CN101250426A - Method for reducing propylene concentration of dry gas in catalytic cracking device absorption stabilizing system - Google Patents
Method for reducing propylene concentration of dry gas in catalytic cracking device absorption stabilizing system Download PDFInfo
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- CN101250426A CN101250426A CNA2008100267695A CN200810026769A CN101250426A CN 101250426 A CN101250426 A CN 101250426A CN A2008100267695 A CNA2008100267695 A CN A2008100267695A CN 200810026769 A CN200810026769 A CN 200810026769A CN 101250426 A CN101250426 A CN 101250426A
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Abstract
The invention discloses a method for lowering propylene concentration in dry gas of an absorption-stabilization system of a catalytic cracking unit, which achieves through improving supplement absorbent flow and heat exchanging process in the absorption-stabilization system. The method comprises the following steps: opening a lateral line on a third to a fifth theoretical plate of a stabilizer, producing light gasoline to be supplementing absorbing agent of an absorbing tower, simultaneously canceling the process of the original supplementing absorbing agent to get into the absorbing tower, increasing heat supply of a reboiler in the center of an absorption tower, or heating up deethanization gasoline with diesel oil. The method can obviously lower the concentration of propylene and propane in dry gas, which greatly improves propylene yield rate of the absorption-stabilization system of the catalytic cracking unit, and meanwhile, products are guaranteed, and energy consumption of a device is basically constant. The problem of inadequate heat load of the reboiler in the center of the absorption tower which is caused by flow process alternation is excellently solved through the optimization of the heat exchanging flow. In the whole process, flow reconstruction is simple and feasible, and economic benefit is obvious.
Description
Technical field
The invention belongs to the refining of petroleum field, particularly a kind of method that reduces density of propylene in the catalytic cracking device absorption stabilizing system dry gas.
Background technology
Propylene (C
3H
6) be one of most important basic Organic Chemicals, be the raw material of producing polypropylene, vinyl cyanide, propylene oxide, isopropyl benzene, Virahol and oxo-alcohols.It is reported that China's polypropylene overall throughput was 6,910,000 tons in 2006, increase by 1.2 times than calendar year 2001, average amplification is 16.7% in the period of 5, but still can not satisfy the demands, and 2005 and import volume in 2006 account for 34.6% of current home consumption all above 3,000,000 tons.Therefore, producing more propylene is pressing for of national economic development.
At present, China's propylene 66% is from the lighter hydrocarbons preparing ethylene by steam cracking, and 32% from refinery, and the latter shows a rising trend.And in the crude propylene, again based on the propylene of catalytic cracking unit production, output accounts for 97%.In recent years, for producing more propylene, domestic correlative study mechanism has developed the ARGG (Atmospheric Residuum Maximum LPG plusGasoline) of long residuum maximum production liquefied petroleum gas (LPG) and gasoline in succession, the deep catalytic cracking DCC (Deep Catalytic Cracking) and the flexible double lifting leg fluid catalytic cracking FDFCC new catalytic cracking technologies such as (Flexible Dual-riser Fluid Catalytic Cracking) of fecund low-molecular olefine, be used for new device construction and old plant modification in a large number, propone output is highly improved.
In the catalytic cracking process, raw material wax oil or residual oil advance reactor for about 250 ℃, under the effect of coke regenerative heat and catalyzer, are cracked into reaction oil gas, go forward side by side into main fractionating tower, are separated into rich gas, raw gasline, diesel oil and slurry oil.Wherein, diesel oil and slurry oil can go out device because quality is qualified substantially; But rich gas and raw gasline because cut cutting is insufficient, need enter absorbing-stabilizing system, under the effect of absorption agent such as diesel oil and pressure, further are separated into dry gas, liquid hydrocarbon and stable gasoline.The basal component of liquid hydrocarbon is C
3And C
4, wherein the mole of propylene is formed approximately 40%, therefore is sent to the gas separation unit in downstream, obtains volumetric molar concentration greater than 99.6% fine propylene by rectifying, with as the polyacrylic monomer of production.The main component of dry gas is C
1And C
2, mainly as the fuel of refinery processes process furnace.But, carry a certain amount of C in the dry gas usually secretly owing to reasons such as technology and operations
3And above component, promptly so-called dry gas " is not done ", and the propylene of high value is acted as a fuel and the low value use.Therefore, improve the technology of absorbing-stabilizing system, make dry gas become " doing ", be about to C in the dry gas
3Reach above component and take in as far as possible in the liquid hydrocarbon product, enter fuel gas system less, be the useful measure of catalytic cracking unit producing more propylene, significant to the economic benefit that improves whole refinery.
