CN105733676B - A kind of energy-saving absorption stabilizing process and system - Google Patents
A kind of energy-saving absorption stabilizing process and system Download PDFInfo
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Abstract
The present invention relates to a kind of energy-saving absorption stabilizing process and system, the technique is the rich absorbing liquid mixing of compression rich gas, the stripping gas and absorbing tower bottom that desorb column overhead from rich gas compressor and enters vapor-liquid separation tank after condensing；Isolated liquid phase enters desorber, and desorber materials at bottom of tower enters stabilizer, obtains liquefied gas and stable gasoline after separation；Isolated gas phase enters absorption tower, it is reacted with first order absorption agent counter current contacting, the lean gas gone out from absorption tower top row reacts in second level absorbing reaction device with second level absorbent, reacting obtained gas phase is dry gas, liquid phase rich absorbent oil enters the regeneration that desorption reaction device realizes second level absorbent, second level absorbent part outlet or return second level absorbing reaction device after regeneration, the gas phase of desorption reaction device discharge return to rich gas compressor through vacuum pump.Present invention process eliminates this interior circulation of the supplement stable gasoline absorbent of former absorbing-stabilizing system, so that the energy consumption of system is greatly reduced.
Description
Technical field
The present invention relates to the devices such as petroleum refining industry, especially catalytic cracking, delayed coking absorption stabilizing process be
System.
Background technique
Absorbing-stabilizing system is the last handling process of catalytic cracking unit and delayed coking unit in petroleum refining industry,
Purpose be using absorb and principles of rectification by fractionator overhead catch pot rich gas and raw gasoline be divided into dry gas (C2With
Under), liquefied gas (C3、C4) and vapour pressure qualification stable gasoline.The device and process optimization of absorbing-stabilizing system are to catalysis
The energy efficiency of cracking and delayed coking unit plays a very important role.
There are four towers altogether in the absorbing-stabilizing system process generallyd use at present, it may be assumed that absorption tower, desorber, reabsorber
And stabilizer, typical process flow are as shown in Fig. 1: the rich oil 6 at absorption tower bottom is exported with from rich gas compressor
The mixing of stripping gas 7 that is ejected of compression rich gas 5 and desorber and will cooler 19 it is cooling after enter knockout drum 9, point
Enter desorber 3 after pump pressurization from obtained liquid phase, desorber tower bottom deethanization gasoline elder generation and stable gasoline are through heat exchanger 20
Stable gasoline and liquefied gas 10 are isolated through stabilizer in the middle part that stabilizer 4 is entered back into after heat exchange；Stabilizer tower bottom obtains steady
Determine gasoline to be allocated as going out device for product 12 by the heat exchange of heat exchanger 20,21 rear portion, partially stablizes vapour as supplement absorbent 11(
Oil) into the top on absorption tower 1, raw gasoline 14 enters the 4th block of plate on absorption tower 1 as absorbent, and absorption tower is equipped in 2
It is anti-to carry out counter current contacting with the gas phase 8 from knockout drum to take the heat of absorption process releasing away for section water cooler 17,18
It answers, the lean gas of absorption tower Base top contact is directly entered the lower part of reabsorber 2, with the diesel oil 15 from fractionating column in reabsorber
It reacts, further absorbs the heavy constituent carried secretly in lean gas, rich absorbent oil 16 returns to main fractionating tower.Dry gas 13 is from reabsorber
Top row, which goes out, is incorporated to gas pipe network.
It is gradually expanded recently as the fast development of low carbon chemical and civil liquefied gas demand, improves dry gas and liquefaction
The separation accuracy of gas improves liquefied gas yield, has become the important means that refinery promotes economic benefit, in addition with section
The increasingly increase of energy emission reduction, how to reduce production energy consumption also becomes focus of attention.Refinery's absorbing-stabilizing system is general at present
It is mainly shown as all over existing common problem:Dry gas is not done, and carries a large amount of liquefied gas in dry gas secretly, and the Gas content that liquefies is 3%
More than (v), cause the liquefied gas of a large amount of high added values that fuel is taken as directly to burn to cause the huge waste of resource；It inhales
It is undesirable to receive tower assimilation effect, in order to reduce the liquefied gas concentration in dry gas, and (vapour must be stablized by increasing supplement absorbent
Oil) internal circulating load improves assimilation effect, and the increase of supplement absorbent internal circulating load do not only result in the increasing of desorber and stabilizer energy consumption
Add, also creates the decline of system actual treatment ability.
