CN206014776U - Catalytic cracking unit - Google Patents
Catalytic cracking unit Download PDFInfo
- Publication number
- CN206014776U CN206014776U CN201620963163.4U CN201620963163U CN206014776U CN 206014776 U CN206014776 U CN 206014776U CN 201620963163 U CN201620963163 U CN 201620963163U CN 206014776 U CN206014776 U CN 206014776U
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- tubular reactor
- catalyst
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- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 45
- 239000003054 catalyst Substances 0.000 claims abstract description 138
- 239000007787 solid Substances 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 13
- 238000006243 chemical reaction Methods 0.000 claims description 52
- 239000000295 fuel oil Substances 0.000 claims description 48
- 239000003921 oil Substances 0.000 claims description 43
- 238000011084 recovery Methods 0.000 claims description 17
- 230000008929 regeneration Effects 0.000 claims description 11
- 238000011069 regeneration method Methods 0.000 claims description 11
- 238000006555 catalytic reaction Methods 0.000 claims description 2
- 239000003502 gasoline Substances 0.000 abstract description 23
- 238000005516 engineering process Methods 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 230000004048 modification Effects 0.000 abstract description 5
- 238000012986 modification Methods 0.000 abstract description 5
- 239000003208 petroleum Substances 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 26
- 238000000034 method Methods 0.000 description 16
- 239000000571 coke Substances 0.000 description 15
- 230000000694 effects Effects 0.000 description 13
- 238000004364 calculation method Methods 0.000 description 11
- 238000001816 cooling Methods 0.000 description 11
- 230000008569 process Effects 0.000 description 9
- 230000003197 catalytic effect Effects 0.000 description 8
- 238000005336 cracking Methods 0.000 description 8
- 229930195733 hydrocarbon Natural products 0.000 description 7
- 150000002430 hydrocarbons Chemical class 0.000 description 7
- 238000002156 mixing Methods 0.000 description 5
- 239000003082 abrasive agent Substances 0.000 description 4
- 239000002283 diesel fuel Substances 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 230000004044 response Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 230000002411 adverse Effects 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000004231 fluid catalytic cracking Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 238000006424 Flood reaction Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- -1 vapour Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model belongs to the catalytic cracking technology field of petroleum chemical industry, is related to a kind of catalytic cracking unit.The catalytic cracking unit that the utility model is provided, including reactor, regenerator and gas-solid separation equipment, reactor includes that the second tubular reactor for reacting the first tubular reactor and 5～10m that segment length is respectively 5～10m, regenerator include tubular type regenerator and turbulent bed regenerator；The entrance of tubular type regenerator is connected with gas-solid separation equipment, the outlet of tubular type regenerator is located at the dilute phase section of turbulent bed regenerator, the close phase section of turbulent bed regenerator is connected with the catalyst inlet of the first tubular reactor, the outlet of the first tubular reactor is connected with gas-solid separation equipment, and the second tubular reactor is connected with gas-solid separation equipment.The utility model can realize that RFCC " high agent-oil ratio, short oil agent time of contact " is operated, and reduce gasoline upgrading energy consumption, can be used for RFCC and gasoline catalyzing modification.
Description
Technical field
The utility model belongs to the catalytic cracking technology field of petroleum chemical industry, and in particular to a kind of catalytic cracking dress
Put.
Background technology
Catalytic cracking is a more important process in oil secondary operation.However, current petroleum chemical industry
The conventional fluid catalytic cracking unit generally existing for being used the shortcoming of following several respects：First, using turbulent bed regenerator
Or the regenerator that turbulent bed is combined with fast bed, coke burning degree is less.Limited by regeneration kinetics, regeneration temperature is higher, led
Cause the regenerated catalyst temperature for participating in reaction higher (typically at 700 DEG C or so)；Due to the thermally equilibrated restriction of device, carry heavy oil
The oil ratio of riser is relatively small, and typically total oil ratio is 5～8 (weights of the total oil ratio of riser for catalyst in riser
The ratio of the weight flow summation that amount internal circulating load is fed with each stock of riser) so that the heavy oil feed of Unit Weight is touched
Number of active center less, this inhibits catalytic cracking reaction to a great extent.Meanwhile, the Contact Temperature of finish in riser
Higher, promote heat cracking reaction to a certain extent.Second, riser reactor length longer (generally more than 30m), finish
The time of contact is longer (typically in 4s or so, s is the second), and this also exacerbates cracking product while feedstock conversion is improved
Secondary response；Show as that cracked gas (including dry gas and liquefied gas) is higher with the yield of coke, vapour, diesel oil distillate yield compared with
Low；The inferior quality of catalytic diesel oil is also made, vehicle fuel blending component is not suitable as.3rd, using single conventional lifting
Pipe reactor, lacks the measure modified by gasoline catalyzing, and content of olefin in gasoline is high, quality is relatively low.For many years, domestic and international research aircraft
Structure has done substantial amounts of research work in terms of the shortcoming existing for above-mentioned conventional fluid catalytic cracking unit is overcome.
