CN101463268B - Hydrocarbon oil transforming method - Google Patents
Hydrocarbon oil transforming method Download PDFInfo
- Publication number
- CN101463268B CN101463268B CN2007101797020A CN200710179702A CN101463268B CN 101463268 B CN101463268 B CN 101463268B CN 2007101797020 A CN2007101797020 A CN 2007101797020A CN 200710179702 A CN200710179702 A CN 200710179702A CN 101463268 B CN101463268 B CN 101463268B
- Authority
- CN
- China
- Prior art keywords
- catalyst
- oil
- oxygen
- gas
- containing 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.)
- Active
Links
Images
Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
The invention provides a hydrocarbon oil conversion method, comprising the steps of: under the condition of catalytic cracking, facilitating the hydrocarbon oil to contact a cracking catalyst in a catalytic cracking reactor to generate reaction oil and gas and a spent catalyst; separating the reaction oil and gas from the spent catalyst, feeding the spent catalyst into a catalyst regeneration system after steam stripping; in the catalyst regeneration system, facilitating the spent catalyst to contact an oxygen-containing gas to acquire a synthesis gas and a semi-regenerated catalyst, completely regenerating the semi-regenerated catalyst and feeding the regenerated catalyst into the catalytic cracking reactor for recycling, wherein, when the spent catalyst is in contact with the oxygen-containing gas, a residual oil is added into the catalyst regeneration system so that the residual oil is in contact with the spent catalyst and the oxygen-containing gas. The hydrocarbon oil conversion method of the invention has the advantages of high hydrogen yield and more internal heat supply in the gasification reaction.
Description
Technical field
The present invention is a kind of conversion method for hydrocarbon oil.
Background technology
Catalytic cracking is one of important means of oil secondary processing, is used for producing gasoline, diesel oil, liquefied gas etc. from heavy hydrocarbon oil.In general, cracking method for hydrocarbon oil is included under cracking conditions, hydrocarbon ils is contacted in catalyst cracker with catalyzer, hydrocarbon ils generates crackate (this crackate comprises light-end products, heavy oil product and gas) by cracking reaction under the effect of catalyzer, the sedimentation of coke that simultaneous reactions generates is on catalyzer, the catalyzer that deposits coke need to be regenerated and could again be used for catalytic cracking reaction, therefore is commonly referred to as reclaimable catalyst; Reclaimable catalyst is separated in reacting-settler with crackate, and reclaimable catalyst enters and enters revivifier regeneration after the reaction stripper removes the oil gas that carries, and obtains regenerated catalyst, and crackate enters subsequent separation system; Regenerated catalyst is sent in reactor and contacts with hydrocarbon ils, continues reaction.
Worldwide crude oil has the development trend of heaviness, in poor quality, and along with the enhancing of mankind's environmental consciousness, the strict degree of relevant environmental regulation is improving day by day.That is to say, need the refining of petroleum industry can utilize the stock oil of heaviness, in poor quality to produce high-quality processed oil in oligosaprobic situation.Wherein, hydrotreatment is the important means that improves processed oil yield and quality, plays very important effect in oil refining enterprise.But, " how obtaining the cheap hydrogen source of q.s? " it is a difficult problem of puzzlement oil refining enterprise.Although the highly purified hydrogen of catforming process energy by-product, this part amounts of hydrogen can not satisfy the demand of hydrogenation technique far away.Prior art also provides multiple other the hydrogen production process such as steam methane cracking hydrogen production, heavy oil hydrogen manufacturing, coal hydrogen manufacturing, but the hydrogen cost that these methods are produced is higher, occupy sizable ratio in whole hydrogenation cost, this can affect the economic benefit of whole hydrogenation process undoubtedly.Therefore, the source of emphasis hydrogen, particularly cheap hydrogen is a thing highly significant in the development hydrogenation technique.
