CN104726131A - Device and method for increasing hydrocarbon productivity employing catalyst and pre-deposit carbon - Google Patents
Device and method for increasing hydrocarbon productivity employing catalyst and pre-deposit carbon Download PDFInfo
- Publication number
- CN104726131A CN104726131A CN201510116549.1A CN201510116549A CN104726131A CN 104726131 A CN104726131 A CN 104726131A CN 201510116549 A CN201510116549 A CN 201510116549A CN 104726131 A CN104726131 A CN 104726131A
- Authority
- CN
- China
- Prior art keywords
- catalyzer
- carbon distribution
- catalytic cracking
- conduit
- catalyst
- 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.)
- Granted
Links
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
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a device and a method for increasing hydrocarbon productivity employing a catalyst and pre-deposit carbon. In the device, zeolite catalysts are output from a regenerator, react with raw materials with high efficient hydrogen-carbon ratio before entering a catalytic cracking reactor to form a relatively good catalytic reaction activity center, and then enter the catalytic cracking reactor to improve the productivity of a bio-oil/petroleum catalytic cracking target product and control the product distribution. The system comprises a catalyst and pre-deposit carbon system, a catalytic cracking reaction system and a catalyst regeneration system. According to the method and the device, an effective pathway is provided for efficient control on the bio-oil/petroleum catalytic cracking target product.
Description
Technical field
The invention belongs to bio oil/oil catalytic pyrolysis and biomass carbon distribution research field, relate to the method and apparatus of bio oil/oil catalytic pyrolysis, catalyst regeneration, the pre-carbon distribution of biomass material.
Background technology
For solving the contradiction between the petroleum resources of worsening shortages and the industrial requirement of sharp increase, rationally utilizing petroleum resources efficiently, Looking For Substitutions Of Oil is two effective methods.Bio oil, in some aspects can good petroleum replacing as the novel energy in recent years occurred, has higher economic worth and environmental benefit.
Bio oil/oil deep catalytic cracking technology is under normal pressure, higher reaction temperatures, bio oil/oil and catalyst exposure carry out deep pyrolytic with the low-carbon alkene such as increasing output of ethylene, propylene and lightweight aromatic hydrocarbon, used catalyst is mainly zeolite [molecular sieve, as ZSM-5, Y-shaped molecular sieve, LOSA-1, FCC etc.But current catalytic cracking reaction system still exists, and target product productive rate is low, catalyzer is easy to the problems such as coking and deactivation.The catalytic mechanism of Chinese scholars to zeolite [molecular sieve is studied, " hydrocarbon pond " is proposed theoretical: catalytic cracking reaction relies on zeolitic catalyst inside to form " hydrocarbon pond " to carry out, and the catalytic active center that " hydrocarbon pond " is made up of multi-methyl benzene.Can form multi-methyl benzene (carbon distribution process) by consumption reaction thing on avtive spot in initial reaction stage, once multi-methyl benzene is formed, reactant with it in conjunction with generation product, namely will carry out catalyzed reaction as catalytic active center.The quality of Gu Tingchi directly affects target product productive rate and selectivity of product.In traditional catalytic cracking reaction, form hydrocarbon pond by consuming bio oil/oil, but bio oil/oil oxygen level is high, grade is low, not easily forms hydrocarbon pond and product is difficult to regulation and control.Therefore we propose to adopt higher-grade raw material to carry out pre-carbon distribution, to form good catalytic reaction activity center, thus can improve products collection efficiency and regulation and control products distribution.Separately there are some researches show, in reactant composition, the ratio of H element and C element has remarkably influenced to alkene and aromatic hydrocarbon productive rate, catalyzer coking rate.Therefore by changing effective ratio of carbon-hydrogen to promote productive rate, the coking of minimizing catalyst surface of catalyse pyrolysis product.In carbon distribution test, optimum effective ratio of carbon-hydrogen is 1.2.
To sum up, proposed before bio oil/oil catalytic cracking reaction, the higher high available hydrogen carbon ratio raw material of available hydrogen carbon ratio and catalyst reaction is adopted to generate pre-carbon distribution, good catalytic reaction activity center is formed in catalyzer, thus improve catalyst activity and reduce coking, finally reach the object of raising bio oil/oil catalytic pyrolysis products collection efficiency and control products distribution.
