CN101063041A - Method for regulating heat balance - Google Patents
Method for regulating heat balance Download PDFInfo
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- CN101063041A CN101063041A CN 200610076192 CN200610076192A CN101063041A CN 101063041 A CN101063041 A CN 101063041A CN 200610076192 CN200610076192 CN 200610076192 CN 200610076192 A CN200610076192 A CN 200610076192A CN 101063041 A CN101063041 A CN 101063041A
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Abstract
The invention discloses a method to adjust thermal balance, which comprises the following steps: reacting raw material and catalytic conversion activator; separating regenerated catalyst and reaction oil gas; leading the reaction oil gas to rear portion separation system; entering the regenerated catalyst into regenerator through carrier pipe; touching with oxygen-containing coke burning agent; transporting fine slaking coal into at least one position of regenerator; touching and burning with oxygen-containing agent. This method utilizes cheap coal as heat resource, which is fit for keeping the active of catalyst.
Description
Technical field
The invention belongs to the catalyst cracking method of hydrocarbon ils under the situation that does not have hydrogen, specifically, is to belong to the thermally equilibrated method of a kind of adjusting fluidized catalytic conversion process.
Background technology
In fluid catalytic cracking or fluidized catalytic cracking process, high-temperature regenerated catalyst enters riser tube or fluidized-bed bottom and stock oil contact reacts from the regenerated catalyst line.These stock oils comprise the mixture of gasoline, wax oil, residual oil or other mink cell focus and above raw material.In general, the reactant of riser reactor enters settling vessel, and at this separating catalyst and oil gas, this catalyzer contains sedimentary coke, is commonly referred to as reclaimable catalyst; Oil gas flows out from the settling vessel top and enters the rear portion separation system, and reclaimable catalyst enters revivifier by line of pipes behind stripping.Coke on the catalyzer in revivifier with oxygen-containing medium such as air catalytic combustion, the activity of burning the coke rear catalyst is able to produce a large amount of heats simultaneously to recover.The heats such as intensification heat that satisfy intensification such as logistics such as empyreumatic air heat, catalyzer in the revivifier when the heat of its generation require and satisfy the heat demand of reactor such as the stock oil heat that heats up, heat demand such as reaction heat, steam intensification heat are, the normal running continuously of this process, claim this process to reach thermal equilibrium this moment.
Sometimes the coke deposited on catalyst charcoal is subjected to factor restrictions such as operating parameters, stock oil character.Sometimes reaction heat is in great demand, and the growing amount of coke can not satisfy its required heat.When coke yield can not satisfy heat demand, need the outer heat of supplementary quota.Sometimes also thermally equilibrated problem can take place in the process of going into operation.
A kind of method of additional heat is that oil fuel is sprayed into revivifier, and stock oil can be stock oil or diesel oil distillate or other liquid fuel of fluid catalytic cracking or fluidized catalytic cracking process itself.Adopt this method generally can cause local temperature too high, thereby cause device impaired, also can cause adverse consequencess such as catalyst deactivation, catalyst structure avalanche.
The method that CN00124665.8 discloses is reclaimable catalyst is entered revivifier with oil fuel at catalyzer contacted in the past, increasing the amount of coke and the hydrocarbon amount of carrying on the catalyzer, thereby reaches the purpose of additional heat.This method need consume more relative high value fuel oil, and himself heats up simultaneously also needs suitable heat, and this method also can increase the load of reactive system in addition.
Another method is before catalyzer enters revivifier live catalyst, reclaimable catalyst, oil fuel and air to be mixed earlier.This method causes the regeneration temperature up to 800 ℃ sometimes, and this method also needs to consume more relative high value fuel oil in addition.
US6 in addition, 558,531 disclose the method for additional heat, and this method is divided into one or more snippets territory, injecting lift area under control with oil fuel before catalyzer enters revivifier, advance to contain oxygen other minute multistage simultaneously and inject this riser tube zone, with the required heat of replenishment system.This method equally also needs to consume more relative high value fuel oil.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of adjusting fluidized catalytic conversion process thermally equilibrated method.