In view of this, developed at present the catalytic cracking process of some co-producing hydrogens, for example publication No. is that the Chinese patent application of CN1400159A has disclosed a kind of method of utilizing regeneration fume from catalytic cracking hydrogen manufacturing, the method mainly comprises: in the first revivifier, reclaimable catalyst and oxygen-containing gas contact 2-25 after second under 500-660 ℃, the condition of gas empty bed speed 0.2-0.8 meter per second, regenerated flue gas is delivered to follow-up hydrogen production process.The method is suitable for the higher technological process of coke content on reclaimable catalyst.Yet, coke content lower (less than 1.2%) on the reclaimable catalyst of most of catalytic cracking processs, when total coke was low in the first revivifier or gasifying reactor, gasification reaction quantity of heat production (interior heat supply) was lower, just need to supply with from the outside more heat; In addition, cause the oxygen content in product gas higher, namely excess oxygen is more, can increase like this aftertreatment cost of product gas and affect hydrogen output (because hydrogen and oxygen reaction generate water, having consumed hydrogen).
Summary of the invention
There is the defective of heat supply deficiency in gasification reaction in the low and catalyst regeneration process of hydrogen yield in order to overcome existing conversion method for hydrocarbon oil, the invention provides that a kind of hydrogen yield is higher, the more conversion method for hydrocarbon oil of heat supply in gasification reaction.
Conversion method for hydrocarbon oil provided by the invention is included under catalytic cracking condition, hydrocarbon ils is contacted formation reaction oil gas and reclaimable catalyst in catalyst cracker with cracking catalyst; Separate described reaction oil gas and described reclaimable catalyst, described reclaimable catalyst is sent into catalyst regeneration system after stripping; In described catalyst regeneration system, described reclaimable catalyst is contacted with oxygen-containing gas, obtain synthetic gas and half regenerated catalyst, again with described half regenerated catalyst holomorphosis, regenerated catalyst is sent into described catalyst cracker and is recycled, wherein, and when described reclaimable catalyst contacts with oxygen-containing gas, add residual oil in catalyst regeneration system, residual oil is contacted with oxygen-containing gas with described reclaimable catalyst.
Conversion method for hydrocarbon oil of the present invention has advantages of that hydrogen yield is higher, the interior heat supply of gasification reaction is more.
Description of drawings
Fig. 1 is the schematic flow sheet of conversion method for hydrocarbon oil of the present invention.
Embodiment
Conversion method for hydrocarbon oil provided by the invention is included under catalytic cracking condition, hydrocarbon ils is contacted formation reaction oil gas and reclaimable catalyst in catalyst cracker with cracking catalyst; Separate described reaction oil gas and described reclaimable catalyst, described reclaimable catalyst is sent into catalyst regeneration system after stripping; In described catalyst regeneration system, described reclaimable catalyst is contacted with oxygen-containing gas, obtain synthetic gas and half regenerated catalyst, again with described half regenerated catalyst holomorphosis, regenerated catalyst is sent into described catalyst cracker and is recycled, wherein, and when described reclaimable catalyst contacts with oxygen-containing gas, add residual oil in catalyst regeneration system, residual oil is contacted with oxygen-containing gas with described reclaimable catalyst.
Described residual oil can disperse to enter through atomizing the gasification reaction layer in described catalyst regeneration system.The method of described residual oil atomizing can be the atomising method of routine, for example can be nozzle atomization and/or sparger atomizing, after atomizing, the oil droplet maximum diameter is 100 microns, 1 micron of minimum diameter, mean diameter can be between the 10-80 micron, between preferred 15-60 micron.Described residual oil can not affect for containing metal, sulfur-bearing, nitrogenous etc. the residual oil of any routine of gasification reaction, can be for example oil at the bottom of catalytically cracked oil and/or tank.
The present invention replenishes residual oil in catalyst regeneration system, this part residual oil generation synthetic gas that gasifies simultaneously on the one hand, replenish on the other hand the required heat of gasification reaction, accelerate the gasification reaction of the coke on reclaimable catalyst, thereby make the Control for Oxygen Content of described synthetic gas hang down scope.
