EP2475944A2 - Procédé d'opération d'au moins un appareil de séparation d'air et d'une unité de consommation d'oxygène - Google Patents
Procédé d'opération d'au moins un appareil de séparation d'air et d'une unité de consommation d'oxygèneInfo
- Publication number
- EP2475944A2 EP2475944A2 EP10763743A EP10763743A EP2475944A2 EP 2475944 A2 EP2475944 A2 EP 2475944A2 EP 10763743 A EP10763743 A EP 10763743A EP 10763743 A EP10763743 A EP 10763743A EP 2475944 A2 EP2475944 A2 EP 2475944A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- oxygen
- during
- air separation
- air
- rich gas
- 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- Withdrawn
Links
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
- F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
- F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
- F25J3/04503—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
- F25J3/04509—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
- F25J3/04515—Simultaneously changing air feed and products output
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
- F25J3/04533—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion"
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
- F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
- F25J3/04545—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels for the gasification of solid or heavy liquid fuels, e.g. integrated gasification combined cycle [IGCC]
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04842—Intermittent process, so-called batch process
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
- F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/24—Multiple compressors or compressor stages in parallel
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Definitions
- the present invention relates to a method of operating at least one air separation apparatus and an oxygen-rich gas consuming unit, comprising a carbonaceous fuel combustion unit or a gasification unit, the consuming unit of the oxygen-rich gas being able to generate electricity.
- the consuming unit is fed with oxygen-rich gas from the apparatus or air separation apparatus.
- Oxycombustion One of the technologies for capturing CO 2 for carbon fuel combustion units for energy production, called Oxycombustion, will require very large amounts of oxygen (from 10,000 M tonnes per day to 20000 M tonnes per day according to the sites) produced by a series of air separation apparatus associated with the waste gas separation units of the combustion units to produce the CO 2 at the outlet of the combustion unit or units before its transport and sequestration .
- These air separation devices are very large consumers of electrical energy, which penalizes the networking of the power produced by the consumer unit at times when the energy is valued at the highest.
- Part of the combustion units are designed to operate in a base, that is to say in a stable and continuous manner over all or almost all the year (high, intermediate, and low season), and this generally close to their nominal consumption, in order to put on the grid a continuous way of electrical energy, other combustion units are planned to walk in a way more erratic and meet the needs from a certain level of electrical energy consumption (high and intermediate season), or even others that are planned to meet only the peak needs (a few hundred, see a little more a thousand hours a year, high season).
- the air separation units which supply the oxygen for the oxycombustion, are sized to supply at their nominal all the needs of the consuming unit when this works normally, and are forced to vent or stop when the combustion unit stops for a few hours each day or a few days a week when the demand is low, which results in the overall a considerable loss of energy.
- a method of operation of an installation comprising at least two air separation apparatus, a storage system and an oxygen-rich gas consuming unit comprising a unit of combustion of carbonaceous fuels or a gasification unit, the consuming unit being able to generate electricity at least according to a first step, in which the installation operates in several steps,
- the consuming unit receives a quantity of oxygen-rich gas, greater than a first consumption threshold, originating from at least one air separation apparatus, the oxygen-rich gas consisting in part of oxygen stored in the storage system, which is supplied by the air separation apparatus during a second step, and in part by the oxygen produced by distillation in at least one air separation apparatus during the first step and
- the number of separation devices operating during the first step is less than the number of devices operating during the second step.
- the number of moles of oxygen in the oxygen-rich liquid stored during the entire second step is less than the number of moles of oxygen sent as oxygen-rich gas to the consuming unit during the first step.
- the consumption of oxygen-rich gas during the first step is substantially constant.
- the quantity of air sent to at least one of the air separation units being that or those operating during the first step, corresponds to an oxygen production of at least 15%, preferably at least 25%; %, or at least 40%, of the production of gaseous oxygen sent to the consuming unit
- the difference between the production of oxygen-rich gas corresponding to the quantity of air sent to the at least one apparatus operating during the first step and the consumption of oxygen-rich gas sent to the consuming unit corresponds to at least a part the amount of liquid oxygen stored during the second step.
- the number of separation devices operating during the first step is at least 2 less than the number of devices operating during the second step.
- the number of air compressors supplying an air separation apparatus and operating during the first step is less than, preferably at least 2, the number of air compressors supplying an air separation apparatus operating during the first step; second step.
