh seam coal from West Virginia. The plant will yield significant quantities of coal liquids, gas and other products for extensive longer term testing in boilers, turbines and other applications. The objectives of the demonstration program are: 1.

To verify the technical feasibility of the SRC-II process in full-size equipment and establish a design basis for future plants.

2.

To i n t e g r a t e v a r i o u s supporting processes such as h i g h pressure g a s i f i c a t i o n i n t o an o v e r a l l c o a l l i q u e f a c t i o n process.

3.

To make p r o d u c t i o n q u a n t i t i e s o f l o w - s u l f u r f u e l o i l , gaseous hydrocarbons and chemical by-products f o r longer term t e s t i n g .

0-8412-0516-7/79/47-110-055$05.00/0 © 1979 American Chemical Society

Pelofsky; Coal Conversion Technology ACS Symposium Series; American Chemical Society: Washington, DC, 1979.

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4.

To develop a p p r o p r i a t e systems and equipment f o r c o n t r o l l i n g any environmental, h e a l t h , and s a f e t y f a c t o r s that may be unique to l a r g e s c a l e c o a l l i q u e f a c t i o n p l a n t s and t h e i r products.

5.

To provide a f i r m b a s i s f o r e s t i m a t i n g c a p i t a l and o p e r a t i n g c o s t s r e q u i r e d f o r a commercial c o a l r e f i n e r y u t i l i z i n g the SRC-II process.

PROCESS DESCRIPTION Flow Scheme Figure 1 presents a schematic f l o w diagram of the process i n a f u l l - s c a l e p l a n t as has been g e n e r a l l y described i n e a r l i e r p u b l i c a t i o n s (_1,_2 ,_3). The feed c o a l i s i n i t i a l l y d r i e d to about 5 percent moisture and p u l v e r i z e d , then mixed w i t h r e c y c l e s l u r r y from the process. The r e s u l t i n g c o a l - s l u r r y mixture i s pumped, together w i t h hydrogen, through a f i r e d preheater to a r e a c t o r at e l e v a t e d temperature and pressure. I n the r e a c t i o n system the c o a l i s not o n l y d i s s o l v e d , but i s a l s o l a r g e l y hydrocracked to d i s t i l l a t e f u e l o i l , naphtha and l i g h t hydrocarbons. The r e a c t o r e f f l u e n t then flows through a s e r i e s of vaporl i q u i d s e p a r a t o r s , where i t i s separated i n t o process gas, l i g h t hydrocarbon l i q u i d and product s l u r r y . The gas, c o n s i s t i n g p r i m a r i l y of hydrogen and gaseous hydrocarbons, together w i t h minor amounts of H2S and CO2, f i r s t goes through an a c i d gas removal step f o r removal of the H2S and CO2. The t r e a t e d gas then goes to à cryogenic s e p a r a t i o n step f o r removal of the hydrocarbons. The p u r i f i e d hydrogen i s r e c y c l e d to the process, w h i l e the recovered hydrocarbons become by-products of the process. The C^ f r a c t i o n i s sent to a methanator to convert the remaining CO to methane. The other l i g h t hydrocarbons are f r a c t i o n a t e d to produce ethane, propane and a mixed butane stream. The l i g h t hydrocarbon l i q u i d goes to a f r a c t i o n a t o r where i t i s separated i n t o naphtha (C -350°F nominal b o i l i n g range) and a middle d i s t i l l a t e (350° 600°F b o i l i n g range). 5

The product s l u r r y i s s p l i t , w i t h one p o r t i o n being r e c y c l e d to the process f o r s l u r r y i n g w i t h the feed c o a l . The other port i o n of the product s l u r r y goes to a vacuum tower where a heavy d i s t i l l a t e i s removed overhead. The heavy d i s t i l l a t e , together w i t h middle d i s t i l l a t e from the f r a c t i o n a t i o n s t e p , makes up the t o t a l f u e l o i l product of the process. The r e s i d u e from the vacuum tower i s sent to a h i g h pressure s l a g g i n g g a s i f i e r f o r p r o d u c t i o n of s y n t h e s i s gas, A p o r t i o n of the s y n t h e s i s gas goes through s h i f t conversion and a c i d gas r e moval steps to produce pure hydrogen f o r the process. The



cm

SIIFT CONVERSION ANN PURIFICATION

IIIEI PIIVERIZE»

INERT

SLAG

Figure 1.

