EP3628722A1 - Générateur de gaz de fissure, procédé de production de gaz de fissure - Google Patents

Générateur de gaz de fissure, procédé de production de gaz de fissure Download PDF

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Publication number
EP3628722A1
EP3628722A1 EP18197619.2A EP18197619A EP3628722A1 EP 3628722 A1 EP3628722 A1 EP 3628722A1 EP 18197619 A EP18197619 A EP 18197619A EP 3628722 A1 EP3628722 A1 EP 3628722A1
Authority
EP
European Patent Office
Prior art keywords
crack
gas
wrf
working fluid
cycle
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.)
Withdrawn
Application number
EP18197619.2A
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German (de)
English (en)
Inventor
Suhel Ahmad
Thomas MÖNK
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.)
Siemens AG
Siemens Corp
Original Assignee
Siemens AG
Siemens Corp
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 Siemens AG, Siemens Corp filed Critical Siemens AG
Priority to EP18197619.2A priority Critical patent/EP3628722A1/fr
Priority to PCT/EP2019/072581 priority patent/WO2020064238A1/fr
Publication of EP3628722A1 publication Critical patent/EP3628722A1/fr
Withdrawn legal-status Critical Current

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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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
    • F01K25/103—Carbon dioxide

Definitions

  • the invention relates to a crack-gas-generator comprising:
  • the invention relates to a method for crack gas generation comprising the following steps:
  • a method for cracking hydrocarbon is known from US2904502A .
  • a cogeneration process using augmented Brayton-cycle is known from US 4,392,346 .
  • Naphtha may be produced from natural gas condensates, petroleum distillates, and the distillation of coal tar and peat
  • gas oil and natural gas are preferably fed into a steam cracker to obtain the desired products respectively olefins.
  • the terminology of the invention considers the compression of the crack gas as one step of the crack gas generation.
  • a typical crack gas generator respectively a typical crack gas generation process comprises a hot section and a cold section.
  • the hot section comprises a convection zone, a radiation zone, a quench section, a fractionation column and a compression of the crack gas.
  • the cold section downstream of the hot section comprises several stages of fractionating and separating the different hydrocarbons from each other and from other components or impurities of the crack gas by stepwise cooling and separating the crack gas.
  • Thermal Cracking of hydrocarbons takes place at temperatures between 800°C up to 1200°C in a cracker comprising a furnace.
  • the invention proposes a method for crack gas generation according to the incipiently defined method comprising the further features of the independent method claim.
  • the respective dependent claims relate to preferred embodiments of the invention.
  • the carbon-dioxide Brayton-cycle can achieve high efficiencies over a wide temperature range - heat flux range or power range - of the heat source respectively the crack gas leaving the cracker. This is in particular true for supercritical carbon dioxide as a working fluid of the Brayton-cycle.
  • the compactness of the components of the carbon dioxide Brayton-cycle - in particular, the heat exchangers - result in a significantly smaller system foot print and therefore lower investment costs and operating costs.
  • One preferred embodiment of the invention provides that the working fluid is always kept at a pressure above 73.75 bar and above a temperature of 70.98°C. Keeping carbon dioxide above these thermodynamic parameters respectively - above the critical parameters - in a supercritical state - avoids a phase change between gaseous and liquid state of the working fluid. Consequently, all disadvantages of a phase change are avoided - in particular, specific design features necessary to cope with a phase change - in particular, in heat exchangers. In addition, the supercritical state of the working fluid of the Brayton-cycle makes the operating range more flexible with regard to pressure and temperature as long as the operation takes place above the critical point.
  • Another preferred embodiment provides that said working fluid is heated in said heat exchanger up to 600°C, preferably above 600°C.
  • said at least one expander of the Brayton-cycle is mechanically coupled to said first crack gas compressor.
  • said crack gas generator comprises at least one first refrigerant compressor, preferably more than one refrigerant compressor being driven by an expander of the Brayton-cycle preferably the respective expander of the Brayton-cycle being directly mechanically coupled to the respective refrigerant compressor.
  • Another preferred feature of the method provides that said working fluid of carbon dioxide is permanently kept in a supercritical state in the Brayton-cycle.
  • FIG. 1 is a schematic depiction of a crack gas generator CGG according to the invention showing the features of the method of crack gas generation according to the invention.
  • the crack gas generator CGG according to the invention comprises a hot section HTS and a cold section CLS.
  • the essential features of the invention are incorporated in the hot section HTS.
  • Said hot section HTS comprises a furnace-and-heat-exchanger-arrangement FHA, a closed loop Brayton-cycle BCY, a steam drum STR, a quencher QNC, several crack gas compressors CG1, CG2, CG3, being driven by a first expander EX1 of the Brayton-cycle BCY, several refrigerant compressors CR1, CR2, CR3, CR4, being driven by a second expander EX2 and a third expander EX3 of said Brayton-cycle BCY.
  • Said cold section CLS comprises several fractionation columns CL1, CL2, CL3 for fractioning different hydrocarbons and separating these streams from each other based on their boiling points.
  • Impurities are removed before the feed is fed to a first heat exchanger HE1.
  • a water content in vapor phase is removed by a non-depicted drying process in the compression process of said crack gas stream CGS preferably between a third and fourth compressor CR3, CR4, .
  • the crack gas generator CGG comprises a crack gas CRC in the hot section HTS located in said furnace-and-heat-exchange-arrangement FHA in a radiant furnace RGF section.