A kind of catalyst cracking method and device disclosed in Chinese patent CN100338185C, the technical characteristics of its device
It is：Using two riser reactors, one of them oil riser reactor of attaching most importance to, another are lighter hydrocarbons riser reactor；
Catalyst blending tank or heavy oil riser that lighter hydrocarbons riser reactor inclined tube to be generated is arranged with heavy oil riser reactor bottom
Reclaimable catalyst delivery pipe is provided between reactor regenerator sloped tube.Due to features above, the device can be catalyzed using double lifting leg
The technical advantage of cracking unit, by higher for part or all of residual activity (being approximately equivalent to the 90% of regenerated catalyst activity), temperature
Spend relatively low (500 DEG C or so) and mix with regenerated catalyst and exchange heat through steam stripped lighter hydrocarbons riser reactor reclaimable catalyst
Introduce heavy oil riser reactor afterwards and participate in residual oil cracking reaction.It is achieved that heavy oil riser reactor " finish low temperature connects
Tactile, high agent-oil ratio " operation, reduces dry gas, coke yield to a certain extent, improves total liquid yield.The technology is not
Foot part is：First, lighter hydrocarbons reclaimable catalyst is mixed with regenerated catalyst, reduces heavy oil riser to a certain extent anti-
Answer the activity of the catalyst that reaction is participated in device, adverse effect is brought to product slates and product property.Second, lighter hydrocarbons are to be generated to urge
The internal circulating load of agent is limited, is restricted the increase rate of heavy oil reaction oil ratio.3rd, it is catalyzed using traditional riser
Cracker, nozzle set location are relatively low, and finish time of contact of heavy oil riser reactor can only actually be controlled to 2～
4s, the reaction time for being shorter than 2s are difficult to realize.As finish time of contact is longer, cause the product point of heavy oil riser reactor
The property of cloth and catalytic diesel oil is relatively poor.4th, the upgrading processes of catalytic gasoline experienced the reaction of heavy oil riser reactor
The fractionation operation of oil gas, the again condensation of gasoline and gasification produce substantial amounts of Low Temperature Thermal, and energy consumption is higher.
A kind of apparatus and method for reducing temperature of catalytic cracking regenerated catalyst disclosed in Chinese patent CN101575534B,
Its device is mainly technically characterized by：In the lower section of conventional turbulent bed regenerator, one regenerated catalyst cooler, regeneration are set
Catalyst cooler bottom is provided with main air distributor.Managed with two that inner-outer sleeve is put between regenerated catalyst cooler and regenerator
Road is connected, and inner tube is regenerated catalyst, and the annular space between outer tube and inner tube is that the main wind after heat exchange enters regeneration
The passage of device.The catalyst outlet of regenerated catalyst cooler is connected with the bottom of heavy oil riser reactor by pipeline.By
In features above, regenerated catalyst introducing regenerated catalyst cooler can be exchanged heat by the device with main wind；Added after heat exchange
Enter on the prevailing wind direction of heat in regenerator and participate in coke burning regeneration, while cooled regenerated catalyst enters heavy oil lifts tube reaction
Device participates in residual oil cracking reaction.It is achieved that heavy oil riser reactor " contact of finish low temperature, high agent-oil ratio " operation, one
Determine in degree, to reduce dry gas, coke yield, improve total liquid yield.The technology is disadvantageous in that：First, regeneration is urged
The barrel diameter of agent cooler is less, is therefore accomplished by limiting the main air quantity of the cooling being passed through by cooling main air distributor
System.Otherwise, the regenerated catalyst in a large amount of regenerated catalyst coolers after cooling is by main for heated cooling wind entrainment, through annular
Space is flowed upwardly in regenerator, forms catalyst interior circulation, affects device normal operating.It is restricted due to cooling down main air quantity,
Thus the cooling effect to high-temperature regenerated catalyst can be affected.Second, traditional riser catalytic cracking reactor is used,
Heavy oil reaction shorter finish time of contact difficult to realize, reason is similar to the explanation to CN100338185C with consequence.
Involved by a kind of catalytic cracking process disclosed in United States Patent (USP) US5,462,652, device is mainly technically characterized by：
A catalyst hooper is provided with the top of reacting-settler and by pipeline and the catalyst tank phase being arranged above reacting-settler
Even, catalyst tank is connected with the close phase section of regenerator and reacting-settler by different pipelines.In reacting-settler dilute phase section
Level is provided with a feed nozzle, feed on the reacting-settler wall corresponding to injection direction perforate and be connected with one external
Cyclone separator, external cyclone water-separator are connected with the close phase section of reacting-settler by dipleg.Due to features above, the device
The finish way of contact different from conventional lift pipe reactor can be adopted.Catalyst by catalyst hooper central opening in gravity
Flow downward under effect, the charging injection direction of nozzle is with catalyst flow direction into 90 degree of angles.Charging is contacted with catalyst
Carry catalyst afterwards high-speed motion to react in the horizontal direction, a part of catalyst granules and reacting-settler wall collision rift
Separate with reaction oil gas, another part catalyst granules is entered external cyclone water-separator together with reaction oil gas and carries out gas-solid point
From.Meanwhile, a part of reclaimable catalyst participates in residual oil cracking reaction after in catalyst tank mixing with regenerated catalyst and exchange heat.
Therefore, described device shortens the reaction time to a certain extent in operation, also achieves " contact of finish low temperature, big agent
Oil ratio " operation, is improved product slates.The technology is disadvantageous in that：First, reclaimable catalyst and regenerated catalyst
Mixing, reduces the activity of the catalyst for participating in reaction to a certain extent, brings unfavorable shadow to product slates and product property
Ring.Second, the activity of heavy oil reclaimable catalyst is very low, very big to participating in the activity influence of catalyst of heavy oil reaction, can only lack
Heavy oil reaction is taken part in, so that the increase rate of heavy oil reaction oil ratio is restricted.3rd, finish contact area
Space is relatively large, and the finish time of contact of heavy oil reaction is not yet controlled effectively completely, still suffers from a certain degree of two
Secondary response.4th, lack the measure modified by gasoline catalyzing, content of olefin in gasoline is high.