PURIFIED

SRC-II process

HYDROGEN

SRC-II PROCESS

PLANT

FIEL

•

IIL

NftUTIft

IITAIES

Φ

CAS

H»PMPUE

PIRIFICATION

58

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s y n t h e s i s gas i n excess of that r e q u i r e d f o r hydrogen p r o d u c t i o n i s passed through a separate a c i d gas removal step f o r removal of CO2 and H^S, then through a power recovery t u r b i n e , and i s f i n a l l y burned as p l a n t f u e l . Major Process Steps and Related Engineering Development The demonstration p l a n t i s expected to c o n f i r m the operab i l i t y and r e l i a b i l i t y of those process steps and c e r t a i n process equipment which have not yet been proven i n commercial s c a l e equipment i n the o p e r a t i n g environment of c o a l r e f i n i n g . C e r t a i n aspects of the engineering development of these areas are d i s cussed, as shown i n Table 1. TABLE I MAJOR SYSTEMS TO BE DEMONSTRATED S l u r r y M i x i n g and Pumping S l u r r y Preheater Dissolver Fractionation Heat Exchange Pressure Letdown Gasification Oxygen Compression

S l u r r y M i x i n g and Pumping The demonstration p l a n t w i l l u t i l i z e a s l u r r y mixing and pumping system which has appeared very promising i n t e s t s at the 50-ton per day p i l o t p l a n t at F t . Lewis, Washington. Coal i s i n i t i a l l y contacted w i t h the s l u r r y i n a s m a l l mixing v e s s e l to accomplish the i n i t i a l mixing r e q u i r e d f o r completely w e t t i n g the c o a l p a r t i c l e s . Most of the 5% moisture remaining i n the feed c o a l i s v a p o r i z e d i n the mixing tank. The r e s u l t i n g t h i c k s l u r r y i s then pumped to the main s l u r r y mixing v e s s e l where mixing i s completed. The mixing step i s complicated by the f a c t t h a t the c o a l - s l u r r y mixture forms a g e l , and the r a t e of formation of the gel i s s t r o n g l y independent upon temperature. The formation of the g e l g r e a t l y i n c r e a s e s the v i s c o s i t y of the mixture and makes


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mixing and pumping more d i f f i c u l t . Although the e f f e c t of the higher v i s c o s i t y can be at l e a s t p a r t i a l l y overcome by strong shear f o r c e s generated by a p p r o p r i a t e mixers and pumps, these e f f e c t s must be demonstrated i n l a r g e r equipment. S l u r r y Preheater S i m i l a r l y , the formation of the g e l and i t s c o m p l i c a t i n g e f f e c t upon the v i s c o s i t y of the three-phase s l u r r y mixture must be c a r e f u l l y managed i n the s l u r r y preheater. Measurements of pressure drop and heat t r a n s f e r i n the F t . Lewis p i l o t p l a n t have provided much v a l u a b l e i n f o r m a t i o n concerning the e f f e c t of v i s c o s i t y of the m i x t u r e s . For example, the observed pressure drop i s s i g n i f i c a n t l y lower than would be c a l c u l a t e d based on the v i s c o s i t y estimated from l a b o r a t o r y t e s t s t u d i e s . This appears to r e s u l t from the non-uniform t e m p e r a t u r e - v i s c o s i t y gradient over the c r o s s - s e c t i o n of the heater tube i n the r e g i o n where the g e l i s a s i g n i f i c a n t f a c t o r i n the v i s c o s i t y . A f t e r the g e l reaches i t s peak v i s c o s i t y , the v i s c o s i t y decreases r a p i d l y as s o l v a t i o n proceeds. Thus, the g e l nearest the hot w a l l i s probably i n a more advanced s t a t e of d e p o l y m e r i z a t i o n and the v i s c o s i t y of the f l u i d near the w a l l i s s i g n i f i c a n t l y lower f o r much of the l e n g t h of the preheater c o i l than the b u l k f l u i d v i s c o s i t y at the same c r o s s - s e c t i o n . Even w i t h the reduced pressure drop, however, the maximum p r a c t i c a l tube diameter i s l i m i t e d by heat t r a n s f e r , and t h i s r e q u i r e s t h a t m u l t i p l e tube passes be used and proven i n the demonstration p l a n t . Dissolvers The b a s i c d e s i g n f o r the d i s s o l v e r i s a v e r t i c a l pressure v e s s e l w i t h no i n t e r n a l s . Continuing s t u d i e s confirm that the r e a c t o r i s w e l l backmixed and that temperature should be reasonably uniform throughout the v e s s e l , even i n l a r g e r s c a l e equipment. The h i g h l y exothermic h y d r o c r a c k i n g r e a c t i o n s o c c u r r i n g i n the d i s s o l v e r make i t f e a s i b l e to feed the r e a c t a n t s at a temperature w e l l below that p r e v a i l i n g i n the d i s s o l v e r . The e f f e c t i v e ness of hydrogen quench i n c o n t r o l l i n g the r e a c t i o n temperature has been confirmed i n p i l o t p l a n t t e s t s and t h i s technique w i l l be employed i n the l a r g e r demonstration p l a n t v e s s e l . The hydrogen quench i s added at v a r i o u s p o i n t s i n the r e a c t o r and a s s i s t s i n m a i n t a i n i n g the backmixing as w e l l as s e r v i n g as a f i n e temperature c o n t r o l . Fractionation Continuing study of the f r a c t i o n a t i o n system f o r the SRC-II process, both i n p i l o t p l a n t and e n g i n e e r i n g work, has i n d i c a t e d that some m o d i f i c a t i o n t o the o r i g i n a l f r a c t i o n a t i o n system des i g n i s d e s i r a b l e . I n the o r i g i n a l d e s i g n the s l u r r y was passed