Although disclosing the patent much about absorbing-stabilizing system in recent years, such as patent 200910068555.9,
200910069667.6,201110000183.3 and 200410083887.1 etc., but the process program and biography of these patents proposition
System technique does not have essential distinction, requires to recycle in reservation supplement stable gasoline to guarantee the liquefaction Gas content in dry gas, these
The process characteristic of scheme, which determines, guarantees that this can not solve contradiction to dry gas mass dryness fraction simultaneously with system energy consumption is reduced.
Summary of the invention
It is an object of the invention to overcome deficiency existing for prior art, provides a kind of Vapor recovery unit new process and be
System, while liquefied gas concentration is greatly reduced in making dry gas, is greatly reduced system energy consumption.
China's diesel oil boiling range range is at 180 DEG C ~ 360 DEG C at present, and gasoline end point is 205 DEG C, therefore there are press from both sides in diesel oil
The problem of with certain petrol, since catalytic diesel oil value is lower, and catalytic gasoline value is higher, therefore the catalysis bavin of low value
The gasoline of entrainment portions high quality undoubtedly will cause certain economic loss in oil.Diesel oil is to pass through fractionation in catalytic unit at present
What the side take-off of tower obtained, raw gasoline produces at the top of the fractionating column, current this separation process can not be achieved gasoline and
The clear cutting of diesel oil.
Existing absorption stabilizing process and system are both provided with circulation in supplement stable gasoline, in order to guarantee the dry of dry gas
Degree, it is also necessary to be absorbed using diesel oil supplement, diesel oil rich absorbent oil returns again in the middle part of fractionating column, realizes bavin using the heat of fractionating column
The separation of oil and lighter hydrocarbons.Since by the thermally equilibrated limitation of fractionating column, the amount of diesel oil absorbent again cannot be too big, so can not pass through
Diesel oil absorbed dose is increased to recycle to cancel in stable gasoline.
The present invention provides a kind of energy-saving absorption stabilizing process, and the technique includes the following contents: coming from rich gas compressor
Compression rich gas, the stripping gas and absorbing tower bottom that desorb column overhead the mixing of rich absorbing liquid and enter vapour-liquid after condensation is cooling
Knockout drum；After vapor-liquid separation tank separates, isolated liquid phase enters desorber, desorption column overhead row from the top of desorber
Stripping gas out returns to vapor-liquid separation tank after cooling, and desorber materials at bottom of tower enters stabilizer, obtained after separation liquefied gas and
Stable gasoline；The isolated gas phase of vapor-liquid separation tank enters the lower part on absorption tower, inhales with the level-one entered from absorption tower top
The reaction of agent counter current contacting is received, the rich absorbing liquid after reaction enters knockout drum after cooling, the lean gas gone out from absorption tower top row
Haptoreaction, the gas phase reacted are dry gas in second level absorbing reaction device with second level absorbent, and liquid phase rich absorbent oil is through adding
Enter the regeneration that desorption reaction device realizes second level absorbent, the second level absorbent part outlet after regeneration, partially through cooling after heat
Second level absorbing reaction device is returned afterwards, and the gas phase of desorption reaction device discharge returns to rich gas compressor entrance through vacuum pump.
In absorption stabilizing process of the present invention, the stripping gas of compression rich gas, desorption column overhead from rich gas compressor and suction
The rich absorbing liquid for receiving tower tower bottom mixes and after level-one condensation is cooling, and temperature of charge is 25~50 DEG C, preferably 35~40 DEG C.
In absorption stabilizing process of the present invention, the vapor-liquid separation tank temperature is 20~50 DEG C, preferably 35~40 DEG C, is operated
Pressure is 1~2 Mpa, preferably 1.2~1.5 Mpa.
In absorption stabilizing process of the present invention, the absorption tower tower top temperature is 40~45 DEG C, absorbs midsection setting 1~3
A intercooler is maintained at the temperature on absorption tower between 30~50 DEG C.
In absorption stabilizing process of the present invention, the first order absorption agent on the absorption tower is raw gasoline, is typically from fractionation
Column overhead.
In absorption stabilizing process of the present invention, the second level absorbent of the second level absorbing reaction device is to adopt from fractionating column side line
Diesel oil out, boiling range are 180 ~ 360 DEG C, and temperature is 30~50 DEG C.
In absorption stabilizing process of the present invention, the second level absorbing reaction device can be cyclone, high-gravity rotating bed reaction
Device or absorption tower, preferably rotating packed bed reactor.It is 30 that the operating condition of the second level absorbing reaction device, which is temperature,
~50 DEG C, liquid-gas ratio (absorbent and lean gas mass ratio) is 5~40, and operating pressure is 1.0 ~ 1.5Mpa.
In absorption stabilizing process of the present invention, the desorption reaction device can for cyclone, rotating packed bed reactor or
Person's flash tank, preferably rotating packed bed reactor.The rich absorbent oil temperature after heating be 50~100 DEG C, preferably 60
~70 DEG C, desorption reaction device is vacuumizing, and operating pressure is 5~50 Kpa, preferably 15~20 Kpa.
In absorption stabilizing process of the present invention, the second level absorbent after the regeneration is to eliminate the diesel oil gently held, at the beginning of
It evaporates and is a little greater than 200 DEG C, preferably greater than 205 DEG C, temperature is 30~50 DEG C after cooling.
The present invention also provides a kind of energy-saving absorbing-stabilizing system, the system comprises rich gas compressor, knockout drum,
Absorption tower, desorber, stabilizer, second level absorbing reaction device, desorption reaction device, vacuum pump；Rich gas compressor outlet, absorbing tower
Bottom liquid-phase outlet, desorber tower top outlet are connect through condenser with knockout drum respectively, and knockout drum liquid-phase outlet is through pipe
Line is connect with desorber, and desorber liquid-phase outlet is connect with stabilizer；Knockout drum gaseous phase outlet is connect with absorption tower lower part,
Absorption tower tower top outlet is connect through pipeline with second level absorbing reaction device, and second level absorbing reaction device liquid-phase outlet is through heat exchanger and desorption
Reactor connection, desorption reaction device liquid-phase outlet divide two-way, wherein the second level all the way through cooler and second level absorbing reaction device is inhaled
The connection of agent entrance is received, another way is connect with product storage tank, and desorption reaction device gaseous phase outlet is through vacuum pump and rich gas compressor entrance
Connection.
In absorbing-stabilizing system of the present invention, the second level absorbing reaction device can be cyclone, high-gravity rotating bed reaction
Device or absorption tower, preferably rotating packed bed reactor.
In absorbing-stabilizing system of the present invention, the desorption reaction device can for cyclone, rotating packed bed reactor or
Person's flash tank, preferably rotating packed bed reactor.
In absorbing-stabilizing system of the present invention, absorbs midsection and be equipped with 1~3 intercooler.
In absorbing-stabilizing system of the present invention, the prior art is can be used in the high-gravity rotating bed absorption, stripping apparatus
Middle various types are high-gravity rotating bed, and high-gravity rotating bed scale and shape can be determined according to the scale and operating condition of device
Formula can specifically include parallel type, reverse-flow and cross-current type, and preferentially select reverse-flow high-gravity rotating bed.
The present invention uses the high-gravity rotating bed absorption equipment as absorbing-stabilizing system, and hypergravity absorption equipment, which utilizes, to be turned
The hypergravity effect that son rotation generates, liquid is stretched or is torn, generate the huge area that is in contact, greatly improve mass transfer
Velocity coefficient, compared to traditional filler or tower tray, 1 ~ 3 order of magnitude is can be improved in mass tranfer coefficient, so that absorption process is theoretical
Grade greatly improves, and substantially increases diesel oil absorbent to the assimilation effect of liquefied gas.The present invention makes full use of high-gravity rotating bed
The strong feature of devolatilization function, is used for the desorption process of second level absorbent, substantially increases desorption efficiency and degree of desorption, mention
The high quality of absorbent regeneration, and energy consumption is greatly reduced.
