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Collection of Scientific Papers of the 2 International
Scientific and Practical Symposium on
LOW-CARBON OPEN INNOVATION FOR REGIONS OF UKRAINE
(30-31 October 2013)
2 -
-
(30-31 2013 .)
2 -
-
(30-31 2013 .)
- 2013
,,
-
504.062.2, 504.062.4, 504.7 20.1, 20.3 232 2- - - (30-31 2013 .)
/ . . . . . . // LCOI-Reviews, No. 16, 30.12.2013. : , 2013. 154 .
, 2- - - , 30-31 2013 . - , . , 2013 . - , , . : ..-.., . .. (. ),
..., . .. (. . ), ... .. (. ), ..., . .., ..., ... .., ..., . ..,
... .. : . . .. : 83050, . , . , 46/616, , , - , Web:
www.lcoir-ua.eu , E-mail: [email protected]
, ,
, 2013 , 2013
-
: 1. , 2- - - 5 .. 2- - - 6 . , 7 .. 16 .., .. 21 .., .. 29 ..,
.. 41 .., .. 48 .. . 59 .., .. 2 64 .. - 72 .., .., .., .. 77
Rosa-Hilda Chavez, Javier J. Guadarrama Theoretical and
Experimental CO2 Capture at Power Plant 84 Semko A.N., Beskrovnaya
M.V., Yagudina N.I. The Usage of High Speed Impulse Liquid Jets for
Putting Out of Gas Flares 87
LCOI-Reviews, 2013, No. 16
3
-
2. , 2- - - 96
.. - 97
.. 106
. - 107
. : 109
.. - 111
.. : , , 114
Saftic Bruno Principles of CO2 geological storage 117
3. , 2013 120
.. - (, 19.04.2013) 121 INTERIM NARRATIVE REPORT (Donetsk,
24.05.2013) 125
(, 24.05.2013) 128
.. - (, , 20.09.2013) 131
Mykola S. Shestavin The Strategy of Creating a Virtual
Interactive Platform for the Low-Carbon Open Innovations Relay
(Paris, France, 08.10.2013) 136
, (08.10.2013) 138
INTERIM NARRATIVE REPORT (IEA, Paris, France, 09.10.2013)
139
Simon Bennett 2013 Technology Roadmap for Carbon Capture and
Storage (IEA, Paris, France, 09.10.2013) 142
Keith Burnard Coal-Fired Power Generation (IEA, Paris, France,
09.10.2013) 145
, (15.10.2013) 148 ANNEX A: GENERAL INFORMATION ABOUT A PROJECT
LOW-CARBON OPPORTUNITIES FOR INDUSTRIAL REGIONS OF UKRAINE
(LCOIR-UA) 149 : - (LCOIR-UA) 151 : - (LCOIR-UA) 153
LCOI-Reviews, 2013, No. 16
4
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LCOI-Reviews, 2013, No. 16
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LCOI-Reviews, 2013, No. 16
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LCOI-Reviews, 2013, No. 16
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LCOI-Reviews, 2013, No. 16
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LCOI-Reviews, 2013, No. 16
15
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() 2020 2011-1015 , , , , , , .
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LCOI-Reviews, 2013, No. 16
16
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LCOI-Reviews, 2013, No. 16
17
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LCOI-Reviews, 2013, No. 16
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, 1995 - . 116-120. 2. . .
-2000- // : II - : 1998. . 104.
3. 5- - : 2004. . 494.
4. .. () : // : : 5 (24-26 2004 ., . ) ., 2004. . 246-251.
5. .. . // . .: 2005. 32. . 5-12.
6. // (21 2007 ., . ). .: 2007. . 289.
7. .. // . .: , 2008. 440 .
8. .. // () . 27-28 2008 . . 2. - .: , 2008. 523 .
9. () 2020 // http://base.spinform.ru/index.fwx
10. : "" , (23.02.2011,8.00) //
http://news.finance.ua/ru/~/2/0/all/2011/02/23/228856
11. // http://ru.wikipedia.org/ 12. ..
: // : V -
LCOI-Reviews, 2013, No. 16
19
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(, 21 2011 .): 2 . .: , 2011. - . 2. - . 468-472.
13. .. // : V - (, 21 2011 .). - .: , 2011. - . 2. - .
345-350.
14. .. // V - 21 2011 . - .: , 2011. - . 2 - . 441-442.
15. +20. , // http://www.un.org/ru/sustainablefuture/
LCOI-Reviews, 2013, No. 16
20
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628.35
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LCOI-Reviews, 2013, No. 16
21
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72% 17,6%. . 2. 71,89 . 1990 ., 1996 . 76,55 . , 71,98 . 2004 .,
. 6,24 . 1990 . 0,01 . 2004 .
LCOI-Reviews, 2013, No. 16
22
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, . (Nitrosomonas, Nitrosococcus, Nitrobacter Nitrocystis) [8],
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.
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, , . . , , Nitrosomonas, :
[9].
LCOI-Reviews, 2013, No. 16
23
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: 150-250 /*,
; 15 70 ,
;
7-7.5, 8.4, , ;
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, , [10].
: 8 NO3-(aq) + 2CH3COOH 8NO2-(aq) + 4CO2 + 4H2O (3) 8 NO2-(aq) +
CH3COOH + 2H2O 8NO(g) + 2CO2 + 8OH- (4) 8NO(g) + CH3COOH 4 N2O(g) +
2CO2 + 2H2O (5) 4N2O(g) + CH3COOH 4N2(g) + 2CO2 + 2H2O (6)
8NO3-(aq) + 5CH3COOH 4N2(g) + 10CO2 + 6H2O + 8OH- (7)
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.
LCOI-Reviews, 2013, No. 16
24
-
- , , . ANAMMOX- , , .. .
, ANAMMOX - . . : Brocadia, Kuenenia, Anammoxoglobus, Jettenia,
Scalindua. .
1986 . . () . CO2 85-90% , .
, -, .. ANAMMOX (ANaerobic AMMonium OXidation). :
NH4+ + NO2- N2 + 2H2O; G = 86 (8) , ,
, . ANAMMOX [11].
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3 (9)
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LCOI-Reviews, 2013, No. 16
25
-
, ( ); , ( ), , . : .
, , . , , , 65% 75% , 30% , 1% (2S) , , . , 28 3 , 16,8 3 20,8
.
. 350-400 . 3/ . 4-5 . 3 , 20000 /3, 350 /3. , 6-7 , .
[14] , , -, ( 25000 3) 75%, .. 19000 3 ( 15000 ), , -, ANAMMOX-,
. .
, .
5 o ( ). 2005 . 3,7 . o .
, ( ), 2007 [15].
, . . .
.
( 8100 ), , 70% .
1000 3 1050 2000 3 50-160 3 (2008); 65 75%, - 22600-25100 /3 (/3
5400-6000).
LCOI-Reviews, 2013, No. 16
26
-
2006 2007 40 44% . (2000 3), .
. , - .
2,26 . . 2005 .
(52,5%) (2008). 15 500000 [15].
2005 . , , , , ..
, , . - , , , . .
, .
, , . , ( 21 25 /3). .
, , , , .
, . , .
, , .
. , .
LCOI-Reviews, 2013, No. 16
27
-
1. World Resources Institute. The greenhouse gas protocol: A
Corporate Accounting and
Reporting Standard // World Business Council for Sustainable
Development. The Hague 2001. 27 p.
2. . . . 2. 1996.
3. . . 2000.
4. .., .., .. . .: , 1993.
5. .., .. / . ., 1997.
6. .. . .: , 1988. 7. .., .. .
.: , 1988. 8. ..
/ .., .. , .. ., .. // i i. i . 2007.