Can be seen that according to above-mentioned analysis sum it up, the problem that is primarily present of catalytic cracking unit of the prior art
It is, for the measure for reducing regenerated catalyst temperature and improve heavy oil reaction oil ratio adjusts underaction (using main air cooling
The method of regenerated catalyst is made cooling effect be affected because the main air quantity of cooling is limited by device, by heavy oil catalysis to be generated
Agent participate in heavy oil reaction improve heavy oil reaction oil ratio method because heavy oil reclaimable catalyst activity very low, partially can only join
React with heavy oil and be restricted the increase rate of heavy oil reaction oil ratio, or by lighter hydrocarbons reclaimable catalyst or outside heat removing
Regenerated catalyst after device cooling participates in heavy oil catalytic cracking reaction and improves the method for heavy oil reaction oil ratio as two kinds are catalyzed
The internal circulating load of agent is limited and be restricted the increase rate of heavy oil reaction oil ratio)；Participate in urging for heavy oil catalytic cracking reaction
Agent activity relatively low (being mixed into and affected by heavy oil reclaimable catalyst or lighter hydrocarbons reclaimable catalyst), it is difficult to realize that shorter finish connects
The tactile time, lack the measure modified by gasoline catalyzing, the upgrading processes energy consumption of catalytic gasoline higher (due to the condensation in gasoline and
Substantial amounts of Low Temperature Thermal is generated in gasification again).Therefore, the above mentioned problem of solution of adopting an effective measure has weight
The meaning that wants.
Utility model content
In view of this, the purpose of this utility model is to provide a kind of catalytic cracking unit, compared with prior art, can
RFCC " high agent-oil ratio, short oil agent time of contact " operation is flexibly effectively realized, and optimizes gasoline catalyzing modification
Condition, while reduce the energy consumption of gasoline upgrading process.
For achieving the above object, the technical solution adopted in the utility model is：
A kind of catalytic cracking unit, including reactor, regenerator, gas-solid separation equipment and cooler, the reactor bag
The first tubular reactor and the second tubular reactor is included, the regenerator includes tubular type regenerator and turbulent bed regenerator；
First tubular reactor for conversion zone length be 5～10m downer reactor, second tubular type is anti-
Answer the riser reactor that the length that device is conversion zone is 5～10m；
Wherein, the entrance of the tubular type regenerator is connected by pipeline with gas-solid separation equipment, the outlet of tubular type regenerator
The dilute phase section of turbulent bed regenerator is located at, the bottom of tubular type regenerator is connected by pipeline with the close phase section of turbulent bed regenerator,
The close phase section of turbulent bed regenerator is connected by pipeline with the catalyst inlet of the first tubular reactor, the first tubular reactor
Outlet is connected with gas-solid separation equipment, and the close phase section of turbulent bed regenerator passes through cooler and pipeline and the second tubular reactor
Catalyst inlet is connected, and the outlet of the second tubular reactor is connected with gas-solid separation equipment.
In alternative of the present utility model, the gas-solid separation equipment includes settler and separator, the settler
Close phase section be stripping section, stripping section is connected by pipeline with separator；
The outlet of first tubular reactor is located at the dilute phase section of settler, the oil gas vent of settler and the second tubular type
The oil gas entrance of reactor is connected, and the outlet of the second tubular reactor is connected with the entrance of separator by closed conduct, stripping
The bottom of section is connected with the bottom of tubular type regenerator by pipeline.
In alternative of the present utility model, the catalyst inlet of first tubular reactor is located on the wall of top,
The outlet of the first tubular reactor is located at the top of the dilute phase section of settler, and exports downwards；Second tubular reactor
Oil gas entrance is located at bottom, and the catalyst inlet of the second tubular reactor is located on the wall of bottom；
The tubular type regenerator only has vertical pipeline section, and tubular type regenerator is coaxially disposed with turbulent bed regenerator, and tubular type is again
Raw device enters the dilute phase section of turbulent bed regenerator through the close phase section of turbulent bed regenerator, settler respectively with turbulent bed regenerator
It is set up in parallel with tubular type regenerator.
In alternative of the present utility model, also include that low-temp recovery catalyst tank, the cooler include that one-level is cooled down
Device and secondary coolers；
The entrance of the one-level cooler is connected by pipeline with the close phase section of turbulent bed regenerator, and one-level cooler is arranged
There are first outlet and second outlet, first outlet to be connected by pipeline with the close phase section of turbulent bed regenerator, second outlet and two
The entrance of level cooler is connected by pipeline, and the outlet of secondary coolers passes through pipeline phase with the entrance of low-temp recovery catalyst tank
Even, the catalyst outlet of low-temp recovery catalyst tank is connected by pipeline with the catalyst inlet of the second tubular reactor, low temperature
The gas vent of regenerated catalyst tank is connected by pipeline with the close phase section of turbulent bed regenerator.
In alternative of the present utility model, the close phase section of the turbulent bed regenerator is by pipeline and the stripping section
Top is connected.
In alternative of the present utility model, the separator be external cyclone separator, external cyclone separator
It is connected with the stripping section by external dipleg.
In alternative of the present utility model, first tubular reactor is provided with 1～3 layer of heavy oil along its axially spaced-apart
Feed nozzle.
In alternative of the present utility model, the exit of the tubular type regenerator is provided with inertia separator, and tubular type is again
The bottom of raw device is provided with distributor pipe of cardinal wind.
In alternative of the present utility model, the length of the tubular type regenerator is 30～50m, internal diameter is 1200～
8000mm；The close phase section internal diameter of the turbulent bed regenerator is 2000～12000mm, and the dilute phase section internal diameter of turbulent bed regenerator is
3400～22000mm.
In alternative of the present utility model, the total length of first tubular reactor is 7～13m, and the first tubular type is anti-
The internal diameter for answering device conversion zone is 400～2500mm；The total length of second tubular reactor be 7～13m, the second pipe reaction
The internal diameter of device conversion zone is 400～2500mm.
The catalytic cracking unit that the utility model is provided, can be used for RFCC and gasoline catalyzing modification.
Compared with prior art, the beneficial effects of the utility model are：
1st, in the utility model, regenerator is made up of tubular type regenerator and turbulent bed regenerator series combination, and turbulence
The close phase section of bed regenerator is connected by pipeline with the bottom of tubular type regenerator.In device operating process, reclaimable catalyst with
From the higher circular regeneration catalyst mixing of turbulent bed regenerator temperature, it is ensured that tubular type regenerator has higher entrance temperature
Degree, allows tubular type regenerator to reach higher coke burning degree, so that the synthesis of two regenerators of whole catalytic cracking unit
Coke burning degree is improved compared with conventional turbulent bed regeneration techniques the (difference of turbulent bed regenerator and tubular type regenerator：One
It is that the coke burning degree of turbulent bed regenerator is much smaller than tubular type regenerator, and two is turbulent bed regenerator in the range of 580～700 DEG C
Catalyst inventory is larger, thermal capacitance is also larger, not there are problems that coke is difficult to ignition.The catalyst inventory of tubular type regenerator compared with
Little, thermal capacitance is also less, and when catalyst inlet temperature is relatively low, coke is difficult to ignition and allows to ignition, and coke burning degree is relatively low).Cause
This can overcome reduces regeneration temperature to the adverse effect burnt, solves oil ratio all the time and greatly improves asking of being restricted
Topic (from the point of view of catalytic cracking unit thermal balance relation, makes the increase of catalyst internal circulating load directly can reduce by changing pressure balance
The temperature of regenerator catalyst bed, in the case where regeneration is constant, coke burning degree will decline to a great extent, and this is limit formulation oils
Principal element than greatly improving), so as to create condition for greatly improving oil ratio.
2nd, in the utility model, the length only 5～10m of the first tubular type reactor reaction section, and the first tubular reactor
Outlet be connected with settler, when heavy oil catalytic cracking reaction is carried out with the first tubular reactor, it is possible to achieve shorter oil
Agent time of contact (0.3～1.0s), so as to effectively suppress secondary response, make RFCC product slates and catalytic diesel oil
Property significantly improves.
3rd, in the utility model, the length of the second tubular type reactor reaction section is only 5～10m, the second tubular reactor
Outlet is connected with the entrance of cyclone separator by closed conduct, and gasoline catalyzing upgrading operation can realize shorter finish contact
Time (0.3～1.0s), so as to effectively suppress unnecessary side reaction during gasoline upgrading, reduce gasoline upgrading process as far as possible
Yield losses.
4th, in the utility model, cooler is regenerated catalyst cooler, and which is by one-level cooler and secondary coolers string
Joint group is into the oil gas entrance of the second tubular reactor is connected with the oil gas vent of settler, the catalyst of the second tubular reactor
Entrance is connected by regenerated catalyst and low-temp recovery catalyst tank with the catalyst outlet of secondary coolers, thus
Can by the reaction oil gas of the first tubular reactor, directly (without fractional distillation process) introduces the second tubular reactor, and through two-stage
(400～450 DEG C) of the low-temp recovery catalyst contact of cooling carry out the low finish Contact Temperature of gasoline, low reaction temperatures (430～
460 DEG C) catalytic reforming reaction.Under this temperature conditions, heavy oil and diesel component in one section of reaction oil gas are not substantially sent out
Raw reaction, so as to avoid gasoline condensation and again gasification, make the energy consumption of gasoline catalyzing upgrading processes decrease before
Put the independent modification that realizes to catalytic gasoline；Heat cracking reaction during also inhibits simultaneously, it is possible to decrease gasoline catalyzing changes
The dry gas of matter and coke yield, make that the property of catalytic gasoline is significantly improved and yield is higher.
For enabling above-mentioned purpose of the present utility model, feature and advantage to become apparent, preferred embodiment cited below particularly, and
Accompanying drawing appended by coordinating, is described in detail below.
Description of the drawings
In order to be illustrated more clearly that the utility model specific embodiment or technical scheme of the prior art, below will be right
Needed for specific embodiment or description of the prior art, accompanying drawing to be used is briefly described, it should be apparent that, describe below
In accompanying drawing be some embodiments of the present utility model, for those of ordinary skill in the art, do not paying creativeness
On the premise of work, can be with according to these other accompanying drawings of accompanying drawings acquisition.
The structural representation of the catalytic cracking unit that Fig. 1 is provided for the utility model.
