WO2012034662A1 - Procédé de purification de condensat de traitement - Google Patents

Procédé de purification de condensat de traitement Download PDF

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Publication number
WO2012034662A1
WO2012034662A1 PCT/EP2011/004483 EP2011004483W WO2012034662A1 WO 2012034662 A1 WO2012034662 A1 WO 2012034662A1 EP 2011004483 W EP2011004483 W EP 2011004483W WO 2012034662 A1 WO2012034662 A1 WO 2012034662A1
Authority
WO
WIPO (PCT)
Prior art keywords
steam
condensate
process condensate
catalytic oxidation
gas
Prior art date
Application number
PCT/EP2011/004483
Other languages
German (de)
English (en)
Inventor
Carsten Taube
Michael Reinke
Christian Thaller
Original Assignee
Linde Aktiengesellschaft
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 Linde Aktiengesellschaft filed Critical Linde Aktiengesellschaft
Publication of WO2012034662A1 publication Critical patent/WO2012034662A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/427—Treatment of water, waste water, or sewage by ion-exchange using mixed beds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
    • C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)

Definitions

  • the invention relates to a process for the purification of process condensate obtained during steam reforming or steam cracking of hydrocarbons.
  • a hydrocarbon-containing feed such as natural gas, light gasoline or naphtha
  • process steam is mixed with process steam and reacted in a reactor with catalytic assistance to a synthesis gas consisting predominantly of hydrogen and carbon monoxide.
  • synthesis gas consisting predominantly of hydrogen and carbon monoxide. From the synthesis gas are subsequently by cooling, cleaning and decomposition products, such as
  • Hydrogen, carbon monoxide or oxo gas (a defined mixture of hydrogen and carbon monoxide) won.
  • the synthesis gas is cooled to below the dew point, whereby the water vapor condenses out and so-called.
  • Process condensate is formed. Process condensate consists for the most part of water, but also contains a variety of different
  • Impurities such as alcohols, carboxylic acids, cations (Na + , Ca 2+ , Fe 273 *, NH 4 ⁇ ...), anions (N0 3 “ , N0 2 “ , C0 3 2 “ , HC0 3 ' , ... ) as well as dissolved gases and solids.
  • Process condensate also accumulates in the vapor cracking of hydrocarbons.
  • hydrocarbon-containing inserts such as naphtha, ethane, propane, butane, gas oil or Hydrorowachse
  • a product gas is formed, which consists primarily of hydrogen, methane, ethylene and propylene.
  • the vapor cracking also becomes excessive
  • Impurities such as uncleaved hydrocarbons and aromatic
  • the process condensate is mixed with demineralized water, which is added to the
  • Process is supplied from the outside. It is then degassed and warmed against cooled process streams, evaporated and superheated, forming steam that is contaminated with impurities contained in the process condensate. The purity of this vapor is sufficiently high to keep it within the
  • Process steam is obtained from a mixture of untreated process condensate and demineralized water, only demineralized water is used to produce export steam. With this method, it is thus possible to produce extremely pure export steam without an additional purification step.
  • a disadvantage is the high expenditure on equipment for the second steam system, the cost of steam reforming considerably
  • the present invention is therefore based on the object to provide a method of the type mentioned, by which the disadvantages of the prior art can be overcome.
  • Catalytic oxidation has been the art for years and known to those skilled in the art as a process for removing organic compounds from aqueous solutions.
  • the aqueous solution is treated with an oxidizing agent, such as. B.
  • Hydrogen peroxide mixed and passed through a fixed bed catalyst.
  • the organic compounds are oxidized here with catalytic support, in particular carbon dioxide and water.
  • the catalytic oxidation is primarily used to convert alcohols - especially methanol and ethanol - and carboxylic acids to carbon dioxide and water and thereby remove.
  • the oxidizing agent used is preferably hydrogen peroxide, which is metered into the process condensate to be purified.
  • an expedient embodiment of the process according to the invention provides that the ion exchange is carried out in a mixed-bed ion exchanger, wherein anions and cations are simultaneously removed from the process condensate.
  • process condensate contains cations in a concentration that is at the
  • Carrying out a catalytic oxidation can lead to disturbances.
  • a process condensate obtained in steam reforming and a subsequent water gas shift, in particular ammonium ions in an amount which does not allow its direct treatment by catalytic oxidation for economic reasons.
  • a preferred embodiment of the method according to the invention therefore provides that the process condensate is treated by cation exchange before the catalytic oxidation for the separation of cations.
  • process condensate often contains solid particles which can be deposited in the apparatuses used for ion exchange and catalytic oxidation and can lead to disturbances.
  • the method provides a purification step which is expediently arranged before the cation exchange and / or the catalytic oxidation, in which solids are separated off from the process condensate.
  • the inventive method can be used for the purification of any process condensate, which in the steam reforming or
  • Process gas is obtained, which is obtained by steam reforming and subsequent water gas shift.
  • the process condensate purified by means of the process according to the invention can be used for the production of export steam and / or process steam.
  • demineralized water is usually supplied from the outside and mixed with the purified process condensate before it is converted by the waste heat to export steam and / or process steam.
  • the export steam produced according to the invention can be used for a variety of applications. With particular benefit, it is used in a steam turbine process in which its energy is converted into mechanical and / or electrical energy.
  • the present invention offers a number of advantages. Thus, it allows a process condensate obtained during steam reforming or steam cracking to be cleaned to such an extent that steam obtained from it meets high purity requirements and can also be used in a steam turbine. To carry out the
  • Process condensate can be performed. At most, it needs smaller
  • Figure 1 shows an embodiment of the method according to the invention for the purification of a resulting in the steam reforming of hydrocarbons
  • FIG. 2 shows an embodiment of the method according to the invention with an optional pretreatment of the process condensate.
  • Heat exchanger E1 preheated combustion air 2 are supplied.
  • the flue gases generated by the burner D give off part of their sensible heat to the reformer tubes F containing a catalytically active material before they are removed via the flue gas system C.
  • the flue gas system C In the flue gas system C are several
  • Heat exchangers E1, E2 and E3 arranged over which the flue gases further heat is removed so that they reach the chimney J with a temperature of about 200 ° C via line 3 and the blower G.
  • a hydrocarbon-containing insert 4 preheated in the heat exchanger E4 is mixed with process steam 5 before it is introduced into the heat exchanger E3 arranged in the flue gas system C of the reformer A and is further superheated there.
  • the process steam 5 is metered in more than stoichiometrically in order to suppress the formation of soot in the subsequent steam reforming reaction.
  • the hydrocarbon / Darrrpf mixture is withdrawn from the superheated E3 and distributed to the reformer tubes F, where they are converted with catalytic support to the process gas 7.
  • the process gas 7, which leaves the reformer A, is cooled in the heat exchangers E5, E6, E4 and E7 to below the dew point, so that excess water vapor condenses out and forms a multiphase flow 8, which is introduced into the separator K.
  • the stream 8 is in the predominantly consisting of hydrogen and carbon monoxide synthesis gas 9 and the predominantly made of water,
  • Synthesis gas 9 further treatment steps, not shown, the process condensate 10 enters the cleaning section L, in which the
  • FIG. 2 shows an embodiment of the cleaning section L in which
  • Process condensate 10 is freed of impurities.
  • the process condensate 10, which typically has a temperature of about 70 ° C, is passed through a solid filter O in a first cleaning step to solid particles, such as
  • Catalyst abrasion or corrosion products separate.
  • the purified solids process condensate 21 is introduced into the cation exchanger P below, in the present as cations impurities such as Na +, Ca 2 ⁇ Fe 213 * or NH 4 + are separated.
  • the aqueous solution 22 obtained in this process which still contains organic impurities, in particular methanol, as well as anions, is subsequently fed to a catalytic oxidation R.
  • the organic contaminants become water with catalytic support
  • the stream 25 is introduced into the mixed bed toner exchanger S, where both anions, such as N0 3 " , N0 2 " , C0 3 2 “ or HC0 3 ⁇ , as well as cations - formed in the previous purification step R or in the cation exchanger P not separated - are removed, so that high-purity water is generated, which leaves the cleaning section L as purified process condensate 11.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