9. . " " 290800 . --: , 1998. 19 .
http://www.rgsu.ru/files/uploads/users/butko_d/AZOT-MU.pdf
10. . / . , . , . --, . .: , 2006. 480 .
11. Effects of aerobic and microaeribic conditions on anaerobic
ammonium-oxidazingng (ANAMMOX) sludge / M. Strous, K. Gerven, U.J.
Kuenen [et al.] // Applied and Environmental Microbiology. 1997. V.
63. P. 2446-2448.
12. Lindsay M.R. Cell compartmentalization in planctomycetes:
novel types of structural organization for the bacterial cell /
M.R. Lindsay, R.I. Webb, M. Strous // Archive of Microbiology.
2001. V. 175. P. 413-429.
13. Van Niftrik L.A. The ANAMMOXosome: an intracytoplasmic
compartment in ANAMMOX bacteria / L.A. Van Niftrik, J.A. Fuerst,
J.S.S. Damste [et al.] // FEMS Microbiology Letters. 2004. V. 233.
P. 7-13.
14. .. ANAMMOX // . : . 2011. . 2. . 82-87.
15. International Water Association. . WTE Wassertechnik GmbH, ,
.
http://www.aquaby.by/index.php/news/1069/56/obrabotka-osadka-stochnyh-vod-v-litve-do-i-posle-vhoda-v-es.
LCOI-Reviews, 2013, No. 16
28
-
614.844+621.227
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, .,
: , .
: , , , ,
, , . , , , .
.
, [1, 2]. , , 50 /, . ' (. 1). , , 15 [2], . , .
. 1. : ; II
, ; () , '
LCOI-Reviews, 2013, No. 16
29
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[3, 4], , (. 2). . , . [3], .
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.. , , .
, . , , -100 -150 (, ), , "The Big Wind" () JFR-250 (), , -200
() [9]. , , . 60% 40% , 14%,
LCOI-Reviews, 2013, No. 16
30
-
, 12-15 17-18%. , , . , , : 60 / (-100) 5 . 950 100-150.
( 15 ) (. 3).
, 50 / 50 [8]. (. 1.4).
. 3.
. 4.
LCOI-Reviews, 2013, No. 16
31
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[9], ( , ). .
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[10, 11]. , . (12) .
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, , . , .
LCOI-Reviews, 2013, No. 16
32
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-1, -2, -3, - (. 6) [12]. 50 (-1 40), 30 . - 4 1,5 . '. , . 50
.
. 6. "-"
"" , ' , , , (300-1500 ).
. iFEX , , Leopard 1 [13].
Fire Commander (. 7). 6-7 25- 65 . , Fire Commander , , "IFEX
hand impulse gun".
. , . Fire Commander . , Fire Commander .
, [14-16].
LCOI-Reviews, 2013, No. 16
33
-
. 7. Fire Commander
, , , , (. 8). (100-1000 ). 100 150 , 40 .
. 8. : 1 ; 2 ; 3
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LCOI-Reviews, 2013, No. 16
34
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132
LCOI-Reviews, 2013, No. 16
35
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1 - ""
350 / 20 150 2,8 1 /30 . 30 . 3000 2 .
2 -
350 / 7,5 0,140 1020 102 132 45 2000 8 40 / 2,5105
-3151 -131.
. 11, (. 3). -3151 .
. 11. -3151
LCOI-Reviews, 2013, No. 16
36
-
3 -3151
3151 -76 110 /. 4 2005 90 . ' 2450 3 . /. 100 /. -76
3151 ,
. .
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LCOI-Reviews, 2013, No. 16
37
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4. -131 6 6 :
6135 6400
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: 3500
: 6500 4000
: 330 355
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/. 35
850 10,8
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: , , 8- , V- 90,
, , 100,0 , 95,0 ', 6,0 6,5 , .. () ( )
148 (108,9) 3000 /. , * () 41,0 (410) 1600-1800 /.
LCOI-Reviews, 2013, No. 16
38
-
1. .
. , , ' , .
2. : ; ; . .
3. .
4. , - . () 102 , 900 . , , , .
5. - . , . -3151 -131 , .
1. : / . . , . . , . . .; . . . . , . . . .: , 1991. 1232 .
2. . . / . . , . . , . . // . . , 2006. 1.
http://scientific-notes.ru.
3. Cooley W. C. Development and Testing of a Water Cannon for
Tunnelling / W. C. Cooley, W. N. Lucke // Proc. 2nd International
Symposium on Jet Cutting Technology. Cambridge (England). 1974.
Paper J3.
4. / . . , . . , . . . // . : . 1971. . 9. C. 7-11.
5. . . / . . , . . // . 2009. . 9 (81), 3. . 56-64.
6. . . : . ...: 01.02.05. : , 2010. 167 .
7. P.A. / P.A. , .. , E.H. . .: , 1987. 200 .
8. .. / .. , .. // : , 2009 .12, 4 (33). . 116 120.
9. .. - /
LCOI-Reviews, 2013, No. 16
39
-
.. , .. , .. . // . - .. , 2011 . 36 .
10. .. / .. , .. , .. , .. // . - 2004. - . 6 (78). 3. - . 3
-9.
11. .. / .. .: , 1976. 504 .
12. . . // . . . : , - 2002. - . 35. . 181 - 185.
13. Semko A. Internal ballistics of a powder impulsive water
device // Proc. 14th International Conference on Jetting Technology
/ Edited by H. Louis, 1998, Belgium, Brugge, 21-23 September, BHR
Group Conference Series Publication No. 32. - P. 195 - 202.
14. .. : . / .. , 2008. 39 .
15. .. / .. , .. , .. . // " ", . 2. .: , 2006. 416 .
16. .. . 1. / .. // . 1998. 3. . 37-43.
17. .. . 2. / .. // . 1998. - 4. . 46-52.
18. . 27155 , 6 62 3/06, 31/02, 31/03, 21 35/00. / .., .. .; . -
96124654; . 13.12.1996; . 28.02.2000, . 1.
19. Watson A.J. IMPACT PRESSURE CHARACTERISTICS OF A WATER JET /
A.J. Watson, F.T. Williams. R.G. Brade. // 6th International
Symposium on Jet Cutting Technology 6-8, April, 1982
20. .. / .. .: , 1981. 296 .
21. 66434 / .., .., .., .. - (2011.01). 62 27/00. u 2011 03022.
15.03.2011. 10.0.1.2012, . 1.
22. 66434 / .., .., .., .., .. - (2013.01). A62C 2/00. u 2012
12587. 05.11.2012.. 25.07.2013, . 14.
LCOI-Reviews, 2013, No. 16
40
-
621-523.8
.., ..
,
.
. - . , , - , . .
: , , , .
.
. - . , , - , . .
: , , , .
Abstract. A combined electricity supply system for chemical
enterprise is proposed. Feasibility study and
ecological analysis were performed. Analysis of greenhouse gases
emissions, particularly CO2, was conducted before and after
implementation the additional capacities of mini-HES and
turbine-generating set which works on the heat produced during
technological process. A strategy for accession renewable energy
sources to enterprises electricity network using electricity from
the UPS of Ukraine as a basic supplier was designed.
Keywords: electricity supply, combined power system, renewable
power generation, ecological analysis.
. , , , . . 2001/77/ " , , " 27.01.2001 . [1] 2009/28/
23.04.2009 . , [2], () .
. 243 2015 . [3] 15-20%. 20-20-20, ( , ) 20% 2020 . . 10 % 2030
. 22 %.
LCOI-Reviews, 2013, No. 16
41
-
, . , , . . 2010-2015 ., 01.03.2010. 243 [3]. , . . , , ,
[4].
