CN1240671A - Absorption stabilizing apparatus for catalytic cracking and its production process - Google Patents
Absorption stabilizing apparatus for catalytic cracking and its production process Download PDFInfo
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- CN1240671A CN1240671A CN 99116296 CN99116296A CN1240671A CN 1240671 A CN1240671 A CN 1240671A CN 99116296 CN99116296 CN 99116296 CN 99116296 A CN99116296 A CN 99116296A CN 1240671 A CN1240671 A CN 1240671A
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Abstract
An absorption stabilizer for catalytic cracking is composed of complex distilling tower-oil-absorbing deethanization tower, reabsorbing tower, stabilizing tower and relative heat exchanger network. Its advantages are high recovery rate of product, low operation cost and reduced by-product.
Description
The present invention relates to petrochemical equipment and technology, specifically be meant absorption stabilizing apparatus for catalytic cracking and production technique thereof.
Catalytic cracking unit is one of main oil refining apparatus.It is with light materialization of heavy oil, produces the important device of liquefied gas, gasoline and diesel oil.According to statistics in 1998, existing more than 130 covers of national catalytic cracking unit, overall throughput reaches 7,200 ten thousand tons/year.And absorption stabilizing apparatus is the after-treatment system in the catalytic cracking unit, and the raw material raw gasline and the rich gas of its fractionation of autocatalysis in the future cat head are separated into product liquefied gas and stable gasoline, obtain the byproduct dry gas simultaneously.The product yield of absorption stabilizing apparatus and energy consumption have crucial influence to the economic benefit of whole catalytic cracking unit.
The absorption stabilizing apparatus of current dominate mainly is made up of absorption tower, desorption tower, reabsorber and stabilizer tower all the people present tower, and 50 to the sixties, and the flow process of absorption stabilizing apparatus is " single tower flow process ".So-called " single tower flow process " is meant that the absorption of carbon three, carbon fourth class component and the desorb of carbon two components carry out in same tower.According to reports, mainly there is following shortcoming in " single tower flow process ":
1, absorption and desorption process is carried out in same tower, and the phase mutual interference is bigger;
2, be difficult to the specific absorption and the desorption efficiency that reach higher;
3, the device regulating and controlling is difficult.
Entered since the seventies, the design of new factory all transfers to adopt " double-column process ", and " double-column process " then is the absorption and desorption process separately, carries out respectively in two independent towers.Existing old device also transform " double-column process " one after another as, and " double-column process " pattern has occupied dominant position fully in catalytic cracking unit so far, and estimating has the catalytic cracking unit more than 80% all to adopt " double-column process " at present approximately.
The shortcoming that " though double-column process " overcome to a certain extent above-mentioned " single tower flow process ", but the control problem that has specific absorption and desorption efficiency too, come absorption and desorption in two towers, to carry out respectively outwardly, operation control easily, yet all have material to be coupled to each other between these towers, the variation of any one tower operational condition all can have influence on other tower and total system.If only consider the optimum operation of indivedual towers separately, and ignore and other influence to overall economic benefit, tend to cause run counter to desire, overall benefit is descended." double-column process " another very important disadvantages be to absorb tower bottoms in the flow process and desorb column overhead gas phase all will turn back to flow process at the beginning, i.e. the inlet of water cooler before the surge tank.With certain large-scale 1,200,000 tons of/year catalytic cracking unit is example, the raw material of its absorption stabilizing apparatus be raw gasline and the compression rich gas, their flow be respectively 63 tons/time and 47 tons/time.And return flow that material absorbs tower bottoms and desorb column overhead gas phase reach respectively 136 tons/time and 16 tons/time.The raw material that enters system amount to 110 tons/time, and above-mentioned return the recycle stock flow add up to 152 tons/time.The recycle stock amount is unexpectedly greater than the material quantity that enters system, and a large amount of relevant equipment such as tower, interchanger, pump and containers or the like in the system will have to handle the nearly material about system feeding amount twice.This not only causes the increase of facility investment, and process cost is risen, and obviously is extremely irrational.Therefore the defective on this flow process is demanded urgently improving.
The objective of the invention is to overcome the shortcoming of present leading flow process " double-column process " and early stage " single tower flow process ", a kind of simple in structure, energy consumption is low, product recovery rate is high, economic benefit is big absorption stabilizing apparatus for catalytic cracking and production technique thereof are provided.
