CN2404575Y - Distilling tower for catalytic cracking and absorption stabilization system - Google Patents
Distilling tower for catalytic cracking and absorption stabilization system Download PDFInfo
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- CN2404575Y CN2404575Y CN 99236680 CN99236680U CN2404575Y CN 2404575 Y CN2404575 Y CN 2404575Y CN 99236680 CN99236680 CN 99236680 CN 99236680 U CN99236680 U CN 99236680U CN 2404575 Y CN2404575 Y CN 2404575Y
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- distillation tower
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- reboiler
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Abstract
The utility model relates to a petrochemical engineering device. A distilling tower used for catalytic cracking, absorption and stabilizing is composed of a main-body condensing system of the distilling tower, a middle cooling system, a middle reboiler and a tower-kettle reboiler. The utility model has the advantages that product output is improved, and byproduct output and operating cost are reduced; compared with the existing device, under the conditions of same material feeding and product specification, when the scale of the petrochemical engineering device is 1200 thousands tons every year, operating cost is reduced by 3968 thousands every year, the sales income of products is increased by 7040 thousands yuan every year, and the net increase of the total economic benefit is 11008 thousands yuan every year.
Description
The utility model relates to petrochemical equipment, is meant that specifically catalytic cracking absorbs the stable distillation tower of using.
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, total throughput reaches 7,200 ten thousand tons/year.And absorbing-stabilizing system is the after-treatment system in the catalytic cracking unit, and the raw gasline and the rich gas of its fractionation of autocatalysis in the future cat head are separated into dry gas, liquefied gas and stable gasoline product.The product yield of absorbing-stabilizing system and energy consumption have crucial influence to the economic benefit of whole device.
Absorbing-stabilizing system 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 domestic absorbing-stabilizing system 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.Mainly there is following shortcoming:
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. install difficulty of regulating and controlling.
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.Original old device also transform " double-column process " one after another as, " double-column process " pattern has occupied dominant position fully in catalytic cracking unit so far, estimating has the catalytic cracking unit more than 80% all to adopt " double-column process " approximately, has all become leading flow process at home, abroad.
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, enter absorbing-stabilizing system raw gasline and the compression rich gas, its 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 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 inventory 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 purpose of this utility model is to overcome the shortcoming of present leading flow process " double-column process " and early stage " single tower flow process ", and the distillation tower that a tower provides a kind of absorption-stabilization system by catalytic cracking simple in structure, that energy consumption is low, product recovery rate is high, economic benefit is big to use is merged on absorption tower and desorption tower.
The purpose of this utility model realizes by following measure:
The distillation tower that a kind of absorption-stabilization system by catalytic cracking is used is made up of distillation tower main body, condenser system, component cooling system, intermediate reboiler and tower still reboiler; Concrete composition and annexation are as follows:
The top of distillation tower main body is provided with the condenser system that condenser, return tank and series connection of pumps is formed by pipeline;
The different positions of the first half rectifying section of distillation tower main body is provided with 1～2 individual component cooling system that side cooler and series connection of pumps is formed by pipeline;
The Lower Half stripping section of distillation tower main body is provided with an intermediate reboiler, and intermediate reboiler links to each other with stripping section by cold side ducts;
The bottom column still of distillation tower main body is provided with tower still reboiler, and its hot side outlet links to each other with the intermediate reboiler of stripping section by pipeline.
Stable tower bottoms in the absorbing-stabilizing system is as the heating medium of distillation tower reboiler, its temperature is reduced to 100～110 ℃ after carrying out heat exchange, through pipeline it is sent to intermediate reboiler as thermal source again, be reduced to 80～95 ℃ from the stabilizer tower still liquid temp of middle reboiler outlet, again about pipeline is delivered to stable gasoline water cooler to 40 ℃, material is divided into two strands then, and one is that the stable gasoline product is sent by pipeline.Another the thigh then as a supplement absorption agent send the distillation tower cat head back to by pump and pipeline.
The utility model compared with prior art has following advantage and effect
1, simple in structure, efficient
Structure of the present utility model has simple, characteristics of high efficiency with existing leading flow process---" double-column process " structure is 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; The second, cancelled and compressed rich gas in the former flow process and return material water cooler and gas-liquid separator; The 3rd, 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 utility model cancelled two plume amounts in the existing leading flow process very considerable return material, absorb tower bottoms and desorb column overhead gas phase, bigger saving the water, electricity, gas consumption of device.
