CN103210060B - For processing the method for hydrocarbon pyrolysis effluent - Google Patents

For processing the method for hydrocarbon pyrolysis effluent Download PDF

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Publication number
CN103210060B
CN103210060B CN201180035764.9A CN201180035764A CN103210060B CN 103210060 B CN103210060 B CN 103210060B CN 201180035764 A CN201180035764 A CN 201180035764A CN 103210060 B CN103210060 B CN 103210060B
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heat exchanger
effluent
partially
fluid
cracking
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CN103210060A (en
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R·D·斯特拉克
J·R·阿诺德
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ExxonMobil Chemical Patents Inc
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Exxon Chemical Patents Inc
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Priority claimed from US12/847,433 external-priority patent/US20120024749A1/en
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/002—Cooling of cracked gases
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

For the treatment of the effluent from hydrocarbon pyrolysis unit, adopt the method and system of little main fractionator to be disclosed.Described method comprises the effluent by the first heat exchanger, vapor liquid separator and the second heat exchanger cooling stove, is then led to fractionator to process further.These heat exchangers also can be used to heat practical fluid, as a part for described method of cooling.And one or more producer and the 3rd heat exchanger also can be used to the heat recuperation of auxiliary described method.

Description

For processing the method for hydrocarbon pyrolysis effluent
The cross reference of related application
The interests of the European application numbers 10175705.2 that this application claims the Application U.S. Serial No 12/847,433 submitted on July 30th, 2010 and submit on September 8th, 2010 and right of priority, their whole disclosures are incorporated herein by reference.
Invention field
The present invention relates to for processing from hydrocarbon pyrolysis unit, particularly utilizing the method for the effluent of those unit of liquid feeding.
Background of invention
The technology that light olefin (ethene, propylene and butylene) typically utilizes pyrolysis or steam cracking is produced by various hydrocarbon feed.Pyrolysis relates to heats described raw material fully to cause more macromolecular thermolysis.Then, the effluent from pyrolyzer can be cooled by the method or device using routine.
But this method for pyrolysis can produce and tend to combine and form the molecule being called as the high molecular weight material of tar.Tar is high boiling, sticky, reactive material, and it under certain conditions can polluting device.The pollution of described device should be minimized, to avoid the inefficiency relevant to clean described device and shut-down period.After pyrolysis effluent leaves steam cracking furnace, the formation of tar can be minimized by the level that greatly slows down by by making the temperature of the effluent leaving pyrolysis unit be reduced to tar formation reaction fast.
Various technology can be used to cooling pyrolysis unit stream effluent and remove the heavy oil and tar that produce.Such as, a kind of by way of adopting heat exchanger and water quench tower thereafter, in water quench tower, condensables is removed.When cracking lighter-than-air gas (mainly ethane, propane and butane), this technology is verified is effective, because the cracker (being jointly called as gas conveter) processing light charging produces tar relatively in a small amount.For the heavier raw material that can be used to steam cracker (its pressure naphtha (such as cracked liquid)), another kind of method may relate to and removes some heats but the heat exchanger of the temperature of condensation being only reduced to tar from liquid cracking.Below this temperature, should not use conventional heat exchanger because they because of the Cumulate Sum thermal destruction of tar on described heat-exchanger surface pickup fast.Like this, in commercial liquid cracker structure, the cooling of pyrolyzer effluent uses line of pipes heat exchanger usually, usually directly quenching, main fractionator, and the system of water quench tower or indirect condenser realizes.
As will be appreciated, effective heat recuperation improves the operation of described system.That is, from steam cracking furnace effluent efficient recovery heat be favourable in the total energy efficiency of olefin hydrocarbon apparatus.Such as, the temperature out of steam cracking furnace typically operates in about 1,500 °F (815 ° of C) (described temperature depends on quality and the cracking severity of raw material).By operating at such high temperatures, be cooled to close to envrionment temperature so that when carrying out initial product separation and compression, a large amount of heats can be recovered at described effluent.
In typical hydrocarbon pyrolysis system, transfer-line exchanger (TLE) is used to produce ultra-high voltage (SHP) steam when stove effluent leaves pyrolyzer by the initial cooling of described stove effluent.Described SHP steam can be included in about 1, the pressure in 500 pounds/square inch of gauge pressure (psig)-Yue 2,000psig (about 10,450 kPas of (kpa)-Yue 13,982kpa) scopes.First heat exchanger produces saturated SHP steam by high-duty boiler feed water.The saturated SHP steam produced by described TLE can be overheated further by the convective region at described stove, can the amount of work to increase it.
But the TLE of typical structure only can the part of recovery furnace effluent heat, because temperature (tar dew point) restriction when it is started condensation by tar.That is, the pickup restriction when running into dew point is subject in the temperature out of the technique side of described TLE.As noted above, the heavy component in described effluent is TLE surface described in the condensation of tar dew point and pickup, makes them be invalid concerning heat transmission.For naphtha cracker, tar dew point pickup restricted T LE temperature out is to minimum about 700 °F (371 ° of C).For the charging heavier than petroleum naphtha, TLE temperature out is higher than 700 °F (371 ° of C), because described effluent tar dew point is higher.Described TLE temperature out is also by the temperature limitation of steam generation temperature, and this temperature is about 600 °F (315 ° of C) for 1500psig (10,450kpa) steam.Like this, the TLE adjacent with described stove only can reclaim the temperature of effluent heat to about 650 °F of-Yue 1000 °F (about 343 ° of C-about 538 ° of C) from liquid cracking, depends on the severe of charging.
After initial cooling, described effluent is typically provided to main fractionator system.Described main fractionator system is unusual complicated apparatus group, and it typically comprises oily quench region, main fractionator tower and one or more oil outer circulation loop.In described oily quench region, quenching oil is added, so that described effluent logistics is cooled from about 400 °F of-Yue 650 °F (about 204 ° of C-about 343 ° of C), and the tar existed in logistics described in condensation thus.In described main fractionator tower, the tar of described condensation is separated by with the rest part of described logistics, and heat is removed by turning oil by one or more race way, and pyrolysis naphtha by one or more distillation zone with heavier material separation.In described one or more external circulation, the oil taken out from described main fractionator is used indirect heat exchanger cool and then turn back to described main fractionator or described direct quench point.
The described main fractionator system with its associated cyclic system is one of assembly costly in whole cracking technology.Described main fractionator tower itself is one piece apparatus maximum in described technique, typically is about 25 ft diams with high more than 100 feet for main fractionator tower described in medium sized liquid cracker.Described tower is large, because its effective fractionation two kinds of accessory constituent under the low-pressure gas of large volume exists, i.e. and tar and pyrolysis gasoline, and need heat significantly excessive in charging described in refoulement.Described circulation loop is large equally, and when medium sized cracker, process is more than the turning oil of 3,000,000 Pounds Per Hours of (lb/hr) (1,363,636kg/hr).Due to high flow, in order to reclaim the close temperature approaches required for heat and the tolerance to pickup with useful level, the heat exchanger in described circulation loop is necessarily large.
In addition, described main fractionator has many other limitation and problem.Especially, heat delivery occurs twice, namely from gas to the circulating liquid in described tower with then from described circulating liquid to exterior cooling service unit.This requires the investment in two heat exchange systems effectively, and on heat removes, impose two temperature approaches (or temperature head), reduces thermo-efficiency thus.
And although there occurs fractionation between described tar and gasoline stream, two logistics often need to be further processed.Sometimes described tar needs by stripping to remove light constituent, and described gasoline may need by fractionation again, to meet its final specification.
And described main fractionator tower and its recycle system are easily dirt.Char build-up in the tower base area of described tower, and finally has to be removed by during turnaround of unit.Described circulation loop is also easily dirt, and requires from strainer removing coke and the cleaned at regular intervals of heat exchanger that is dirt.Tower tray in described tower and filler are also easily dirt sometimes, and this may limit plant production.Described system is also containing quite a large amount of flammable liquid hydrocarbons, and from intrinsic safety viewpoint, this is undesirable.
Therefore need for cooling pyrolysis unit stream effluent and the method providing the raising from the effective heat recuperation of described effluent.And, therefore need the method for the simplification of heavy oil and the tar produced for cooling pyrolysis unit stream effluent and removing, this method avoid the needs to main fractionator tower and its supplementary unit.The technology of the present invention provides effective heat recovery method and/or effluent method of cooling, and it is one or more that described method overcomes in shortcoming discussed above.
Relevant material can find in following file: U.S. Patent number 3,907,661; 3,923,921; 3,959,420; 4,121,908; 4,150,716; 4,233,137; 4,279,733; 4,279,734; 4,444,697; 4,446,003; 5,092,981; 5,107,921; 5,294,347; With 5,324,486.Other material can be shown in international patent application no 2000/56841 and 1993/12200; British Patent No. 1,390,382 and 1,309,309; The EP patent No. 205205 and Japanese Patent No. 2001-40366.Other material can also be shown in following publication: Lohretal., " Steam-crackerEconomyKeyedtoQuenching, " Oil & GasJournal, Vol.76 (No.20), pp.63-68, (1978).
Summary of the invention
In one embodiment, the method for the charging of cracking hydrocarbon is described.Described method comprises: provide hydrocarbon to be fed into hydrocarbon pyrolysis unit, to produce the effluent of cracking; Make the effluent of the cracking from described hydrocarbon pyrolysis unit at least partially by the first heat exchanger; The effluent of the described cracking from described first heat exchanger is separated into gaseous effluent and liquid efflunent at least partially, and this can carry out in vapor liquid separator; Make from separator gaseous effluent at least partially by the second heat exchanger; Described effluent from described second heat exchanger led to fractionator at least partially; By making practical fluid by described second heat exchanger from the heat of recovery at least partially of described gaseous effluent in described second heat exchanger; With by making described practical fluid from described second heat exchanger by described first heat exchanger from the heat of recovery at least partially of the effluent of described cracking in described first heat exchanger.Described method may further include other technique as operation turbine in use as described in by the practical fluid heated.
