CN101503631A - Catalytic cracking fractionating tower oil gas energy-saving apparatus and operation technique - Google Patents
Catalytic cracking fractionating tower oil gas energy-saving apparatus and operation technique Download PDFInfo
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Abstract
The invention relates to an oil-gas energy-saving device for a catalytic cracking fractionating tower and operation technology. The tower top of the fractionating tower is provided with a plurality of stages of compression systems. Each stage of compression system comprises a gas compressor, a heat exchanger and a gas-liquid separating tank; oil-gas current of each stage of compression system is compressed by the gas compressor to raise the temperature, then enters the heat exchanger for cooling and recovering low-temperature heat, and then enters the gas-liquid separating tank to finish the gas-liquid separation operation; and the downstream of each stage of compression system is provided with a public low-pressure desorption tank, outlet liquid of the gas-liquid separating tank of each stage of compression system enters the public low-pressure desorption tank for low-pressure desorption operation, and an outlet gas phase flows into an inlet of the first-stage gas compressor. The device has the advantages that the device can produce a large amount of byproduct low-pressure steam which can be taken as a low-temperature heat source of a catalytic cracker and other devices under the condition that a gas compressor system consumes partial power excessively, fully recover a large amount of latent heat of condensation and sensible heat of cooling of oil and gas at the tower top of a main fractioning tower, greatly reduce the consumption of public engineering such as cooling water at the same time, and has remarkable energy-saving effect.
Description
Technical field
The present invention relates to petroleum refining process, especially catalytic cracking fractionating tower oil gas energy-saving apparatus and operating procedure.
Background technology
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.The main task of catalytic cracking unit fractionating system is that the gas-oil mixture that reactor is sent here is divided into cuts such as rich gas, raw gasline, solar oil, heavy gas oil, recycle stock and slurry oil by boiling spread, and guarantees that the quality of each cut meets the requirements prescribed.In addition, also to be preheating to higher temperature to stock oil or other cryogenic medias, and reclaim heat etc. with vapour generator with reflux heat and cut waste heat.The energy consumption of catalytic cracking unit fractionating system and quality product have crucial influence to the economic benefit of whole catalytic cracking unit.
Along with expanding economy, energy-conservation and quality product is improved and is become the problem that oil refining industry is paid close attention to the most gradually.Catalytic cracking unit (FCCU) is the usefulness energy rich and influential family of enterprise, and its energy consumption accounts for 1/3rd of whole refining energy consumption.China's catalytic cracking unit energy consumption is generally higher, and comparing with international most advanced level has bigger gap, and therefore for the catalytic cracking unit of China, saving energy and reduce the cost seems particularly important.The reaction oil gas (about 500 ℃) that comes out from the catalytic cracking reaction regeneration system rapidly has a large amount of heats, be separated into cuts such as rich gas, raw gasline, solar oil, heavy gas oil, recycle stock, slurry oil at catalytic cracking main fractionating tower internal reaction oil gas, about 110 ℃ of its tower top temperature, 330 ℃～380 ℃ of column bottom temperatures, be that reaction oil gas has a large amount of heats, mainly in main fractionating tower, emit by products such as backflow heat-obtaining, recycle stock and slurry oil, weight diesel oil.Reasonably utilizing this part heat how fully, is the key that reduces the catalytic cracking unit energy consumption.
In order to make full use of the heat energy of catalytic cracking reaction oil gas, except the hot trap potentiality of excavating gear as far as possible itself, consider public engineer system (as steam power system and accumulating, heating etc.) in catalytic cracking unit and near device (as atmospheric and vacuum distillation unit etc.) and the factory hot integrated, also answer the specific requirement of combined process flow process, flow process reconstruct and optimization are carried out in technical process, fully effectively utilize the low-temperature heat source of device itself, to realize the energy-optimised of catalytic cracking unit.Fully effectively utilize low-temperature heat source, realize the optimization utilization of low-temperature heat source, both can save a large amount of high temperature heat sources, can reduce the consumption of general facilitiess such as water coolant again in a large number, will have remarkable economic efficiency.Catalytic cracking unit main fractionating tower overhead oil airshed is considerable, and temperature is about 110 ℃, has a large amount of tow taste heats.Main fractionating tower cat head oil gas is after reclaiming a small amount of low warm back and air or water coolant heat exchange condensation and being cooled to 50 ℃～80 ℃ in the industry practical application, in the vapor liquid equilibrium jar, be separated into rich gas and raw gasline, wherein part raw gasline part is as the main fractionating tower trim the top of column, and other enter the absorbing-stabilizing system absorption tower and use as absorption agent.In the condensation process of cooling of main fractionating tower cat head oil gas, a large amount of condensation latent heat and cooling sensible heat are taken away by air or water coolant, and not only this low-temperature heat source can not get effective utilization, and has consumed general facilitiess such as a large amount of water coolants, electricity.Therefore a large amount of condensation latent heat and the cooling sensible heat that how fully to effectively utilize main fractionating tower cat head oil gas are the importances of catalytic cracking unit fractionating system Study on energy saving.
