EP4305129A1 - Procédé et installation de vapocraquage - Google Patents

Procédé et installation de vapocraquage

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Publication number
EP4305129A1
EP4305129A1 EP22710121.9A EP22710121A EP4305129A1 EP 4305129 A1 EP4305129 A1 EP 4305129A1 EP 22710121 A EP22710121 A EP 22710121A EP 4305129 A1 EP4305129 A1 EP 4305129A1
Authority
EP
European Patent Office
Prior art keywords
steam
preheating
feed water
combustion air
feedwater
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP22710121.9A
Other languages
German (de)
English (en)
Other versions
EP4305129C0 (fr
EP4305129B1 (fr
Inventor
Mathieu Zellhuber
David Bruder
Michael Hörenz
Stefan Glomb
Christopher Eberstein
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP4305129A1 publication Critical patent/EP4305129A1/fr
Application granted granted Critical
Publication of EP4305129C0 publication Critical patent/EP4305129C0/fr
Publication of EP4305129B1 publication Critical patent/EP4305129B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • 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

Definitions

  • the present invention relates to a method and a plant for steam cracking according to the preambles of the independent claims.
  • the present invention relates to steam cracking (steam cracking, thermal cracking, steam cracking, etc.) used in the production of olefins and other bulk chemicals and is described, for example, in the article "Ethylene” in Ullmann's Encyclopedia of Industrial Chemistry, online publication April 15 2009, DOI: 10.1002/14356007. a10_045.pub2. With regard to the terms used below, reference is also made to the relevant specialist literature.
  • the heat energy required is typically provided by the combustion of fuel gas in a combustion chamber, which forms the so-called radiant zone of a cracking or cracking furnace, and through which so-called coils (cracking tubes) are guided which a hydrocarbon-steam mixture to be converted is passed to obtain a product mixture, the so-called raw or cracked gas.
  • the combustion air required for combustion is fed into the radiation zone without preheating (so-called natural draft) and burned there together with the heating gas.
  • a cracker furnace 10 shown in FIG. 1 or a corresponding furnace unit (here also referred to as a cracking furnace or furnace for short) has the radiation zone 11 and a convection zone 12 .
  • a plant for steam cracking can contain several corresponding cracking furnaces 10. Plant components or units referred to below as central are available for several cracker furnaces 10 , decentralized units are provided separately for each cracker furnace 10 .
  • a central feed preheater 20 shown as an example and a central process steam generator 30 a hydrocarbon feed H is heated and process steam P provided, which is further heated in the convection zone 12 in a manner known per se (see in particular Figure 4), combined to form a feed stream F and then the Radiation zone 11 are supplied.
  • a corresponding feed stream can already be divided into several partial streams in the area of the convection zone 12, which are then preheated separately from one another and finally passed through groups of, for example, six or eight cracking tubes in the radiation zone 11.
  • Centralized units can be replaced here and subsequently by decentralized units and vice versa at any time.
  • the cleavage gas C is removed from the radiation zone 11, which is cooled by means of one or more quench gas coolers 13, which can in particular be designed as known quench coolers or can include such quench coolers and which can also function as steam generators at the same time, and then undergo a central cleavage gas separation and cleavage gas treatment 90 is supplied. Further details on corresponding quench coolers, which can be designed in particular as classic quench coolers or so-called linear quench exchangers (LQE), are explained below. The invention is not limited by a specific embodiment.
  • a central feedwater system 40 provides feedwater W, which in the example shown is also heated in the convection zone 12 and then further heated by means of one or more cracked gas coolers 13 to obtain high-pressure or super-high-pressure saturated steam S (hereinafter also referred to as saturated steam for short) and finally evaporates becomes.
  • saturated steam S is superheated in the convection zone 12 to obtain superheated high-pressure steam or superheated superhigh-pressure steam T (also referred to as superheated steam below) and fed into a central steam system 50 .
  • feed heating gas Y is heated to preheated heating gas X and supplied to the radiation zone 11 or to burners that are not separately illustrated.
  • combustion air L reaches the radiation zone 11 or the burners there via an air intake 79 .
  • Flue gas Z is discharged from the radiation zone 11, which passes through the convection zone 12 and is then discharged into a flue gas treatment system or to a central or decentralized chimney 80 with or without a fan and via this to the atmosphere.
  • Central heating gas preheating 65 illustrated in FIG. 1 is optional. Decentralized heating gas preheating (i.e. separately for the individual cracker ovens 10 or oven units) is also possible. The same applies to the preheating of the insert and the generation of process steam, which can also be carried out decentrally as an alternative to the central design.