The present invention establishes the proprietary re-absorption circulatory system, eliminates former Vapor recovery unit by using efficient mass transfer equipment
The supplement stable gasoline absorbent of system circulation in this, so that the energy consumption of system is greatly reduced, and liquid in the product that makes to bring about the desired sensation
Change gas entrainment rate and is reduced to 1% (v) hereinafter, substantially increase the economic benefit of device, it, can be in addition for old device
Greatly improve device processing capacity.
The present invention cleverly utilizes the devolatilization function of overweight revolving bed, eliminates the gasoline fraction in diesel oil, realizes bavin
The clear cutting of oil and gasoline, has achieved the purpose that increasing gasoline yield, has significantly increased device economic benefit.And it is revolved with hypergravity
Rotated bed as absorption equipment, the tower of solving over due to diesel oil absorbent easily foams caused by sudden liquid flooding rush tower and ask
Topic has ensured that device long period is safely operated.
Detailed description of the invention
Fig. 1 is conventional absorption systems stabilisation process flow chart.
Fig. 2 is absorbing-stabilizing system process flow chart of the present invention.
Specific embodiment
The present invention provides a kind of energy-saving absorbing-stabilizing system, and in conjunction with Fig. 2, the system comprises rich gas compressors 24, gas
Liquid knockout drum 9, absorption tower 2, desorber 11, stabilizer 25, second level absorbing reaction device 16, desorption reaction device 20, vacuum pump 23；It is rich
The outlet of air compressor 24,2 tower bottom liquid-phase outlet of absorption tower, 11 tower top outlet of desorber are respectively through condenser 7 and knockout drum 9
Connection, 9 liquid-phase outlet of knockout drum are connect through pipeline with desorber 11, and 11 liquid-phase outlet of desorber is connect with stabilizer 25；
9 gaseous phase outlet of knockout drum is connect with 2 lower part of absorption tower, and 2 tower top outlet of absorption tower is through pipeline and second level absorbing reaction device 16
Connection, 16 liquid-phase outlet of second level absorbing reaction device are connect through heat exchanger 26 with desorption reaction device 20, and 20 liquid phase of desorption reaction device goes out
Mouth divides two-way, wherein 19 connecting all the way through cooler 25 with the second level absorbent entrance of second level absorbing reaction device 16, another way 27
Product storage tank is removed through pipeline, desorption reaction device gaseous phase outlet is connect through vacuum pump with 23 entrance of rich gas compressor.
In conjunction with Fig. 2, the rich gas 3 from fractionating column is through rich gas pressure to be further illustrated to absorption stabilizing process process of the present invention
It mixes and after the pressurization of contracting machine 24, with the rich absorbing liquid 5 of 2 tower bottom of the stripping gas 6 of 11 tower top of desorber and absorption tower through cooler 7 one
Enter vapor-liquid separation tank 9 after grade condensation is cooling；After vapor-liquid separation tank separates, isolated liquid phase 10 is from the top of desorber
Into desorber 11, the stripping gas 6 of 11 tower top of desorber discharge returns to vapor-liquid separation tank 9,11 bottoms of desorber after cooling
Material 12 enters stabilizer 25, and liquefied gas 14 and stable gasoline 13 are obtained after separation；The isolated gas phase 4 of vapor-liquid separation tank 9 into
The lower part for entering absorption tower 2 is reacted, the absorption tower with 1 counter current contacting of first order absorption agent raw gasoline entered from 2 top of absorption tower
Level-one interconderser 8 is arranged in middle section, and the rich absorbing liquid 5 after reaction is through the cooling laggard knockout drum 9 of cooler 7, from absorption
The lean gas 15 and second level absorbent (mixture of diesel oil 22 and partial regeneration absorbent from fractionating column) that 2 top row of tower goes out are two
Haptoreaction in grade absorbing reaction device 16, the gas phase reacted are dry gas 17, and liquid phase rich absorbent oil 18 heats up through heat exchanger 26
Enter the regeneration that desorption reaction device 20 realizes second level absorbent afterwards, the second level absorbent after regeneration can divide two-way, wherein all the way
27 outlets, another way 19 are recycled back to second level absorbing reaction device 16, the gas phase 21 of desorption reaction device discharge after cooler 25 is cooling
Rich gas compressor entrance is returned through vacuum pump 23.
The following examples will be further described method provided by the invention, but the present invention not therefore and by appoint
What is limited.
Embodiment 1
By taking the absorbing-stabilizing system of certain domestic 500,000 tons/year of catalytic cracking unit as an example, using ASPEN PLUS process mould
Quasi- software respectively simulates present invention process and traditional handicraft:
It is as follows using present invention process key process parameter: 1.4 MPa of compressor delivery pressure, vapor-liquid separation tank operation temperature
35 DEG C of degree, 35 DEG C of desorber liquid phase feeding temperature, absorption tower are arranged an intermediate reboiler and return 35 DEG C of tower temperature degree, desorber
Tower bottom de-oiling ethane content 0.1%w, stabilizer determine reflux ratio 2.2,20 t/h of internal circulating load in diesel oil, diesel regenerated initial boiling point 205
DEG C, 13.2 t/h of catalytic diesel oil inlet amount desorbs 15 KPa of bed vacuum degree, 2.5 t/h of dry gas yield, 14 t/ of liquefied gas yield
H, 28 t/h of stable gasoline yield.
Comparative example 1
Using conventional process flow described in Fig. 1, however it remains circulation and diesel oil resorption process in stable gasoline are stablized
30 t/h of internal circulating load in gasoline, 11 t/h of reabsorber diesel feed amount.
Energy consumption comparison result such as table 1.
1 energy consumption of table compares
| Project | Traditional handicraft | Present invention process |
| Desorption tower reboiler | 2543 KW | 1798 KW |
| Stabilizer reboiler | 4933 KW | 2755 KW |
| Supplement gasoline absorbent internal circulating load | 30 t/h | 0 t/h |
| Absorb agent flux | 10 t/h | 30 t/h |
| Vacuum pump energy consumption | - | 100 KW |
| Energy consumption of compressor | - | Increase by 80 KW |
| C in dry gas3 +Content (V%) | 2.8% | 1.0% |
As can be seen from Table 1: using present invention process, C in dry gas can be made3 +Content significantly reduces, and system energy consumption is big
Width reduces.In addition show can 0.4 t/h of increasing gasoline yield using present invention process for calculated result.
Claims (14)
1. a kind of energy-saving absorption stabilizing process, the technique includes the following contents: compression rich gas, solution from rich gas compressor
It inhales the stripping gas of column overhead and the rich absorbing liquid mixing at absorbing tower bottom and enters vapor-liquid separation tank after condensation is cooling；Through vapour-liquid
After knockout drum separation, isolated liquid phase enters desorber, the stripping gas warp of desorption column overhead discharge from the top of desorber
Vapor-liquid separation tank is returned to after cooling, desorber materials at bottom of tower enters stabilizer, obtains liquefied gas and stable gasoline after separation；Vapour-liquid
The isolated gas phase of knockout drum enters the lower part on absorption tower, anti-with the first order absorption agent counter current contacting that enters from absorption tower top
It answers, the rich absorbing liquid after reaction enters knockout drum after cooling, and the lean gas and second level absorbent gone out from absorption tower top row exists
Haptoreaction in second level absorbing reaction device, the gas phase reacted are dry gas, and it is anti-to enter desorption after liquid phase rich absorbent oil is heated
Device is answered to realize the regeneration of second level absorbent, the second level absorbent part outlet after regeneration, part returns to second level after cooling and absorbs
The gas phase of reactor, the discharge of desorption reaction device returns to rich gas compressor entrance through vacuum pump；The first order absorption on the absorption tower
Agent is raw gasoline, and the second level absorbent of the second level absorbing reaction device is diesel oil, and the second level absorbing reaction device is hypergravity
Rotary drill reactor, the desorption reaction device are rotating packed bed reactor.
2. technique described in accordance with the claim 1, it is characterised in that: compression rich gas, desorption column overhead from rich gas compressor
Stripping gas and absorbing tower bottom the mixing of rich absorbing liquid and after level-one condensation is cooling, temperature of charge is 25~50 DEG C.
3. technique according to claim 2, it is characterised in that: compression rich gas, desorption column overhead from rich gas compressor
Stripping gas and absorbing tower bottom the mixing of rich absorbing liquid and after level-one condensation is cooling, temperature of charge is 35~40 DEG C.
4. technique described in accordance with the claim 1, it is characterised in that: the vapor-liquid separation tank temperature is 20~50 DEG C, operation pressure
Power is 1~2 Mpa.
5. technique according to claim 4, it is characterised in that: the vapor-liquid separation tank temperature is 35~40 DEG C, operation pressure
Power is 1.2~1.5 Mpa.
6. technique described in accordance with the claim 1, it is characterised in that: the absorption tower tower top temperature is 40~45 DEG C, absorption tower
1~3 intercooler is arranged in middle section, is maintained at the temperature on absorption tower between 30~50 DEG C.
7. technique described in accordance with the claim 1, it is characterised in that: the second level absorbent of the second level absorbing reaction device be from
The diesel oil of fractionating column side take-off, boiling range are 180 ~ 360 DEG C, and temperature is 30~50 DEG C.
8. technique described in accordance with the claim 1, it is characterised in that: the operating condition of the second level absorbing reaction device is that temperature is
30~50 DEG C, liquid-gas ratio is 5~40, and operating pressure is 1.0 ~ 1.5Mpa.
9. technique described in accordance with the claim 1, it is characterised in that: the rich absorbent oil temperature after heating is 50~100 DEG C.
10. technique according to claim 9, it is characterised in that: the rich absorbent oil temperature after heating is 60~70 DEG C.
11. technique described in accordance with the claim 1, it is characterised in that: the desorption reaction device is vacuumizing, and operating pressure is
5~50 Kpa.
12. technique according to claim 11, it is characterised in that: the desorption reaction device is vacuumizing, operating pressure
For 15~20 Kpa.
13. using the energy-saving absorbing-stabilizing system of absorption stabilizing process described in any claim in claim 1 to 12,
The system comprises rich gas compressor, knockout drum, absorption tower, desorber, stabilizer, second level absorbing reaction device, desorption are anti-
Answer device, vacuum pump；Rich gas compressor outlet, absorbing tower bottom liquid-phase outlet, desorber tower top outlet are respectively through condenser and gas
The connection of liquid knockout drum, knockout drum liquid-phase outlet are connect through pipeline with desorber, and desorber liquid-phase outlet is connect with stabilizer；
Knockout drum gaseous phase outlet is connect with absorption tower lower part, and absorption tower tower top outlet is connect through pipeline with second level absorbing reaction device,
Second level absorbing reaction device liquid-phase outlet is connect through heat exchanger with desorption reaction device, and desorption reaction device liquid-phase outlet is through cooler and two
The second level absorbent entrance connection of grade absorbing reaction device, desorption reaction device gaseous phase outlet connect through vacuum pump and rich gas compressor entrance
It connects.
14. system according to claim 13, it is characterised in that: absorb midsection and be equipped with 1~3 intercooler.
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| CN105733663B (en) * | 2014-12-06 | 2017-12-22 | 中国石油化工股份有限公司 | A kind of absorption stabilizing process and system |
| CN115999314A (en) * | 2021-10-21 | 2023-04-25 | 中国石油化工股份有限公司 | Internal heat integration type absorption stabilization process |
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| EP0023745B1 (en) * | 1977-12-01 | 1985-05-08 | Imperial Chemical Industries Plc | Process and apparatus for effecting mass transfer |
| CN101659876A (en) * | 2008-08-29 | 2010-03-03 | 中国石油天然气股份有限公司 | Method for saving energy and increasing yield of propylene by catalytic cracking absorption stabilization system |
| CN102021033A (en) * | 2011-01-04 | 2011-04-20 | 中山大学 | Reinforced mass transfer and efficient energy-saving type absorption stabilizing system |
-
2014
- 2014-12-06 CN CN201410732095.6A patent/CN105733676B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0023745B1 (en) * | 1977-12-01 | 1985-05-08 | Imperial Chemical Industries Plc | Process and apparatus for effecting mass transfer |
| CN101659876A (en) * | 2008-08-29 | 2010-03-03 | 中国石油天然气股份有限公司 | Method for saving energy and increasing yield of propylene by catalytic cracking absorption stabilization system |
| CN102021033A (en) * | 2011-01-04 | 2011-04-20 | 中山大学 | Reinforced mass transfer and efficient energy-saving type absorption stabilizing system |
Non-Patent Citations (1)
| Title |
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| 旋流器用于气体吸收的试验研究;曹仲文等;《环境工程学报》;20070417;第1卷(第2期);第102-104页 |
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