CN102051210B - Dual-riser petroleum hydrocarbon feed stock catalytic conversion method and device - Google Patents
Dual-riser petroleum hydrocarbon feed stock catalytic conversion method and device Download PDFInfo
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- CN102051210B CN102051210B CN200910066364.9A CN200910066364A CN102051210B CN 102051210 B CN102051210 B CN 102051210B CN 200910066364 A CN200910066364 A CN 200910066364A CN 102051210 B CN102051210 B CN 102051210B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
- C10G11/187—Controlling or regulating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1809—Controlling processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
- C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
- C10G51/026—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only catalytic cracking steps
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
- C10G51/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a dual-riser petroleum hydrocarbon feed stock catalytic conversion method and dual-riser petroleum hydrocarbon feed stock catalytic conversion device. A reaction is performed in a heavy feed stock riser reactor and a light feed stock riser reactor. The method and the device are characterized in that: a catalyst of which the temperature is lower than that of a regenerated catalyst enters the heavy feed stock riser reactor pre-rising section, and is conveyed to an oil contact reaction section by pre-rising gas to contact a feed stock for a catalytic conversion reaction; and the temperature-reduced regenerated catalyst, a self refluxing spent catalyst or a relay catalyst from the rear reaction section of the light feed stock riser reactor enter the heavy feed stock riser reactor from the upside of a feed nozzle to participate in the catalytic conversion reaction. While dry reaction gas is reduced and the product distribution is improved, the catalyst/oil ratio and the reaction temperature of the contact reaction section and the rear reaction section of a riser are independently adjusted and controlled, so that the catalytic conversion is flexible enough to adapt to the feed stock quality and the change of product requirement of the market.
Description
Technical field
The present invention relates to petrochemical technology field, particularly relate to double lifting leg catalystic conversion method of petroleum hydrocarbon raw material and device.
Background technology
Catalyzed conversion is the important secondary processing means of oil heavy ends, existing petroleum hydrocarbon raw material catalytic convention design nearly all adopts riser reactor, and reaction raw materials catalyzed conversion in riser reactor forms the reactor products such as gasoline, diesel oil, liquefied petroleum gas (LPG).
Conventional catalysis conversion method and device are used riser reactor, its reaction process exists significantly not enough, first be that regenerated catalyst temperature is higher, reagent oil ratio and heavy oil preheating temperature have been limited, in existing catalytic conversion reaction process, reaction raw materials oil directly contacts with the high temperature catalyst of 700 ℃ of left and right, and excessive heat cracking reaction often occurs, stock oil is too much changes into the byproducts such as dry gas and coke, affects economic benefit; Next is that the latter half of efficiency of riser reactor is lower, and research shows, total conversion reaction of 80% completes in riser tube Lower Half, and major reason is at the latter half of catalyst deactivation of riser tube; The quality product of catalytic convention design is unsatisfactory in addition, and especially content of olefin in gasoline is higher, does not meet environmental requirement.
For can be when guaranteeing that feed vaporization transforms, heat cracking reaction when reducing as much as possible stock oil and contacting with catalyzer, CN99120517.0 discloses a kind of pipeline of heavy oil catalytic cracking regenerating agent cool-down method, be, on regenerator transfer line, heat exchange sleeve is installed, the regenerated catalyst after cooling enters riser reactor and stock oil contact reacts; US5,800,697 disclose a kind of catalytic conversion reaction-renovation process, on revivifier 12 sides, cooling catalyst district 72 is set, from the thermal regenerant of dense bed 66, from exporting 70, enters cooling area 72 heat exchange and to optimal temperature, by standpipe 24, guiding valve 26, enter riser reactor 16 bottoms and participate in reaction.In order to improve the reaction efficiency of heavy raw oil in riser reactor, there is the invention of the latter half of catalyst activity of multiple raising reactor, CN1302843A has proposed catalyzer relay scheme, at riser tube middle part, carrying out catalyzer transposition changes, the catalyzer reacting is all isolated, the low-temp recovery catalyzer of be replaced as high reactivity, processing through cooling, make the riser tube second half section return to the efficiency of first half section completely, although solved so previous problem, increased the feasibility of engineering construction.