  • FIGS. 2 and 3 Corresponding configurations are shown in FIGS. 2 and 3, with FIG. 2 showing central combustion air compression and FIG. 3 decentral combustion air compression 70 and combustion air preheating 75 .
  • the term "increase in efficiency” can be understood here as an increase in the so-called specific efficiency, which in turn means the proportion of the heating gas energy introduced that is found in the products formed, here the cracked gas.
  • the specific efficiency is increased by preheating the air because less bottom firing is required for the same amount of cracked gas.
  • the thermal efficiency does not necessarily increase through the use of air preheating, since this may also be limited by a minimum flue gas emission temperature, see below.
  • Centrally and decentrally arranged units are provided with the same reference symbols below.
  • the type of arrangement results from the illustrated positioning inside or outside of the respective cracker furnace 10 or the furnace unit, with a decentralized arrangement being present if it is positioned inside and a central arrangement if it is positioned outside.
  • central combustion air compression 70 can also take place with decentralized combustion air preheating 75 .
  • the combustion air is also referred to as air for short, and its preheating is also referred to as air preheating.
  • non-superheated steam can be used at high, medium or low pressure, washing water and/or quench oil as heating media or electricity as a heat source. It is also possible to use directly transferred heat from the exhaust gas stream Z as a heat source.
  • superheated high-pressure or super-high-pressure steam T shown in the figures is optional and is carried out depending on the selected preheating temperature.
  • the preheated combustion air can be provided centrally or decentrally.
  • SHD super high-pressure steam
  • HP high-pressure steam
  • MP medium-pressure steam
  • LP low-pressure steam
  • saturated steam wash water or quench oil
  • Low-pressure steam should here generally be steam at a pressure level of 1 to 10 bar absolute pressure (abs.), in particular 4 to 8 bar (abs.), medium-pressure steam should be steam at a pressure level of 10 to 30 bar (abs.), in particular 15 up to 25 bar (abs.), under high-pressure steam steam at a pressure level of 30 to 60 bar (abs.), in particular from 35 to 50 bar (abs.), and under super high-pressure steam steam at a pressure level of 60 to 175 bar (abs. ), in particular from 80 to 125 bar (abs.), To be understood. If the term abbreviated to high-pressure steam is used below, this should also be understood as meaning super-high-pressure steam.
  • super high pressure level means the pressure level specified for super high pressure steam, whether that is specified for the steam itself or, for example, for feed water used to form the steam. The same applies to the terms high pressure level,
  • the air drawn in from the atmosphere can be compressed by a driven fan in the air compression, either centrally or decentrally.
  • a blower which is arranged downstream of the air preheating and causes a corresponding suction.
  • Air preheating is described in connection with steam cracking, for example, in US Pat. No. 3,426,733 A, EP 0229 939 B1 and EP 3415587 A1, and in connection with air preheating in boilers, for example in DE 102004020223 A1 and WO 2013/178446 A1.
  • US 2020/172814 A1 discloses a cracking furnace system for converting a hydrocarbon feedstock into cracked gas, the cracking furnace system comprising a convection section, a radiant section and a cooling section, the convection section including a plurality of convection banks configured to Receive and preheat feedstock, wherein the radiant section includes a furnace comprising at least one radiant coil configured to heat the feedstock to a temperature enabling a pyrolysis reaction, wherein the cooling section includes at least one transfer line heat exchanger. Air preheating generally improves heat transfer in the radiant zone and reduces the fuel requirements of the kiln.
  • the hydrocarbon charge to be split and the associated process steam are preheated to temperatures of 550 to 700°C.
  • high or super high pressure level boiler feed water fed to the furnace is preheated, typically at 100 to 110°C, in the convection zone, vaporized in the quench cooler and finally superheated in the convection zone.
  • the present invention is therefore intended to provide solutions with which an economical, efficient and practically implementable operation of a steam cracking plant is possible.
  • the present invention proposes a method and a plant for steam cracking according to the preambles of the independent claims.
  • Advantageous configurations are the subject of the dependent patent claims and the following description.
  • the present invention allows an extremely compact design of the convection zone, viewed here as the sum of the heights of the individual convection bundles in the flue gas duct, a simple construction of the chimney lines downstream of the convection zone and maximum use of flue gas heat, i.e. low flue gas outlet temperature at the chimney. Furthermore, a minimum fuel requirement can be achieved with the maximum possible production of superheated high pressure or super high pressure steam.
  • the core of the present invention is the use of feed water, i.e. water that is then used to generate (super) high-pressure steam, for the preheating of combustion air.