Reference：
The first tubular reactors of 1-；The second tubular reactors of 2-；3- separators；
4- settlers；5- stripping sections；6- tubular type regenerators；7- turbulent bed regenerators；
8- one-level coolers；9- secondary coolers；10- low-temp recovery catalyst tanks；
11a, 11b- regenerator primary cyclone；12a, 12b- regenerator secondary cyclone；
13- flue gas collection chambers；The external diplegs of 14-；15- reclaimable catalyst delivery pipes；
16th, 17,18,19,20,21,22,23- regenerated catalysts；
24- air delivery pipes；25a, 25b- heavy oil feed nozzle；26- distribution of steam pipes；
27a, 27b- distributor pipe of cardinal wind；28- catalyst distribution plates；29- inertia separators；
30- reclaimable catalysts circulate control valve；31- regenerated catalysts circulate control valve.
Specific embodiment
Purpose, technical scheme and advantage for making the utility model embodiment is clearer, new below in conjunction with this practicality
Accompanying drawing in type embodiment, is clearly and completely described to the technical scheme in the utility model embodiment, it is clear that described
Embodiment be only a part of embodiment of the utility model, rather than whole embodiment.Generally described in accompanying drawing herein
Can arrange and design with a variety of configurations with the component of the utility model embodiment for illustrating.Therefore, below to
The detailed description of the embodiment of the present utility model provided in accompanying drawing is not intended to limit claimed model of the present utility model
Enclose, but be merely representative of selected embodiment of the present utility model.Embodiment of the present utility model is based on, those skilled in the art exist
The every other embodiment obtained on the premise of not making creative work, belongs to the scope of the utility model protection.
With reference to embodiment and specific embodiment, the utility model is described in more detail.
Embodiment
The structural representation of the catalytic cracking unit that Fig. 1 is provided for the utility model, as shown in figure 1, the one of the present embodiment
Catalytic cracking unit is planted, including reactor, regenerator and gas-solid separation equipment, wherein, reactor includes the first tubular reactor 1
With the second tubular reactor 2, regenerator includes tubular type regenerator 6 and turbulent bed regenerator 7, and gas-solid separation equipment includes settler
4 and separator 3, the close phase section of settler 4 is stripping section 5.Also include that regenerator cyclone separator, cooler and low-temp recovery are urged
Agent tank 10, cooler include one-level cooler 8 and secondary coolers 9；Regenerator cyclone separator includes two regenerators one
Level cyclone separator 11a, 11b, and two regenerators secondary cyclone 12a, 12b.
The exit of tubular type regenerator 6 is provided with inertia separator 29, the bottom of tubular type regenerator 6 is provided with main wind point
Stringing 27a, the close phase section bottom of turbulent bed regenerator 7 are provided with distributor pipe of cardinal wind 27b；The bottom of settler 4 is provided with steam point
Stringing 26.Catalyst distribution plate 28, the first tubular reactor 1 is provided with below the catalyst inlet of the first tubular reactor 1
Its axially spaced-apart is provided with 1～3 layer of heavy oil feed nozzle 25a, 25b.
Position annexation between the structure of each equipment and each equipment is as follows：
First tubular reactor 1 is downer reactor, and on the wall of top, outlet is located at sedimentation to its catalyst inlet
The top of the dilute phase section of device 4, and export downwards.Second tubular reactor 2 is the riser reactor with horizontal segment, its oil gas
Entrance is located at bottom, and catalyst inlet is located on the wall of bottom.
Tubular type regenerator 6 is coaxially disposed with turbulent bed regenerator 7, and settler 4 is respectively with turbulent bed regenerator 7 and tubular type again
Raw device 6 is set up in parallel, and separator 3 is located at the top of settler 4, and low-temp recovery catalyst tank 10 is located at the top of settler 4.One
Level cooler 8 and the catalyst cooler for being catalyst upper intake lower outlet type of secondary coolers 9, and one-level cooler 8 is located at
The top of secondary coolers 9.
First tubular reactor 1 is exported and is connected with the dilute phase section of settler 4, the oil gas vent of settler 4 and the second tubular type
The oil gas entrance of reactor 2 is connected, and the outlet of the second tubular reactor 2 is connected with the entrance of separator 3 by closed conduct.Vapour
Carry 5 bottom of section to be connected with the bottom inlet of tubular type regenerator 6 by reclaimable catalyst delivery pipe 15, separator 3 is revolved for external
Wind separator 3, the oil gas vent of external cyclone separator 3 are connected with fractionating column by reaction oil gas pipeline and (are not shown in figure
Go out), the catalyst outlet of external cyclone separator 3 is connected with the top of stripping section 5 by external dipleg 14.Tubular type regenerator
6 only have vertical pipeline section, the outlet of tubular type regenerator 6 to be located at the dilute phase section of turbulent bed regenerator 7, the close phase of turbulent bed regenerator 7
Section is respectively by regenerated catalyst 16 and the catalyst inlet of regenerated catalyst 17 and the first tubular reactor 1
It is connected with the entrance of one-level cooler 8, the first outlet of one-level cooler 8 passes through regenerated catalyst 21 with turbulent bed again
The close phase section of raw device 7 is connected, and second outlet is connected with the entrance of secondary coolers 9 by regenerated catalyst 18, two grades
The outlet of cooler 9 is connected with the entrance of low-temp recovery catalyst tank 10 by regenerated catalyst 19, and low-temp recovery is urged
The catalyst outlet of agent tank 10 is connected with the catalyst inlet of the second tubular reactor 2 by regenerated catalyst 20,
The gas vent of low-temp recovery catalyst tank 10 is connected with the close phase section of turbulent bed regenerator 7 by air delivery pipe 24.Turbulence
Bed regenerator 7 close phase section be connected with the top of stripping section 5 by regenerated catalyst 22, turbulent bed regenerator 7 close
Phase section is connected with the bottom of tubular type regenerator 6 by regenerated catalyst 23.