Summary of the invention
Technical problem: the deep catalytic cracking technology of application at present, exists the problem that the productive rate of target product and low-carbon alkene is lower.In addition, activity of molecular sieve catalysts used is more weak, easy coking and deactivation in catalytic pyrolysis process.In the face of the industrial requirement of constantly change, prior art can not regulate products distribution according to demand, causes the waste of raw material.Therefore, need development new technologies badly to strengthen catalyst activity, to improve target product productive rate, and by regulating products distribution, to meet industrial requirement to the process of catalyzer; The present invention proposes the apparatus and method that the pre-carbon distribution of a kind of catalyzer increases hydro carbons productive rate thus.
Technical scheme: for achieving the above object, the technical scheme used is as follows: on traditional cat-cracker basis, set up pre-carbon distribution reactor, catalyzer before entering catalytic cracking reaction device with high available hydrogen carbon ratio raw material reaction, generate pre-carbon distribution, these carbon distributions are good catalytic reaction activity centers, can reduce catalyzer coking, improve hydrocarbons productive rate.This process is carried out under normal pressure, moderate temperature, and can form reactive hydrocarbon pond in catalyzer in the short period of time, and the treatment time is short, and technique is simple.
This device comprises:
The pre-carbon distribution system of catalyzer, for according to charge proportion, makes catalyzer and pre-carbon distribution raw material fully react, and forms the pre-carbon distribution of catalyst surface that massfraction is 1-3%;
Catalytic cracking reaction system, for bio oil or oil catalytic pyrolysis are prepared low-carbon alkene and lightweight aromatic hydrocarbon, the conveying of realization response product and reclaimable catalyst simultaneously;
Catalyst regeneration system, is used for the reclaimable catalyst of carbon deposit to carry out burning reaction, completes the regeneration of catalyzer and realizes the conveying of catalyzer;
Catalytic cracking reaction device is conveying bed, and dual-side, respectively with bio oil or oil entrance, the 4th conduit is connected, is incondensable gas entrance bottom catalytic cracking reaction device, and catalytic cracking reaction device top is connected with the first cyclonic separator; First cyclonic separator upper outlet is connected with separation column by the first conduit, and the lower outlet of the first cyclonic separator is connected with revivifier by conduit; Separation column side is products export; Regenerator bottoms is gas inlet, and top is connected with the second cyclonic separator; Export under second cyclonic separator and be connected with pre-carbon distribution reactor by the 3rd conduit, upper outlet is revivifier offgas outlet; Pre-carbon distribution reactor side is cross air blow entrance, and bottom is high available hydrogen carbon ratio feed(raw material)inlet; Pre-carbon distribution reactor is connected with catalytic cracking reaction device by conduit, makes catalyzer continuous recycle in reactive system.
Described pre-carbon distribution reactor is divided into four reaction chambers by three pieces of dividing plates: material supply chamber, the first material transferring room, the second material transferring room, returning charge room; Material supply chamber is connected with revivifier by conduit; Material supply chamber side is cross air blow entrance, and bottom material supply chamber, the first material transferring room, the second material transferring room uniform three high available hydrogen carbon ratio feed(raw material)inlets, and returning charge room is connected with catalytic cracking reaction device by the 4th conduit.
Described pre-carbon distribution raw material is methyl alcohol, ethanol.
The method that the pre-carbon distribution of catalyzer of the present invention increases hydro carbons productive rate is:
Fresh regenerated catalyst enters the material supply chamber top of pre-carbon distribution reactor by the 3rd conduit, and rare gas element blasts from cross air blow entrance, carries catalyzer flow forward; Do carrier gas with nitrogen, blast bottom after high available hydrogen carbon ratio feed vaporization point of three route material supply chambers, the first material transferring room, the second material transferring room, the abundant hybrid reaction with catalyzer, generates pre-carbon distribution at ambient pressure; In addition, do carrier gas with nitrogen and can provide power for conveying catalyzer, improve reaction chamber internal pressure, to prevent in catalytic cracking reaction device gas to anti-channeling in pre-carbon distribution reactor, play good sealing function, the catalyzer completing pre-carbon distribution enters catalytic cracking reaction device by the 4th conduit;
Utilize revivifier tail gas preheating bio oil or oil to 200 DEG C, again bio oil or oil are passed into catalytic cracking reaction device, the catalyzer inputted with pre-carbon distribution reactor carries out scission reaction at normal pressure, 500-700 DEG C, incondensable gas is as fluidizing agent, pass into bottom catalytic cracking reaction device, reactant and catalyzer are fully mixed; Reaction product enters the first cyclonic separator from catalytic cracking reaction device top, and the oil gas that reaction generates is separated, and enter separation column segmentation condensation and obtain desired product, all the other incondensable gases return catalytic cracking reaction device as fluidizing agent; Coked catalyst then enters revivifier by the second conduit;
Air enters from regenerator bottoms, carry out burning reaction at normal pressure, 600-800 DEG C with reclaimable catalyst, burn tail gas to carry live catalyst and enter the second cyclonic separator and be separated, the heat heatable catalyst that reaction produces, provide thermal source for subsequent reactions, isolated the 3rd conduit that is regenerated catalyst through enters pre-carbon distribution reactor, so far realizes the recycle of catalyzer; Revivifier tail gas then leaves from the second cyclonic separator top, as the preheating thermal source before bio oil/petroleum cracking.