  • the present invention is based on a method for converting one or more hydrocarbons by steam cracking, in which one or more feed streams containing the one or more hydrocarbons, to obtain one or more product streams, ie cracked gas streams or Raw gas streams are passed through one or more radiation zones of one or more cracker furnaces, in which the one or more radiation zones are heated by firing fuel gas with combustion air, in which at least part of the combustion air is subjected to combustion air preheating, in which steam is generated from feed water , and wherein the feedwater is subjected to feedwater preheating in one or more convection zones of the one or more cracker furnaces.
  • the input streams can also be routed in parallel in one or more convection zones, for example in accordance with the division into a number of groups of cans in the radiant zone.
  • the combustion air preheating is carried out using heat which is extracted from at least part of the feedwater upstream of the feedwater preheating.
  • the invention thus includes supplying cooled feed water to the convection zone of the furnace or furnaces, as a result of which the greatest possible cooling and thus energetic use of the flue gas can be achieved.
  • cooling the feed water in which the hot gas quality in particular can be taken into account to avoid corrosion in the exhaust gas tract.
  • the feedwater can also, as explained below, be used additionally or alternatively as a heating medium in a centralized or decentralized heating gas preheating system.
  • cooling can take place outside of the furnace process.
  • the feedwater preheating can be carried out in particular in such a way that only a, in particular adjustable, first part of the feedwater undergoes heat exchange in one or more combustion air preheaters with at least part of the combustion air to be heated and optionally in one or more fuel gas preheaters heat exchange with at least part of the combustion air to be heated Heating gas is used and a, in particular adjustable, second part of the feed water is guided as a bypass flow around the combustion air preheater and, if necessary, the heating gas preheater. The first and second part can then combined again and then fed to the feed water preheating in the convection zone.
  • the temperature of the feed water at the entry into the convection zone can be regulated in this way.
  • the latter can be used during operation in particular to control the outlet temperature of the flue gas in the chimney. In such a process control, the latter depends strongly on the temperature of the feed water.
  • the temperature of the flue gas can be adjusted by adjusting a proportion of the feedwater used in the air preheating and optionally also in the heating gas preheating, which can be done in particular on the basis of a temperature of a flue gas that is to be achieved or detected in the convection zone downstream of the feedwater preheating.
  • the present invention is used in a process in which the steam generated from the feedwater comprises superheated or non-superheated high or super high pressure steam formed from the feedwater downstream of the feedwater preheater.
  • the feedwater After the feedwater has been preheated, at least part of the feedwater can be subjected to feedwater evaporation, using heat that is extracted from at least part of the one or more product streams, in particular in one or more cracked gas or quench coolers, to obtain high- or super-high-pressure saturated steam will.
  • At least part of the high or super high pressure saturated steam can then be subjected to steam superheating in the one or more convection zones to obtain the (superheated) high or super high pressure steam.
  • FIGS. 1 to 4 Reference is made to the explanations for FIGS. 1 to 4 for further details.
  • the combustion air can be preheated using heat that is extracted from part of the (superheated) high-pressure or super-high-pressure steam. In configurations according to the invention, this takes place in addition to the use of the heat of the feed water, in configurations not according to the invention as an alternative to this.
  • the heating gas can be subjected to a heating gas preheating, which can also be carried out using heat which is extracted from at least part of the feedwater upstream of the feedwater preheating.
  • a heating gas preheating which can also be carried out using heat which is extracted from at least part of the feedwater upstream of the feedwater preheating.
  • the feedwater is preheated in one or more flue gas ducts in the one or more convection zones, with the feedwater preheating being carried out in particular at a lower temperature level than is required for the steam superheating to obtain the superheated high- or super-high-pressure steam, a process steam heating providing process steam used to form the one or more feed streams and performing a majority of the feed heating of the one or more feed streams.
  • the feed water is preheated near the end or at the very end of the flue gas duct, from which the flue gas, which has then been cooled accordingly, flows out, i.e. at a point downstream (in the direction of flow of the flue gas) there is at most one further heat recovery from the flue gas. In this way, the outlet temperature of the flue gas from the convection zone can be controlled particularly advantageously.
  • the feed water can, in particular, be at a temperature level of 80 to 140° C., in particular by means of a central or decentralized feed water system, and the feed water can be cooled to a temperature level of 40 to 100°C, to 95°C, to 90°C or to 85°C during the preheating of the combustion air.
