CN103436286B - Catalytic rectification hydrogenation desulfurization process of gasoline heavy distillate - Google Patents
Catalytic rectification hydrogenation desulfurization process of gasoline heavy distillate Download PDFInfo
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- CN103436286B CN103436286B CN201310302034.1A CN201310302034A CN103436286B CN 103436286 B CN103436286 B CN 103436286B CN 201310302034 A CN201310302034 A CN 201310302034A CN 103436286 B CN103436286 B CN 103436286B
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- 239000003502 gasoline Substances 0.000 title claims abstract description 43
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title abstract description 11
- 238000006477 desulfuration reaction Methods 0.000 title abstract description 9
- 230000023556 desulfurization Effects 0.000 title abstract description 9
- 230000008569 process Effects 0.000 title abstract description 9
- 238000005984 hydrogenation reaction Methods 0.000 title abstract 2
- 238000006243 chemical reaction Methods 0.000 claims abstract description 122
- 239000001257 hydrogen Substances 0.000 claims abstract description 44
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 44
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000003054 catalyst Substances 0.000 claims abstract description 32
- 239000007789 gas Substances 0.000 claims abstract description 10
- 238000002156 mixing Methods 0.000 claims description 56
- 239000000203 mixture Substances 0.000 claims description 19
- 229910003296 Ni-Mo Inorganic materials 0.000 claims description 18
- 238000004821 distillation Methods 0.000 claims description 13
- 229910000428 cobalt oxide Inorganic materials 0.000 claims description 11
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 claims description 11
- 229910000476 molybdenum oxide Inorganic materials 0.000 claims description 11
- PQQKPALAQIIWST-UHFFFAOYSA-N oxomolybdenum Chemical compound [Mo]=O PQQKPALAQIIWST-UHFFFAOYSA-N 0.000 claims description 11
- 229910000480 nickel oxide Inorganic materials 0.000 claims description 10
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 241000209094 Oryza Species 0.000 claims description 6
- 235000007164 Oryza sativa Nutrition 0.000 claims description 6
- 235000009566 rice Nutrition 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 abstract description 8
- 229910052759 nickel Inorganic materials 0.000 abstract description 4
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 230000036632 reaction speed Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 6
- 150000002431 hydrogen Chemical class 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The invention relates to a gasoline heavy distillate treatment process, and particularly relates to a catalytic rectification hydrogenation desulfurization process of a gasoline heavy distillate. The process comprises the following steps: the gasoline heavy distillate and hydrogen are added into a premixing chamber of a catalytic rectification tower, and the hydrogen/gasoline mixed gas rises to successively pass through a first reaction chamber, a second reaction chamber and a third reaction chamber and is subjected to haptoreaction with a catalyst in the reaction chambers. The premixing chamber is added; one side of each tower plate is provided with inlets, and the other side is provided with catalyst chambers; the Co-Mo catalyst with nickel is provided and improves the reaction speed and conditions, and thus the reaction can be finished only through the three reaction chambers, the height of the catalytic rectification tower is lowered, and the equipment cost is decreased; and through the above high-efficiency reaction rate and premixing, the hydrogen/gasoline volume ratio is relatively low, the reaction temperature is also relatively low, the process difficulty is reduced, and the final desulfurization rate can reach 95% or more.
Description
Technical field
The present invention relates to a kind of gasoline last running treatment process, more specifically a kind of gasoline last running catalytic distillation hydrodesulfurization and equipment thereof.
Background technology
Conventional hydrogenating desulfurization technology has operation, technical process is complicated, apparatus expensive, the shortcomings such as sweetening effectiveness difference, technically improving therefore in routine, obtain a kind of new technology: gasoline last running catalytic distillation hydrogenating desulfurization technology, this technical matters flow process is simple, the expense of operation and fixture is few, degree of olefin saturation is low, catalyst life is long, the features such as reaction heat is fully utilized, the hydrogenating desulfurization of gasoline last running in the world at present uses above-mentioned technology substantially, but by article " FCC gasoline last running catalytic distillation hydrodesulfurization process model analysis, Yang Hongjian, Luo Xiang, Hou Kaihu, chemical engineering institute of Hebei University of Technology " known, this processing condition harshness (temperature 275-280 DEG C, feed entrance point will in the 24th allegro, catalytic rectifying tower used is higher, have 45 fast column plates, tray spacing 1m), and which employs high hydrogen to oil volume ratio, this just causes a large amount of hydrogen needs to recycle, cause the waste of raw material and the energy.
Summary of the invention
For above deficiency, the invention provides a kind of gasoline last running catalytic distillation hydrodesulfurization and equipment, by the improvement to equipment, hydrogen and gasoline are carried out pre-mixing, gasoline is contacted more abundant with hydrogen, thus reaction is rapider, and design column plate side be horn-like import, opposite side is catalyst chamber, hydrogen and gasoline mixture are concentrated through catalyst chamber, make reactant and catalyst exposure more even, further increase the speed of reaction, and provide a kind of Co-Mo catalyzer with nickel, wherein molybdenum oxide 18-22wt%, nickel oxide 1.8-3.5wt%, cobalt oxide 6.5-10.5wt%, due to the existence of nickel, the activity of Co-Mo catalyst reaction can be improved, further increase again the efficiency of catalyzed reaction, therefore the present invention can terminate reaction only by three reaction chambers, reduce the height of catalytic rectifying tower, reduce the cost of equipment.By above-mentioned efficient speed of reaction and pre-mixing, make hydrogen to oil volume ratio lower, temperature of reaction is also lower, reduces the difficulty of technique.
The present invention is achieved by the following technical solutions:
A kind of gasoline last running catalytic distillation hydrodesulfurization, comprise the steps: pre-mixing chamber gasoline last running and hydrogen added in catalytic rectifying tower, pre-mixing room temp 250-300 DEG C, hydrogen to oil volume ratio is 50-100, when pre-mixing chamber internal pressure is 10-20MPa, pre-mixing chamber pressure valve is opened automatically, hydrogen oil gas mixture rises successively through the first reaction chamber, second reaction chamber and the 3rd reaction chamber, and react with the catalyst exposure in reaction chamber, first reaction room temp 200-220 DEG C, second reaction room temp is 100-120 DEG C, 3rd reaction room temp is 180-200 DEG C.
Above-mentioned first chamber volume air speed is 1.0-1.5h
-1.
Above-mentioned second chamber volume air speed is 3.0-4.5h
-1.
Above-mentioned 3rd chamber volume air speed is 1.5-2.5h
-1.
Above-mentioned three reaction chambers, after the reaction of the first reaction chamber, react at the 3rd reaction chamber of rapid temperature increases to 180-200 DEG C after reaction in the low temperature of 100-120 DEG C rapidly, after the cooling of 100-120 DEG C, although W-response reduces speed, when again arriving 180-200 DEG C, rapidly response rises, be conducive to react quick, carry out thoroughly, be conducive to deviating from of sulphur.
Above-mentioned catalyzer is Co-Ni-Mo, and the composition of described Co-Ni-Mo comprises molybdenum oxide 18-22wt%, nickel oxide 1.8-3.5wt%, cobalt oxide 6.5-10.5wt%.
Optimize, above-mentioned a kind of gasoline last running catalytic distillation hydrodesulfurization, comprise the steps: pre-mixing chamber gasoline last running and hydrogen added in catalytic rectifying tower, pre-mixing room temp 260 DEG C, hydrogen to oil volume ratio is 55, when pre-mixing chamber internal pressure is 15MPa, pre-mixing chamber pressure valve is opened automatically, hydrogen oil gas mixture rises successively through the first reaction chamber, second reaction chamber and the 3rd reaction chamber, and react with the catalyst exposure in reaction chamber, described catalyzer is Co-Ni-Mo, the composition of described Co-Ni-Mo comprises molybdenum oxide 19wt%, nickel oxide 1.8wt%, cobalt oxide 8.5wt%, first reaction room temp 210 DEG C, second reaction room temp is 110 DEG C, 3rd reaction room temp is 190 DEG C, first chamber volume air speed is 1.0h
-1, the second chamber volume air speed is 3.5h
-1, the 3rd chamber volume air speed is 2.0h
-1.