For fear of various harmful and nonselective conversion reactions in riser reactor, outlet temperature of riser and all should be able to independently regulating separately along the mixing temperature of each section of riser tube, early application be 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 obviously now outlet temperature of riser is to be maintained by the hot regenerated catalyst internal circulating load of controlling by regeneration guiding valve.
The catalytic conversion reaction of petroleum hydrocarbon is a complicated systems engineering, the composition of reaction product and raw material concentration, the temperature of reaction in differential responses district, reaction times, the catalyst recirculation amount in reactor is closely bound up, GPRS the regulation rule of a certain or certain several variable wherein, just may become the huge advance made in theory and practice.Existing theoretical investigation and practice confirm, reduce the catalyst temperature contacting with stock oil, can effectively reduce heat cracking reaction degree; In addition with regard to whole reaction process, when the overall activity of catalyzer and selectivity improve, katalysis strengthens, and catalyzed reaction proportion increases, and thermal response is effectively controlled, to improving product yield, reduce dry gas and coke yield is favourable; If can be simultaneously regulate temperature of reaction or the agent-oil ratio of finish contact segment and rear conversion zone in riser reactor from macroscopic view, just may control whole catalytic conversion reaction process and carry out towards target product direction, reduce to greatest extent the generation of by product.
Summary of the invention
The object of the present invention is to provide a kind of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material and device, can be when reducing reaction dry gas, improving product distribution, realization regulates and controls the independent of riser tube contact reacts section, rear conversion zone agent-oil ratio or temperature of reaction, 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:
Double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, reaction is carried out in heavy feed stock riser reactor and lightweight material riser reactor, make the catalyzer lower than regenerated catalyst temperature enter heavy feed stock riser reactor pre lift zone, through pre-lift gas, deliver into finish contact reacts section and contact with raw material and carry out catalytic conversion reaction; Regenerated catalyst, self backflow reclaimable catalyst or from the relay catalyzer of conversion zone after lightweight material riser reactor, from feed nozzle top, enter heavy feed stock riser reactor and participate in catalytic conversion reaction make to lower the temperature.
The catalyzer lower than regenerated catalyst temperature is cooling regenerated catalyst, cooling regenerated catalyst and regenerated catalyst or self backflow reclaimable catalyst or from the mixture of the relay catalyzer of conversion zone after lightweight material riser reactor, or regenerated catalyst and self backflow reclaimable catalyst or from the mixture of the relay catalyzer of conversion zone after lightweight material riser reactor.
From the catalyst member of conversion zone after lightweight material riser reactor, being back to id reaction device pre lift zone mixes with regenerated catalyst.
By regulating heavy feed stock riser reactor different sites different catalysts inlet amount, adjust this position temperature or/and agent-oil ratio.
Realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, comprise and be divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is by two road standpipes, one road standpipe is communicated with heavy feed stock riser reactor and lightweight material riser reactor pre lift zone respectively, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor pre lift zone, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor finish contact reacts section, by catalyzer relay pipe, be communicated with.
Realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, comprise and be divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor pre lift zone, settling vessel bottom is communicated with heavy feed stock riser reactor pre lift zone by autocatalysis agent return line, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor finish contact reacts section, by catalyzer relay pipe, be communicated with, after lightweight material riser reactor, between conversion zone and self pre lift zone, by catalyzer return line, be communicated with.
Realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, comprise and be divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor pre lift zone, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor finish contact reacts section, by catalyzer relay pipe, be communicated with, after lightweight material riser reactor, between conversion zone and self pre lift zone, by catalyzer return line, be communicated with.
Realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, comprise and be divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, the pipe connecting of leading up to bottom settling vessel is communicated with regenerator bottoms, the autocatalysis agent return line of separately leading up to is communicated with heavy feed stock riser reactor finish contact reacts section, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor pre lift zone, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor pre lift zone, by catalyzer relay pipe, be communicated with.
Realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, comprise and be divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, the pipe connecting of leading up to bottom settling vessel is communicated with regenerator bottoms, the autocatalysis agent return line of separately leading up to is communicated with heavy feed stock riser reactor finish contact reacts section, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by two road standpipes, be communicated with heavy feed stock riser reactor pre lift zone, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor pre lift zone, by catalyzer relay pipe, be communicated with.
Realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, comprise and be divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by two road standpipes, be communicated with heavy feed stock riser reactor pre lift zone, after heavy feed stock riser reactor, between conversion zone and self pre lift zone, by catalyzer return line, be communicated with, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor finish contact reacts section, by catalyzer relay pipe, be communicated with, after lightweight material riser reactor, between conversion zone and self pre lift zone, by catalyzer return line, be communicated with.
Realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, comprise and be divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is by two road standpipes, one road standpipe is communicated with heavy feed stock riser reactor and lightweight material riser reactor pre lift zone respectively, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor finish contact reacts section, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor pre lift zone, by relay catalyst tube, be communicated with.
Adopt catalysis conversion method of the present invention, at least there is following useful result:
1, the present invention introduces low temperature catalyst at heavy feed stock riser 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;
2, the present invention has realized the temperature at least two regions in heavy feed stock riser reactor has been controlled, 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.In finish contact reacts section, improve finish contact situation to reduce heat cracking reaction, in rear conversion zone dose oil ratio, regulate temperature of reaction further to improve catalytic conversion reaction, thereby realize the control to whole catalyzed reaction;
3, the present invention is when carrying out effectively adjusting control to heavy feed stock riser reactor finish contact reacts section, rear conversion zone, at pre lift zone regenerated catalyst, mix with low temperature catalyst with before raw material contact reacts, not only can realize the cooling to regenerated catalyst, and can pass through the adjusting of low temperature catalyst internal circulating load to realize the control to pre lift zone temperature, thereby realize on the whole reactor pre lift zone, finish contact reacts section, the trizonal control simultaneously of rear conversion zone.Specifically, by to participating in catalyst temperature, the activity of 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, by reactor bottom, enter with stock oil and contact, 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.
4, the present invention adopts regenerated catalyst is directly lowered the temperature or reduced with relay catalyst mix the catalyst temperature contacting with stock oil by regenerated catalyst and from reflux reclaimable catalyst mixing or regenerated catalyst, reduce to greatest extent the dry gas yied in whole reaction process, liquid is received to be increased, economy improves greatly, ethylene content in the gasoline products simultaneously generating declines, and has met environmental requirement.