  • This cracker CRC is the core of the crack gas process being heated up to a temperature of 1100 °C to crack down large hydrocarbon molecules into smaller ones.
  • the radiant furnace RDF is heated by fuel being supplied to the furnace-and-heat-exchange-arrangement FHA.
  • the furnace-and-heat-exchange-arrangement FHA comprises said first heat exchanger HE1 of said Brayton-cycle BCY.
  • the Brayton-cycle BCY circulates a working fluid WRF in a closed loop, wherein said working fluid is carbon-dioxide CO2 in a supercritical state.
  • first heat exchanger HE1 a first cooling fluid CF1 - here a flue gas from said radiant furnace RGF section - provides heat to crack gas stream CGS (for preheating) as well as to said working fluid WRF of said Brayton-cycle BCY .
  • said crack gas generation takes place with said crack gas generator CGG.
  • a feed stream FDS - here Naphta NPF - is fed into said cracker CRC.
  • said feed stream FDS is increased in temperature during a residence time RDT and transformed into a crack gas stream CGS.
  • Said first cooling fluid CF1 - here the flue gas from said radiant furnace RGF section - provides heat to said working fluid WRF by means of said first heat exchanger HE1 of said Brayton-cycle BCY.
  • this heat transfer takes place indirectly by said first cooling fluid CF1 passing said cracker CRC and said first heat exchanger HE1.
  • Other heat transfer options are possible as well - for example direct heat transfer.
  • Said cooling fluid CF1 is preferably an open cycle circulated air stream.
  • Said first cooling fluid CF1 takes heat energy from said radiant furnace RDF and carries this heat energy to a convection zone CNV of said furnace-and-heat-exchange-arrangement FHA.
  • Said first cooling fluid CF1 passes several heat exchangers HE3, HE5, HE1, HE4, HE2 before leaving the furnace-and-heat-exchange-arrangement FHA.
  • Said Brayton-cycle BCY converts the energy of the working fluid WRF respectively the supercritical carbon dioxide CO 2 into mechanical energy TWO by means of a first expander EX1, a second expander EX2 and a third expander EX3.
  • the working fluid WRF After the working fluid WRF has been expanded in the three expanders EX1, EX2, EX3 it enters downstream a high temperature recuperator HTR and a low temperature recuperator LTR to exchange heat with a stream of said working fluid WRF on its way to the downstream located first heat exchanger HE1. After passing the high temperature recuperator HTR and the low temperature recuperator LTR the working fluid WRF enters a cooler COL and downstream of the cooler a supercritical carbon-dioxide compressor SCC to deliver the working fluid WRF at a higher pressure level for the next loop of expansion after temperature increase. Downstream of said supercritical carbon-dioxide compressor SCC the working fluid WRF enters the energy receiving side of said low temperature recuperator LTR and further downstream said high temperature recuperator HTR before entering said downstream located first heat exchanger HE1.
  • Said feed stream FDS is diluted with dilution steam DST after temperature increase in said second heat exchanger HE2. Downstream of the dilution said feed stream enters a third heat exchanger HE3 (being split in two heat exchangers HE3 in the example of figure 1 ) taking heat energy from said first cooling fluid CF1.
  • the cracked gas CGS enters a steam drum STR to be quenched generating a steam STM entering downstream of said steam drum STR a fifth heat exchanger HE5 to be superheated in the furnace-and-heat-exchange-arrangement FHA by said first cooling fluid CF1.
  • the crack gas stream CGS Downstream of said steam drum STR the crack gas stream CGS enters a quencher QNC to be cooled and stop any crack reaction and to be separated from pyrolysis gas oil PGO.
  • the remaining crack gas stream CGS further enters the first crack gas compressors CG1, the second crack gas compressor CG2 and after passing a caustic wash CWS the third crack gas compressor CG3 in a serial order.
  • the three crack gas compressors CG1, CG2, CG3 are driven by said first expander EX1, wherein the driving first expander EX1 is mechanically coupled to the three crack gas compressors CG1, CG2, CG3.
  • a first fractionation column CL1 divides said crack gas stream CGS in a stream of heavier crack gas HCG and lighter crack gas LCG.
  • the lighter crack gas LCG enters downstream a second fractionation column CL2 dividing the lighter crack gas LCG into ethylene C 2 H 4 and ethane C2H6.
  • the heavier crack gas HCG enters a downstream third fractionation column CL3 dividing the heavier crack gas HCG into propylene C3H6 and liquid pressure gas LPG.
  • a heat exchanging cooler is provided to prepare the streams of hydro carbon for being split in the downstream columns.
  • Said coolers are operated with an ethylene refrigerant train ERT and a propylene refrigerant train PRT respectively.
  • Said ethylene refrigerant train ERT operates said cooler COE at a temperature of -108°C and said propylene refrigerant train PRT operates said cooler COP at a temperature of -50°C.
  • Said ethylene refrigerant train ERT is operated with a first refrigerant compressor CR1 and a second refrigerant compressor CR2 both being driven by the second expander EX2 of said Brayton-cycle BCY.
  • Said propylene refrigerant train PRT is operated with a third refrigerant compressor CR3 and a fourth refrigerant compressor CR4 both being driven by said third expander EX3 of said Brayton-cycle BCY.
  • Said furnace-and-heat-exchange-arrangement FHA is further used to heat up a boiler feed water BFW by means of a fourth heat exchanger HE4.
  • Said crack gas stream CGS has a temperature of 830°C when leaving said furnace-and-heat-exchange-arrangement FHA entering said steam drum STR.
  • Said convection section CNV is operated at a medium temperature of approximately 605°C of said first cooling fluid CF1.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Organic Chemistry (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP18197619.2A 2018-09-28 2018-09-28 Générateur de gaz de fissure, procédé de production de gaz de fissure Withdrawn EP3628722A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP18197619.2A EP3628722A1 (fr) 2018-09-28 2018-09-28 Générateur de gaz de fissure, procédé de production de gaz de fissure
PCT/EP2019/072581 WO2020064238A1 (fr) 2018-09-28 2019-08-23 Générateur de gaz de craquage, procédé de génération de gaz de craquage