Described hydrocarbon oil crude material can be residual oil or heavy hydrocarbon oil, and described residual oil or heavy hydrocarbon oil can be selected from: one or more at the bottom of heavy crude, acid-containing raw oil, tank in oil, normal pressure wax oil, long residuum, decompressed wax oil, vacuum residuum, wax tailings, deasphalted oil and hydrocracking tail oil.Described catalyzer is the catalyzer that hydrothermal stability has catalytic cracking activity preferably, for example can be for containing the cracking catalyst of molecular sieve, particularly contain or do not contain Y or HY type zeolite, the ultrastable Y－type zeolite that contains or do not contain rare earth, the ZSM-5 series zeolite of rare earth and have one or more cracking catalyst in supersiliceous zeolite, β zeolite and the ferrierite of five-membered ring structure, catalyzer can be also the amorphous silicon aluminium catalyzer.These cracking catalyst are conventionally known to one of skill in the art.Described catalyzer is preferably micro-activity scope (ASTM D3907-87) between 30-70, and particle size range is between 20-200 μ m.
described catalyst cracker can be the catalyst cracker of routine, for example can be riser reactor, at this moment, the method comprises in riser reactor sends into lifting WATER AS FLOW MEDIUM steam, the weight ratio of water vapor and hydrocarbon oil crude material can be 0.02-0.20: 1, the weight ratio of described catalyzer and described hydrocarbon oil crude material can be 4-15: 1, described catalytic cracking condition can comprise that temperature of reaction is 200 ℃-700 ℃, be preferably and be divided into 300 ℃-600 ℃ and 600 ℃-700 ℃ two stages, total reaction time can be 0.8-5 second, reaction pressure can be 130-450 kPa.
Described stripping process can be the stripping process of routine, for example can contact under 350-500 ℃ of condition with steam for described reclaimable catalyst oil gas is deviate from.
Described catalyst regeneration system can be catalyst regeneration system that can separating synthetic gas well known in the art, namely can be used for the present invention as long as install the device of conventional supply and atomizing residual oil in this system.
Described catalyst regeneration system can comprise a plurality of revivifiers, is preferably to comprise the first revivifier and Second reactivator, and the device of described supply and atomizing residual oil is preferably and is arranged on the first revivifier.Described residual oil enters in described the first revivifier through atomizing, contacts with oxygen-containing gas with described reclaimable catalyst, and half regenerated catalyst of the part that is removed carbon deposit, described half regenerated catalyst contact with oxygen-containing gas in Second reactivator and generate regenerated catalyst.
In described the first revivifier, it is the 0.1-0.5 % by weight that described residual oil makes the carbon distribution of half regenerated catalyst that obtains with the condition that described reclaimable catalyst contacts with oxygen-containing gas.Described oxygen-containing gas is conventional gasification reaction gas, and being preferably volume ratio is 3-7: 1 water vapour and oxygen.Oxygen purity can affect the purity of synthetic gas, so in theory, oxygen purity is more high better, and purity for example can be between 98.0-99.9%, and oxygen can be from air separation by PSA unit or cryogenic air separation unit unit.Described residual oil comprises that with the condition that described reclaimable catalyst contacts with oxygen-containing gas Contact Temperature is 600-800 ℃, and the pressure of contact is 110-450 kPa, and be 0.5-20 second duration of contact, and gas space velocity is 30-200 hour
-1, the add-on of described residual oil is the 0.1-1 % by weight of the amount of the reclaimable catalyst that contacts with oxygen-containing gas.
In described Second reactivator, the condition that described half regenerated catalyst contacts with oxygen-containing gas makes the carbon distribution content of the regenerated catalyst that obtains less than 0.02 % by weight, is preferably less than 0.01 % by weight.Described oxygen-containing gas can be the oxygen-containing gas that is used for regenerated cracking catalyst of routine, can be for example oxygen-rich air for the mixed gas of air or air and oxygen, the condition that described half regenerated catalyst contacts with oxygen-containing gas comprises that Contact Temperature is 600-750 ℃, the pressure of contact is 100-450 kPa, be 5-35 second duration of contact, and the gas space velocity of oxygen-containing gas is 50-300 hour
-1, preferred 70-200 hour
-1
Described synthetic gas mainly contains carbonic acid gas, carbon monoxide and hydrogen.Conversion method for hydrocarbon oil provided by the invention can also comprise the carbon monoxide in synthetic gas is converted into hydrogen.The method that carbon monoxide is converted into hydrogen can be known water-gas shift method.Conversion method for hydrocarbon oil provided by the invention can also be before being converted into hydrogen with carbon monoxide and/or afterwards, and the sulfide in synthetic gas and/or carbonic acid gas are removed, and for example can reclaim sulfide by the Sulfur Recovery Unit mode.One or more methods that can pass through in pressure-variable adsorption, low-temperature rectisol, hot potash method, NHD (Polyethylene glycol dimethyl ether) gas washing method and Deep Cooling Method reclaim carbonic acid gas.Described transformation and hydrogen production method is preferably in the stagnant catalyst bed of two or more carries out, and it is that medium temperature shift catalyst, Cu-Zn are that low temperature shift catalyst and Co-Mo are one or more in sulfur-resistant transformation catalyst that the transformation catalyst that adopts is preferably Fe-Cr.
For the method for catalytic cracking provided by the invention and catalyst regeneration more clearly is described, based on top described, below in conjunction with Fig. 1, embodiments of the present invention are described consistently on the whole.In order to make description clear succinct, wherein some reactive component and reaction conditions to be done to describe more specifically, these reactive components and reaction conditions are all with reference to above description enforcement.
As shown in Figure 1, the catalyzer of packing in catalyst cracker 1, and to send into weight ratio in the catalyst cracker 1 be 0.02-0.20: 1 steam A and hydrocarbon oil crude material B, the weight ratio of catalyzer and hydrocarbon oil crude material B is 4-15: 1, keeping pressure is 130-450 kPa, described catalyzer and described hydrocarbon oil crude material react 300 ℃-600 ℃ and 600 ℃-700 ℃ two stages respectively, and total reaction time is 0.8-5 second.Separate the reaction oil gas C and the reclaimable catalyst D that generate, reclaimable catalyst is sent into stripper 2 and is contacted under 350-500 ℃ of part with steam E, makes the oil gas on described reclaimable catalyst D deviate to generate stripping gas F and reclaimable catalyst G.
Send into the first revivifier 3 through the reclaimable catalyst G after stripping, supplying with volume ratio in the first revivifier 3 is 3-7: the mixed gas H of 1 water vapor and oxygen, send into simultaneously the residual oil I of atomizing, and preheating temperature is between 120-350 ℃.In described the first revivifier 3, described residual oil contacts with oxygen-containing gas with described reclaimable catalyst, generate synthetic gas J and half regenerated catalyst K, it is the 0.1-0.5 % by weight that described residual oil makes the carbon distribution of half regenerated catalyst that obtains with the condition that described reclaimable catalyst contacts with oxygen-containing gas.
Half regenerated catalyst K sends into Second reactivator 4, and synthetic gas J sends into synthetic gas treatment system (not shown).Half regenerated catalyst contacts with oxygen-containing gas in Second reactivator 4 and generates regenerated catalyst generation regenerated catalyst M and flue gas N, and the condition that half regenerated catalyst contacts with oxygen-containing gas makes the carbon distribution content of the regenerated catalyst that obtains less than 0.02 % by weight.Regenerated catalyst M is sent in catalyst cracker 1 and recycles.
Below in conjunction with embodiment, the present invention is described in more detail.In following examples, reactive system used is equivalent to general catalytic cracking and catalyst regeneration system are transformed, namely install the device of conventional supply and atomizing residual oil in the first revivifier, described transformation does not affect the operation of reactive system and Second reactivator.
Raw material used in embodiment:
Catalyzer: the cracking catalyst that embodiment 1-3 and Comparative Examples 1-3 use is MLC-500 industry poiser, and China PetroChemical Corporation's Shandong catalyst plant is produced, and the character of this cracking catalyst is listed in table 1;
Hydrocarbon ils: the hydrocarbon ils that embodiment 1-3 and Comparative Examples 1-3 use is long residuum, and this long residuum character is listed in table 2;
Residual oil: the character of the residual oil that embodiment 1-3 uses is listed in table 3.
The pre-thermal recovery electrically heated of device Raw that embodiment adopts, there is auxiliary electrical heater the small riser outside.
Embodiment 1
This embodiment is used for illustrating conversion method for hydrocarbon oil provided by the invention.
As shown in Figure 1, use the hydrocarbon oil conversion system of laboratory 10 kg catalyst reserves.Catalyzer M after the interior holomorphosis of Second reactivator 4 is sent into the bottom of riser reactor 1, approximately 5 kg/hrs of catalyzer flow rates, send into weight ratio in the riser reactor 1 and be water vapor A and the hydrocarbon oil crude material B of 0.1: 1, the catalyzer flow rate is 5: 1 with the flow rate ratio of hydrocarbon oil crude material B, keeping pressure is 300 kPas, and described catalyzer M and described hydrocarbon oil crude material B were 500 ℃ of reactions of medial temperature 4 seconds.
Separate the reaction oil gas C and the reclaimable catalyst D that generate, reclaimable catalyst is sent into stripper 2 and is contacted under 480 ℃ with steam E, makes the oil gas on described reclaimable catalyst D deviate to form stripping gas F and reclaimable catalyst G.
Send into the first revivifier 3 through the reclaimable catalyst G after stripping, the flow rate of reclaimable catalyst G consistent with the flow rate of catalyzer M (coke content on reclaimable catalyst is lower), namely be about 5 kg/hrs, supply with volume ratio in the first revivifier 3 and be 3.71 water vapor and the mixed gas H of oxygen, reaction bed is fluidized-bed, and gas space velocity is 80 hours
-1Carry out gasification reaction under 700 ℃, add atomizing residual oil I in the time of gasification reaction in the first revivifier, the mean diameter of atomizing residual oil oil droplet is about 50 microns, flow rate is 20 Grams Per Hours, the gasification reaction time is 10 seconds, and through generating synthetic gas J and half regenerated catalyst K after gasification reaction, the composition of synthetic gas J is as shown in table 4.Half regenerated catalyst K send into Second reactivator 4 with air L in Second reactivator 4, generate regenerated catalyst M and flue gas N at 680 ℃ of temperature, in revivifier, gas residence time is 20 seconds, 310 kPas of gas outlet pressures.Regenerated catalyst M sends into riser reactor 1 and recycles.
Comparative Examples 1
This Comparative Examples is used for illustrating existing conversion method for hydrocarbon oil.
Removed the step of replenishing residual oil in embodiment 1 to the first revivifier, other operation steps is identical with embodiment 1.The composition of the synthetic gas J that generates in the first revivifier is as shown in table 4.
This embodiment is used for illustrating conversion method for hydrocarbon oil provided by the invention.
According to the method identical with embodiment 1, hydrocarbon ils is transformed, different is, in the first revivifier, gasifying gas is that volume ratio is 4.83 steam and the mixed gas of oxygen, temperature of reaction is 650 ℃, the flow rate of atomizing residual oil I is 40 Grams Per Hours, and the reaction times is 12 seconds, and other reaction conditions is identical with embodiment 1.The composition of the synthetic gas J that generates in the first revivifier is as shown in table 4.
Comparative Examples 2
This Comparative Examples is used for illustrating existing conversion method for hydrocarbon oil.
Removed the step of replenishing residual oil in embodiment 2 to the first revivifier, other operation steps is identical with embodiment 2.The composition of the synthetic gas J that generates in the first revivifier is as shown in table 4.
This embodiment is used for illustrating conversion method for hydrocarbon oil provided by the invention.
According to the method identical with embodiment 1, hydrocarbon ils is transformed, different is, in the first revivifier, temperature of reaction is 750 ℃, and the flow rate of atomizing residual oil I is 10 Grams Per Hours, and the reaction times is 10 seconds, and other reaction conditions is identical with embodiment 1.The composition of the synthetic gas J that generates in the first revivifier is as shown in table 4.
Comparative Examples 3
This Comparative Examples is used for illustrating existing conversion method for hydrocarbon oil.
Removed the step of replenishing residual oil in embodiment 2 to the first revivifier, other operation steps is identical with embodiment 3.The composition of the synthetic gas J that generates in the first revivifier is as shown in table 4.
Table 1
Table 2
Table 3
Table 4
Annotate: "-" expression does not measure corresponding gaseous fraction
In an embodiment, the residual oil and the oxygen generation thermopositive reaction that replenish have increased the interior heat supplied in the first revivifier.The composition of the reaction product gas that embodiment 1-3 and Comparative Examples 1-3 obtain from table 4 can be found out: the hydrogen content of the reaction product gas that embodiment 1-3 obtains obviously raises, can improve more than 30 percentage points under the same terms, available gas (carbon monoxide and hydrogen, carbon monoxide can be converted into hydrogen in subsequent process) total content also obviously raise, improve approximately 10 percentage points under the same terms, therefore can learn that conversion method for hydrocarbon oil provided by the invention has advantages of that hydrogen yield is higher.
Claims (13)
1. conversion method for hydrocarbon oil, the method is included under catalytic cracking condition, hydrocarbon ils is contacted formation reaction oil gas and reclaimable catalyst in catalyst cracker with cracking catalyst; Separate described reaction oil gas and described reclaimable catalyst, described reclaimable catalyst is sent into catalyst regeneration system after stripping; In described catalyst regeneration system, described reclaimable catalyst is contacted with oxygen-containing gas, obtain synthetic gas and half regenerated catalyst, described half regenerated catalyst is contacted with oxygen-containing gas again, make half regenerated catalyst holomorphosis, regenerated catalyst is sent into described catalyst cracker and is recycled, it is characterized in that, when described reclaimable catalyst contacts with oxygen-containing gas, add residual oil in catalyst regeneration system, residual oil is contacted with oxygen-containing gas with described reclaimable catalyst; Wherein, the oxygen-containing gas that contacts with described reclaimable catalyst is that volume ratio is water vapour and the oxygen of 3-7:1, described residual oil comprises that with the condition that described reclaimable catalyst contacts with oxygen-containing gas Contact Temperature is 600-800 ℃, and the condition that described half regenerated catalyst contacts with oxygen-containing gas comprises that Contact Temperature is 600-750 ℃.
2. method according to claim 1, wherein, add after the atomizing of described residual oil process.
3. method according to claim 2, wherein, described atomizing is nozzle atomization and/or sparger atomizing, after atomizing, the diameter of oil droplet is the 1-100 micron.
4. method according to claim 1, wherein, described catalyst regeneration system comprises the first revivifier and Second reactivator, described residual oil enters in described the first revivifier through atomizing, contact with oxygen-containing gas with described reclaimable catalyst, half regenerated catalyst of the part that is removed carbon deposit, described half regenerated catalyst contact with oxygen-containing gas in Second reactivator and generate regenerated catalyst.
5. method according to claim 4, wherein, the condition that described half regenerated catalyst contacts with oxygen-containing gas makes the carbon distribution content of the regenerated catalyst that obtains less than 0.02 % by weight; It is the 0.1-0.5 % by weight that described residual oil makes the carbon distribution of half regenerated catalyst that obtains with the condition that described reclaimable catalyst contacts with oxygen-containing gas.
6. method according to claim 1 or 5, wherein, described residual oil also comprises with the condition that described reclaimable catalyst contacts with oxygen-containing gas: the pressure of contact is 110-450 kPa, and be 0.5-20 second duration of contact, and the gas space velocity of oxygen-containing gas is 30-200 hour
-1, the add-on of described residual oil is the 0.1-1 % by weight of the amount of the reclaimable catalyst that contacts with oxygen-containing gas.
7. method according to claim 1 or 5, wherein, the condition that described half regenerated catalyst contacts with oxygen-containing gas also comprises: the pressure of contact is 100-450 kPa, and be 5-35 second duration of contact, and the gas space velocity of oxygen-containing gas is 50-300 hour
-1
8. the described method of any one according to claim 1-5, wherein, described residual oil is oil at the bottom of catalytically cracked oil and/or tank.
9. method according to claim 1, wherein, the method also comprises the carbon monoxide in synthetic gas is converted into hydrogen.
10. method according to claim 1, wherein, the method also comprises removes the sulfide in synthetic gas and/or carbonic acid gas.
11. method according to claim 1, wherein, described hydrocarbon ils is one or more in oil at the bottom of heavy crude, acid-containing raw oil, tank, normal pressure wax oil, long residuum, decompressed wax oil, vacuum residuum, wax tailings, deasphalted oil and hydrocracking tail oil.