COAL

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through the f r a c t i o n a t o r , then to a vacuum tower. In the r e v i s e d d e s i g n , however, the s l u r r y bypasses the f r a c t i o n a t o r . Bypassing the f r a c t i o n a t o r has been made p o s s i b l e by more e x t e n s i v e f l a s h i n g of l i g h t e r l i q u i d from the s l u r r y , thereby e l i m i n a t i n g a d i f f i c u l t s o l i d s - h a n d l i n g problem i n the f r a c t i o n a t i o n step. The f r a c t i o n a tor handles e s s e n t i a l l y a l l of the d i s t i l l a t e l i q u i d s f l a s h e d d u r i n g pressure letdown of the s l u r r y , and separates the combined l i q u i d i n t o naphtha and middle d i s t i l l a t e . Heat Exchange The f i r s t v a p o r - l i q u i d separator f o l l o w i n g the d i s s o l v e r separates excess hydrogen and uncondensed hydrocarbons from the product s l u r r y . The vapor stream must then be cooled to condense normally l i q u i d hydrocarbons. This c o o l i n g i s c a r r i e d out i n a s e r i e s of c o o l i n g and v a p o r - l i q u i d s e p a r a t i o n s t e p s , the f i r s t of which i s a hot high-pressure heat exchanger. This exchanger r e q u i r e s c a r e f u l design because of the p r o b a b i l i t y that some s o l i d s c a r r y - o v e r may occur i n the f i r s t s e p a r a t o r , l e a d i n g to the presence of s o l i d s i n the exchanger. A major engineering e f f o r t was made to accomplish a design which should s a t i s f a c t o r i l y handle c o n c u r r e n t l y the problems of h i g h temperature, h i g h pressure, the presence of hydrogen and the presence of s o l i d s . Pressure Letdown The letdown of the hot s l u r r y to lower pressures i s a l s o of concern because of p o t e n t i a l e r o s i o n of letdown v a l v e s . The h i g h v e l o c i t y created by f l a s h i n g vapors, combined w i t h the presence of e r o s i v e s o l i d s , make t h i s an important c o n s i d e r a t i o n i n the mechanical design of the demonstration p l a n t . E x t e n s i v e s t u d i e s have been c a r r i e d out i n the 50 ton per day p i l o t p l a n t at F o r t Lewis, and s e v e r a l arrangements and type of v a l v e s have been t e s t e d . This experience has l e d to design of a three-stage l e t down system f o r the s l u r r y i n the demonstration p l a n t . T e s t i n g of promising v a l v e systems i s c o n t i n u i n g i n the p i l o t p l a n t . Oxygen Compression The design f o r the oxygen p l a n t i n c l u d e s l a r g e c e n t r i f u g a l compressors f o r r a i s i n g the oxygen pressure to the l e v e l r e q u i r e d f o r the g a s i f i c a t i o n step. C e n t r i f u g a l compressors have been s u c c e s s f u l l y operated i n commercial i n s t a l l a t i o n s at high pressure but now q u i t e as h i g h as the design pressure. A major engineering study, undertaken i n c o n s u l t a t i o n w i t h oxygen compressor manufact u r e r s , concludes that o p e r a t i o n at the higher pressure appears f e a s i b l e by the use of three casings of s e v e r a l stages each.