  • the feed water for the combustion air preheating can be at a pressure level of 30 to 60 bar (abs.), in particular from 35 to 50 bar (abs.), or from 60 to 175 bar (abs.), in particular from 80 to 125 bar (abs.), and subjected to feedwater preheating at this pressure level without additional pressurization.
  • the feed water for combustion air preheating can be supplied at a pressure level of 20 to 60 bar (abs.), in particular between 25 to 50 bar (abs.) or between 30 and 40 bar (abs.) and after additional pressurization at a pressure level of 30 to 60 bar (absolute), in particular from 35 to 50 bar (absolute), or from 60 to 175 bar (absolute), in particular from 80 to 125 bar (absolute), of the feed water preheating.
  • the feed water can advantageously be brought to a corresponding pressure by means of one or more pumps.
  • the air can therefore be preheated directly with feed water at (super) high pressure level, so that the intermediately cooled feed water can then be fed directly to the convection zone.
  • the air can also be preheated with feed water at a reduced pressure level, as explained. The latter leads to a significantly lower design pressure of the associated air preheater and thus to less structural effort for this apparatus.
  • several cracker furnaces can be used, which are supplied with the feed water by means of a central feedwater system, with the combustion air preheating being carried out separately for each of the several cracker furnaces (decentralized combustion air preheating) or for the several cracker furnaces together (central Combustion air preheating) can be carried out.
  • the combustion air can be preheated, in particular in several stages, with feed water being used as the heating medium in a first stage, medium-pressure steam being used as the heating medium in a second stage, and saturated or superheated (super) high-pressure steam being used as the heating medium in a third stage can.
  • heating or heating media including electricity
  • more or fewer than the preheating stages mentioned can also be provided.
  • all or part of the heating medium that is running off (in particular condensate that has formed) in previous stages i.e. at a lower temperature level
  • the correspondingly cooled feed water is then fed into the convection zone, but at a noticeably reduced temperature.
  • the invention also relates to a plant for the conversion of one or more hydrocarbons by steam cracking, the characteristics of which, as mentioned, are reproduced in the corresponding independent claim.
  • measure 1 Another major advantage of measure 1 is the simple design of the flue gas routing after exiting the convection zone. This is very similar to that of a furnace without air preheating, and is therefore much easier than using a direct heat exchanger between the flue gas stream and the combustion air, which requires the installation of large-volume tube assemblies and heat exchange surfaces in the flue gas path of each individual furnace. Measure 1 creates a similar process effect, namely the transfer of exhaust gas heat to the combustion air, but indirectly using a heat transfer medium (feed water) already present in the furnace area, which requires significantly smaller pipe cross-sections due to its liquid aggregate state.
  • a further advantage is the described possible temperature regulation via the explained bypass guide, so that, in contrast to a system with direct heat exchange between the combustion air and the exhaust gas flow, the exhaust gas temperature can be set/changed easily during operation. Fluctuations in the heating gas quality can thus be handled much better, see previous description.
  • measure 3 a combination of measures 1 and 2 (referred to as measure 3 according to the invention) leads to a simultaneous improvement in the furnace in terms of construction complexity and energy efficiency.
  • variant 3B shows the effect of an additional process steam overheating with (super) high-pressure saturated steam (measure 4 not according to the invention considered in isolation). Similar to measure 2, this extraction of saturated steam and its use for process steam overheating leads to a reduction in the construction costs, which in the given example through combination with measures 1 (in accordance with the invention) and 2 (not considered in accordance with the invention) leads to a constant furnace energy efficiency.
  • variant 3B shows the effect of additional feed preheating with (super) high-pressure saturated steam (not viewed in isolation Measure 5) according to the invention. Similar to measures 2 and 4 (each considered individually not according to the invention), this removal of saturated steam and its use for preheating the insert leads to a reduction in the construction effort, which in the given example 5B is achieved by the simultaneous application of measures 1 (according to the invention) and 2 (considered individually not according to the invention) leads to a constant oven energy efficiency.
  • variant 4B or variant 5B shows the effect of the joint use of process steam superheating and feed preheating with (super) high-pressure saturated steam (measure 6 not considered in accordance with the invention when considered individually).
  • the maximum extraction of saturated steam and its use for process steam superheating and insert preheating leads to a maximum reduction in construction costs, which in the given example through the simultaneous application of measures 1 (according to the invention) and 2 (not considered according to the invention) to a constant furnace energy efficiency as in the variants 3B, 4B, and 5B leads.