12. method according to claim 1, wherein, described catalyst cracker is riser reactor, described catalytic cracking condition comprises that temperature of reaction is 200 ℃-700 ℃, reaction times is 0.8-5 second, reaction pressure is 130-450 kPa, and the weight ratio that promotes WATER AS FLOW MEDIUM steam and hydrocarbon oil crude material is 0.02-0.20:1, and the weight ratio of described catalyzer and described hydrocarbon oil crude material is 4-15:1.
13. method according to claim 1, wherein, described cracking catalyst is the cracking catalyst that contains molecular sieve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007101797020A CN101463268B (en) | 2007-12-17 | 2007-12-17 | Hydrocarbon oil transforming method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007101797020A CN101463268B (en) | 2007-12-17 | 2007-12-17 | Hydrocarbon oil transforming method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101463268A CN101463268A (en) | 2009-06-24 |
| CN101463268B true CN101463268B (en) | 2013-06-26 |
Family
ID=40804062
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007101797020A Active CN101463268B (en) | 2007-12-17 | 2007-12-17 | Hydrocarbon oil transforming method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101463268B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103055959B (en) * | 2011-10-24 | 2015-02-25 | 中国石油化工股份有限公司 | Catalyst regeneration method |
| CN103965958B (en) * | 2013-01-30 | 2015-12-02 | 中国石油天然气股份有限公司 | A kind of working method containing sour oil |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1371960A (en) * | 2002-03-29 | 2002-10-02 | 清华大学 | Gas and solid parallel flow upflow and downflow coupled catalytic cracking reaction technology and reactor thereof |
| US20040121898A1 (en) * | 2000-11-01 | 2004-06-24 | Mayes Warden W. | Catalytic cracking of a residuum feedstock to produce lower molecular weight gaseous products |
-
2007
- 2007-12-17 CN CN2007101797020A patent/CN101463268B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040121898A1 (en) * | 2000-11-01 | 2004-06-24 | Mayes Warden W. | Catalytic cracking of a residuum feedstock to produce lower molecular weight gaseous products |
| CN1371960A (en) * | 2002-03-29 | 2002-10-02 | 清华大学 | Gas and solid parallel flow upflow and downflow coupled catalytic cracking reaction technology and reactor thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101463268A (en) | 2009-06-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102031140B (en) | Combination method of gasification and coke processing from inferior heavy oil | |
| Ramachandran et al. | An overview of industrial uses of hydrogen | |
| CN102260529B (en) | Combined method for processing inferior heavy oil | |
| CN102378748A (en) | Hydropyrolysis of biomass for producing high quality liquid fuels | |
| CN102234534B (en) | Method for processing inferior heavy oil | |
| CN101845319B (en) | Process for producing wax and clean fuel oil by using biomass as raw material | |
| CN102300960B (en) | Method for refining FT synthetic oil and mixed crude oil | |
| CN102796559A (en) | Method and apparatus for producing fuel oil by hydrocracking | |
| CN101457152B (en) | Hydrocarbon oil conversion method | |
| CN102234535B (en) | Method for processing low-quality heavy oil and simultaneously producing synthetic gas | |
| CN102618324B (en) | Combination method for processing heavy oil raw material | |
| CN109111950B (en) | Method for producing liquid fuel by hydrogenating full-fraction tar | |
| CN101463268B (en) | Hydrocarbon oil transforming method | |
| CN102031135A (en) | Comprehensive processing and utilizing method for heavy oil | |
| CN101210195A (en) | Hydrocracking method for more producing chemical industry light oil from poor heavy raw material | |
| CN101463269B (en) | Hydrocarbon oil transforming method | |
| EP3165588A1 (en) | Process for production of syngas through regeneration of coked cracking agent | |
| WO2014110085A1 (en) | Direct coal liquefaction process | |
| US2628890A (en) | Process for the decomposition of hydrocarbons | |
| CN101875858B (en) | Method for treating solid particles of deposited carbon-containing compound | |
| JP4564176B2 (en) | Crude oil processing method | |
| CN106609151B (en) | A kind of method for producing low-carbon alkene | |
| US10487279B2 (en) | Production of high yield of syngas through regeneration of coked upgrading agent | |
| CN111689829A (en) | Method and device for preparing ethylene by catalytic conversion of petroleum hydrocarbon | |
| CN101210196A (en) | Conversion method for hydrocarbon oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |