CN1710028A - Stepwise condensation process for catalytic cracking absorbing-stabilizing system and its combining process - Google Patents
Stepwise condensation process for catalytic cracking absorbing-stabilizing system and its combining process Download PDFInfo
- Publication number
- CN1710028A CN1710028A CN 200510014443 CN200510014443A CN1710028A CN 1710028 A CN1710028 A CN 1710028A CN 200510014443 CN200510014443 CN 200510014443 CN 200510014443 A CN200510014443 A CN 200510014443A CN 1710028 A CN1710028 A CN 1710028A
- Authority
- CN
- China
- Prior art keywords
- craft
- desorption tower
- gas
- tower
- feed
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to the producing craft of catalysis crack absorption stabilizing system, including step condensation craft and its composite craft with middle reboiler. The characteristic of step condensation craft are: after mixed, the compressed rich gas, rich absorption oil and desorption gases directly get into balance kettle to have gas-liquid separation, then step cool condensable oil and non-condensable gases, the condensable oil gets into the middle and upside of desorption tower as hot feed after slightly cooled, and the non-condensable gases get into the top of desorption tower as cold feed after cooled to a lower temperature. The step condensation craft and its composite craft has two-gate feed characteristic, which avoids back-mix. Under same feed, operating condition and production specification, compared with two-tower flow normal craft, it's the cool load before balance kettle is greatly reduced, which are respectively reduced by 48.6%, 39.5%; the load of desorption tower reboiler of the composite craft is reduced by 37.3% than cold feed craft.
Description
Technical field
The present invention relates to petroleum refining process, especially stepwise condensation process for catalytic cracking absorbing-stabilizing system and recombining process thereof.
Background technology
Along with expanding economy, it is the problem that oil refining industry is paid close attention to the most that energy-conservation and quality product is improved.It all is single tower flow process that old device is stablized in the catalytic cracking absorption sixties in 20th century, and its shortcoming is C in the cat head lean gas
3C in the deethanizing gasoline at the bottom of content height and the tower
2The content height.The eighties in 20th century, these old devices of great majority changed single tower flow process into double-column process, had avoided the shortcoming of single tower flow process.
The feeding manner of double-column process desorption tower mainly contains three kinds of cold feed, hot feed and cold and hot bifilar chargings.
The characteristics of cold feed technical process are that the condensed oil with surge tank does not heat and directly enters the desorption tower top.The advantage of this technology is: C in the dry gas
3 +Content is few, good absorbing effect, and gas desorption quantity is few; Shortcoming is that desorption tower load and desorb tower bottom reboiler load are big.
The hot feed technical process enters the desorption tower top after then utilizing the heat energy of stable gasoline that condensed oil is heated again; Its advantage is the load that reduces desorption tower reboiler, but gas desorption quantity is very big under the hot feed situation, causes absorption tower assimilation effect variation, and the load of rich gas condenser also increases.
Bifilar feeding process flow process characteristics are: condensed oil is divided into two strands, and the laggard middle and upper part of one and stable gasoline heat exchange to desorption tower, another strand cold feed directly enters the desorption tower top.Bifilar charging combines the advantage of hot and cold two bursts of chargings, has obvious superiority, not only reduces the load of desorption tower bottom reboiler but also make gas desorption quantity reduce relatively.Yet, owing to this technology is formed the different positions that identical condensed oil enters tower respectively with the temperature difference, there is axial backmixing, make impellent descend, mass transfer is caused disadvantageous effect, decrease in efficiency.
Hot feed and bifilar charging for routine, a large amount of gas-liquid mixtures drop to 40 ℃ earlier, and afterwards, cryocondensation oil can be heated to 80 ℃ through stable gasoline again and enter the desorption tower top, the process of this " cooling post-heating earlier " is actually a kind of energy waste, and unreasonable.
Summary of the invention
The objective of the invention is to, overcome the deficiency that above-mentioned each technology exists, and a kind of stepwise condensation process for catalytic cracking absorbing-stabilizing system and recombining process thereof are provided, technology of the present invention has the characteristics of bifilar charging, avoid back-mixing, can reduce energy expenditure simultaneously, reduced the tower internal loading.
Purpose of the present invention reaches by following measure: adopt the double-column process desorption tower, to compress and directly enter surge tank after rich gas, rich absorbent oil and stripping gas mix and carry out gas-liquid separation, and then fractional condensation, after the condensed oil temperature reaches 55 ℃～70 ℃, as the desorption tower hot feed, after non-condensable gas is cooled to 35 ℃～40 ℃ as the desorption tower cold feed.