Above-mentioned a kind of catalytic rectifying tower, comprise tower body, pre-mixing chamber is provided with in the middle part of described tower body, described pre-mixing chamber is connected with hydrogen inlet and gasoline entrance, pressure valve is provided with above described pre-mixing chamber, refluxing opening is provided with between described pre-mixing chamber and tower body, the first reaction chamber is provided with successively above described pre-mixing chamber, second reaction chamber and the 3rd reaction chamber, first reaction chamber, column plate is provided with in second reaction chamber and the 3rd reaction chamber, described column plate is provided with through hole, the lower end of described through hole is provided with inlet mouth, described through hole upper end is provided with catalyst chamber, described pre-mixing chamber, first reaction chamber, the second reaction chamber tower body outside corresponding with the 3rd reaction chamber is respectively provided with circulation water layer, be not communicated with between circulation water layer, described first reaction chamber, second reaction chamber and the 3rd reaction chamber height 1.5-3 rice respectively, catalytic rectifying tower height overall 7-15 rice.
Design pre-mixing chamber, hydrogen and gasoline are carried out pre-mixing, gasoline is made to contact with hydrogen more fully thus react rapider, and without the need to higher hydrogen to oil volume ratio, column plate is provided with through hole, and the lower end of described through hole is provided with inlet mouth, and described through hole upper end is provided with catalyst chamber, make hydrogen, gasoline and catalyst exposure more evenly, fully, for the height reducing catalytic rectifying tower provides sufficient condition.
Above-mentioned inlet mouth is horn-like, is conducive to entering of gas.
The sidewall of above-mentioned catalyst chamber and top are reticulated structure.
Be provided with web plate between above-mentioned catalyst chamber and described through hole, prevent catalyzer from departing from catalyst chamber.
The invention has the beneficial effects as follows: add pre-mixing chamber, hydrogen and gasoline are carried out pre-mixing, gasoline is contacted more abundant with hydrogen, thus reaction is rapider, and design column plate side be horn-like import, opposite side is catalyst chamber, hydrogen and gasoline mixture are concentrated through catalyst chamber, make reactant and catalyst exposure more even, further increase the speed of reaction, and provide a kind of Co-Mo catalyzer with nickel, further increase again the efficiency of catalyzed reaction, therefore the present invention can terminate reaction only by three reaction chambers, reduce the height of catalytic rectifying tower, reduce the cost of equipment.By above-mentioned efficient speed of reaction and pre-mixing, make hydrogen to oil volume ratio lower, temperature of reaction is also lower, reduces the difficulty of technique, and its final desulfurization degree can reach more than 95%.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention;
Fig. 2 is tower plate structure schematic diagram of the present invention;
In figure: 1-tower body, 2-pre-mixing chamber, 3-hydrogen inlet, 4-gasoline entrance, 5-pressure valve, 6-refluxing opening, 7-first reaction chamber, 8-second reaction chamber, 9-the 3rd reaction chamber, 10-column plate, 11-through hole, 12-inlet mouth, 13-catalyst chamber, 14-circulation water layer, 15-web plate.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention will be further described, so that those skilled in the art better can understand the present invention, but therefore do not limit the present invention.
Embodiment 1
A kind of catalytic rectifying tower, comprise tower body 1, pre-mixing chamber 2 is provided with in the middle part of described tower body 1, described pre-mixing chamber 2 is connected with hydrogen inlet 3 and gasoline entrance 4, pressure valve 5 is provided with above described pre-mixing chamber 2, refluxing opening 6 is provided with between described pre-mixing chamber 2 and tower body 1, the first reaction chamber 7 is provided with successively above described pre-mixing chamber 2, second reaction chamber 8 and the 3rd reaction chamber 9, first reaction chamber 7, column plate 10 is respectively equipped with in second reaction chamber 8 and the 3rd reaction chamber 9, described column plate 10 is provided with through hole 11, the lower end of described through hole 11 is provided with inlet mouth 12, described through hole 11 upper end is provided with catalyst chamber 13, described pre-mixing chamber 2, first reaction chamber 7, second reaction chamber 8 and corresponding tower body 1 outside of the 3rd reaction chamber 9 are respectively provided with circulation water layer 14, be not communicated with between circulation water layer 14, described first reaction chamber 7, second reaction chamber 8 and the 3rd reaction chamber 9 height 1.5-3 rice respectively, catalytic rectifying tower height overall 7-15 rice, inlet mouth 12 is horn-like, be conducive to entering of gas, the sidewall of catalyst chamber 13 and top are reticulated structure, web plate 15 is provided with between catalyst chamber 13 and described through hole 11, prevent catalyzer from departing from catalyst chamber 13.
Embodiment 2
Analyze sulphur content in gasoline, the last running of 1Kg gasoline and hydrogen are added the pre-mixing chamber in catalytic rectifying tower, pre-mixing room temp 250 DEG C, hydrogen to oil volume ratio is 50, when pre-mixing chamber internal pressure is 10MPa, pre-mixing chamber pressure valve is opened automatically, and hydrogen oil gas mixture rises successively through the first reaction chamber, the second reaction chamber and the 3rd reaction chamber, and react with the catalyst exposure in reaction chamber, described catalyzer 15.21m
3, described catalyzer is Co-Ni-Mo, and the composition of described Co-Ni-Mo comprises molybdenum oxide 18wt%, nickel oxide 1.8wt%, cobalt oxide 6.5wt%, first reaction room temp 200 DEG C, second reaction room temp is 100 DEG C, and the 3rd reaction room temp is 180 DEG C, and the first chamber volume air speed is 1.0h
-1, the second chamber volume air speed is 3.0h
-1, the 3rd chamber volume air speed is 1.5h
-1, reaction terminates post analysis sulphur content, and detected result is in table 1, if without specified otherwise, following examples all adopt above-mentioned raw materials gasoline.
Embodiment 3
The last running of 1Kg gasoline and hydrogen are added the pre-mixing chamber in catalytic rectifying tower, pre-mixing room temp 260 DEG C, hydrogen to oil volume ratio is 55, when pre-mixing chamber internal pressure is 15MPa, pre-mixing chamber pressure valve is opened automatically, hydrogen oil gas mixture rises successively through the first reaction chamber, the second reaction chamber and the 3rd reaction chamber, and reacts with the catalyst exposure in reaction chamber, described catalyzer 15.21m
3, described catalyzer is Co-Ni-Mo, and the composition of described Co-Ni-Mo comprises molybdenum oxide 19wt%, nickel oxide 1.8wt%, cobalt oxide 8.5wt%, first reaction room temp 210 DEG C, second reaction room temp is 110 DEG C, and the 3rd reaction room temp is 190 DEG C, and the first chamber volume air speed is 1.0h
-1, the second chamber volume air speed is 3.5h
-1, the 3rd chamber volume air speed is 2.0h
-1, detected result is in table 1.
Embodiment 4
The last running of 1Kg gasoline and hydrogen are added the pre-mixing chamber in catalytic rectifying tower, pre-mixing room temp 300 DEG C, hydrogen to oil volume ratio is 100, when pre-mixing chamber internal pressure is 20MPa, pre-mixing chamber pressure valve is opened automatically, hydrogen oil gas mixture rises successively through the first reaction chamber, the second reaction chamber and the 3rd reaction chamber, and reacts with the catalyst exposure in reaction chamber, described catalyzer 15.21m
3, described catalyzer is Co-Ni-Mo, and the composition of described Co-Ni-Mo comprises molybdenum oxide 19wt%, nickel oxide 1.8wt%, cobalt oxide 8.5wt%, first reaction room temp 220 DEG C, second reaction room temp is 120 DEG C, and the 3rd reaction room temp is 200 DEG C, and the first chamber volume air speed is 1.5h
-1, the second chamber volume air speed is 4.5h
-1, the 3rd chamber volume air speed is 2.5h
-1, detected result is in table 1.
Embodiment 5
Pre-mixing room temp 245 DEG C, other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 6
Pre-mixing room temp 305 DEG C, other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 7
Hydrogen to oil volume ratio is 45, and other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 8
Hydrogen to oil volume ratio is 105, and other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 9
First reaction room temp 190 DEG C, the first chamber volume air speed is 1.0h
-1, other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 10
First reaction room temp 230 DEG C, other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 11
Second reaction room temp is 90 DEG C, and other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 12
Second reaction room temp is 130 DEG C, and other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 13
3rd reaction room temp is 170 DEG C, and other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 14
3rd reaction room temp is 210 DEG C, and other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 15
Catalyzer is Co-Mo, and the composition of described Co-Mo comprises molybdenum oxide 19wt%, cobalt oxide 8.5wt%, and other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 16
Catalyzer is Co-Ni-Mo, and the composition of described Co-Ni-Mo comprises molybdenum oxide 19wt%, nickel oxide 1.5wt%, cobalt oxide 8.5wt%, and other parameters are identical with embodiment 3, and detected result is in table 1.
Embodiment 17
Catalyzer is Co-Ni-Mo, and the composition of described Co-Ni-Mo comprises molybdenum oxide 19wt%, nickel oxide 3.8wt%, cobalt oxide 8.5wt%, and other parameters are identical with embodiment 3, and detected result is in table 1.
As seen from the above table, utilize equipment of the present invention, with reference to parameter of the present invention, desulfurization degree more than 95%, and to exceed or lower than after parameter of the present invention, although be only less change, desulfurization degree also there will be decline sharply, cannot reach effect of the present invention.
Claims (10)
1. a gasoline last running catalytic distillation hydrodesulfurization, comprise the steps: pre-mixing chamber gasoline last running and hydrogen added in catalytic rectifying tower, pre-mixing room temp 250-300 DEG C, hydrogen to oil volume ratio is 50-100, when pre-mixing chamber internal pressure is 10-20MPa, pre-mixing chamber pressure valve is opened automatically, hydrogen oil gas mixture rises successively through the first reaction chamber, second reaction chamber and the 3rd reaction chamber, and react with the catalyst exposure in reaction chamber, first reaction room temp 200-220 DEG C, second reaction room temp is 100-120 DEG C, 3rd reaction room temp is 180-200 DEG C.
2. a kind of gasoline last running catalytic distillation hydrodesulfurization according to claim 1, is characterized in that: described first chamber volume air speed is 1.0-1.5h
-1.
3. a kind of gasoline last running catalytic distillation hydrodesulfurization according to claim 1, is characterized in that: described second chamber volume air speed is 3.0-4.5h
-1.
4. a kind of gasoline last running catalytic distillation hydrodesulfurization according to claim 1, is characterized in that: described 3rd chamber volume air speed is 1.5-2.5h
-1.
5. a kind of gasoline last running catalytic distillation hydrodesulfurization according to claim 1, it is characterized in that: described catalyzer is Co-Ni-Mo, the composition of described Co-Ni-Mo comprises molybdenum oxide 18-22wt%, nickel oxide 1.8-3.5wt%, cobalt oxide 6.5-10.5wt%.
6. a kind of gasoline last running catalytic distillation hydrodesulfurization according to claim 1, comprise the steps: pre-mixing chamber gasoline last running and hydrogen added in catalytic rectifying tower, pre-mixing room temp 260 DEG C, hydrogen to oil volume ratio is 55, when pre-mixing chamber internal pressure is 15MPa, pre-mixing chamber pressure valve is opened automatically, hydrogen oil gas mixture rises successively through the first reaction chamber, second reaction chamber and the 3rd reaction chamber, and react with the catalyst exposure in reaction chamber, described catalyzer is Co-Ni-Mo, the composition of described Co-Ni-Mo comprises molybdenum oxide 19wt%, nickel oxide 1.8wt%, cobalt oxide 8.5wt%, first reaction room temp 210 DEG C, second reaction room temp is 110 DEG C, 3rd reaction room temp is 190 DEG C, first chamber volume air speed is 1.0h
-1, the second chamber volume air speed is 3.5h
-1, the 3rd chamber volume air speed is 2.0h
-1.
7. a kind of catalytic rectifying tower according to claim 1, comprise tower body, it is characterized in that being provided with pre-mixing chamber in the middle part of described tower body, described pre-mixing chamber is connected with hydrogen inlet and gasoline entrance, pressure valve is provided with above described pre-mixing chamber, refluxing opening is provided with between described pre-mixing chamber and tower body, the first reaction chamber is provided with successively above described pre-mixing chamber, second reaction chamber and the 3rd reaction chamber, first reaction chamber, column plate is respectively equipped with in second reaction chamber and the 3rd reaction chamber, described column plate is provided with through hole, the lower end of described through hole is provided with inlet mouth, described through hole upper end is provided with catalyst chamber, described pre-mixing chamber, first reaction chamber, the second reaction chamber tower body outside corresponding with the 3rd reaction chamber is respectively provided with circulation water layer, be not communicated with between circulation water layer, described first reaction chamber, second reaction chamber and the 3rd reaction chamber height 1.5-3 rice respectively, catalytic rectifying tower height overall 7-15 rice.
8. a kind of catalytic rectifying tower according to claim 7, is characterized in that: described inlet mouth is horn-like.
9. a kind of catalytic rectifying tower according to claim 7, is characterized in that: the sidewall of described catalyst chamber and top are reticulated structure.
10. a kind of catalytic rectifying tower according to claim 7, is characterized in that: be provided with web plate between described catalyst chamber and described through hole.
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| CN201310302034.1A CN103436286B (en) | 2013-07-18 | 2013-07-18 | Catalytic rectification hydrogenation desulfurization process of gasoline heavy distillate |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1193991A (en) * | 1995-08-28 | 1998-09-23 | 化学研究及许可证公司 | Gasoline desulfurization process |
| CN1386560A (en) * | 2001-05-18 | 2002-12-25 | 中国石化集团齐鲁石油化工公司 | Reactive distilling apparatus |
| CN1429884A (en) * | 2001-12-30 | 2003-07-16 | 中国石化集团齐鲁石油化工公司 | Desulfurization process of gasoline |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7927480B2 (en) * | 2008-01-29 | 2011-04-19 | Catalytic Distillation Technologies | Process for desulfurization of cracked naphtha |
| US20090223866A1 (en) * | 2008-03-06 | 2009-09-10 | Opinder Kishan Bhan | Process for the selective hydrodesulfurization of a gasoline feedstock containing high levels of olefins |
-
2013
- 2013-07-18 CN CN201310302034.1A patent/CN103436286B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1193991A (en) * | 1995-08-28 | 1998-09-23 | 化学研究及许可证公司 | Gasoline desulfurization process |
| CN1386560A (en) * | 2001-05-18 | 2002-12-25 | 中国石化集团齐鲁石油化工公司 | Reactive distilling apparatus |
| CN1429884A (en) * | 2001-12-30 | 2003-07-16 | 中国石化集团齐鲁石油化工公司 | Desulfurization process of gasoline |
Non-Patent Citations (2)
| Title |
|---|
| FCC汽油重馏分催化精馏加氢脱硫过程模拟分析;杨红健等;《石油炼制与化工》;20101231;第41卷(第10期);47-51 * |
| FCC汽油重馏分催化蒸馏加氢脱硫研究;王迎春等;《齐鲁石油化工》;20051231;第33卷(第03期);178-180 * |
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