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High-Pressure G a s i f i c a t i o n High-pressure g a s i f i c a t i o n of the vacuum bottoms permits t h e r m a l l y - e f f i c i e n t p r o d u c t i o n of hydrogen from g a s i f y i n g the carbonaceous matter i n the m i n e r a l r e s i d u e , as w e l l as recovery of the i n o r g a n i c matter as a r e l a t i v e l y c l e a n i n e r t s l a g . High pressure o p e r a t i o n of the s l a g g i n g g a s i f i e r w i t h the h i g h s o l i d s content feed i s an important element i n the demonstration program. PRODUCTS Y i e l d s and A p p l i c a t i o n s Although the SRC-II process has been developed p r i m a r i l y f o r conversion of c o a l i n t o d i s t i l l a t e f u e l o i l s , a number of other l i g h t e r hydrocarbon products are a l s o obtained. The demonstration p l a n t would be designed t o produce p r i m a r i l y u t i l i t y f u e l s f o r d i r e c t use without f u r t h e r r e f i n i n g and t o permit product purchase support of the p r o j e c t by the u t i l i t y i n d u s t r y . A subsequent commercial f a c i l i t y , w h i l e s t i l l producing s i g n i f i c a n t q u a n t i t i e s of f u e l s f o r b o i l e r s and t u r b i n e s , o f f e r s the economies of s c a l e for recovery and upgrading (as a p p r o p r i a t e ) of l i g h t e r hydrocarbons, as w e l l as more s e l e c t i v e product a p p l i c a t i o n s based on d i s t i l l a t e product c h a r a c t e r i s t i c s and end-use requirements. A b r i e f o u t l i n e of the products expected i n a demonstration p l a n t and i n f u t u r e commercial p l a n t s i s shown i n F i g u r e 2. I n f u t u r e commercial p l a n t s , f o r example, ethane and propane could be u t i l i z e d as chemical i n t e r m e d i a t e s and naphtha as a source of chemicals or f o r p r o d u c t i o n of high-octane unleaded g a s o l i n e . Synthesis gas produced i n excess of the requirements f o r hydrogen could be u t i l i z e d as a source of chemicals as w e l l as a f u e l . The f u e l o i l could be s e l e c t i v e l y f r a c t i o n a t e d to produce a middle d i s t i l l a t e f o r use as t u r b i n e f u e l , l i g h t i n d u s t r i a l b o i l e r f u e l or r e f i n e r y f e e d s t o c k s , w h i l e the heavy d i s t i l l a t e could serve as a fuel o i l f o r large u t i l i t y boilers. The a n t i c i p a t e d product s l a t e from a t y p i c a l commercial p l a n t feeding 33,500 tons per stream day of dry c o a l i s given i n Table I I . This product s l a t e i s based on conversion of a t y p i c a l P i t t s b u r g h seam c o a l from West V i r g i n i a . The u l t i m a t e a n a l y s i s of the c o a l used as a design b a s i s i s given i n Table I I I .


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COAL CONVERSION TECHNOLOGY

SRC-II PRODUCT DEVELOPMENT DEMO P L A N - 1 9 8 0 S HIGH-SULFUR COAL 2.2 M M T / Y R

SRC-II MODULE DEMO

FUEL OIL

ELECTRIC UTILITIES

PIPELINE GAS, LPG

GAS UTILITIES

2 0 , 0 0 0 B/D EQUIVALENT

COMMERCIAL PLAN - 1 9 8 0 S HIGH-SULFUR BITUMINOUS COAL 11 M M T / Y R

SRC-II COMMERCIAL PLANT 100,000 B/D EQUIVALENT

METHANE

GAS UTILITIES

ETHANE, PROPANE

CHEMICAL INTERMEDIATES

CHEMICALS

SYNGAS

NAPHTHA

PETROLEUM REFINERY FEEDSTOCKS >>>»>}t}ff}W}t»»})WWftt/W»}W>>HM>f»>)77TrJ

Figure 2.

MIDDLE DISTILLATE

TURBINE F U E L S , I N D U S T R I A L BOILER FUELS

HEAVY DISTILLATE

E L E C T R I C UTILITY FUELS

SRC-II product development


JACKSON AND scHMiD

Distilfote Fuels

TABLE I I PRODUCTS FROM TYPICAL COMMERCIAL PLANT 33,500 T/SD-HIGH SULFUR BITUMINOUS COAL 120 MM SCF/D

METHANE ETHANE

1,100 T/D

PROPANE

12,000 B/D

BUTANES

8,000 B/D

NAPHTHA (C -350°F)

13,200 B/D

FUEL OIL (350-900°F)

57,500 B/D

5

SULFUR

800 T/D

AMMONIA

150 T/D

PHENOLS

35 T/D

TABLE I I I ANALYSIS OF FEED COAL HIGH SULFUR BITUMINOUS COAL - PITTSBURGH SEAM % BY WT. CARBON

71.0

HYDROGEN

5.0

NITROGEN

1.4

SULFUR, PYRITIC

1.6

SULFUR, ORGANIC

1.0

OXYGEN ASH MOISTURE

7.0 12.0 1.0 100.0


64


The major market f o r the product f u e l o i l f o r the demonstrat i o n p l a n t and near-term f u t u r e commercial p l a n t s i s expected to be e x i s t i n g power p l a n t s i n the c o a s t a l m e t r o p o l i t a n areas, where the p h y s i c a l and environmental c o s t s of conversion to c o a l make such a conversion i m p r a c t i c a l . A s i g n i f i c a n t c h a r a c t e r i s t i c of the SRC-II f u e l o i l f o r t h i s a p p l i c a t i o n i s i t s low s u l f u r content and thus the c a p a b i l i t y to meet s t r i n g e n t emission l i m i t s i n urban areas. Coal-derived r e s i d u a l f u e l s w i l l , i n g e n e r a l , not meet these requirements without stack gas cleanup. TABLE IV PROPERTIES OF TEST FUELS (Based on average a n a l y s i s of samples taken during t e s t program) No. 6 Fuel O i l Gravity:

°API

25.0

Viscosity: SUS at 100°F SUS at 122°F U l t i m a t e A n a l y s i s (Dry): % By Carbon Hydrogen Nitrogen Sulfur Oxygen Ash Heating Value: BTU/LB.

300-700

SRC-II Fuel O i l 11.0

40

Wt. 87.02 12.49 0.23 0.24 0.02 19.200

85.50 8.86 1.02 0.22 4.38 0.02 17.081

Table IV gives the p r o p e r t i e s of the SRC-II f u e l o i l compared to a l o w - s u l f u r r e s i d u a l o i l u t i l i z e d i n a recent combustion t e s t . The SRC-II f u e l o i l i s a d i s t i l l a t e product w i t h a nominal b o i l i n g range of 350-900°F, a v i s c o s i t y of 40 Saybolt seconds at 100°F and a pour p o i n t below -20°F. Thus, i t i s r e a d i l y pumpable at a l l temperatures normally encountered i n t r a n s p o r t a t i o n of the f u e l o i l . The f u e l o i l has a very low content of ash and sediment as w e l l as a low Conradson carbon r e s i d u e . These c h a r a c t e r i s t i c s are f a v o r a b l e from the standpoint of p a r t i c u l a t e emissions during combustion. Tests of c o m p a t i b i l i t y w i t h t y p i c a l petroleum f u e l o i l s and on s t a b i l i t y of the c o a l d i s t i l l a t e s over time have not revealed any unusual c h a r a c t e r i s t i c s t h a t would preclude u t i l i z a t i o n of these c o a l - d e r i v e d f u e l s i n c o n v e n t i o n a l b o i l e r applications.