- the quantity of liquid oxygen sent from the apparatus or the air separation devices to the storage system during the first step does not exceed 1%, preferably 2% or even 5% of the air flow sent to the air separation apparatus (to the air separation apparatus).
- the quantity of liquid oxygen sent from the storage system to the apparatus or air separation apparatus during the second step does not exceed 1%, preferably 2% or even 5% of the air flow sent to the air separation apparatus or air separation apparatus.
- the amount of gaseous oxygen withdrawn from the air separation units (1) during the second step does not exceed 1%, preferably 2% or even 5% of the air flow rate sent to the air separation units.
- liquid nitrogen and / or liquid air is sent to the air separation units, liquid nitrogen and / or liquid air being produced (s) during the first step, and preferably not during the second step, by the air separation device (s).
- n being preferably at least 2
- at least one of the air separation apparatus or the air separation apparatus has a nominal oxygen-rich gas capacity lower than the nominal capacity of the oxygen-rich gas consumption unit divided by n
- n is at least equal to three and at least two of the air separation apparatuses have a nominal oxygen-rich gas capacity lower than the nominal capacity of the oxygen-rich gas consumption unit divided by n,
- n being preferably at least 2, and at least one of the air separation apparatus or the air separation apparatus has a nominal oxygen-rich gas capacity higher than the nominal capacity of the oxygen-rich gas consumption unit divided by n, n is at least three and at least two of the air separation units have a nominal oxygen-rich gas capacity that is greater than the nominal capacity of the oxygen-rich gas consumption unit divided by n.
- each installation generally comprises at least two air separation devices.
- Each separating apparatus comprises a purification unit for water and carbon dioxide to purify the air as well as a cold box where the distillation columns are located.
- To compress the air is provided at least as much air compressor as air separation devices, so for the case of two devices, at least two air compressors. These compressors are possibly associated with air boosters.
- the installation also includes a liquid product storage system (liquid oxygen, liquid nitrogen, and possibly liquid air) consisting of one or more storage products.
- This storage system can be pooled with these air separation units.
- Air compressors and air boosters can be networked together to provide all air separation devices.
- the consuming unit consumes a substantially constant amount of oxygen.
- This constant amount is provided by the air separation device (s) at all times.
- the cost of electricity is above the minimum rate and the consumption of oxygen by the consuming unit is above a first consumption threshold.
- Oxygen from the storage can be vaporized in a vaporizer external to the air separation apparatus but it is more energetically attractive that the air separation apparatus receives the cold energy from the latent heat of the oxygen from the storage.
- Liquid nitrogen and / or liquid air may be produced during periods of high demand for electrical energy (tariff above the first tariff threshold) on the network by supplying an element of the apparatus (apparatus) with liquid oxygen, while the air separation apparatuses are supplied with liquid oxygen from a storage of the storage system, a storage of the cold box or an outside source.
- At least one of the air separation apparatus still operates and produces large amounts of liquid oxygen, a column of the air separation apparatus optionally being supplied with liquid nitrogen and / or liquid air from storage of the storage system, storage of the cold box or an external source.
- a column of the air separation apparatus optionally being supplied with liquid nitrogen and / or liquid air from storage of the storage system, storage of the cold box or an external source.
- the number of air separation devices operating when stopping the consumer unit is higher than the number of air separation devices operating when the consuming unit is operating. In this way, we take advantage of the low electricity rate during the second step to make liquid oxygen that will be used to power the consumer unit during the first step when electricity is expensive.
- the installation comprises an assembly 1 of four air separation units, a storage system 2 and an oxygen-rich gas consuming unit 3 which can be a combustion unit for carbon fuels or a gasifier. If it is a combustion unit, the consuming unit can also be supplied with air in place of oxygen.
- Each air separation apparatus comprises a purification unit 5A, 5B, 5C, 5D and a cold box 7A, 7B, 7C, 7D, the apparatuses being substantially identical.
- the air separation units can receive air from four air compressors 3A, 3B, 3C, 3D connected by a common pipe 9, so that they can supply all air separation devices.
- the oxygen-rich gas consuming unit 3 receives this gas from at most three of the air separation units.
- the cost of electricity exceeds a first tariff threshold and is expensive. It is therefore desirable to minimize electricity consumption during this walk.