Beneficial effect: apparatus and method of the present invention have following characteristic and advantage: utilize the method for the pre-carbon distribution of high-quality feedstocks to strengthen the activity of catalyzer, thus improve the productive rate of bio oil/oil catalytic pyrolysis target product.By changing the ratio of pre-carbon distribution raw material and catalyzer, can products distribution be regulated and controled, meeting the industrial requirement of constantly change.This process is carried out under normal pressure, moderate temperature, and can form reactive hydrocarbon pond in catalyzer in the short period of time, and the treatment time is short, and technique is simple.Further, the gas-phase product generated in pre-carbon distribution reaction process can directly pass into catalytic cracking reaction device, and then is converted into required Industrial products.This pre-carbon distribution method enhances catalyst activity, reduces catalyzer coking, effectively can improve products collection efficiency.The raw materials such as the methyl alcohol that pre-carbon distribution uses be easy to obtain, cheap, therefore the method has good economy and feasibility.
Accompanying drawing explanation
Fig. 1 is the device schematic diagram that in bio oil/oil catalytic pyrolysis, the pre-carbon distribution of catalyzer increases hydro carbons productive rate.
Fig. 2 is the structural representation of pre-carbon distribution reactor.
Have in figure: catalytic cracking reaction device 1, first cyclonic separator 2, second cyclonic separator 7, first conduit 3, second conduit 5,3rd conduit the 8, four conduit 10, separation column 4, revivifier 6, pre-carbon distribution reactor 9, bio oil or oil entrance I, incondensable gas entrance II, products export III, gas inlet IV, revivifier offgas outlet V, cross air blow entrance VI, high available hydrogen carbon ratio feed(raw material)inlet VII, material supply chamber I, the first material transferring room II, the second material transferring room III, returning charge room IV.
Embodiment
The invention provides the device that the pre-carbon distribution of catalyzer in a kind of bio oil/oil catalytic pyrolysis increases hydro carbons productive rate, comprise the pre-carbon distribution system of catalyzer, catalytic cracking reaction system, catalyst regeneration system.Regenerated catalyst is before entering catalytic cracking reaction device, with pre-carbon distribution raw material (high available hydrogen carbon ratio raw material, as methyl alcohol, ethanol etc.) fully react, form the pre-carbon distribution of catalyst surface that massfraction is 1-3%, then enter catalytic cracking reaction device.In catalytic cracking reaction device, bio oil/oil catalytic pyrolysis prepares the various product such as low-carbon alkene and lightweight aromatic hydrocarbon, simultaneously realization response product and reclaimable catalyst conveying be separated.In a regenerator, isolated coked catalyst carries out burning reaction, completes the regeneration of catalyzer and realizes the conveying of catalyzer.So far the recycle of catalyzer is completed.