The thermally equilibrated method of adjusting provided by the invention is as follows: raw material and catalytic converting catalyst contact reacts, separate reclaimable catalyst and reaction oil gas, reaction oil gas goes the rear portion separation system, reclaimable catalyst enters revivifier through transfer lime, with contain oxygen and burn medium and contact, will be through the coal of fine-powdered by transport medium at least one position in the revivifier, with the oxygen-containing medium catalytic combustion.
This method utilizes cheap coal as origin of heat, is fluid catalytic cracking or fluidized catalytic cracking process additional heat, and what of flexible additional heat as required.Different with the coke on the catalyzer is that therefore coal helps keeping activity of such catalysts not in the activity of such catalysts central burner.
Description of drawings
Accompanying drawing is the thermally equilibrated method flow synoptic diagram of adjusting provided by the invention.
Embodiment
A kind of method for fluid catalytic cracking or fluidized catalytic cracking process additional heat provided by the invention comprises:
Raw material and fluid catalytic cracking or fluidized catalytic cracking catalyzer contact reacts, separate reclaimable catalyst and reaction oil gas, reaction oil gas goes the rear portion separation system, and reclaimable catalyst enters revivifier through transfer lime, with contain oxygen and burn medium and contact, recover active after burning the coke that reclaimable catalyst carries.To with the oxygen-containing medium catalytic combustion, discharge the heat that heat needs with replenishment system through the coal microballoon of fine-powdered by transport medium at least one position in the revivifier.
The coal microballoon of described fine-powdered is that coal has the requirement of certain granules diameter after mechanical treatment or screening, and the coal microsphere diameter after mechanical treatment or screening is distributed as 5-500 μ m, and mean diameter is 30-200 μ m.Preferred coal microsphere diameter is distributed as 20-300 μ m, and mean diameter is 40-100 μ m.
The coal microballoon of described fine-powdered is transported at least one position in the revivifier, more preferably 2-4 position.
The coal microballoon entry site of described fine-powdered can be installed coal microballoon sparger, so that this coal microballoon distributes in revivifier as required, and also coal microballoon sparger not, but result of use is poor slightly.
The coal microballoon of described fine-powdered is transported in the revivifier, can mix with reclaimable catalyst earlier, enters revivifier then jointly, also can enter revivifier separately.
The coal microballoon delivery medium of described fine-powdered can make oxygen-containing medium such as air, oxygen etc., also can be oxygen-free medium such as nitrogen, more preferably oxygen-containing medium.
The coal microballoon of described fine-powdered is at normal temperature or do not influence under temperature that coal microsphere particle diameter requires or other condition and carry.
The coal microballoon of described fine-powdered can adopt dilute phase or close phase mode to carry.
Described raw material petroleum hydrocarbon and/or other mineral oil, wherein petroleum hydrocarbon is selected from decompressed wax oil (VGO), normal pressure wax oil (AGO), wax tailings (CGO), deasphalted oil (DAO), vacuum residuum (VR), long residuum (AR), diesel oil, gasoline, carbonatoms is the hydrocarbon of 4-8, carbonatoms is a kind of in the alkane of 2-3 or more than one mixture wherein, other mineral oil is liquefied coal coil, tar sand oil, the described raw material of shale oil is petroleum hydrocarbon and/or other mineral oil, wherein petroleum hydrocarbon is selected from decompressed wax oil (VGO), normal pressure wax oil (AGO), wax tailings (CGO), deasphalted oil (DAO), vacuum residuum (VR), long residuum (AR), diesel oil, gasoline, carbonatoms is the hydrocarbon of 4-8, carbonatoms is a kind of in the alkane of 2-3 or more than one mixture wherein, and other mineral oil is liquefied coal coil, tar sand oil, shale oil.
Wherein VGO, AGO, CGO, DAO, VR, AR, diesel oil, gasoline are the full cut or the part cut of not hydrogenation, or be behind the hydrogenation full cut or part cut.