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() . , . , , , . , . , - - . , (), , , . . , .
- (), . . . .
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LCOI-Reviews, 2013, No. 16
42
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LCOI-Reviews, 2013, No. 16
43
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LCOI-Reviews, 2013, No. 16
44
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LCOI-Reviews, 2013, No. 16
45
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0
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25000
,
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24
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. 2.
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( ) . 3.
-;
81%
-
18%
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-
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. 3.
.
. , .
LCOI-Reviews, 2013, No. 16
46
-
1. , ,
.
2. , - , , .
3. , .
4. , , 2 .
1. 2001/77/ "
, , " 27.01.2001 .
2. 2009/28/ 23.04.2009 . 3. 243 2015 . 4. / .. [ .];
. . . . : - , "". - .: , 2007. - 560 . - ISBN 978-8578-08-3
5. .. / .. - , 2. - .: , , "". - 1999. - .39-42.
6. . . . - Energy Policy, .3, 17, -2005. . 2237-2243.
LCOI-Reviews, 2013, No. 16
47
-
537.84:669.001:519.63
.., ..
, .
. , . , , , , .
: , , , .
. . , .
70% . .
, , , , . , , , (, , .) .
. . , , .
[13, 18, 21, 29-
31]. [16, 27, 34]. , [8, 15]. , [19, 20, 22, 23, 25, 32].
LCOI-Reviews, 2013, No. 16
48
-
[24, 28, 33]. [24]. : , , .
. 1 [17].
, , , . . . , , . , . . , , . , . , , , , , .
. , , , , . , . , . , , . , , , .
. :
, ;
, .
, Danieli [5] .
LCOI-Reviews, 2013, No. 16
49
-
, .
[2] , . .
, , , . .
: , , . Danieli . 2 [7]. : 100 , 5500 , 1100 , 500 , 650 ,
80-100 k, 500-1000 , 40-100 , + .
:
; , ; . 15 60 %
[6, 9, 11, 12]. ,
. 3500 C 1650 C . . 50 C [32].
, . , . , . , .
/, . , -. /, . [26].
624 1022
84
, ( ), . , .
LCOI-Reviews, 2013, No. 16
50
-
: , , , . , .
. , , 3,0000 Ljv / [14]. , , ,
15,1818501010 2220 TvTgLGr ( ) ( ),
[14]. , .
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, , 110 3
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,
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. , ( 14,0Re 00 Lvm ), . .
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. . , , :
- BjgIvvvpIvv TT 32 ; (1) 0 v ; (2) k
vkvPkkv T
k
T 3
2 ; (3)
LCOI-Reviews, 2013, No. 16
51
-
k
CvkvPk
Cv TT2
213
2)(
; (4)
22
,3
2 kCvvv
vvP TT
; (5)
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g
; ; j B ; ; T ; , , ;
1C 2C C,k ;
; E , T , , ,
aTa 2j
, . (4.1) : ,
pCpI )()(( TT u )u ,
g , . Bj
. , [10] ANSYS Multiphysics [1], ANSYS CFX [3] COMSOL [4]. :
1- ; 2- ; 3-
.
, .
1- , , .
LCOI-Reviews, 2013, No. 16
52
-
2- , .
3- .
, 1- 2- , 3- . , .
. ANSYS Multiphysics 1- , ANSYS CFX, 2- 3- . COMSOL .
, , , . 3, , . 3. 1 , 2 , 3 , 4 (). . , B1 B9, . 3 1.
, ( B8), , . .
, :
, 1 = 0,712106 ()-1 1750, .. 1550-2730 ;
2 = 0,2106 ()-1; = 1; = 1; = 1;
1500-2000 pC = 750 /();
1500-2500 = 32 /; ,
[26]. k 09,0C ,
, , 44,11 C 92,12kC 0,1k , 3,1 .
. , . 3 1. 1- ANSYS Emag ( ) , , . , .
LCOI-Reviews, 2013, No. 16
53
-
. : , , 0,01 . , , ( 10 ).
. 4 , . . 5 , . . . . , , . . 0,3 /. 0,1 /. 1-3 %. , . , .
. . 6 . , , , . , , [1], . : ( 0 rT ) , ( 0 rT ) . , , .
, , . . 7 , .
, . . , . 7, . , , . 0,5 /, 1,5 . 0,3 /. , .
, . , . . 1/3 .
LCOI-Reviews, 2013, No. 16
54
-
, . . .
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p.
4. COMSOL Multiphysics Version 3.5: Modeling guide COMSOL
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5. G. Gensini, M. Pavlicevic. Cooled bottom electrode for a
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13. .. / .. , .., .. // . 1977. 1. . 115-120
14. .. / .. , .. , .. , ... : . 1985. 315 .
15. .. - ANSYS / .. , .. () // ANSYS Solutions. . - , 2007. .
13-18.
16. .. / .. , .. // . 1986. 3. . 110-116
17. .. : / .. . .:, ACT. 2003. 528 .
LCOI-Reviews, 2013, No. 16
55
-
18. .. - / .. , .. , .. , .. // . 1980. 2. . 127-130122
19. .. / .. , .. , .. . .: 1986. 360 .
20. , .. . . / .. . : , 1998. 184 .
21. .. / .. , .. // . 1980. 1. . 77-80
22. .. / .. , .. , .. . .: . 1995. 592 .
23. .. / .. , .. . .:1970. 264 .
24. .. XXI / .. , . // . 2004. 8. .2-6
25. .. / .. , .. . .: . 1989. 176 .
26. . . // . .. . .: . 1976. 1008 .
27. .. / .. , .. . .: . 1991. 280 .
28. . / . , . // . 2002. 9 . 49-53
29. .. - / .. // . 1977. 4. . 121-125.
30. .. / .. , .. // . 1977. 8. . 713-714.
31. .. / .. // . 1977. 2. . 139-141.
32. .. / .. , .. , .. , ... : . 2005. 139 .
33. .. / .. , .. , .. // .125 . 2: . . . .-. . / . .. . : .
2003. . 78-82
34. . : . ... / . , 2009. 363 .
LCOI-Reviews, 2013, No. 16
56
-
. 1. ) )
(1 ; ; 2 ; 3 ; 4 ; 5 6 ; 7 ; 8 ()
)
500
1100
5500 650
. 2.
LCOI-Reviews, 2013, No. 16
57
-
. 3.
1. / B1 B2 B3 B4 B5 B6 B7 B8 B9 0j 0nj 0 0j nj 0j
21 EE , 21 nn DD , 21 nn BB
, 21 BB
- - - - - 2=1980 3 = 1900 1=3300 - - - - - 0v
. 4.
LCOI-Reviews, 2013, No. 16
58
-
. 5.
. 6.
. 7.
LCOI-Reviews, 2013, No. 16
59
-
.
..
, .,
- .
( , .). - 2004 122,7 . . , . 19 2011 . .
- . , . 1975 .
(), . , .. , "... , , , . .. - (1966 .) " , , . . , .
16- . , , () , 1782 . 20- 19 . 12 .
1872-1874 .. . .. . 1872 1953 81 , 1881 1896 , .. 15- 4- 41 . -
671580 . 1924 1946 , 1.5 . . ( 450 . ) 1950 , . , , . NaCl - , , ,
- . 2.5 .. . ""
LCOI-Reviews, 2013, No. 16
60
-
. , 804551 . . 250 335 / .
1951 . ( II - - , .. ).
" " . , ""
1950 , 4- - .
. , , 800 000 . . . 4- / 1979 2 . 272 . 880 . , , 34- . , , . ,
887 . 12959620 . . 4059144 . :
36. 1950 . 439 . 1953 . 2706833 3, 742997 . (-) 1273, 813. 4593.
. 88 . 30 - 450 . 0-151,5 250 . 200-100 351,8-352,4 .
45. 1953 . 406,8 . 1957 . 4943209 3, 1732392 . 8203, - . 833880
3, 28 , 95 . 324 349,5 .
, , .
"" , , , :
1) - . 5 2, , (. 8,18).
LCOI-Reviews, 2013, No. 16
61
-
30 , - , 1800 , 385 / (. 6);
2) ;
3) , ;
4) .
, 1961 . , , .
. . , . 1960 . 30 . , 27 . , 1964 . 60 . , 53 . . , 28.5 . 3. ,
, 18 . 3. 84 12 . , 5.7 . 3. . , . , , : 5.7 84 = 478.8 . 3, , , ,
. : 1952 . 1953 . 238 . 3 , 44 . 3, .. 40%. , , , 172.8 . 3 - 56.3
. 3, 1954-55 . 163,3- 76.1 . 3, 1955-56 . 150.5-87.9 . 3, .
. 36, 42, 44, 45 / (. 1994 .) , / , 209- 09.07.1991 , , :
1. ( , ).
2. 1 2- ( ).
3. () () ( , , ).
4. .
LCOI-Reviews, 2013, No. 16
62
-
5. 1/45 . 2/45 ( ).
6. 36,44,45 20 .
, , . , , 90- / - - , .
LCOI-Reviews, 2013, No. 16
63
-
2
..1, ..2
1 , .,
2 ,
:
. 2 . , , 2. (- ) 2 . 2 , , .
: 2, 2, 2, , . ,
(2) . ().
, , () .
, , 2050 , 2 2050 130% 2005 2 50%.
, , , , , , 2.
, , , .
2 90-
2, 2011 , 2 .
2 , , 2 10 . [8]. (, , , )
LCOI-Reviews, 2013, No. 16
64
-
(), : , , , , , , , , .
, ( 2 2- ), , .
2 (, , ) - (, ).
2 2
- . , 2. 2 (), ( ) [9]. , ( ) , .
, 2: , , . , .
2 , MRCSP, MGSC, SECARB, SWP, WESTCARB, Big Sky, PCOR (),
Weyburn, Fenn Big Valley (), Sleipner (), Yubari (), Qinshui Basin
() .
, 2 , , .
. - - () (). - - . .
, [6]. ( , ).
, - ,
LCOI-Reviews, 2013, No. 16
65
-
. . - - (. 1). , 2012 . 8 . 2, 4 3. , , ( ).
- : , . 2.
( 500 ) . , , 2.
. 1. - (a) (b).
LCOI-Reviews, 2013, No. 16
66
-
, . , , , , , [3].
- , . . . ( 5 ) (, , ).
- . . () (, , ) . , .
: (P1kr), (P1nk), (P1sl) ( ) (P1km) ( ). P1sl P1km, , , . .
, (. 1). P1sl , , , . 40-50 . 500 .
, - P1sl - , .
P1km - - . P1km , 92% , 80-85%. 400-530 . 1000 .
P1sl, P1kr, , . P1nk.
, , . , , , .
- . , . : C33, C32, C2-31 ( ), C27, C26, C25 ( ), 24 ( ).
LCOI-Reviews, 2013, No. 16
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-
24, 25, 26 32 (30-47% ), 20-30%. : 21 22 ( ) 16-20%. , , 35-60 (
100 ). 31 25 27 24, 26 [5].
, 2 - , :
- ; - ; 2
. :
1.1. ; 1.2. ; 1.3. 2. . 1.1.
: , , , . , . , , . . , , () [7]. 2-10% , , , [1].
, 50% ( ) 2% 7-11% [7]. - 10-13% 20-22% [5].
, . , 2- . 2- .
1.2. , . .
1.3. 2 , 2 800 . 2 50-80% , [9]. 2.
LCOI-Reviews, 2013, No. 16
68
-
, - , - . .
2 :
2.1. 2 , .
2.2. 2 , ().
2.3. 2 . . 2.1. ,
, . 2.
2.2. , , 50%. , .
() CO2 [9]. : - 2. ( 50%) .
. , , .
2.3. . 2.
2.1 2.2 , , , , , .
2 - :
3.1. , ( ), 800 , .
3.2. .
3.3. . , 800 .
3.4. , , , ( , , .).
3.5. , .
LCOI-Reviews, 2013, No. 16
69
-
, , - , , , - . .
, , 2, 2 , .
- . 2 .
, - , , , .
- - , . 2 - .
, 2 - :
1. 2 - .
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4. , - 2 - .
2- , - .
1. .. /
.. // . 2010. 88. . 70 76. 2. .. 2
/ .. , .. , .. , .. // . - , 2012. . 18.
LCOI-Reviews, 2013, No. 16
70
-
3. . / . , . , . // . 2011. 2. . 99 102.
4. .. 2 / .. , .. // , 1 - , 2012. . 50 53.
5. .. / .. // . 2011. 2. . 103 107.
6. .. , - / .. // . , 1961. . 51 57.
7. .. , / .. , .. // . 2010. 88. . 118 123.
8. : / ; .. . :, 2011. 205 .
9. : . , / . 2005. 58 .
LCOI-Reviews, 2013, No. 16
71
-
622.831.3.02 (075.8)
-
..
,
:
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: , , .
-
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, . [1].
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, [3].
.
LCOI-Reviews, 2013, No. 16
72
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[4] ,
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, :
22 11 22 21( ( )) : ,
2 1tc cE h t h h h h dx
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, ..
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LCOI-Reviews, 2013, No. 16
73
-
, : - , , , , , , , . , - (LCOIR-UA). .
, - , , , , . , , , , - .
, - , , , - .
- , , , , , , .
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LCOI-Reviews, 2013, No. 16
74
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- , - - , , .
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; -
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1. .. / ..,
.. - .: . - 1979. - 296 . 2. .. /
.. , .. , .. // . - 1998. - 8, 9. . 9. 3. .. ,
./.., .. // .- 1979. - 6. - . 8-10.
4. .. / .. , .. , .. // . ... . . 22 (61), , - 2009. - .
79-89.
5. .., .. / .. , .. // 13, 4. : , 2002. - . 45- 52.
1. .. /
.. , .. // 10- , . - 2007. - . 34-36.
LCOI-Reviews, 2013, No. 16
75
-
2. .. / .. , .. , .. . // - , . 10. - : , 2007. . 119-127
3. .. / .. , .. // 11- , . - 2008. - . 28-32.
4. .. - / .. // IV - , , 2008. - . 22-24.
5. .. - / .. , .. // . - : , 2009, 1-2, . 70-74.
6. .. - / .. , .. // . - . - 2010. - . - . 25-32.
7. .. - / .. , .. ., .. // . - 2010, . XI, , . 158 .
178-187.
8. .. - - / .. // VI - , , 2010. - . 89-94.
9. .. - / .. , .. ., .. // . - 2010, .XI, , . 158 .178-187.
10. Prihodko S. Conceptual aspects of the development of
information telecommunication environment of the system of life
support region (on the example of Donbas) / S. Prihodko, P.
Polyacov, L. Polyacova // The International Symposium
Euro-ECO-Hanover 2010: Environmental, Engineering-Economic and
Legal Aspects for Sustainable Living. 2010.
11. .. - ( ) / .. , .. // : II . .-. . - 2011. - . - .
10-14.
12. .. - 4- / .. , .. // . - 2011. - . -. 111-115.
LCOI-Reviews, 2013, No. 16
76
-
669.187.2
.., .., .., ..
,
.
, - . .
: , , , , .
,
, , , (, ), . .