In another embodiment, hydrocarbon pyrolysis system is described.This system comprises hydrocarbon pyrolysis unit, separator, the first heat exchanger, the second heat exchanger and fractionator.Described hydrocarbon pyrolysis unit is built into certain forms, to receive hydrocarbon charging and the effluent by described hydrocarbon charging generation cracking.And described first heat exchanger is communicated with described hydrocarbon pyrolysis unit fluid, and be built into certain forms with cooling from the described cracking of described hydrocarbon pyrolysis unit effluent at least partially with heating practical fluid at least partially.Described separator is communicated with described first heat exchanger fluid, and is built into certain forms with separating liquid effluent and gaseous effluent at least partially described in the effluent by described cracking.Described second heat exchanger is communicated with described separator fluid, and be built into certain forms with cooling from described separator described gaseous effluent at least partially and described first heat exchanger receive described practical fluid at least partially before heat described practical fluid this at least partially.Described fractionator can be communicated with described second heat exchanger fluid, and be built into certain forms with receive from the described effluent of described second heat exchanger this at least partially.
In still another embodiment, the method for steam cracking of hydrocarbons charging is described.Described method comprises: provide hydrocarbon to be fed into hydrocarbon pyrolysis unit, to produce the effluent of cracking; Be separated from the described cracking of described hydrocarbon pyrolysis unit effluent at least partially, wherein gaseous effluent is separated by with liquid efflunent, and described liquid efflunent can comprise tar and other bottoms of steam cracking; Cool in the first heat exchanger from described separator described gaseous effluent at least partially; Effluent from described first heat exchanger led to one or more vapour generator at least partially; Effluent from described one or more vapour generator led to the second heat exchanger at least partially; With the effluent from described second heat exchanger led to fractionator at least partially.
In still another embodiment, effluent treatment system is described.This system comprises hydrocarbon pyrolysis unit, separator, the first heat exchanger, the second heat exchanger, one or more vapour generator and fractionator.Described hydrocarbon pyrolysis unit is built into certain forms, to receive hydrocarbon charging and the effluent by described hydrocarbon charging generation cracking.Described separator is communicated with described hydrocarbon pyrolysis unit fluid, and is built into certain forms with the effluent of separating liquid at least partially of the effluent by the described cracking from described hydrocarbon pyrolysis unit (tar and other bottom product as steam cracking) and gaseous effluent.Described first heat exchanger is communicated with described separator fluid, and be built into certain forms with cooling from described separator described gaseous effluent at least partially.Described one or more vapour generator is communicated with described first heat exchanger fluid, and be built into certain forms with receive from described first heat exchanger described effluent at least partially.Described second heat exchanger is communicated with described one or more producer fluid, and be built into certain forms with cooling from described one or more vapour generator described effluent at least partially.Described fractionator is communicated with described second heat exchanger fluid, and be built into certain forms with receive from described second heat exchanger described effluent at least partially.
Brief Description Of Drawings
Fig. 1 is the block flow diagram reclaiming heat according to the exemplary of the technology of the present invention from the cooling of the effluent of cracking hydrocarbon charging.
Fig. 2 is the block flow diagram reclaiming heat according to one of the technology of the present invention alternative exemplary from the cooling of the effluent of cracking hydrocarbon charging.
Fig. 3 is the block diagram reclaiming heat according to another exemplary substituted of the technology of the present invention from the cooling of cracking hydrocarbon effluent.
Fig. 4 is another block diagram reclaiming heat according to another exemplary substituted of the technology of the present invention from the cooling of cracking hydrocarbon effluent.
The preferred embodiment of combined the technology of the present invention describes by the present invention.But, be that with regard to the degree for specific embodiment of the invention scheme or concrete purposes, it is only illustrative that this descriptions is intended to, and should not be interpreted as limiting the scope of the invention with regard to following detailed description.On the contrary, its intention covers all alternative option that can be included in the spirit and scope of the present invention that defined by appended claims, change and Equivalent.
The detailed description of embodiment
Present technology provides the efficient arrangement of the effluent logistics for the treatment of hydrocarbon pyrolysis unit (it can be called as pyrolysis reactor or stove), to be removed by described effluent logistics and reclaim heat and be separated the hydrocarbon of wishing.Such as, the technology of the present invention can separation of C 5+ hydrocarbon, provides the pyrolysis gasoline of separation, gas oil, quenching oil and tarry cut, and the C of hope in described effluent 2-C 4alkene, and do not utilize main fractionator to circulate.
Typically, the described effluent used in one or more embodiments of the technology of the present invention is produced by hydrocarbon charging such as the pyrolysis of petroleum naphtha, truncation crude oil (tailedcrudes) or gas oil of boiling in the temperature range of about 40 ° of C-about 704 ° of C (about 104 °F-Yue 1300 °F).Such as, described effluent can be produced by the pyrolysis of hydrocarbon charging as the charging heavier than petroleum naphtha with the full boiling point exceeding about 180 ° of C (about 356 °F).Those chargings of seething with excitement in the scope that such charging is included in about 177 ° of C-about 538 ° of C (about 350 °F-Yue 1000 °F) or in the scope of about 204 ° of C-about 510 ° of C (about 400 °F-Yue 950 °F).Typically heavy than petroleum naphtha charging can comprise heavies condensation thing, gas oil, isocrackate, kerosene, condensation product, truncation crude oil and/or truncation crude oil fractions, the reduced oil of such as truncation.Described effluent in the temperature of the outlet of pyrolysis reactor usually in the scope of about 760 ° of C-about 930 ° of C (about 1400 °F-Yue 1706 °F), and inventive technique provides for the described effluent of cooling to the method in the temperature of the hope of fractionator, the temperature of described hope can be included in the temperature in about 100 ° of C-about 200 ° of C (212 °F-392 °F) scopes.In this temperature range, the C of described hope 2-C 4alkene can be further cooled and effectively compress.
Remove to effectively manage described heat and reclaim, one or more embodiments of the technology of the present invention relate to arrangement or the configuration of the optimization of the heat exchanger for removing and reclaim heat from cracker effluent.Typically, single heat exchanger limits by the temperature head between the temperature of hot effluent logistics and the temperature of practical fluid stream.The use of two or more cooling sections (particularly with specific order) overcomes this restriction by providing more reversed flow arrangements of hot and cold logistics.Like this, configure described heat exchanger to be provided for practical fluid two or more heating zones as boiler feed water, two or more cooling sections being simultaneously also provided for the effluent of described stove are useful.Initial section or first paragraph can relate to higher temperature, and below or second segment relate to lower temperature.Result, described two heating and cooling sections (being such as two or more heat exchangers of this configuration or order) can heat described practical fluid to the temperature higher than any single heat exchanger of employing temperature in the cards, and provide the efficient mechanism for being reclaimed heat by described effluent.
And in other embodiments, these heat exchangers can be used by together with other device in concrete configuration, to improve the heat recovery method of described hydrocarbon pyrolysis system further.These configurations or arrangement can be used to the larger temperature head of the heat exchanger be provided in different heating and cooling sections, as discussed further below.Such as, in certain embodiments, described heat exchanger can be arranged by together with one or more vapour generator, to reclaim heat in a more effective manner.
And in the various embodiments discussed further below, should be appreciated that, the effluent of described practical fluid and described stove is unmixed logistics separated.Each in these different logistics can be maintained at different pressure, based on concrete configuration and the operational design of described system.Such as, described heat exchanger can comprise transfer-line exchanger, double-pipe exchanger or tube and shell heat exchanger.
Forward Fig. 1 to, according to the technology of the present invention an exemplary, square process Figure 100 of the method that reclaims heat from the cooling of cracking hydrocarbon effluent is disclosed.In this flow process Figure 100, provide hydrocarbon pyrolysis unit 102 (such as cracker, reactor or stove) and the first heat exchanger 104, separator 106, second heat exchanger 108 and fractionator 110.These unit 102-110(they are parts of hydrocarbon pyrolysis system) by specifically to arrange to use together, to reclaim heat when the hydrocarbon effluent of cracking is cooled from the hydrocarbon effluent of described cracking.The method comprises the charging of cracking hydrocarbon and in various sections, cools the hydrocarbon effluent of cracking, and practical fluid is heated to reclaim the energy be input in described hydrocarbon pyrolysis method simultaneously.Especially, the cooling of the hydrocarbon effluent of described cracking is described in square 122-130, and the heating of described practical fluid is described in square 134-138.
First, hydrocarbon charging is provided at square 120.Described hydrocarbon charging can comprise such as ethane, propane, butane, oil, petroleum naphtha, pentane, gas oil, condensation product and crude oil.At square 122, described hydrocarbon charging is cleaved to produce effluent.This cleavage method can comprise gas cracking, steam cracking or liquid cracking, as will be understood by the skilled person in the art.As concrete example, U.S. Patent Application No. 2007/0007172 and 2007/0007174(they be combined in by reference herein) describe exemplary cleavage method.As noted above, the cracking (it produces effluent) of described hydrocarbon charging can comprise the temperature of about 760 ° of C-about 930 ° of C (about 1400 °F-Yue 1706 °F), and described temperature depends on the quality of described hydrocarbon charging.As a part for described cleavage method, described hydrocarbon charging is heated, to cause the thermolysis of described charging to produce more low-molecular-weight hydrocarbon, and such as C 2-C 4alkene.