Accompanying drawing explanation
Fig. 1 is the embodiment of the present invention 1 structural representation;
Fig. 2 is the embodiment of the present invention 1 along heavy feed stock riser reactor catalyst recirculation amount distribution schematic diagram from bottom to top;
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 the embodiment of the present invention 3 along heavy feed stock riser reactor catalyst recirculation amount distribution schematic diagram from bottom to top;
Fig. 6 is the embodiment of the present invention 4 structural representations;
Fig. 7 is the embodiment of the present invention 5 structural representations;
Fig. 8 is the embodiment of the present invention 6 structural representations;
Fig. 9 is the embodiment of the present invention 7 structural representations;
Number description: 1 heavy feed stock riser reactor; 2 settling vessels; 3 stripping stages; 4 revivifiers; 5,25 feed nozzles; 6 regeneration standpipes; 7,7a, 7b standpipe; 8,12 catalyzer return lines; 9 cooling catalyst devices; 10 catalyzer relay pipes; 11 lightweight material riser reactors; 13 pre-coolers; 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
Below in conjunction with accompanying drawing, describe technical scheme of the present invention in detail, protection scope of the present invention includes but not limited to this:
Embodiment 1: see Fig. 1.What by standpipe 7, entered lowers the temperature the cooling regenerated catalyst forming and a part of hot regenerated catalysts that entered by standpipe 7b after the pre lift zone II of heavy feed stock riser reactor 1 bottom mixes through cooling catalyst device 9, upwards contact with the atomization heavy feed stock entering through feed nozzle 5 and participate in catalyzed reaction, after reaction mixture upwards contact with the activated relay catalyzer from lightweight material riser reactor 11 through catalyzer relay pipe 10 and enters, conversion zone IV proceeds to react, and completes the catalyzed conversion of heavy feed stock; Part hot regenerated catalyst enters lightweight material riser reactor 11 bottoms by standpipe 7a, promoting under medium effect, upwards contact with the atomization lightweight material entering through feed nozzle 25 and participate in catalyzed reaction, reaction mixture upwards enters rear conversion zone, the still activated relay catalyzer that a part was reacted is entered in heavy feed stock riser reactor 1 by feed nozzle 5 tops through catalyzer relay pipe 10, remaining reaction logistics continues up along lightweight material riser reactor 11, completes the catalyzed conversion of lightweight material; The reactant flow that completes catalyzed conversion in two riser reactors enters shared settling vessel 2 and isolates catalyzer, after stripping stage 3 strippings, by regeneration standpipe 6, enters revivifier 4 regeneration.
In the present embodiment, along the catalyst recirculation amount distribution from bottom to top of heavy feed stock riser reactor as shown in Figure 2, the introducing of cooling regenerated catalyst makes the catalyst recirculation amount of pre lift zone II have significantly and increase 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 heavy feed stock, and this reacting section catalyst internal circulating load remains unchanged; Reactant flow upwards enters rear conversion zone IV, introducing relay catalyzer rear catalyst internal circulating load obviously increases, not only improved the agent-oil ratio of rear conversion zone but also can maintain the outlet temperature of riser of hope, made the reaction of whole riser reaction zone all in adjustable horizontal.
Embodiment 2: see Fig. 3.Self backflow reclaimable catalyst from catalyzer return line 8, after mixing in the pre lift zone II of heavy feed stock riser reactor 1 bottom with the cooling regenerated catalyst forming through 9 coolings of cooling catalyst device being entered by standpipe 7, upwards contact with the atomization heavy raw oil entering through feed nozzle 5 and participate in catalyzed reaction, reaction mixture upwards contacts at rear conversion zone IV and proceeds reaction with the activated relay catalyzer from lightweight material riser reactor 11 of being introduced by catalyzer relay pipe 10, completes the catalyzed conversion of heavy feed stock, part hot regenerated catalyst enters lightweight material riser reactor 11 bottoms by standpipe 7a, promoting under medium effect, reflux after self backflow reclaimable catalyst of coming mixes with the rear conversion zone of lightweight material riser reactor 11, upwards contact with the atomization lightweight material entering through feed nozzle 25 and participate in catalyzed reaction, reaction mixture upwards enters rear conversion zone, still an activated relay catalyzer part of reacting is entered in heavy feed stock riser reactor 1 by feed nozzle 5 tops through catalyzer relay pipe 10, a part is refluxed and is entered lightweight material riser reactor 11 bottoms by catalyzer return line 12, remaining reaction logistics continues up along lightweight material riser reactor 11, complete the catalyzed conversion of lightweight material, the reactant flow that completes catalyzed conversion in two riser reactors enters shared settling vessel 2 and isolates catalyzer, a reclaimable catalyst part after stripping stage 3 strippings is refluxed and is entered in heavy feed stock riser reactor 1 pre lift zone II by return line 8, and another part enters revivifier 4 regeneration by regeneration standpipe 6.
Embodiment 3: see Fig. 4.The cooling regenerated catalyst forming through 9 coolings of cooling catalyst device being entered by standpipe 7 enters in the pre lift zone II of heavy feed stock riser reactor 1 bottom, upwards contacts with the atomization heavy raw oil entering through feed nozzle 5 and participates in catalyzed reaction, reaction mixture upwards contact with the activated relay catalyzer from lightweight material riser reactor 11 through catalyzer relay pipe 10 after proceed to react in conversion zone IV, complete the catalyzed conversion of heavy feed stock, part hot regenerated catalyst enters lightweight material riser reactor 11 bottoms by standpipe 7a, promoting under medium effect, reflux after self backflow reclaimable catalyst of coming mixes with the rear conversion zone of lightweight material riser reactor 11, upwards contact with the atomization lightweight material entering through feed nozzle 25 and participate in catalyzed reaction, reaction mixture upwards enters rear conversion zone, still an activated relay catalyzer part of reacting is entered in heavy feed stock riser reactor 1 by feed nozzle 5 tops through catalyzer relay pipe 10, a part is refluxed and is entered lightweight material riser reactor 11 bottoms by catalyzer return line 12, remaining reaction logistics continues up along lightweight material riser reactor 11, complete the catalyzed conversion of lightweight material, the reactant flow that completes catalyzed conversion in two riser reactors enters shared settling vessel 2 and isolates catalyzer, after stripping stage 3 strippings, by regeneration standpipe 6, enters revivifier 4 regeneration.
In the present embodiment, along the catalyst recirculation amount distribution from bottom to top of heavy feed stock riser reactor as shown in Figure 5, the cooling regenerated catalyst of pre lift zone II upwards enters finish contact segment III, contact vaporization, the conversion reaction of carrying out raw material with raw material, this reacting section catalyst internal circulating load remains unchanged; Reactant flow upwards enters rear conversion zone IV, introduces the agent-oil ratio that relay reclaimable catalyst has improved rear conversion zone, makes the reaction of conversion zone after riser reactor in adjustable horizontal.
Embodiment 4: see Fig. 6.Through catalyzer relay pipe 10 from the activated relay catalyzer of lightweight material riser reactor 11, after mixing in the pre lift zone II of heavy feed stock riser reactor 1 bottom with the cooling regenerated catalyst forming through 9 coolings of cooling catalyst device being entered by standpipe 7, upwards contact with the atomization heavy raw oil entering through feed nozzle 5 and participate in catalyzed reaction, reaction mixture upwards contact and in rear conversion zone IV, proceeds to react with self backflow reclaimable catalyst from catalyzer return line 8, completes the catalyzed conversion of heavy feed stock; Part hot regenerated catalyst enters lightweight material riser reactor 11 bottoms by standpipe 7a, promoting under medium effect, upwards contact with the atomization lightweight material entering through feed nozzle 25 and participate in catalyzed reaction, reaction mixture upwards enters rear conversion zone, the still activated relay catalyzer that a part was reacted enters in heavy feed stock riser reactor 1 pre lift zone II through catalyzer relay pipe 10, remaining reaction logistics continues up along lightweight material riser reactor 11, completes the catalyzed conversion of lightweight material; The reactant flow that completes catalyzed conversion in two riser reactors enters shared settling vessel 2 and isolates catalyzer, a reclaimable catalyst part after stripping stage 3 strippings enters heavy feed stock riser reactor 1 through return line 8 by feed nozzle 5 tops, and another part enters revivifier 4 regeneration by regeneration standpipe 6.
Embodiment 5: see Fig. 7.After the activated relay catalyzer from lightweight material riser reactor 11 of catalyzer relay pipe 10 mixes in the pre lift zone II of heavy feed stock riser reactor 1 bottom with a part of hot regenerated catalyst being entered by standpipe 7, upwards contact with the atomization heavy raw oil entering through feed nozzle 5 and participate in catalyzed reaction, reaction mixture upwards contact and in rear conversion zone IV, proceeds to react with self backflow reclaimable catalyst from catalyzer return line 8, completes the catalyzed conversion of heavy feed stock; Part hot regenerated catalyst enters lightweight material riser reactor 11 bottoms by standpipe 7a, after pre-cooler 13 cooling precoolings, promoting under medium effect, upwards contact with the atomization lightweight material entering through feed nozzle 25 and participate in catalyzed reaction, reaction mixture upwards enters rear conversion zone, the still activated relay catalyzer that a part was reacted enters in heavy feed stock riser reactor 1 pre lift zone II through catalyzer relay pipe 10, remaining reaction logistics continues up along lightweight material riser reactor 11, completes the catalyzed conversion of lightweight material; The reactant flow that completes catalyzed conversion in two riser reactors enters shared settling vessel 2 and isolates catalyzer, a reclaimable catalyst part after stripping stage 3 strippings enters heavy feed stock riser reactor 1 through return line 8 by feed nozzle 5 tops, and another part enters revivifier 4 regeneration by regeneration standpipe 6.
Embodiment 6: see Fig. 8.By the rear conversion zone IV of heavy feed stock riser reactor 1, refluxed after self backflow reclaimable catalyst of coming mixes in the pre lift zone II of heavy feed stock riser reactor 1 bottom with a part of hot regenerated catalyst being entered by standpipe 7, upwards contact with the atomization heavy raw oil entering through feed nozzle 5 and participate in catalyzed reaction, reaction mixture upwards contact with the activated relay catalyzer from lightweight material riser reactor 11 through catalyzer relay pipe 10 after proceed to react in conversion zone IV, the still activated reclaimable catalyst that a part was reacted refluxes and enters in heavy feed stock riser reactor 1 pre lift zone II through catalyzer return line 8, remaining reaction logistics continues up along lightweight material riser reactor 11, complete the catalyzed conversion of heavy feed stock, part hot regenerated catalyst enters lightweight material riser reactor 11 bottoms by standpipe 7a, promoting under medium effect, reflux after self backflow reclaimable catalyst of coming mixes with the rear conversion zone of lightweight material riser reactor 11, upwards contact with the atomization lightweight material entering through feed nozzle 25 and participate in catalyzed reaction, reaction mixture upwards enters rear conversion zone, still an activated relay catalyzer part of reacting is entered in heavy feed stock riser reactor 1 by feed nozzle 5 tops through catalyzer relay pipe 10, a part is refluxed and is entered lightweight material riser reactor 11 bottoms by catalyzer return line 12, remaining reaction logistics continues up along lightweight material riser reactor 11, complete the catalyzed conversion of lightweight material, the reactant flow that completes catalyzed conversion in two riser reactors enters shared settling vessel 2 and isolates catalyzer, after stripping stage 3 strippings, by regeneration standpipe 6, enters revivifier 4 regeneration.
Embodiment 7: see Fig. 9.After the activated relay catalyzer from lightweight material riser reactor 11 of catalyzer relay pipe 10 mixes in the pre lift zone II of heavy feed stock riser reactor 1 bottom with a part of hot regenerated catalyst being entered by standpipe 7b, upwards contact with the atomization heavy raw oil entering through feed nozzle 5 and participate in catalyzed reaction, reaction mixture upwards contact with the cooling regenerated catalyst forming through 9 coolings of cooling catalyst device after proceed to react in conversion zone IV, complete the catalyzed conversion of heavy feed stock; Part hot regenerated catalyst enters lightweight material riser reactor 11 bottoms by standpipe 7a, promoting under medium effect, upwards contact with the atomization lightweight material entering through feed nozzle 25 and participate in catalyzed reaction, reaction mixture upwards enters rear conversion zone, the still activated relay catalyzer that a part was reacted enters in heavy feed stock riser reactor 1 pre lift zone II through catalyzer relay pipe 10, remaining reaction logistics continues up along lightweight material riser reactor 11, completes the catalyzed conversion of lightweight material; The reactant flow that completes catalyzed conversion in two riser reactors enters shared settling vessel 2 and isolates catalyzer, after stripping stage 3 strippings, by regeneration standpipe 6, enters revivifier 4 regeneration.
Claims (7)
1. realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described double lifting leg catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter heavy feed stock riser reactor pre lift zone, through pre-lift gas, deliver into finish contact reacts section and contact with raw material and carry out catalytic conversion reaction; Regenerated catalyst, self backflow reclaimable catalyst or from the relay catalyzer of conversion zone after lightweight material riser reactor, from feed nozzle top, enter heavy feed stock riser reactor and participate in catalytic conversion reaction make to lower the temperature;
Catalytic convention design comprises and is divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is by two road standpipes, one road standpipe is communicated with heavy feed stock riser reactor and lightweight material riser reactor pre lift zone respectively, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor pre lift zone, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor finish contact reacts section, by catalyzer relay pipe, be communicated with.
2. realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described double lifting leg catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter heavy feed stock riser reactor pre lift zone, through pre-lift gas, deliver into finish contact reacts section and contact with raw material and carry out catalytic conversion reaction; Regenerated catalyst, self backflow reclaimable catalyst or from the relay catalyzer of conversion zone after lightweight material riser reactor, from feed nozzle top, enter heavy feed stock riser reactor and participate in catalytic conversion reaction make to lower the temperature;
Catalytic convention design comprises and is divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor pre lift zone, settling vessel bottom is communicated with heavy feed stock riser reactor pre lift zone by autocatalysis agent return line, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor finish contact reacts section, by catalyzer relay pipe, be communicated with, after lightweight material riser reactor, between conversion zone and self pre lift zone, by catalyzer return line, be communicated with.
3. realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described double lifting leg catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter heavy feed stock riser reactor pre lift zone, through pre-lift gas, deliver into finish contact reacts section and contact with raw material and carry out catalytic conversion reaction; Regenerated catalyst, self backflow reclaimable catalyst or from the relay catalyzer of conversion zone after lightweight material riser reactor, from feed nozzle top, enter heavy feed stock riser reactor and participate in catalytic conversion reaction make to lower the temperature;
Catalytic convention design comprises and is divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor pre lift zone, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor finish contact reacts section, by catalyzer relay pipe, be communicated with, after lightweight material riser reactor, between conversion zone and self pre lift zone, by catalyzer return line, be communicated with.
4. realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described double lifting leg catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter heavy feed stock riser reactor pre lift zone, through pre-lift gas, deliver into finish contact reacts section and contact with raw material and carry out catalytic conversion reaction; Regenerated catalyst, self backflow reclaimable catalyst or from the relay catalyzer of conversion zone after lightweight material riser reactor, from feed nozzle top, enter heavy feed stock riser reactor and participate in catalytic conversion reaction make to lower the temperature;
Catalytic convention design comprises and is divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, the pipe connecting of leading up to bottom settling vessel is communicated with regenerator bottoms, the autocatalysis agent return line of separately leading up to is communicated with heavy feed stock riser reactor finish contact reacts section, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor pre lift zone, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor pre lift zone, by catalyzer relay pipe, be communicated with.
5. realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described double lifting leg catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter heavy feed stock riser reactor pre lift zone, through pre-lift gas, deliver into finish contact reacts section and contact with raw material and carry out catalytic conversion reaction; Regenerated catalyst, self backflow reclaimable catalyst or from the relay catalyzer of conversion zone after lightweight material riser reactor, from feed nozzle top, enter heavy feed stock riser reactor and participate in catalytic conversion reaction make to lower the temperature;
Catalytic convention design comprises and is divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, the pipe connecting of leading up to bottom settling vessel is communicated with regenerator bottoms, the autocatalysis agent return line of separately leading up to is communicated with heavy feed stock riser reactor finish contact reacts section, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by two road standpipes, be communicated with heavy feed stock riser reactor pre lift zone, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor pre lift zone, by catalyzer relay pipe, be communicated with.
6. realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described double lifting leg catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter heavy feed stock riser reactor pre lift zone, through pre-lift gas, deliver into finish contact reacts section and contact with raw material and carry out catalytic conversion reaction; Regenerated catalyst, self backflow reclaimable catalyst or from the relay catalyzer of conversion zone after lightweight material riser reactor, from feed nozzle top, enter heavy feed stock riser reactor and participate in catalytic conversion reaction make to lower the temperature;
Catalytic convention design comprises and is divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is communicated with lightweight material riser reactor pre lift zone by a road standpipe, by two road standpipes, be communicated with heavy feed stock riser reactor pre lift zone, after heavy feed stock riser reactor, between conversion zone and self pre lift zone, by catalyzer return line, be communicated with, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor finish contact reacts section, by catalyzer relay pipe, be communicated with, after lightweight material riser reactor, between conversion zone and self pre lift zone, by catalyzer return line, be communicated with.
7. realize the device of double lifting leg catalystic conversion method of petroleum hydrocarbon raw material, it is characterized in that: described double lifting leg catalystic conversion method of petroleum hydrocarbon raw material is: make the catalyzer lower than regenerated catalyst temperature enter heavy feed stock riser reactor pre lift zone, through pre-lift gas, deliver into finish contact reacts section and contact with raw material and carry out catalytic conversion reaction; Regenerated catalyst, self backflow reclaimable catalyst or from the relay catalyzer of conversion zone after lightweight material riser reactor, from feed nozzle top, enter heavy feed stock riser reactor and participate in catalytic conversion reaction make to lower the temperature;
Catalytic convention design comprises and is divided into pre lift zone from bottom to top, the heavy feed stock riser reactor of finish contact reacts section and rear conversion zone, lightweight material riser reactor, heavy feed stock riser reactor exit portion is provided with settling vessel, lightweight material riser reactor outlet pipe connects settling vessel, settling vessel bottom is communicated with regenerator bottoms by pipe connecting, revivifier is by two road standpipes, one road standpipe is communicated with heavy feed stock riser reactor and lightweight material riser reactor pre lift zone respectively, by three road standpipes, through cooling catalyst device, be communicated with heavy feed stock riser reactor finish contact reacts section, after lightweight material riser reactor, between conversion zone and heavy feed stock riser reactor pre lift zone, by relay catalyst tube, be communicated with.
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| CN200910066364.9A CN102051210B (en) | 2009-11-04 | 2009-11-04 | Dual-riser petroleum hydrocarbon feed stock catalytic conversion method and device |
| PCT/CN2010/078163 WO2011054265A1 (en) | 2009-11-04 | 2010-10-27 | Catalytic conversion process of petroleum hydrocarbon in double reactor and apparatus thereof |
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| CN200910066364.9A CN102051210B (en) | 2009-11-04 | 2009-11-04 | Dual-riser petroleum hydrocarbon feed stock catalytic conversion method and device |
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|---|---|---|---|---|
| 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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| CN1888025B (en) * | 2005-06-30 | 2010-04-21 | 洛阳石化设备研究所 | Catalytic conversion method and apparatus |
| CN100393848C (en) * | 2005-08-08 | 2008-06-11 | 洛阳石化设备研究所 | Catalytic cracking conversion method with relay use of catalyst curd its device |
| CN1861753A (en) * | 2005-10-12 | 2006-11-15 | 洛阳石化设备研究所 | Catalyzing transforming process and apparatus of using gasoline heavy oil coupling reactor |
| CN100387687C (en) * | 2006-09-06 | 2008-05-14 | 中国石油化工集团公司 | Lift leg catalytic cracking method and apparatus |
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| 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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