()
( 1015%) [1]. - , . , (- ) .
() (Midrex, Energiron-HYL, ITmk3 .) (Corex, Finex,OxyCup .) [2],
.
Midrex , , (DRI). , , . , () 2 .
Fe2O3 2 2. (95% Fe; 0,7 1,0% C) 50 65 , , .
. Midrex 400 . 1 .
LCOI-Reviews, 2013, No. 16
77
-
Energiron-HYL (70-87 %), ( 550 ) ( 920). HYL-III (70 %) (30%). ,
.
COREX , . , -. 96% . -, . 1450 1550. , .
FINEX - , . FINEX (DRI) . FINEX .
( 250300 . .), 200500 . . . , (20-50 . . ) 1-2 . , ITmk-3
OxyCup.
ITmk-3 [3] . , , . 135014500, , . 10 . 95-97 %. 13,5 / . , , ,
200 . . .
OxyCup [4] , , , . , 4 % . 1 . 1100-1200 3, 200300 , 1,5 . (, ,
), 200 . . [5], .
. (MIT) ,
LCOI-Reviews, 2013, No. 16
78
-
, . . IT Donald Sadoway (Molten Oxide Electrolysis (MOE)), .
(MOE) , . MOE , .
. . , , .
, . , Donald Sadoway, , [5]. , , [6].
MIT . , , . , , , .
, .. , , , . , , . [7].
[9], , . , , , .
, , 20-50 . . . , . ; , . ; , . ; , . .
, , . , , , , .
LCOI-Reviews, 2013, No. 16
79
-
[10]
, .. , , , , . , , . , . , , , -, .
, , , , . ( ) , , . , .
, .1, :
, ;
, , ;
.
, 1 2, , 3 . 4. 5 (5.1), (5.2) (5.3), 6. 7. () 8 9. - 10.
- 50 . . 1 2. ( 1-3) : 68-75 , 1,75-1,90 , ( 4) . (): 1 4 , 2 ,
3 .
LCOI-Reviews, 2013, No. 16
80
-
1-3 25 % , 10 % . . 4 . .
, , , .
.
, , , , 1,4-1,6, ... 0,6.
, , 94 % 2,12 ./ . , , , 12-13 / , ITmk-3. : 20-25 % , . 2 .
, , ... 0,6 0.7, 1,7-1,8 .. ( ) 10-12 . , , ITmk-3.
(50-60 %); , (20-25 %); ().
- . . 3.
: 68-75 , 1,75-1,90 . (35 ), (7 ) (3 ). 3,56 / . .
, . , , (, , ) , .
1-3 . . - , 20-50 . . .
LCOI-Reviews, 2013, No. 16
81
-
- . : , .
, .
. 71-94 %, 2,12-2,29 ./ , 12-13 / .
.
: 1. H. Kim, J. Paramore, A. Allanore, D.R. Sadoway.
Electrolysis of molten iron oxide
with an iridium anode: the role of electrolyte basicity /
Journal of the Electrochemical Society. USA, 2011. - p. 13.
2. D. Wang, A.J. Gmitter, D.R.Sadoway. Production of oxygen gas
and liquid metal by electrochemical decomposition of molten iron
oxide / Journal of the Electrochemical Society. USA, 2011. - p.
14.
3. D.R.Sadoway. Eco-friendly steelmaking/MIT Technology Review.
2013. - p.12. 4. .., ..,. ..
/ 8- ( , 2004). .: 2005, . 270273.
5. .., .., .. . . 1. , , . - : , 2011. 430 .
6. H. Tanaka, R. Miyagawa, T. Harada/ Fastmet, Fastmelt and
ITmk3: development of new coal-based Ironmaking process/ Direct
from Midrex. Special Report. Winter 2007/2008. P. 813.
7. . . / ( MPT International), 2005, 2. . 613.
8. .., .., .. / . VI . . . : , 2009. - . 6163.
9. .., .., .., .. - // / .: .. () .-: , 2002. - . 40 (.: ). .
7681.
10. 97745 , 224/00. / .. , . , .. . . 201013890; 22.11.2010; .
12.12.2011. . 23. 6 .
LCOI-Reviews, 2013, No. 16
82
-
. 1. ( )
1. . (), % (), %
Fe2O3 + FeO
CaO +MgO
SiO2 MnO Zn C Fe C Mn S P Zn
1 90,9 1,0 3,2 0,4 - 0,26 96,5 2,2 0,32 0,040 0,08 - 2 63,5 4,4
14,0 0,06 0,1 5,8 94,8 3,4 0.12 0,065 0,12 0,08 3 66,8 6,9 8,6 0,2
1,5 9,4 94,6 4,1 0,14 0,055 0,11 0,34 4 90,9 1,0 3,2 0,4 - 0,26
97,3 2,2 0,33 0,040 0,08 -
2. .
, % , 1 Fe2O3 + FeO
CaO +MgO
SiO2
, .
, % - ,
. , 3.
9,4 64,5 11,9 42,0 27,5 6,5 57 94 2,12 0,25 17,9 41,8 32,7 39,5
17,4 15,8 68 76 2,25 0,28 15,2 40,3 33,8 38,9 15,7 13,4 66 71 2,29
0,28 4,8 57,3 32,2 25,5 8,4 6,2 125 48 4,54 -
3. .
c , % , % Cu Pb Sn Zn Ni Fe Cu Pb Sn Zn Ni Fe 1 78,1 2,13 10,5
0,89 0,78 2 76,9 2,16 11,9 0,82 0,92 3
19,58 2,85 1,15 3,98 0,10 -
80,3 1,82 10,2 0,94 0,73
-
LCOI-Reviews, 2013, No. 16
83
-
THEORETICAL AND EXPERIMENTAL CO2 CAPTURE AT POWER PLANT
Rosa-Hilda Chavez1 and Javier J. Guadarrama2
1Instituto Nacional de Investigaciones Nucleares La Marquesa,
Ocoyoacac, Mexico
2Instituto Tecnolgico de Toluca Metepec, Mexico
ABSTRACT. The main challenge of the chemical absorption CO2
capture processes is reducing the energy
requirement in the stripper with the reboiler at post-combustion
method when ambient air is used as an oxidant. This paper discusses
several CO2 capture process configurations and most important
parameters necessary to obtain 90% capture rate and lowest energy
consumption at solvent regeneration for CO2 capture from flue gas
of thermoelectric power plant. Carbon dioxide is removed by
chemical absorption processes from the flue of power plant with
mono-ethanol-amine (MEA). Absorption of CO2 was conducted using an
experimental packed column of three different structured packing
materials. The mass transfer characteristics were determined by
experimental absorption columns and modeling columns with Aspen
Plus using RADFRAC. The results show decreased reboiler energy
consumption from the base case process configuration with 8MJ/kg of
CO2 at solvent regeneration.
KEYWORDS: CO2 capture efficiency, numerical simulation,
re-boiler energy requirement at stripper, structured packing,
liquid/gas flows ratio
INTRODUCTION A major concern in developed countries is climate
change and consequently the effect of
CO2 emissions. These have subsequently generated great interest
in efficient CO2 capture studies and resourceful methods to enhance
energy-intensive processes [1], [2].
The G-8 has risen to have more than 20 industrial scale projects
in operation by 2020 in order to maintain its timeline regarding
effective mitigation option [3]. International Energy Agency (IEA)
suggests in case CO2 Capture and Sequestration (CCS) are not used
as a mitigation option, the cost of achieving required reductions
would increase by 70%. The conclusion is that all mitigation
measures are required because there is no single solution to
climate change [4], [5], [6].
Three CCS methods are being developed: Pre-combustion,
oxy-combustion and post-combustion. The last alternative works
properly well; this is applicable to power generation technologies
(5-20% CO2). Advantages include over 60 years experience, no risk,
low pressure of 0.1MPa, currently in use, and CO2 recovery for
carbonated beverages. On the other hand, disadvantages include,
high investment cost and power consumption, and large equipment
size [6], [7], [8]. This process provides a high capture efficiency
and selectivity, and lower cost than other processes [9], [10],
[11].
Among all the different techniques for capturing CO2, absorption
with aqueous alkanolamine is recognized as a proper commercial
option for capturing CO2 in gas diluted flows, which contain 10% to
12% of CO2 volume [12]. The carbon dioxide capture with
Monoethanolamine (MEA) aqueous solution consists of gas stream
contact with amine aqueous solution which reacts with carbon
dioxide to form a soluble carbonate salt, by reaction acid-base
neutralization [12], [13], [14].
CO2 capture simulation using MEA with Aspen Plus, helps to
obtain chemical and physical component properties, equilibrium
properties of ionic and molecular species by the electrolyte-NRTL
models; also it helps to evaluate different case studies and to
compare three different structured packings: ININ 18, Sulzer BX and
Mellapak 250Y, this way it is feasible to choose which one fits the
requirements of greater CO2 absorption and lower height of mass
transfer unit.
With all the previous configurations in mind, it has been
established that the purpose of this work is to evaluate the
minimum energy consumption for solvent regeneration and maximum CO2
absorption with 600 ton/day flue gas flow treated by Aspen Plus of
CO2 capture process, using MEA at 30 % weight.
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Parameters that determine technical and economic feasibility of
CO2 absorption systems are [6], [12], [13]:
- Flue gas flow. The absorption column size is determined by
characteristics of combustion gas flow: its flow and composition of
components. The first one to obtain diameter of the column, and the
second one, the number of mass transfer stages in order to separate
one o more components from one to another composition.
- CO2 concentration. Flue gas is at atmospheric pressure,
partial pressure of CO2 is between 3 to 15kPa under these
conditions, and amine chemical solvent in aqueous solution is most
suitable.
- CO2 separation. CO2 recovery is a parameter related to
absorber height. - Solvent flow. It determines equipment size used
to capture CO2. - Power requirements. It involves thermal energy to
regenerate solvent and power
energy to operate pumps. - Cooling requirements. To bring flue
gas and regenerated solvent to required
temperatures, unless there is a gas desulphurization process
where gas combustion temperature leaves at an appropriate
temperature to enter the absorption process.
METHODOLOGY The MEA solvent was selected to make a system model
for CO2 removal by
absorption/stripping. Both the absorber and the stripper used
RateSepTM to rigorously calculate mass transfer rate. The accuracy
of the new model was assessed using a pilot plant run with 30% MEA.
A rigorous model adopted from the literature, built on RATEFRAC of
Aspen Plus is used to simulate the complex reactive absorption
behavior. The reactions employed were defined by internal software
wizard [15], [16], [17].
The methodology was divided in two sections: 1) Hydrodynamic
analysis. Column was performed by exploring different regions
of
operation: preload, loading and flooding regimens, in order to
find GL flow ratio per each packing in order to ensure loading at
turbulent regimen and optimum mass transfer operation.
The hydrodynamics of each packing was obtained by determining
the pressure drop over packed bed height, ZP , due to the passage
of gas through the packed bed, either dry (zero liquid flow) or
with liquid flow [18].
2) Mass transfer model was developed to calculate and analyze
the effect of mass transfer unit height (HTU) on the gas and liquid
phases. The Double Film theory correlates height of global mass
transfer unit OGHTU and OLHTU , with height of gas mass transfer
unit GHTU and liquid mass transfer unit LHTU for a system [12].
CONCLUSIONS - ININ18 packing showed a higher pressure drop than
the other two structured packings.
This one reached flood with lower liquid and gas flow values. -
Sulzer BX packing showed the highest mass transfer efficiency due
to having the lowest
value than the other two structured packings, as a result of its
highest geometric area. OGHTU- Sulzer BX packing was the most
efficient in CO2 whole capture with MEA and showed
greater efficiency in the absorption column, although requiring
a larger number of mass transfer stages. It showed lower mass
transfer height in both columns; also, highest CO2 absorption
efficiency and CO2 capture efficiency.
- The minimum energy consumption for solvent regeneration was
120MW at energy requirement in order to carry out the regeneration
of the MEA.
- For CO2 absorption, gas film resistance is important for this
type of CO2 capture with chemical reaction with absorber loading
and removal.
- The accuracy of the new model was assessed using a recent
pilot plant run with 30% MEA. Absorber loading and removal were
matched and the temperature profile was approached within 5C.
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REFERENCES [1] IPCC, Climate Change: The scientific basis,
contribution of working group 1 to the third
assessment report of the intergovernmental panel on climate
change, U.K. 2001, Cambridge University Press.
[2] Thompson A.M., Hogan K.B., Hoffman J.S., Methane reductions:
Implications for global warming and atmospheric climate change,
Atmos Environ, 26, (2003), pp. 2665-2668.
[3] NETL, Carbon Sequestration ATLAS for North America, USA
2008. Department of Energy, Office of Fossil Fuels.
[4] Rubin E., Marks A., Mantipragada H., Versteeg P., Kitchin
J., Report to the Congressional research Service, Washington D.C.,
2010, Carnegie Mellon University.
[5] Hougton J.T., Callander B.A., and Varney S.K., Climate
Change: The IPCC Scientific Assessment. U.K. 1990, Cambridge
University Press.
[6] Leites I.L., Sama D.A., Lior N., The theory and practice of
energy saving in the chemical industry: some methods for reducing
thermodynamic irreversibility in chemical technology processes,
Energy 28, (2003), pp. 55-97.
[7] Amrollahi Z., Ertesvag I.S., Bolland O., Ystad P.A.M.,
Optimized Process Configurations of Post-combustion CO2 Capture for
Natural-gas-fired Power Plant Power Plant Efficiency Analysis,
Proceeding of Third ICEPE, (2011), pp. 629-640.
[8] Kawabata M., Iki N., Murata O., Tsutsumi A., Koda E., Suda
T., Matsuzawa Y., and Furutani H., Energy Flow of Advanced IGCC
with CO2 capture Option, Proceeding of ASME2010, IMECE, (2010), pp.
1-6.
[9] Wilson M.A., Wrubleski R.M. and Yarborough L., Recovery of
CO2 from power plant flue gases using amines, Energy Convers. Mgmt.
33 No. 5-8, (1992), pp. 325.331.
[10] Austgen D.M., Rochelle G.T., Peng X., and Chen CC., Model
of vapor-liquid equilibria for aqueous acid gas alkanolamines
systems using the electrolyte NTRL equation, Ind. Eng., Chem. Res.,
28, (1989) pp. 1060-1073.
[11] Jassim M.S. and Rochelle G.T., Innovative absorber/stripper
configurations for CO2 capture by aqueous monoethanolamine,
Innovative absorber/stripper configurations for CO2 capture by
aqueous monoethanolamine, Ind. Eng. Chem. Res. 45. No. 8, (2006),
pp. 2465-2472.
[12] Danckwerts P.V., McNeil K.M., The absorption of Carbon
Dioxide into aqueous amine solutions and the effects of catalysis,
Trans. Inst. Chem. Eng, 45, (1967), T32.
[13] Dey A., Aroonwilas A., Carbon dioxide absorption
characteristics of blended monoethanolamine and
2-Amino-2-methyl-1-propanol, Faculty of Engineering, University of
Regina, Regina, Saskatchewan, (2006), IEEE.