In order to cool described effluent, various step is carried out to described hydrocarbon pyrolysis effluent, as shown in square 124-130.In square 124, described effluent is cooled by the first heat exchanger 104.The heat of described effluent can be delivered to described practical fluid by described first heat exchanger 104, and described first heat exchanger 104 can be such as transfer-line exchanger (TLE).In this stage, described effluent can be cooled to the first heat exchanger outlet temperature by the temperature from the ingress at described first heat exchanger 104, and the temperature of the ingress of described first heat exchanger 104 can be identical with the temperature of described outlet of still or lower than the temperature of described outlet of still.As will be appreciated, the temperature range in described first paragraph can change, and depends on different hydrocarbon chargings.Again, as noted above, described first heat exchanger outlet temperature should be set to prevent pickup, such as, higher than the tar dew point pickup limit 371 ° of C-537 ° of C (700 °F-1000 °F).
Described first heat exchanger can optionally be coupled to direct quenching.Described direct quenching can cool effluent from described first heat exchanger 104 to the temperature of the tar condensing at least formed by the reaction between the component of described effluent.Described direct quenching can comprise oily quenching, water quenching or other suitable method.As an example, U.S. Patent number 3,923,921 describe direct method of quenching.
Once described tar is condensed, described effluent can be separated into different logistics, such as liquid efflunent and gaseous effluent, as shown in square 126.Described liquid efflunent can comprise tar and other bottoms of steam cracking.The tar (it can be pyrolysis fuel oil) of described steam cracking is typically obtained by as bottoms product, nominally its have 550 °F+(288 ° of C+) and higher boiling point, such as, temperature more than 550 °F or more than 288 ° of C.Described separator 106 can comprise vapor liquid separator or tar knock-out drum, as known in the art.Described separator 106 can be identical or lower than described first heat exchanger outlet temperature in described first heat exchanger outlet temperature temperature operate between separation and thickening.The service temperature of described separator 106 can be conditioned, and depends on severity, hydrocarbon charging or the other factors of the operation of described first heat exchanger 104.Therefore, should be appreciated that, at described effluent by described first heat exchanger 104 by afterwards and before it enters described separator 106, it can by directly injecting fluid in a small amount or being further cooled at direct method of quenching.
At square 128, the gaseous effluent from described separator 106 can be further cooled.About the discussion of the first heat exchanger above being similar to, the heat of described gaseous effluent can be delivered to described practical fluid by by the second heat exchanger 108, and described second heat exchanger 108 can be such as tube and shell heat exchanger.In this stage, described gaseous effluent can be cooled to the second heat exchanger outlet temperature by from identical with described separation and thickening or lower than described separation and thickening temperature.Described second heat exchanger outlet temperature can be conditioned, based on the temperature head of the hope of this unit.
At square 130, the effluent from described second heat exchanger 108 can be provided to another unit, to process described effluent further.As an example, described unit can be fractionator 110, or small-sized fractionator more specifically.Described fractionator 110 can be small-sized main fractionator, and it is further described in U.S. Patent Application No. 2007007174.
As a part for described heat recovery method, practical fluid heating in each section at least partially, as described in square 134-138 by the effluent of the described hydrocarbon pyrolysis.In square 132, practical fluid is provided to described hydrocarbon pyrolysis system.Described practical fluid can comprise the boiler feed water in the source from such as degasser and so on, or can comprise other suitable fluid any.Then, described practical fluid is heated by square 134.Especially, described practical fluid can be heated by the transmission of the heat of the gaseous effluent from described separator 106 by described second heat exchanger 108.In this heating phase, described gaseous effluent in described second heat exchanger 108 is in the temperature higher than described practical fluid, to such an extent as to described second heat exchanger 108 can heat described practical fluid and described practical fluid can cool described gaseous effluent.Then, in square 136, described practical fluid can be heated by described first heat exchanger 104.In this heating phase, the described effluent in described first heat exchanger 104 is in the temperature higher than the practical fluid from described second heat exchanger 108.Utilize this temperature head, the described effluent in described first heat exchanger 104 can heat described practical fluid, and described practical fluid can cool described effluent.Then, after the heating in described first heat exchanger 104, described practical fluid can be heated further by described hydrocarbon pyrolysis unit 102, as shown in square 138.Especially, if described practical fluid is feed water, it can be heated by described hydrocarbon pyrolysis unit 102, to convert it into overheated ultra-high voltage (SHP) steam.Then, at square 140, describedly can be used by other method by the practical fluid heated.As an example, describedly such as can be used to drive large turbine in other district (such as the recovery zone of described steam cracker) of described device by the practical fluid heated.
Beneficially, the use of two sections of heat exchangers in described configuration provides by described hydrocarbon pyrolysis method recovery heat with than the mechanism adopting single heat exchanger more effectively to heat described practical fluid.That is, this configuration of two heating zones in this order provides the more efficient countercurrent flow arrangement of the logistics of described differing temps.
As will be appreciated, the temperature of described various unit can change, and depends on that the quality of hydrocarbon charging or other operation are considered.For typical operation, the heater outlet temperature of the effluent of the described hydrocarbon pyrolysis can comprise the temperature of about 760 ° of C-about 930 ° of C (1400 °F-1706 °F).Described first heat exchanger process inlet temperature can in the scope of about 760 ° of C-about 930 ° of C (1400 °F-1706 °F), or be preferably about 816 ° of C (1500 °F), and described first heat exchanger process outlet temperature can in the scope of about 343 ° of C-about 650 ° of C (about 650 °F-Yue 1200 °F), preferably in the scope of 343 ° of C-538 ° of C (650 °F-1000 °F).Described separator can at the temperature operation of 190 ° of C-about 350 ° of C (about 374 °F-Yue 662 °F), or preferably at the temperature operation of about 190 ° of C-about 315 ° of C (about 374 °F-Yue 599 °F).Described second heat exchanger entrance temperature can in the scope of about 190 ° of C-about 350 ° of C (about 374 °F-Yue 662 °F), and described second heat exchanger outlet temperature can between about 170 ° of C and about 300 ° C (about 338 °F-Yue 572 °F).
For described heat recovery method, described practical fluid can by about 2,172kPa-about 17,340kPa (300psig-2500psig), about 10,450kpa-about 13,982kPa (1,500psig-about 2,000psig), or the pressure of about 10,450kPa (1500psig) provide, and have about 50 ° of C-about 200 ° of C (122 °F-392 °F), the temperature preferably in about 100 ° of C-about 150 ° of C (212 °F-302 °F) scopes.As will be appreciated, the heat reclaimed in described second heat exchanger can heat described practical fluid to the temperature in 100 ° of C-about 300 ° of C (about 212 °F-Yue 572 °F) scope.Further, the heat recuperation in described first heat exchanger can in the temperature range of 205 ° of C-about 355 ° of C (about 401 °F-Yue 671 °F) the described practical fluid of heating.In described hydrocarbon pyrolysis unit 102, described practical fluid can be further heated, and relates in about 2,172kPa-about 17, in 340kPa (300psig-2500psig) scope, about 10,450kPa-about 13,982kPa (about 1,500psig-about 2,000psig) in scope, or about 10, the pressure of 450kPa (about 1500psig), and the temperature range relating to about 490 ° of C-about 550 ° of C (about 914 °F-Yue 1022 °F).
Further, as will be appreciated, another optional heating zone can be used in described method.Such as, described practical fluid can be heated by described hydrocarbon pyrolysis unit 102 between described second heat exchanger 108 and described first heat exchanger 104.That is, can described hydrocarbon pyrolysis unit 102 be passed through by the described practical fluid of heating in described second heat exchanger 108, then be provided to described first heat exchanger 104.In like fashion, other heat can be reclaimed in the process.
As an alternative embodiment, Fig. 2 is the square process Figure 200 being reclaimed the method for heat according to one of the technology of the present invention alternative exemplary by the cooling of hydrocarbon pyrolysis effluent.Described flow process Figure 200 comprises some similar similar devices of the square discussed with the flow process Figure 100 above about Fig. 1 and operation.Therefore, for simplicity, described flow process Figure 200 be referred to before about Fig. 1 open in some square of describing.But, in described flow process Figure 200, make use of other heating zone and other unit, to reclaim other heat from described hydrocarbon pyrolysis method.Especially, described flow process Figure 200 comprises the one or more unit 202 being coupled to the 3rd heat exchanger 204, and described 3rd heat exchanger 204 is connected between described second heat exchanger 108 and described fractionator 110.Described one or more unit 202 and the 3rd heat exchanger 204 are arranged, to be provided for the other of described practical fluid or the 3rd heating zone and cooling is from the effluent of described second heat exchanger 108 further, then described effluent is provided to described fractionator 110.
First, square 120-128 is similar to discussion operation above.But the effluent from square 128 can be led to described one or more unit 202 in square 212.Described one or more unit 202 can be used to reclaim other heat by the effluent from described second heat exchanger 108, and can be used to increase the temperature head between described second heat exchanger 108 and described 3rd heat exchanger 204, to improve the heat recuperation in described system further.Especially, described one or more square 212 can comprise one or more vapour generator, pressure producer, low pressure generator or their combination such as, to reclaim other heat and to increase the temperature head between described second heat exchanger 108 and described 3rd heat exchanger 204.
Howsoever, heat can be reclaimed by by the described effluent by described one or more unit 202, as shown in square 214.About the discussion of described first heat exchanger 104 and the second heat exchanger 108 above being similar to, the heat of described effluent can be delivered to described practical fluid by the 3rd heat exchanger 204, and the 3rd heat exchanger 204 can be such as tube and shell heat exchanger.In this stage, described effluent can be cooled to the 3rd heat exchanger outlet temperature by from the temperature in described 3rd heat exchanger 204 ingress.This temperature range in described 3rd heating zone 204 can change again, depends on the operating and setting of described different hydrocarbon charging and other unit in described configuration.
