CN101050391B - Sulfur resisting transform technique under low water / gas for gasifying powdered coal - Google Patents
Sulfur resisting transform technique under low water / gas for gasifying powdered coal Download PDFInfo
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- CN101050391B CN101050391B CN 200710087573 CN200710087573A CN101050391B CN 101050391 B CN101050391 B CN 101050391B CN 200710087573 CN200710087573 CN 200710087573 CN 200710087573 A CN200710087573 A CN 200710087573A CN 101050391 B CN101050391 B CN 101050391B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
This invention relates to a process for gasifying pulverized coal at a low water/gas ratio by sulfur-tolerant conversion. The process comprises: introducing crude coal gas into a gas-liquid separator, heating the crude coal gas exhausted from the separator top to 180-220 deg.C, removing impurities, sending to a first reactor, and performing sulfur-tolerant conversion. In the first reactor, the water/gas volume ratio at the inlet is 0.15-0.20; the temperature at the inlet is 180-220 deg.C; the hot-point temperature of the bed layer is 330-400 deg.C; the space velocity is 6000-9000 h<-1>; the reaction pressure is 3.0-4.0 MPa; the CO volume content in the crude coal gas at the inlet is 55-70%. The process has such advantages as low water/gas ratio and low energy consumption.
Description
Technical field
The present invention relates to a kind of is the low water of the coal gasification/gas sulfur resistant conversion process of raw material with the coal, be the sulfur resistant conversion process that the shell coal gasification is produced ammonia synthesis gas, oxo-synthesis gas and town gas, specifically relating to a kind of is that raw material adopts the shell coal gasification to produce the sulfur resistant conversion process that is used for first reactor of ammonia synthesis gas, oxo-synthesis gas and town gas with the raw gas.
Background technology
Entered since 21 century, owing to the influence that is subjected to be becoming tight petroleum resources day, the coal chemical industry of China has changed a Rapid development stage over to, engineering projects such as gasification system ammonia, system methyl alcohol, coal synthetic gasoline start comprehensively, and have introduced the Dutch Shell Co. Ltd of many covers development powder coal gasifying process (being called for short the Shell fine coal gasification process) in succession.Compare with " Texaco " water coal slurry pressure gasification technology, low although the Shell fine coal gasification process has the ature of coal requirement, active principle content height (CO+H in the synthetic gas
289%), raw coal and oxygen depletion are low, characteristics such as the little and working cost of environmental pollution is low, but since in the unstripped gas that makes of Shell gasification CO up to more than 60%, like this, when water/gas less, when the hot(test)-spot temperature of bed is higher, not only increase the weight of the CO conversion load of sulfur-resisting transformation system, but also may cause the generation of methanation side reaction.Therefore, the control of the first reactor reaction degree of depth and bed hot(test)-spot temperature, the particularly control problem of methanation side reaction just become the key that is used for synthetic ammonia or methyl alcohol or hydrogen manufacturing production that can the Shell coal gasifying process successful.
At present, in the technology of the number cover Shell coal gasification system gas that China introduces, for fear of the problem of methanation side reaction, adopted the flow process of Gao Shui/gas conversion mostly, water/gas is generally greater than 1.1.Improve water/gas, though the generation that helps suppressing the methanation side reaction still, but when one section catalysts loadings calculating is more than needed, because CO content height in the unstripped gas, the impellent of reaction increases, the degree of depth of reaction also increases with the bed hot(test)-spot temperature and increases, and causes the bad result of bed " temperature runaway ".Therefore for reducing the temperature of reaction of first reactor, many factories adopt the way that increases water/gas (water/gas of some factory even be increased to 1.8) that furnace temperature " is forced down ", so not only cause energy to waste greatly, and under Gao Shui/gas and hot conditions, the decline of meeting accelerator activator performance and aging, make catalyzer shortening in work-ing life, be difficult to guarantee the long-term operation of production equipment.