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SCHMBD

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Combustion C h a r a c t e r i s t i c s The major question i n v o l v i n g burning c h a r a c t e r i s t i c s of c o a l l i q u i d s r e l a t e s to the higher n i t r o g e n content compared to p e t r o leum f u e l o i l s and the p o t e n t i a l e f f e c t on NO emissions. Since NO emissions are s e n s i t i v e to burning c o n d i t i o n s , however, a c t u a l burning t e s t s are r e q u i r e d under v a r i o u s c o n d i t i o n s to assess the effects. S e v e r a l burning t e s t programs have been c a r r i e d out to con f i r m t h a t the SRC-II f u e l o i l could be s u c c e s s f u l l y used i n con v e n t i o n a l power p l a n t s and that emission l e v e l s of p o t e n t i a l a t mospheric contaminants could be c o n t r o l l e d . The f i r s t burning t e s t f o r the l i q u i d f u e l o i l was conducted i n a 3 MM Btu per hour t e s t b o i l e r . The f u e l h a n d l i n g charac t e r i s t i c s of the o i l were a t t r a c t i v e . V i s c o s i t y was comparable to No. 2 f u e l o i l , thus no preheating was r e q u i r e d . The SRC f u e l o i l was used interchangeably w i t h No. 2 f u e l o i l without forming sediments. Cold b o i l e r l i g h t - o f f s were made without i n c i d e n t . Although the f u e l o i l has the r e l a t i v e l y h i g h organic n i t r o g e n content c h a r a c t e r i s t i c of c o a l - d e r i v e d l i q u i d s , each of s e v e r a l combustion c o n t r o l t e c h n o l o g i e s were e f f e c t i v e i n decreasing NO formation and smoke to environmentally acceptable l e v e l s . These combustion c o n t r o l methods i n c l u d e staged combustion, steam a t o m i z a t i o n , low-NO^ burner d e s i g n , and smoke i n h i b i t i n g a d d i t i v e s . In the f a l l of 1978 a f u l l - s c a l e t e s t program was pursued i n a commercial power p l a n t of the Consolidated Edison Company i n New York C i t y ( 4 ) . The t e s t was conducted i n three phases i n Con Edison's 74th s t r e e t s t a t i o n u t i l i z i n g a 450,000 l b / h r steam e l e c t r i c Combustion Engineering t a n g e n t i a l l y - f i r e d b o i l e r , as shown i n Table V. PHASE I - I n i t i a l B a s e l i n e T e s t i n g Work i n the f i r s t phase i n v o l v e d p r e l i m i n a r y checking of equipment and instruments f o r measuring emissions, as w e l l as establishment of Ν 0 r e d u c t i o n trends u s i n g staged combustion techniques, w h i l e burning the c u r r e n t power p l a n t f u e l , a lows u l f u r No. 6 f u e l o i l . The purpose of t h i s phase was to reduce the time necessary to c a r r y out the subsequent SRC-II t e s t s and to achieve minimum NO l e v e l s w i t h the l i m i t e d supply (4,500 b b l s ) of SRC-II f u e l o i l . χ

X

PHASE I I - SRC-II F u e l O i l T e s t i n g The second phase i n v o l v e d a 6-day t e s t of the SRC-II f u e l o i l to determine i t s combustion performance and emission l e v e l s under v a r i o u s o p e r a t i n g c o n d i t i o n s . Tests were made at f u l l l o a d ,


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three-quarter load and one-half load w h i l e using normal combustion ( b a s e l i n e ) and staged combustion techniques. The staged combus t i o n t e s t s were made t o evaluate the p o s s i b i l i t y f o r s u b s t a n t i a l l y decreasing Ν 0 emission l e v e l s . χ

TABLE V SRC-II FUEL OIL TEST PROGRAM OBJECTIVE: Assess o p e r a t i o n and emissions u s i n g SRC-II F u e l O i l i n a u t i l i t y size boiler. PHASE I - INITIAL BASELINE TESTING ο Develop NO r e d u c t i o n trends by staged combustion ο 29 Emissions t e s t (24 f u l l load/5 h a l f load)

techniques

PHASE I I - SRC-II FUEL OIL TESTING ο C h a r a c t e r i z e nominal o p e r a t i o n emissions l e v e l s and performance ο E s t a b l i s h acceptable minimum NO l e v e l s ( s t a r t i n g w i t h trends of Phase I ) and c h a r a c t e r i z e emissions and performance a t these c o n d i t i o n s ο 17 Emissions t e s t (9 f u l l l o a d / 6 h a l f load/2@3/4 load) PHASE I I I - FINAL BASELINE TESTING ο Operate b o i l e r w i t h No. 6 o i l i n same c o n f i g u r a t i o n s as o p e r a t i n g i n Phase I I ο C h a r a c t e r i z e emissions and performance ο 28 Emissions t e s t s (13 f u l l load/13 h a l f load/2@ 3/4 load) TABLE VI LARGE SCALE SRC-II FUEL OIL BURN TEST AT CON ED EPA REQUIREMENTS

TEST BURN RESULTS

175-300 PPM 95% REMOVED

Production of Distillate Fuels by SRC-II - ACS Publications

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