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP18197619.2A EP3628722A1 (fr) 2018-09-28 2018-09-28 Générateur de gaz de fissure, procédé de production de gaz de fissure

Publications (1)

Publication Number Publication Date
EP3628722A1 true EP3628722A1 (fr) 2020-04-01

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EP18197619.2A Withdrawn EP3628722A1 (fr) 2018-09-28 2018-09-28 Générateur de gaz de fissure, procédé de production de gaz de fissure

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WO (1) WO2020064238A1 (fr)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2904502A (en) 1954-02-19 1959-09-15 Hercules Powder Co Ltd Method of cracking hydrocarbons
US4392346A (en) 1980-07-22 1983-07-12 Uop Inc. Cogeneration process using augmented Brayton cycle
US7622033B1 (en) * 2006-07-12 2009-11-24 Uop Llc Residual oil coking scheme
US20150089949A1 (en) * 2013-10-01 2015-04-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Closed loop supercritical carbon dioxide power cycle
US20170081980A1 (en) * 2013-05-31 2017-03-23 Supercritical Technologies, Inc. Systems and methods for power peaking with energy storage
US9624793B1 (en) * 2013-05-01 2017-04-18 Sandia Corporation Cascaded recompression closed Brayton cycle system
WO2018044558A1 (fr) * 2016-08-31 2018-03-08 Exxonmobil Chemical Patents Inc. Compression de produit de pyrolyse

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2904502A (en) 1954-02-19 1959-09-15 Hercules Powder Co Ltd Method of cracking hydrocarbons
US4392346A (en) 1980-07-22 1983-07-12 Uop Inc. Cogeneration process using augmented Brayton cycle
US7622033B1 (en) * 2006-07-12 2009-11-24 Uop Llc Residual oil coking scheme
US9624793B1 (en) * 2013-05-01 2017-04-18 Sandia Corporation Cascaded recompression closed Brayton cycle system
US20170081980A1 (en) * 2013-05-31 2017-03-23 Supercritical Technologies, Inc. Systems and methods for power peaking with energy storage
US20150089949A1 (en) * 2013-10-01 2015-04-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Closed loop supercritical carbon dioxide power cycle
WO2018044558A1 (fr) * 2016-08-31 2018-03-08 Exxonmobil Chemical Patents Inc. Compression de produit de pyrolyse

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Publication number Publication date
WO2020064238A1 (fr) 2020-04-02

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