The objective of the invention is to realize by following measure:
Absorption stabilizing apparatus for catalytic cracking is by complicated distillation tower---and the pipeline that oil absorbs deethanizing column 1, reabsorber 2, stabilizer tower 3 and heat exchanger network, pump, container and is connected them is formed;
The top that oil absorbs deethanizing column 1 is provided with by condenser 4, return tank 5 and pump 6 and the condenser system that is in series by pipeline 19,21 successively, also is provided with the pipeline 20 that links to each other with reabsorber 2 bottom inlet on its return tank 5;
The upper rectifying section that oil absorbs deethanizing column 1 is provided with the component cooling system that is in series by pipeline 22, side cooler 7, pump 8 and pipeline 23 successively, such component cooling system can have one to two group, if there are two groups, then be located at the upper and lower different positions of rectifying section respectively.
The Lower Half stripping section that oil absorbs deethanizing column 1 is provided with the intermediate reboiler system that is in series by pipeline 24, intermediate reboiler 9 and pipeline 25 successively;
The bottom that oil absorbs deethanizing column 1 is provided with a tower still reboiler 10;
The still liquid of oil absorption deethanizing column 1 is sent to the inlet of stabilizer tower 3 by pipeline 26, stabilizer tower 3 cats head are provided with a circulating cooling system that is in series by pipeline 30, condenser 12, return tank 13, pipeline 31, pump 14 and pipeline 32 successively, and tower still reboiler is an equipment 15;
The hot side outlet pipeline of stable gasoline water cooler 11 is divided into two strands, one is linked to each other by the inlet of pipeline 37 with pump 16, link to each other the stable gasoline product output channel 39 of another strand for before pump 16 inlets, telling with the top that oil absorbs deethanizing column by pipeline 38 through this pump.
The annexation of heat exchanger network is: the hot side entrance that oil absorbs the tower still reboiler 10 of deethanizing column 1 links to each other with stable tower bottoms outlet by pipeline 34, the hot side outlet of tower still reboiler 10 links to each other by the hot side entrance of pipeline 35 and intermediate reboiler 9, and the hot side outlet of intermediate reboiler 9 links to each other by the hot side entrance of pipeline 36 and stable gasoline water cooler 11.
The production technique of this device is as follows: the material of motion device has three strands, and promptly 17 that enter by pipeline, temperature is 34-40 ℃ a raw gasline, and raw gasline directly enters the top that oil absorbs deethanizing column; , temperature 18 that enter by pipeline is 34-40 ℃ compression rich gas, and the compression rich gas is no longer as existing apparatus, and advanced water cooler and gas-liquid separator are divided into gaseous phase materials and liquid phase material then, but directly enters the middle part that oil absorbs deethanizing column; Also has the lean absorption oil that enters reabsorber by pipeline 28 in addition.The pressure that oil absorbs deethanizing column 1 is 1.0-1.45Mpa, and the phegma temperature is 34-42 ℃, by the adjustment of reflux ratio, can effectively control the quality of overhead product.The tower still reboiler that oil absorbs deethanizing column 1 is that the temperature by stabilizer tower is that 170-190 ℃ high-temperature kettle liquid heats, stable tower bottoms directly enters the tower still reboiler 10 that oil absorbs deethanizing column, after should stablize tower bottoms coming out from tower still reboiler 10, temperature is reduced to 100-110 ℃, be re-used as the thermal source of intermediate reboiler 9, after the intermediate reboiler heat exchange, the temperature of this still liquid is reduced to 80-95 ℃, enter the stable gasoline water cooler then, be as cold as about 40 ℃, after this be divided into two strands of materials, one is the stable gasoline product, another thigh is absorption agent as a supplement, sends the top that oil is inhaled deethanizing column back to.Oil absorbs the cat head gaseous products of deethanizing column, then enters reabsorber 2, obtains byproduct dry gas and recycle stock rich absorbent oil through separation; Oil absorbs the tower bottoms phase product of deethanizing column, then directly enters stabilizer tower 3, is divided into product liquefied gas and stable gasoline by this tower.
The present invention compared with prior art has following advantage and effect:
1, flow process is simple, efficient
Flowage structure of the present invention has simple, characteristics of high efficiency with existing leading flow process---" double-column process " compared.The first, it adopts the distillation tower of a novel texture---and oil absorbs deethanizing column and has replaced original absorption tower and desorption tower, makes the sum of tower in this device be kept to three from all the people present; The second, cancelled the feed preheater of desorption tower and stabilizer tower in the former flow process; The 3rd, cancelled and compressed rich gas in the former flow process and return material water cooler and gas-liquid separator; The 4th, because the change on the flowage structure, also reduced the heat interchanging area of some interchanger in the platform number of pump and the flow process.
2, save process cost
The present invention cancelled two plume amounts in the existing leading flow process very considerable return material, promptly absorb tower bottoms and desorb column overhead gas phase, bigger saving the water, electricity, gas consumption of device.
Table 1 has provided the material quantity of certain existing 1,200,000 tons of absorption stabilizing apparatus for catalytic cracking and has returned inventory.Therefrom can find out into the material quantity of this device be 110 tons/time, return inventory then up to 152 tons/time, it is big that its throughput ratio material quantity is also wanted.Thereby these two bursts of cancellations of returning material, undoubtedly with the process cost of significant economy system.
Table 1 " double-column process " material quantity and return inventory relatively
Unit: ton/time
| The device raw material | Return thing section | |||
| Material | The compression rich gas | Raw gasline | Absorb tower bottoms | Desorption tower cat head gas phase |
| Flow | ????47 | ????63 | ????136 | ????16 |
| Amount to | ????????????110 | ????????????152 | ||
3, improved the controllable quality ability
As everyone knows, distillation tower overhead product quality is mainly recently controlled by refluxing.The present invention is owing to adopted complicated distillation tower----oil to absorb the pattern of deethanizing column, and cat head is established condenser, makes the quality of cat head lean gas be able to better control.Can recently effectively control by regulating to reflux the quality of cat head gas phase.This in the past " double-column process " and " single tower flow process " do not possess.
4, improved the ability that reclaims carbon four above hydro carbons and gasoline fraction
Because oil absorbs the employing of deethanizing column, the absorption tower that its separating power is more independent, or absorb and steam tower and all want height, thereby, separating power for carbon four above hydro carbons and gasoline fraction is improved, and makes this partly loss of material minimizing in the final dry gas, has improved economic benefit.
The present invention oil absorbs deethanizer overhead gas phase and existing " double-column process " absorption tower cat head gas phase and all is sent to reabsorber and handles, thus relatively in these two bursts of gas phases the flow of relevant component just can find out separately recovery ability.Table 2 has provided the absorption tower cat head and oil absorbs deethanizer overhead gas phase component weight rate relatively, the weight rate that therefrom can find out carbon four of the present invention, carbon five and gasoline fraction is all little compared with existing " double-column process ", proves that oil absorbs deethanizing column and has the ability of higher recovery carbon four above hydro carbons and gasoline fraction.
Table 2. absorption tower cat head and oil absorb deethanizer overhead gas phase component weight rate relatively
Unit: kilogram/time
| Component | Non-hydrocarbon gas | ??CH4 | ??∑C2 | ??∑C3 | ??∑C4 | ??∑C5 | Gasoline fraction | Total flux |
| Double-column process | 3523 | ??3089 | ??5793 | ??902 | ??121 | ??1004 | ??1381 | ??15814 |
| The present invention | 3523 | ??3089 | ??5792 | ??893 | ??106 | ??813 | ??1061 | ??15276 |
5, product recovery rate and output have been improved
On identical charging and product specification basis, the present invention has improved the output of added value high product liquefied gas and stable gasoline, reduced the output of the lower byproduct dry gas of price and returned the flow of the rich absorbent oil of upstream equipment, thereby the economic benefit of whole device there has been bigger lifting.As seen from Table 3, dry gas output 13 of the present invention, 755kg/hr, 14 of " double-column process ", the little 344kg/hr of 099kg/hr, and the output sum of liquefied gas and stable gasoline " double-column process " want high 537kg/hr.
6, Economic and Efficiency Analysis relatively
The quality of full scale plant is on the size of the present economic benefit of final body.Now select certain " double-column process " that has 1,200,000 tons of catalytic cracking unit now object as a comparison, by the relatively product production and the general facilities consumption of the present invention and this existing procedure, economic benefit more separately.Should be noted that the price difference of benefit size and variant production, product distribute and the price of general facilities has crucial relation.Detailed performance analysis must be carried out for different catalytic cracking unit and just concrete numerical value can be drawn.
1) Benefit Calculation
In general, the economic benefit of full scale plant should be the residue after product sales revenue deducts the prices of raw and semifnished materials, general facilities consumption, labour cost, depreciation funds and overheads.Analysis for the different process flow process is compared, and then except that product sales revenue was different with general facilities consumption, all the other are every substantially all to be the same.Thereby only need analyze these two expenses and can finish benefit relatively.
Product relevant with absorbing-stabilizing system and general facilities price are as follows: 2050 yuan/ton of stable gasolines; 1450 yuan/ton of liquefied gas; 600 yuan/ton of dry gas; 0.25 yuan/ton of recirculated water; 0.40 yuan/kilowatt-hour of electricity; 80 yuan/ton of steam;
2) benefit benchmark
Two kinds of devices must compare under identical condition, thereby the following benchmark of regulation:
1. the charging of two kinds of devices is identical;
2. C3 concentration is 3% in the dry gas;
3. the quality product of liquefied gas and stable gasoline is identical, and promptly carbon two concentration are 1% in the liquefied gas, and carbon five concentration are 2%; The concentration of carbon four is 1% in the stable gasoline;
4. the lean absorption oil flow is identical, and rich absorbent oil is that material is returned in inside, and these two strands of materials are all without charge in performance analysis;
5. stabilizer tower and desorb Tata still reboiler are materials inside heating in the separation column one, do not have concrete price, for simplicity, all valuate by steam;
6. the flow that replenishes absorption agent is not stipulated, as long as satisfy the said products specification.
3) two kinds of device product output and general facilities consumption
Press the benchmark of afore mentioned rules, two kinds of devices are carried out flowsheeting calculate.Now the results are shown in the table 3,4 relevant:
Two kinds of device turnover material balances of table 3 and product production are relatively
Unit: kilogram/time
| Motion device material total flux | Dry gas output | Liquefied gas output | The stable gasoline amount | The rich absorbent oil amount | Go out device material total flux | |
| Double-column process | ??123090 | ??14099 | ?23511 | ?70266 | ?15214 | ?123090 |
| The present invention | ??123090 | ??13755 | ?23532 | ?70782 | ?15021 | ?123090 |
Two kinds of devices of table 4 general facilities consumption rate
| Water (ton/time) | Electricity (degree/time) | Steam (ton/time) | |
| Double-column process | ????1361 | ????318 | ????26.35 |
| The present invention | ????1129 | ????260 | ????21.17 |
From table 3 data as can be known, dry gas amount of the present invention " double-column process " is little, this is because the present invention has adopted oily absorption deethanizing column, separating power is greatly improved, though the regulation of carbon three concentration is 3% in the dry gas, but the present invention is stronger for the Separation and Recovery ability of carbon four above hydro carbons and gasoline fraction, so its product recovery rate is higher.
Table 4 data then be the general facilities consumption rate since cancelled two plume amounts very considerable return material, the consumption of water of the present invention, electricity and steam is generally little than existing " double-column process ", the saving of energy consumption is fairly obvious.
4) two kinds of device economic benefits are than changeing
Two kinds of devices of table 5 economic benefit relatively
Unit: unit/time
| Product sales revenue S | General facilities consumes U | ?????S-U | |
| Double-column process | ????186596 | ????2575 | ????184021 |
| The present invention | ????187476 | ????2079 | ????185397 |
| The present invention has a net increase of benefit | Have a net increase of sales revenue | General facilities consumption reduces | Have a net increase of benefit |
| ????880 | ????496 | ????1376 |
Just can count the economic benefit of flow process according to product production and general facilities consumption, as shown in table 5.Existing " double-column process " product sales revenue of the present invention increase by 880 yuan/time, general facilities consumption reduce 496 yuan/time, amount to have a net increase of 1376 yuan of benefits/time.If number was by 8000 hours when year produced, the present invention compares with existing " double-column process " can have a net increase of 1100.8 ten thousand yuan of economic benefits every year.
Fig. 1 is an absorption stabilizing apparatus for catalytic cracking schematic flow sheet of the present invention.
The invention will be further described by following embodiment and accompanying drawing thereof:
As shown in Figure 1, absorption stabilizing apparatus for catalytic cracking is by a complicated distillation tower that 50-80 piece actual plate is arranged---and the pipeline that oil absorbs deethanizing column 1, reabsorber 2, stabilizer tower 3 and heat exchanger network, pump, container and is connected them is formed.Annexation between them is as follows:
Pipeline 17 absorbs deethanizing column 1 top inlet with oil and links to each other, pipeline 18 absorbs deethanizing column 1 centre inlet with oil and links to each other, oil absorbs between the outlet of deethanizing column 1 top gas and condenser 4 imports and is linked to each other by pipeline 19, condenser 4 outlets link to each other with the import of return tank 5, link to each other by pipeline 20 between the bottom inlet of the pneumatic outlet of return tank 5 and reabsorber 2, the liquid exit of return tank 5 is linked to each other by pipeline 21 with pump 6 imports, and pump 6 outlets absorb deethanizing column 1 top phegma import with oil and link to each other;
The top that oil absorbs deethanizing column 1 is rectifying section, rectifying section is provided with side cooler 7, the import of water cooler 7 links to each other with pump 8, pump 8 absorbs the outlet of deethanizing column 1 upper rectifying section side line with oil and is linked to each other by pipeline 22, and the material outlet of water cooler 7 absorbs deethanizing column 1 top material inlet with oil and linked to each other by pipeline 23;
The Lower Half that oil absorbs deethanizing column 1 is a stripping section, stripping section is provided with intermediate reboiler 9, the cold side import of intermediate reboiler 9 absorbs the outlet of deethanizing column 1 stripping section side line with oil and is linked to each other by pipeline 24, and the cold side outlet and the oil of intermediate reboiler 9 absorb deethanizing column 1 stripping section side line import and linked to each other by pipeline 25;
The bottom that oil absorbs deethanizing column 1 is the tower still, the tower still is provided with tower still reboiler 10, reboiler 10 adopts the still liquid of stabilizer tower 3 to make heating medium, link to each other with stable Tata still still liquid outlet pipe by the hot side entrance of pipeline 34 reboiler 10, the hot side entrance of intermediate reboiler 9 is linked to each other by pipeline 35 with the hot side outlet of reboiler 10, intermediate reboiler 9 hot side outlets are linked to each other by pipeline 36 with 11 imports of stable gasoline water cooler, these water cooler 11 outlets are linked to each other by pipeline 37 with pump 16, pump 16 absorbs deethanizing column 1 cat head import with oil and is linked to each other by pipeline 38, and the stable gasoline product is sent via pipeline 39;
Reabsorber 2 is provided with the dry gas outlet that a lean absorption oil import that links to each other with pipeline 28 and links to each other with pipeline 27, also is provided with a still liquid outlet that links to each other with pipeline 29 and a stingy import that links to each other with pipeline 20;
The middle part of stabilizer tower 3 is provided with opening for feed, this opening for feed absorbs deethanizing column 1 bottom still liquid outlet with oil and is linked to each other by pipeline 26, stabilizer tower 3 top gas phase discharge ports are linked to each other by pipeline 30 with condenser 12, return tank 13 is linked to each other by pipeline 31 with pump 14, pump 14 is linked to each other by pipeline 32 with stabilizer tower 3 top phegma imports, and pipeline 33 is the liquefied gas product transfer limes that link to each other with pump 14.Equipment 15 is to stablize Tata still reboiler.
Temperature is that 34～40 ℃ additional absorption agent is sent into oil absorption deethanizing column 1 top through pipeline 38; Temperature is that 34～40 ℃ raw gasline is sent into the cat head that oil absorbs deethanizing column 1 through pipeline 17; Temperature is that 34～40 ℃ pressure rich gas is sent into the middle part that oil absorbs deethanizing column 1 through pipeline 18, and the working pressure that oil absorbs deethanizing column is 1.0～1.45Mpa, and its overhead condenser material outlet temperature is 34-42 ℃, and its tower still temperature is 115～135 ℃.The rectifying section that oil absorbs deethanizing column 1 is provided with side cooler 7, and this water cooler adopts recirculated water cooling, will absorb the deethanizing column 1 through pipeline 22 from oil, after the liquid material of being extracted out by pump 8 is cooled to 36～40 ℃, sends back in the tower through pipeline 23 again.The stripping section that oil absorbs deethanizing column is provided with intermediate reboiler 9, and it will be in the tower that pipeline 24 is extracted out behind liquid heat to 85～95 ℃, sends back in the tower through pipeline 25 again.Tower still reboiler 10 adopts through pipeline 34 and sends here, and temperature is that 170～190 ℃ the still liquid of stabilizer tower 3 is as heating medium.After this still liquid went out tower still reboiler 10, temperature was reduced to 100～110 ℃, was sent to intermediate reboiler 9 as thermal source by pipeline 35.Stabilizer tower still liquid temp by intermediate reboiler 9 outlets further is reduced to 80～95 ℃.Deliver to stable gasoline water cooler 11 through pipeline 36 then, in this water cooler, be cooled to 36～40 ℃ again.Stable tower bottoms is divided into two strands after going out water cooler 11, and one is the stable gasoline product, sends through pipeline 39, and another strand is to replenish absorption agent, is sent to oil through pipeline 38 and absorbs the deethanizing column top.
