CN1665910A

CN1665910A - Converting mist flow to annular flow in thermal cracking application

Info

Publication number: CN1665910A
Application number: CN03815806XA
Authority: CN
Inventors: R·C·斯特尔; A·R·蒂尼克兰特尼奥; J·L·班克罗伏特; G·斯蒂芬
Original assignee: Exxon Chemical Patents Inc
Current assignee: ExxonMobil Chemical Patents Inc
Priority date: 2002-07-03
Filing date: 2003-06-27
Publication date: 2005-09-07
Anticipated expiration: 2023-06-27
Also published as: WO2004005432A1; SG177003A1; EP1527151A1; AU2003247756A1; EP1527151B1; JP2005531683A; CA2489888A1; EP1523534A1; KR20050016708A; CN1281715C; CA2489888C; CN1665909A; JP4387301B2; CA2489876A1; JP2006508198A; EP1639060A1; WO2004005431A1; JP2005531684A; CN1665908A; CN100494318C

Abstract

A process to increase the non-volatile removal efficiency in a flash drum in the steam cracking system. The gas flow from the convection section is converted from mist flow to annular flow before entering the flash drum to increase the removal efficiency. The conversion of gas flow from mist flow to annular flow is accomplished by subjecting the gas flow first to at least one expander and then to bends of various degrees and force the flow to change directions at least once. The change of gas flow from mist to annular helps coalesce fine liquid droplets and thus being removed from the vapor phase.

Description

In thermally splitting is used, spray is converted to annular flow

Background of invention

Invention field

The present invention relates in steam cracking is used spray is converted to the remove efficient of annular flow with the fixed hydrocarbon that improves flash drum.

Background and description of related art

Utilize steam cracking that various hydrocarbon feed crackings have been had for a long time for alkene.The stove with two main region is adopted in conventional steam cracking: convection section and radiant section.Hydrocarbon feed enters the convection section of stove usually with liquid form (unless the light raw material that enters with the steam form), at this, hydrocarbon feed usually by with from the hot flue gases indirect contact of radiant section be heated and vaporize by directly contacting with steam.Then, the raw material of vaporization enters radiant section, at this cracking takes place.The alkene of gained leaves pyrolysis oven in order to further downstream processing such as quenching.

Conventional steam cracking system is effective for cracking high-quality raw materials such as gas oil and petroleum naphtha.Yet the steam cracking economy is wished the heavy feed stock of cracking cheapness sometimes, as crude oil and the atmospheric resids as limiting examples.Crude oil and atmospheric resids contain the high-molecular weight nonvolatile element that boiling point is higher than 1100 (590 ℃).The non-volatile hjeavu ends of these raw materials at the convection section of conventional pyrolysis oven as under the sedimentation of coke.In the convection section in the some downstream of vaporizing fully, only can allow very low-level non-volatile matter than light constituent.In addition, some petroleum naphtha in transportation by crude oil pollution.Conventional pyrolysis oven does not have processing Residual oil, the perhaps many Residual oils of crude oil or the gas oil of crude oil pollution or the handiness of petroleum naphtha, contains a large amount of non-volatile heavy in these above-mentioned oil.

In order to solve this coking problem, United States Patent (USP) 3,617,493 (this document is combined in herein by reference) disclose the outside vaporization tank that is used for crude oil material, and disclose and utilize first flash distillation to remove petroleum naphtha with the steam form, utilize second flash distillation to remove the steam that boiling point is 450 to 1100 (230 to 600 ℃).The cracking in pyrolysis oven of described steam is an alkene, and isolating liquid is removed from two flash drums, uses steam stripped and is used as fuel.

United States Patent (USP) 3,718,709 (this document is combined in herein by reference) disclose the method that minimizes sedimentation of coke.It discloses the inner or outside preheating heavier feedstocks at pyrolysis oven, to vaporize about 50% heavier feedstocks and remove residual liquid with superheated vapour.The hydrocarbon of vaporization is carried out cracking.

United States Patent (USP) 5,190,634 (this document is combined in herein by reference) disclose by preheating material in the presence of the hydrogen of convection section in a spot of, critical amount, suppress the method for coke formation in the stove.The existence of hydrogen has suppressed the polyreaction of hydrocarbon in the convection section, has suppressed coke formation thus.

United States Patent (USP) 5,580,443 (this document is combined in herein by reference) disclose a kind of method, and wherein raw material at first is preheated, and then by from the preheater of the convection section of pyrolysis oven, extracting out.The raw material of this preheating mixes with predetermined quantity of steam (dilution steam generation) then, and is introduced into gas-liquid separator then, to separate from separator and to remove the non-volatile matter of required ratio with liquid form.Turn back to pyrolysis oven from the steam of gas-liquid separator separates and carry out overheated and cracking.

The inventor recognizes, use flash distillation with non-volatile heavy when volatile hydrocarbon that can cracked is lighter in pyrolysis oven separates, importantly maximize the efficient that removes of fixed hydrocarbon.Otherwise, coke, non-volatile heavy may be entrained in the vapor phase, and taken to the stove from cat head, produces coking problem.

Have found that,, in pipeline, require the gas flow of a minimum, to realize good heat exchange and to make the film temperature enough low to reduce coking at the convection section of steam cracking pyrolysis oven.Usually, the minimum air flow speed of having found about 100ft/sec (30m/sec) is favourable.

When utilizing flash drum from the liquid phase non-volatile heavy during with the lighter volatile hydrocarbon of vapour phase isolated in form, the flash stream that enters flash drum generally includes the vapour phase of the liquid (non-volatile hydrocarbon components) that has with entrained as fine droplets.Therefore, flash stream is a two phase flow.Under the frictional belt film temperature desired flow rates that requires in the pipeline in keeping convection section, this two phase flow is " spray " mode.In this mist flow regime, the small droplets that comprises non-volatile heavy is entrained in the vapour phase, and described vapour phase is volatile hydrocarbon and randomly is steam.There is operational issue in this two-phase spray in flash drum, because under so high gas velocity, the small droplets that comprises fixed hydrocarbon can not be coalescent, and therefore can not remove effectively from flash drum with liquid form.Have found that under the gas velocity of 100 feet per seconds (30m/s), flash drum only can be removed non-volatile heavy with about 73% poor efficiency.

The invention provides the method for in flash drum, from the volatile hydrocarbon steam, effectively removing fixed hydrocarbon liquid.Therefore the invention provides a kind of method, this method is converted to " annular flow " mode with " spray " mode (regime), and has obviously improved separating of non-volatile and volatile hydrocarbon in the flash drum.

The invention summary

The invention provides the method for handling heavy hydrocarbon feeds, this method comprises: the heavy hydrocarbon feeds that randomly comprises steam in the convection section preheating of steam cracker furnace, with vaporization part material and be formed on the spray that comprises drop in the volatile hydrocarbon steam that randomly contains steam, described drop comprises fixed hydrocarbon, described spray when leaving convection section, have first flow velocity and first-class to; Handle described spray with coalescent drop, this processing comprises and at first reduces flow velocity, changes subsequently to flow to; In flash drum, from steam, separate at least a portion drop, to form liquid and vapor capacity; With vapour phase is fed in the thermally splitting stove.

In one embodiment of the invention, described vapour phase is fed to the lower convection section and the radiant section of steam cracker furnace.

In one embodiment, the processing of described spray comprises the flow velocity that reduces spray.Mist stream flow velocity can reduce at least 40%.Mist flow velocity can be reduced to and be lower than 60 feet per seconds (18m/s).

According to another embodiment, reduce mist stream flow velocity, make spray experience at least one centrifugal force, droplet coalescence so then.The flow direction of this spray can change once at least.

In yet another embodiment of the present invention, the spray drop is being lower than 25 calibers, preferably is lower than 8 interior calibers and most preferably is lower than in the distance of 4 interior calibers coalescent.

According to another embodiment, spray flows through the stream that comprises at least one bend pipe.This stream can also comprise at least one expander.Preferably, described stream comprises a plurality of bend pipes.Bend pipe can be at least 45 °, 90 °, 180 ° or their combination.

In another embodiment, described spray is converted into the logistics of annularly flow.Flash efficiency can increase at least 85%, and preferably at least 95%, more preferably at least 99%, most preferably at least 99.8%.Described spray can be less than 50 calibers, preferably be less than 25 calibers, more preferably less than 8 calibers and most preferably be less than 4 calibers circularize the mobile logistics apart from internal conversion.