Then, at square 130, the effluent from described 3rd heat exchanger 204 can be provided to another unit, to process described effluent further, this can be similar to discussion above.
As the part of heat recuperation being advised arrangement, described practical fluid is heated by various sections, as above in conjunction with described by square 134-138.But, in this flow process Figure 200, perform other or the 3rd heating zone.First, in square 132, described practical fluid is provided.Then, described practical fluid is heated in block 216.Especially, described practical fluid can be heated by described effluent by described 3rd heat exchanger 204.In this heating zone, the described effluent in described 3rd heat exchanger 204 is in the temperature higher than described practical fluid, to such an extent as to described 3rd heat exchanger 204 can heat described practical fluid and described practical fluid can cool described effluent.Then, described practical fluid can be heated further and is used by other method, as discussed in square 134-140 above in other heat exchanger 104 and 108 and described hydrocarbon pyrolysis unit 102.
Be similar to the discussion regarding to Fig. 1, the temperature of described various unit can change, and depends on that the quality of hydrocarbon charging or other operation are considered.For typical operation, described heater outlet temperature, described first heat exchanger entrance and temperature out, separator inlet and temperature out, and the second heat exchanger entrance and temperature out can be similar to example above.But, described 3rd heat exchanger entrance temperature can in the scope of about 265 ° of C-about 160 ° of C (509 °F-320 °F), and described 3rd heat exchanger outlet temperature can between about 210 ° of C and about 125 ° C (about 410 °F-Yue 257 °F).
And for described heat recovery method, described practical fluid can relate to and pressure and temperature similar to those pressure and temperatures in the discussion of Fig. 1 just pointed by described first heat exchanger, the second heat exchanger and pyrolysis unit above.Practical fluid for described 3rd heat exchanger can from about 50 ° of C of ingress to about 250 ° of C (122 °F-482 °F) in exit, preferably from about 110 ° of C of ingress to about 175 ° of C (230 °F-347 °F) in exit, or more preferably operate from the temperature in the scope of about 136 ° of C to about 157 ° of C in exit of ingress.
As will be appreciated, various other embodiments can be utilized, to improve the heat recuperation for described hydrocarbon pyrolysis system further.As an example, described one or more unit 202 can comprise the middle pressure steam producer be connected between described second heat exchanger 108 and described 3rd heat exchanger 204.This producer can be used to produce for heating, the general steam of boiling etc. again, and/or it can be used to produce the dilution steam generation for described hydrocarbon pyrolysis method or another kind of method.Namely, described dilution steam generation can mix before described hydrocarbon pyrolysis unit 102 or in described hydrocarbon pyrolysis unit 102 with described hydrocarbon charging, improving yield, alleviate coking and prevent the metallurgy of the pipe in described stove or relative unit, described hydrocarbon pyrolysis unit 102 can be steam cracking reaction device.Described middle pressure producer can operate steam under the pressure of the about 150psig (1,034kpa) of described stove ingress.Therefore, described middle pressure producer produces the steam under about this pressure easily, makes it be applicable to dilution steam generation well and produces.As another example, described one or more unit can comprise the low pressure generator be connected between described second heat exchanger 108 and described 3rd heat exchanger 204.This producer can be used to produce for heating, boiling or the general steam of other appropriate process again.In another example, middle pressure producer and low pressure generator can be connected between described second heat exchanger and described 3rd heat exchanger.
Except above embodiment, various unit can be bypassed, to provide other function.Such as, in described flow process Figure 200, before being provided to described first heat exchanger 104, the flowing of described practical fluid can comprise bypass by one of upstream heat exchanger (such as described second heat exchanger 108 or the 3rd heat exchanger 204).That is, described second heat exchanger 108 can receive practical fluid from source such as boiler or degasser, and provides it to described first heat exchanger 104 (walking around described 3rd heat exchanger 204).Or described 3rd heat exchanger 204 can receive practical fluid from source such as boiler or degasser, and provides it to described first heat exchanger 104 (walking around described second heat exchanger 108).This technical process can be used to the heating managing described practical fluid.
As another example, before being provided to described first heat exchanger 104, the described of upstream heat exchanger (such as described second heat exchanger 108 or the 3rd heat exchanger 204) come in comfortable described practical fluid stream can by described hydrocarbon pyrolysis unit 102 (such as the convective region of described stove) by the practical fluid heated.This can be provided for the other heating zone of described practical fluid.That is, described practical fluid can be preheated, and then such as described practical fluid transforms becomes super high pressure fluid as steam by described first heat exchanger 104.This configuration can effectively utilize available too much heat in described convective region.
As another example, the described of upstream heat exchanger (such as described second heat exchanger 108 or the 3rd heat exchanger 204) come in comfortable described practical fluid stream by described hydrocarbon pyrolysis unit 102 (such as the convective region of described stove), and can be passed to described first heat exchanger 104 by the practical fluid heated.This arrangement can walk around described first heat exchanger 108, but still for described practical fluid provides two or more heating zones.That is, described practical fluid can be preheated by described second heat exchanger 108 and/or the 3rd heat exchanger 204, then makes it by described hydrocarbon pyrolysis unit 102, becomes super high pressure fluid as steam to make described practical fluid.
No matter the specific embodiments (arrangement of such as unit described in described hydrocarbon pyrolysis system or configuration) of described system how, should utilize controlling mechanism to remove to manage described heat.That is, described hydrocarbon pyrolysis system should comprise heat controlling machine system, with the total amount of the heat controlling to remove from described effluent in order to a variety of causes and the heat that is provided to described practical fluid.First reason of such heat controlling machine is, the amount of the heat removed from described effluent in described various heat exchanger and other unit any may need to be managed, because the operation of described system becomes severe in time or change.Because the temperature range of some unit as concrete in small-sized fractionator is in the process wished, the heat removed from described effluent must be managed.Otherwise the structure of unit can not produce the quantity of reflux of hope in described small-sized fractionator.
One of described heat controlling machine can comprise by-pass valve and bypass line, and they control the temperature of practical fluid to the flow of some heat exchanger and the described practical fluid at described different units.Adopt this mechanism, one or more by-pass valve and bypass line can be performed by with certain arrangement, for walking around or control flowings one or more in the heat exchanger in practical fluid to one or more embodiment discussed above.Namely, that can walk around in described heat exchanger is one or more, to manage the heating of described practical fluid, make the temperature of the practical fluid entering described stove can be controlled to optimize described stove heat balance, or also can be used to the cooling of effluent in described various heat exchanger managing described stove.
Another kind of heat controlling machine system can comprise and is provided to the use of described one or more producer as the one or more back-pressure controller on the fluid of low pressure generator and/or middle pressure producer.As an example, if use low pressure steam generator in the system between described second heat exchanger and the 3rd heat exchanger, in this producer, so increase the boiling point that pressure will raise at water/steam side, this raises the temperature out in technique side.The amount of the heat that can be removed in described second heat exchanger limits by temperature head between process-stream and described water or practical logistics.Net result is, in described low pressure steam generator, temperature and the energy content of the described process flow effluent of described second heat exchanger is left in raised pressure increase.As another example, back-pressure controller can be used to middle pressure producer.This back-pressure controller can be similar to and operate about described low pressure generator the operation described.Also the replenishment control of the back-pressure controller of described low pressure generator can be used as, if described middle pressure producer uses together with the low pressure generator of sequence arrangement to the control of described middle pressure producer.Because middle pressure steam is usually more valuable than low-pressure steam, raise back pressure that low pressure occurs as controlling the first measure of removing of heat and the back pressure (if the further reduction in requiring heat to remove) then raised in middle pressure steam generation may be preferred.
The heat reclaimed in a heat exchanger can be sizable.Therefore, some configuration can comprise multiple heat exchangers of parallel arrangement.Each in these heat exchangers can be connected to other unit, such as low pressure generator and/or middle pressure producer.Such as, each in described heat exchanger row can comprise the be one another in series heat exchanger connected, middle pressure producer, low pressure generator and another heat exchanger.And in this configuration, described parallel heat exchanger row can comprise segregaion valve, and each in arranging to allow described heat exchanger is excluded from service (such as off-line), so that clean or maintenance.Similarly, another kind of heat controlling machine system can be use described segregaion valve to block described effluent to the one or more flowing in described heat exchanger row, if heat remove require low.By this way, described different row can be added or remove, to manage described heat recuperation further.
And as will be appreciated, described different heat controlling machine system can be used together in certain embodiments, to provide the other handiness that in described system, heat transmission controls.Such as, described by-pass valve can use together with the back-pressure controller for middle pressure producer with the back-pressure controller for low pressure generator with bypass line.Be similar to discussion above, first can use the back-pressure controller on described low pressure generator, then can use the back-pressure controller on described middle pressure producer, and finally can use described by-pass valve and bypass line.
By this way, described system efficiency by based on described by the value control of practical fluid of heating.That is, described heat controlling machine system can be utilized to produce more SHP steam, and it is typically valuable than middle pressure steam, and middle pressure steam is more valuable than low-pressure steam.As an example, effluent heat can be used to produce SHP steam, its such as can be used to other district of described device as described in the recovery zone of steam cracker drive large turbine.And although the steam of lower pressure has the fact of the practicality (because it can not carry the useful work of as much) less than SHP steam, the steam produced at low pressures also can be useful for described some operation intrasystem.Such as, the steam of lower pressure can be used as stove dilution steam generation or be used in the tower that seethes with excitement again.As a result, heat recovery method can increase the efficiency of the operation of described system, if it reclaims the heat of several levels and uses it in an efficient way.
As a specific examples of the arrangement of the unit in described hydrocarbon pyrolysis system, Fig. 3 provides and reclaims the block diagram of heat according to another exemplary substituted of the technology of the present invention by the effluent of the hydrocarbon pyrolysis.In this block diagram 300, described hydrocarbon pyrolysis system can comprise various unit, such as stove 302, first heat exchanger (such as main conveyor line interchanger) 304, vapour/liquid separator 306, the second heat exchanger (such as the first shell-and-tube exchanger) 308, middle pressure producer 310, low pressure generator 312, the 3rd heat exchanger (such as the second shell-and-tube exchanger) 314, and small-sized fractionator 316.Each in these unit can be arranged with by concrete structure fluid communication with each other together with being coupled to by various connection (such as pipe, junctor, valve etc.), as being readily appreciated by one skilled in the art.And the effluent of described practical fluid and described stove can be unmixed logistics separated from described outlet of still to described 3rd heat exchanger outlet.
Described method is supplied to stove 302 with hydrocarbon charging through pipeline 303 and is started.Described hydrocarbon charging also can be merged with diluted fluid such as the steam provided by pipeline 305.Described hydrocarbon charging can by cracking in described stove 302 to produce effluent, and this effluent is provided to described first heat exchanger 304, and then described effluent is passed to described vapor liquid separator 306.Described vapor liquid separator 306 divided gas flow effluent becomes two different logistics with liquid efflunent.Especially, after the described effluent of initial cooling in described first heat exchanger 304, described vapor liquid separator 306 can be used to liquid efflunent (such as bottom product, the tar of such as steam cracking) to be separated with gaseous effluent.In some embodiments, after leaving described first heat exchanger 304, described cooled effluent logistics can by between the outlet and the entrance of described vapor liquid separator 306 of described first heat exchanger 304 with the liquid quench oil introduced through quenching pipeline 319 or liquid water quenching, to provide supplementary cooling.Liquid efflunent from described vapor liquid separator 306 can be removed by through pipeline 322, and can further in other unit (not shown).
Described gaseous effluent is supplied to the unit group be connected in series by described vapor liquid separator 306, it comprises described second heat exchanger 308, described middle pressure producer 310, described low pressure generator 312, and described 3rd heat exchanger 314.This unit group can be used to cool described effluent before described effluent is led to described small-sized fractionator 316.In this unit group, described middle pressure producer 310 and low pressure generator below 312 can be used to produce for other unit as described in the steam of other device in small-sized fractionator 316 or this system or other system.The configuration advised can be particularly advantageous for described small-sized fractionator 316, because the comparatively high temps that can obtain in described producer 310 and 312 can be used for other practical fluid preheating by it.Described small-sized fractionator 316 can be coupled to other downstream units, to process described effluent logistics further and to isolate the alkene of described hope.
As noted above, the use of described different heat exchanger 304,308 and 314 and described stove 302, provides the various heating zones for the practical fluid provided through pipeline 320.Described practical fluid can be provided by boiler or degasser (not shown), and can comprise the boiler feed water as described intrasystem practical fluid.In this configuration, first described practical fluid can be heated in described 3rd heat exchanger 314, then by described second heat exchanger 308 and then in described first heat exchanger 304 heat, or by preheating in described stove 302, then described practical fluid is heated by final in described stove 302 and be supplied to other device in outlet 324 as turbine, other unit, or as inputting the input logistics of different methods.
In order to control described intrasystem heat transmission, described heat controlling machine system can comprise by-pass valve 323, its through bypass line, pipe etc. be connected to described practical fluid intake pipeline 320, between described 3rd heat exchanger 314 and the outlet of described second heat exchanger 308.Described by-pass valve 323 may be constructed such certain forms to limit the flowing of practical fluid to described unit, or may be constructed such certain forms to be provided to the flowing of one of the outlet of described 3rd heat exchanger 314 and described second heat exchanger 308.As an example, in first location, described by-pass valve 323 may be constructed such certain forms with limit described practical fluid led to described 3rd heat exchanger 314 from boiler or degasser at least partially and through bypass line by described for the guiding at least partially of described practical fluid the first heat exchanger 304.Similarly, in the second position, described by-pass valve 323 can by described practical fluid be directed to from source at least partially described 3rd heat exchanger 314 and the described practical fluid of restriction at least partially by described bypass line to described first heat exchanger 304.As will be appreciated, the restriction of described flowing can block flow or only block the part of described flowing, depends on utilized valve and pipeline.
In addition, other heat controlling machine system comprises middle pressure valve 326 and low pressure valve 328.As discussed above, these valves 326 and 328 can be used to the temperature of the gaseous effluent controlled respectively by middle pressure producer 310 and low pressure generator 312.Described middle pressure valve 326 is coupled to described middle pressure producer 310 by between the entrance 330 and the outlet 332 of middle pressure steam of boiler feed fluid.Described low pressure valve 328 is coupled to described low pressure generator 312 by between the entrance 334 and the outlet 336 of low-pressure steam of boiler feed fluid.Especially, described middle pressure valve 326 can be used to increase pressure in described middle pressure producer 310 to raise the boiling point of described boiler feed water, and this raises the temperature out of described middle pressure producer 310.Similarly, described low pressure valve 328 can be used to increase pressure in described low pressure generator 312 to raise the boiling point of described boiler feed water, and this raises the temperature out of described low pressure generator 312.
The concrete temperature adopted in the operation of described system can change, and depends on concrete configuration.Such as, the outlet of described stove 302 can be operating as about 760 ° of C (about 1400 °F), and this temperature can be identical with the temperature of the ingress of described first heat exchanger 304.Described first heat exchanger 304 and directly quenching oil or water can cool the temperature of described effluent to about 300 ° of C (about 572 °F), this be for separating of temperature.Gaseous effluent from described separator 306 can be supplied to described second heat exchanger by with the temperature of about 299 ° of C (about 570 °F), and it is cooled to the temperature of about 260 ° of C (about 500 °F).Then described effluent can be supplied to the 3rd heat exchanger 314 by described producer 310 and 312 with by with the temperature of about 166 ° of C (about 330 °F).Described 3rd heat exchanger 314 can cool the temperature of described effluent to about 154 ° of C (about 310 °F).
Described practical fluid can utilize described various sections, to heat described practical fluid, as discussed above.Especially, for this example, described practical fluid can be supplied to described 3rd heat exchanger by with the temperature of about 125 ° of C (about 257 °F).Described 3rd heat exchanger can use described effluent to heat the temperature of described practical fluid to about 149 ° of C (about 300 °F).Then, described practical fluid can be provided to described second heat exchanger 308, and it can heat the temperature of described practical fluid to about 268 ° of C (about 515 °F) further.Then described practical fluid can be heated to the temperature of about 316 ° of C (about 600 °F) in described first heat exchanger 304.Then, described practical fluid can be heated to the temperature of about 538 ° of C (about 1000 °F) further by the convective region at stove 302.
Fig. 4 reclaims another block diagram of heat according to another exemplary substituted of the technology of the present invention by the cooling of the hydrocarbon effluent of cracking.In the figure, described hydrocarbon charging is by two separators 402 and 404, and they are coupled to described hydrocarbon pyrolysis unit 302.These separators 402 and 404 are used as separating at high temperature drum, and they removed Residual oil and asphaltene molecules before hydrocarbon charging enters the radiation zone of hydrocarbon pyrolysis unit 302 from hydrocarbon charging.Beneficially, the use of described separator 402 and 404 can utilize by the practical fluid heated in this concrete configuration, to improve the efficiency of described system further and to optimize olefin recovery further.
Typically, the steam cracking furnace of use separator as being incorporated into the exterior knockout drum between convective region and radiation zone is the highest only runs to about 454 ° of C (about 850 °F).These typical configurations are recorded in other patent, such as U.S. Patent number 7, and 097,758; 7,138,047; 7,193,123; 7,235,705 and 7,247,765.The equipment of separator downstream described in excessive pickup may be caused in the operation of more than 454.4 ° of C (about 850 °F).This pickup may be the result of two reaction mechanism.The first, the steam in described separator more than tangential inlet is through thermo-negative reaction cracking, and described separator loses some heats.These effects merge with temperature about 7 ° of C reducing described steam to about 1 ° of C.Because described steam is at its dew point when described steam enters described separator, any cooling is by molecule the heaviest for condensation.Vapor/liquid EQUILIBRIUM CALCULATION FOR PROCESS is predicted, the heavy liquid (being entrained in described steam) obtained is rich in 760 ° of C+ (1400 °F+) molecule, and they are coke precursors.The second, the condensation reaction of described heavy liquid experience, described reaction produces larger polynuclear aromatic compound, finally causes described polynuclear aromatic compound to become coke.
As the result of this pair of reaction mechanism, pickup typically appears at two positions, and they are tubing system and the radiation entrance manifold (RIM) of described separator downstream.Pickup in described RIM may produce by being retained in some pickup precursors of vaporizing in described vapor phase or in convective region, bottom.In described convective region, cracking and some condensation reactions occur, but because technological temperature rises, do not have liquid to be formed.These reactions can experience fast condensation reaction (2 grades of kinetics are probably deferred in condensation reaction) subsequently.But, in crossover piping and RIM, the endothermic pyrolysis of calorific loss and continuation reaction cooling described technique about 10 ° of C-about 38 ° of C (about 50 °F-Yue 100 °F).Here, described condensation reaction is also even quickly in described vapor phase.Once temperature drops to below the dew point of the polynuclear aromatic compound of these new condensations, they become liquid and coke rapidly, they with relatively low deposited at rates in described RIM.
Therefore, reduce residence time in described separator can less pickup to the level being convenient to manage.This aspect can reduce the pickup in the tubing system of described separator downstream.But, this can not reduce the pickup in crossover piping and/or inlet manifold, because described 760 ° of C+ (the 1400 °F+) vapour molecule entering described separator still exists in the convective region of bottom, crossover piping and RIM, cracking and condensation still can occur there.In fact, the residence time reduced in described drum can be increased in the pickup in described RIM.