Summary of the invention
The object of the present invention is to provide a kind of catalytic cracking fractionating tower oil gas energy-saving apparatus and operating procedure.Technology of the present invention consumes under the situation of part merit more in the pneumatic press system, fully reclaim main fractionating tower a large amount of low temperature latent heat of cat head oil gas and sensible heat, by-product low-pressure steam or for the use of the low warm trap of catalytic cracking unit and other device, reduce the consumption of general facilitiess such as water coolant significantly, have obvious energy-saving effect.
Technology of the present invention is in fractionator overhead multi-stage compression system to be set.
For existing equipment, can realize technological transformation, receiving portions is low warmly laggardly goes into the pneumatic press multi-stage compression system and reclaims a large amount of low warm step by step catalytic fractionator cat head oil gas cooling back.
Described multi-stage compression system is secondary, three grades or level Four compression system.Every grade of compression system comprises pneumatic press, heat exchanger and knockout drum; It is low warm to enter the heat exchanger cooling recovery after every grade of compression system hydrocarbon flow stock-traders' know-how pneumatic press compression heats up, and enters knockout drum then and finishes the gas-liquid separation operation; Every grade of compression system downstream all exists public low pressure to separate cucurbitula, and the outlet liquid of every grade of compression system knockout drum enters public low pressure and separates cucurbitula low pressure desorb operation, and the outlet gas phase flows into the import of one-level pneumatic press; Public low pressure is separated the raw gasline cooling branch phase system that the cucurbitula downstream is provided with raw gasline water cooler and raw gasline skimmer.
The operating procedure of catalytic cracking fractionating tower oil gas energy-saving apparatus of the present invention, every grade of compression system heat exchanger outlet oil stripping temperature is 70 ℃～96 ℃; It is 0.2MPa～0.4MPa that public low pressure is separated cucurbitula low pressure desorb working pressure.
For the secondary compression system, the pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.4MPa～0.9MPa and 0.8MPa～1.7MPa.
For three grades of compression systeies, the pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.4MPa～0.8MPa, 0.6MPa～1.1MPa and 1.3MPa～1.7MPa.
For the level Four compression system, the pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.2MPa～0.5MPa, 0.4MPa～0.8MPa, 0.7MPa～1.3MPa and 1.0MPa～1.7MPa.
The recovery low temperature thermal center that regards to three grades of compression systeies of catalytic cracking unit fractionator overhead oil gas down can technology be elaborated: as shown in Figure 3, from the effusive cat head oil gas of catalytic cracking main fractionating tower cat head (1) at low warm laggard vapor liquid equilibrium jar (3) separatory of going into of recovery part, decant water enters light sump oil pipe network, oil phase enters raw gasline water cooler (16) cooling, gas phase enters one-level pneumatic press (4) compression supercharging, and simultaneous temperature rises.A large amount of condensation latent heat and cooling sensible heat from one-level pneumatic press (4) the effusive oil gas of outlet and low-temperature water heating or other cryogenic flow thigh heat exchange recycling high-temperature oil gas.Oil gas produces part oil phase and decant water after heat exchange condensation cooling, therefore oily vapour enters one-level vapor liquid equilibrium jar (6) and realizes the separatory operation, gas phase enters secondary pneumatic press (6) compression supercharging, oil phase enters a small amount of light constituent of vapor liquid equilibrium jar (10) low pressure desorb dissolved, and decant water enters light sump oil pipe network.Temperature rose after the gas phase that one-level vapor liquid equilibrium jar (5) comes out entered secondary pneumatic press (7) compression supercharging, therefore utilized a large amount of condensation latent heat of this high-temperature oil gas and cooling sensible heat to heat low-temperature water heating or other cryogenic flow thighs.Oil gas produces part oil phase and decant water after heat exchange condensation cooling, secondary vapor liquid equilibrium jar (8) is set, realize the separatory operation of mixing oil vapour, secondary vapor liquid equilibrium jar (8) outlet gas phase enters three stage gas pressure machine (9) compression supercharging, oil phase enters raw gasline low pressure and separates cucurbitula (20) low pressure desorb dissolved light constituent, and decant water then enters light sump oil pipe network.The gas phase of coming out from secondary vapor liquid equilibrium jar (8) enters three stage gas pressure machine (9) further compress supercharging after temperature rise, therefore make it a large amount of condensation latent heat and the cooling sensible heat to recycle high-temperature oil gas with low-temperature water heating or other cryogenic flow thigh heat exchange.Oil gas condensation cooling back produces the oil phase and the decant water of part, three grades of vapor liquid equilibrium jars (10) is set to realize the separatory operation of three stage gas pressure machine (9) outlet mixing oil vapour.Three grades of vapor liquid equilibrium jars (10) outlet gas phase is the compression rich gas, enter the absorbing-stabilizing system lock out operation, oil phase then is mixed into raw gasline low pressure and separates cucurbitula (20) low pressure desorb dissolved light constituent with one-level, secondary vapor liquid equilibrium jar (6,8) outlet oil phase, and decant water then enters light sump oil pipe network.The oil phase that one-level, secondary and the operation of three grades of vapor liquid equilibrium jars (6,8,10) separatory produce is the higher raw gasline of temperature, this three plumes thigh is mixed into raw gasline low pressure and separates cucurbitula (20) low pressure desorb, a large amount of light constituents in the raw gasline are separated be drawn onto gas phase, gas phase turns back to the import of one-level pneumatic press, liquid phase enters raw gasline water cooler (16) and water coolant or air heat exchange to carry out cooling operation, after the cooling of raw gasline water cooler, further produce decant water in the stream thigh, raw gasline skimmer (17) is set to separate oil phase and decant water.The decant water that produces through the operation of raw gasline skimmer (17) separatory enters light sump oil pipe network, the oil phase that comes out from raw gasline skimmer (17) then is divided into two plume thighs, one enters the absorbing-stabilizing system absorption tower after another strand further cools off and uses as absorption agent (14) as FCC main fractionating tower cat head cold reflux (13).
Reclaim low temperature thermal center energy new technology for catalytic cracking unit fractionator overhead oil gas pneumatic press secondary compression system: as shown in Figure 2, reclaiming the low temperature thermal center in three grades of compressions of catalytic cracking unit fractionator overhead oil gas can cancel three stage gas pressure machine (9), heat exchanger (2) and three grades of vapor liquid equilibrium jars (10) on the new technology basis, and one-level vapor liquid equilibrium jar (6) outlet gas phase directly enters secondary pneumatic press (7).
Reclaim low temperature thermal center energy new technology for catalytic cracking unit fractionator overhead oil gas pneumatic press level Four compression system: as shown in Figure 4, reclaim newly-increased pneumatic press (18), low temperature heat collector (2) and vapor liquid equilibrium jar (19) on the low temperature thermal center energy new technology basis in three grades of compressions of catalytic cracking unit fractionator overhead oil gas.
The present invention transforms the pneumatic press multi-stage compression system on the basis of former catalytic cracking fractionating system and absorbing-stabilizing system flow process: receiving portions is low warmly laggardly goes into the pneumatic press multi-stage compression system and reclaims a large amount of low warm step by step catalytic fractionator cat head oil gas cooling back.The invention has the beneficial effects as follows in the pneumatic press system and consume under the situation of part merit more, can a large amount of low-pressure steam of by-product or as catalytic cracking unit and other device low-temperature heat sources, fully reclaim a large amount of condensation latent heat and the cooling sensible heat of main fractionating tower cat head oil gas, reduce simultaneously the consumption of general facilitiess such as water coolant significantly, have obvious energy-saving effect.
Description of drawings
Fig. 1: be general fractionator overhead condensation cooling system and three grades of compression system process flow diagrams of pneumatic press that adopt in the industrial reality;
Fig. 2: for catalytic cracking unit fractionator overhead oil gas pneumatic press secondary compression system of the present invention reclaims low temperature thermal center energy technical matters general flow chart;
Fig. 3: for three grades of compression systeies of catalytic cracking unit fractionator overhead oil gas pneumatic press of the present invention reclaim low temperature thermal center energy technical matters general flow chart;
Fig. 4: for catalytic cracking unit fractionator overhead oil gas pneumatic press level Four compression system of the present invention reclaims low temperature thermal center energy technical matters general flow chart.