L'invention concerne un procédé de purification de condensat de traitement (10) produit lors du reformage à la vapeur d'hydrocarbures. Pour séparer les impuretés, le gaz de traitement (10) est soumis à une oxydation catalytique (R) et à un échange ionique (S).
PCT/EP2011/004483 2010-09-16 2011-09-06 Procédé de purification de condensat de traitement WO2012034662A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102010045587.3 2010-09-16
DE201010045587 DE102010045587A1 (de) 2010-09-16 2010-09-16 Verfahren zur Aufreinigung von Prozesskondensat

Publications (1)

Publication Number Publication Date
WO2012034662A1 true WO2012034662A1 (fr) 2012-03-22

Family

ID=44653252

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2011/004483 WO2012034662A1 (fr) 2010-09-16 2011-09-06 Procédé de purification de condensat de traitement

Country Status (2)

Country Link
DE (1) DE102010045587A1 (fr)
WO (1) WO2012034662A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102016107612A1 (de) * 2016-04-25 2017-10-26 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und Anlage zur Reinigung von Prozesskondensat aus der katalytischen Dampfreformierung eines kohlenwasserstoffhaltigen Einsatzgases

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5387548A (en) * 1976-12-28 1978-08-02 Kurita Water Ind Ltd Cleaning recovery of condensed water formed from gasification step by steamreforming process
EP0349164A1 (fr) * 1988-06-27 1990-01-03 Exxon Research And Engineering Company Procédé pour le recyclage et la purification d'un produit de condensation provenant d'un procédé de synthèse d'hydrocarbures ou d'alcools
DE102006019100A1 (de) 2006-04-25 2007-10-31 Linde Ag Verfahren zur Produktion von Exportdampf in Dampfreformern
WO2010086182A1 (fr) * 2009-01-30 2010-08-05 Eni S.P.A. Procédé d'épuration d'un courant aqueux provenant de la réaction de fischer-tropsch

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5387548A (en) * 1976-12-28 1978-08-02 Kurita Water Ind Ltd Cleaning recovery of condensed water formed from gasification step by steamreforming process
EP0349164A1 (fr) * 1988-06-27 1990-01-03 Exxon Research And Engineering Company Procédé pour le recyclage et la purification d'un produit de condensation provenant d'un procédé de synthèse d'hydrocarbures ou d'alcools
DE102006019100A1 (de) 2006-04-25 2007-10-31 Linde Ag Verfahren zur Produktion von Exportdampf in Dampfreformern
WO2010086182A1 (fr) * 2009-01-30 2010-08-05 Eni S.P.A. Procédé d'épuration d'un courant aqueux provenant de la réaction de fischer-tropsch

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Publication number Publication date
DE102010045587A1 (de) 2012-03-22

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