In the present embodiment, the main body of low-temp recovery catalyst tank 10 is cylindrical tube, and bottom and top are respectively equipped with envelope
Head.The side wall of cylindrical tube is provided with entrance, is respectively equipped with gas vent and catalyst goes out on top end socket and bottom end socket
Mouthful.
In the present embodiment, the first tubular reactor 1 enters settler 4, its outlet at bottom through the top end socket of settler 4
To lower open mouth.The top of the first tubular reactor 1 is provided with end socket, is provided with catalyst distribution plate 28, along which below catalyst inlet
Axially spaced-apart is provided with two-layer heavy oil feed nozzle 25a and 25b.Under normal circumstances, the first tubular reactor 1 can be along its axial direction
1～3 layer of heavy oil feed nozzle of interval setting.
In the present embodiment, the dilute phase section of turbulent bed regenerator 7 be provided with two regenerator primary cyclone 11a, 11b and
Two regenerators secondary cyclone 12a, 12b.Wherein, the entrance of regenerator primary cyclone 11a and turbulent bed be again
The dilute phase section of raw device 7 is communicated, and the outlet of regenerator primary cyclone 11b is by closed conduct and two grades of whirlwind of regenerator point
Entrance from device 12b is connected, and the outlet of regenerator secondary cyclone 12a is pushed up with turbulent bed regenerator 7 by closed conduct
The entrance of the flue gas collection chamber 13 in portion is connected, and the outlet of flue gas collection chamber 13 is by flue gas pipeline and smoke energy recovering system phase
Connect (not shown).The close phase section bottom of turbulent bed regenerator 7 is provided with distributor pipe of cardinal wind 27b, and bottom is provided with end socket.Generally,
The dilute phase section top of turbulent bed regenerator 7 can arrange two grades of 1～6 regenerator primary cyclone and 1～6 regenerator
Cyclone separator.
In the alternative of the present embodiment, the entrance of regenerated catalyst 16,17,22 and 23 is using flooding head piece shape
Formula, and stream bucket is flooded in setting.Reclaimable catalyst circulation control valve 30, regenerated catalyst is provided with reclaimable catalyst delivery pipe 15
Regenerated catalyst circulation control valve 31 is equipped with delivery pipe 16,17,18,19,20,21,22 and 23, to control to urge in each pipe
The internal circulating load of agent.And for avoiding catalyst from walking short circuit, the entrance of regenerated catalyst 17 is conveyed with regenerated catalyst
The distance between outlet of pipe 21 is not less than 3 meters.
In the alternative of the present embodiment, each equipment, the main body of pipeline are metal material (usually carbon steel or stainless
Steel), the surface contacted with catalyst can arrange high-abrasive material, the operation of the model of high-abrasive material and thickness according to each position
Temperature and linear gas velocity and chips washing system are determining.The internal diameter of equipment described in the utility model or pipeline each means interior straight
Footpath；For the equipment or pipeline that are provided with high-abrasive material, the interior diameter after installing high-abrasive material is each meant.
In the present embodiment, the total length of the first tubular reactor 1 is generally 7～13m, and the length of wherein conversion zone is (most adjacent
The distance between the jet of the heavy oil feed nozzle of nearly catalyst inlet and the outlet of the first tubular reactor 1) generally 5～
10m, pre- fluidisation section length (between the jet of the heavy oil feed nozzle of catalyst inlet and closest catalyst inlet away from
From) generally 2～3m, the internal diameter generally 400～2500mm of conversion zone, the internal diameter of pre- fluidisation section are generally 200～1300mm.
The total length of the second tubular reactor 2 is generally 7～13m, and wherein reaction segment length is generally 5～10m (catalyst
The distance between entrance and the outlet of most the second tubular reactor 2), conversion zone internal diameter is generally 400～2500mm.
The concrete length of 2 each several part of the first tubular reactor 1 and the second tubular reactor can be anti-according to two tubular types respectively
Design finish time of contact, the design linear speed of each several part of device, and the entirely parameter such as pressure balance of catalytic cracking unit is answered,
Determined using the design and calculation method of Conventional riser FCC riser.Two tubular reactors are each
Partial concrete internal diameter can respectively according to respective design treatment amount, amount of steam and two tubular reactor each several parts
The parameters such as design linear speed, the design and calculation method for using for reference Conventional riser FCC riser are determined.
In the alternative of the present embodiment, heavy oil feed nozzle 25a, 25b belong to existing conventional equipment, meet Conventional catalytic
The general features of cracked fuel oil feed nozzle 25a, 25b.Its concrete structure size and space layout can respectively according to first pipe
The operating conditions such as the physical dimension of formula reactor 1, design treatment amount and atomizing steam amount, using Conventional catalytic cracking heavy oil feed
The design and calculation method of nozzle 25a, 25b is determined.The concrete set location of each layer heavy oil feed nozzle can be according to various heavy
The parameters such as finish time of contact, the design linear speed of 1 conversion zone of the first tubular reactor required for oil charging carry out calculating determination.
The concrete material of heavy oil feed nozzle 25a, 25b can be determined according to the property and operating condition of each stock heavy oil feed respectively.
In the alternative of the present embodiment, reclaimable catalyst delivery pipe 15 and each regenerated catalyst 16,17,
18th, 19,20,21,22 and 23 meet the general features of catalyst transport pipeline.Its concrete structure and size can be each according to device
The space layout of the catalyst internal circulating load, mode of movement and device of catalyst recycle circuit, using catalyst transport pipeline
Design and calculation method is determined.The stream bucket that floods of regenerated catalyst porch setting belongs to existing conventional equipment.Its
Concrete structure size can be determined using the existing design and calculation method for flooding stream bucket according to the operating condition of device.
In the present embodiment, the length of tubular type regenerator 6 is generally 30～50m, and internal diameter is generally 1200～8000mm；Turbulence
The close phase section internal diameter of bed regenerator 7 is generally 2000～12000mm, and the dilute phase section internal diameter of turbulent bed regenerator 7 is generally 3400
～22000mm.
In the alternative of the present embodiment, the structurally and operationally mode of tubular type regenerator 6 and Conventional riser catalytic cracking
The turbulent bed regenerator 7 adopted by device compares that difference is larger, need pressure balance relation according to whole catalytic cracking unit,
The design linear speed at the design coke-burning capacity of tubular type regenerator 6 and coke burning degree and its each position, using dilute phase tubular type regenerator 6
Design and calculation method determines the concrete structure size at its each position.
In the alternative of the present embodiment, turbulent bed regenerator 7 meets what Conventional riser catalytic cracking unit was adopted
The general features of turbulent bed regenerator 7.Can be according to the design coke-burning capacity of turbulent bed regenerator 7 and coke burning degree and its each portion
The physical dimension of the design linear speed and regenerator primary cyclone and regenerator secondary cyclone of position and installation side
The Parameter Conditions such as formula, the tool that its each position is determined using the design and calculation method of existing catalytic cracking unit turbulent bed regenerator 7
Body physical dimension.
In the alternative of the present embodiment, the structurally and operationally mode of settler 4 and Conventional riser catalytic cracking unit
Institute has compared certain difference using settler 4, but conforms generally to the general spy of Conventional riser catalytic cracking unit settler 4
Levy.Its concrete structure size can be calculated using the design of existing catalytic cracking unit settler 4 according to the operating condition of device
Method is determined.
In the alternative of the present embodiment, one-level cooler 8 and secondary coolers 9 belong to existing conventional equipment.Which is concrete
Physical dimension can according to the operating condition of device, using existing catalytic cracking unit external warmer design and calculation method in addition
Determine.
In the alternative of the present embodiment, the height of the cylindrical tube of low-temp recovery catalyst tank 10 is generally 4～6m,
Internal diameter is generally 1～5m.Its concrete structure size can be de- using existing catalytic cracking catalyst according to the internal circulating load of catalyst
The design and calculation method of gas surge tank is determined.
In the alternative of the present embodiment, the inertia separator 29 for being arranged on 6 exit of tubular type regenerator often can be adopted
Umbrella crown type separator (as shown in Figure 1), inverted L shape separator, T-shaped separator, trilobal cross separator, ejection type separator
Deng.In concrete application, according to the design feature of tubular type regenerator 6 and to 6 exit gas-solid disngaging efficiency of tubular type regenerator
Requirement is selected.
In the alternative of the present embodiment, two grades of cyclonic separations of regenerator primary cyclone 11a, 11b and regenerator
Device 12a, 12b belong to existing conventional equipment.Its concrete structure size and space layout can be adopted according to the operating condition of device
Determined with the design and calculation method of existing cyclone separator.
In the alternative of the present embodiment, distribution of steam pipe 26 and distributor pipe of cardinal wind 27a, 27b can be distributed using dendriform
Pipe or annular spread pipe, belong to existing conventional equipment.Its concrete structure size and space layout can be according to the operations of device
Condition, is determined using the design and calculation method of existing distribution of steam pipe 26 and distributor pipe of cardinal wind 27a, 27b.
Finally it should be noted that：Embodiment described above, specific embodiment only of the present utility model, in order to illustrate this
The technical scheme of utility model, rather than a limitation, protection domain of the present utility model is not limited thereto, although with reference to aforementioned
Embodiment has been described in detail to the utility model, it will be understood by those within the art that：Any it is familiar with this skill
, in the technical scope that the utility model is disclosed, which still can be to the skill described in previous embodiment for the technical staff in art field
Art scheme is modified or can readily occur in change, or carries out equivalent to which part technical characteristic；And these modifications,
Change is replaced, and does not make the essence of appropriate technical solution depart from spirit and the model of the utility model embodiment technical scheme
Enclose.Should all cover within protection domain of the present utility model.Therefore, protection domain of the present utility model should be wanted with the right
The protection domain that asks is defined.