Embodiment
Comparative Examples 1: general fractionator overhead condensation cooling system and three grades of compression system Technologies of pneumatic press that adopt in the industrial reality, structure as shown in Figure 1 and mode of connection.
With the catalysis amount of finish is that certain refinery of 0.4Mt/a is that example is simulated, and its main fractionating tower cat head oil gas (1) flow is 50000kg/h, and temperature is 110 ℃.Warmly be cooled to 80 ℃ from the effusive cat head oil gas of main fractionating tower cat head (1) recovery part is low, after being cooled to 40 ℃, overhead oil gas water cooler (2) condensation enters vapor liquid equilibrium jar (3) separatory then, gas phase enters one-level pneumatic press (4) compression and is pressurized to 0.5MPa, temperature rises to 95 ℃, oil phase (raw gasline) is divided into two strands, one is as main fractionating tower trim the top of column (13), and another strand is cooled to 40 ℃ as absorbing-stabilizing system absorptive tower absorbent (14).One-level pneumatic press (4) outlet oil gas enters and enters vapor liquid equilibrium jar (6) separatory after the oil gas water cooler is cooled to 40 ℃, and gas phase enters secondary pneumatic press (7) compression and is pressurized to 1.0MPa, and temperature rises to 90 ℃.Secondary pneumatic press (7) outlet oil gas enters and enters knockout drum (8) separatory after the oil gas water cooler is cooled to 40 ℃, and gas phase enters three stage gas pressure machine (9) compression and is pressurized to 1.5MPa, and temperature rises to 80 ℃.Three stage gas pressure machine (9) outlet oil gas enters and enters knockout drum (10) separatory after the oil gas water cooler is cooled to 40 ℃, gas phase is compression rich gas (11) and enters absorbing-stabilizing system, oil phase and knockout drum (6), (8) outlet condensed oil are mixed into absorbing-stabilizing system, and the decant water (15) that all knockout drums are separated mixes incorporates light sump oil pipe network into.
Embodiment 1: three grades of compression systeies of catalytic cracking unit fractionator overhead oil gas pneumatic press reclaim low temperature thermal center energy new technology, structure as shown in Figure 2 and mode of connection.
Every grade of compression system heat exchanger outlet oil stripping temperature is 70 ℃～96 ℃; It is 0.2MPa～0.4Mpa that public low pressure is separated cucurbitula low pressure desorb working pressure; The pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.4MPa～0.8MPa, 0.6MPa～1.1MPa and 1.3MPa～1.7MPa.
With the catalysis amount of finish is that certain refinery of 0.4Mt/a is that example is simulated, and its main fractionating tower cat head oil gas (1) flow is 50000kg/h, and temperature is 110 ℃.From the effusive cat head oil gas of main fractionating tower cat head (1) through low warm laggard vapor liquid equilibrium jar (3) separatory of going into of recovery part, oil phase enters raw gasline water cooler (16), decant water enters light sump oil pipe network, and gas phase enters one-level pneumatic press (4) compression and is pressurized to 0.5MPa.One-level pneumatic press (4) effusive oil gas of outlet and low-temperature water heating or other cryogenic flow thigh heat exchange are cooled to 80 ℃, outlet mixing oil vapour enters one-level vapor liquid equilibrium jar (6) and realizes the separatory operation, oil phase enters raw gasline and separates cucurbitula (20), decant water enters light sump oil pipe network, and gas phase enters secondary pneumatic press (7) compression and is pressurized to 0.9MPa.Secondary pneumatic press (7) outlet oil gas and low-temperature water heating or other cryogenic flow thigh heat exchange are cooled to 80 ℃, outlet mixing oil vapour enters secondary vapor liquid equilibrium jar (8) and realizes the separatory operation, oil phase enters raw gasline and separates cucurbitula (20), decant water enters light sump oil pipe network, and gas phase enters three stage gas pressure machine (9) compression and is pressurized to 1.5MPa.Three stage gas pressure machine (9) outlet oil gas and low-temperature water heating or other cryogenic flow thigh heat exchange are cooled to 80 ℃, outlet mixing oil vapour enters three grades of vapor liquid equilibrium jars (10) and realizes the separatory operation, oil phase enters raw gasline and separates cucurbitula (20), and decant water enters light sump oil pipe network, and gas phase is the compression rich gas.The raw gasline that one-level, secondary and the operation of three grades of vapor liquid equilibrium jars (6,8,10) separatory produce enters raw gasline and separates cucurbitula (20) part light constituent in the desorb raw gasline under 0.3MPa, light constituent enters one-level pneumatic press (4) import, and heavy constituent and vapor liquid equilibrium jar (3) outlet oil phase are mixed into and enter raw gasline skimmer (17) separatory after raw gasline water cooler (16) cools off with water coolant or air heat exchange.The oil phase that raw gasline skimmer (17) is separated is divided into two plume thighs, and one is as catalytic cracking main fractionating tower trim the top of column (13), and another strand is cooled to 40 ℃ as absorbing-stabilizing system absorptive tower absorbent (14).
Embodiment 2: catalytic cracking unit fractionator overhead oil gas pneumatic press secondary compression system reclaims low temperature thermal center energy new technology, structure as shown in Figure 3 and mode of connection.
Every grade of compression system heat exchanger outlet oil stripping temperature is 70 ℃～96 ℃; It is 0.2MPa～0.4Mpa that public low pressure is separated cucurbitula low pressure desorb working pressure; The pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.4MPa～0.9MPa and 0.8MPa～1.7MPa.
Cancellation three stage gas pressure machine (9), heat exchanger (2) and three grades of vapor liquid equilibrium jars (10) on embodiment 2 bases, one-level vapor liquid equilibrium jar (6) outlet gas phase directly enters secondary pneumatic press (7).The pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.7MPa and 1.5MPa, 80 ℃ of low temperature heat collector hot-fluid thigh temperature outs, and it is 0.3MPa that public low pressure is separated cucurbitula low pressure desorb working pressure.Embodiment 3: catalytic cracking unit fractionator overhead oil gas pneumatic press level Four compression system reclaims low temperature thermal center energy new technology, structure as shown in Figure 4 and mode of connection.
Every grade of compression system heat exchanger outlet oil stripping temperature is 70 ℃～96 ℃; It is 0.2MPa～0.4MPa that public low pressure is separated cucurbitula low pressure desorb working pressure; The pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.2MPa～0.5MPa, 0.4MPa～0.8MPa, 0.7MPa～1.3MPa and 1.0MPa～1.7MPa.
Newly-increased pneumatic press (18), low temperature heat collector (2) and vapor liquid equilibrium jar (19) on embodiment 2 bases.The pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.4MPa, 0.8MPa, 1.2MPa and 1.5MPa, 80 ℃ of newly-increased low temperature heat collector hot-fluid thigh temperature outs, and it is 0.3MPa that public low pressure is separated cucurbitula low pressure desorb working pressure.
Under same treatment capacity, feed conditions and treatment effect, (Comparative Examples 1) treatment effect of the common process flow process in the industrial practical application and technology of the present invention (embodiment 1, example 2, example 3) treatment effect are compared, comparative result is as follows:
Table 1 technology of the present invention and industrial general technology energy consumption are relatively
Table 1 is the comparison of technology of the present invention with the general technology energy consumption of industry employing.Two kinds of aspects that technology compared are mainly the consumption of pneumatic press system merit, recirculated cooling water consumption and low temperature recovery of heat amount.
As can be seen from Table 1, compare with industrial general technology, adopt technology of the present invention, because the handled oil gas flow of pneumatic press increases, temperature increases, so the merit consumption of pneumatic press system increases.But, this patent technology can fully reclaim a large amount of condensation latent heat and the cooling sensible heat of fractionator overhead oil gas, reduce recirculated cooling water consumption significantly, low temperature recovery of heat amount increased value reaches 4.74,5.23,5.61 respectively with the ratio of pneumatic press system merit consumption increased value, has obvious energy saving effect.
Open catalytic cracking fractionating tower oil gas energy-saving apparatus of the present invention and operating procedure, 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.The present invention is described by different examples of implementation, 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.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 (8)
1. a catalytic cracking fractionating tower oil gas energy-saving apparatus is characterized in that in fractionator overhead multi-stage compression system being set.
2. catalytic cracking fractionating tower oil gas energy-saving apparatus as claimed in claim 1, receiving portions is low warmly laggardly goes into the pneumatic press multi-stage compression system and reclaims a large amount of low warm step by step cooling back to it is characterized in that fractionator overhead oil gas.
3. catalytic cracking fractionating tower oil gas energy-saving apparatus as claimed in claim 1 is characterized in that described multi-stage compression system is secondary, three grades or level Four compression system.
4. catalytic cracking fractionating tower oil gas energy-saving apparatus as claimed in claim 1 is characterized in that every grade of compression system comprises pneumatic press, heat exchanger and knockout drum; It is low warm to enter the heat exchanger cooling recovery after every grade of compression system hydrocarbon flow stock-traders' know-how pneumatic press compression heats up, and enters knockout drum then and finishes the gas-liquid separation operation; Every grade of compression system downstream all exists public low pressure to separate cucurbitula, and the outlet liquid of every grade of compression system knockout drum enters public low pressure and separates cucurbitula low pressure desorb operation, and the outlet gas phase flows into the import of one-level pneumatic press; Public low pressure is separated the raw gasline cooling branch phase system that the cucurbitula downstream is provided with raw gasline water cooler and raw gasline skimmer.
5. the operating procedure of the catalytic cracking fractionating tower oil gas energy-saving apparatus of claim 1 is characterized in that every grade of compression system heat exchanger outlet oil stripping temperature is 70 ℃～96 ℃; It is 0.2MPa～0.4MPa that public low pressure is separated cucurbitula low pressure desorb working pressure.
6. operating procedure as claimed in claim 5 is characterized in that for the secondary compression system, and the pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.4MPa～0.9MPa and 0.8MPa～1.7MPa.
7. operating procedure as claimed in claim 5 is characterized in that for three grades of compression systeies, and the pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.4MPa～0.8MPa, 0.6MPa～1.1MPa and 1.3MPa～1.7MPa.
8. operating procedure as claimed in claim 5 is characterized in that for the level Four compression system, and the pneumatic press phase pressure of working off one's feeling vent one's spleen is respectively 0.2MPa～0.5MPa, 0.4MPa～0.8MPa, 0.7MPa～1.3MPa and 1.0MPa～1.7MPa.
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| CN 200910068065 CN101503631B (en) | 2009-03-06 | 2009-03-06 | Catalytic cracking fractionating tower oil gas energy-saving apparatus and operation technique |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101967394A (en) * | 2010-10-18 | 2011-02-09 | 李湘平 | Low-temperature heat recovery system of catalytic cracking unit |
| CN104479734A (en) * | 2014-11-12 | 2015-04-01 | 天津大学 | Catalytic cracking fractionation and absorbing-stabilizing system and energy-saving method |
| JP2019536839A (en) * | 2016-10-07 | 2019-12-19 | サビック グローバル テクノロジーズ ベスローテン フェンノートシャップ | Stages and systems for compressing cracked gas |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5568737A (en) * | 1994-11-10 | 1996-10-29 | Elcor Corporation | Hydrocarbon gas processing |
| EP1513789B1 (en) * | 2002-06-12 | 2013-04-03 | Stone & Webster Process Technology, Inc. | Eb/sm splitter heat recovery |
| CN101358143B (en) * | 2008-08-28 | 2012-08-15 | 天津大学 | Ethylene quenching apparatus and compressing energy-saving technique |
-
2009
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101967394A (en) * | 2010-10-18 | 2011-02-09 | 李湘平 | Low-temperature heat recovery system of catalytic cracking unit |
| CN104479734A (en) * | 2014-11-12 | 2015-04-01 | 天津大学 | Catalytic cracking fractionation and absorbing-stabilizing system and energy-saving method |
| CN104479734B (en) * | 2014-11-12 | 2016-06-08 | 天津大学 | Catalytic cracking fractionation and absorbing-stabilizing system and power-economizing method |
| JP2019536839A (en) * | 2016-10-07 | 2019-12-19 | サビック グローバル テクノロジーズ ベスローテン フェンノートシャップ | Stages and systems for compressing cracked gas |
| JP7092754B2 (en) | 2016-10-07 | 2022-06-28 | サビック グローバル テクノロジーズ ベスローテン フェンノートシャップ | Stages and systems for compressing decomposition gas |
| US11560523B2 (en) | 2016-10-07 | 2023-01-24 | Sabic Global Technologies B.V. | Stage and system for compressing cracked gas |
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