- Air from the two or three running compressors is sent to the two or three air separation units and distills into the columns placed in the cold boxes to form a low pressure oxygen rich gas. This pressure rarely exceeds 5 bar abs.
- Oxygen can be withdrawn in gaseous form from the low pressure column of a double column.
- the double columns can be devices having two condensers in the low pressure column, in known manner. It is also possible to vaporize a liquid withdrawn from the column by taking the usual precautions for a low pressure vaporization.
- liquid oxygen 13 is sent from the storage system 2 to the air separation units in operation, from so that their frigories are used intelligently in the devices.
- the gaseous oxygen thus formed becomes a part of the oxygen-rich gas 17 sent to the consumer unit 3.
- no flow of liquid oxygen is sent from the air separation units to the storage system.
- a flow of liquid oxygen not exceeding 1%, preferably 2% or 5% of the air can be sent air separation apparatus to the storage system.
- the consuming unit 3 does not operate and therefore no flow of oxygen-rich gas is sent to this unit or the flow sent to the unit does not exceed 2% of the air sent to the units of the unit. air separation.
- the cost of electricity is below a second rate threshold, the second rate threshold being lower than the first rate threshold and electricity is therefore comparatively cheap.
- the production of gaseous oxygen by separation devices becomes marginal or non-existent.
- the production of gaseous oxygen may represent up to 1%, preferably 2% or even 5% of the supply air, this oxygen being vented.
- the air separation devices all produce liquid oxygen 1 1 which is sent to the storage system 2.
- the storage system 2 fills with liquid oxygen during the second step but not during the first and empties in liquid oxygen during the first walk but not during the first. However, it is possible to empty very small amounts of liquid from the storage during the second step.
- the cold behavior of the apparatus during the second step is partially ensured by sending liquid nitrogen and / or liquefied air to the air separation apparatus or apparatus.
- This sending liquid nitrogen and / or liquefied air does not take place during the first step and preferably liquid nitrogen and / or liquefied air is produced during the first step and sent to the storage system 2.
- the liquid nitrogen and / or liquid air can be sent at least partly to a column of the apparatus, a separator pot or an exchanger of the apparatus.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Gas Separation By Absorption (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0956167A FR2949845B1 (fr) | 2009-09-09 | 2009-09-09 | Procede d'operation d'au moins un appareil de separation d'air et d'une unite de combustion de combustibles carbones |
PCT/FR2010/051765 WO2011030035A2 (fr) | 2009-09-09 | 2010-08-24 | Procédé d'opération d'au moins un appareil de séparation d'air et d'une unité de consommation d'oxygène |
Publications (1)
Publication Number | Publication Date |
---|---|
EP2475944A2 true EP2475944A2 (fr) | 2012-07-18 |
Family
ID=42244263
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP10763743A Withdrawn EP2475944A2 (fr) | 2009-09-09 | 2010-08-24 | Procédé d'opération d'au moins un appareil de séparation d'air et d'une unité de consommation d'oxygène |
Country Status (10)
Country | Link |
---|---|
US (1) | US20120174624A1 (fr) |
EP (1) | EP2475944A2 (fr) |
JP (1) | JP2013509557A (fr) |
CN (1) | CN102483301B (fr) |
AU (1) | AU2010294078B2 (fr) |
CA (1) | CA2771201C (fr) |
FR (1) | FR2949845B1 (fr) |
IN (1) | IN2012DN01485A (fr) |
WO (1) | WO2011030035A2 (fr) |
ZA (1) | ZA201201567B (fr) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2985005B1 (fr) | 2011-12-21 | 2017-12-22 | L'air Liquide Sa Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et appareil de separation d'air par distillation cryogenique |