Absorb deethanizer overhead return tank 5 by oil, the lean gas of sending through pipeline 20 enters reabsorber, and in reabsorber and the lean absorption oil counter current contact of cat head under drenching, the cat head gas phase is the byproduct dry gas, sends via pipeline 27.Tower still still liquid is rich absorbent oil, is sent to upstream equipment by pipeline 29.The working pressure of reabsorber is for being that tower top temperature is about 46-58 ℃ about 1.0-1.35Mpa, and tower still temperature is about 40-56 ℃.
Oil absorbs the discharging of deethanizing column tower bottoms phase and is sent to stabilizer tower 3 through pipeline 26, and the working pressure of stabilizer tower is about 0.9-1.2Mpa, and the phegma temperature is about 36-42 ℃, and tower still temperature is about 170-190 ℃.The discharging of cat head gas phase enters overhead condenser 12 by pipeline 30, this condenser is a complete condenser, adopt water quench, the cat head gas phase all is condensed into liquid, enters return tank 13, and the liquid phase of return tank is sent by pump 14 by pipeline 31, a part is as the phegma of stabilizer tower, return cat head by pipeline 32, another part is sent via pipeline 33 as the liquefied gas product.
Absorption stabilizing apparatus for catalytic cracking of the present invention is imported and exported material to be had: the material of motion device has the raw gasline that enters by pipeline 17, the compression rich gas that enters by pipeline 18 and the lean absorption oil that enters by pipeline 28.The liquefied gas that the material that goes out device has the dry gas sent by pipeline 27, send by pipeline 33, the stable gasoline of sending by pipeline 39 and the rich absorbent oil of sending by pipeline 29.
Be one below and use production instance of the present invention that to further specify the present invention and effect, the charging of device has raw gasline, compression rich gas and the lean absorption oil from upstream equipment.
The temperature of raw gasline is 40 ℃, and pressure is 1.25Mpa, and flow is 63,000Kg/hr, and its engler's boiling range such as following table:
The temperature of rich gas is 40 ℃, and pressure is 1.28Mpa, and flow is 46,590Kg/hr.It is composed as follows:
The temperature of lean absorption oil is 40 ℃, and pressure is 0.95Mpa, and flow is 13,500Kg/hr.Its engler's boiling range is as follows:
Use device of the present invention above-mentioned charging is processed, product reaches following specification (mol%):
| Boiling range (%) | ????0 | ????5 | ????10 | ????30 | ????50 | ????70 | ????90 | ????100 |
| Temperature (℃) | ????40 | ????54 | ????68 | ????99 | ????124 | ????150 | ????86 | ????212 |
| Component | Non-hydrocarbon gas | ??CH4 | ????∑C3 | ????∑C4 | ????∑C5 | |
| Form (mol%) | ???19.92 | ??15.08 | ????16.04 | ????19.60 | ????18.57 | ????10.79 |
| Boiling range (%) | ??0 | ??5 | ??10 | ??30 | ??50 | ??70 | ??90 | ??100 |
| Temperature (℃) | ??193.5 | ??220 | ??229.5 | ??248 | ??269 | ??295 | ??324 | ??347 |
Dry gas: ∑ C3＜3%
Liquefied gas: ∑ C2＜1%, ∑ C5＜2%
Stable gasoline: the processing condition of ∑ C4＜1% each tower of the present invention are as follows:
| Tower | Oil absorbs deethanizing column | Reabsorber | Stabilizer tower |
| Working pressure (Mpa) | ????1.28 | ????0.85 | ????0.96 |
| The return tank temperature (℃) | ????38 | ????--- | ????38 |
| Tower top temperature (℃) | ????43.8 | ????50.1 | ????54.3 |
| Tower still temperature (℃) | ????120 | ????46 | ????178 |
| Reflux ratio | ????0.92 | ????--- | ????2.46 |
| Cat head thermal load (Mkcal/hr) | ???-0.3125 | ????--- | ???-7.1189 |
| Tower still thermal load (Mkcal/hr) | ????4.9532 | ????--- | ????6.6288 |
| Side cooler thermal load (Mkcal/hr) | ???-0.7710 | ????--- | ????--- |
| Intermediate reboiler thermal load (Mkcal/hr) | ????1.2273 | ????--- | ????--- |
Composition, the output of each product of the present invention are as follows:
Claims (10)
1, a kind of absorption stabilizing apparatus for catalytic cracking, it comprises reabsorber and stabilizer tower, it is characterized in that it is by a complicated distillation tower---the pipeline that oil absorbs deethanizing column (1), reabsorber (2), stabilizer tower (3) and heat exchanger network, pump, container and is connected them is formed; The top that oil absorbs deethanizing column (1) is provided with a condenser system; Oil absorbs deethanizing column (1) first half rectifying section and is provided with one or two component cooling system; Oil absorbs deethanizing column (1) Lower Half stripping section and is provided with an intermediate reboiler system; Oil absorbs deethanizing column (1) bottom and is provided with a tower still reboiler (10); Stabilizer tower 3 cats head are provided with a circulating cooling system.