The catalyzer that the present invention is suitable for can be that active ingredient is selected from a kind of, two or three the catalyzer in Y or HY type zeolite, the ultrastable Y that contains or do not contain rare earth, the ZSM-5 series zeolite that contains or do not contain rare earth or the supersiliceous zeolite with five-membered ring structure, the β zeolite, also can be the amorphous silicon aluminium catalyzer.Generally speaking, the method for this patent be adapted to the catalyzer of the catalytic cracking that is useful on and fluidized catalytic cracking.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but does not therefore limit the present invention.
Accompanying drawing is the thermally equilibrated method flow synoptic diagram of adjusting provided by the invention.
Its technical process is as follows:
Claims (9)
1, the thermally equilibrated method of a kind of adjusting, raw material and catalytic converting catalyst contact reacts, separate reclaimable catalyst and reaction oil gas, reaction oil gas goes the rear portion separation system, reclaimable catalyst enters revivifier through transfer lime, with contain oxygen and burn medium and contact, it is characterized in that with through the coal of fine-powdered by transport medium at least one position in the revivifier, with the oxygen-containing medium catalytic combustion.
2, according to the method for claim 1, it is characterized in that the coal microsphere diameter of described fine-powdered is distributed as 5-500 μ m, mean diameter is 30-200 μ m.
3, according to the method for claim 1 or 2, it is characterized in that the coal microsphere diameter of described fine-powdered is distributed as 20-300 μ m, mean diameter is 40-100 μ m.
4,, it is characterized in that the coal microballoon of described fine-powdered is transported at least one position in the revivifier according to the method for claim 1.
5,, it is characterized in that the coal microballoon of described fine-powdered is transported to 2-4 position in the revivifier according to the method for claim 1 or 4.
6,, it is characterized in that the coal microballoon entry site of described fine-powdered can be installed coal microballoon sparger according to the method for claim 1.
7, according to the method for claim 1, it is characterized in that the coal microballoon of described fine-powdered is transported in the revivifier, can mix with reclaimable catalyst earlier, enter revivifier then jointly, also can enter revivifier separately.
8, according to the method for claim 1, the coal microballoon delivery medium that it is characterized in that described fine-powdered is oxygen-containing medium or oxygen-free medium.
9, according to the method for claim 8, it is characterized in that described oxygen-containing medium is an air or oxygen, described oxygen-free medium is a nitrogen.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200610076192XA CN101063041B (en) | 2006-04-28 | 2006-04-28 | Method for regulating heat balance |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200610076192XA CN101063041B (en) | 2006-04-28 | 2006-04-28 | Method for regulating heat balance |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101063041A true CN101063041A (en) | 2007-10-31 |
| CN101063041B CN101063041B (en) | 2011-04-20 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN200610076192XA Active CN101063041B (en) | 2006-04-28 | 2006-04-28 | Method for regulating heat balance |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023098879A1 (en) * | 2021-12-03 | 2023-06-08 | 中国石油化工股份有限公司 | Fluid catalytic cracking regeneration apparatus, and use thereof |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4708785A (en) * | 1979-11-14 | 1987-11-24 | Ashland Oil, Inc. | Carbo-metallic oil conversion |
| CN1151232C (en) * | 2000-09-28 | 2004-05-26 | 中国石油化工股份有限公司 | Method for regulating heat balance of catalytic conversion technological reaction-regeneration system |
| CN1318548C (en) * | 2002-05-28 | 2007-05-30 | 印度石油有限公司 | Raffinate oil cracking device with catalyst and adsorhent reactivator and its technology |
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2006
- 2006-04-28 CN CN200610076192XA patent/CN101063041B/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023098879A1 (en) * | 2021-12-03 | 2023-06-08 | 中国石油化工股份有限公司 | Fluid catalytic cracking regeneration apparatus, and use thereof |
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| CN101063041B (en) | 2011-04-20 |
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