FR2985006A1 (fr) * | 2011-12-21 | 2013-06-28 | Air Liquide | Procede de production d'un systeme pour la realisation d'un procede de separation d'air, procede de production d'un appareil de separation d'air et installation de separation d'air par distillation cryogenique |
EP2703717B1 (fr) * | 2012-09-03 | 2016-05-18 | Alstom Technology Ltd | Procédé de fonctionnement d'un système de chaudière à combustion d'oxygène |
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BE564694A (fr) * | 1957-02-13 | |||
DE3012062A1 (de) * | 1980-03-28 | 1981-10-08 | Linde Ag, 6200 Wiesbaden | Verfahren und vorrichtung zur erzeugung von gasfoermigen sauerstoff |
AT386279B (de) * | 1986-04-02 | 1988-07-25 | Voest Alpine Ag | Vorrichtung zur zerlegung von gasen mittels koaxial ineinander angeordneter rektifikationskolonnen |
FR2652887B1 (fr) * | 1989-10-09 | 1993-12-24 | Air Liquide | Procede et installation de production d'oxygene gazeux a debit variable par distillation d'air. |
CN1071444C (zh) * | 1992-02-21 | 2001-09-19 | 普拉塞尔技术有限公司 | 生产气体氧的低温空气分离系统 |
JPH08189759A (ja) * | 1995-01-09 | 1996-07-23 | Kawasaki Steel Corp | 空気分離装置の酸素ガス発生量決定方法 |
JP3667875B2 (ja) * | 1996-05-28 | 2005-07-06 | 大陽日酸株式会社 | 空気液化分離方法 |
FR2751737B1 (fr) * | 1996-07-25 | 1998-09-11 | Air Liquide | Procede et installation de production d'un gaz de l'air a debit variable |
WO1999040304A1 (fr) * | 1998-02-04 | 1999-08-12 | Texaco Development Corporation | Separation d'air cryogenique combinee avec une gazeification integree |
US6745573B2 (en) * | 2001-03-23 | 2004-06-08 | American Air Liquide, Inc. | Integrated air separation and power generation process |
JP3884240B2 (ja) * | 2001-05-15 | 2007-02-21 | 株式会社神戸製鋼所 | 空気分離装置およびその制御運転方法 |
US7284362B2 (en) * | 2002-02-11 | 2007-10-23 | L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Étude et l'Exploitation des Procedes Georges Claude | Integrated air separation and oxygen fired power generation system |
US7228715B2 (en) * | 2003-12-23 | 2007-06-12 | L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude | Cryogenic air separation process and apparatus |
US20080115531A1 (en) * | 2006-11-16 | 2008-05-22 | Bao Ha | Cryogenic Air Separation Process and Apparatus |
FR2924203B1 (fr) * | 2007-11-26 | 2010-04-02 | Air Liquide | Adaptation d'une centrale a oxycombustion a la disponibilite de l'energie et a la quantite de co2 a capturer |
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2009
- 2009-09-09 FR FR0956167A patent/FR2949845B1/fr active Active
-
2010
- 2010-08-24 CN CN201080040115.3A patent/CN102483301B/zh not_active Expired - Fee Related
- 2010-08-24 EP EP10763743A patent/EP2475944A2/fr not_active Withdrawn
- 2010-08-24 AU AU2010294078A patent/AU2010294078B2/en not_active Ceased
- 2010-08-24 JP JP2012528414A patent/JP2013509557A/ja not_active Withdrawn
- 2010-08-24 CA CA2771201A patent/CA2771201C/fr not_active Expired - Fee Related
- 2010-08-24 WO PCT/FR2010/051765 patent/WO2011030035A2/fr active Application Filing
- 2010-08-24 US US13/393,858 patent/US20120174624A1/en not_active Abandoned
- 2010-08-24 IN IN1485DEN2012 patent/IN2012DN01485A/en unknown
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2012
- 2012-03-01 ZA ZA2012/01567A patent/ZA201201567B/en unknown
Non-Patent Citations (1)
Title |
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See references of WO2011030035A2 * |
Also Published As
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---|---|
IN2012DN01485A (fr) | 2015-06-05 |
JP2013509557A (ja) | 2013-03-14 |
CA2771201C (fr) | 2017-05-16 |
AU2010294078A1 (en) | 2012-03-29 |
WO2011030035A2 (fr) | 2011-03-17 |
US20120174624A1 (en) | 2012-07-12 |
FR2949845A1 (fr) | 2011-03-11 |
CN102483301B (zh) | 2015-11-25 |
CA2771201A1 (fr) | 2011-03-17 |
WO2011030035A3 (fr) | 2013-12-19 |
FR2949845B1 (fr) | 2011-12-02 |
AU2010294078B2 (en) | 2014-09-18 |
CN102483301A (zh) | 2012-05-30 |
ZA201201567B (en) | 2014-03-26 |
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