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mermaid332

至尊木虫 (著名写手)

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虫号: 130955
注册: 2005-12-12
性别: GG
专业: 物理有机化学

[交流] 200金币求下文改错，谢谢了

Preparation of novel catalyst and research of new technology for gasoline hydrodesulfurization

Abstract: A novel multi-functional catalyst was prepared and used for hydrodesulphurization of FCC gasoline. The results showed that the catalyst with Mo-Co-Ni multi-metal components and additives increase the selectivity of hydrodesulphurization and reduce the amount of the low olefin. Dual purpose, hydrodesulphurization and reduction of octane number loss, were achieved. Sulfur content in FCC gasoline decreased from 1200 μg/g to 115 μg/g and olefin content fall to 20.5 v% from 44.2 v%. The RON loss is 0.5 units. The stability test for 2000 hours indicated that the catalyst is very stable. The catalyst was characterized with strong adaptability concluded from the adaptability test for different raw materials.
Key words: desulfurization; olefin; catalyst; octane number
1. Introduction
Harmful substances such as sulphides and CxHy came from automobile exhaust emissions would have caused serious pollutions to the environment. In order to reduce the pollution caused by automobile exhaust, the gasoline was cleaning in recent years. Olefins, aromatics and sulfides were thought as the harmful substances, so their contents in gasoline were limited repeatedly [1-3]. Each standard about the contents are shown in Table 1. Every country has been doing their best to reduce the harmful substances amount.
In China, more than 90% mass fraction of sulfur and more than 98% volume fraction of the olefins in motor gasoline are from the FCC (Fluid Catalytic Cracking) gasoline [4-6]. Conventional hydrodesulphurization (HDS) method is effective to remove organic sulfur form FCC gasoline, but the alkenes hydrogenation easily generate low-octane saturated group that results a sharp decline of the octane number. New HDS method is that the FCC gasoline was divided into LCN (Light fraction) and HCN (Heavy fraction), HCN was desulfurized and hydrogenated. The method largely avoided the hydrogenation of the high-octane light olefin in LCN. However, in HDS process, the high-octane olefin in HCN was saturated which resulted the loss of the octane number. Therefore, it is important to develop high selective HDS catalyst for reducing saturation in the hydrogenation process of olefins to control the octane number loss. The foreign new technology of FCC gasoline hydrodesulphurization, such as the technology from Prime-G & Prime-G+(IFP), SCANFining & OCTGAIN (ExxonMobil) and ISAL (UOP), has poor adaptability to the FCC gasoline of high-sulfur (1000~1500 μg/g), high olefins (40~55 v%), low aromatics (13~20 v%) in China. It is necessary to develop new olefin FCC gasoline hydrodesulphurization technology and new catalyst.
In this paper, it is the emphases to reduce the octane number loss in the process of FCC gasoline hydrodesulphurization. The components in catalyst were determined. Catalyst performance and stability were studied in the hydrodesulphurization of FCC gasoline. The hydrogenation process conditions were optimized.
2. Experimentation
2.1. Preparation of Catalysts
In order to improve the selectivity of hydrodesulphurization catalyst and to reduce the loss of octane number in the HCN hydrogenation process, the support of catalyst being developed should have large specific area and concentrated pore distribution that make the active metal distribute evenly. MoO3-CoO metal components was chosen because excellent HDS selectivity over them. Additives were added to increase the HDS selectivity. Two catalysts were developed, one with low metal content, the other with high metal content.
The dispersion of active metal components in the acidic carriers is another important parameter that affects the catalyst activity and selectivity of hydrogenation. Therefore, it is best when the metal components can spread out in the greatest form of single-molecule in the carrier. The catalyst prepared by impregnation could disperse well. First, the carrier of the catalyst was obtained by squeezing. Then the precursors of Mo, Co and Ni in proportion were introduced to the catalyst. After drying and calcinations, the required catalyst is obtained. The process is shown in Figure 1.
2.2. Gasoline fraction cutting
Data shows that the sulfur contents were re-presented with the fraction of variable incremental distribution in two typical FCC gasoline in China, one is high-sulfur content (1635 μg/g) and high olefin content (53 v%), another is has medium sulfur content (806 μg / g) and medium-olefin content (47.3v%). Sulfur mainly concentrated in HCN (> 90 ℃). Ninety percent sulfur of FCC gasoline is in HCN. Olefin which is re-presented with the fraction of variable incremental distribution mainly concentrated in LCN and more than 70% olefin in FCC gasoline concentrated in LCN (90 ℃).
FCC gasoline produced by Fushun Petrochemical Company was rectified and separated as raw material. The distillation cut below 90 ℃ is the LCN with C7 fraction.
Using gas chromatography coupled atomic radiation technology (GC-AED), the form of sulfur was analyzed in whole distillate FCC gasoline, light distillate (LCN) and heavy distillate (HCN) as well as the effect of caustic washing to it. The results show that mercaptans and thiophene are the major component in whole FCC gasoline, as well as small amounts of sulfide and other sulfides. While sulfur in LCN (<90 ℃) is mainly C1 ~ C4 mercaptans and a small amount of thiophene. By caustic washing, about 90% of the mercaptan in LCN (<90 ℃) is removed. Whereas, the thiophene content remain unchanged.
2.3. Hydrogenation experiments
Hydrodesulphurization reaction takes place in a self-made continuous liquid phase fixed-bed reactor. It is characterized with temperature control, pressure control, power-off self-protection features, continuous feed and timing sampling functions. In order to ensure that the reactor has long enough constant temperature zone along the axial direction, a metal casing is placed between the reactor and the electric furnace tube. The constant temperature range is over 20 cm. Temperature control accuracy is up to ± 1 ℃. The device mainly consists of raw materials tank, micro-metering pump, heating systems, fixed-bed reactor, the product tank, temperature control system, pressure-conditioning systems, and gas flow control system. Reaction reactor is shown in Figure 2. The technology of catalyst sub-loading is used to fill the upper bed in the reactor with low metal content of the catalyst and fill the lower part with higher metal content catalyst. The aim is to get HDS reaction take place gently in catalyst bed to avoid the loss of octane number caused by over-hydrogenation of olefin saturation.
2.4. Product sweetening and reconcile
Mixture is produced by mixing the product from HCN hydro-treating with the cutting out LCN. This mixture is sent to the alkaliless deodorizing device for further sweetening process to get clean petroleum products with low-sulfur, low olefin and low mercaptan content (<10 μg / g).
2.5 Experimental Analysis of Instruments and analytical conditions
2.5.1. Determination of Sulfur
Sulfur content from raw materials and products were measured by WK-2B micro-Coulomb Instrument (Jiangsu Electro analytical Instrument Factory). WK-2B instrument micro-Coulomb is used to measure liquid micro-sample with testing conditions as follows: Carrier gas: Nitrogen, Reaction gas: Oxygen, Vaporization temperature paragraphs: 600 ℃, Combustion temperature paragraphs: 800 ℃, Stable temperature of paragraphs: 700 ℃.
2.5.2. Olefin content
The composition of FCC gasoline was analyzed by gas chromatography. OV-101 fused silica capillary (length 50m, internal diameter 0.23mm) is produced by Beijing Research Institute of Petroleum system. Column temperature: initial temperature of 33 ℃, keep for 5 min, and then rise to 50 ℃ at the rate of 1 ℃ / min, and then rise to 180 ℃ at the rate of 2 ℃ / min, keep 10min; detector temperature: 240 ℃; vaporization chamber temperature : 240 ℃; split ratio: 400: l; high-purity nitrogen as carrier gas; hydrogen as gas; air as assist gas.
2.5.3. N2 adsorption - desorption (BET)
Surface area of catalyst is measured by ASAP-2010 automatic physisorption from U.S. Micromeritics's Company. N2 adsorption temperature is 77 K. Catalyst is activated in vacuum afor 16 h under 383 K before measurement. Surface area is obtained through BET equation, using N2 adsorption isotherms.
3. Results and discussion
3.1. Catalyst component
Metal components are the active center for Hydrogenation catalyst. These active contents are mainly VIB group metal elements (Mo, W) and VIII group metal elements (Co, Ni). The activity of the Mo-Ni-P catalyst is compared with the Co-Mo-Ni catalyst and the results of desulfurization and de-olefin are shown in Figure 3. It can be seen from Figure 3 that the catalyst with Co-Mo-Ni combined as active component has high activity, which is due to the strong selectivity of the catalyst with Co-Mo as the active component and the large specific area of Ni. The appropriate amount of Ni could increase the degree of metal dispersion that could improve the hydrogenation activity of the catalyst [7, 8]. Through the study of catalytic activity, the ratio of active metals is determined and the essential nature of the catalyst is demonstrated. Results were shown in Table 2.