Petroleum naphtha in the hydrocarbon pyrolysis unit (it can be steam cracking furnace) with separator, kerosene and hydrocracking oil breaking show, 760 ° of C+ (1400 °F+) molecules can cause described pickup, are not only described cracking and condensation reaction.Described hydrocarbon charging typically enters separator 490 ° of C-502 ° of C (915 °F-935 °F), and described temperature is than atmospheric resids height about 21 ° of C-32 ° of C (about 70 °F-90 °F).The temperature that the identical separator residence time is experienced in described charging and bottom line is higher than atmospheric resids (it has insignificant pickup) in convective region, bottom, crossover piping and RIM.Therefore, owing to not having large (760 ° of C+ (1400 °F+)) molecule, described condensation reaction does not produce enough large with the molecule becoming liquid when technological temperature declines in described crossover piping and RIM.Therefore, in described steam, remove described 760 ° of C+ (1400 °F+) molecule can be useful, not only reduces the separator residence time.
In this embodiment, the described SHP by making described practical fluid be produced by described hydrocarbon pyrolysis unit (such as stove 302) can be used together with 404 with described separator 402, to reduce the pickup in described system.In this configuration, the cut from described separator 402 can be dark (deep), produces molecule (such as 760 ° of C+ (1400 °F+)) with the coke of vaporizing quite a large amount of.Clean steam cracking feed in a small amount also can be added in described overhead vapours by venturi mixer 406.Coke described in this clean steam cracking feed condensation produces molecule.The liquid produced in described venturi mixer 406 is removed by by described separator 404.Described steam is transported to convective region, bottom by from described separator 404, is then transported to radiation zone.Adopt the steam that described 760 ° of C+ (1400 °F+) remove, pickup is insignificant, allows described separator 402 and 404 in the high-temperature operation of 482 ° of C-510 ° of C (900 °F-950 °F).
Far and away, the benefit reducing pickup is the ability operating described separator at higher temperature.Described higher service temperature adds vaporization and is cracked into the Residual oil of valuable product or the mark of crude oil subsequently.But described separator bottoms becomes more tacky, per unit mass requires that more low viscous solubility promoter (fluxant) is to meet oil fuel viscosity specification.But because nominal cut point temperature increases, total bottoms adding thinner is still significantly less.Such as, the nominal cut point temperature of Arab heavy crude is increased to 593 ° of C (being increased to 1100 °F from 1000 °F) (with that described bulging temperature is increased to 504 ° of C (being increased to 940 °F from 840 °F) from 449 ° of C is approximately identical) from 538 ° of C, the described bottoms adding thinner is reduced to 40 pounds of (18kg)/100 pound (46kg) crude oil from 47 pounds (lbs) (21 kilograms (kg))/100 pounds of (46kg) crude oil.That is, other 7 pounds of (3kg)/100 pound (46kg) crude oil is cracked into valuable product.
In order to operate, hydrocarbon charging such as crude oil or Residual oil are preheated by upper convection section, and then described hydrocarbon charging mixes with overheated dilution steam generation.Described overheated dilution steam generation can be provided by outlet 324 discussed above.Described mixture is heated in described convective region further, and this can comprise and is heated to such as about 510 ° of C (about 950 °F).Because described tubing system, by remaining large liquid distillate continuous washing, does not have coke to be formed.By the tubing system comprising various bend pipe and joint, described two-phase process-stream is transported to separator 402 and 404.Described bend pipe tends to spray (mistflow) is transformed into laminar flow or the stream that goes in ring.Described separator 402 and 404 greatly can reduce the size of the pipeline leading to described separator 402 and the size both separator 402 and 404.That is, because described separator 402 with 404 in series, fluid flow communication is connected, each separator effectively need not be separated steam and liquid as single separator.Such as, if the liquid of 1% only carried secretly by single separator, two separators of series connection can carry the liquid of 10% separately secretly, cause identical total 1% liquid entrainment.As a result, described double separator tangential inlet internal diameter (ID) can be less than single separator by about 50%, and described separator ID can be less than single separator by about 1/3rd.Therefore, even if there are two separators, total required separator metal is less than single separator by about 50%.
Leave the steam of described separator 402 and some liquid are transported to venturi mixer 406, described steam is by diesel oil, hydrocrackates, wax, condensation product or even quenching oil partial quench there.Described quenching turbulence mixing and the heaviest molecule of vaporizing in described vapor phase, molecule the heaviest described in condensation simultaneously.Described venturi mixer 406 does not have any described liquid can the stagnation point of coking there.This is advantage compared with dish or filler, and in dish or filler, static liquid can become coke.The amount of quenching is little, to reduce 760 ° of C+ (1400 °F+) molecule in described steam close to an order of magnitude.This aspect is indicated by table 1 below.
The rightest hurdle of this table shows, removes 0.68 mmbtu/hour (MBtu/hr) (199 kilowatts (kW)) and to reduce in described steam 760 ° of C+ (1400 °F+) molecules 6 times.Energy balance computational prediction, the quenching of about 1,300 (lb/hr) (591kg/hr) removes described 0.68MBtu/hr (199kW).The pipeline in described venturi mixer 406 downstream has bend pipe, spray is transformed back laminar flow or annular-flow before entering described separator 404.Described process-stream enters described separator 404 through one or two tangential inlet.Because divide described logistics may cause imbalance of flow and rest point, a tangential inlet can be preferred.Single entrance separator 404 and the pipeline to it can be greater than two entrance separators 402 more or less.
Described separator 404 removes the remaining liq of about 90%, obtains the total vapor/liquid separation efficiency of 99%.In a preferred embodiment, once set up laminar flow or annular-flow in the pipeline of each leading to described separator 402 and 404, first described process mixture can enter the taper(ed)pipe increasing ID10%-20%, then enters the pipeline with these larger ID.Vapor/liquid separation efficiency can be increased to 99.5%-99.7% from 99% by the reduction (reducing 17%-31%) of this process speed of separator 402 and 404 upstream.Be similar to described separator 402, described separator 404 can have boot-shaped leg (boot), and bottoms is by quenching to about 343 ° of C (650 °F) there, reacts to stop cracking and coking.Optionally, then described liquid return bend pipe trap by two, then mixes with the process-stream of described separator 402 upstream.This pair returns bend pipe and provides the pressure head required for flowing performing and enter the pipeline of described separator 402 upstream.The overhead vapours from separator 404 with significantly less 760 ° of C+ (1400 °F+) molecule by the further preheating in convective region, bottom with by crossover piping and RIM, has minimum pickup.Then described hydrocarbon charging is further processed in radiation zone cracking, as discussed above.
Also other embodiment can be utilized, to improve the operation of this configuration further.Such as, steam stripped can be provided at entrance 410.The steam stripped of the bottoms of separator 402 can be used to vaporize the light material be trapped in heavy residual bottoms, produces other hydrocarbon charging.And overheated steam (it can be provided by outlet 324) can be added to the vapor space of more than the entrance of separator 404 at entrance 408.This embodiment can prevent any upstream being condensate in convective region, bottom from occurring.And in another embodiment, described radiation zone may be constructed such higher more or less, this allows lower cross-over connection temperature (XOT), and does not have too much radiations heat energy flow and coking.Lower XOT can significantly increase gas oil cracking selectivity and yield of ethene.
In another embodiment, the technology of the present invention relates to:
1. the method for cracking hydrocarbon charging, described method comprises:
Hydrocarbon is provided to be fed into hydrocarbon pyrolysis unit, to produce the effluent of cracking;
Make the effluent of the described cracking from described hydrocarbon pyrolysis unit at least partially by the first heat exchanger;
Gaseous effluent and liquid efflunent is separated at least partially described in the effluent of the described cracking from described first heat exchanger;
Make described gaseous effluent at least partially by the second heat exchanger;
Fractionator is led at least partially described in the described effluent from described second heat exchanger;
By making practical fluid by described second heat exchanger from reclaiming heat described in described effluent at least partially in described second heat exchanger; With
By making described practical fluid from described second heat exchanger by described first heat exchanger, in described first heat exchanger, described in the effluent of described cracking, reclaim heat at least partially.
2. the method for paragraph 1, it comprises the described practical fluid that makes from described first heat exchanger by described hydrocarbon pyrolysis unit, to heat described practical fluid.
3. the method for paragraph 1 and 2, it leads to one or more vapour generator at least partially before being included in and a described part for the described effluent from described second heat exchanger being led to described fractionator described in the described effluent from described second heat exchanger.
4. the method for paragraph 3, it is included in before leading to described fractionator at least partially described in described effluent, leads to the 3rd heat exchanger at least partially by described in the described effluent from described one or more vapour generator.
5. the method for paragraph 4, it is included in before leading to described fractionator at least partially described in the described effluent from described one or more producer, by making described practical fluid reclaim heat by described 3rd heat exchanger at least partially described in the described effluent from described one or more vapour generator in described 3rd heat exchanger.
6. the method for any one in earlier paragraphs, it comprises the valve regulated on described one or more vapour generator, to control from heat recuperation at least partially described in the effluent by described one or more vapour generator.
7. the method for any one in earlier paragraphs, wherein said practical fluid was heated by degasser before by described first heat exchanger.
8. the method for any one in earlier paragraphs, it comprises and is driven turbine with from the described of described first heat exchanger by the practical fluid heated.
9. the method for any one in earlier paragraphs, wherein before being separated of described gaseous effluent and described liquid efflunent, from the described cracking of described first heat exchanger effluent described in direct quenching, be cooled to the temperature of the tar condensing at least formed by the reaction between the component of described effluent at least partially.
10. hydrocarbon pyrolysis system, it comprises:
Hydrocarbon pyrolysis unit, its be built into certain forms with:
Receive hydrocarbon charging; With
The effluent of cracking is produced by described hydrocarbon charging;
First heat exchanger, itself and described hydrocarbon pyrolysis unit fluid connected sum be built into certain forms with:
Cool from the described cracking of described hydrocarbon pyrolysis unit effluent at least partially; With
Heat practical fluid at least partially; With
Separator, itself and described first heat exchanger fluid connected sum are built into certain forms to be separated into liquid efflunent and gaseous effluent at least partially by described in the effluent of described cracking;
Second heat exchanger, itself and described separator fluid connected sum be built into certain forms with:
Cool from described separator described gaseous effluent at least partially;
Described practical fluid was heated before described first heat exchanger to receive described in described practical fluid at least partially; With
Fractionator, itself and described second heat exchanger fluid connected sum are built into certain forms to receive described in the described effluent from described second heat exchanger at least partially.
The system of 11. paragraphs 10, wherein said hydrocarbon pyrolysis unit be built into certain forms with: to heat described in the described practical fluid from described first heat exchanger at least partially, be wherein kept at least partially in non-mixed logistics separately with described in the effluent of described cracking at least partially described in practical fluid described in described hydrocarbon pyrolysis unit.
The system of 12. paragraphs 10, it comprises one or more vapour generator, described vapour generator fluid is communicated with between described second heat exchanger and described fractionator, and is built into certain forms to make to lead to described fractionator at least partially described in the described effluent from described second heat exchanger.
The system of 13. paragraphs 12, it comprises the 3rd heat exchanger, 3rd heat exchanger fluid is communicated with between described one or more vapour generator and described fractionator, and be built into certain forms, cooling before leading to described fractionator at least partially described in described effluent described in described effluent at least partially.
The system of 14. paragraphs 13; wherein said 3rd heat exchanger is communicated with described second heat exchanger fluid; and being built into certain forms with before the described practical fluid of described second heat exchanger reception, described in described effluent, reclaiming heat by described 3rd heat exchanger at least partially by making described practical fluid; Wherein in described second heat exchanger, described practical fluid and the described of described effluent are kept at least partially in non-mixed logistics separately.
The system of 15. paragraphs 14, it comprises by-pass valve, and this by-pass valve is connected to the source of described practical fluid, between described first heat exchanger and described 3rd heat exchanger, and be built into certain forms with:
In first location, described 3rd heat exchanger is led in the first part limiting described practical fluid from described source, and by the remaining first part of described practical fluid through described first heat exchanger of bypass line guiding; With
In the second position, guide the second section of described practical fluid to lead to described 3rd heat exchanger from described source, and the second remainder of the described practical fluid of restriction is by described bypass line extremely described first heat exchanger.
The system of any one in 16. earlier paragraphs 12-15, it comprises control valve, this control valve be coupled to described one or more vapour generator one of at least, and be built into certain forms to control described in the described effluent by described one or more vapour generator cooling at least partially.
The system of any one in 17. earlier paragraphs 10-16, it comprises degasser, this degasser is communicated with described second heat exchanger fluid, and is built into certain forms with practical fluid described in preheating before described practical fluid is led to described second heat exchanger.
The system of any one in 18. earlier paragraphs 10-17, wherein said first heat exchanger is built into certain forms, with cooling from the described cracking of described hydrocarbon pyrolysis unit effluent described at least partially and to provide described in the effluent of described cracking at least partially to direct quenching, it is described at least partially to the temperature of reacting the tar condensing of formation between the described component at least partially by the effluent of described cracking that this direct quenching cools the effluent of described cracking.
The system of any one in 19. earlier paragraphs 10-18, it comprises driving turbine, this driving turbine be built into certain forms with receive from described hydrocarbon pyrolysis unit described by described in the practical fluid that heats at least partially.
The system of any one in 20. earlier paragraphs 10-19, wherein said practical fluid and the described of described effluent are kept at least partially in non-mixed logistics separately.
The method of 21. steam cracking of hydrocarbons chargings, described method comprises:
Hydrocarbon is provided to be fed into hydrocarbon pyrolysis unit, to produce the effluent of cracking;
Be separated from the described cracking of described hydrocarbon pyrolysis unit effluent at least partially, wherein gaseous effluent is separated with the liquid efflunent of the tar comprising steam cracking;
Described gaseous effluent is cooled at least partially in the first heat exchanger;
One or more vapour generator is led at least partially described in the described effluent from described first heat exchanger;
To cool described in the described effluent from described one or more vapour generator at least partially in the second heat exchanger; With
Fractionator is led at least partially described in the described effluent from described second heat exchanger.
The method of 22. paragraphs 21, it is included in before leading to separator at least partially described in the effluent of described cracking, makes described in the effluent from the described cracking of described hydrocarbon pyrolysis unit at least partially by the 3rd heat exchanger.
The method of any one in 23. earlier paragraphs 21 and 22, it comprises by making practical fluid heat described practical fluid by described hydrocarbon pyrolysis unit and using described by the practical fluid heated in other technique.
The method of 24. paragraphs 23, its make described practical fluid by hydrocarbon pyrolysis unit before, by making described practical fluid reclaim heat by described first heat exchanger at least partially described in described effluent in described first heat exchanger.
The method of 25. paragraphs 24, it is included in and makes described practical fluid by before described first heat exchanger, by making described practical fluid reclaim heat by described second heat exchanger at least partially described in described effluent in described second heat exchanger.
The method of 26. paragraphs 25, it comprises and regulates valve on described one or more vapour generator, to control from heat recuperation at least partially described in the described effluent by described one or more vapour generator.
The method of 27. paragraphs 24, wherein before passing through described first heat exchanger, described practical fluid is heated by degasser.
The method of 28. paragraphs 22, the described of the effluent of wherein said cracking is reacted the temperature of the temperature of the tar condensing of formation between being cooled in described 3rd heat exchanger at least higher than the component by described gaseous effluent at least partially.
The method of any one in 29. earlier paragraphs 23-28, wherein uses the described step by the practical fluid heated to comprise and is driven turbine with described by the practical fluid heated in described other technique.
30. gaseous effluent treatment systems, it comprises:
Hydrocarbon pyrolysis unit, its be built into certain forms with:
Receive hydrocarbon charging; With
The effluent of cracking is produced by described hydrocarbon charging; With
Separator, it is communicated with described hydrocarbon pyrolysis unit fluid, and is built into certain forms and has liquid efflunent and the gaseous effluent of the tar of steam cracking with being separated at least partially of the effluent by the described cracking from described hydrocarbon pyrolysis unit; With
First heat exchanger, it is communicated with described separator fluid, and be built into certain forms with cooling from described separator described gaseous effluent at least partially;
One or more vapour generator, it is communicated with described first heat exchanger fluid, and be built into certain forms with receive from described first heat exchanger described effluent described at least partially;
Second heat exchanger, it is communicated with described one or more producer fluid, and be built into certain forms with cooling from described one or more vapour generator described effluent described at least partially; With
Fractionator, it is communicated with described second heat exchanger fluid, and be built into certain forms with receive from described second heat exchanger described effluent described at least partially.
The system of 31. paragraphs 30, it comprises the 3rd heat exchanger, 3rd heat exchanger fluid be communicated with between described separator and described hydrocarbon pyrolysis unit, and be built into certain forms be cooled through described 3rd heat exchanger to described separator described cracking effluent described at least partially.
The system of 32. paragraphs 30, wherein said hydrocarbon pyrolysis unit is built into certain forms, with by making practical fluid heat described practical fluid by described hydrocarbon pyrolysis unit.
The system of 33. paragraphs 32, wherein said first heat exchanger is built into certain forms, with make described practical fluid by hydrocarbon pyrolysis unit before, by making described practical fluid reclaim heat by described first heat exchanger at least partially described in described effluent in described first heat exchanger.
The system of 34. paragraphs 33, wherein said second heat exchanger is built into certain forms, with make described practical fluid by described first heat exchanger before, reclaim heat by making described practical fluid by described second heat exchanger.
The system of 35. paragraphs 34, it comprises one or more valve, described valve is coupled to described one or more vapour generator, and is built into certain forms to regulate by heat recuperation at least partially described in the described effluent by described one or more vapour generator.
The system of any one in 36. paragraph 30-34, it comprises
The first separator be communicated with radiation zone fluid with the convective region of described hydrocarbon pyrolysis unit and the second separator;
Described first separator is built into certain forms, to receive hydrocarbon charging by described convective region and described hydrocarbon charging is separated into the first vapor feed and first liquid charging;
Described second separator is built into certain forms, to receive described first vapor feed; Described first vapor feed is separated into the second vapor feed and second liquid charging; Described first separator is led in described second liquid charging; With the radiation zone described second vapor feed being led to described hydrocarbon pyrolysis unit, to produce the effluent of cracking.
For illustrative purposes, aforementioned application is for the specific embodiments of the technology of the present invention.But, it will be apparent to those skilled in the art that to the many modifications and variations of described embodiment described herein be possible.And some embodiments can preferably be carried out at least partially on computer, the embodiment that namely computer of the inventive method performs is preferred, but is not basic.All such modifications and variations intentions are in the scope of the present invention that appended claims defines.

Claims (35)

1. the method for cracking hydrocarbon charging, described method comprises:
Hydrocarbon is provided to be fed into hydrocarbon pyrolysis unit, to produce the effluent of cracking;
Make the effluent of the described cracking from described hydrocarbon pyrolysis unit at least partially by the first heat exchanger;
Gaseous effluent and liquid efflunent is separated at least partially described in the effluent of the described cracking from described first heat exchanger;
Make described gaseous effluent at least partially by the second heat exchanger;
Fractionator is led at least partially described in the described effluent from described second heat exchanger;
By making practical fluid by described second heat exchanger from reclaiming heat described in described effluent at least partially in described second heat exchanger; With
By making described practical fluid from described second heat exchanger by described first heat exchanger, in described first heat exchanger, described in the effluent of described cracking, reclaim heat at least partially.