  • the variants listed in Table 1 use different versions of the air preheater sequences, with three stages, using wash water, medium pressure steam and/or superheated (super) high pressure steam in addition to the explained use of feed water and/or (super) high pressure saturated steam.
  • Table 2 shows the results for versions of different variants with even more increased air preheating (300°C) and correspondingly further reduced fuel consumption. The effects of the measures described apply unchanged.
  • the comparison of variants 4A* with 4B* shows the positive influence of measure 2 on the construction costs.
  • the comparison of example 4B* with 4B** shows the added value in terms of furnace efficiency when adding measure 1.
  • Table 2 - Comparison of effectiveness for air preheat temperature of 300°C . Version without use of feed water in air preheating : Version with use of feed water in air preheating
  • Variant 6C** shows the possibility of achieving increased steam export by means of increased construction costs compared to Variant 6B** with almost the same furnace efficiency. In this case, this is achieved by means of a serial connection of process steam superheating and feed preheating on the heat transfer medium side, i.e. the condensate formed in the process steam superheating is used downstream as a heat transfer medium for feed preheating.
  • Table 2 use different designs of air preheater sequences, with 2, 3 or 4 stages, with use of low pressure steam and/or superheated (super) high pressure steam in addition to the illustrated use of feed water and/or (super) high pressure saturated steam.
  • the present invention can also be used in particular in a system as described in EP 3415 587 A1, for example, and in which the cracked gas is cooled directly against the feed stream and thus only part of the heat given off during cooling of the cracked gas is used for production of (super) high pressure steam is used. This is because the application of the measures described in the present application also provides the same or at least approximately the same advantages in such a system.
  • the present invention can also be used in a system with the separation of carbon dioxide from the flue gas.
  • measure 1 according to the invention particularly low exit temperatures of the flue gas are achieved at the end of the convection zone, which is advantageous for subsequent removal of carbon dioxide, e.g. by means of an amine scrubber (typical operating temperatures of amine scrubbers are 20 to 60°C).
  • the combustion air can also be enriched with oxygen.
  • oxygen enrichment is approximately comparable to air preheating, since the adiabatic combustion temperature is increased in each case and thus an increased
  • the effect is not (entirely) equivalent to air preheating, since the relatively higher oxygen content (with a lower nitrogen content, etc.) achieves the equivalent effect with a slightly different flue gas composition.
  • This is because proportionally more carbon dioxide and water are formed from the combustion - the former is advantageous, for example, when recovering the carbon dioxide by means of amine scrubbing and would apply even more to any flue gas recirculation.
  • the advantage is that you can achieve radiation zone efficiency. or flue gas reduction and thus lower firing savings beyond the values described for air preheating with (super) high-pressure steam.
  • the measures can be used for steam cracking furnaces with all possible hydrocarbon feeds. Examples are hydrocarbons with two, three and/or four carbon atoms (gaseous), naphtha (liquid), gas oil (liquid), and products from recycling processes such as plastics recycling (gaseous and liquid).
  • Partial air preheating can be chosen, for example, in the case where both bottom burners and side burners are used and only part of the burners are supplied with preheated air, preferentially the bottom burners.
  • the specified numerical values for air preheating temperatures always relate to the resulting preheating temperature of the entire combustion air.
  • Process streams from other plants e.g. gas turbine exhaust gas
  • saturated steam refers to the level up to approx. 175 bar (abs.) that has been typical and technically used up to now.
  • a higher pressure and temperature level e.g. 175 bar abs. and 355°C
  • the present invention is preferably used in combination with the electric drive of one or more compressors in the associated separating part of the system. This preferably compensates for the reduction in the (super) high-pressure steam export caused by the air preheating according to the invention.
  • Such increased electrification of the system also enables increased use of renewable energies by importing them from the power grid. Also to a lesser extent, steam boilers need to be kept available as backup systems for plant start-up.
  • the measures described can be applied both to completely new steam cracking furnaces and to the modernization of existing furnaces.
  • the advantages with regard to the total bundle height are particularly relevant, for example when it comes to accommodating modified bundle structures in an existing steel structure.
  • FIGS 1 to 4 show arrangements not according to the invention.
  • FIGS. 5 to 22 show arrangements according to embodiments of the invention and, where mentioned, arrangements not according to the invention.