Summary of the invention
The objective of the invention is to overcome the shortcoming of prior art, a kind of method that reduces density of propylene in the catalytic cracking device absorption stabilizing system dry gas is provided, this method reduces the concentration of propylene in the dry gas by the improvement to the absorbing-stabilizing system technical process, and propylene yield in liquid hydrocarbon is improved.
Purpose of the present invention is achieved through the following technical solutions: a kind of method that reduces density of propylene in the catalytic cracking device absorption stabilizing system is that additional absorption agent flow process and the heat exchange process to absorbing-stabilizing system improves, and comprising:
(1) improvement of additional absorption agent flow process
Open a side line in the stabilizer tower bottom, the extraction petroleum naphtha is absorption agent as a supplement;
(2) improvement of heat exchange process
Increase Analytic Tower intermediate reboiler heat supply or heat deethanizing gasoline with diesel oil.
Being improved to additional absorption agent flow process in described (1): the 3rd～5 theoretical stage (first theoretical stage is numbered 1 at the bottom of stablizing Tata) at described stabilizer tower located out a side line, the extraction petroleum naphtha, described petroleum naphtha is after heat exchange, be cooled to 35 ℃～40 ℃, enter the top, absorption tower as replenishing absorption agent, cancel the additional absorption agent of original stable gasoline simultaneously and advance the absorption tower flow process.
Increasing the heat supply of Analytic Tower intermediate reboiler in described (2) is: other with Analytic Tower intermediate reboiler of parallel way increase at the Analytic Tower intermediate reboiler; It once is thermal source that the Analytic Tower intermediate reboiler of described increase replenishes absorption agent with described stabilizer tower bottom side line; Concrete heat exchange process is: come out at the bottom of the stable gasoline self stabilization tower, heating deethanizing gasoline is done the original intermediate reboiler thermal source of desorption tower more earlier, is cooled to suitable temp then and all goes out to reduce catalytic cracking unit; The petroleum naphtha of stabilizer tower bottom side line extraction is cooled to 35 ℃～40 ℃ again and enters absorption cat head absorption agent as a supplement earlier by newly-increased desorption tower intermediate reboiler and the backflow heat exchange of desorption tower stage casing from (1).
Heat exchange process with diesel oil heating deethanizing gasoline in described (2) is: the diesel oil of extracting out with FCC main fractionating tower once heats deethanizing gasoline, cancelled original stable gasoline heating deethanizing gasoline flow process simultaneously, promptly stable gasoline once all goes out to reduce catalytic cracking unit again by reboiler in the desorption tower and the backflow heat exchange of desorption tower stage casing after the water recirculator cooling.
Ultimate principle of the present invention is: with molecular polarity and C
3Stabilizer tower bottom petroleum naphtha substituted molecule polarity and C that propylene is close
3Propylene differs at the bottom of the bigger stable Tata stable gasoline and does the absorption tower and replenish absorption agent, to improve the assimilated efficiency on absorption tower.
Replenish in the absorbing-stabilizing system prior art to come out after the heat exchange cooling at the bottom of the absorption agent flow process comprises stable gasoline self stabilization Tata, a part goes out device as product, another part is squeezed into and is absorbed cat head absorption agent as a supplement, heat exchange process comprises heat supply of desorption tower intermediate reboiler and deethanizing gasoline heating procedure, described desorption tower intermediate reboiler heat supply stable gasoline secondary, deethanizing gasoline heats with stable gasoline once.The present invention strengthens the assimilation effect of propylene in the absorption tower by improving the additional absorption agent flow process and the heat exchange process of absorbing-stabilizing system, and the density of propylene in the downstream unit reabsorber cat head dry gas is reduced.
The present invention has following advantage and beneficial effect with respect to prior art:
1, adopt technical solution of the present invention can reduction dry gas by a relatively large margin in propylene content, reclaim the propylene of more high values, the economic benefit of lifting gear.
2, in parallel to increase by one once be the intermediate reboiler of thermal source with stabilizer tower bottom side line petroleum naphtha at Analytic Tower in the present invention, can guarantee boiling hot again load in the middle of the desorption tower, also can be used as at the bottom of the desorb Tata a kind of regulating measure in boiling hot source more simultaneously.Once heat deethanizing gasoline if adopt FCC main fractionating tower to extract diesel oil out, the temperature that can make deethanizing gasoline advance stabilizer tower raises, and then can reduce the thermal load of stabilizer tower tower bottom reboiler.
3, after the employing flow process of the present invention, C in the dry gas
4Component has increase slightly, and (the stabilizer tower side line is extracted additional absorption agent itself out and is contained portion C
4The cause of component), but the minimizing of dry gas total amount, whole C
3And above component total concn descends.
4, workflow reengineering of the present invention is simple, feasible, substantially only increases stabilizer tower bottom side line petroleum naphtha extractor pump and adjusts heat exchange process.
Description of drawings
Fig. 1 is the catalytic cracking unit fractionation of comparative example of the present invention and the technical process of absorbing-stabilizing system.
Fig. 2 is the catalytic cracking unit fractionation of the embodiment of the invention 1 and the technical process of absorbing-stabilizing system.
Fig. 3 is the catalytic cracking unit fractionation of the embodiment of the invention 2 and the technical process of absorbing-stabilizing system.
Embodiment
The present invention is described in further detail below in conjunction with embodiment and accompanying drawing, but the working of an invention mode is not limited thereto.
Comparative example (technical process of existing catalytic cracking unit fractionation flow process and absorbing-stabilizing system)
Fig. 1 is seen in the technical process of existing catalytic cracking unit fractionation and absorbing-stabilizing system.Reaction oil gas from the 142.8t/h of reaction-regeneration system enters the chevron shaped baffle plate of main fractionating tower bottom for 490 ℃, contact by the herringbone baffle plate is reverse with 275 ℃ circulation slurry oil after the heat exchange, after the part last running that is cooled (being externally extracting oil), enter rectifying section, be separated into recycle stock, diesel oil, raw gasline and rich gas.For the heat of compensation tower, main fractionating tower is provided with and refluxes in the top pump around circuit, one and the slurry oil backflow; In order to improve light receipts, be provided with stripped vapor at the bottom of the tower.
114 ℃ of the cat head oil gas, the 2.5kg/cm that come out from the main fractionating tower cat head
2Advance a minute flow container by being cooled to 40 ℃, isolate raw gasline, sewage, cold reflux and rich gas.Wherein, raw gasline enters the absorption tower, compressed, the cooling of rich gas, with from the rich absorbent oil of bottom, absorption tower and the stripping gas at desorption tower top, advance condensing oil tank through condensing to 40 ℃ again, be separated into condensed oil and non-condensable gas, condensed oil removes desorption tower, and non-condensable gas enters the absorption tower.
The working pressure on absorption tower is 1.25MPa, and the additional absorption agent of 40 ℃ raw gasline and stable gasoline is placed in top and advances tower, and tower is advanced in the non-condensable gas bottom, replenishes the absorption agent counter current contact with raw gasline, stable gasoline from bottom to top, to remove light ends fractionation wherein.In order to strengthen assimilation effect, the absorption tower also is provided with two stage casing cold refluxs, takes the absorption process rejected heat away with recirculated cooling water, to reduce the service temperature of tower.After finishing absorption, the cat head lean gas enters reabsorber, with diesel oil absorption agent counter current contact, further removes the lighter hydrocarbons of wherein carrying secretly, comes out from cat head then, goes out device as dry gas, enters refinery's gas burning system through desulfurization.At the bottom of the tower rich absorbent oil then after heat exchange 130 ℃ return main fractionating tower.
The effect of desorption tower is the C that removes in the condensed oil
2Cut is for stabilizer tower provides qualified charging.Its flow process is that condensed oil is placed in the top cold feed, under the effect of intermediate reboiler and tower bottom reboiler, obtains deethanizing gasoline at the bottom of tower, enters stabilizer tower.Stabilizer tower then under the effect of tower bottom reboiler, separates liquid hydrocarbon with stable gasoline.The top gas cools off through condensation, advances a minute flow container again, and portioned product is returned through pump and stablized cat head as cold reflux, and part goes out device as liquid hydrocarbon product, and after desulfurization, the branch that degass is produced fine propylene.The bottom obtains stable gasoline, extracts out through pump, by with the heat exchange of deethanizing gasoline, does desorption tower intermediate reboiler thermal source, and cooling, cools to 40 ℃, and part goes out device as stable gasoline, and part absorption agent is as a supplement gone to the absorption tower.
Embodiment 1
Fig. 2 is the catalytic cracking unit fractionation of present embodiment and the technical process of absorbing-stabilizing system, has done following improvement compared to the catalytic cracking unit fractionation of comparative example and the technical process present embodiment of absorbing-stabilizing system:
(1) improvement of additional absorption agent flow process
Open a side line (first theoretical stage is numbered 1 at the bottom of stablizing Tata) at the 3rd theoretical stage place of stabilizer tower, one petroleum naphtha of extraction, this petroleum naphtha is cooled to 40 ℃ through water recirculator again through newly-increased desorption tower intermediate reboiler and the backflow heat exchange of desorption tower stage casing earlier, enter the top, absorption tower and do to replenish absorption agent, cancel simultaneously and replenish absorption agent in the prior art and advance the absorption tower flow process.
(2) improvement of heat exchange process
Is the interchanger of thermal source one of the other increase in parallel of Analytic Tower intermediate reboiler with the side line petroleum naphtha, its heat exchange process is: come out once to heat deethanizing gasoline at the bottom of the stable gasoline self stabilization tower, secondary is made former desorption tower intermediate reboiler thermal source, is cooled to then go out this device about 40 ℃; The petroleum naphtha of stabilizer tower side line extraction through newly-increased desorption tower intermediate reboiler and the backflow heat exchange of desorption tower stage casing, is cooled to 40 ℃ through water recirculator earlier again from (1), squeezes into the absorption tower cat head then.
The controlled variable of all the other flow processs and Ge Ta all with above-mentioned prior art comparative example in identical.
The effect of the catalytic cracking unit fractionation of employing present embodiment and the technical process of absorbing-stabilizing system is as follows:
1, the massfraction of propylene is reduced to 3.91% (volumetric molar concentration is 1.35%) by 5.68% (volumetric molar concentration is 1.97%) in the dry gas, and the amount going along with of propylene is reduced to 231kg/h by 339kg/h in the dry gas, reduces 108kg/h.
2, the massfraction of propane is reduced to 0.77% (volumetric molar concentration is 0.25%) by 1.06% (volumetric molar concentration is 0.35%) in the dry gas, and the amount going along with of propane reduces 17.6kg/h by the near 45.5kg/h of 63.1kg/h in the dry gas.Add up to C in the dry gas
3Amount decline 125.6kg/h total going along with.
3, C in the dry gas
4The massfraction of component rises to 0.93% (volumetric molar concentration is 0.24%), C by 0.48% (volumetric molar concentration is 0.12%)
4Amount going along with rises to 55.7kg/h by 27.2kg/h, increases 28.5kg/h.
4, the dry gas total amount is reduced to 5871.6kg/h by 5971.3kg/h, reduces 99.7kg/h.The output of liquid hydrocarbon rises to 19151kg/h by 19057kg/h, improves 94kg/h.
5, it is constant substantially that stable gasoline goes out the output and the quality of device.Output is respectively 41294kg/h and 41304kg/h before and after the process modification, and doing all is 193 ℃.
6, the energy consumption of stabilizer tower and desorption tower is constant substantially.The thermal load of former stable tower bottom reboiler, desorb tower bottom reboiler and desorption tower intermediate reboiler is respectively 586 * 10
4Kcal/h, 279 * 10
4Kcal/h and 233 * 10
4Kcal/h; After the improvement, they are respectively 605 * 10
4Kcal/h, 278 * 10
4Kcal/h and 237 * 10
4Kcal/h.
Embodiment 2
Fig. 3 is the catalytic cracking unit fractionation of present embodiment and the process flow sheet of absorbing-stabilizing system.The difference of present embodiment and embodiment 1 is the improvement of heat exchange process, and is specific as follows:
(2) improvement of heat exchange process
With diesel oil heating deethanizing gasoline, its heat exchange process is: the diesel oil of extracting out with FCC main fractionating tower once heats deethanizing gasoline, cancel simultaneously stable gasoline heating deethanizing gasoline flow process (be stable gasoline earlier in desorption tower reboiler after the recirculated water cooling, all go out device again with the backflow heat exchange of desorption tower stage casing) side line replenishes absorption agent and once is recycled water cooling to 40 again with the low-temperature water heating heat exchange and ℃ squeezes into and to absorb cat head and make additional absorption agent.
1, the mass concentration of propylene is reduced to 4% (volumetric molar concentration is 1.37%) by 5.68% (volumetric molar concentration is 1.97%) in the dry gas, and the amount going along with of propylene is reduced to 234kg/h by 339kg/h in the dry gas, reduces 105kg/h.
2, the mass concentration of propane is reduced to 0.78% (volumetric molar concentration is 0.26%) by 1.06% (volumetric molar concentration is 0.35%) in the dry gas, and the amount going along with of propane reduces 17.1kg/h by the near 46kg/h of 63.1kg/h in the dry gas.Add up to C in the dry gas
3Amount decline 122.1kg/h total going along with.
3, C in the dry gas
4The mass concentration of component rises to 0.93% (volumetric molar concentration is 0.24%), C by 0.48% (volumetric molar concentration is 0.12%)
4Amount going along with rises to 55.7kg/h by 27.2kg/h, increases 28.5kg/h.
4, the dry gas total amount is reduced to 5881kg/h by 5971.3kg/h, reduces 90.3kg/h.The output of liquid hydrocarbon rises to 19148kg/h by 19057kg/h, improves 91kg/h.
5, it is constant substantially that stable gasoline goes out the output and the quality of device.Output is respectively 41294kg/h and 41308kg/h before and after the process modification, and doing all is 193 ℃.
6, the energy consumption of stabilizer tower and desorption tower is constant substantially.The thermal load of former stable tower bottom reboiler, desorb tower bottom reboiler and desorption tower intermediate reboiler is respectively 586 * 10
4Kcal/h, 279 * 10
4Kcal/h and 233 * 10
4Kcal/h; Thermal load is respectively 544 * 10 after the process modification
4Kcal/h, 278 * 10
4Kcal/h and 237 * 10
4Kcal/h.
To sum up, C in the embodiment of the invention 1 and embodiment 2 dry gas
3And above concentration of component all reduces the minimizing of dry gas total amount, propene yield raising, and the C that reclaims
3The component overwhelming majority enters in the liquid hydrocarbon, and product is guaranteed simultaneously, and plant energy consumption is constant substantially.Workflow reengineering is simple, feasible, and economic benefit is very obvious.
Embodiment 3
The difference of present embodiment and embodiment 1 is that extraction position that side line replenishes absorption agent changes the 5th theoretical stage and side line into by the 3rd theoretical stage and replenishes the temperature that absorption agent enters the absorption tower and change 35 ℃ into by 40 ℃, and all the other flow processs are all identical.The present embodiment effect is substantially the same manner as Example 1.
The foregoing description is a preferred implementation of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other any do not deviate from change, the modification done under spirit of the present invention and the principle, substitutes, combination, simplify; all should be the substitute mode of equivalence, be included within protection scope of the present invention.
Claims (6)
1, a kind of method that reduces density of propylene in the catalytic cracking device absorption stabilizing system dry gas is that additional absorption agent flow process and the heat exchange process to absorbing-stabilizing system improves, and comprising:
(1) improvement of additional absorption agent flow process
Open a side line in the stabilizer tower bottom, the extraction petroleum naphtha is absorption agent as a supplement;
(2) improvement of heat exchange process
Increase Analytic Tower intermediate reboiler heat supply or heat deethanizing gasoline with diesel oil.
2, a kind of method that reduces density of propylene in the catalytic cracking device absorption stabilizing system dry gas according to claim 1, it is characterized in that: being improved to additional absorption agent flow process in described (1): be numbered 1 in first theoretical stage at the bottom of the described stable Tata, the 3rd～5 theoretical stage place opens a side line at described stabilizer tower, the extraction petroleum naphtha, described petroleum naphtha is after heat exchange, be cooled to 35 ℃～40 ℃, enter the top, absorption tower as replenishing absorption agent, cancel the additional absorption agent of original stable gasoline simultaneously and advance the absorption tower flow process.
3, a kind of method that reduces density of propylene in the catalytic cracking device absorption stabilizing system dry gas according to claim 1, it is characterized in that: increase the heat supply of Analytic Tower intermediate reboiler in described (2) and be meant, other at described Analytic Tower intermediate reboiler with Analytic Tower intermediate reboiler of parallel way increase.
4, a kind of method that reduces density of propylene in the catalytic cracking device absorption stabilizing system dry gas according to claim 3 is characterized in that: it once is thermal source that the Analytic Tower intermediate reboiler of described increase replenishes absorption agent with described stabilizer tower bottom side line.
5, a kind of method that reduces density of propylene in the catalytic cracking device absorption stabilizing system dry gas according to claim 1, it is characterized in that: the heat exchange process in described (2) after the heat supply of increase Analytic Tower intermediate reboiler is: come out at the bottom of the stable gasoline self stabilization tower, heat deethanizing gasoline earlier, do the original intermediate reboiler thermal source of desorption tower again, be cooled to suitable temp then and all go out to reduce catalytic cracking unit; The petroleum naphtha of stabilizer tower bottom side line extraction is cooled to 35 ℃～40 ℃ again and enters absorption cat head absorption agent as a supplement earlier by newly-increased desorption tower intermediate reboiler and the backflow heat exchange of desorption tower stage casing from (1).
6, a kind of method that reduces density of propylene in the catalytic cracking device absorption stabilizing system dry gas according to claim 1, it is characterized in that: the heat exchange process with diesel oil heating deethanizing gasoline in described (2) is: the diesel oil of extracting out with FCC main fractionating tower once heats deethanizing gasoline, cancelled original stable gasoline heating deethanizing gasoline flow process simultaneously, promptly stable gasoline once all goes out to reduce catalytic cracking unit again by reboiler in the desorption tower and the backflow heat exchange of desorption tower stage casing after the water recirculator cooling.
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Cited By (7)
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| CN101906318A (en) * | 2010-07-30 | 2010-12-08 | 华南理工大学 | Method and device for upgraded recycle of energy of raffinate tower and extract tower |
| CN103254931A (en) * | 2013-04-12 | 2013-08-21 | 华南理工大学 | Absorption and stabilization system and method for realizing pressure reduction of desorber |
| CN104593057A (en) * | 2015-01-27 | 2015-05-06 | 华南理工大学 | Low-energy-consumption delayed coking device |
| CN104910951A (en) * | 2015-05-26 | 2015-09-16 | 成都高普石油工程技术有限公司 | Catalytic cracking unit of rich gas and crude gasoline |
| CN106433771A (en) * | 2016-10-26 | 2017-02-22 | 华南理工大学 | Low-energy-consumption catalytic cracking and catalytic gasoline selective hydrogenation combined process |
| CN107216913A (en) * | 2017-07-10 | 2017-09-29 | 中山大学 | A kind of catalytic cracking Vapor recovery unit method and its device |
| CN107227172A (en) * | 2017-07-11 | 2017-10-03 | 华南理工大学 | A kind of method for reducing absorbing-stabilizing system power consumption |
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2008
- 2008-03-13 CN CN2008100267695A patent/CN101250426B/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101906318A (en) * | 2010-07-30 | 2010-12-08 | 华南理工大学 | Method and device for upgraded recycle of energy of raffinate tower and extract tower |
| CN103254931A (en) * | 2013-04-12 | 2013-08-21 | 华南理工大学 | Absorption and stabilization system and method for realizing pressure reduction of desorber |
| CN103254931B (en) * | 2013-04-12 | 2015-08-26 | 华南理工大学 | Absorbing-stabilizing system and realize the method for desorption tower reduced pressure operation |
| CN104593057A (en) * | 2015-01-27 | 2015-05-06 | 华南理工大学 | Low-energy-consumption delayed coking device |
| CN104910951A (en) * | 2015-05-26 | 2015-09-16 | 成都高普石油工程技术有限公司 | Catalytic cracking unit of rich gas and crude gasoline |
| CN106433771A (en) * | 2016-10-26 | 2017-02-22 | 华南理工大学 | Low-energy-consumption catalytic cracking and catalytic gasoline selective hydrogenation combined process |
| CN106433771B (en) * | 2016-10-26 | 2018-04-13 | 华南理工大学 | A kind of catalytic cracking of low energy consumption and catalytic gasoline selective hydrogenation process integration |
| CN107216913A (en) * | 2017-07-10 | 2017-09-29 | 中山大学 | A kind of catalytic cracking Vapor recovery unit method and its device |
| CN107227172A (en) * | 2017-07-11 | 2017-10-03 | 华南理工大学 | A kind of method for reducing absorbing-stabilizing system power consumption |
| CN107227172B (en) * | 2017-07-11 | 2019-05-14 | 华南理工大学 | A method of reducing absorbing-stabilizing system energy consumption |
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