By reference to the accompanying drawings 1, in bio oil/oil catalytic pyrolysis, the pre-carbon distribution of catalyzer increases in the device of hydro carbons productive rate, catalytic cracking reaction device is conveying bed, dual-side is connected with bio oil/oil entrance, conduit respectively, be incondensable gas entrance bottom catalytic cracking reaction device, catalytic cracking reaction device top is connected with cyclonic separator; Cyclonic separator upper outlet is connected with separation column by conduit, lower outlet is connected with revivifier by conduit; Separation column side is products export, top is incondensable gas outlet.Regenerator bottoms is gas inlet, top is connected with cyclonic separator; Export under cyclonic separator be connected with pre-carbon distribution reactor by conduit, upper outlet is revivifier offgas outlet.Pre-carbon distribution reactor side is cross air blow entrance, bottom is high available hydrogen carbon ratio feed(raw material)inlet; Pre-carbon distribution reactor is connected with catalytic cracking reaction device by conduit, makes catalyzer continuous recycle in reactive system.Pre-carbon distribution reactor is divided into four reaction chambers by three pieces of dividing plates: material supply chamber I, the first material transferring room II, the second material transferring room III, returning charge room IV.Material supply chamber is connected with revivifier by conduit; Material supply chamber side is cross air blow entrance.Uniform three high available hydrogen carbon ratio feed(raw material)inlets bottom material supply chamber I, the first material transferring room II, the second material transferring room III.Returning charge room is connected with catalytic cracking reaction device by conduit.Described bio oil/oil catalytic cracking reaction system can increase hydrocarbons productive rate: on traditional cat-cracker basis, set up pre-carbon distribution reactor, catalyzer before entering catalytic cracking reaction device with high available hydrogen carbon ratio raw material reaction, generate pre-carbon distribution, these carbon distributions are good catalytic reaction activity centers, catalyzer coking can be reduced, improve hydrocarbons productive rate.High available hydrogen carbon ratio raw material is the material that methyl alcohol etc. has high available hydrogen carbon ratio.
In bio oil/oil catalytic pyrolysis, the pre-carbon distribution of catalyzer increases the method for hydro carbons productive rate is carry out pre-carbon distribution to catalyzer before catalytic cracking reaction, to form good catalytic reaction activity center, concrete grammar is as follows: fresh regenerated catalyst enters the material supply chamber top of pre-carbon distribution reactor by conduit, rare gas element blasts from cross air blow entrance, carries catalyzer flow forward.Do carrier gas with nitrogen, blast bottom after high available hydrogen carbon ratio feed vaporization point of three route material supply chamber I, the first material transferring room II, the second III room, material transferring room, the abundant hybrid reaction with catalyzer, generates pre-carbon distribution at ambient pressure; In addition, power can be provided for conveying catalyzer again, improve reaction chamber internal pressure, prevent gas in catalytic cracking reaction device from, to anti-channeling in pre-carbon distribution reactor, playing good sealing function.The catalyzer completing pre-carbon distribution enters catalytic cracking reaction device by conduit.Utilize reheater tail gas preheating bio oil/oil to 200 DEG C, again bio oil/oil is passed into catalytic cracking reaction device, the catalyzer inputted with pre-carbon distribution reactor carries out scission reaction at normal pressure, 500-700 DEG C, incondensable gas is as fluidizing agent, pass into bottom catalytic cracking reaction device, reactant and catalyzer are fully mixed.Reaction product enters cyclonic separator from catalytic cracking reaction device top, and the oil gas that reaction generates is separated, and enter separation column segmentation condensation and obtain desired product, all the other incondensable gases return catalytic cracking reaction device as fluidizing agent; Coked catalyst then enters revivifier by conduit.Air enters from regenerator bottoms, carries out burning reaction at normal pressure, 600-800 DEG C with reclaimable catalyst, burns tail gas and carries live catalyst and enter cyclonic separator and be separated.The heat heatable catalyst that reaction produces, provide thermal source for subsequent reactions.The isolated conduit that is regenerated catalyst through enters pre-carbon distribution reactor, so far realizes the recycle of catalyzer.Revivifier tail gas then leaves from cyclonic separator top, as the preheating thermal source before bio oil/petroleum cracking.
Described bio oil/oil catalytic cracking reaction system can increase hydrocarbons productive rate: on traditional cat-cracker basis, set up pre-carbon distribution reactor, catalyzer before entering catalytic cracking reaction device with high available hydrogen carbon ratio raw material reaction, generate pre-carbon distribution, these carbon distributions are good catalytic reaction activity centers, catalyzer coking can be reduced, improve hydrocarbons productive rate.High available hydrogen carbon ratio raw material is the material that methyl alcohol etc. has high available hydrogen carbon ratio.
The pre-carbon distribution reactor proposed by the present invention as shown in Figure 2.