Claims (10)
1. a kind of catalytic cracking unit, it is characterised in that including reactor, regenerator, gas-solid separation equipment and cooler, described
Reactor includes that the first tubular reactor and the second tubular reactor, the regenerator include tubular type regenerator and turbulent bed regeneration
Device；
First tubular reactor for conversion zone length be 5～10m downer reactor, second tubular reactor
For conversion zone length be 5～10m riser reactor；
Wherein, the entrance of the tubular type regenerator is connected by pipeline with gas-solid separation equipment, and the outlet of tubular type regenerator is located at
The dilute phase section of turbulent bed regenerator, the bottom of tubular type regenerator are connected by pipeline with the close phase section of turbulent bed regenerator, turbulence
The close phase section of bed regenerator is connected by pipeline with the catalyst inlet of the first tubular reactor, the outlet of the first tubular reactor
It is connected with gas-solid separation equipment, the close phase section of turbulent bed regenerator passes through the catalysis of cooler and pipeline and the second tubular reactor
Agent entrance is connected, and the outlet of the second tubular reactor is connected with gas-solid separation equipment.
2. catalytic cracking unit according to claim 1, it is characterised in that the gas-solid separation equipment include settler and
Separator, the close phase section of the settler is stripping section, and stripping section is connected by pipeline with separator；
The outlet of first tubular reactor is located at the dilute phase section of settler, the oil gas vent of settler and the second pipe reaction
The oil gas entrance of device is connected, and the outlet of the second tubular reactor is connected with the entrance of separator by closed conduct, stripping section
Bottom is connected with the bottom of tubular type regenerator by pipeline.
3. catalytic cracking unit according to claim 2, it is characterised in that the catalyst of first tubular reactor enters
Mouth is located on the wall of top, and the outlet of the first tubular reactor is located at the top of the dilute phase section of settler, and exports downward；Described
The oil gas entrance of the second tubular reactor is located at bottom, and the catalyst inlet of the second tubular reactor is located on the wall of bottom；
The tubular type regenerator only has vertical pipeline section, and tubular type regenerator is coaxially disposed with turbulent bed regenerator, tubular type regenerator
Close phase section through turbulent bed regenerator enters the dilute phase section of turbulent bed regenerator, settler respectively with turbulent bed regenerator and pipe
Formula regenerator is set up in parallel.
4. the catalytic cracking unit according to Claims 2 or 3, it is characterised in that also include low-temp recovery catalyst tank, institute
Stating cooler includes one-level cooler and secondary coolers；
The entrance of the one-level cooler is connected by pipeline with the close phase section of turbulent bed regenerator, and one-level cooler is provided with
One outlet and second outlet, first outlet are connected by pipeline with the close phase section of turbulent bed regenerator, and second outlet is cold with two grades
But the entrance of device is connected by pipeline, and the outlet of secondary coolers is connected by pipeline with the entrance of low-temp recovery catalyst tank,
The catalyst outlet of low-temp recovery catalyst tank is connected by pipeline with the catalyst inlet of the second tubular reactor, low-temp recovery
The gas vent of catalyst tank is connected by pipeline with the close phase section of turbulent bed regenerator.
5. the catalytic cracking unit according to Claims 2 or 3, it is characterised in that the close phase section of the turbulent bed regenerator
It is connected with the top of the stripping section by pipeline.
6. the catalytic cracking unit according to Claims 2 or 3, it is characterised in that the separator is external whirlwind point
From device, external cyclone separator is connected with the stripping section by external dipleg.
7. catalytic cracking unit according to claim 1, it is characterised in that first tubular reactor is along between its axial direction
Every being provided with 1～3 layer of heavy oil feed nozzle.
8. catalytic cracking unit according to claim 1, it is characterised in that the exit of the tubular type regenerator is provided with
Inertia separator, the bottom of tubular type regenerator are provided with distributor pipe of cardinal wind.
9. catalytic cracking unit according to claim 1, it is characterised in that the length of the tubular type regenerator is 30～
50m, internal diameter are 1200～8000mm；The close phase section internal diameter of the turbulent bed regenerator be 2000～12000mm, turbulent bed regenerate
The dilute phase section internal diameter of device is 3400～22000mm.
10. catalytic cracking unit according to claim 1, it is characterised in that the total length of first tubular reactor
For 7～13m, the internal diameter of the first tubular type reactor reaction section is 400～2500mm；The total length of second tubular reactor is
7～13m, the internal diameter of the second tubular type reactor reaction section is 400～2500mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620963163.4U CN206014776U (en) | 2016-08-27 | 2016-08-27 | Catalytic cracking unit |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620963163.4U CN206014776U (en) | 2016-08-27 | 2016-08-27 | Catalytic cracking unit |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109609175A (en) * | 2019-01-30 | 2019-04-12 | 李群柱 | A kind of descending-bed reactor lighter hydrocarbons catalysis conversion method and its device |
| CN109609176A (en) * | 2019-01-30 | 2019-04-12 | 李群柱 | A kind of descending-bed reactor method for catalytic conversion of heavy oil and its device |
| CN109609174A (en) * | 2019-01-30 | 2019-04-12 | 李群柱 | A kind of descending-bed reactor hydrocarbons catalytic conversion method and its device |
-
2016
- 2016-08-27 CN CN201620963163.4U patent/CN206014776U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109609175A (en) * | 2019-01-30 | 2019-04-12 | 李群柱 | A kind of descending-bed reactor lighter hydrocarbons catalysis conversion method and its device |
| CN109609176A (en) * | 2019-01-30 | 2019-04-12 | 李群柱 | A kind of descending-bed reactor method for catalytic conversion of heavy oil and its device |
| CN109609174A (en) * | 2019-01-30 | 2019-04-12 | 李群柱 | A kind of descending-bed reactor hydrocarbons catalytic conversion method and its device |
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