CN102051198B - Catalytic conversion method and device for single-riser petroleum hydrocarbon type raw material - Google Patents
Catalytic conversion method and device for single-riser petroleum hydrocarbon type raw material Download PDFInfo
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- CN102051198B CN102051198B CN200910066363.4A CN200910066363A CN102051198B CN 102051198 B CN102051198 B CN 102051198B CN 200910066363 A CN200910066363 A CN 200910066363A CN 102051198 B CN102051198 B CN 102051198B
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Abstract
The invention discloses a catalytic conversion method and a catalytic conversion device for a single-riser petroleum hydrocarbon type raw material. A catalyst which has a temperature lower than that of a regenerated catalyst is fed into a pre-rising section of a riser reactor and is conveyed into an oil-catalyst contact reaction section by pre-risen gas to be contacted with the raw material for catalytic conversion reaction; and a cooled regenerated catalyst or a reflowed spent catalyst is fed into the riser reactor from the space above a raw material nozzle to participate in the catalytic conversion reaction. By the method and the device, reaction dry gas can be reduced, product distribution can be improved, and the temperature or the catalyst-oil ratio of the riser oil-catalyst contact reaction section and a post-reaction section can be adjusted and controlled, so catalytic conversion has sufficient flexibility to adapt to change of quality of raw material oil or the requirement of a market on products.
Description
Technical field
The invention belongs to petrochemical technology field, be specifically related to a kind of single riser tube catalystic conversion method of petroleum hydrocarbon raw material and device.
Background technology
Fluidized catalytic conversion is the important secondary processing technique of petrochemical field, and existing petroleum hydrocarbon raw material fluidized catalytic conversion device mostly adopts riser reactor.
Riser reactor has advantages of the reactant flow of minimizing back-mixing, improves object product selectivity, but also exist shortcoming: exactly because approach " piston flow ", and catalyst inventory is few, having in the reaction process of temperature effective (neither endothermic nor exothermic), must cause the larger temperature difference, the control of impact to temperature of reaction, increases byproduct.
For improving the larger contradiction of the temperature difference in riser tube reaction process, outlet temperature of riser and the mixing temperature along each section of riser tube all should be able to independently regulate separately, and what early apply is temperature control technology (MTC) after mixing.After mixing, temperature control is to inject liquid phase stream by employing, as recycle stock circulates to realize in the downstream of fresh feed inlet zone, riser tube is just divided into Two Areas like this: upstream (below) has the advantages that mixing temperature is high, catchment reaction is carried out under more conventional and relatively mild condition, and now outlet temperature of riser is to be maintained by the hot regenerated catalyst internal circulating load of controlling by regeneration guiding valve.
Obviously at present another deficiency of technology be reaction by outlet temperature of riser control, the catalytic amount that participates in reaction determines by outlet temperature of riser, can not regulate, the agent-oil ratio of reaction can not regulate.
Another shortcoming of technology is at present: the agent-oil ratio of riser tube inner catalyst reserve and each reaction zone is basic identical, can not regulate change.
In the last few years, catalytic conversion technique has been obtained very much progress, 200510017986.4 disclose a kind of low-temperature high agent-oil ratio catalytic conversion reaction method and reactor, adopt catalyzer to reduce from the method refluxing the catalyst temperature contacting with reaction raw materials in reactor, suppress heat cracking reaction, improve product yield, 200610113673.3 disclose a kind of method for transformation of petroleum hydrocarbon, the regenerated catalyst of heat is through the cooling reactor bottom that turns back to, contact with the stock oil of preheating respectively in the first reaction zone, second reaction zone reaction, after reaction mixes, the reclaimable catalyst after gas solid separation is transported to after stripping that revivifier carries out recycling after coke burning regeneration or part directly enters device after the mixing of reactor bottom in thing, the method is by reducing finish Contact Temperature, improve the contact condition of stock oil and catalyzer, thereby improve the yield of object reactant, selectivity and the character of improving object product.
Research shows, riser tube different zones completes the condition that different reaction needed is different, and the temperature of the zone of action of catalyzer and reaction raw materials has material impact to reaction process; Increase catalysts beneficial to catalyzed conversion, with regard to whole reaction process, in the time that the overall activity of catalyzer and selectivity improve, katalysis strengthens, catalyzed reaction proportion increases, and thermal response is effectively controlled, and is favourable to improving product yield, reducing byproduct.How can both utilize the product selectivity of riser reactor, realize again the temperature control to reaction zone, be still and need the constantly problem of research of each scientific research institutions.
Summary of the invention
The object of the present invention is to provide a kind of single riser tube catalystic conversion method of petroleum hydrocarbon raw material and device, can be in reducing reaction dry gas, improving product distribution, realize adjusting and control to riser tube finish contact reacts section, rear conversion zone temperature or agent-oil ratio, make catalyzed conversion there is enough handinesies, to adapt to the variation to product demand of raw material oil quality or market.
The technical solution used in the present invention is as follows:
Single riser tube catalystic conversion method of petroleum hydrocarbon raw material, makes the catalyzer lower than regenerated catalyst temperature enter riser reactor pre lift zone, delivers into finish contact reacts section contact with raw material and carry out catalytic conversion reaction through pre-lift gas; Make to lower the temperature regenerated catalyst or backflow reclaimable catalyst enters riser reactor and participates in catalytic conversion reaction from feed nozzle top.
The catalyzer lower than regenerated catalyst temperature is mixture, cooling regenerated catalyst and the mixture of backflow reclaimable catalyst or the mixture of regenerated catalyst and backflow reclaimable catalyst of cooling regenerated catalyst, cooling regenerated catalyst and regenerated catalyst.
Adjust this position temperature or/and agent-oil ratio by regulating riser tube different sites different catalysts inlet amount.
Realize the device of single riser tube catalystic conversion method of petroleum hydrocarbon raw material, comprise and be divided into pre lift zone from bottom to top, the riser reactor of finish contact reacts section and rear conversion zone and catalyst regenerator, riser reactor outlet connects settling vessel, settling vessel bottom one side is communicated with regenerator bottoms by pipe connecting, after settling vessel bottom opposite side or riser reactor, between conversion zone and riser reactor pre lift zone, be communicated with by catalyzer return line, revivifier is communicated with riser reactor pre lift zone by a road standpipe, be communicated with riser reactor finish contact reacts section through cooling catalyst device by two road standpipes.
Realize the device of single riser tube catalystic conversion method of petroleum hydrocarbon raw material, comprise and be divided into pre lift zone from bottom to top, the riser reactor of finish contact reacts section and rear conversion zone and catalyst regenerator, riser reactor outlet connects settling vessel, settling vessel bottom one side is communicated with regenerator bottoms by pipe connecting, after settling vessel bottom opposite side or riser reactor, between conversion zone and riser reactor finish contact reacts section, be communicated with by catalyzer return line, revivifier is communicated with riser reactor pre lift zone by a road standpipe, be communicated with riser reactor pre lift zone through cooling catalyst device by two road standpipes.
Realize the device of single riser tube catalystic conversion method of petroleum hydrocarbon raw material, comprise the riser reactor and the catalyst regenerator that are divided into pre lift zone, finish contact reacts section and rear conversion zone from bottom to top, riser reactor outlet connects settling vessel, settling vessel bottom one side is communicated with regenerator bottoms by pipe connecting, after settling vessel bottom opposite side or riser reactor, between conversion zone and riser reactor finish contact reacts section, be communicated with by catalyzer return line, revivifier is communicated with riser reactor pre lift zone through cooling catalyst device by standpipe.
Adopt catalysis conversion method of the present invention, at least there is following useful result:
1, the present invention at pre lift zone by use lower the temperature mixture, cooling regenerated catalyst and the mixture of backflow reclaimable catalyst or the mixture of regenerated catalyst and backflow reclaimable catalyst of regenerated catalyst, cooling regenerated catalyst and regenerated catalyst, can be by the adjusting of low temperature catalyst internal circulating load be realized to the control to pre lift zone temperature.
2, the present invention introduces low temperature catalyst at reactor middle part, make the agent-oil ratio (C/O) in whole reaction process be divided into Liang Ge district, be the rear conversion zone of finish contact reacts section and dose oil ratio, thereby realize the control to total conversion reaction by the level of response that the adjusting of Dui Liang district catalyst recirculation amount can be controlled each district.
3, the present invention can realize the temperature control at least two regions in reactor, reactor outlet temperature no longer with conventional catalytic conversion reaction by controlling by the situation that maintains of hot regenerated catalyst internal circulating load of regeneration guiding valve, but regulated by the low temperature catalyst internal circulating load that control enters rear conversion zone, and finish contact reacts section temperature is regulated by the regenerated catalyst internal circulating load of controlling by standpipe section.Improve finish contact situation to reduce heat cracking reaction in finish contact reacts section, regulate temperature of reaction further to improve catalytic conversion reaction in rear conversion zone dose oil ratio, thereby realize the control to whole catalyzed reaction; Reduce to greatest extent the dry gas yied in whole reaction process, liquid is received to be increased, and economy improves greatly.
4, the present invention can realize reactor pre lift zone, finish contact reacts section on the whole, rear conversion zone is trizonal controls simultaneously, by catalyst temperature, activity to participation catalytic conversion reaction and the flexible that enters reactor different positions, can meet the different needs of industrial application, as: for meeting both at home and abroad growing to oil liquefied gas and low-carbon alkene (take propylene as main) demand, after can adopting regenerated catalyst to mix with reclaimable catalyst, enter with stock oil and contact by reactor bottom, catalyzed conversion under comparatively high temps, high reactivity; If productive aromatic hydrocarbon, can adopt reactor middle part hole enlargement is that aromatization section, reclaimable catalyst pass back into feed nozzle top, aromatization section agent-oil ratio 3-20 etc., and those skilled in the art can adjust as the case may be.
Accompanying drawing explanation
Fig. 1 is the embodiment of the present invention 1 structural representation;
Fig. 2 is along riser reactor catalyst recirculation amount distribution schematic diagram from bottom to top in the embodiment of the present invention 1;
Fig. 3 is the embodiment of the present invention 2 structural representations;
Fig. 4 is the embodiment of the present invention 3 structural representations;
Fig. 5 is along riser reactor catalyst recirculation amount distribution schematic diagram from bottom to top in the embodiment of the present invention 3.
Number description: 1 riser reactor; 2 settling vessels; 3 stripping stages; 4 revivifiers; 5 feed nozzles; 6 regeneration standpipes; 7,7 ' standpipe; 8 catalyzer return lines; 9 cooling catalyst devices; I standpipe section; II pre lift zone; III finish contact reacts section; Conversion zone after IV; H riser tube height; C catalyst recirculation amount.
Embodiment
Describe technical scheme of the present invention in detail below in conjunction with accompanying drawing, protection scope of the present invention includes but not limited to this:
Embodiment 1: see Fig. 1.Reflux through catalyzer return line 8 from the reclaimable catalyst of stripping stage 3 with a part of hot regenerated catalyst by standpipe 7 ' enter after riser reactor 1 bottom pre lift zone II mixes, upwards contact participation catalyzed reaction with the atomized feed oil entering through feed nozzle 5; Reaction mixture upwards contacts and proceeds reaction through the lower the temperature cooling regenerated catalyst that forms of cooling catalyst device 9 with the another part being entered by standpipe 7; Reactant flow separates in settling vessel 2, and reclaimable catalyst is at stripping stage 3 strippings, and a part enters the pre lift zone II of reactor 1 bottom through return line 8, and another part enters revivifier 4 through regeneration standpipe 6 and regenerates.
In the present embodiment, along riser reactor from bottom to top catalyst recirculation amount distribute as shown in Figure 2, the catalyst recirculation amount that the introducing of backflow catalyzer makes pre lift zone II has significantly and increases than the catalyst recirculation amount of standpipe section I; The catalyzer of abundant mixed pre lift zone II upwards enters finish contact segment III, contacts vaporization, the conversion reaction of carrying out raw material with raw material, and this reacting section catalyst internal circulating load remains unchanged; Reactant flow upwards enters rear conversion zone IV, introduces the outlet temperature of riser that cooling regenerated catalyst has not only improved the agent-oil ratio of rear conversion zone but also can maintain hope, makes the reaction of whole riser reaction zone all in adjustable horizontal.
Embodiment 2: see Fig. 3.The a part of hot regenerated catalyst being entered by standpipe 7 forms cooling regenerated catalyst through cooling catalyst device 9, after the pre lift zone II of riser reactor 1 bottom mixes, upwards contact participation catalyzed reaction with the atomized feed oil entering through feed nozzle 5 with another part hot regenerated catalyst by standpipe 7 ' enter; Reaction mixture upwards with reflux through catalyzer return line 8 from after the reclaimable catalyst of conversion zone III contact and proceed reaction; Reactant flow is up along rear conversion zone III, a part of reclaimable catalyst through return line 8 reflux enter after conversion zone participate in reaction, remaining reaction mixture upwards enters in settling vessel 2, stripping stage 3 through separating, after stripping, enter revivifier 4 regenerate through regeneration standpipe 6.
Embodiment 3: see Fig. 4.What entered by standpipe 7 enters riser reactor 1 bottom through the cooling catalyst device 9 cooling regenerated catalyst forming of lowering the temperature, and upwards contact participation catalyzed reaction with the atomized feed oil entering through feed nozzle 5; Reaction mixture upwards contacts with the reclaimable catalyst from stripping stage 3 refluxing through catalyzer return line 8 proceeds reaction; Reactant flow separates in settling vessel 2, and reclaimable catalyst is at stripping stage 3 strippings, part conversion zone after return line 8 enters riser reactor 1, and another part enters revivifier 4 through regeneration standpipe 6 and regenerates.
In the present embodiment, along riser reactor from bottom to top catalyst recirculation amount distribute as shown in Figure 5, the cooling regenerated catalyst of pre lift zone II upwards enters finish contact segment III, contacts vaporization, the conversion reaction of carrying out raw material with raw material, and this reacting section catalyst internal circulating load remains unchanged; Reactant flow upwards enters rear conversion zone IV, introduces backflow reclaimable catalyst and improved the agent-oil ratio of rear conversion zone, makes the reaction of conversion zone after riser reactor in adjustable horizontal.
Claims (3)
1. realize the device of single riser tube catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described single riser tube catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter riser reactor pre lift zone, deliver into finish contact reacts section through pre-lift gas and contact with raw material and carry out catalytic conversion reaction; Make to lower the temperature regenerated catalyst or backflow reclaimable catalyst enters riser reactor and participates in catalytic conversion reaction from feed nozzle top;
Catalytic convention design comprises and is divided into pre lift zone from bottom to top, the riser reactor of finish contact reacts section and rear conversion zone and catalyst regenerator, riser reactor outlet connects settling vessel, settling vessel bottom one side is communicated with regenerator bottoms by pipe connecting, after settling vessel bottom opposite side or riser reactor, between conversion zone and riser reactor pre lift zone, be communicated with by catalyzer return line, revivifier is communicated with riser reactor pre lift zone by a road standpipe, be communicated with riser reactor finish contact reacts section through cooling catalyst device by two road standpipes.
2. realize the device of single riser tube catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described single riser tube catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter riser reactor pre lift zone, deliver into finish contact reacts section through pre-lift gas and contact with raw material and carry out catalytic conversion reaction; Make to lower the temperature regenerated catalyst or backflow reclaimable catalyst enters riser reactor and participates in catalytic conversion reaction from feed nozzle top;
Catalytic convention design comprises and is divided into pre lift zone from bottom to top, the riser reactor of finish contact reacts section and rear conversion zone and catalyst regenerator, riser reactor outlet connects settling vessel, settling vessel bottom one side is communicated with regenerator bottoms by pipe connecting, after settling vessel bottom opposite side or riser reactor, between conversion zone and riser reactor finish contact reacts section, be communicated with by catalyzer return line, revivifier is communicated with riser reactor pre lift zone by a road standpipe, be communicated with riser reactor pre lift zone through cooling catalyst device by two road standpipes.
3. realize the device of single riser tube catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described single riser tube catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter riser reactor pre lift zone, deliver into finish contact reacts section through pre-lift gas and contact with raw material and carry out catalytic conversion reaction; Make to lower the temperature regenerated catalyst or backflow reclaimable catalyst enters riser reactor and participates in catalytic conversion reaction from feed nozzle top;
Catalytic convention design comprises the riser reactor and the catalyst regenerator that are divided into pre lift zone, finish contact reacts section and rear conversion zone from bottom to top, riser reactor outlet connects settling vessel, settling vessel bottom one side is communicated with regenerator bottoms by pipe connecting, after settling vessel bottom opposite side or riser reactor, between conversion zone and riser reactor finish contact reacts section, be communicated with by catalyzer return line, revivifier is communicated with riser reactor pre lift zone through cooling catalyst device by standpipe.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1473909A (en) * | 2003-06-19 | 2004-02-11 | 中国石油化工集团公司 | Light olefine catalytic concersion method |
| CN1928022A (en) * | 2005-09-09 | 2007-03-14 | 洛阳石化设备研究所 | Low-temperature high agent-oil ratio catalytic conversion reaction method and reactor |
| CN101161786A (en) * | 2006-10-12 | 2008-04-16 | 中国石油化工股份有限公司 | Conversion method for petroleum hydrocarbons |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1473909A (en) * | 2003-06-19 | 2004-02-11 | 中国石油化工集团公司 | Light olefine catalytic concersion method |
| CN1928022A (en) * | 2005-09-09 | 2007-03-14 | 洛阳石化设备研究所 | Low-temperature high agent-oil ratio catalytic conversion reaction method and reactor |
| CN101161786A (en) * | 2006-10-12 | 2008-04-16 | 中国石油化工股份有限公司 | Conversion method for petroleum hydrocarbons |
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