In this example pre-carbon distribution raw material to be available hydrogen carbon ratio be 2 methyl alcohol, zeolites ZSM-5 catalyzer selected by catalyzer, and catalytic pyrolysis raw material is bio oil.Fresh regenerated catalyst enters the material supply chamber top of pre-carbon distribution reactor by conduit, and nitrogen blasts from cross air blow entrance, carries catalyzer flow forward.Carrier gas is done with nitrogen, blast bottom after methyl alcohol vaporizing point of three route material supply chamber I, the first material transferring room II, the second material transferring room III, the abundant hybrid reaction with catalyzer at ambient pressure, generate pre-carbon distribution, these carbon distributions are good catalytic reaction activity centers, catalyzer coking can be reduced, improve hydrocarbons productive rate.In addition, do carrier gas with nitrogen and can provide power for conveying catalyzer, improve reaction chamber internal pressure, prevent gas in catalytic cracking reaction device from, to anti-channeling in pre-carbon distribution reactor, playing good sealing function.The catalyzer completing pre-carbon distribution enters catalytic cracking reaction device by conduit.
Utilize revivifier tail gas preheating bio oil to 200 DEG C, again bio oil is passed into catalytic cracking reaction device, the catalyzer inputted with pre-carbon distribution reactor carries out scission reaction at normal pressure, at 500 DEG C, incondensable gas is as fluidizing agent, pass into bottom catalytic cracking reaction device, reactant and catalyzer are fully mixed.Reaction product enters cyclonic separator from catalytic cracking reaction device top, the oil gas that reaction generates is separated, enter separation column segmentation condensation and obtain the product such as low-carbon alkene, lightweight aromatic hydrocarbon, all the other incondensable gases return catalytic cracking reaction device as fluidizing agent; Coked catalyst then enters revivifier by conduit.Air enters from regenerator bottoms, carries out burning reaction at normal pressure, at 650 DEG C with reclaimable catalyst, burns tail gas and carries live catalyst and enter cyclonic separator and be separated.The heat heatable catalyst that reaction produces, provide thermal source for subsequent reactions.The isolated conduit that is regenerated catalyst through enters pre-carbon distribution reactor, so far realizes the recycle of catalyzer.Revivifier tail gas then leaves from cyclonic separator top, as the preheating thermal source before bio oil cracking.
The foregoing is only better embodiment of the present invention; protection scope of the present invention is not limited with above-mentioned embodiment; in every case those of ordinary skill in the art modify or change according to the equivalence that disclosed content is done, and all should include in the protection domain recorded in claims.
Claims (4)
1. the pre-carbon distribution of catalyzer increases a device for hydro carbons productive rate, it is characterized in that: this device comprises:
The pre-carbon distribution system of catalyzer, for according to charge proportion, makes catalyzer and pre-carbon distribution raw material fully react, and forms the pre-carbon distribution of catalyst surface that massfraction is 1-3%;
Catalytic cracking reaction system, for bio oil or oil catalytic pyrolysis are prepared low-carbon alkene and lightweight aromatic hydrocarbon, the conveying of realization response product and reclaimable catalyst simultaneously;
Catalyst regeneration system, is used for the reclaimable catalyst of carbon deposit to carry out burning reaction, completes the regeneration of catalyzer and realizes the conveying of catalyzer;
Catalytic cracking reaction device (1) is conveying bed, dual-side is connected with bio oil or oil entrance (I), the 4th conduit (10) respectively, catalytic cracking reaction device (1) bottom is incondensable gas entrance (II), and catalytic cracking reaction device (1) top is connected with the first cyclonic separator (2); First cyclonic separator (2) upper outlet is connected with separation column (4) by the first conduit (3), and the lower outlet of the first cyclonic separator (2) is connected with revivifier (6) by conduit (5); Separation column (4) side is products export (III); Revivifier (6) bottom is gas inlet (IV), and top is connected with the second cyclonic separator (7); Export under second cyclonic separator (7) and be connected with pre-carbon distribution reactor (9) by the 3rd conduit (8), upper outlet is revivifier offgas outlet (V); Pre-carbon distribution reactor (9) side is cross air blow entrance (VI), and bottom is high available hydrogen carbon ratio feed(raw material)inlet (VII); Pre-carbon distribution reactor (9) is connected with catalytic cracking reaction device (1) by conduit (10), makes catalyzer continuous recycle in reactive system.
2. the pre-carbon distribution of a kind of catalyzer according to claim 1 increases the device of hydro carbons productive rate, it is characterized in that: described pre-carbon distribution reactor (9) is divided into four reaction chambers by three pieces of dividing plates: material supply chamber (I), the first material transferring room (II), the second material transferring room (III), returning charge room (IV); Material supply chamber (I) is connected with revivifier (6) by conduit (8); Material supply chamber (I) side is cross air blow entrance (VI), material supply chamber (I), the first material transferring room (II), the second uniform three high available hydrogen carbon ratio feed(raw material)inlets (VII) in bottom, material transferring room (III), returning charge room (IV) is connected with catalytic cracking reaction device (1) by the 4th conduit (10).
3. the pre-carbon distribution of a kind of catalyzer according to claim 1 increases the device of hydro carbons productive rate, it is characterized in that: described pre-carbon distribution raw material is methyl alcohol, ethanol.
4. the pre-carbon distribution of the catalyzer of device increases a method for hydro carbons productive rate as claimed in claim 1, it is characterized in that:
Fresh regenerated catalyst enters material supply chamber (I) top of pre-carbon distribution reactor (9) by the 3rd conduit (8), and rare gas element blasts from cross air blow entrance (VI), carries catalyzer flow forward; Carrier gas is done with nitrogen, after high available hydrogen carbon ratio feed vaporization point of three route material supply chambers (I), the first material transferring room (II), the second bottom, material transferring room (III) are blasted, the abundant hybrid reaction with catalyzer, generates pre-carbon distribution at ambient pressure; In addition, do carrier gas with nitrogen and can provide power for conveying catalyzer, improve reaction chamber internal pressure, prevent catalytic cracking reaction device (1) interior gas to the interior anti-channeling of pre-carbon distribution reactor (9), play good sealing function, the catalyzer completing pre-carbon distribution enters catalytic cracking reaction device (1) by the 4th conduit (10);
Utilize revivifier tail gas preheating bio oil or oil to 200 DEG C, again bio oil or oil are passed into catalytic cracking reaction device (1), the catalyzer inputted with pre-carbon distribution reactor (9) carries out scission reaction at normal pressure, 500-700 DEG C, incondensable gas is as fluidizing agent, pass into from catalytic cracking reaction device (1) bottom, reactant and catalyzer are fully mixed; Reaction product enters the first cyclonic separator (2) from catalytic cracking reaction device (1) top, the oil gas that reaction generates is separated, enter separation column (4) segmentation condensation and obtain desired product, all the other incondensable gases return catalytic cracking reaction device (1) as fluidizing agent; Coked catalyst then enters revivifier (6) by the second conduit (5);
Air enters from revivifier (6) bottom, carry out burning reaction at normal pressure, 600-800 DEG C with reclaimable catalyst, burn tail gas to carry live catalyst and enter the second cyclonic separator (7) and be separated, the heat heatable catalyst that reaction produces, provide thermal source for subsequent reactions, isolated the 3rd conduit (8) that is regenerated catalyst through enters pre-carbon distribution reactor (9), so far realizes the recycle of catalyzer; Revivifier tail gas then leaves from the second cyclonic separator (7) top, as the preheating thermal source before bio oil/petroleum cracking.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510116549.1A CN104726131B (en) | 2015-03-17 | 2015-03-17 | The pre-carbon distribution of a kind of catalyst increases the apparatus and method of hydro carbons productivity |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510116549.1A CN104726131B (en) | 2015-03-17 | 2015-03-17 | The pre-carbon distribution of a kind of catalyst increases the apparatus and method of hydro carbons productivity |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104726131A true CN104726131A (en) | 2015-06-24 |
| CN104726131B CN104726131B (en) | 2016-06-08 |
Family
ID=53450558
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510116549.1A Active CN104726131B (en) | 2015-03-17 | 2015-03-17 | The pre-carbon distribution of a kind of catalyst increases the apparatus and method of hydro carbons productivity |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104726131B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11680210B2 (en) * | 2021-11-04 | 2023-06-20 | Chevron U.S.A. Inc. | Catalytic cracking of glyceride oils with deactivated phosphorus-containing ZSM-5 light olefins additives |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5158670A (en) * | 1989-12-27 | 1992-10-27 | Exxon Research And Engineering Company | Hydrocarbon catalytic cracking utilizing a precoked catalyst |