On the basis of stepwise condensation process, the desorption tower middle and lower part of stepwise condensation process flow process is provided with intermediate reboiler, constitute the recombining process that absorption-stabilization system by catalytic cracking of the present invention divides.
The present invention considers to utilize the heat of material self, has avoided " cold after heat earlier " process; Condensed oil only needs cooling a little, only the part charging is cooled to lesser temps, avoids unnecessary energy expenditure, and makes the preceding cooling load of surge tank to reduce significantly, thereby reaches energy-saving effect.The present invention with temperature, form the different positions that two bursts of different chargings enter desorption tower respectively, avoided back-mixing largely.And condensation is a proceed step by step among the present invention, and only partial material is cooled to lesser temps, and the operation of this fractional condensation can make C in the condensed oil
2Content reduces significantly, and after condensed oil entered desorption tower, the column plate load can reduce largely, and the flow of stripping gas also can reduce to some extent, and desorption effect is better.
The most special operating parameters that the present invention is different from general technology is two condensing temperatures.Generally speaking, compression, rich gas rich absorbent oil and the mixed temperature of charge of stripping gas three can be between 70 ℃～80 ℃, and therefore, the condensed oil condensing temperature of stepwise condensation process generally is not higher than 70 ℃; Simultaneously, this temperature can not be too low, otherwise can cause the desorption tower reboiler load excessive.
Desorption tower middle and lower part in the stepwise condensation process flow process is provided with intermediate reboiler, obtain recombining process, its thermal source is the stable gasoline from the stabilizer tower bottom, can be by suitably reducing condensed oil condensing temperature to 50 ℃～60 ℃, load to reduce gas desorption quantity and absorption tower, and reboiler is not too large at the bottom of the desorption tower.
The invention has the beneficial effects as follows, reduced the preceding condenser duty of surge tank significantly, have the advantage that reduces cold and hot energy expenditure, reduction gas desorption quantity, alleviates desorb Tata internal loading.The intermediate reboiler of recombining process partly also can reduce reboiler at the bottom of the desorption tower.
Description of drawings
Fig. 1 is a stepwise condensation process for catalytic cracking absorbing-stabilizing system schema of the present invention.
Fig. 2 is provided with the recombining process schema of intermediate reboiler for desorption tower of the present invention.
Fig. 3 is the character of each scheme stripping gas.
Fig. 4 is a desorption tower column plate gas phase load condition.
1-compresses rich gas, and 2-replenishes absorption agent, the 3-raw gasline, the 4-lean gas, 5-absorption tower, 6-rich absorbent oil, the 7-surge tank, 8-stripping gas, 9-condensed oil, 10-water, 11-condenser, 12-desorption tower, 13-desorb tower bottom reboiler, 14-deethanizing gasoline, 15-absorption tower intermediate condenser, 16-desorption tower intermediate reboiler
Embodiment
Embodiment 1: stepwise condensation process
As shown in Figure 1: with the catalysis amount of finish is that the refinery of 0.8Mt/a is that example is simulated, and its compression rich gas amount is that 16000kg/h, raw gasline flow are 32800kg/h.Compress rich gas 1 and mix, enter surge tank 7 afterwards and carry out gas-liquid separation, and remove water 10 from the rich absorbent oil 6 of 5 bottoms, absorption tower and the stripping gas 8 at desorption tower 12 tops; The condensed oil that obtains enters the desorption tower middle and upper part as hot feed after condenser 11 is cooled to 60 ℃, and non-condensable gas carries out gas-liquid separation after being cooled to 35 ℃ once more; Its condensed oil that obtains 9 enters desorption tower 12 tops as cold feed, and non-condensable gas then enters 5 bottoms, absorption tower.5 tops enter from the absorption tower as absorption agent with raw gasline 3 to replenish absorption agent 2, for reducing the tower temperature assimilation effect are improved, and are provided with absorption tower intermediate condenser 15, and lean gas 4 is extracted out from cat head.And desorption tower 12 bottoms are provided with reboiler 13, then obtain deethanizing gasoline 14 at the bottom of the tower.This processing quality controlling index is: C in the deethanizing gasoline
2＜0.1% (v), C in the liquefied gas
5＜0.1% (v), C in the stable gasoline
4＜0.5% (wt), C in the dry gas
3 +Component concentration is 1.5% (v).
Embodiment 2: recombining process
As shown in Figure 2: desorption tower 12 middle and lower parts at stepwise condensation process are provided with intermediate reboiler 16, and it returns temperature is 100 ℃; For reducing gas desorption quantity and absorption tower load, the condensing temperature of condensed oil is reduced to 55 ℃.This example is the improvement of example 1, and except that above-mentioned improvement part, all the other technical process are as example 1.
Under same charging and product specification, present embodiment 1 and the embodiment 2 treatment effects treatment effect with conventional cold feed technology, hot feed technology, bifilar feeding process is compared, five technology comparative results are as follows: table 1 is the comparison of cooling and heating load, Fig. 3 is the character of each scheme stripping gas, and Fig. 4 is a desorption tower column plate gas phase load condition.
Table 1 cooling and heating load is (M*kJ.h relatively
-1)
Annotate :-: cooling; +: heating.
Table 1 is the comparison of cooling and heating load.The cold energy consumption of absorption-desorb part mainly comprises: cooling load and absorption tower intercooling load before the surge tank, latter's numerical value is less.The heat energy consumption comprises: desorption tower reboiler load, desorption tower intermediate reboiler load and desorption tower feeding preheating amount, wherein back two waste heats that utilize the internal system stable gasoline are not considered.
Can find out from table 1, for cooling load before the surge tank, be benchmark with the cold feed, and hot feed has increased by 12.8%, the same substantially cold feed of bifilar charging.And for fractional condensation, mixture directly enters surge tank and carries out gas-liquid separation, and then fractional condensation, after condensed oil is cooled to 60 ℃ as the desorption tower hot feed, after non-condensable gas is cooled to 35 ℃ as the desorption tower cold feed; Therefore cooling load is very little before the surge tank, has reduced 48.6% than cold feed.For the recombining process of fractional condensation and intermediate reboiler, the condensed oil cooling temperature is 55 ℃, and cooling load has reduced 39.5% than cold feed before the surge tank.The desorption tower reboiler load of recombining process is minimum, compares with the cold feed situation, has reduced 37.3%.As seen, reducing on the total energy consumption, fractional condensation and recombining process thereof have very big advantage, and hot feed, bifilar charging effect are suitable, cold feed energy consumption maximum.
Fig. 3 is the character of each technology stripping gas.With the cold feed is benchmark, and the stripping gas flow maximum of hot feed has increased by 98.6% than cold feed, and contains a large amount of C in the stripping gas
3, C
4Component has increased by 189.2%, 221.3% respectively.Bifilar charging gas desorption quantity has increased by 10.6% than cold feed, C
3, C
4Composition flow rate has then increased by 34%, 14.4% respectively.For stepwise condensation process, since most of in the charging for hot feed, more C can be caused
3, C
4Component circulates in stripping gas, C
3, C
4Composition flow rate increases to some extent; But wherein contained C
2Component reduces significantly, so gas desorption quantity has reduced 17.9%.The gas desorption quantity of recombining process has reduced 22.6%, C
3, C
4Composition flow rate has had minimizing than fractional condensation.This shows that stepwise condensation process and recombining process gas desorption quantity reduce than common process, effect is fine.
Fig. 4 is a desorption tower column plate gas phase load condition.As we can see from the figure, along with stage number increases, the tower internal loading is in rapid ascendant trend always under the cold feed situation, and load is very big, and reason is that temperature is lower in the tower, is not easy to desorb.Loading under the hot feed situation, it is milder to rise, and maximum load is also low than cold feed.For bifilar charging situation, the duty ratio hot feed of desorption tower top is little.During stepwise condensation process, because most of hot feed enters from the 6th block of plate of desorption tower, make the gas phase load sharply increase at the 7th plate place, after this, curve is almost overlapping with bifilar feed column load curve.Recombining process sharply descends in that intermediate reboiler place tower internal loading is set.To sum up can obtain, cold feed tower load is maximum, and effect is the poorest; Adopt stepwise condensation process to make that whole desorb Tata load is all very little, effect is best; It is favourable to alleviating the tower load to add intermediate reboiler.
Open stepwise condensation process for catalytic cracking absorbing-stabilizing system of the present invention and recombining process thereof, those skilled in the art can be by using for reference this paper content, and links such as appropriate change processing parameter, structure design realize.System of the present invention is described by preferred embodiment, and person skilled obviously can be changed or suitably change and combination system as herein described in not breaking away from content of the present invention, spirit and scope, realizes the technology of the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as being included in spirit of the present invention, scope and the content.
Claims (3)
1. stepwise condensation process for catalytic cracking absorbing-stabilizing system, adopt the double-column process desorption tower, it is characterized in that: directly enter surge tank after compression rich gas, rich absorbent oil and stripping gas mix and carry out gas-liquid separation, and then fractional condensation, after the condensed oil temperature reaches 55 ℃～70 ℃, as the desorption tower hot feed, after non-condensable gas is cooled to 35 ℃～40 ℃ as the desorption tower cold feed.