The situation of the water vapour undersupply that exists at many factories, Xu Banghao has delivered in " chemical fertilizer industry " the 33rd the 4th phase of volume and has been entitled as " selection of shell coal gasification carbon monodixe conversion technology " literary composition, the situation of the middle pressure steam shortage that exists at Liuzhou fertilizer plant in the literary composition, processing condition to each section reaction in the shift process have been carried out new design, and have adopted five sections CO conversion process altogether in this design.As can be seen, in water/gas=0.25 of first shift converter, temperature in is 220 ℃ from process flow sheet, and total dry gas amount is 98783m
3/ h, reaction pressure is 3.56MPa, inlet CO content is 67.44%, the CO content of outlet is 37.39%, adopts this operation can save steam 3.6t/h, saves recirculated water 230t/h, reduce daily process cost, yet must increase equipment such as saturator, hot-water tower, the low pump of saturated Tata.
In " the middle nitrogenous fertilizer " in May, 2004, disclose and be entitled as " discussion " a literary composition of methanation side reaction problem in the shell fine coal gasification process, the influence of water/gas to the methanation side reaction has been discussed in the literary composition, the result shows that the methane content of outlet drops to minimum when water/gas=1.0; Pressure is low more with also having mentioned in the eight-legged essay, and the methane content of outlet is low more, and is low more with the hot(test)-spot temperature that bed also has been described in the eight-legged essay, and the methanation side reaction is also just low more.
In " the chemical fertilizer design " in August, 2005, disclose and be entitled as " segmentation of transformationreation research in the shell coal gasification Ammonia Process " literary composition, ratio when calculating water outlet/gas balance by kinetic equation in the literary composition, with the bed hot(test)-spot temperature, the variation relation of the content of CO and catalyzer loading amount during balance.Calculation result shows, when choosing low water/gas 0.2-0.25 and low temperature in 200-220 ℃, air speed is 2500-3000h
-1The time, can control the degree of depth of " Shell " coal gasification system solid/liquid/gas reactions and reduce the content of the first reactor outlet methane.Yet show at the actual industrial operation result, when the air speed of reaction when being lower than 3000h-1,,, reaction can not in time take out of because emitting a large amount of heat even water/gas is 0.27 much larger than 0.20 of research, heat of reaction is assembled also can cause the methanation side reaction to take place, bed temperature waterfall is risen.So in actual industrial utilization, when water/gas=0.20, because air speed is lower, can not reach the effect that reduces bed temperature, the degree of the side reaction of methanation simultaneously is higher.
Summary of the invention
The purpose of this invention is to provide the low water of a kind of shell coal gasification/gas sulfur resistant conversion process.
The invention provides the low water of a kind of coal gasification/gas sulfur resistant conversion process, described technology is the low water of shell coal gasification/gas sulfur resistant conversion process, raw gas at first enters gas-liquid separator, then the raw gas that comes out from the separator top is heated to 180-220 ℃, after entering the detoxification groove and removing decon, enter first reactor and carry out transformationreation, wherein the aqueous vapor volume ratio of first reactor inlet is 0.15-0.20, temperature in is 180-220 ℃, the hot(test)-spot temperature of first reactor bed is 330-400 ℃, and air speed is 6000-9000h
-1, reaction pressure 3.0-4.0MPa, the volume content of butt CO is 55-70% in the raw gas that enters first reactor inlet, described process using CO sulfur-tolerant water gas shift catalyzer.
The present invention also provides a kind of technology, wherein raw gas that comes out from the separator top and water vapour are heated to 180-220 ℃ jointly, after entering the detoxification groove and removing decon, enter first reactor and carry out transformationreation, the aqueous vapor volume ratio that it is characterized in that described first reactor inlet is 0.15-0.20, temperature in is 180-220 ℃, and the hot(test)-spot temperature of first reactor bed is 330-400 ℃, and air speed is 6000-9000h
-1, reaction pressure 3.0-4.0MPa, the volume content of butt CO is 55-70% in the raw gas that enters first reactor inlet, described process using CO sulfur-tolerant water gas shift catalyzer.
The butt volume content of the conversion gas CO that comes out from first reactor is 40-50%.
The water of first reactor inlet/gas volume ratio is 0.180～0.20.
The temperature in of first reactor is 190-200 ℃.
Hot(test)-spot temperature is 350-360 ℃.
The air speed of the first above-mentioned reactor is 6000-7000h
-1
The first reactor reaction pressure is 3.3-3.6MPa.
It has been generally acknowledged that in the prior art that water/gas is important control means of regulating the transformationreation index, when water/gas is higher, the main transformationreation that CO takes place, methanation side reaction degree is low, therefore in the prior art usually all with water/gas control built in more than 1.0, yet among the present invention when the volume ratio of the water/gas of first reactor inlet in 0.18～0.20 scope, with respect to prior art, methanation side reaction degree is still very low, volume ratio owing to the water/gas among the present invention has reduced with respect to prior art much simultaneously, so adopt technology of the present invention also to play energy saving purposes.
Through repeatedly discovering repeatedly, when the hot(test)-spot temperature of first reactor bed high more, the methane content of outlet also increases thereupon, simultaneously when the hot(test)-spot temperature of bed surpasses 400 ℃, the methanation side reaction is just fairly obvious, so the inventor is controlled at 330～400 ℃ with the hot(test)-spot temperature of bed, preferred 350～360 ℃.
In addition, the hot(test)-spot temperature of bed and first reactor inlet temperature have very big relation, increase along with first reactor inlet temperature, the hot(test)-spot temperature of bed also increases, the degree height of methane side reaction, so the temperature in of first reactor should be controlled at 180～220 ℃, preferred 190～200 ℃.
The contriver finds that through repetition test repeatedly the air speed of first reactor is big more, and methane side reaction degree is more little, so the present invention brings up to 6000-9000h with the air speed of first reactor
-1, preferred 6000-7000h
-1, in existing research, this was not related to.
Adopt processing condition of the present invention, by controlling the water/gas of first reactor, temperature in, air velocity, and the performance of catalyzer, the catalyzer of first reactor can be moved under the demulcent processing condition, reach the purpose in the work-ing life that prolongs catalyzer, industrial long-term operation is had important practical significance.In addition, can also reach under the conversion condition of high concentration CO, the butt volume content of growing amount that makes byproduct methane is less than 0.05%.
For realizing the processing condition among the present invention, adopt New CO sulphur-resistant transformation catalyst of the prior art, the QDB-04 type CO sulfur-resistant transformation catalyst of preferred Qingdao connection letter chemical production is referring to the advertisement of 2006 " chemical fertilizer design ".
Because the sulfur-resisting transformation novel process that raw gas can be implemented under the low water of first reactor/gas condition behind this process implementing, can reduce the water/gas of transformationreation significantly, energy-saving effect is remarkable.Producing 180000 tons of synthetic ammonia per year with one is example, compares with Gao Shui/gas " Shell " coal gasification gas-made technology that present industry is adopted, and required water/gas can reduce about 0.5 at least, and a year economic benefit rises to more than 25,000,000 yuan at least.
Description of drawings
Fig. 1 shell coal gasification sulfur resistant conversion process.
Second kind of sulfur resistant conversion process of Fig. 2 shell coal gasification.
Embodiment
Embodiment 1
Raw gas from " Shell " coal gasification operation, directly enter gas-liquid separator, the raw gas that comes out from the separator top is heated to 190 ℃, after entering the detoxification groove and removing decon, enter first reactor and carry out transformationreation, the volume content that enters butt CO in the raw gas of first reactor inlet is that 61%, the first reactor inlet temperature is 190 ℃, water/gas volume is 0.15, air speed 6000h
-1Reaction pressure is 3.0MPa, and the hot(test)-spot temperature of first reactor bed is 330 ℃, is 45% from one section conversion gas CO that comes out with respect to the content of butt, entering the transformationreation that follow-up workshop section carries out, is 0.01% as the output of the methane of byproduct of reaction with respect to the volume of butt finally.
Embodiment 2
Raw gas from " Shell " coal gasification operation, directly enter gas-liquid separator, raw gas that comes out from the separator top and water vapour are heated to 200 ℃ jointly, after entering the detoxification groove and removing decon, enter first reactor and carry out transformationreation, enter wherein that butt CO volume content is that 63%, the first reactor inlet temperature is 200 ℃ in the raw gas of first reactor inlet, water/gas volume ratio is 0.20, air speed 7000h
-1Reaction pressure is 3.6MPa, and the hot(test)-spot temperature of first reactor bed is 380 ℃, is 40% from one section conversion gas CO that comes out with respect to the content of butt, entering the transformationreation that follow-up workshop section carries out, is 0.3% as the output of the methane of byproduct of reaction with respect to the volume of butt finally.
Embodiment 3
Raw gas from " Shell " coal gasification operation, directly enter gas-liquid separator, the raw gas that comes out from the separator top is heated to 190 ℃ jointly with the water vapour that comes out from medium pressure boiler, after entering the detoxification groove and removing decon, enter first reactor and carry out transformationreation, enter wherein that butt CO volume content is 69% in the raw gas of first reactor inlet, water/gas volume ratio is 0.18, first reactor inlet temperature is 190 ℃, and the aqueous vapor volume ratio is 0.20, air speed 7000h
-1Reaction pressure is 3.6MPa, and the hot(test)-spot temperature of first reactor bed is 355 ℃, is 50% from one section conversion gas CO that comes out with respect to the content of butt, enter the transformationreation that follow-up workshop section carries out, finally the output as the methane of byproduct of reaction is 0.12%.
Embodiment 4
Raw gas from " Shell " coal gasification operation, directly enter gas-liquid separator, the raw gas that comes out from the separator top is heated to 210 ℃ jointly with the water vapour that comes out from medium pressure boiler, after entering the detoxification groove and removing decon, enter first reactor and carry out transformationreation, the volume content that wherein enters butt CO in the raw gas of first reactor inlet is that 66%, the first reactor inlet temperature is 210 ℃, the aqueous vapor volume ratio is 0.20, air speed 6000h
-1Reaction pressure is 3.8MPa, the hot(test)-spot temperature of first reactor bed is 360 ℃, the CO of inlet is 66% with respect to the butt volume content, is 46% from one section conversion gas CO that comes out with respect to the content of butt, enter the transformationreation that follow-up workshop section carries out, finally the output as the methane of byproduct of reaction is 0.10%.
Embodiment 5
Raw gas from " Shell " coal gasification operation, directly enter gas-liquid separator, then the raw gas that comes out from the separator top is heated to 200 ℃, after entering the detoxification groove and removing decon, enter first reactor and carry out transformationreation, the volume content that wherein enters butt CO in the raw gas of first reactor inlet is 70%, directly enters gas-liquid separator, the aqueous vapor volume ratio of first reactor inlet is 0.20, air speed 8000h
-1Reaction pressure is 3.7MPa, the temperature in of first reactor bed is 200 ℃, hot(test)-spot temperature is 370 ℃, the CO of inlet is 70% with respect to contents on dry basis, is 48% from one section conversion gas CO that comes out with respect to the content of butt, enters the transformationreation that follow-up workshop section carries out, and finally the output as the methane of byproduct of reaction is 0.15%.
Claims (1)
1. a coal gasification hangs down water/gas sulfur resistant conversion process, described technology is the low water of shell coal gasification/gas sulfur resistant conversion process, raw gas at first enters gas-liquid separator, then the raw gas that comes out from the separator top is heated to 190 ℃ jointly with the water vapour that comes out from medium pressure boiler, after entering the detoxification groove and removing decon, enter first reactor and carry out transformationreation, water/gas the volume ratio that it is characterized in that described first reactor inlet is 0.18, temperature in is 190 ℃, the hot(test)-spot temperature of first reactor bed is 355 ℃, and air speed is 7000h
-1Reaction pressure 3.6MPa, the volume content of butt CO is 69% in the raw gas that enters first reactor inlet, the QDB-04 type CO sulfur-resistant transformation catalyst of described process using Qingdao connection letter chemical production, the butt volume content of the conversion gas CO that comes out from described first reactor is 50%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2014259567B2 (en) * | 2013-11-25 | 2018-12-13 | Clariant International Ltd. | Treatment of synthesis gases from a gasification facility |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| MY154030A (en) † | 2009-03-19 | 2015-04-30 | Shell Int Research | Process to prepare a hydrogen rich gas mixture |
| CN101768488B (en) * | 2009-12-07 | 2013-05-29 | 赛鼎工程有限公司 | Technique for producing coal natural gas by utilizing crushed coal slag through gasification |
| CN101955154A (en) * | 2010-10-25 | 2011-01-26 | 付元波 | Isothermal conversion process method for high-concentration carbon monoxide conversion |
| CN102001623B (en) * | 2010-11-01 | 2012-08-29 | 中国五环工程有限公司 | Process method for converting entrained-bed coal gasification high-concentration carbon monoxide |
| CN102002403B (en) * | 2010-11-09 | 2013-06-19 | 中国石油化工股份有限公司 | Low water-air ratio and middle water-air ratio carbon monoxide (CO) conversion process |
| CN102102040B (en) * | 2010-12-20 | 2014-03-05 | 中国石油化工股份有限公司 | Ash coal gasification low water/gas ratio total low temperature chilling CO sulfur resistant shifting technology |
| CN102337160B (en) * | 2011-08-30 | 2013-09-18 | 中国石油化工股份有限公司 | High-water-steam-ratio saturated hot water tower split CO transformation process |
| CN102337159B (en) * | 2011-08-30 | 2013-09-04 | 中国石油化工股份有限公司 | Saturated hot water tower high-water-steam-ratio CO transformation process |
| CN102337161B (en) * | 2011-08-30 | 2013-12-04 | 中国石油化工股份有限公司 | Low water-to-gas ratio serial saturation tower and hot water tower CO conversion process |
| CN102337162B (en) * | 2011-08-30 | 2013-11-27 | 中国石油化工股份有限公司 | Low-water-steam-ratio saturated hot water tower CO transformation process |
| CN102491268B (en) * | 2011-12-10 | 2015-05-06 | 青岛联信催化材料有限公司 | Control method for stabilizing high-density carbon monoxide virgin gas transformation process |
| CN102732329A (en) * | 2012-06-12 | 2012-10-17 | 中国石油化工股份有限公司 | Fine coal gasification product crude synthetic gas CO sulfur-tolerant shift technology |
| CN102888253B (en) * | 2012-10-08 | 2014-02-12 | 中国石油化工集团公司 | Low-moisture low-variable serial saturation tower thermal CO transformation technology |
| CN102888252B (en) * | 2012-10-08 | 2014-02-12 | 中国石油化工集团公司 | Saturation tower/isothermal furnace series/heat isolation furnace CO transformation technology |
| CN103449365B (en) * | 2013-04-28 | 2015-09-30 | 山东齐鲁科力化工研究院有限公司 | Process for converting high-concentration CO-tolerant sulfur and device thereof |
| DE102013224037A1 (en) | 2013-11-25 | 2015-05-28 | Siemens Aktiengesellschaft | Preparation and conditioning of synthesis crude gases |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2402890A (en) * | 2003-05-16 | 2004-12-22 | Gen Motors Corp | Systems and methods for carbon monoxide clean-up |
| CN1830756A (en) * | 2006-03-16 | 2006-09-13 | 五环科技股份有限公司 | Secondary transformation technological method of high concentration carbon monooxide |
-
2007
- 2007-03-30 CN CN 200710087573 patent/CN101050391B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2402890A (en) * | 2003-05-16 | 2004-12-22 | Gen Motors Corp | Systems and methods for carbon monoxide clean-up |
| CN1830756A (en) * | 2006-03-16 | 2006-09-13 | 五环科技股份有限公司 | Secondary transformation technological method of high concentration carbon monooxide |
Non-Patent Citations (4)
| Title |
|---|
| 李海洋，纵秋云等.shell煤气化工艺中甲烷副反应的控制研究.上海化工31 8.2006,31(8),17-18. |
| 李海洋,纵秋云等.shell煤气化工艺中甲烷副反应的控制研究.上海化工31 8.2006,31(8),17-18. * |
| 纵秋云，王迎春.shell粉煤气化制氨工艺中变换反应的分段研究.化肥设计43 4.2005,43(4),15-17. |
| 纵秋云,王迎春.shell粉煤气化制氨工艺中变换反应的分段研究.化肥设计43 4.2005,43(4),15-17. * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2014259567B2 (en) * | 2013-11-25 | 2018-12-13 | Clariant International Ltd. | Treatment of synthesis gases from a gasification facility |
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