2,, it is characterized in that the condenser system that the oily top that absorbs deethanizing column (1) is provided with is to be in series by pipeline (19), (21) successively by condenser (4), return tank (5) and pump (6) according to the described a kind of absorption stabilizing apparatus for catalytic cracking of claim 1.
3, according to the described a kind of absorption stabilizing apparatus for catalytic cracking of claim 1, the component cooling system that it is characterized in that the first half rectifying section setting of oil absorption deethanizing column (1) is to be in series by pipeline (22), water cooler (7), pump (8) and pipeline (23) successively, such cooling system can be provided with one or two, if there are two, then be separately positioned on the different positions up and down of rectifying section.
4, according to the described a kind of absorption stabilizing apparatus for catalytic cracking of claim 1, it is characterized in that the annexation of heat exchanger network: the hot side entrance that oil absorbs the tower still reboiler (10) of deethanizing column (1) links to each other with stable tower bottoms outlet by pipeline (34); The hot side outlet of tower still reboiler (10) links to each other by the hot side entrance of pipeline (35) and intermediate reboiler (9), and the hot side outlet of intermediate reboiler (9) links to each other by the hot side entrance of pipeline (36) and stable gasoline water cooler 11.
5, a kind of absorption stabilizing apparatus for catalytic cracking according to claim 1 is characterized in that the stripping section of oil absorption deethanizing column (1) is provided with the intermediate reboiler system that is in series successively by pipeline (24), intermediate reboiler (9) and pipeline (25).
6, a kind of production technique of absorption stabilizing apparatus for catalytic cracking, it comprises the production technique of reabsorber and stabilizer tower, it is characterized in that: the material of motion device has three strands, promptly enter by pipeline (17), temperature is 34-40 ℃ raw gasline, raw gasline directly enters the top that oil absorbs deethanizing column; Enter by pipeline (18), temperature is that 34-40 ℃ compression rich gas directly enters the middle part that oil absorbs deethanizing column; Also has the lean absorption oil that enters reabsorber by pipeline (28) in addition;
The pressure that oil absorbs deethanizing column (1) is 1.0-1.45Mpa, the phegma temperature is 34-42 ℃, adjustment by reflux ratio, the quality of may command overhead product, the tower still reboiler that oil absorbs deethanizing column (1) is that the temperature by stabilizer tower is that 170-190 ℃ high-temperature kettle liquid heats, stable tower bottoms directly enters the tower still reboiler (10) that oil absorbs deethanizing column, after should stablize tower bottoms coming out from tower still reboiler (10), temperature is reduced to 100-110 ℃, be re-used as the thermal source of intermediate reboiler (9), after the intermediate reboiler heat exchange, the temperature of this still liquid is reduced to 80-95 ℃, enter the stable gasoline water cooler then, be as cold as about 40 ℃, after this be divided into two strands of materials, one is the stable gasoline product, another thigh is absorption agent as a supplement, sends the top that oil is inhaled deethanizing column (1) back to;
Oil absorbs the cat head gaseous products of deethanizing column, then enters reabsorber (2), obtains byproduct dry gas and recycle stock rich absorbent oil through separation; Oil absorbs the tower bottoms phase product of deethanizing column, then directly enters stabilizer tower (3), is divided into product liquefied gas and stable gasoline by this tower.
7, described a kind of catalytic cracking absorbs stably manufactured technology according to claim 6, it is characterized in that heating medium that oil absorbs the tower still reboiler (10) of deethanizing column (1) and intermediate reboiler (9) is the high-temperature kettle liquid of the stabilizer tower (3) directly sent here through pipeline (34); The first thermal source of this still liquid as tower still reboiler (10), and then enter intermediate reboiler (9) as heating medium.
8, described a kind of catalytic cracking absorbs stably manufactured technology according to claim 6, and the inlet feed that it is characterized in that stable gasoline water cooler (11) is the heated side outlet material that is absorbed deethanizing column (1) intermediate reboiler (9) by the oil that pipeline (36) is sent here.
9, described a kind of catalytic cracking absorbs stably manufactured technology according to claim 6, it is characterized in that the pressure from upstream equipment is 1.0～1.45Mpa, temperature is 34～40 ℃ a compression rich gas, directly enter the middle part that oil absorbs deethanizing column (1) by pipeline (18), no longer be provided with any interchanger and/or gas-liquid separator therebetween.
10, described a kind of catalytic cracking absorbs stably manufactured technology according to claim 6, it is characterized in that oil absorbs the still liquid of deethanizing column (1), directly enters stabilizer tower middle part opening for feed by pipeline (26), no longer is provided with any interchanger therebetween.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 99116296 CN1089264C (en) | 1999-07-20 | 1999-07-20 | Absorption stabilizing apparatus for catalytic cracking and its production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 99116296 CN1089264C (en) | 1999-07-20 | 1999-07-20 | Absorption stabilizing apparatus for catalytic cracking and its production process |
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| Publication Number | Publication Date |
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| CN1240671A true CN1240671A (en) | 2000-01-12 |
| CN1089264C CN1089264C (en) | 2002-08-21 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 99116296 Expired - Fee Related CN1089264C (en) | 1999-07-20 | 1999-07-20 | Absorption stabilizing apparatus for catalytic cracking and its production process |
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| CN (1) | CN1089264C (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100400624C (en) * | 2005-07-07 | 2008-07-09 | 天津大学 | Stepwise condensation process for catalytic cracking absorbing-stabilizing system and its combining process |
| CN100425673C (en) * | 2005-07-07 | 2008-10-15 | 天津大学 | Catalytic cracking absorbing stable system composite technique |
| CN102382680A (en) * | 2010-08-30 | 2012-03-21 | 中国石油化工股份有限公司 | Combined technology of catalytic cracking absorbing stabilizing system and C3 intercooling oil absorption |
| CN102942488A (en) * | 2012-11-02 | 2013-02-27 | 天津大学 | Regeneration technology of recovered methylamine solution and device thereof |
| CN107022378A (en) * | 2016-02-01 | 2017-08-08 | 中国石化工程建设有限公司 | The technique of the dry-gas recovery system and recovery dry gas of hydrocracking unit or hydro-upgrading unit |
| CN114307549A (en) * | 2021-12-20 | 2022-04-12 | 华南理工大学 | Process for reducing energy consumption of absorption stabilization system in oil refining process |
-
1999
- 1999-07-20 CN CN 99116296 patent/CN1089264C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100400624C (en) * | 2005-07-07 | 2008-07-09 | 天津大学 | Stepwise condensation process for catalytic cracking absorbing-stabilizing system and its combining process |
| CN100425673C (en) * | 2005-07-07 | 2008-10-15 | 天津大学 | Catalytic cracking absorbing stable system composite technique |
| CN102382680A (en) * | 2010-08-30 | 2012-03-21 | 中国石油化工股份有限公司 | Combined technology of catalytic cracking absorbing stabilizing system and C3 intercooling oil absorption |
| CN102382680B (en) * | 2010-08-30 | 2014-12-31 | 中国石油化工股份有限公司 | Combined technology of catalytic cracking absorbing stabilizing system and C3 intercooling oil absorption |
| CN102942488A (en) * | 2012-11-02 | 2013-02-27 | 天津大学 | Regeneration technology of recovered methylamine solution and device thereof |
| CN102942488B (en) * | 2012-11-02 | 2014-10-15 | 天津大学 | Regeneration technology of recovered methylamine solution and device thereof |
| CN107022378A (en) * | 2016-02-01 | 2017-08-08 | 中国石化工程建设有限公司 | The technique of the dry-gas recovery system and recovery dry gas of hydrocracking unit or hydro-upgrading unit |
| CN114307549A (en) * | 2021-12-20 | 2022-04-12 | 华南理工大学 | Process for reducing energy consumption of absorption stabilization system in oil refining process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1089264C (en) | 2002-08-21 |
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