2. the method for claim 1, it comprises the described practical fluid that makes from described first heat exchanger by described hydrocarbon pyrolysis unit, to heat described practical fluid.
3. the method for claim 1, it leads to one or more vapour generator at least partially before being included in and a described part for the described effluent from described second heat exchanger being led to described fractionator described in the described effluent from described second heat exchanger.
4. the method for claim 3, it is included in before leading to described fractionator at least partially described in the described effluent from described one or more vapour generator, leads to the 3rd heat exchanger at least partially by described in the described effluent from described one or more vapour generator.
5. the method for claim 4, it is included in before leading to described fractionator at least partially described in the described effluent from described one or more vapour generator, by making described practical fluid reclaim heat by described 3rd heat exchanger at least partially described in the described effluent from described one or more vapour generator in described 3rd heat exchanger.
6. the method for claim 3, it comprises and regulates valve on described one or more vapour generator, to control from heat recuperation at least partially described in the effluent by described one or more vapour generator.
7. the process of claim 1 wherein that described practical fluid was heated by degasser before by described first heat exchanger.
8. the method for claim 1, it comprises with being driven turbine from described first heat exchanger by the practical fluid heated.
9. the method for claim 1, wherein before the described gaseous effluent of separation and described liquid efflunent, from the described cracking of described first heat exchanger effluent described in reacted the temperature of the tar condensing of formation between the component that is cooled in direct quenching at least by described effluent at least partially.
10. hydrocarbon pyrolysis system, it comprises:
Hydrocarbon pyrolysis unit, its be built into certain forms with:
Receive hydrocarbon charging; With
The effluent of cracking is produced by described hydrocarbon charging;
First heat exchanger, itself and described hydrocarbon pyrolysis unit fluid connected sum be built into certain forms with:
Cool from the described cracking of described hydrocarbon pyrolysis unit effluent at least partially; With
Heat practical fluid at least partially; With
Separator, itself and described first heat exchanger fluid connected sum are built into certain forms to be separated into liquid efflunent and gaseous effluent at least partially by described in the effluent of described cracking;
Second heat exchanger, itself and described separator fluid connected sum be built into certain forms with:
Cool from described separator described effluent at least partially;
Described practical fluid was heated before described first heat exchanger to receive described in described practical fluid at least partially; With
Fractionator, itself and described second heat exchanger fluid connected sum are built into certain forms to receive described in the described effluent from described second heat exchanger at least partially.
The system of 11. claims 10, wherein said hydrocarbon pyrolysis unit be built into certain forms with heating from described first heat exchanger practical fluid described at least partially, wherein in described hydrocarbon pyrolysis unit described in practical fluid at least partially be kept at least partially described in the effluent of described cracking in non-mixed logistics separately.
The system of 12. claims 10, it comprises one or more vapour generator, described vapour generator fluid is communicated with between described second heat exchanger and described fractionator, and is built into certain forms to make to lead to described fractionator at least partially described in the described effluent from described second heat exchanger.
The system of 13. claims 12, it comprises the 3rd heat exchanger, 3rd heat exchanger fluid is communicated with between described one or more vapour generator and described fractionator, and be built into certain forms, cooling before leading to described fractionator at least partially described in described effluent described in described effluent at least partially.
The system of 14. claims 13, wherein said 3rd heat exchanger is communicated with described second heat exchanger fluid, and being built into certain forms with before the described practical fluid of described second heat exchanger reception, described in described effluent, reclaiming heat by described 3rd heat exchanger at least partially by making described practical fluid; Wherein in described second heat exchanger, described practical fluid and the described of described effluent are kept at least partially in non-mixed logistics separately.
The system of 15. claims 14, it comprises by-pass valve, and this by-pass valve is connected to the source of described practical fluid, between described first heat exchanger and described 3rd heat exchanger, and be built into certain forms with:
In first location, described 3rd heat exchanger is led in the first part limiting described practical fluid from described source, and by the first remainder of described practical fluid through described first heat exchanger of bypass line guiding; With
In the second position, guide the second section of described practical fluid to lead to described 3rd heat exchanger from described source, and the second remainder of the described practical fluid of restriction is by described bypass line extremely described first heat exchanger.
The system of 16. claims 12, it comprises control valve, this control valve be coupled to described one or more vapour generator one of at least, and be built into certain forms to control described in the described effluent by described one or more vapour generator cooling at least partially.
The system of 17. claims 10, it comprises degasser, and this degasser is communicated with described second heat exchanger fluid, and is built into certain forms with practical fluid described in preheating before described practical fluid is led to described second heat exchanger.
The system of 18. claims 10, wherein said first heat exchanger is built into certain forms, with cooling from the described cracking of described hydrocarbon pyrolysis unit effluent described at least partially and to provide described in the effluent of described cracking at least partially to direct quenching, it is described at least partially to the temperature of reacting the tar condensing of formation between the described component at least partially by the effluent of described cracking that this direct quenching cools the effluent of described cracking.
The system of 19. claims 10, it comprises driving turbine, this driving turbine be built into certain forms with receive from described hydrocarbon pyrolysis unit by the practical fluid that heats at least partially.
The system of 20. claims 10, wherein said practical fluid and the described of described effluent are kept at least partially in non-mixed logistics separately.
The method of 21. steam cracking of hydrocarbons chargings, described method comprises:
Hydrocarbon is provided to be fed into hydrocarbon pyrolysis unit, to produce the effluent of cracking;
Be separated from the described cracking of described hydrocarbon pyrolysis unit effluent at least partially, wherein gaseous effluent is separated with the liquid efflunent of the tar comprising steam cracking;
Described gaseous effluent is cooled at least partially in the first heat exchanger;
Described effluent from described first heat exchanger led to one or more vapour generator at least partially;
To cool described in the described effluent from described one or more vapour generator at least partially in the second heat exchanger; With
Fractionator is led at least partially described in the described effluent from described second heat exchanger.
The method of 22. claims 21, it is included in before leading to separator at least partially described in the effluent of described cracking, makes described in the effluent from the described cracking of described hydrocarbon pyrolysis unit at least partially by the 3rd heat exchanger.
The method of 23. claims 22, it comprises by making practical fluid heat described practical fluid by described hydrocarbon pyrolysis unit and using described by the practical fluid heated in other technique.
The method of 24. claims 23, its make described practical fluid by hydrocarbon pyrolysis unit before, by making described practical fluid reclaim heat by described first heat exchanger at least partially described in described effluent in described first heat exchanger.
The method of 25. claims 24, it is included in and makes described practical fluid by before described first heat exchanger, by making described practical fluid reclaim heat by described second heat exchanger at least partially described in described effluent in described second heat exchanger.
The method of 26. claims 25, it comprises and regulates valve on described one or more vapour generator, to control from heat recuperation at least partially described in the described effluent by described one or more vapour generator.
The method of 27. claims 24, wherein before passing through described first heat exchanger, described practical fluid is heated by degasser.
The method of 28. claims 22, the described of the effluent of wherein said cracking is reacted the temperature of the temperature of the tar condensing of formation between being cooled in described 3rd heat exchanger at least higher than the component by described effluent at least partially.
The method of 29. claims 23, wherein uses the described step by the practical fluid heated to comprise and is driven turbine with described by the practical fluid heated in other technique.
30. gaseous effluent treatment systems, it comprises:
Hydrocarbon pyrolysis unit, its be built into certain forms with:
Receive hydrocarbon charging; With
The effluent of cracking is produced by described hydrocarbon charging; With
Separator, it is communicated with described hydrocarbon pyrolysis unit fluid, and is built into certain forms and has liquid efflunent and the gaseous effluent of the tar of steam cracking with being separated at least partially of the effluent by the described cracking from described hydrocarbon pyrolysis unit; With
First heat exchanger, it is communicated with described separator fluid, and be built into certain forms with cooling from described separator described gaseous effluent at least partially;
One or more vapour generator, it is communicated with described first heat exchanger fluid, and be built into certain forms with receive from described first heat exchanger described effluent described at least partially;
Second heat exchanger, it is communicated with described one or more producer fluid, and be built into certain forms with cooling from described one or more vapour generator described effluent described at least partially; With
Fractionator, it is communicated with described second heat exchanger fluid, and be built into certain forms with receive from described second heat exchanger described effluent described at least partially.
The system of 31. claims 30, it comprises the 3rd heat exchanger, 3rd heat exchanger fluid be communicated with between described separator and described hydrocarbon pyrolysis unit, and be built into certain forms be cooled through described 3rd heat exchanger to described separator described cracking effluent described at least partially.
The system of 32. claims 30, wherein said hydrocarbon pyrolysis unit is built into certain forms, with by making practical fluid heat described practical fluid by described hydrocarbon pyrolysis unit.
The system of 33. claims 32, wherein said first heat exchanger is built into certain forms, with make described practical fluid by hydrocarbon pyrolysis unit before, by making described practical fluid reclaim heat by described first heat exchanger at least partially described in described effluent in described first heat exchanger.
The system of 34. claims 33, wherein said second heat exchanger is built into certain forms, with make described practical fluid by described first heat exchanger before, reclaim heat by making described practical fluid by described second heat exchanger.
The system of 35. claims 34, it comprises one or more valve, described valve is coupled to described one or more vapour generator, and is built into certain forms to regulate by heat recuperation at least partially described in the described effluent by described one or more vapour generator.
CN201180035764.9A 2010-07-30 2011-04-11 For processing the method for hydrocarbon pyrolysis effluent Expired - Fee Related CN103210060B (en)

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