  • FIG. 23 summarizes configurations of the invention and configurations not according to the invention in a schematic diagram.
  • the topology of the underlying convection zone 12 is shown in particular in FIG. However, other process configurations can also be used within the scope of the invention.
  • This topology includes, counter to the direction of the outflowing flue gas Z, a first feedwater preheater 121, a feed preheater 122, a second feedwater preheater 123, a first high-temperature bundle 124, a process steam superheater 125, a first (super) high-pressure steam superheater 126, a second (super) ) High-pressure steam superheater 127 and a second high-temperature bundle 128.
  • Feedwater W is passed through the first feedwater preheater 121 and the second feedwater preheater 123 and then fed to a corresponding (super) high-pressure steam generator, for example in the cracked gas cooler 13 .
  • (Super) high-pressure steam S generated there but not yet superheated is superheated (super) high-pressure steam T through the first (super) high-pressure steam superheater 126 and the second (super) high-pressure steam superheater
  • FIGS. 1 to 4 also apply to the following figures, and the reference symbols used in FIGS. 1 to 4 are also used in the following figures. For the sake of clarity, not all material flows are identified repeatedly in the following figures.
  • FIGS. 5 to 10 show variants of steam cracking plants designated 1A to 1F according to a first group of embodiments according to the invention.
  • the common feature is the use of chilled feed water for maximum energy recovery.
  • the principle of all variants 1A to 1F shown is to use the feed water already present in the furnace unit 10 as a heating medium for the air preheating 75 and optionally also for the heating gas preheating 65 in the low-temperature range, i.e. in a temperature range of up to 100°C.
  • the cooled feed water emerging from the preheater 75 and possibly 65 is fed after this to the convection zone 12, however, as also already mentioned, at a noticeably reduced temperature compared to the prior art.
  • the preheating shown in Figures 5 to 10 can consist of several stages, e.g. a first stage with feed water as the heating medium, a second stage with medium-pressure steam as the heating medium and a third stage with (super) high-pressure steam as the heating medium.
  • heating or heating media can also be used, as mentioned.
  • more or fewer preheating stages can also be provided, as also mentioned. Reference is also made to the above explanations for the use of heating medium that is running off or the return of condensate to the steam generation.
  • decentralized air preheating 75 is heated with feedwater WH, but no heating gas preheating takes place.
  • both a decentralized air preheater 75 with feedwater WH1 and a decentralized heating gas preheater 65 with feedwater WH2 are heated.
  • decentralized air preheating 75 is heated with feedwater WH1, but also central heating gas preheating 65 with feedwater WH2.
  • Two bypasses designated WB1, WB2 result.
  • decentralized air preheating 75 is heated with feedwater WH, while central heating gas preheating 65 takes place without heating with feedwater.
  • FIGS. 11 to 13 show variants of plants for steam cracking, denoted by 2A to 2C, according to a second group of configurations not according to the invention.
  • the feature that connects these is the use of the furnace's own (super) high-pressure saturated steam S as a heating medium in the air preheating 75.
  • the principle of the variants shown is that the saturated steam S generated in the steam generator 13 of the same cracker furnace 10 is used partially as a heating medium for the heating 75 of air in the middle to high temperatures, i.e. in a temperature range of 150 to 330°C.
  • the amount of saturated steam supplied to the steam superheaters 126, 127 in the convection zone 12 (cf. FIG. 4) is reduced accordingly, as a result of which proportionally more exhaust gas heat is available to the heat exchangers 121 to 125 arranged downstream in the path of the flue gas Z in the convection zone 12.
  • the resulting (super) high-pressure condensate can be fed to the central steam system of the plant, as shown in Figures 11, 12 and 13 for variants 2A, 2B and 2C, in order to continue to use the residual energy contained therein and finally to feed a suitable condensate treatment. It is also possible to reuse all or part of the condensate formed in previous preheating stages (i.e. at a lower temperature level), preferably after partial expansion to a reduced pressure level and addition of superheated steam at this reduced pressure level. However, subcooling of the condensate in the preheating can also be provided without prior expansion and admixture of superheated steam.
  • FIGS. 14 and 15 show variants, denoted by 3A and 3B, of plants for steam cracking according to a third group of embodiments according to the invention.
  • the feature that connects them is a combined use of feed water and (super) high-pressure saturated steam S as heating media in the air and/or heating gas preheating 65, 75.
  • the principle of all variants shown is the same as the measures previously explained for the first and second groups of configurations to be used, i.e. to be used for air and/or heating gas preheating 65, 75 in the low temperature range up to 100°C feed water W and additionally for air preheating 75 in the medium or high temperature range from 150 to 330°C saturated steam.
  • the preheating can consist of several stages, for example a first stage with feed water as the heating medium, a second stage with medium-pressure steam as the heating medium, and a third stage with super-high-pressure saturated steam as the heating medium.
  • Other possible types of heating or heating media can also be used, as mentioned.
  • more or fewer preheating stages can also be provided, as also mentioned.
  • draining heating medium or the recirculation of condensate in the steam generation reference is also made to the above explanations.
  • FIGS. 16 and 17 show variants, denoted 4A and 4B, of plants for steam cracking according to a fourth group of embodiments, FIG. 16 showing an embodiment not according to the invention and FIG. 17 showing an embodiment according to the invention.
  • the feature that connects these is the use of (super) high-pressure saturated steam S as a heating medium for overheating process steam P.
  • the principle of all variants shown is that the saturated steam S generated in the steam generator 13 of the same furnace 10 is partly used as a heating medium for overheating process steam P on average - to be used up to high temperatures, i.e. in the temperature range from 150 to 330°C.
  • the amount of saturated steam supplied to the steam superheaters 126, 127 for the saturated steam S in the convection zone 12 (cf.
  • a decentralized process steam heater 35 is provided in each case, whereby in the variant 4A illustrated in Figure 16 only this, in the variant illustrated in Figure 17 on the other hand also a decentralized air preheating 75' with (Super -) High-pressure saturated steam S is heated as the heating medium.
  • the variant illustrated in FIG. 17 also uses feed water as an embodiment according to the invention Air preheating, in this case in an upstream central air preheating 75.
  • FIGS. 18 and 19 show variants of steam cracking installations, previously designated 5A and 5B, according to a fifth group of embodiments, FIG. 18 showing an embodiment not according to the invention and FIG. 19 showing an embodiment according to the invention.
  • the feature that connects these is the use of (super) high-pressure saturated steam S as a heating medium for preheating the hydrocarbon charge H.
  • the principle of all variants shown is that the saturated steam S generated in the steam generator 13 of the same cracking furnace 10 is used partially as a heating medium for preheating the hydrocarbon charge H (incl . possible partial evaporation with liquid inserts) in the medium to high temperature range from 100 to 330°C.
  • a single-phase preheating of the feed stream takes place on the feed side (liquid or gaseous).
  • a decentralized insert heater 25 is provided in each case, whereby in the variant 5A illustrated in Figure 18 only this, in the variant illustrated in Figure 19, on the other hand, a decentralized air preheating 75' with (Super -) High-pressure saturated steam S is heated as the heating medium.
  • the variant illustrated in Figure 19 also has, as a configuration according to the invention, the use of feed water for air preheating, in this case in an upstream central air preheating system 75.
  • FIGS. 20 to 22 show variants of steam cracking installations, previously designated 6A to 6C, according to a sixth group of embodiments illustrated, wherein Figure 20 shows an embodiment not according to the invention and Figures 21 and 22 embodiments according to the invention.
  • the feature that connects them is a combined use of (super) high-pressure saturated steam S as a heating medium for process steam overheating and preheating of the insert.
  • the principle of all variants shown is that the saturated steam S generated in the steam generator 13 of the same cracking furnace 10 is partly used as a heating medium both for superheating process steam P in the medium to high temperature range of 150 to 330°C and for preheating the hydrocarbon feed stream H (incl.
  • the amount of saturated steam fed to the steam superheaters 126, 127 for the (super) high-pressure saturated steam S in the convection zone 12 is reduced accordingly, whereby proportionately more exhaust gas heat is distributed at a higher temperature level downstream in the path of the flue gas Z in the convection zone 12 Heat exchangers 121 to 125 is available.
  • the load on the superheater 125 for process steam P in the convection zone 12 is partially or completely reduced, so that even more exhaust gas heat is available at a higher temperature level for the heat exchangers 121 to 124 arranged downstream.
  • decentralized insert heating 25 and decentralized process steam superheating 35 are provided in each case.
  • these units are charged with saturated steam S in the manner shown.
  • the process steam superheater 35 and the insert preheater 25 are connected in series on the heat transfer medium side.
  • a decentralized air preheater 75' is additionally charged with saturated steam S.
  • the variants illustrated in Figures 21 and 22 also show, as configurations according to the invention, the use of feed water for air preheating, in this case in an upstream central air preheating system 75.
  • FIG. 23 summarizes configurations of the invention and configurations not according to the invention in a schematic diagram, with the corresponding material flows not being separately identified again.
  • the figure 23 illustrates in particular the possibility of centralized and decentralized provision of the previously explained units.

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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)
  • Air Supply (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Feeding And Controlling Fuel (AREA)

Abstract

La présente invention concerne un procédé de conversion d'un ou plusieurs hydrocarbures par vapocraquage. Dans ledit procédé, un ou plusieurs flux d'entrée (F) contenant l'un ou les hydrocarbures (H) sont guidés à travers une ou plusieurs zones rayonnantes (11) d'un ou de plusieurs fours de craquage (10), de telle sorte qu'un ou les flux de produit (C) soient obtenus ; l'une ou les zones rayonnantes (11) sont chauffées par combustion de gaz de chauffage (X) avec de l'air de combustion (L) ; au moins une partie de l'air de combustion (L) est soumise à un préchauffage de l'air de combustion (75) ; la vapeur (S, T) est produite à partir d'eau d'alimentation (W) ; et l'eau d'alimentation (W) est soumise à un préchauffage d'eau d'alimentation dans une ou plusieurs zones de convection (12) du ou des fours à craqueur (10). Le préchauffage de l'air de combustion (75) est effectué, au moins en partie et/ou au moins une partie du temps, au moyen de l'utilisation de la chaleur prélevée à partir d'au moins une partie de l'eau d'alimentation (W) en amont du préchauffage de l'eau d'alimentation. La présente invention concerne également une installation correspondante.
EP22710121.9A 2021-03-10 2022-03-08 Procédé et installation de vapocraquage Active EP4305129B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP21161729.5A EP4056668A1 (fr) 2021-03-10 2021-03-10 Procédé et installation de vapocraquage
PCT/EP2022/055873 WO2022189421A1 (fr) 2021-03-10 2022-03-08 Procédé et installation de vapocraquage

Publications (3)

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EP4305129A1 true EP4305129A1 (fr) 2024-01-17
EP4305129C0 EP4305129C0 (fr) 2024-06-26
EP4305129B1 EP4305129B1 (fr) 2024-06-26

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EP21161729.5A Withdrawn EP4056668A1 (fr) 2021-03-10 2021-03-10 Procédé et installation de vapocraquage
EP22710121.9A Active EP4305129B1 (fr) 2021-03-10 2022-03-08 Procédé et installation de vapocraquage

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EP (2) EP4056668A1 (fr)
JP (1) JP2024509584A (fr)
KR (1) KR20230154263A (fr)
CN (1) CN117295806A (fr)
AU (1) AU2022233249A1 (fr)
BR (1) BR112023018135A2 (fr)
CA (1) CA3212550A1 (fr)
WO (1) WO2022189421A1 (fr)

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WO2024218524A1 (fr) * 2023-04-20 2024-10-24 Dow Global Technologies Llc Modifications pour le craquage de charges lourdes

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3426733A (en) 1967-09-19 1969-02-11 Peter Von Wiesenthal Furnace and related process involving combustion air preheating
US4321130A (en) * 1979-12-05 1982-03-23 Exxon Research & Engineering Co. Thermal conversion of hydrocarbons with low energy air preheater
US4617109A (en) 1985-12-23 1986-10-14 The M. W. Kellogg Company Combustion air preheating
DE102004020223B4 (de) 2004-04-22 2015-05-21 Udo Hellwig Verfahren und Einrichtung zur Verbesserung des Wirkungsgrades von Kesselanlagen
WO2013178446A1 (fr) 2012-05-31 2013-12-05 Robert Bosch Gmbh Procédé de préchauffage d'air pour des chaudières à vapeur et dispositif pour mettre en œuvre ce procédé
EP3415587B1 (fr) 2017-06-16 2020-07-29 Technip France Système et procédé de four de craquage pour le craquage d'une charge d'hydrocarbures en son sein

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AU2022233249A1 (en) 2023-09-28
EP4056668A1 (fr) 2022-09-14
BR112023018135A2 (pt) 2023-12-12
CN117295806A (zh) 2023-12-26
WO2022189421A1 (fr) 2022-09-15
EP4305129C0 (fr) 2024-06-26
JP2024509584A (ja) 2024-03-04
CA3212550A1 (fr) 2022-09-15
EP4305129B1 (fr) 2024-06-26
KR20230154263A (ko) 2023-11-07

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