2. a catalytic cracking absorbing stable system composite technique adopts stepwise condensation process, it is characterized in that in the desorption tower middle and lower part of stepwise condensation process flow process intermediate reboiler being set.
3. a kind of catalytic cracking absorbing stable system composite technique as claimed in claim 2 is characterized in that, the condensed oil condensing temperature is 50 ℃～60 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100144437A CN100400624C (en) | 2005-07-07 | 2005-07-07 | Stepwise condensation process for catalytic cracking absorbing-stabilizing system and its combining process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100144437A CN100400624C (en) | 2005-07-07 | 2005-07-07 | Stepwise condensation process for catalytic cracking absorbing-stabilizing system and its combining process |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006101041911A Division CN100425673C (en) | 2005-07-07 | 2005-07-07 | Catalytic cracking absorbing stable system composite technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1710028A true CN1710028A (en) | 2005-12-21 |
| CN100400624C CN100400624C (en) | 2008-07-09 |
Family
ID=35706318
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100144437A Expired - Fee Related CN100400624C (en) | 2005-07-07 | 2005-07-07 | Stepwise condensation process for catalytic cracking absorbing-stabilizing system and its combining process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100400624C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101602960B (en) * | 2009-07-09 | 2012-06-27 | 天津大学 | Coking, absorbing and stabilizing energy-saving process |
| CN101531919B (en) * | 2009-04-21 | 2012-12-12 | 天津大学 | Energy-saving device and operation process for absorption-stabilization system |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1089264C (en) * | 1999-07-20 | 2002-08-21 | 华南理工大学 | Absorption stabilizing apparatus for catalytic cracking and its production process |
-
2005
- 2005-07-07 CN CNB2005100144437A patent/CN100400624C/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101531919B (en) * | 2009-04-21 | 2012-12-12 | 天津大学 | Energy-saving device and operation process for absorption-stabilization system |
| CN101602960B (en) * | 2009-07-09 | 2012-06-27 | 天津大学 | Coking, absorbing and stabilizing energy-saving process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100400624C (en) | 2008-07-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101659876A (en) | Method for saving energy and producing more propylene in absorption-stabilization system by catalytic cracking | |
| CN1129708C (en) | Generator of steam to generate dynamic power | |
| CN101717658B (en) | Multi-vaporization feeding method of oil product fractionator | |
| WO2016197487A1 (en) | Three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption | |
| CN101602959A (en) | Downstream separation system of catalytic cracking device improves the method for yield of liquefied gas | |
| CN1847203A (en) | Separating method for converting methanol to prepare low carbon olefin gas | |
| CN1861553A (en) | Rectifying tech. and equipment of high purity methanol | |
| CN1134748A (en) | Cryogenic separation | |
| CN102021033B (en) | Reinforced mass transfer and efficient energy-saving type absorption stabilizing system | |
| CN100344743C (en) | Method for making low-alcohol or alcohol-less raw juice fermented alcohol drink by low-temperature two-tower rectification method | |
| CN100425673C (en) | Catalytic cracking absorbing stable system composite technique | |
| CN1710028A (en) | Stepwise condensation process for catalytic cracking absorbing-stabilizing system and its combining process | |
| CN1268590C (en) | Method for separating catalytic splitting gas of enriching propylene and propane | |
| CN101531919B (en) | Energy-saving device and operation process for absorption-stabilization system | |
| CN101602960B (en) | Coking, absorbing and stabilizing energy-saving process | |
| CN1380274A (en) | Alcohol refining process for producing several products | |
| CN1974501A (en) | Parallel trimethyl benzene separating apparatus and method | |
| CN102746882A (en) | Method for separating gas products in catalytic cracking device | |
| CN2732743Y (en) | Light hydrocarbon recovering integrated device | |
| CN101723791B (en) | Method for enriching mesitylene from C9 aromatics | |
| CN112410069A (en) | Hydrorefining process for catalytic cracking crude gasoline | |
| CN1091413A (en) | Method with seperation of hydrocarbon mixture as function of extractive distillation | |
| CN204447370U (en) | The device of a kind of extracting rectifying and flash distillation integrated separation propylene and propane | |
| CN101302436B (en) | Catalytic cracking absorption stabilization system having gasoline cutting and process producing more propene and reducing alkene | |
| KR870000182B1 (en) | Constant pressure separation of normal paraffins from hydrocarbon mixtures |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080709 Termination date: 20110707 |