Table 1 has provided the inlet amount of certain 1,200,000 tons of absorption stabilizing apparatus for catalytic cracking and has returned inventory.The inventory that therefrom can find out motion device be 110 tons/time, return inventory then up to 152 tons/time, it is big that its throughput ratio inlet amount 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 " charging and return inventory relatively
Unit: ton/time
| The device charging | Return material | |||
| 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 utility model is owing to adopted the pattern of oily absorption 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 utility model oil absorbs deethanizer overhead gas phase and " 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 separating power.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 " 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 utility model | 3523 | 3089 | 5792 | 893 | 106 | 813 | 1061 | 15276 |
5, improved product production
On identical charging and product specification basis, the utility model has improved the output of added value high product liquefied gas and stable gasoline, reduced the lower output of paying the product dry gas of price, thereby the economic benefit of whole device has had bigger lifting.
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 " double-column process " of selecting certain 1,200,000 tons of catalytic cracking unit be object as a comparison, calculates the product production and the general facilities consumption of the present invention and former flow process, economic benefit more separately by flowsheeting.Should be noted that the price difference of benefit size and variant production, product distribute and the price of general facilities has crucial relation.Must carry out concrete flowsheeting and performance analysis can draw concrete benefit size for different catalytic cracking unit.
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
Newly, old two kinds of flow processs must compare on identical benchmark.Thereby the following benchmark of regulation:
1. two kinds of flow system chargings are 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; 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 flow process product productions and general facilities consumption
Press the benchmark of afore mentioned rules, new, old two kinds of flow processs are carried out flowsheeting.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
| Advance system's material total flux | Dry gas output | Liquefied gas output | The stable gasoline amount | The rich absorbent oil amount | Go out system's material total flux | |
| Double-column process | 123090 | 14099 | 23511 | 70266 | 15214 | 123090 |
| The utility model | 123090 | 13755 | 23532 | 70781 | 15021 | 123089 |
Two kinds of general facilities consumption rates of table 4
| Water (ton/time) | Electricity (degree/time) | Steam (ton/time) | |
| Double-column process | 1361 | 318 | 26.35 |
| The utility model | 1129 | 260 | 21.17 |
From table 3 data as can be known, the utility model dry gas amount " 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 utility model, electricity and steam is generally little than " double-column process ", the saving of energy consumption is fairly obvious.
4) two kinds of device economic benefits relatively
Two kinds of devices of table 5 economic benefit relatively
Unit: unit/time
| The product essence is sold income S | General facilities consumes U | S-U | |
| Double-column process | 186596 | 2575 | 184021 |
| The utility model | 187476 | 2079 | 185397 |
| The utility model 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.The utility model " double-column process " product sales revenue 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 utility model is compared with " double-column process " and can be had a net increase of 1100.8 ten thousand yuan of economic benefits every year.
Fig. 1 is the stable distillation tower structural representation of using for catalytic cracking absorbs.
The utility model is described in further detail by following embodiment and accompanying drawing thereof:
As shown in Figure 1, catalytic cracking absorbs to stablize and is made up of distillation tower main body 1, condenser system, component cooling system, intermediate reboiler and tower still reboiler with distillation tower.Annexation between them is as follows:
Pipeline 10 links to each other with distillation tower main body 1 top inlet, pipeline 11 links to each other with distillation tower main body 1 centre inlet, link to each other by pipeline 12 between distillation tower main body 1 top gas outlet and condenser 2 imports, condenser 2 outlets link to each other with the import of return tank 3, the pneumatic outlet of return tank 3 links to each other with pipeline 21, the liquid exit of return tank 3 is linked to each other by pipeline 13 with pump 4 imports, and pump 4 outlets link to each other with the 1 top phegma import of distillation tower main body;
The top of distillation tower main body 1 is rectifying section, rectifying section is provided with side cooler 5, the import of water cooler 5 links to each other with pump 6, and pump 6 is linked to each other by pipeline 16 with the outlet of distillation tower main body 1 upper rectifying section side line, and the material outlet of water cooler 5 is linked to each other by pipeline 15 with distillation tower main body 1 top material inlet;
The bottom of distillation tower main body 1 is a stripping section, stripping section is provided with intermediate reboiler 7, the cold side import of intermediate reboiler 7 is linked to each other by pipeline 17 with the outlet of distillation tower main body 1 stripping section side line, and the cold side outlet of intermediate reboiler 7 is linked to each other by pipeline 18 with the 1 stripping section side line import of distillation tower main body;
The bottom of distillation tower main body 1 is the tower still, the tower still is provided with tower still reboiler 8, reboiler 8 employings stablizing tower bottoms is made heating medium and is linked to each other by pipeline 19, intermediate reboiler 7 is linked to each other by pipeline 14 with the hot side of tower still reboiler 8, intermediate reboiler 7 hot side outlets link to each other with water cooler, carry the pipeline 9 that replenishes absorption agent to link to each other with the cat head inlet pipe of distillation tower 1.
Temperature is that the raw gasline about 34-40 ℃ directly enters the top of distillation tower main body 1 by pipeline 10.Temperature is that the compression rich gas about 34-40 ℃ enters the middle part of distillation tower main body 1 via pipeline 11, the overhead gas of distillation tower main body 1 enters condenser 2 through pipeline 12, this condenser is cooled with circulating water, the cat head gas phase that is cooled to about 36-40 ℃ is divided into gas-liquid two-phase in return tank 3, gas phase is referred to as lean gas, enters the bottom of reabsorber through pipeline 21; Liquid phase then as the phegma of distillation tower main body, by pipeline 13, is returned cat head by pump 4.The working pressure of distillation tower is about 1.0-1.45Mpa, rectifying section at this tower is provided with side cooler 5, and this water cooler adopts the recirculated water cooling, will be through pipeline 16 from distillation tower main body 1, after the liquid material of being extracted out by pump 6 is cooled to about 36-40 ℃, send back in the tower through pipeline 15 again.Stripping section in distillation tower main body 1 is provided with intermediate reboiler 7, it will be in the tower that pipeline 17 is extracted out about liquid heat to 90 ℃ after, through pipeline 18, send back in the tower again by potential difference.Tower still in distillation tower main body 1 is provided with tower still reboiler 8, it is that stable tower bottoms about 170-190 ℃ is as heating medium that tower still reboiler adopts through the temperature that pipeline 19 is sent here, tower still temperature is controlled at about 115-135 ℃, after this still liquid goes out tower still reboiler, temperature is reduced to about 100-110 ℃, be sent to intermediate reboiler 7 by pipeline 14, as its thermal source.The stabilizer tower still liquid temp that is come out by intermediate reboiler 7 is reduced to about 80-95 ℃, deliver to the stable gasoline water cooler through pipeline 20, this material is divided into two strands then, and one is the stable gasoline product, another strand by pipeline 9 as a supplement absorption agent send distillation tower main body 1 cat head back to.
Claims (1)
1, the distillation tower used of a kind of absorption-stabilization system by catalytic cracking, it is characterized in that: it is made up of distillation tower main body, condenser system, component cooling system, intermediate reboiler and tower still reboiler; Concrete composition and annexation are as follows:
The top of distillation tower main body (1) is provided with the condenser system that is in series successively by pipeline (12), condenser (2), return tank (3), pipeline (13) and pump (4);
The different positions of the first half rectifying section of distillation tower main body (1) is provided with 1～2 component cooling system that is in series successively by pipeline (15), water cooler (5), pump (6) and pipeline (16);
The Lower Half stripping section of distillation tower main body (1) is provided with intermediate reboiler (7), and its cold side links to each other with (18) with pipeline (17), and its hot side is to link to each other with (20) with pipeline (14);
The bottom column still of distillation tower main body (1) is provided with tower still reboiler, and its hot side outlet links to each other with the intermediate reboiler (7) of stripping section by pipeline (14).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 99236680 CN2404575Y (en) | 1999-07-22 | 1999-07-22 | Distilling tower for catalytic cracking and absorption stabilization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 99236680 CN2404575Y (en) | 1999-07-22 | 1999-07-22 | Distilling tower for catalytic cracking and absorption stabilization system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2404575Y true CN2404575Y (en) | 2000-11-08 |
Family
ID=34024462
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 99236680 Expired - Fee Related CN2404575Y (en) | 1999-07-22 | 1999-07-22 | Distilling tower for catalytic cracking and absorption stabilization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2404575Y (en) |
-
1999
- 1999-07-22 CN CN 99236680 patent/CN2404575Y/en not_active Expired - Fee Related
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |