WO2025257407A1 - Procédé de production d'oléfines par vapocraquage - Google Patents

Procédé de production d'oléfines par vapocraquage

Info

Publication number
WO2025257407A1
WO2025257407A1 PCT/EP2025/066619 EP2025066619W WO2025257407A1 WO 2025257407 A1 WO2025257407 A1 WO 2025257407A1 EP 2025066619 W EP2025066619 W EP 2025066619W WO 2025257407 A1 WO2025257407 A1 WO 2025257407A1
Authority
WO
WIPO (PCT)
Prior art keywords
water
stream
steam
heat exchanger
liquid
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.)
Pending
Application number
PCT/EP2025/066619
Other languages
English (en)
Inventor
Tim LERCH
Iven Clausen
Martin Dorn
Marco SCHOENWALD
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.)
BASF SE
Original Assignee
BASF SE
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of WO2025257407A1 publication Critical patent/WO2025257407A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • 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

Definitions

  • the invention relates to a process for producing olefins comprising generating an olefins containing gas stream by steam cracking and cooling the gas stream in a quench apparatus by injecting water, thereby obtaining a cooled gas stream and a liquid stream.
  • Olefins for example ethylene, propylene or a mixture of butylene and aromatics are produced for example by steam cracking of raw materials like liquefied petroleum gas, natural gas liquids or naphtha.
  • the steam cracking process is described for example in Ullmann's Encyclopedia of Industrial Chemistry, "Ethylene”, Volume 13, 2012, pages 469 to 522.
  • the raw materials are fed into a furnace, in which the raw material are cracked by steam cracking forming a raw gas containing the desired product.
  • the raw gas obtained in the furnace then is fed into a working up section for cooling and separating the components in the raw gas.
  • a steam cracking process in which the product stream, which is obtained in the steam cracker, is cooled in a quench cooling train comprising at least two quench apparatus, is described in WO-A 2022/189424.
  • water evaporates and the steam is fed into a steam drum, in which saturated steam is obtained.
  • the saturated steam is used in another heat exchanger, in which it is superheated.
  • the steam then may be used in further applications.
  • EP-A 3730 592 and US-A 2022/0127209 describe processes for olefin synthesis, in which the energy required for operating the process is provided by a non-carbon based and/or renewable energy source and/or electricity. Heat being removed in a quench can be utilized in a heat integration, for example to preheat the feed stream. Further, a heat pump may be utilized.
  • EP-A 4 166 629 describes an ethylene plant, comprising an electrically-powered pyrolysis reactor and a quench cooling system with an oil quench and a water quench. At the bottom section of the water quench, a heat pump system is arranged to generate dilution steam.
  • cooling media particularly the liquids used in the quench apparatus still contain heat that may be used.
  • the water used in the water quench usually is circulated and the heat absorbed by the water in the water quench subsequently must be removed.
  • a part of the heat is used in heat integration, for example for preheating feed streams and as described for example in EP-A 3730 592 and US-A 2022/0127209.
  • additional coolers are used. These usually are operated with cooling water or ambient air. However, depending on ambient conditions, the temperature of the cooling water or the ambient air varies, which results in varying cooling conditions.
  • This object is achieved by a process for producing olefins comprising generating an olefins containing gas stream by steam cracking and cooling the gas stream in a quench apparatus by injecting water, thereby obtaining a cooled gas stream and a liquid stream, wherein at least a part of the liquid stream is used as a heat transfer medium to transfer heat to a water stream in a first heat exchanger and wherein the water stream after being heated in the first heat exchanger is fed into a flash evaporator in which the water partially evaporates by expansion to form steam, preferably for a steam grid to supply another plant or plants with industrial steam.
  • a device for operating the process comprises a steam cracker for generating an olefins comprising gas stream, a quench apparatus with an inlet for the olefins comprising gas stream, an outlet for a cooled gas stream and an outlet for a liquid stream, a first heat exchanger for heating water by heat exchange with the liquid stream withdrawn from the quench apparatus, a flash apparatus for evaporating water by expansion, which is connected to a water outlet of the first heat exchanger and preferably at least one compressor for compressing steam obtained by the evaporation of water in the flash apparatus.
  • starting hydrocarbons are fed into a cracking reactor in which they are cracked into the olefins, thereby obtaining a gaseous intermediate product stream.
  • Typical hydrocarbons used for producing the olefins are saturated aliphatic hydrocarbons.
  • the starting hydrocarbons may be of fossil origin, or bio-based hydrocarbons or may be obtained by chemical recycling, for example by ChemCycling® as described for example on "https://www.basf.com/global/de/who-we-are/sustainability/we-drive- sustainable-solutions/circular-economy/mass-balance-approach/chemcycling.html”, retrieved on March 22, 2024, or may be obtained by any other chemical process or be a byproduct thereof, or may be a combination of hydrocarbons obtained by any of those or all mentioned processes.
  • the starting hydrocarbons used in the process for producing olefins are at least one of liquefied petroleum gas, natural gas liquids, like ethane, propane, butane, isobutane, and pentane, particularly ethane or propane, and naphtha.
  • Olefins produced in the cracking reactor and contained in the gaseous intermediate product stream preferably are ethylene, propylene and/or butene, particularly butene with one double bond.
  • the olefins are ethylene and/or propylene.
  • waste products are converted by pyrolysis, i.e.
  • a feedstock such as plastic waste under inert conditions that results in a gas, a liquid, and a solid char fraction.
  • the feedstock is converted in a pyrolysis unit into a great variety of chemicals including gases such as H2, Ci- to C4-alkanes, C2- to C4-alkenes, ethyne, propyne, 1 -butyne, pyrolysis liquid having a boiling temperature of 25 °C to 500 °C or more and char.
  • gases such as H2, Ci- to C4-alkanes, C2- to C4-alkenes, ethyne, propyne, 1 -butyne, pyrolysis liquid having a boiling temperature of 25 °C to 500 °C or more and char.
  • the direct products from such a pyrolysis are "pyrolysis gas” and solid products.
  • the liquid product "pyrolysis liquid” is then separated by condensation from the "pyrolysis gas”.
  • water is formed during the pyrolysis.
  • the water may be partially dispersed in the pyrolysis liquid and may be partially contacted with the pyrolysis liquid in a separate phase.
  • the water formed during pyrolysis comprises various organic compounds and/or salts thereof, which were also formed during the pyrolysis.
  • the term "pyrolysis” includes slow pyrolysis, fast pyrolysis, flash pyrolysis and catalytic pyrolysis. These pyrolysis types differ regarding process temperature, heating rate, residence time, feed particle size, etc. resulting in different product quality.
  • the pyrolysis unit may be operated adiabatically, isothermally , nonadiabatically, non-isothermally, or combinations thereof.
  • the pyrolysis reactions of this disclosure may be carried out in a single stage or in multiple stages.
  • the pyrolysis unit can comprise two reactor vessels fluidly connected in series.
  • pyrolysis liquid is understood to mean any oil originating from the pyrolysis of plastic waste.
  • plastic waste includes rubber waste such as end-of-life tires and feedstocks comprising plastic waste.
  • the pyrolysis liquid is obtained and/or obtainable from pyrolysis of such plastic waste.
  • plastic waste refers to any plastic material discarded after use, i.e., the plastic material has reached the end of its useful life and is considered post-consumer waste.
  • the plastic waste can be pure polymeric plastic waste, mixed plastic waste or film waste, including soiling, adhesive materials, fillers, residues etc.
  • the plastic waste may have an oxygen content, a nitrogen content, sulfur content, halogen content and optionally also a heavy metal content.
  • the plastic waste can originate from any plastic material containing source.
  • plastic waste includes industrial and domestic plastic waste and including used tires and agricultural and horticultural plastic material.
  • plastic waste is a mixture of different plastic materials, including hydrocarbon plastics, e.g., polyolefins such as polyethylene (HDPE, LDPE) and polypropylene, polystyrene, and copolymers thereof, etc., and polymers composed of carbon, hydrogen, and other elements such as chlorine, fluorine, oxygen, nitrogen, sulfur, silicone, etc., for example chlorinated plastics, such as polyvinylchloride (PVC), polyvinylidene chloride (PVDC), etc., nitrogencontaining plastics, such as polyamides (PA), polyurethanes (PU), acrylonitrile butadiene styrene (ABS), etc., oxygen-containing plastics such as polyesters, e.g., polyethylene terephthalate (PET), polycarbonate (PC), etc., silicones and/or sulfur bridges crosslinked rubbers.
  • hydrocarbon plastics e.g., polyolefins such as polyethylene (HDPE, LDPE)
  • the plastic material comprises additives, such as processing aids, plasticizers, flame retardants, pigments, light stabilizers, lubricants, impact modifiers, antistatic agents, antioxidants, etc.
  • additives may comprise elements other than carbon and hydrogen.
  • bromine is mainly found in connection to flame retardants.
  • Heavy metal compounds may be used as lightfast pigments and/or stabilizers in plastics.
  • Cadmium, zinc, and lead may be present in heat stabilizers and slip agents used in plastics manufacturing.
  • the plastic waste can also contain residues. Residues in the sense of the invention are contaminants adhering to the plastic waste.
  • the additives and residues are usually present in an amount of less than 50 wt.-%, preferably less than 30 wt.-%, more preferably less than 20 wt.-%, even more preferably less than 10 wt.-%, based on the total weight of the dry weight plastic.
  • Examples of rubber waste include end-of-life tires, rubber waste produced during manufacturing processes and discarded rubber containing products such as latex examining gloves and gaskets.
  • End-of-life tires comprise further ingredients such as textiles and organic and inorganic additives which may be separated from the rubber portion of end-of-life tires prior to pyrolysis.
  • Pyrolysis liquids obtained by pyrolysis of (predominantly) end-of-life tires are also known as tire pyrolysis oils (TPO).
  • bio-based starting hydrocarbons typically start with the conversion of biomass to bio-oil, e.g., via mechanical operations and chemical processes. Due to its chemical composition, especially due to its high oxygen content, said bio-oil is typically not directly suitable to be used in cracking processes to obtain olefins, aromatics, and other cracking products, but needs to be further refined and/or upgraded, especially catalytically hydrotreated.
  • This hydrotreatment yields hydrocarbons that may be separated into different fractions like renewable fuels (HVO, SAF), bio-naphtha, and bio-based Cu-hydrocarbons (bio-Cu-HCs) which can be used as feed streams for cracking processes, e.g. steam cracking.
  • HVO renewable fuels
  • SAF bio-naphtha
  • bio-Cu-HCs bio-based Cu-hydrocarbons
  • Bio-based hydrocarbons Animal fats, vegetable oils (e.g., rapeseed, sunflower, soybean, palm, and camelina oil), waste oils and fats (e.g., used cooking oil, waste animal fats), microbial and algal oils, and fatty acids represent the most important biomass- derived raw materials for bio-based hydrocarbon production.
  • bio-based hydrocarbons Among the major pathways towards bio-based hydrocarbons is the catalytic hydrotreatment of these mono-, di-, and triglycerides and fatty acids, which includes hydrogenation, decarboxylation, decarbonylation, hydroisomerization, and cracking processes under high temperature and pressure conditions, frequently also including a catalytic isomerization step, resulting in a hydrocarbon mixture comprising n- and iso-paraffins, among others.
  • reaction products may be further separated into gaseous and liquid fractions, which constitute valuable transportation fuels and chemical feedstocks, e.g., as renewable diesel (hydrotreated vegetable oils: HVOs), renewable jet fuel (sustainable aviation fuel: SAF), bio-naphtha (a mixture of hydrocarbons mainly comprising paraffins, e.g. of up to 10 carbon atoms, that can be used - similar to naphtha of fossil origin - as a gasoline blending component or as a chemical feedstock, e.g., for crackers), and other low-boiling hydrocarbons (i.e. mainly C1-4 hydrocarbons, in particular C1-4 alkanes) like bio-based liquefied petroleum gas (LPG; e.g.
  • LPG liquefied petroleum gas
  • biomass designates any material of vegetable or animal origin that is in principle suitable to be converted at least into bio-oils.
  • biomass comprises plants or parts thereof like crops, wood, or residues thereof, marine organisms like algae, and bio waste such as organic food waste, e.g., animal fat from meat industry waste, fish fat from fish processing waste, or used cooking oil.
  • biomass may comprise or be derived from algae, oil crops, oil palms, soybeans, rapeseed, mustard, flax, cottonseed, sunflower, corn, castor beans, hemp, field pennycress, pongamia, jatropha, macauba palm (kernel or pulp), mahua, camelina, salicornia, carinata, lignocellulose, wood, forestry residues, agricultural residues, crop residues, straw, residues from vegetable oil production, green waste, food waste, and used vegetable cooking oil.
  • the biomass may be composed of biomass streams from various of the above-mentioned sources.
  • the processing of biomass into bio-oil may comprise both mechanical and physical operations, like harvesting and collecting as well as crushing, cracking, cutting, shredding, grinding, chipping, milling, extrusion, irradiation, squeezing, pressing, filtering, sieving, adsorption, and thermal treatments such as drying and torrefaction, and chemical processes, like extraction, distillation, thermochemical conversions like pyrolysis or hydrothermal liquefaction, gasification followed by Fischer-Tropsch processes, hydrolysis, saponification, neutralization, ketonization, or hydrogenation.
  • mechanical and physical operations like harvesting and collecting as well as crushing, cracking, cutting, shredding, grinding, chipping, milling, extrusion, irradiation, squeezing, pressing, filtering, sieving, adsorption, and thermal treatments such as drying and torrefaction, and chemical processes, like extraction, distillation, thermochemical conversions like pyrolysis or hydrothermal liquefaction, gasification followed by Fischer-Trop
  • processing of biomass into bio-oil comprises purification steps, inter alia the removal of all by-products from the biooil that are not suitable or are detrimental for further use as a feedstock for subsequent hydrotreatment.
  • purification steps inter alia the removal of all by-products from the biooil that are not suitable or are detrimental for further use as a feedstock for subsequent hydrotreatment.
  • suitable process steps and operating conditions is mainly dependent on the biomass to be processed; but the one skilled in the art will be familiar with such considerations.
  • processing biomass into bio-oil suitable may include the removal of solids, ash particles, and/or metal residues, e.g., via filtration and adsorption steps. Further, said processing may include extraction, distillation, neutralization, esterification, and ketonization steps, e.g., to remove water, oxygen-rich species, and/or high-boiling components. Said process steps may also be used to increase the stability and/or the heating value of the bio-oil or to reduce its viscosity and/or its corrosivity.
  • processing the biomass into bio-oil may also comprise purification steps, e.g., to remove contaminants or impurities that may be detrimental for the further process steps or for further use of the end-products of the process.
  • the starting hydrocarbons are thermally cracked with steam in the cracking reactor.
  • the reaction is carried out at high temperatures, generally in the range from 750 to 875 °C.
  • the starting hydrocarbons may be heated for example by heat exchange against flue gas in a convection section of the cracking reactor, mixed with steam and further heated to incipient cracking temperature, which generally is in a range from 500 to 680 °C.
  • the reaction stream containing the steam and the starting hydrocarbons may be fed for example into a fired tubular reactor, in which the starting hydrocarbons are cracked into smaller molecules within a short reaction time, which generally is in a range between 0.1 and 0.5 s.
  • the cracking may be carried out in any other reactor known to the skilled person in which the starting hydrocarbons can be cracked into the desired olefins.
  • the gaseous intermediate product stream is rapidly cooled to a temperature at which the reaction stops and also the formation of undesired by-products is minimized. This rapid cooling generally is carried out in a transfer line exchanger (TLE). Subsequently, the gaseous intermediate product stream is cooled by adding a quenching liquid in a quenching apparatus, thereby obtaining the crude product stream containing the gaseous olefins and the liquid stream containing the quenching liquid and condensed by-products.
  • TLE transfer line exchanger
  • Typical by-products obtained in the cracking process are acetylenic, diolefinic and aromatic compounds, for example benzene, ethyl benzene, toluene, xylene, styrene, cyclopentane, cyclopentene, n-hexane, methyl cyclopentane, and methyl cyclopentene.
  • these by-products usually have a boiling temperature above the boiling temperature of the olefins which are obtained in the cracking reaction as desired products, they are condensed during cooling and then referred to as the "condensed by-products”.
  • the TLE preferably is directly connected to the cracking reactor to avoid additional reaction time due to the time the gaseous intermediate product stream needs for flowing from the cracking reactor to the TLE.
  • the quenching liquid used for cooling the intermediate product stream in the quenching apparatus following the TLE may be any liquid which is inert to the components in the intermediate product stream and which is inflammable at the temperature the intermediate product stream comes into contact with the quenching liquid.
  • Quenching of the intermediate product stream may be carried out in one or more quenching steps. Independently of whether cooling is carried out in only one quenching step or in more than one quenching steps, it is preferred that the quenching liquid used in the quenching apparatus is water.
  • quenching is carried out in more than one quenching step, more preferred in at least two quenching steps and particularly in two quenching steps.
  • the intermediate product stream firstly is cooled in an oil quench and subsequently in a water quench.
  • the oil being used for cooling the gaseous intermediate reaction product in the oil quench may be for example Cw- to Ci6-hydrocarbons with a boiling point below 250 °C, preferably with a boiling point below 200 °C.
  • water is used as the quenching liquid.
  • an oil as previously described for quenching in two steps is used and in the at least one further quenching step between the first quenching step and the last quenching step in which water is used as quenching liquid, either an oil, particularly the same oil as in the first quenching step, or water may be used as quenching liquid.
  • water particularly the same oil as in the first quenching step
  • water may be used as quenching liquid.
  • quenching steps following the first quenching step in which water is used as a quenching liquid also water is used as the quenching liquid, so that independently of the number of quenching stages, first an oil is used as quenching liquid and then water.
  • the first quenching apparatus is connected downstream to the TLE and the following quenching apparatuses may be connected directly to the outlet of the first quenching apparatus or may be connected to the first quenching apparatus by suitable connecting pipes.
  • the crude product stream containing the gaseous olefins may be transferred into a working-up treatment for removing undesired gaseous products and separating the different olefins and obtain the desired products in desired purity.
  • the crude product stream is treated by a caustic wash.
  • the crude reaction product may be further worked up to obtain the pure products.
  • Working-up the crude product stream after the caustic wash may be carried out by any processes known to a skilled person, for example condensation, extraction, distillation, rectification and/or hydrogenation.
  • the crude product stream is worked-up by rectification and subsequent hydrogenation.
  • the liquid phase containing the quenching liquid and the condensed by-products is further worked up to separate the condensed by-products from the quenching liquid.
  • Separating the condensed by-products from the quenching liquid may be carried out in any suitable separation apparatus.
  • the separation apparatus preferably is a phase separator. Suitable phase separators for example are gravity separators or coalescers.
  • separating the condensed by-products from the quenching liquid is operated before using the heat of the liquid stream for heating the water stream in the first heat exchanger.
  • the liquid stream used for heating the water stream in the first heat exchanger usually comprises 95 to 100 wt-% water and 0 to 5 pyrolysis gasoline, more preferred 97 to 99.99 wt-% water and 3 to 0,01 wt-% pyrolysis gasoline and particularly 99 to 99.9 wt-% water and 0.1 to 1 wt-% pyrolysis gasoline.
  • the quenching liquid After being separated, the quenching liquid can be recycled into the quenching apparatus. As residues of the condensed by-products which are not separated in the separation step result from the reaction process, it is not necessary to further clean the quenching liquid before recycling into the quenching apparatus. However, to avoid accumulation of components which are not separated off in the phase separation, it either may be necessary to further clean the quenching liquid for removing these components or to withdraw a part of the quenching liquid and add a respective amount of fresh quenching liquid. As the quenching liquid absorbs heat during quenching, it is further necessary to cool the quenching liquid before recycling into the quenching apparatus. The heat absorbed by the quenching liquid particularly is used in a heat integration for example for preheating the feed stream.
  • At least a a part of the liquid stream obtained in the quench apparatus is used as a heat transfer medium to transfer heat to a water stream in a first heat exchanger.
  • the water stream is heated to a temperature in a range from 17 to 80 °C, more preferred to a temperature in a range from 45 to 75 °C, more preferred to a temperature in a range from 55 to 73 °C and particularly to a temperature in a range from 55 to 70 °C and the liquid stream is cooled to a temperature in a range from 50 to 80 °C, particularly to a temperature in a range from 55 to 70 °C.
  • the water stream After being heated, the water stream is fed into the flash evaporator, in which the water partially evaporates by expansion to form steam.
  • the water stream which absorbs heat in the first heat exchanger preferably has a pressure in a range from 0.8 to 16 bar(abs), more preferred in a range from 0.95 to 6 bar(abs) and particularly in a range from 1 to 3 bar(abs).
  • the water stream In the flash evaporator, the water stream is expanded to a pressure in a range from 20 to 300 mbar(abs), more preferred in a range from 120 to 280 mbar(abs) and particularly in a range from 150 to 220 mbar(abs).
  • a feed water stream is fed into the first heat exchanger.
  • the feed water stream may be mixed constantly into the water stream withdrawn from the flash evaporator or the feed water stream is fed into the process discontinuously and during feeding the feed water stream, no water is withdrawn from the flash evaporator and recycled into the first heat exchanger.
  • the feed water stream is in a range from 0.5 to 18 wt-%, more preferred in a range from 1 to 5.5 wt-% and particularly in a range from 2 to 4 wt-% based on the total amount of water stream circulated from the flash evaporator and the feed water stream.
  • a part of the liquid stream may be used as a heat transfer medium to transfer heat in a second heat exchanger to the feed water stream, wherein the feed water stream preferably is heated to a temperature in a range from 30 to 85 °C, more preferred to a temperature in a range from 50 to 75 °C and particularly to a temperature in a range from 65 to 70 °C.
  • the part of the liquid stream used for preheating the feed water stream in the second heat exchanger preferably is recycled into the quenching apparatus as cooling medium downstream the second heat exchanger. If a part of the liquid stream is used as a heat transfer medium in the first heat exchanger and a part is used as a heat transfer medium in the second heat exchanger, it is preferred to mix the liquid streams downstream the first and second heat exchangers and feed the combined liquid streams into the quench apparatus or into an air cooler.
  • 0.1 to 10.0 wt-% of the water stream evaporate in the flash evaporator. More preferred, 1 to 5 wt-% of the water stream evaporate in the flash evaporator, more preferred, 2.2 to 3.3 wt-% of the water stream evaporate in the flash evaporator and particularly, 2.4 to 3.1 wt-% of the water stream evaporate in the flash evaporator.
  • the flash evaporator may be any suitable flash evaporator known to a skilled person.
  • a suitable flash evaporator for example may be a flash tank or a column.
  • a pressure is set, which corresponds to the pressure at which the water partly evaporates.
  • the pressure in the flash is generated by the compressors for compressing the steam.
  • a suitable vacuum pump may be provided which keeps the pressure in the flash evaporator during process interruptions or for start-up processes.
  • steam used in industrial processes usually has a pressure and a temperature above the pressure and the temperature in the flash evaporator, it is particularly preferred that steam is withdrawn from the flash evaporator the steam is compressed to a higher pressure in compressors downstream the flash evaporator. By compression also the temperature of the steam rises.
  • the compressed steam may be used in a steam grid to supply a plant or plants with industrial steam.
  • the steam shall have, it may be advantageous to compress the steam obtained by evaporation of the water stream in the flash evaporator in at least one compressor, preferably in a compressor cascade comprising 2 to 15 compressors.
  • the steam produced by compression of the steam obtained in the flash evaporator may be low-pressure steam, midpressure steam or high-pressure steam. Further, it is also possible to compress a part of the steam to low-pressure steam, a part of the steam to mid-pressure steam and/or a part of the steam to high pressure-steam. If low-pressure steam and mid-pressure steam and/or high-pressure steam are produced, it is preferred to compress the whole steam to low-pressure steam and to further compress the part of the stream not to be used as low-pressure steam to mid-pressure steam and, if mid-pressure steam is used, the final part to high-pressure steam, or if no mid-pressure steam is used, the part not to be used as low-pressure steam to high-pressure steam. Accordingly, if no low-pressure steam is to be produced, all steam obtained in the flash evaporator is compressed to mid-pressure steam and/or high-pressure steam.
  • the steam compressed in the compressors may be directly fed to consumers or, preferably, into a respective steam grid in which the steam is distributed to different consumers.
  • the steam compressed in the compressors may be used to transfer a part of its thermal energy to evaporate at least partially a water mass flow, wherein the evaporated water mass flow is preferably fed into a respective steam grid in which that steam is distributed to different consumers.
  • the water of the water mass flow is preferably desalinated or degassed water, more preferred desalinated and degassed water.
  • Low-pressure steam in the context of the present invention is steam having a pressure in a range from 900 to 4000 mbar(abs), preferably in a range from 2000 to 3500 mbar(abs) and particularly in a range from 2500 to 3000 mbar(abs), and a temperature in a range from 96 to 220 °C, more preferred in a range from 111 to 210 °C and particularly in a range from 127 to 200 °C.
  • Mid-pressure steam in the context of the present invention is steam having a pressure in a range from 4000 to 8000 mbar(abs), more preferred in a range from 4500 to 7000 mbar(abs) and particularly in a range from 5000 to 6800 mbar(abs) and a temperature in a range from 143 to 230 °C, more preferred in a range from 148 to 215 °C and particularly in a range from 159 to 200 °C.
  • High-pressure steam in the context of the present invention is steam having a pressure in a range from 8000 mbar(abs) to 50 bar(g), more preferred in a range from 9 to 49 bar(g) and particularly in a range from 15 to 49 bar(g) and a temperature in a range from 170 to 350 °C, more preferred in a range from 180 to 325 °C and particularly in a range from 250 to 300 °C.
  • a compressor cascade comprising 1 to 15 compressors, more preferred 1 to 11 compressors and particularly 1 to 9 compressors.
  • a compressor cascade comprising 1 to 20 compressors, more preferred 1 to 15 compressors and particularly 1 to 11 compressors, and for producing high-pressure steam, it is preferred to use a compressor cascade comprising 1 to 30 compressors, more preferred 1 to 25 compressors and particularly 1 to 20 compressors.
  • the compressors used to produce the steam with the lower pressure also are regarded as being part of the compressor cascade to produce the steam with the higher pressure.
  • a part of the feed water stream into the compressor cascade between two compressors after being heated in the second heat exchanger.
  • a connecting line for feeding water withdrawn from the second heat exchanger into at least one of the at least one compressors is provided for feeding the part of the feed water stream into the compressor cascade.
  • the part of the feed water stream may be fed directly into a compressor or, preferably, into a line connecting two compressors.
  • the water of the feed water stream is degassed and demineralized water.
  • Demineralizing and degassing of the water may be carried out as well known to a skilled person, for example by boiling. Degassing may be carried out simultaneously with the demineralizing, but preferably, the water firstly is demineralized and subsequently degassed, because it cannot be excluded that during demineralization gas is absorbed by the water. Degassing may be carried out for example by boiling the water in a closed vessel.
  • the present invention further relates to a target product that can be obtained or achieved by a method according to the present invention.
  • Reference RF1 The publication Prior Art Disclosure; Issue 684; paragraphs [1000] to [8005]; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1, which is incorporated herein by reference in its entirety.
  • the target product is a product as described in Reference RF1; paragraphs [1000] to [8005],
  • the process described herein is further a process for the production of a product, preferably a target product.
  • the converting step to obtain the target product preferably comprises one or more step(s) as described below and can be performed by conventional methods well known to a person skilled in the art.
  • the converting step preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and/or steam cracking; and/or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and/or subjecting to ion exchanger; and/or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and/or compounding; and/or forming, preferably foaming, extruding and/or molding; and/or finishing, preferably coating and/or smoothing.
  • the one or more step(s) are described in detail in Reference RF1; paragraphs [1000] to [8005],
  • building block comprises compounds, which are in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a higher structural complexity and/or higher molecular weight than the building block on which the secondary product is based.
  • the building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic compounds.
  • the alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.
  • the term "monomer”, as used herein, comprises molecules, which can react with each other to form polymer chains by polymerization.
  • the monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates.
  • (Meth)acrylates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms.
  • (meth)acrylic acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable.
  • the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.
  • the building block can further be an intermediate compound.
  • intermediate compound comprises organic reagents, which are applied for formation of compounds with higher molecular complexity.
  • the intermediate compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide.
  • the polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and/or diphenylmethane diisocyanate (MDI).
  • TDI toluene diisocyanate
  • MDI diphenylmethane diisocyanate
  • polymer A comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs [2001] to [2007] of Reference RF1.
  • polymer composition A comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. reinforcement, colorant, modifier and/or flame retardant, and is defined in more detail in paragraph [2008] of Reference RF1.
  • additive(s) e.g. reinforcement, colorant, modifier and/or flame retardant
  • polymer product A comprises any product comprising the polymer A and/or polymer composition A as described above and is defined in more detail in paragraphs [2009] and [2010] of Reference RF1.
  • the step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymer composition A or polymer product, preferably polymer product A is/are described in more detail in paragraph [2011] of Reference RF1 .
  • the term "industrial use polymer”, as used herein, comprises rheological polymers, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, polyether-based, dye inhibition polymers and soil release cleaning polymers defined in more detail in paragraphs [3035] to [3044] of Reference RF1.
  • industrial use surfactant comprises non-ionic, anionic and amphoteric industrial use surfactants defined in more detail in paragraphs [3008] to [3034] of Reference RF1.
  • NPB nonphosphate based builders
  • CoP phosphonates
  • the term "industrial use biocide”, as used herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs [3006] to [3007] of Reference RF1 .
  • the term "industrial use solvent”, as used herein, comprises alkyl amides, alkyllactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs [3045] to [3055] of Reference RF1.
  • the term "industrial use dispersant”, as used herein, comprises anionic and non-ionic industrial use dispersants defined in more detail in paragraphs [3056] to [3058] of Reference RF1.
  • composition and/or formulation thereof' with reference to the industrial use polymers, industrial use surfactants, descaling compounds and/or industrial use biocides refers to industrial use compositions and/or institutional use products and/or fabric and home care products and/or personal care products defined in more detail in paragraph [3059] of Reference RF1.
  • the converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and/or industrial use biocide are defined in more detail in paragraph [3060] of Reference RF1 .
  • the converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and/or industrial use biocide are defined in more detail in paragraph [3061] of Reference RF1.
  • agrochemical composition typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary.
  • agrochemical compositions include agrochemically active ingredient and at least one agrochemical formulation auxiliary.
  • active ingredients and auxiliaries are described in more detail in Reference RF1, paragraph [4001].
  • the agrochemical composition may take the form of any customary formulation.
  • the agrochemical compositions are prepared in a known manner, e.g. described by Mollet and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005.
  • the converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes.
  • conversion to compounds mentioned in sections "Polymer” and "Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof' may be performed as described in these sections as well as the respective paragraphs in Reference RF1.
  • active pharmaceutical ingredients and/or intermediates thereof comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body.
  • Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient.
  • pharmaceutical excipients comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and/or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph [5001] of Reference RF1.
  • the converting step(s) to obtain the active pharmaceutical ingredients and/or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
  • animal feed additives human food additives, dietary supplements, as used herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propionic acid and ammonium propionate
  • Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph [5002] of Reference RF1.
  • the converting step(s) to obtain the animal feed additives, human food additives, dietary supplements may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
  • aroma chemical and aroma composition as used herein, comprise a volatile organic substance with a molecular weight between 70-250 g/mol comprising a functional group with a carbon skeleton of C5-C16 carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-C18, bicyclic or tricyclic aliphatic chains and but not necessarily one or more unsaturated structural elements like double bonds, triple bonds, aromatics or heteroaromatics and preferably the one or more additional functional groups are selected from alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, amine.
  • the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes or tetraterpenes.
  • Aroma chemicals can be combined with further aroma chemicals to give an aroma composition.
  • Aroma chemicals and aroma compositions are defined in more detail in paragraph [5003] of Reference RF1.
  • the converting step(s) to obtain the aroma chemical and aroma composition may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
  • aqueous polymer dispersion comprises aqueous composition(s) comprising dispersed polymer(s) and is defined in more detail in the section [6001] entitled “aqueous polymer dispersion” of Reference RF1.
  • the dispersed polymer(s) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s).
  • emulsion polymer comprises polymer(s) made by free-radical emulsion polymerization.
  • Aqueous polyurethane dispersion(s) are defined in more detail in the section [6002] entitled “Polyurethane dispersions” of Reference RF1.
  • UV-curable polyurethane(s) is/are defined in more detail in the section [6017] of Reference RF1.
  • Polyurethane - poly(meth)acrylate hybrid polymer(s) is/are defined in more detail in the section [6016] of Reference RF1.
  • polymeric dispersant comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph [6020] entitled “Polymeric dispersant” of Reference RF1.
  • the converting (polymerization) step(s) to obtain the aqueous polymer dispersion(s) comprising emulsion polymer(s) is/are defined in more detail in the section [6003] entitled “Emulsion polymerization” of Reference RF1.
  • the converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is/are defined in more detail in the section [6014] entitled “Process for the preparation of aqueous polyurethane dispersions” and section [6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1.
  • composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail in the following sections of Reference RF1 : section [6004] entitled “Uses of aqueous polymer dispersions”, section [6005] entitled “Binders for architectural and construction coatings” section [6006] entitled “Binders for paper coating” section [6007] entitled “Binders for fiber bonding” section [6008] entitled “Adhesive polymers and adhesive compositions” section [6015] entitled “Aqueous polyurethane dispersions suitable for use in coating compositions” section [6016] entitled “Aqueous polyurethane - poly(meth)acrylate hybrid polymer dispersions suitable for use in coating compositions” section [6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them section [6018] entitled “Inorganic binder compositions comprising polymeric dispersants and their use” [60
  • Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section [6010] entitled “Polyisocyanates” of Reference RF1.
  • Hyperbranched polyester polyol(s) and its/their uses are defined in more detail in section [6011] entitled “Organic solvent based hyperbranched polyester polyols suitable for use in coating compositions” of Reference RF1.
  • the converting step(s) to obtain the hyperbranched polyester polyols is/are defined in more detail in the section [6012] entitled "Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1 .
  • Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section [6013] entitled "Organic solvent based two component coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1.
  • Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsaturated polyester polyol(s) and substrate(s) for coating with said coating composition(s) are defined in more detail in section [6018] entitled “Organic solvent based coating composition comprising unsaturated polyester polyols” of Reference RF1.
  • 100% curable coating composition(s) is/are defined in more detail in section [6019] of Reference RF1.
  • Polymeric dispersant(s) for inorganic binder compositions is/are defined in more detail in section [6020] of Reference RF1.
  • the inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section [6021] of Reference RF1.
  • the converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section [6020] of Reference RF1 .
  • inorganic binder composition comprising the polymeric dispersant(s), as used herein, comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section [6021] of Reference RF1 entitled "Inorganic binder compositions comprising the polymeric dispersant and their use”.
  • Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section [6021] of Reference RF1.
  • cosmetic surfactant comprises non-ionic, anionic, cationic, and amphoteric surfactants and is defined in more detail in paragraph [7002] of Reference RF1.
  • emollient refers to a chemical compound used for protecting, moisturizing, and/or lubricating the skin and is defined in more detail in paragraph [7003] of Reference RF1.
  • wax comprises pearlizers and opacifiers and is defined in more detail in paragraph [7004] of Reference RF1.
  • cosmetic polymer comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph [7005] of Reference RF1.
  • UV filter refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph [7006] of Reference RF1.
  • consumer cosmetic ingredient comprises any ingredient suitable for making a cosmetic formulation.
  • cosmetically acceptable ingredients E. g. the database Cosing on the internet pages of the European Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredients.
  • composition and/or formulation thereof' with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and/or further cosmetic ingredient refers to personal care and/or cosmetic compositions or formulations defined in more detail in paragraph [7007] of Reference RF1.
  • the converting step(s) to obtain the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is/are defined in more detail in paragraph [7008] of Reference RF1.
  • the target product is selected from: i) building block or monomer; or ii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or ill) cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or vi) aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyper branched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% cur
  • the content of the olefin in the target product is 1 weight-% or more, preferably 2 weight- % or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and/or the content of the olefin in target product is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably the content is determined based on identity preservation and/or segregation and/or mass balance and/or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.
  • ISCC International Sustainability and Carbon Certification
  • the method comprises the step of converting the product of the process, namely olefin, which can be achieved or obtained by one of the above-mentioned embodiments, to obtain the target product.
  • Figure 1 shows schematically a steam cracking process
  • Figure 2 shows schematically a process for producing steam by use of the heat of the liquid stream obtained in a quench apparatus of a steam cracking process in a first embodiment
  • Figure 3 shows schematically a process for producing steam by use of the heat of the liquid stream obtained in a quench apparatus of a steam cracking process in a second embodiment
  • Figure 4 shows schematically a process for producing steam by use of the heat of the liquid stream obtained in a quench apparatus of a steam cracking process in a third embodiment
  • Figure 5 shows schematically a process for producing steam by use for the heat of the liquid stream obtained in a quench apparatus of a steam cracking process in a fourth embodiment.
  • Figure 1 shows a schematic flow chart of a steam cracking process.
  • starting hydrocarbons 1, for example naphtha, and steam 3 are fed into a furnace 5 for steam cracking.
  • the furnace 5 may be any furnace suitable for steam cracking known to a skilled person and may be heated for example by combusting a fuel gas.
  • the furnace 5 comprises burners 7 in which the fuel gas 9 is combusted and the heat necessary for carrying out the endothermic cracking reaction is supplied.
  • the temperature in the furnace 5 usually is in a range from 700 to 1200 °C, preferably 750 to 1000 °C.
  • the reaction mixture comprising olefins and steam is cooled in a transfer line exchanger 11. Due to the heat consumed by the reaction, the reaction mixture leaving the furnace usually has a temperature in a range from 750 to 875 °C, for example 840 °C.
  • the transfer line exchanger 11 the reaction mixture is cooled to a temperature in a range from 300 to 600 °C, preferably in a range from 350 to 500 °C and particularly in a range from 380 to 450 °C, for example 450 °C by indirect heat transfer to water 13 as heat transfer medium.
  • the water evaporates, thereby forming high-pressure steam 15.
  • the reaction mixture is fed into a first quench apparatus 17, in which the reaction mixture is cooled to a temperature in a range from 90 to 120 °C, preferably in a range from 95 to 115 °C and particularly in a range from 100 to 110 °C, for example 105 °C by mixing the reaction mixture with a quenching liquid, particularly a quenching oil like C10- to Ci6-hydrocarbons with a boiling point below 250 °C.
  • a quenching liquid particularly a quenching oil like C10- to Ci6-hydrocarbons with a boiling point below 250 °C.
  • a part of the liquid quenching medium is mixed into the reaction mixture upstream the first quenching apparatus 17, thereby further cooling the reaction mixture to a temperature in a range from 200 to 240 °C, preferably in a range from 210 to 230 °C, particularly in a range from 215 to 225 °C, for example 220 °C, which is the temperature with which the reaction mixture is fed into the first quench apparatus 17.
  • liquid quenching medium also contains heavy residues, which shall not accumulate, a part of the liquid quenching medium containing the heavy residues is withdrawn from the process via line 23.
  • liquid quenching medium it is preferred to separate the heavy residues from the liquid quenching medium, mixing the quenching medium into the reaction mixture and withdraw the heavy residues.
  • the reaction mixture After cooling in the first quenching apparatus 17, the reaction mixture is fed into a second quench apparatus 25, in which the reaction mixture is cooled to a temperature in a range from 25 to 45 °C, preferably in a range from 30 to 40 °C for example 35 °C, by direct heat transfer to a second quenching liquid, particularly water.
  • a second quench apparatus 25 in which the reaction mixture is cooled to a temperature in a range from 25 to 45 °C, preferably in a range from 30 to 40 °C for example 35 °C, by direct heat transfer to a second quenching liquid, particularly water.
  • the gaseous reaction product which contains different olefins, is withdrawn at the top 27 of the second quench apparatus 25 and fed into a compressor cascade 29. Since the olefins in the reaction product have different boiling points and, thus, condense at different pressures while keeping the temperature constant, by compression in the compressor cascade 29 the different olefins condense in different compressors 31 and can be separated in this way.
  • the remaining reaction product is fed into a carbon dioxide wash 33 to remove carbon dioxide.
  • the carbon dioxide wash can be any suitable carbon dioxide wash known by the skilled person.
  • the carbon dioxide is washed out of the reaction product by absorption in a suitable washing liquid, for example an amine solution or NaOH, preferably NaOH.
  • reaction product After washing, the remaining reaction product is compressed in a final compressor 35 to a pressure in a range from 30 to 35 bar(g), for example 32 bar(g). Compression of the reaction mixture and condensation of the different olefins for separation is carried out at a constant temperature. For this purpose, it is preferred to use coolable compressors.
  • the quenching liquid particularly the water of the second quench apparatus 25, generally contains pyrolysis gasoline and collects at the bottom 37 of the second quench apparatus 25.
  • This mixture of water and pyrolysis gasoline is separated in a phase separator, the pyrolysis gasoline is withdrawn and the water, which may contain remainders of the pyrolysis gasoline, is fed as a liquid stream into a heat integration 39.
  • the heat integration usually comprises at least one heat exchanger 41, in which heat is transferred from the liquid stream to a stream in the process, which has to be heated, for example the starting hydrocarbons. After passing the heat exchanger 41, the liquid stream still has a temperature in a range from 55 to 82°C, for example 75°C, and, therefore, contains enough energy that can be used for producing steam. This is schematically shown in figure 2.
  • a part of the liquid stream is fed into a first heat exchanger 43, in which the liquid stream transfers heat to a water stream, which is heated to a temperature in a range from 17 to 70 °C, for example 58 °C.
  • the water is fed into a flash evaporator 45, in which a part of the water evaporates, thereby forming steam.
  • the steam is withdrawn from the flash evaporator 45 and passes at least one compressor.
  • the steam passes two compressors, a first compressor47 and a second compressor 49.
  • water is injected into the steam between the first compressor 47 and the second compressor 49 and downstream the second compressor 49.
  • the steam obtained by compression and water injection, is fed into a steam grid 50.
  • the non-evaporated water is withdrawn from the flash evaporator 45 and circulated through the first heat exchanger 43.
  • the pressure in the flash evaporator must be lower than the pressure of the water stream which passes the first heat evaporator 43, a pump 51 is used in which the pressure increases.
  • the pressure of the water stream passing the first heat exchanger 43 preferably is in a range from 950 mbar(abs) to 5 bar(g) and is expanded to a pressure in a range from 20 to 300 mbar(abs) in the flash evaporator 45.
  • a feed line 53 is provided by which water can be fed into the connecting line between the flash evaporator 45 and the first heat exchanger 43 at a position that the additional water is added upstream the first heat exchanger 43 and downstream the flash evaporator 45.
  • the feed line 53 as well as the water injectors between the first compressor 47 and the second compressor 49 and downstream the second compressor 49 are connected to a feed water supply 55.
  • the feed water supply 55 provides a feed water stream, which preferably contains demineralized water.
  • the demineralized water preferably is preheated in a second heat exchanger 59 by heat exchange with at least a part of the liquid stream withdrawn from the second quench apparatus 25. After being preheated, may be fed into a feed water tank 61 and then fed from the feed water tank 61 into the water stream upstream the first heat exchanger 43 and/or downstream the first and second compressors 47, 49. Preferably, the water also is degassed by boiling in the feed water tank 61.
  • the second heat exchanger 59 for preheating the demineralized and degassed water is connected in parallel to the first heat exchanger 43.
  • the parts of the liquid streams, which have passed the first heat exchanger 43 and the second heat exchanger 59 are combined and recycled into a circulation loop 63 and returned as quenching liquid into the second quench apparatus 25.
  • the liquid stream is divided into a first part 64 and a second part 66.
  • the first part 64 of the liquid stream is fed back to the quench apparatus 25.
  • the second part 66 of the liquid stream is fed into a heat exchanger 65 for cooling, preferably a water cooler.
  • the liquid stream can be cooled to the required temperature for being used as quenching medium.
  • the heat exchanger 65 for cooling is operated with cooling water as cooling medium.
  • an air cooler 67 may be provided.
  • the air cooler 67 cools the liquid stream by using ambient air as cooling medium.
  • the air cooler 67 preferably is located upstream the position where the liquid stream is divided into the first part 64 and the second part 66.
  • FIG. 3 A second embodiment of the process for producing steam by use of the heat of the liquid stream obtained in a quench apparatus of a steam cracking process is shown in figure 3.
  • the feed line 53 is arranged such that the additional water can be fed into the connecting line between the first heat exchanger 43 and the flash evaporator 45 at a position downstream the first heat exchanger 43 and upstream the flash evaporator 45.
  • the first heat exchanger 43 and the second heat exchanger 59 are arranged in series.
  • the second heat exchanger 59 is located downstream the first heat exchanger 43.
  • the embodiments shown in figures 4 and 5 differ in the position of the feed line 53.
  • the feed line enters the connecting line upstream the second heat exchanger 59 and downstream the flash evaporator 45 as in the embodiment shown in figure 2 and in the embodiment shown in figure 5, the feed line 53 enters the connecting line downstream the first heat exchanger 43 and upstream the flash evaporator 59.

Landscapes

  • 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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé de production d'oléfines consistant à produire des oléfines contenant un flux de gaz par vapocraquage et refroidissement du flux de gaz dans un appareil de refroidissement rapide (25) par injection d'eau, ce qui permet d'obtenir un flux de gaz refroidi et un flux de liquide, au moins une partie du flux de liquide étant utilisée en tant que milieu de transfert de chaleur pour transférer de la chaleur à un flux d'eau dans un premier échangeur de chaleur (43) et le flux d'eau après avoir été chauffé dans le premier échangeur de chaleur (43) étant introduit dans un évaporateur flash (45), l'eau s'évaporant partiellement par expansion pour former de la vapeur, de préférence pour un réseau de vapeur (50) afin d'obtenir une installation avec de la vapeur industrielle.
PCT/EP2025/066619 2024-06-14 2025-06-13 Procédé de production d'oléfines par vapocraquage Pending WO2025257407A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP24182343.4 2024-06-14
EP24182343 2024-06-14

Publications (1)

Publication Number Publication Date
WO2025257407A1 true WO2025257407A1 (fr) 2025-12-18

Family

ID=91580675

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2025/066619 Pending WO2025257407A1 (fr) 2024-06-14 2025-06-13 Procédé de production d'oléfines par vapocraquage

Country Status (1)

Country Link
WO (1) WO2025257407A1 (fr)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3725865A1 (fr) * 2019-04-17 2020-10-21 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
EP3730592A1 (fr) 2019-04-24 2020-10-28 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
US20220127209A1 (en) 2019-01-15 2022-04-28 Sabic Global Technologies B.V. Use of renewable energy in olefin synthesis
WO2022189424A1 (fr) 2021-03-10 2022-09-15 Linde Gmbh Procédé et système de vapocraquage
EP4166629A1 (fr) 2021-10-14 2023-04-19 Technip Energies France SAS Installation d'éthylène, comprenant un réacteur de pyrolyse électrique et échangeur de chaleur à effluent d'alimentation
WO2023178146A1 (fr) * 2022-03-17 2023-09-21 Eastman Chemical Company Installation de recyclage chimique à consommation d'eau réduite
US20240150260A1 (en) * 2021-03-12 2024-05-09 Sabic Global Technologies B.V. Separation processes for pyrolysis products of annular jet vortex chamber reactor

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20220127209A1 (en) 2019-01-15 2022-04-28 Sabic Global Technologies B.V. Use of renewable energy in olefin synthesis
EP3725865A1 (fr) * 2019-04-17 2020-10-21 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
EP3730592A1 (fr) 2019-04-24 2020-10-28 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
WO2022189424A1 (fr) 2021-03-10 2022-09-15 Linde Gmbh Procédé et système de vapocraquage
US20240150260A1 (en) * 2021-03-12 2024-05-09 Sabic Global Technologies B.V. Separation processes for pyrolysis products of annular jet vortex chamber reactor
EP4166629A1 (fr) 2021-10-14 2023-04-19 Technip Energies France SAS Installation d'éthylène, comprenant un réacteur de pyrolyse électrique et échangeur de chaleur à effluent d'alimentation
WO2023178146A1 (fr) * 2022-03-17 2023-09-21 Eastman Chemical Company Installation de recyclage chimique à consommation d'eau réduite

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
"Ethylene", ULLMANN'S ENCYCLOPEDIA OF INDUSTRIAL CHEMISTRY, vol. 13, 2012, pages 469 - 522
MOLLETGRUBEMANN: "Formulation technology", 2001, WILEY VCH

Similar Documents

Publication Publication Date Title
CA2805521A1 (fr) .nstallation et methode de production de carburants a partir de melanges biomasse/plastique
EP3234084A2 (fr) Systèmes et procédés de production non catalytique de biodiesel à partir d'huiles
WO2023203465A1 (fr) Conversion de glycérol en composés organiques de la gamme des carburants
KR102709734B1 (ko) 열수 정제 방법
US20240417350A1 (en) Processes for the integration of hydrolysis of renewable glycerides with the generation of paraffins and propylene glycol
WO2025257407A1 (fr) Procédé de production d'oléfines par vapocraquage
US10988708B2 (en) Systems and methods for fatty acid alkyl ester production with recycling
WO2025224103A1 (fr) Procédé de production d'hydrocarbures gazeux
WO2025256936A1 (fr) Procédé de traitement d'huiles de pyrolyse dans une unité de vapocraquage
WO2025256933A1 (fr) Procédé de traitement d'une huile de pyrolyse dans une unité de vapocraquage
WO2025261879A1 (fr) Procédé d'utilisation de flux de déchets de production de (méth)acrylate d'alkyle
WO2025219136A1 (fr) Procédé d'utilisation de flux de déchets de production d'acide acrylique
WO2026046847A1 (fr) Procédé de séparation d'une fraction à point d'ébullition élevé d'un effluent de pyrolyse de déchets plastiques
WO2025219166A1 (fr) Production d'oléfines renouvelables
WO2025262260A1 (fr) Procédé de fabrication d'un produit de craquage à faible empreinte carbone
WO2026074008A1 (fr) Procédé de préparation d'éthyne à partir d'un matériau à base de caoutchouc solide
WO2025219135A1 (fr) Procédé d'utilisation de flux de déchets de production d'acide acrylique à pouvoir calorifique élevé
WO2026046845A1 (fr) Processus de séparation d'une fraction à haut point d'ébullition d'un effluent de pyrolyse de déchets plastiques
WO2025219137A1 (fr) Procédé d'utilisation de flux de déchets de production d'acide acrylique par gazéification et fermentation
WO2025119724A1 (fr) Procédé de fabrication d'aldéhydes et d'alcools à partir de déchets plastiques
WO2025172517A1 (fr) Procédé de préparation de monoxyde de carbone (co) et d'hydrogène moléculaire (h2) à partir d'un matériau textile
WO2025201948A1 (fr) Amélioration des propriétés d'écoulement à froid d'huiles de pyrolyse
WO2026057368A1 (fr) Amélioration des propriétés d'écoulement à froid des bio-huiles
WO2025132804A1 (fr) Procédé de préparation de monoxyde de carbone (co) et d'hydrogène moléculaire (h2)
Muduru et al. Hydrothermal Conversion of Individual and Mixed Plastic Waste to Hydrocarbon Fuels and Chemicals

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 25733928

Country of ref document: EP

Kind code of ref document: A1