[14] Asrarita G., 1964, The influence of carbonation ratio and
total amine concentration on carbon dioxide absorption in aqueous
monoethanolamine solutions, Chem Eng Sci, 19, (1964),
pp.95-103.
[15] Pacheco M.A., Rochelle G.T., Rate-based modeling of
reactive absorption of CO2 and H2S into aqueous
Methyldiethanolamine, Ind.Eng.Chem.Res. 37, (1998), pp.
4107-4117.
[16] Plaza J.M., Van Wagener, Rochelle G.T, Modeling CO2 capture
with aqueous Monoethanolamine, Energy Procedia 1, Elsevier, (2009),
pp. 1171-1178.
[17] Chang H., Shih Ch.M., Simulation and optimization for power
plant flue gas CO2 absorption-stripping systems, Separ Sci Technol,
40, (2005), pp. 877-909.
[18] Stichlmair J., Bravo J.L., and Fair R.J., General model for
prediction of pressure drop and capacity of countercurrent
gas/liquid packed columns, Gas Sep Purif, 3, (1989), pp. 19-28.
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UDC 614.844+621.227
THE USAGE OF HIGH SPEED IMPULSE LIQUID JETS FOR PUTTING OUT OF
GAS FLARES
Semko A.N., Beskrovnaya M.V., Yagudina N.I.
Donetsk National University Donetsk, Ukraine
Abstract. The researches results of gas flame suppression by
high speed pulse liquid jets which are generated
powder pulse hydro cannon are shown in this article. The
velocity of the pulse jet was depended on charge energy and it
ranged from 300 to 600 m/s. The flow photographing was held. The
head jet velocity right near the gas flame was measured by laser
non-contact measuring instrument. It is shown, that the high-speed
cloud of splashes with the big cross-section is formed around the
pulse liquid jet of high speed. This cloud effectively forces down
a flame of the gas flame on distances 5 - 20 m from
installation.
Key words: suppression, gas torch, high speed pulse liquid jet,
powder pulse hydro cannon, measurement of
jet speed Introduction Fire extinguishing represent a
complicated man-caused emergency. Response actions to
such an emergency require substantial financial expenditure and
involvement of a great number of firefighting equipment units and
manpower. Open blowouts as for their power level are divided into
[1]:
- small-scale with gas output less than 0,5 mln m3 per day and
oil output less than 100 t per day; - medium-scale with gas output
(0,51,0) mln m3 per day and oil output (100300) t per day; -
powerful with gas output (1,010,0) mln m3 per day and oil output
(3001000) t per day; - high-power with gas output more than 10 mln
m3 per day and oil output more than 1000 t per day. Practice shows
that fire and accident occurrence in oil and gas wells amounts on
average to
0,12 cases in 100 wells [2]. For instance, in the fields based
in Texas number of blowouts during prospecting drilling amounts to
approximately 244, during development drilling on a well it makes
up 180, during well completion 64, during well work over (also
called reworking) 197, during well operation 85. In the fields
located on American continental shelf, number of blowouts is lower
and makes up respectively 45, 49, 25, 23 and 12. It is due to a
smaller quantity of wells and to the usage of more reliable well
casing design and down hole and wellhead equipment.
1. Modern methods of putting out of gas blowout However, cases
of fires in the gas fields take place [3], the causes are any
source of ignition: - sparks from stones being thrown and equipment
in an emergency, - lightning, - failure of electrical equipment, -
sparks at using steel tools in the course of emergency work, etc.
At least ten different methods of fire extinguishing of oil and gas
blowouts have been
developed because of an outstanding complexity of the technical
problem on one hand, and of limited efficiency of each method on
the other hand [4]. In the paper [5] are provided main methods of
putting out of gas flame fires according to their type:
- water bull heading into the well or closing of preventer
stopcock and blowout prevention equipment; - putting out by jets of
gas-water firefighting cars;
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- impulse delivery of powder by special setups; - water jets
from carriage hoses; - explosion of high explosive charge; -
vortex-powder method; - fire extinguisher powder from firefighting
cars; - combined method; - drilling of inclined well and special
solution bull heading (also called injection). The carriage barrels
(hydraulic monitors), gas-water firefighting cars (AGVT-100 and
AGVT -150) and pressure-operated powder flame-arresters
(PPP-200) are widely used in Ukraine and in other CIS countries for
the purpose of fire extinguishing in open blowouts [4].
Quenching of fires and oil and gas fountains is a complex
man-made disaster, coupled with significant financial costs and the
need to attract a large number of fire-fighting equipment and
personnel [6]. Several different methods that take into account the
diversity of specific situations and the technical complexity of
the problem, designed for extinguishing fires of oil and gas
fountains [6, 7]. In Ukraine and CIS the fire monitors
(hydromonitors), gas-extinguishing vehicles AGVT-100 and AGVT-150,
pneumatic powder flame-suppressor SPT-200 are most often used in
fire-fighting of gushers [4].
Fire monitors are used in fire fountains of small capacity, as
they must be located at a distance of 10 - 15 m, which is not
permissible with a strong thermal radiation from a fountain with a
large flow rate (fig 1). The supply of water jets is carried out in
two stages to extinguish of fountains of average power when several
fire monitors are used. For a long time this method takes a leading
place in extinguishing of gas fountains. In this technique, a jet
of water is supplied from the fire monitors at the wellhead, i.e.
at the base of the fountain. Then water jets synchronously lift up
the pillar of fire to his complete liftoff. Portable fire monitors
or trunks installed on the tank chassis - setting GPM-64, are used
for this purpose [7]. In the Czech Republic the installation of
this type has been modernized under the name SPOT-55 [8]. It has
been successfully used to extinguish fires fountains and other
types of fires.
Automobiles of gas-water extinguishment AGVT-100 and AGVT-150
are applied for fighting fires of all kinds of fountains, but more
often for fighting fires of powerful fountains [5] (fig 2).
Gas-water jets that are generated by these installations are a
mixture of exhaust gases of turbo-jet engine and sprayed water.
About 60% water and 40% of the gas are contained in the gas-water
jet; the oxygen concentration is not more than 14% at the outlet of
the nozzle. In process of removal from the nozzle oxygen content
increases and equal to 17-18% in the area of extinguishing at a
distance of 12-15 m. The water is partially vaporized in the
exhaust gas jet and into the dispersed state in the combustion
zone. It was established experimentally that the finely dispersed
gas-water jet has a high cooling effect. For example, when applying
60 l / s water (AGVT-100) for 5 minutes, the temperature of flowing
wellhead equipment decreases from 950 to 100-150 C. The quenching
efficiency in this way depends on the water content in the jet,
which is equal to (55-60) l/s. Analogous setup under the name Big
Wind was developed in Hungary, also known as T-34 with Mig-21
engines, which was used to extinguish fires of fountains in Kuwait
[6].
Pneumatic powder flame-suppressor SPT-200 are used for fighting
fires of fountains of high power [4]. Great contribution to the
theoretical and practical development of this method extinguishing
of oil and gas fountains was made by [9, 10]. The fire was
extinguished by spray powder which was ejected out of the barrel
with compressed gas. Fire extinguishing is performed by the
atomized powder, which is ejected from the barrel with compressed
gas. Extinguishing powder concentration is impulsive generated in
the combustion zone of the fountain for a short time (1 - 2) with a
directional peak emission by installation [7].
This principle is implemented in installations on the basis of
chassis of tank T-62 "Impulse-1", "Impulse-2", "Impulse-3" and
"Impulse-Storm" [7] (fig. 3). Machines have from 15 to 50 barrels
each of which is charged to 30 kg of extinguishing powder. The
installation "Impulse-Storm" is able to deliver to the seat of fire
1.5 tons of fire extinguishing powder in 4 seconds. This allows to
create powerful extinguishing impact simultaneously over the entire
area or volume. The main difference
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of this installation is a powerful percussive effect on the seat
of fire in the compound with extinguishing effects produced by
special powder formulations. The optimal distance for fighting
fires in this way is about 15 m.
Method of detonation of the explosive charge, which creates a
shock wave of high speed (up to 1000 m / s), which disrupts the
flames and extinguish the fire [11], not rarely is used to
extinguish fires of fountains. Explosive charge is supplied at the
mouth of the borehole or a steel rope thrown over the blocks
brace-suspended, or on a cart with a cantilever on rail tracks laid
to the mouth of the borehole. The main disadvantages of this method
are high risk, high volume and complexity of the preparatory work,
as well as a large amounts of explosive substances (100-1000
kg).
New highly efficient way of extinguishing gas and oil fountains
with vortex rings, which are created by distributed explosive
charge, is developed at the Institute of Hydrodynamics of the USSR
Academy of M.A. Lavrentyev [12]. According to the authors, the main
advantage of this method is the simplicity and the possibility of
quick implement at application of small amounts of extinguishing
agents.
In work [13] different ways of extinguishing intensive local
fires (wood piles, boxes, oil and gas fountains, etc.) are
analyzed, and the conclusion that modern mechanical, pneumatic,
hydraulic fitting of supply of the extinguishing agents do not
provide the operational firefighting due to the large time that
required for the delivery and deployment of firefighting equipment,
as well as to achieve the desired mode [14], is made. The existing
firefighting machinery is unable to handle with the developed fire
due to low parameters of the jet quenching: power, speed, range,
area of the front cover, the penetrating power. Multilateral
installation of impulsive feed of the fire extinguishing agents on
the basis of chassis of tanks, trailers, carriages, jeeps, are the
most promising for solutions of such problems, fig. 4 shows the
project of such installation, that can extinguish the flare by
impulse high-speed jets (fig 4). Impulsive installation has shown
their ability to not only put out high-output fountains, but also
to prevent large-sized gas environment from fire and explosion.
In this paper we propose a method of extinguishing the burning
fountains by means pulsed high speed liquid jets, which generates a
pulsed water jet with tapered conical nozzle [15]. Application of
tapered nozzle allows increasing velocity of pulsed jet of fluid,
and its range. Pulse jet feature is that for some time the liquid
jet flows with almost constant rate of about 300 m/s from the
nozzle jet. The high speed of the jet contributes to the formation
around it the finely divided high speed cloud, which effectively
extinguishes the torch. In work the preliminary experimental
studies of extinguishing flames in such a way that have been
confirmed experimentally, were carried out.
2. Promising areas of development of gas blowout extinguishing
devices Through all times the most available and simple
fire-fighting resource has been water. Water
is widely used in firefighting practice. It is evident that
among gas blowout extinguishing mediums water is the most used
agent compared to other extinguishing means due its availability,
cheapness, simple delivery and use, as well as its high fire
extinguishing properties.
The most promising fire-fighting method is the using of
fine-water mist. The main mechanism of putting out the fire by
fine-water mist is cooling of burning material and formation of a
steam cloud, which localizes the burning center. If the drops do
not have enough kinetic energy, they will not be able to overcome
the barrier of convective stream of hot gas, which is generated by
flame, and as the result will not be able to reach the flame
surface and neutralize this process. In this case fine-water mist
could only be used as an auxiliary mean and not the main
fire-fighting method. The drop diameter influences mainly the
effectiveness of putting out procedure. Decreasing of drop
diameters in fine-water mist can considerably decrease water rate
necessary for putting out of the flame. At the same time decreasing
of particle size obstructs maintenance of drop high speed and
promotes faster drop evaporation in zone, which is previous to
flame.
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This factors decrease the effectiveness of fine-water mist
putting out. The analyses of different authors works prove that
optimal drop diameter is equal to )150100( d mkm [17].
For water delivery from safety distance to the burning flame it
is necessary to support the high speed at firefighting device
output. Calculated value of this speed should take into account
losses during the jet flight and provide required speed directly
before blow out for overcoming of convective stream as well as
separated impact on blow out [18, 19]. The equilibrium position of
blow-out flame drifts with flow with increasing of the flow speed.
This is the substance of separated impact. The recent aero-team
ignitable mixture becomes more and more diluted with moving away
due to reciprocal diffusion with steam. This mixture speed
decreases proportionally to the dilution degree and exceeds the
burning speed at some critical steam value; the jet is broken for a
moment, and the flame is driven upward and separated from it.
The analysis of specific data concerning flame character changes
with increasing of the speed of burning jet shows that separation
of diffusion flame is going on at 80 100 m/s. It is evident that
mentioned values of speed from safety distance (110 130 m) could be
guaranteed with high speed liquid jets. These jets are generated by
devices which are similar to impulse hydro cannons. 3
3. The schemes of the experiment Fig. 5 is a schematic diagram
of the experiment (fig. 5). From the powder IWC 1, which was
located at a predetermined distance from the torch 3, a
series of shots of high-speed water jets 2 have been produced
towards the gas torch. The burnout of the torch was qualitatively
recorded, as well as the speed of high-speed jet was measured
directly in front of torch using non-contact laser speed detector,
which consists of two blocks 4 and 5 [20]. The mass of a powder
charge and the distance from the IWC to the torch varied during the
experiments, the last one was measured by a tape measure. Changing
of these two parameters allows adjusting of impulse jet speed
before the torch in a wide range from 60 to 430 m/sec, registered
in the experiments. The aiming was performed by means of a special
laser sight, which was mounted on the trunk of impulse water
cannon. The speed of impulse jet liquid at which the quenching of
the gas torch occurred was measured during the experiments. Speed
measuring device allowed recording the speed in the range from 50
to 3000 m/sec.
A series of shots from a distance of 5, 10 and 12 for powder
charges with a mass of 5, 10 and 15 g was conducted. In the
experiments, the rate of head pulsed jet of liquid before the torch
was measured, photographing and video shooting of jet at different
stages of its spreading was carried out (fig. 6 ). The results are
presented in Table 1. (tab. 1)
It can be concluded from the analysis of the experimental
results that the rate of the impulse liquid jet head which provides
for the hearth extinguishing of the model fire gas fountain ranges
from (80 90) m/sec, which confirms the experimental studies
obtained by other authors.
A series of experiments in which the dependence of the rate of
the head of pulsed jet from the traveled distance was measured, was
conducted. Some results of these experiments are shown in Table. 2
and in Fig. 6 in which dependency diagrams the velocity of the jet
of the head the distance traveled are depicted.(tab. 2, fig. 7)
It is clear that the testimonies of 2-5 modules are close and
differ markedly from the testimony of the 1st module, which was
closest to the IWC at a distance of 1 m from the installation.
These differences in the r testimonies of the modules are connected
solely with features of the expiration of pulsed jet of fluid from
IWC. The jet IWC begins to run with almost zero speed, which
rapidly increases, reaches a maximum and then decreases relatively
slowly. Therefore, the 1st module detects the velocity of the head
jet at the beginning of expiration, which is far from the maximum
and increases during expiration. Velocity of the head jet reaches a
maximum at the approach to the second module, the distance to which
is 2 m. In the future, the speed of the head of jet is slightly
reduced due to the air diffusion. The results of measuring the
velocity of the head of jet on the stationary section are in good
agreement between itself. Maximum estimated speed of the jet
discharge for IWC in the specified mode is about 350 m/sec.
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The specific nature of the dependence of the outflow speed of
the liquid jet of hydro-cannon from time (a fast increase in the
beginning of outflow from zero