Also according to the present invention, a kind of method of processing hydrocarbons raw material comprises: the hydrocarbon feed that randomly comprises steam in the convection section preheating of thermally splitting stove, to vaporize a part of raw material and be formed on the spray that comprises drop in the hydrocarbon vapour that randomly contains steam, described drop comprises hydrocarbon, described spray when leaving convection section, have first flow velocity and first-class to; Handle described spray with coalescent drop; In flash drum, from steam, separate at least a portion drop, to form liquid and vapor capacity; With vapour phase is fed in the steam cracker furnace, wherein flash distillation comprise will contain the spray of coalescent drop introduce flash drum, remove vapour phase and remove liquid phase from the flash drum outlet at least one top from the flash drum outlet of at least one bottom.

The invention also discloses another embodiment, wherein spray is tangentially introduced in the flash drum by at least one tangential flash drum inlet.

Brief description of drawings

Fig. 1 illustrates the block diagram of process for steam cracking.

Fig. 2 illustrates the design of expander.

Fig. 3 illustrates the design according to flash drum of the present invention.

Detailed Description Of The Invention

Unless otherwise noted, all percentage ratio, umber, ratio etc. all are based on weight.

Unless otherwise noted, comprise compound or component itself when mentioning compound or component, and with the combination of other compound or component, as the mixture of compound.

In addition, when quantity, concentration or other value or parameter provide with a series of upper limit preferred value and lower limit preferred value, this should be understood to specifically disclose all scopes of any a pair of formation of upper limit preferred value and lower limit preferred value, no matter whether described scope is by open separately.

When using in this article:

Flow pattern is the visual of fluid stream or performance qualitatively.The drop size that does not have the speed of setting and do not have to set.Spray is meant two phase flow, and wherein small droplets is dispersed in by in the pipeline mobile vapour phase.In transparent pipeline, spray looks like the small rain droplets of quick travel.

Annular flow is meant two phase flow, and wherein liquid flows on side opposite with the form of logistics, and steam is in the center flow of pipeline.The steam flow velocity of annular flow is about 20 feet per seconds (6m/s).In transparent pipeline, can see the liquid of one deck quick travel.Drop is almost can't see at center at steam flow.In the outlet of pipeline, liquid oozes usually and only sees a spot of mist.Variation from the spray to the annular flow generally includes transitory stage, at this moment spray and annular flow exist.

Raw material comprises at least two kinds of components: volatile hydrocarbon and fixed hydrocarbon.According to the present invention, spray comprises the small droplets that is entrained in the fixed hydrocarbon in the volatile hydrocarbon steam.

It is as follows that non-volatile matter removes efficiency calculation:

Non-volatile matter removes efficient=[1-leaves the non-volatile matter (quality/time) in the hydrocarbon of non-volatile matter (quality/time) in the vapour phase of flash drum/enter flash drum] * 100%

Hydrocarbon is the summation of steam (generally being volatile) and liquid (generally being nonvolatile) hydrocarbon.Non-volatile matter is tested according to following method: the boiling point of hydrocarbon feed distributes and tests with gas-chromatography distillation (GCD) according to ASTMD-6352-98.Non-volatile matter is the hydrocarbon fraction that is higher than 1100 (590 ℃) according to the normal boiling point (nominal boiling point) of ASTMD-6352-98 test.The present invention is very good for the non-volatile matter effect that normal boiling point is higher than 1400 (760 ℃).

Analyze according to ASTM D-6352-98 at whole hydrocarbon that add stove and the fraction of removing the non-volatile matter 1100 to 1400 (590-760 ℃) in the flash drum overhead product sample after anhydrating.

The method of crackene raw material 10 of the present invention shown in Figure 1 comprises, exist or do not exist under the situation of water 11 and steam 12, at the top of steam cracker furnace 3 convection section 1, pipe row preheated hydrocarbon raw material by exchange pipe 2, with vaporization part material and be formed on the spray 13 that comprises drop in the volatility hydrocarbon/steam, described drop comprises fixed hydrocarbon.The further preheating of feedstock/water/steam mixture can be undertaken by the pipe row of heat exchanger tube 6.The spray 14 that leaves convection section have first flow velocity and first-class to.This method also comprises handles spray with coalescent drop, separates at least a portion drop in flash drum 5 from hydrocarbon vapour, to form vapour phase 15 and liquid phase 16 and vapour phase 8 to be fed to the low convection section and the radiant section of thermally splitting stove.

As mentioned above, raw material is a hydrocarbon.Any hydrocarbon feed with heavy non-volatile hjeavu ends can be advantageously used in the inventive method.As non-limiting instance, such raw material can comprise one or more in following: steam cracked gas oil and resistates, gas oil, oil fuel, rocket engine fuel, diesel oil, kerosene, gasoline, coking naphtha, the steam cracking petroleum naphtha, the catalytic cracking petroleum naphtha, isocrackate, reformate, the Residual oil reformate, Fischer-Tropsch liquid, Fischer-Tropsch gas, natural gasoline, distillment, virgin naphtha, crude oil, normal pressure pipe still Residual oil, comprise the decompression pipe still logistics of Residual oil, the petroleum naphtha of wide boiling range is to the gas oil enriched material, from the non-straight run hydrocarbon stream of the weight of refinery, vacuum gas oil, heavy gas oil, the petroleum naphtha of crude oil pollution, atmospheric resids, heavy residual stocks, C4 ' s/ residue mixture and naphtha residue mixture.

Heavy hydrocarbon feeds has the standard full boiling point of at least 600 (310 ℃).Preferred raw material is the petroleum naphtha of low sulfur waxy resids, atmospheric resids and crude oil pollution.Most preferably comprise the Residual oil that the 60-80% boiling point is lower than the component of 1100 (590 ℃), for example low sulfur waxy resids.

As mentioned above, heavy hydrocarbon feeds is preheated at the top of stove 1 convection section.Described raw material can be randomly before preheating or after the preheating (for example in preheater 2 after the preheating), in atomizer 4 with vapor mixing.The preheating of heavy hydrocarbon can be adopted any form known to those of ordinary skills.Preferred heating comprises makes raw material at the convection section of stove and from furnace radiant hot flue gases indirect contact partly.As non-limiting instance, this can realize by the pipe of the heat exchanger tube 2 of the top convection section 1 of raw material by being positioned at pyrolysis oven 3 is arranged.Before Controlling System 6, the temperature of the raw material 14 of preheating is 600 to 950 °F (310 to 510 ℃).Preferably about 700 to 920 of the temperature (370 to 490 ℃) of the raw material of heating, more preferably 750 to 900 (400 to 480 ℃), most preferably 810 to 890 (430 to 475 ℃).

The result of preheating is, part material is vaporized, and be formed on contain or not vapoury volatile hydrocarbon steam in comprise the spray of drop, described drop comprises fixed hydrocarbon.Under the flow velocity greater than 100 feet per seconds, liquid exists with the small droplets form that comprises fixed hydrocarbon that is entrained in the vapour phase.This two-phase spray is very difficult to be separated into liquid and steam.Before entering flash drum, little droplet need be agglomerated into big drop.Yet in order in fact to carry out with the heat exchange of hot flue gases and to reduce the coking of convection section, 100ft/sec or bigger flow velocity are normally necessary.

According to the present invention, spray is processed with coalescent drop.In one embodiment of the invention, processing comprises the flow velocity that reduces spray.Have found that before flash drum 5 (position 9 among Fig. 1), the speed that reduces the spray 14 that leaves convection section helps coalescent spray.The preferred mist flow velocity at least 40% that reduces, preferably at least 70%, more preferably at least 80%, most preferably 85%.The mist flow stream speed that also preferably will leave convection section is reduced to from least 100 feet per seconds (30m/s) and is lower than 60 feet per seconds (18m/s), more preferably less than 30 feet per seconds (27 to 9m/s), most preferably is lower than 15 feet per seconds (27 to 5m/s).

Annular flow can be by realizing owing to friction reduces flow velocity in large-diameter pipeline.In order to realize that desired reduction so that spray is converted to annular flow, needs quite long pipeline.Required duct length is by the definition of the quantity of interior caliber.The engineering practice requirement after reducing mist flow velocity to 60 feet per second (18m/s), needs the friction of straight tube (for example 24 inches * 100=200 foot or the 0.6 meter * 100=60 rice) generation of 50 to 150 pipe diameter length to set up annular flow.

The reduction of mist flow stream speed is by comprising what one or more expanders were realized in the pipeline outside convection section.In closed system, it is believed that needing an expander to reach preferred speed at least reduces.As non-limiting instance, expander can be simple tapers 101 or a manifold 102 shown in Figure 2.The sectional area of exit end is greater than the summation of the sectional area of all inlets.In an embodiment preferred of the present invention, spray at first passes through at least one expander, passes through at least one bend pipe then, preferably through having a plurality of bend pipes of the different number of degrees.When mist flow stream flows by one or more expanders, speed will reduce.The quantity of expander can change according to required speed reduction amount.As general practice rule, big if desired speed reduces, and can use more expander.Can use any expander such as manifold among the present invention.

The feasible annular flow that forms although expander just can underspeed separately, preferably, speed is used a bend pipe after reducing at least.Bend pipe plays the effect that is similar to whizzer.Stream of liquid droplets is to the bend pipe outer wall, and they can be coalescent at this.

The present invention can be converted to annular flow with spray in significantly less pipeline.According to the present invention, the spray drop is being less than 25, more preferably less than 8, and most preferably is less than in the pipe range of 4 interior calibers coalescent.

According to the present invention, the processing of vaporific logistics is comprised that spray is flowed through goes through a centrifugal force at least one expander and expander downstream so that droplet coalescence.This can change by the flow direction that makes vaporific logistics at least once realizes.For mist flow stream being converted to the annular flow logistics, the piping design that convection section is outer becomes to comprise at least one bend pipe.Bend pipe can be in the whole pipe expander downstream, between before Controlling System 17 and the flash drum.

Can use the bend pipe of different angles.For example, can use 45 °, 90 ° and/or 180 ° of bend pipes among the present invention.After expander, 180 ° of bend pipes provide maximum steam central speed to reduce.In one embodiment of the invention, described method comprises at least one bend pipe of at least 45 °.In another embodiment, described method comprises at least one bend pipe of 90 °.In another embodiment, described method comprises at least one bend pipe of 180 °.

Find, utilize invention disclosed herein, can realize at least 85% flash drum removal efficiency.Utilize the present invention, can also realize at least 95% preferred flash efficiency, at least 99% preferred flash efficiency and at least 99.8% most preferred flash efficiency.

After for example the needed speed in combination of expanders reduces, the small droplets in the mist flow stream will be coalescent in one or more bend pipes, and therefore be easy to separate with vapor phase stream in flash drum 5.Flash distillation is carried out at least one flash drum usually.In flash drum 5, remove vapor phase stream from the flash drum outlet at least one top, and remove liquid phase from the flash drum outlet of at least one bottom.Preferably, exist two or more to be used to remove the bottom flash drum outlet of liquid phase in the flash drum.

Equally according to the present invention, a kind of method that is used for the processing hydrocarbons raw material comprises: at the convection section heating liquid hydrocarbon feeds of thermally splitting stove, with vaporization part material and being formed on contain or not vapoury hydrocarbon vapour in comprise the spray of drop, described drop comprises hydrocarbon, spray when leaving convection section, have first flow velocity and first-class to; Handle spray with coalescent drop; In flash drum, from hydrocarbon vapour, separate at least a portion drop, to form liquid and vapor capacity; With the radiant section that vapour phase is fed to steam cracker furnace, wherein flash distillation comprises containing the logistics introducing flash drum of coalescent drop, removes vapour phase from the flash drum outlet at least one top, and removes liquid phase from the flash drum outlet of at least one bottom.

Fig. 3 illustrates according to a flash drum of the present invention.The efficient that removes of flash drum reduces along with the reduction of the drop size that enters flash drum.Drop size reduces with the increase of gas velocity.In order to increase separation efficiency, need enough duct length, expander and bend pipe, under lower speed, to form stable bigger drop.

Remove efficient in order further to increase fixed hydrocarbon in flash drum, the flash stream 9 of preferred Fig. 1 tangentially enters flash drum by the tangential flash drum inlet 201 of at least one Fig. 3.Preferably, tangential inlet is a horizontal flow or slightly to dirty.Non-volatile hydrocarbon liquid phase will form outside annular flow along the flash drum inwall, and volatile vapor phase begins formation inside center stream, then in flash drum on flow.In a preferred embodiment, tangential inlet and Coriolis (Coriolis) effect in the same way.

Liquid phase is removed from the flash drum outlet at bottom.Randomly, can increase side flash drum outlet (203) or vortex breaker, prevent from the interruption-forming eddy current.The inside center that the makes progress stream of vapour phase turns to around the ring baffle 202 of flash drum inside, and removes from the flash drum outlet 204 at least one top.Baffle plate is installed in flash drum inside, is entrained in flash drum upwards in the mobile vapour phase with the isolating liquid phase of further avoiding and reduce any part (flowing downward in flash drum).Preferably, vapour phase flow to the convection section 7 of the bottom of Fig. 1, and laterally arrives the radiant section of pyrolysis oven by pipeline 8.

Illustrate the present invention by the following examples, it is as the purpose of representing that described embodiment is provided, and can not be interpreted as the restriction to invention scope.Unless otherwise indicated, all percentage ratio, umber etc. are based on weight.

Embodiment 1

The isolating vapor/liquid separation efficient of flash drum height depends on the drop size.Stoke law instruction, square being directly proportional of drop or particulate terminal velocity and diameter.Therefore, if very little droplet enters flash drum, the gas velocity that makes progress so will cause and carry secretly greater than the terminal velocity of drop.Drop extensively is agglomerated into annular flow will form very large drop, this big drop separate easily in flash drum.

Annular flow can be realized with friction by reducing bulk flow velocity and giving the needed grace time of coalescent drop.After overall rate (bulk velocity) reduces, need the coalescent drop of about 100 pipe flow diameters.Carry out the air/water flow test, to determine how in being lower than 100 calibers, to obtain annular flow." produce high-speed gas in the ID pipe with two 6HP fans 2.The air that comes out from two fans merges in breeches joint, and flows into 2 " in the ID transparent tube.A bit be a T connector before transparent tube, add entry to produce spray at this.Measure fluid velocity with wind meter at the end of guard system.

Tested various pipe bends, for example 45 ° of elbows, ell and return pipes, and expander, whether the small droplets of observing in the spray is coalescent.They are summarized in the following table 1.

The observations of table 1 droplet coalescence

Test	Describe	Observations
Test	Describe	Observations	?1 ? ?2 ?3 ? ?4 ? ?5 ? ?6 ?	In air, add 6GPM water, the two phase flow that produces overall flow and be 110ft/sec increases by 90 ° of bend pipes, and " the ID straight tube is terminal increase expander and 6ft 3 " transparent tube increases 3 " transparent tube; obtain the expander of the length overall of 18ft or 75 diameters at 2 " ID straight tube end increases to 3 " ID, 3 " transparent tube-speed 50ft/sec is 2 " ID pipe end of 90 ° of ells and 6ft the increases to 6 " expanders of ID of 12ft again in test 32 to produce centrifugal force, 90 ° of ells, 6 " the ID pipes; the 6 " pipes of 90 ° of ells and 4ft of 4ft	2 " the ducted droplet spray of ID spray be reinforced whole 6ft or 25ID 3 " some droplet coalescence of spray of transparent pipe; But still exist spray film drip obviously coalescent-flow annular stratified flow with the annular of some mists, almost do not have mist

The summary observations is as follows: test 2 shows, under high speed, bend pipe separately can not coalescent drop, and even may produce mist.Test 3 and 4 shows that even behind 75 calibers of larger diameter pipeline, expander separately can not coalescent fully drop.Test 5 and 6 shows that the expander that is connected to the bend pipe of band short straight tube can coalescent drop.The expander that is connected to bend pipe is big more, and droplet coalescence is an annular flow, even it is complete more to gather into stratified flow.

Claims

1. method of handling heavy hydrocarbon feeds, this method comprises: the heavy hydrocarbon feeds that randomly comprises steam in the convection section preheating of steam cracker furnace, with the vaporization part material, and be formed on the spray that comprises drop in the volatile hydrocarbon steam that randomly contains steam, described drop comprises fixed hydrocarbon, and described spray has a flow velocity and a flow direction when leaving convection section; Handle described spray with coalescent drop, this processing comprises and at first reduces flow velocity, changes subsequently to flow to; In flash drum, from steam, separate at least a portion drop, to form liquid and vapor capacity; With vapour phase is fed in the steam cracker furnace.

2. the method for claim 1 also comprises the low convection section and the radiant section that vapour phase are fed to steam cracker furnace.

3. claim 1 or 2 method, wherein heavy hydrocarbon feeds comprises one or more in following: steam cracked gas oil and resistates, gas oil, oil fuel, rocket engine fuel, diesel oil, kerosene, gasoline, coking naphtha, the steam cracking petroleum naphtha, the catalytic cracking petroleum naphtha, isocrackate, reformate, the Residual oil reformate, Fischer-Tropsch liquid, Fischer-Tropsch gas, natural gasoline, distillment, virgin naphtha, crude oil, normal pressure pipe still Residual oil, comprise the decompression pipe still logistics of Residual oil, the petroleum naphtha of wide boiling range is to the gas oil enriched material, from the non-straight run hydrocarbon stream of the weight of refinery, vacuum gas oil, heavy gas oil, the petroleum naphtha of crude oil pollution, atmospheric resids, heavy residual stocks, C4/ residue mixture and petroleum naphtha/residue mixture.

4. claim 1,2 or 3 method, wherein heavy hydrocarbon feeds comprises low sulfur waxy resids.

5. according to the method for any aforementioned claim, wherein 60 to 80% heavy hydrocarbon feeds seethes with excitement below 590 ℃ (1100 °F).

6. according to the method for any aforementioned claim, wherein the flow velocity of spray reduces at least 40%.

7. according to the method for any aforementioned claim, wherein the flow velocity of spray is reduced to and is lower than 60 feet per seconds (18m/s).

8. according to the method for any aforementioned claim, wherein handle and comprise and at first reduce mist stream flow velocity to being lower than 60 feet per seconds (18m/s), make spray stand at least one centrifugal force then, so that droplet coalescence.

9. according to the method for any aforementioned claim, wherein the drop in the spray is coalescent in less than 25 interior calibers basically.

10. according to the method for any aforementioned claim, wherein the drop in the spray is coalescent in less than 4 interior calibers basically.

11. according to the method for any aforementioned claim, wherein spray flows through the stream that at first comprises at least one expander and at least one bend pipe.

12., handle that wherein the circulation of spray animal is changed to the annularly flow logistics according to the method for any aforementioned claim.

13. according to the method for any aforementioned claim, wherein flash drum is realized at least 85% non-volatile matter separation efficiency.

14. according to the method for any aforementioned claim, wherein flash drum is realized at least 95% non-volatile matter separation efficiency.

15. according to the method for any aforementioned claim, wherein flash drum is realized at least 99% non-volatile matter separation efficiency.

16. according to the method for any aforementioned claim, wherein flash drum is realized at least 99.8% non-volatile matter separation efficiency.

17. according to the method for any aforementioned claim, wherein spray is the spray flowing mode, and is being the annularly flow mode less than 25 caliber internal conversions.

18. according to the method for any aforementioned claim, wherein spray is the spray flowing mode, and is being the annularly flow mode less than 4 caliber internal conversions.

19. according to the method for any aforementioned claim, wherein spray flows through the stream that comprises a plurality of bend pipes.

20. the method for claim 19, wherein at least one bend pipe is at least 45 °.

21. the method for claim 19 or 20, wherein at least one bend pipe is at least 90 °.

22. claim 19,20 or 21 method, wherein at least one bend pipe is 180 °.

23. the method for a processing hydrocarbons raw material, comprise: randomly comprise the hydrocarbon feed of steam in the convection section preheating of thermally splitting stove,, and be formed on the spray that comprises drop in the hydrocarbon vapour that randomly contains steam with a part of raw material of vaporizing, described drop comprises hydrocarbon, and described spray leaves convection section; Handle described spray with coalescent drop; In flash drum, from steam, separate at least a portion drop, to form liquid and vapor capacity; With vapour phase is fed in the thermally splitting stove, wherein flash distillation comprise will contain the spray of coalescent drop introduce flash drum, remove vapour phase from the flash drum outlet at least one top, and remove liquid phase from the flash drum outlet of at least one bottom.

24. the method for claim 23, wherein spray is tangentially introduced flash drum by at least one tangential flash drum inlet.

25. the method for claim 23 or 24, wherein liquid phase is removed from least one lower side flash drum outlet and flash drum outlet at bottom.

26. claim 23,24 or 25 method, wherein flash drum has the ring baffle that is installed in the flash drum, reduces the liquid phase that flows downward effectively and be entrained in part in the vapour phase in flash drum.