CN105273755A - Method for reducing content of hydrogen in catalytic cracking dry gas - Google Patents
Method for reducing content of hydrogen in catalytic cracking dry gas Download PDFInfo
- Publication number
- CN105273755A CN105273755A CN201410331861.8A CN201410331861A CN105273755A CN 105273755 A CN105273755 A CN 105273755A CN 201410331861 A CN201410331861 A CN 201410331861A CN 105273755 A CN105273755 A CN 105273755A
- Authority
- CN
- China
- Prior art keywords
- reaction zone
- reaction
- regenerated catalyst
- riser reactor
- dry gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Abstract
The invention belongs to the field of catalytic cracking of heavy oil, and relates to a method for reducing the content of hydrogen in a catalytic cracking dry gas. The method comprises the following steps: a high temperature regenerated catalyst from a regenerator enters a reaction zone a, and the cooled regenerated catalyst enters a reaction zone b; cracked C9 aromatic hydrocarbons are injected to the reaction zone b of a riser reactor, and react in the reaction b full of the cooled regenerated catalyst, a material flow obtained after the reaction and the high temperature regenerated catalyst not participating in the reaction in the reaction zone a move upward along the riser reactor in respective reaction zones and meet in the outlet of the separator plate of the riser reactor, and the obtained mixture contacts and reacts with an FCC main raw material atomized by steam; and a material obtained after the reaction is separated to obtain a reaction product, a coked catalyst is stripped and regenerated, and the regenerated catalyst returns to the riser reactor for cycle use. The reactor has the advantages of simple structure, easy manufacturing and mounting, small cost, reduction of the catalytic dry gas yield, reduction of the content of hydrogen in the dry gas, and improvement of the yield and the quality of light oil.
Description
Technical field
The invention belongs to the catalytic cracking field of heavy oil, relate to a kind of hydrogen content method in reduction catalytic cracked dry gas.
Background technology
Fluid catalytic cracking (FCC) is one of technical way of processing heavy oil in oil refining process, and its main purpose product is gasoline, diesel oil and liquefied gas.The increase of dry gas, coke yield in catalytic cracking process, the especially increase of hydrogen content in dry gas, certainly will make the hydrogen content had in the light oil of high added value reduce, thus have influence on the quality of light oil products.Along with heaviness day by day and the in poor quality of crude oil, lightweight oil demand increases day by day simultaneously, and the heaviness of FCC main raw material oil and in poor quality are also in continuous aggravation.The change how adapting to stock oil improves yield of light oil with maximum amplitude, reduces dry gas and coke yield, reduces the content of hydrogen in dry gas simultaneously, becomes one of problem that FCC pays close attention to this year.
Patent documentation CN101275081, disclose a kind of method reducing catalytic cracked dry gas, a kind of active ingredient is introduced in Conventional catalytic cracking raw material, active ingredient is utilized to be easy to generate the response characteristic of three-fold coordination carbonium ion, react through hydride transfer with raw molecule again, thus decrease the generation of dry gas, improve product slates, the active ingredient mentioned is catalytically cracked gasoline.
Patent documentation CN200910015985.4, is mixed for catalytically cracked material by cracking C9 aromatic or makes the terminator of catalytic unit, at pressure 0.1 ~ 0.8MPa, react at temperature 450 ~ 600 DEG C, mixed ratio 2% ~ 15% when being mixed for fcc raw material, when making terminator, mixed ratio is 2% ~ 10%.Result shows to improve catalytic cracking product distribution, improves yield of light oil.But this patent is not mentioned and is reduced dry gas yied and reduce this technical characterstic of hydrogen content in dry gas.
Summary of the invention
The object of this invention is to provide a kind of hydrogen content method in reduction catalytic cracked dry gas, flexibly, easy, improve productive rate and the quality of object product, reduce the productive rate of catalytic cracked dry gas, reduce hydrogen content in dry gas simultaneously, thus change the severity of reaction conditions, effectively can reduce the productive rate of catalytic cracked dry gas, reduce hydrogen content in dry gas simultaneously.
The present invention reduces hydrogen content method in catalytic cracked dry gas, between the pre-lift medium inlet of FCC riser reactor and FCC main raw material entrance, reactor dividing plate is set, the lower part of riser reactor is divided into and is parallel to axial a reaction zone, 2 reaction zones and b reaction zone, and corresponding catalyst inlet and raw material nozzles are set in each reaction zone; Wherein, the high-temperature regenerated catalyst from revivifier enters a reaction zone, and cooled regenerated catalyst enters b reaction zone; By the b reaction zone in cracking C9 aromatic injecting lift pipe reactor, react in cracking C9 aromatic and the b reaction zone being full of cooled regenerated catalyst, the high-temperature regenerated catalyst having neither part nor lot in reaction in reacted logistics and a reaction zone is up along riser reactor in respective reaction zone, after riser reactor baffled outlet place converges, contact with the FCC main raw material through steam atomizing and react; Reacting rear material is through reaction product isolated, and spent agent returns riser reactor and recycles after stripping, regeneration.
The height of reactor dividing plate accounts for 15 ~ 45% of riser reactor total length.
The temperature of high-temperature regenerated catalyst is 600 ~ 700 DEG C;
The mass ratio of catalyzer and FCC main raw material is 6:1 ~ 10:1, and the temperature of cooling regenerated catalyst is 400 ~ 550 DEG C; Temperature 600-680 DEG C before regenerated catalyst contacts with FCC main raw material.
The mass ratio of regenerated catalyst and FCC main raw material is 6:1 ~ 10:1, the temperature of reaction 360 DEG C ~ 500 DEG C of cooling regenerated catalyst and cracking C9 aromatic, and reaction pressure is 0.2 ~ 0.4MPa; The temperature of reaction of regenerated catalyst and FCC main raw material 500 DEG C ~ 600 DEG C, reaction pressure 0.3 ~ 0.6MPa, the mass ratio of regenerated catalyst and FCC main raw material is 4:1 ~ 10:1.
The regeneration temperature of revivifier is 600 DEG C ~ 750 DEG C.
FCC main raw material is one or more mixing in long residuum, vacuum residuum, straight-run gas oil, wax tailings or hydrogenation tail oil.
The add-on of cracking C9 aromatic is 3% ~ 12% of FCC main raw material quality.
Catalyzer is zeolite, ultrastable Y－type zeolite, ZSM-5 series zeolite, the one, two or three had in five-membered ring structure high-silicon zeolite, β zeolite, ferrierite that active ingredient contains Y or HY, or amorphous silicon aluminium catalyzer.Preferred RMS-8 catalyzer, manufacturer is Qilu Petrochemical catalyst plant.
The structure of riser reactor is: a side lower part of the riser reactor body of riser reactor arranges regenerator sloped tube, and the opposite side of the riser reactor body corresponding with regenerator sloped tube arranges cracking C9 aromatic entrance; The bottom of riser reactor inside arranges pre-lift medium inlet, inner top arranges main raw material entrance, reactor dividing plate is set between pre-lift medium inlet and main raw material entrance, the lower part of riser reactor is divided into and is parallel to axial a reaction zone and b reaction zone by reactor dividing plate, and arranges corresponding catalyst inlet and raw material nozzles in each reaction zone.
The cross-sectional area ratio of a and b two reaction zone is 1:1 ~ 5:1.
The add-on of cracking C9 aromatic is 3% ~ 12% of catalytically cracked material mass ratio.Cracking C9 aromatic is selected from crude oil processing byproduct, mainly from the cracker of olefin plant.
Reactor dividing plate is arranged on the inside of riser reactor, and its upper end is positioned at below main FCC main raw material entrance, and the height of dividing plate accounts for 15 ~ 45% of riser reactor total length; Dividing plate is made up of a block plate, and its material can be identical with the material of riser tube.Riser tube inwall should be fixed in two limits being parallel to riser tube axis of steel plate by the placement of dividing plate, the lower part of reactor is divided into mutually isolated and is parallel to 2 axial reaction zone a and b.From a reaction zone of 600 ~ 700 DEG C of regenerator injecting lift pipe reactor bottoms of revivifier, and continue to rise along riser tube to leave reactor dividing plate; Regenerated catalyst 60 ~ 95% after regeneration enters the reaction zone a of riser reactor through regenerator sloped tube, another part 5 ~ 40% regenerated catalyst is drawn from regenerator sloped tube, with compress wind be cooled to temperature required after enter the b reaction zone of riser reactor bottom, cracking C9 aromatic contacts with cooling regenerated catalyst in this reaction zone, the impurity such as colloid are preferentially adsorbed on regenerated catalyst, and generating portion cracking reaction.Catalyzer in each reaction zone mixes mutually after leaving reactor baffle plate, contacts and react with FCC main raw material.
According to prior art, the catalyzer in system at riser reactor, settling vessel, separator, stripper, treat that the annexation of defeated line and revivifier is prior art, technique is also common process.
Preferred following technique: the high-temperature regenerated catalyst warp from revivifier enters a reaction zone at defeated line, and cooled regenerated catalyst enters b reaction zone; By the b reaction zone in cracking C9 aromatic injecting lift pipe reactor, react in cracking C9 aromatic and the b reaction zone being full of cooled regenerated catalyst, the high-temperature regenerated catalyst having neither part nor lot in reaction in reacted logistics and a reaction zone is up along riser reactor in respective reaction zone, after riser reactor baffled outlet place converges, contact with the FCC main raw material through steam atomizing and react; Reacting rear material is through reaction product isolated, and spent agent returns riser reactor and recycles after stripping, regeneration.Catalyzer is mixed into riser reactor through the stock oil of pre-lift and preheating and atomizing steam.Stock oil is contact catalyst generation cracking reaction after nozzle atomization, and oil gas rises to separator together with catalyzer, and oil gas is gone out from settling vessel top and entered rear portion fractionating system after sedimentation and filtration.Carbon deposited catalyst falls into stripper after steam stripped, and form dense bed in stripper bottom, this dense bed makes seal isolation between reactor and revivifier.Bottom close phase section, carbon deposited catalyst is through treating that defeated line is transported to regenerator overhead.In a regenerator, carbon deposited catalyst with from dispersion plate out air burn regeneration.Regenerator flow into regenerator transfer limes downwards, and transfer limes forms by founding and stand inclined tube again.Utilize the aperture size of guiding valve to be generated and regeneration guiding valve to control the internal circulating load of catalyzer.Regenerator is re-circulated to reactor bottom and again contacts with charging.Oil gas enters gas-liquid separation tower, goes out reacted gas and liquid composition through fractionation subzero fractionation.Reacted gas is through the metering of dry gas table, and thief hole sampling analysis forms.Product liquid passes through weighing, Fen Shui, point oil, samples and use gas Chromatographic Simulation distillation apparatus to analyze its oil sample composition, obtains gasoline, diesel oil and heavy oil yield.From revivifier flue gas out through the metering of dry gas table, and analyze carbonic acid gas, carbon monoxide content wherein by infrared spectrum analyser continuously from thief hole.According to composition and the quality of reacted gas, liquid, flue gas, calculated the product slates data of test by material balance application software.
Compared with prior art, the present invention has following beneficial effect:
The structure of reactor that the present invention uses is simple, is easy to manufacture and install, and cost is little; Change the severity of reaction conditions, the finish way of contact can be regulated neatly, physico-chemical property according to petroleum hydrocarbon selects the suitable finish way of contact and condition, the effect improving catalytic cracking unit product yield and quality product can be played, reduce catalysis drying gas productive rate, and reduce hydrogen content in dry gas, improve yield of light oil and quality.
Accompanying drawing explanation
Fig. 1 is the structural representation of riser reactor;
Fig. 2 is the sectional view in A-A direction in Fig. 1;
In figure, 1, riser reactor body, 2, FCC main raw material entrance, 3, reactor dividing plate, 4, cracking C9 aromatic entrance, 5, pre-lift medium inlet, 6, regenerator sloped tube, 7, a reaction zone, 8, b reaction zone.
Embodiment
Below in conjunction with embodiment, the present invention is described further.
Embodiment 1
Below in conjunction with embodiment, the invention will be further described, but content not thereby limiting the invention.
The mass ratio of regenerated catalyst and FCC main raw material represents with agent-oil ratio in the examples below that.
The FCC main raw material oil adopted in embodiment, the character of cracking C9 aromatic are as shown in table 1.The character of catalyzer is as shown in table 2.
Table 1 stock oil and cracking C9 aromatic character
Table 2 catalyst property
Embodiment 1
The present embodiment is that the riser fluid catalytic cracking of 100,000 tons/year carries out in a set for the treatment of capacity.The main FCC main raw material oil 1 of this device is the mixing oil of decompressed wax oil and residual oil, and the mass ratio of cracking C9 aromatic and main raw material is 0.11.
Testing sequence is as follows: as shown in Figure 1, between the pre-lift medium inlet 5 of FCC riser reactor and FCC main raw material entrance 2, reactor dividing plate 3 is set, the height of reactor dividing plate 3 accounts for 25% of riser reactor total length, the lower part of riser reactor is divided into and is parallel to axial a reaction zone, 2 reaction zones 7 and b reaction zone 8, and corresponding catalyst inlet and raw material nozzles are set in each reaction zone; Wherein, the high-temperature regenerated catalyst from revivifier enters a reaction zone, and cooled regenerated catalyst enters b reaction zone; By the b reaction zone in cracking C9 aromatic injecting lift pipe reactor, react in cracking C9 aromatic and the b reaction zone being full of cooled regenerated catalyst, the high-temperature regenerated catalyst having neither part nor lot in reaction in reacted logistics and a reaction zone is up along riser reactor in respective reaction zone, after riser reactor baffled outlet place converges, contact with the FCC main raw material through steam atomizing and react; Reacting rear material reaction product isolated and spent agent.Reaction product enters subsequent separation system, is separated into the various products such as gasoline, diesel oil, liquefied gas further.Catalyzer 85% after regeneration enters a district through regenerator sloped tube, and another part 15% enters b district through pipeline after cooling.
The structure of the riser reactor that the present embodiment adopts is: a side lower part of the riser reactor body 1 of riser reactor arranges regenerator sloped tube 6, and the opposite side of the riser reactor body 1 corresponding with regenerator sloped tube 6 arranges cracking C9 aromatic entrance 4; The bottom of riser reactor inside arranges pre-lift medium inlet 5, inner top arranges main raw material entrance 2, reactor dividing plate 3 is set between pre-lift medium inlet 5 and main raw material entrance 2, the lower part of riser reactor is divided into and is parallel to axial a reaction zone 7 and b reaction zone 8 by reactor dividing plate 3, and arranges corresponding catalyst inlet and raw material nozzles in each reaction zone.
The catalyzer adopted is RMS-8 catalyzer.
The cross-sectional area ratio of a and b two reaction zone is 4:1.
Prevailing operating conditions and product slates are in table 3.
Embodiment 2
The catalyzer that this embodiment adopts, device are identical with embodiment 1 with technical process.Difference is, adopt another kind of main FCC main raw material oil 2, this stock oil is mainly decompressed wax oil.Prevailing operating conditions and product slates are in table 3.
Embodiment 3
The catalyzer adopted, device and technical process are with embodiment 1.Difference is, this embodiment is the long residuum after adopting hydrogenation.Prevailing operating conditions and product slates are in table 3.
Comparative example 1
This comparative example adopts the stock oil identical with embodiment 1 and catalyzer, and the riser fluid catalytic cracking of 100,000 tons/year is tested.This device does not arrange reactor dividing plate.
In process of the test, after main FCC main raw material oil and cracking C9 aromatic fully mix, through preheating, atomization, injecting lift reactor, contacts with high temperature regeneration agent and reacts.Reactant flow is up along riser tube, and realizes being separated of oil gas and catalyzer at leg outlet.Reaction oil gas sends into subsequent separation system, is separated into the various products such as gasoline, diesel oil, liquefied gas further.Spent agent falls into stripper, and after water vapour stripping, send into revivifier coke burning regeneration, the catalyzer after regeneration returns riser reactor and recycles.Prevailing operating conditions and product slates are in table 3.
Comparative example 2
This comparative example adopts the stock oil identical with embodiment 2 and catalyzer, and the riser fluid catalytic cracking of 100,000 tons/year is tested.This device does not arrange reactor dividing plate.Process of the test is with comparative example 1.
Table 3 embodiment 1-2 and comparative example 1-2 operational condition and product slates contrast
As can be seen from Table 3, after adopting FCC main raw material provided by the invention and catalyst exposure method, embodiment 1 and embodiment 2 compare with comparative example 1 and comparative example 2 respectively, dry gas yied reduces 0.38 and 0.23 percentage point respectively relative to comparative example, in dry gas, hydrogen content have dropped 2.31 and 2.24 percentage points respectively, yield of light oil adds 2.45 and 1.91 percentage points respectively, coke yield have dropped 1.03 and 1.24 percentage points respectively, slurry oil productive rate have dropped 0.53 and 1.41 percentage point respectively, and product slates situation can arrive obviously to be improved.
Claims (10)
1. one kind is reduced hydrogen content method in catalytic cracked dry gas, it is characterized in that: between the pre-lift medium inlet (5) and FCC main raw material entrance (2) of FCC riser reactor, reactor dividing plate (3) is set, the lower part of riser reactor is divided into and is parallel to axial a reaction zone, 2 reaction zones (7) and b reaction zone (8), and corresponding catalyst inlet and raw material nozzles are set in each reaction zone; Wherein, the high-temperature regenerated catalyst from revivifier enters a reaction zone, and cooled regenerated catalyst enters b reaction zone; By the b reaction zone in cracking C9 aromatic injecting lift pipe reactor, react in cracking C9 aromatic and the b reaction zone being full of cooled regenerated catalyst, the high-temperature regenerated catalyst having neither part nor lot in reaction in reacted logistics and a reaction zone is up along riser reactor in respective reaction zone, after riser reactor baffled outlet place converges, with through steam atomizing FCC contact raw and react; Reacting rear material is through reaction product isolated, and spent agent returns riser reactor and recycles after stripping, regeneration.
2. hydrogen content method in reduction catalytic cracked dry gas according to claim 1, is characterized in that: the height of reactor dividing plate (3) accounts for 15 ~ 45% of riser reactor total length.
3. hydrogen content method in reduction catalytic cracked dry gas according to claim 1, is characterized in that: the temperature of high-temperature regenerated catalyst is 600 ~ 700 DEG C.
4. hydrogen content method in reduction catalytic cracked dry gas according to claim 1, is characterized in that: the temperature of cooling regenerated catalyst is 400 ~ 550 DEG C; Temperature before regenerated catalyst contacts with FCC main raw material is 600-680 DEG C.
5. hydrogen content method in reduction catalytic cracked dry gas according to claim 1, it is characterized in that: the mass ratio of regenerated catalyst and FCC main raw material is 6:1 ~ 10:1, the temperature of reaction 360 DEG C ~ 500 DEG C of cooling regenerated catalyst and cracking C9 aromatic, reaction pressure is 0.2 ~ 0.4MPa; The temperature of reaction of regenerated catalyst and FCC main raw material 500 DEG C ~ 600 DEG C, reaction pressure 0.3 ~ 0.6MPa, the mass ratio of regenerated catalyst and FCC main raw material is 4:1 ~ 10:1.
6. hydrogen content method in reduction catalytic cracked dry gas according to claim 1, is characterized in that: FCC raw material is one or more mixing in long residuum, vacuum residuum, straight-run gas oil, wax tailings or hydrogenation tail oil.
7. hydrogen content method in reduction catalytic cracked dry gas according to claim 1, is characterized in that: the add-on of cracking C9 aromatic is 3% ~ 12% of FCC raw materials quality.
8. hydrogen content method in reduction catalytic cracked dry gas according to claim 1, it is characterized in that: catalyzer is zeolite, ultrastable Y－type zeolite, ZSM-5 series zeolite, the one, two or three had in five-membered ring structure high-silicon zeolite, β zeolite, ferrierite that active ingredient contains Y or HY, or amorphous silicon aluminium catalyzer.
9. hydrogen content method in reduction catalytic cracked dry gas according to claim 1, it is characterized in that: the structure of riser reactor is: a side lower part of the riser reactor body (1) of riser reactor arranges regenerator sloped tube (6), the opposite side of the riser reactor body (1) corresponding with regenerator sloped tube (6) arranges cracking C9 aromatic entrance (4); The bottom of riser reactor inside arranges pre-lift medium inlet (5), inner top arranges main raw material entrance (2), reactor dividing plate (3) is set between pre-lift medium inlet (5) and main raw material entrance (2), the lower part of riser reactor is divided into and is parallel to axial a reaction zone (7) and b reaction zone (8) by reactor dividing plate (3), and arranges corresponding catalyst inlet and raw material nozzles in each reaction zone.
10. hydrogen content method in reduction catalytic cracked dry gas according to claim 1, is characterized in that: the cross-sectional area ratio of a and b two reaction zone is 1:1 ~ 5:1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410331861.8A CN105273755A (en) | 2014-07-11 | 2014-07-11 | Method for reducing content of hydrogen in catalytic cracking dry gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410331861.8A CN105273755A (en) | 2014-07-11 | 2014-07-11 | Method for reducing content of hydrogen in catalytic cracking dry gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105273755A true CN105273755A (en) | 2016-01-27 |
Family
ID=55143603
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410331861.8A Pending CN105273755A (en) | 2014-07-11 | 2014-07-11 | Method for reducing content of hydrogen in catalytic cracking dry gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105273755A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107557070A (en) * | 2016-06-30 | 2018-01-09 | 中国石油化工股份有限公司 | In a kind of reduction catalytic cracked dry gas hydrogen methane than method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1340593A (en) * | 2000-08-30 | 2002-03-20 | 中国石油化工股份有限公司 | Contact method for catalytic cracking of oil |
| CN1340595A (en) * | 2000-08-30 | 2002-03-20 | 中国石油化工股份有限公司 | Feeding method for catalytic cracking of hydrocarbon oil |
| US20090107884A1 (en) * | 2007-10-31 | 2009-04-30 | Mehlberg Robert L | Stripping apparatus and process |
| CN101906314A (en) * | 2009-06-08 | 2010-12-08 | 中国石油化工股份有限公司 | Method for utilizing pyrolysis C9 by performing catalytic reforming |
-
2014
- 2014-07-11 CN CN201410331861.8A patent/CN105273755A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1340593A (en) * | 2000-08-30 | 2002-03-20 | 中国石油化工股份有限公司 | Contact method for catalytic cracking of oil |
| CN1340595A (en) * | 2000-08-30 | 2002-03-20 | 中国石油化工股份有限公司 | Feeding method for catalytic cracking of hydrocarbon oil |
| US20090107884A1 (en) * | 2007-10-31 | 2009-04-30 | Mehlberg Robert L | Stripping apparatus and process |
| CN101906314A (en) * | 2009-06-08 | 2010-12-08 | 中国石油化工股份有限公司 | Method for utilizing pyrolysis C9 by performing catalytic reforming |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107557070A (en) * | 2016-06-30 | 2018-01-09 | 中国石油化工股份有限公司 | In a kind of reduction catalytic cracked dry gas hydrogen methane than method |
| CN107557070B (en) * | 2016-06-30 | 2020-05-12 | 中国石油化工股份有限公司 | Method for reducing hydrogen-methane ratio in catalytic cracking dry gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102051213B (en) | Catalytic cracking method | |
| CN102206509B (en) | Hydrocarbon catalytic conversion method for producing propylene and light aromatic hydrocarbon | |
| CN102102028A (en) | Fractional and divisional catalytic cracking method and device for heavy oil | |
| CN102234531B (en) | Device for catalytically cracking heavy oil in sections and application thereof | |
| CN102233253B (en) | Riser catalysis device for processing heavy oil and application thereof | |
| CN103664454A (en) | Low energy consumption method for producing propylene through catalytic reforming of Fischer-Tropsch synthesis oil | |
| CN105505462A (en) | Catalytic cracking method of heavy oil and device thereof | |
| CN102086413B (en) | Hydrocarbon oil catalytic conversion method | |
| CN102268291B (en) | Catalytic cracking technology and device for reducing olefins in gasoline | |
| CN105273755A (en) | Method for reducing content of hydrogen in catalytic cracking dry gas | |
| CN102952575B (en) | Catalytic conversion method for increasing gasoline octane number | |
| CN106609151B (en) | A kind of method for producing low-carbon alkene | |
| CN105001907B (en) | A kind of method and system of paraffinic base crude oil with poor quality Poly-generation | |
| CN103666551A (en) | Catalytic processing method and catalytic processing device of high-temperature Fischer-Tropsch synthetic oil | |
| CN102234530B (en) | Pressure-reduced deep-drawing classified-partitioned combined process method for catalytic cracking of heavy oil | |
| CN102465036B (en) | Shale oil processing method for producing propylene | |
| CN105505459A (en) | Catalytic cracking method of heavy oil and device thereof | |
| CN102234532B (en) | Series-connected, partitioned and classified method and apparatus for catalytic cracking of heavy oil | |
| CN101906314A (en) | Method for utilizing pyrolysis C9 by performing catalytic reforming | |
| CN109679687B (en) | Catalytic conversion method for producing low-benzene high-octane gasoline | |
| CN102102027B (en) | Heavy oil serial graded and zoned catalytic conversion method and device | |
| CN102796558A (en) | Method for highly efficient catalytic conversion of petroleum hydrocarbons | |
| CN105505460A (en) | Catalytic cracking method of heavy oil and device thereof | |
| CN105419868A (en) | Heavy oil fluid catalytic cracking method and device | |
| CN105400546A (en) | Catalytic cracking method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160127 |
|
| RJ01 | Rejection of invention patent application after publication |