| CN1268402A (en) * | 1999-03-30 | 2000-10-04 | 中国石油化工集团公司 | Catalyst for producing ethylbenzene and its preparation method |
| CN1380898A (en) * | 2000-05-19 | 2002-11-20 | 埃克森美孚化学专利公司 | Process for selectively producing propylene in fluid catalytic cracking process |
| CN101270023A (en) * | 2008-04-11 | 2008-09-24 | 中国石油化工股份有限公司 | Method for improving selectivity of light olefin hydrocarbon |
| CN101362961A (en) * | 2007-08-09 | 2009-02-11 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing aromatic hydrocarbons and light olefins |
| CN102464536A (en) * | 2010-11-17 | 2012-05-23 | 中国石油化工股份有限公司 | Method for producing low carbon olefin |
-
2015
- 2015-03-17 CN CN201510116549.1A patent/CN104726131B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5158670A (en) * | 1989-12-27 | 1992-10-27 | Exxon Research And Engineering Company | Hydrocarbon catalytic cracking utilizing a precoked catalyst |
| CN1268402A (en) * | 1999-03-30 | 2000-10-04 | 中国石油化工集团公司 | Catalyst for producing ethylbenzene and its preparation method |
| CN1380898A (en) * | 2000-05-19 | 2002-11-20 | 埃克森美孚化学专利公司 | Process for selectively producing propylene in fluid catalytic cracking process |
| CN101362961A (en) * | 2007-08-09 | 2009-02-11 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing aromatic hydrocarbons and light olefins |
| CN101270023A (en) * | 2008-04-11 | 2008-09-24 | 中国石油化工股份有限公司 | Method for improving selectivity of light olefin hydrocarbon |
| CN102464536A (en) * | 2010-11-17 | 2012-05-23 | 中国石油化工股份有限公司 | Method for producing low carbon olefin |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11680210B2 (en) * | 2021-11-04 | 2023-06-20 | Chevron U.S.A. Inc. | Catalytic cracking of glyceride oils with deactivated phosphorus-containing ZSM-5 light olefins additives |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104726131B (en) | 2016-06-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101333142B (en) | Starting method of reaction-regenerative device for preparing low carbon olefin form methanol | |
| CN101279877B (en) | Method for increasing yield of ethylene and propone in conversion process of oxocompound | |
| CN103193574B (en) | On-stream method of methanol to light olefin reaction-regeneration device | |
| CN103804110B (en) | Organic oxygen-containing compound producing light olefins and C 5+hydrocarbon catalytic pyrolysis coupling technique | |
| CN104479720B (en) | Living beings binary catalyst pyrolysis high yield is produced the method and apparatus of hydrocarbon compound | |
| CN101328101B (en) | Rapid parking method of methanol to olefins reaction-regeneration system | |
| CN101279875A (en) | Method for increasing production of ethylene and propone | |
| CN101029248B (en) | Method for increasing light olefin yield | |
| CN102603457B (en) | Production device and process for generating propylene by utilizing C3 and C4 in liquid gas deep processing | |
| CN100567460C (en) | Utilize catalyzing and cracking light-hydrocarbon material to prepare the method and the device of low-carbon alkene | |
| CN101811072B (en) | Regeneration control method in methanol-to-olefins reaction process | |
| CN101327447B (en) | Method for reducing catalyst contamination in reaction for preparing light olefins from methanol | |
| CN101306969B (en) | Reaction device for preparing low-carbon olefin from oxygen-containing compounds | |
| CN101318870A (en) | Process for improving yield of ethylene and propylene | |
| CN102559240B (en) | Dual-cycle mode catalytic cracking reaction regenerative system production technology and device | |
| CN110194967B (en) | Catalytic reaction regeneration method for producing more propylene | |
| CN102746873B (en) | Method for preparing ethylene and propylene through catalytic cracking of light hydrocarbons | |
| CN102485840B (en) | Catalytic cracking method and device thereof | |
| CN104726131B (en) | The pre-carbon distribution of a kind of catalyst increases the apparatus and method of hydro carbons productivity | |
| CN101279876A (en) | Method for preparing ethylene and propone with oxocompound | |
| CN104478642A (en) | Device and method for producing olefin from methanol | |
| CN105983455A (en) | Regeneration method of catalyst for producing aromatic hydrocarbon from organic oxide through catalytic conversion | |
| CN102875294B (en) | Start-up method of reaction-regeneration device for preparing low-carbon olefins from methanol | |
| CN101941874A (en) | Method for producing low-carbon olefins | |
| CN102276391B (en) | Method for catalyzing and converting methanol and naphtha into low-carbon olefins |
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 |