3.2. Optimization of the hydrogenation process conditions
It was investigated separately the impact that reaction conditions (including reaction temperature, pressure, space velocity and hydrogen-oil ratio) have on the reaction rate and the desulfurization rate of de-olefin. The results are shown in Figure 4 to Figure 7.
The impacts of reaction conditions like HCN hydro-desulfurization reaction pressure, temperature, and hydrogen oil volume ratio on the desulfurization and octane loss were examined. The optimized hydrodesulphurization reaction conditions were determined and shown in Table 3.
3.3. Effect of hydrogen sulfide in the cycle of hydrogen on hydrodesulphurization
The effect of hydrogen sulfide in circulating hydrogen on the activity reaction is studied. When the concentration of H2S in circulating hydrogen is over 0.14 v%, sulfur content of HCN after distillation HDS increased from 70μg/g to 160 μg/g. The circulating hydrogen was washed by ethanolamine (hydrogen sulfide concentration of 0.01 v%), sulfur content in HAD is 85 μg/g. The study results show that hydrogen sulfide in circulating hydrogen has significant inhibiting effect on HDS and it is necessary to remove H2S in circulating hydrogen to improve the HDS effect. Without the process that remove H2S in circulating hydrogen, the inhibitory effect that hydrogen sulfide has on the desulfurization of sulfur can be compensated by appropriately raising the reaction temperature. Under the condition of the same degree of HDS, the reaction temperature is usually to increase 15~20 ℃, and RON suffers the loss of about 0.3 units. Therefore, HDS reaction system needs to be equipped with the facilities to remove hydrogen sulfide in circulating hydrogen.
3.4. Stability Evaluation
In the optimal reaction conditions, the stability of catalyst was evaluated with 2000 h. The change of desulfurization rate and the de-olefin rate with the time in line of catalyst is shown in Figure 8. The results shown that the sulfur content of product is less than 115 μg/g, olefin content is less than 20.5 v% and RON loss is less than 1.0 units when raw FCC gasoline material from Fushun Petrochemical Company No. 1 Factory which has sulfur content of 1200 μg/g, olefin content of 44.2 v% is used in the experiments. Therefore, the catalyst is characterized with excellent HDS selectivity, activity and stability.
3.5. Sweetening Program
LCN with <90 ℃ is through the technology of alkali-free sweetening process. Then, the sweetened LCN is mixed with HCN of HDS after hydrodesulphurization. Thiol content in the mixture reduced to 10 μg/g.
3.6. Material balance and nature of the product
About 0.20% of hydrogen is consumed when HCN with > 90 ℃ heavy fraction reacting with HDS and gasoline liquid product is over of 99.4%. HCN with > 90 ℃ heavy fraction is mixed with HDS product with <90 ℃ light fraction to get a total liquid yield ≮ 99.4%.
After being treated with HDS olefin, the indicators of gasoline from Fushun Petrochemical Company No. 1 Factory are shown in Table 4. It can be seen that sulfur content and olefin content has decreased significantly. Mercaptan in the mixed oil is now below 10 μg/g after the process of alkali-free sweetening. Olefins are as low as 20.5%. Octane number loss is within one unit. The yield of liquid-gas is greater than 99%.
4. Conclusion
(1) This catalyst that used Mo-Co-Ni multi-metal components and additives achieve a high HDS selectivity and low olefin saturation effect. Two purpose of hydrodesulphurization and reduction of octane loss are realized.
(2) This catalyst was being conducted with 2000 h stability tests and the adaptability to different raw materials. The results indicated that this catalyst had good catalytic stability and adaptability of raw materials.
(3) The technology of the selective hydrodesulphurization of gasoline suit the cut-off point temperature of the light and heavy FCC gasoline fraction is about 90 ℃.
(4) The process conditions to the technology are as below: pressure is 2.0 MPa, reaction temperature is 230 ℃, space velocity is 2.18 h-1 and hydrogen oil volume ratio is 400:1.
(5) This technology could reduced the sulfur content of FCC gasoline from Fushun Petrochemical Company No. 1 Factory from 1200 μg/g to 115 μg/g and olefin content from 44.2 v% down to 20.5 v%. RON loss is 0.5 units. That has reached the expectant goal.

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没有可以拼的爹，只有拼自己了！

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fandewei

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★ ★ ★
mermaid332(金币+10, 翻译EPI+1):谢谢帮助 2010-04-18 14:03
sirljz(金币+3):谢谢交流 2010-04-19 15:54

Abstract: A novel multi-functional catalyst has been prepared and used for hydrodesulphurization of FCC gasoline. The results show that the catalyst with Mo-Co-Ni multi-metal components and additives increase the selectivity of hydrodesulphurization and reduce the amounts of the low olefin. Dual purpose, hydrodesulphurization and reduction of octane number loss, have been achieved. Sulfur content in FCC gasoline decreases from 1200 μg/g to 115 μg/g and olefin content falls to 20.5 v% from 44.2 v%. The RON loss is 0.5 units. The stability test for 2000 hours indicates that the catalyst is very stable. The catalyst is characterized with strong adaptability concluded from the adaptability test for different raw materials.
Key words: desulfurization; olefin; catalyst; octane number
1. Introduction
Harmful substances such as sulphides and CxHy come from automobile exhaust emissions would have caused serious environmental pollutions . In order to reduce the pollution caused by automobile exhaust, the gasoline has been cleaned in recent years. Olefins, aromatics and sulfides are considered as the harmful substances, so their contents in gasoline are limited repeatedly [1-3]. Each standard about the contents are shown in Table 1. Every country has been doing their best to reduce the harmful substances amount.
In China, more than 90% mass fraction of sulfur and more than 98% volume fraction of the olefins in motor gasoline are from the FCC (Fluid Catalytic Cracking) gasoline [4-6]. Conventional hydrodesulphurization (HDS) method is effective to remove organic sulfur form FCC gasoline, but the alkenes hydrogenation easily generate low-octane saturated group that results a sharp decline of the octane number. New HDS method is that the FCC gasoline has been divided into LCN (Light fraction) and HCN (Heavy fraction), HCN is desulfurized and hydrogenated. The method largely avoided the hydrogenation of the high-octane light olefin in LCN. However, in HDS process, the high-octane olefin in HCN is saturated which results the loss of the octane number. Therefore, it is important to develop high selective HDS catalyst for reducing saturation in the hydrogenation process of olefins to control the octane number loss. The foreign new technology of FCC gasoline hydrodesulphurization, such as the technology from Prime-G & Prime-G+(IFP), SCANFining & OCTGAIN (ExxonMobil) and ISAL (UOP), has poor adaptability to the FCC gasoline of high-sulfur (1000~1500 μg/g), high olefins (40~55 v%), low aromatics (13~20 v%) in China. It is necessary to develop new olefin FCC gasoline hydrodesulphurization technology and new catalyst.
In this paper, it is the emphases to reduce the octane number loss in the process of FCC gasoline hydrodesulphurization. The components in catalyst are determined. Catalyst performance and stability have been studied in the hydrodesulphurization of FCC gasoline. The hydrogenation process conditions are optimized.
2. Experimentation
2.1. Preparation of Catalysts
In order to improve the selectivity of hydrodesulphurization catalyst and to reduce the loss of octane number in the HCN hydrogenation process, the support of catalyst being developed should have large specific area and concentrated pore distribution that make the active metal distribute evenly. MoO3-CoO metal components is chosen because of the excellent HDS selectivity over them. Additives are added to increase the HDS selectivity. Two catalysts are developed, one with low metal content, the other with high metal content.
The dispersion of active metal components in the acidic carriers is another important parameter that affects the catalyst activity and selectivity of hydrogenation. Therefore, it will be much better when the metal components can spread out in the greatest form of single-molecule in the carrier. The catalyst prepared by impregnation could disperse well. First, the carrier of the catalyst is obtained by squeezing. Then the precursors of Mo, Co and Ni in proportion were introduced to the catalyst. After drying and calcinations, the required catalyst is obtained. The process is shown in Figure 1.
2.2. Gasoline fraction cutting
Data shows that the sulfur contents are re-presented with the fraction of variable incremental distribution in two typical FCC gasoline in China, one is high-sulfur content (1635 μg/g) and high olefin content (53 v%), another is medium sulfur content (806 μg / g) and medium-olefin content (47.3v%). Sulfur mainly concentrated in HCN (> 90 ℃). Ninety percent sulfur of FCC gasoline is in HCN. Olefin which is re-presented with the fraction of variable incremental distribution mainly concentrated in LCN and more than 70% olefin in FCC gasoline concentrated in LCN (90 ℃).
FCC gasoline produced by Fushun Petrochemical Company was rectified and separated as raw material. The distillation cut below 90 ℃ is the LCN with C7 fraction.
Using gas chromatography coupled atomic radiation technology (GC-AED), the form of sulfur was analyzed in whole distillate FCC gasoline, light distillate (LCN) and heavy distillate (HCN) as well as the effect of caustic washing to it. The results show that mercaptans and thiophene are the major component in whole FCC gasoline, as well as small amounts of sulfide and other sulfides. While sulfur in LCN (<90 ℃) is mainly C1 ~ C4 mercaptans and a small amount of thiophene. By caustic washing, about 90% of the mercaptan in LCN (<90 ℃) is removed. Whereas, the thiophene content remain unchanged.
2.3. Hydrogenation experiments
Hydrodesulphurization reaction takes place in a self-made continuous liquid phase fixed-bed reactor. It is characterized with temperature control, pressure control, power-off self-protection features, continuous feed and timing sampling functions. In order to ensure that the reactor has long enough constant temperature zone along the axial direction, a metal casing is placed between the reactor and the electric furnace tube. The constant temperature range is over 20 cm. Temperature control accuracy is up to ± 1 ℃. The device mainly consists of raw materials tank, micro-metering pump, heating systems, fixed-bed reactor, the product tank, temperature control system, pressure-conditioning systems, and gas flow control system. Reaction reactor is shown in Figure 2. The technology of catalyst sub-loading is used to fill the upper bed in the reactor with low metal content of the catalyst and fill the lower part with higher metal content catalyst. The aim is to get HDS reaction take place gently in catalyst bed to avoid the loss of octane number caused by over-hydrogenation of olefin saturation.
2.4. Product sweetening and reconcile
Mixture is produced by mixing the product from HCN hydro-treating with the cutting out LCN. This mixture is sent to the alkaliless deodorizing device for further sweetening process to get clean petroleum products with low-sulfur, low olefin and low mercaptan content (<10 μg / g).
2.5 Experimental Analysis of Instruments and analytical conditions
2.5.1. Determination of Sulfur
Sulfur content from raw materials and products were measured by WK-2B micro-Coulomb Instrument (Jiangsu Electro analytical Instrument Factory). WK-2B instrument micro-Coulomb is used to measure liquid micro-sample with testing conditions as follows: Carrier gas: Nitrogen, Reaction gas: Oxygen, Vaporization temperature paragraphs: 600 ℃, Combustion temperature paragraphs: 800 ℃, Stable temperature of paragraphs: 700 ℃.
2.5.2. Olefin content
The composition of FCC gasoline was analyzed by gas chromatography. OV-101 fused silica capillary (length 50m, internal diameter 0.23mm) is produced by Beijing Research Institute of Petroleum system. Column temperature: initial temperature of 33 ℃, keep for 5 min, and then rise to 50 ℃ at the rate of 1 ℃ / min, and then rise to 180 ℃ at the rate of 2 ℃ / min, keep 10min; detector temperature: 240 ℃; vaporization chamber temperature : 240 ℃; split ratio: 400: l; high-purity nitrogen as carrier gas; hydrogen as gas; air as assist gas.
2.5.3. N2 adsorption - desorption (BET)
Surface area of catalyst is measured by ASAP-2010 automatic physisorption from U.S. Micromeritics's Company. N2 adsorption temperature is 77 K. Catalyst is activated in vacuum afor 16 h under 383 K before measurement. Surface area is obtained through BET equation, using N2 adsorption isotherms.
3. Results and discussion
3.1. Catalyst component
Metal components are the active center for Hydrogenation catalyst. These active contents are mainly VIB group metal elements (Mo, W) and VIII group metal elements (Co, Ni). The activity of the Mo-Ni-P catalyst is compared with the Co-Mo-Ni catalyst and the results of desulfurization and de-olefin are shown in Figure 3. It can be seen from Figure 3 that the catalyst with Co-Mo-Ni combined as active component has high activity, which is due to the strong selectivity of the catalyst with Co-Mo as the active component and the large specific area of Ni. The appropriate amount of Ni could increase the degree of metal dispersion that could improve the hydrogenation activity of the catalyst [7, 8]. Through the study of catalytic activity, the ratio of active metals is determined and the essential nature of the catalyst is demonstrated. Results were shown in Table 2.
3.2. Optimization of the hydrogenation process conditions
It was investigated separately the impact that reaction conditions (including reaction temperature, pressure, space velocity and hydrogen-oil ratio) have on the reaction rate and the desulfurization rate of de-olefin. The results are shown in Figure 4 to Figure 7.
The impacts of reaction conditions like HCN hydro-desulfurization reaction pressure, temperature, and hydrogen oil volume ratio on the desulfurization and octane loss were examined. The optimized hydrodesulphurization reaction conditions were determined and shown in Table 3.
3.3. Effect of hydrogen sulfide in the cycle of hydrogen on hydrodesulphurization
The effect of hydrogen sulfide in circulating hydrogen on the activity reaction is studied. When the concentration of H2S in circulating hydrogen is over 0.14 v%, sulfur content of HCN after distillation HDS increased from 70μg/g to 160 μg/g. The circulating hydrogen was washed by ethanolamine (hydrogen sulfide concentration of 0.01 v%), sulfur content in HAD is 85 μg/g. The study results show that hydrogen sulfide in circulating hydrogen has significant inhibiting effect on HDS and it is necessary to remove H2S in circulating hydrogen to improve the HDS effect. Without the process that remove H2S in circulating hydrogen, the inhibitory effect that hydrogen sulfide has on the desulfurization of sulfur can be compensated by appropriately raising the reaction temperature. Under the condition of the same degree of HDS, the reaction temperature is usually to increase 15~20 ℃, and RON suffers the loss of about 0.3 units. Therefore, HDS reaction system needs to be equipped with the facilities to remove hydrogen sulfide in circulating hydrogen.
3.4. Stability Evaluation
In the optimal reaction conditions, the stability of catalyst was evaluated with 2000 h. The change of desulfurization rate and the de-olefin rate with the time in line of catalyst is shown in Figure 8. The results shown that the sulfur content of product is less than 115 μg/g, olefin content is less than 20.5 v% and RON loss is less than 1.0 units when raw FCC gasoline material from Fushun Petrochemical Company No. 1 Factory which has sulfur content of 1200 μg/g, olefin content of 44.2 v% is used in the experiments. Therefore, the catalyst is characterized with excellent HDS selectivity, activity and stability.
3.5. Sweetening Program
LCN with <90 ℃ is through the technology of alkali-free sweetening process. Then, the sweetened LCN is mixed with HCN of HDS after hydrodesulphurization. Thiol content in the mixture reduced to 10 μg/g.
3.6. Material balance and nature of the product
About 0.20% of hydrogen is consumed when HCN with > 90 ℃ heavy fraction reacting with HDS and gasoline liquid product is over of 99.4%. HCN with > 90 ℃ heavy fraction is mixed with HDS product with <90 ℃ light fraction to get a total liquid yield ≮ 99.4%.
After being treated with HDS olefin, the indicators of gasoline from Fushun Petrochemical Company No. 1 Factory are shown in Table 4. It can be seen that sulfur content and olefin content has decreased significantly. Mercaptan in the mixed oil is now below 10 μg/g after the process of alkali-free sweetening. Olefins are as low as 20.5%. Octane number loss is within one unit. The yield of liquid-gas is greater than 99%.
4. Conclusion
(1) This catalyst that used Mo-Co-Ni multi-metal components and additives achieve a high HDS selectivity and low olefin saturation effect. Two purpose of hydrodesulphurization and reduction of octane loss are realized.
(2) This catalyst was being conducted with 2000 h stability tests and the adaptability to different raw materials. The results indicated that this catalyst had good catalytic stability and adaptability of raw materials.
(3) The technology of the selective hydrodesulphurization of gasoline suit the cut-off point temperature of the light and heavy FCC gasoline fraction is about 90 ℃.
(4) The process conditions to the technology are as below: pressure is 2.0 MPa, reaction temperature is 230 ℃, space velocity is 2.18 h-1 and hydrogen oil volume ratio is 400:1.
(5) This technology could reduced the sulfur content of FCC gasoline from Fushun Petrochemical Company No. 1 Factory from 1200 μg/g to 115 μg/g and olefin content from 44.2 v% down to 20.5 v%. RON loss is 0.5 units. That has reached the expectant goal.

一般论文里面大部分都用现在时态，过去时只表示时间上的关系

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学海无涯

2楼2010-04-17 09:50:56

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yinjuanchen

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mermaid332(金币+5): 谢谢帮助 2010-04-18 14:03
sirljz(金币+2):谢谢交流 2010-04-19 15:55

line 4

lefin content fall to 20.5 v% from 44.2 v%. The RON loss is 0.5 units
fall should be changed into fell
line 8:Harmful substances such as sulphides and CxHy came from automobile exhaust emissions would have caused serious pollutions to the environment
came should be changed into coming
It is too long for me to read. BEST WISHES.
时态比较乱。

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闭关，写写写

3楼2010-04-17 10:25:09

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