EP3307700A1 - Procédé et installation pour une synthèse chimique - Google Patents

Procédé et installation pour une synthèse chimique

Info

Publication number
EP3307700A1
EP3307700A1 EP16745693.8A EP16745693A EP3307700A1 EP 3307700 A1 EP3307700 A1 EP 3307700A1 EP 16745693 A EP16745693 A EP 16745693A EP 3307700 A1 EP3307700 A1 EP 3307700A1
Authority
EP
European Patent Office
Prior art keywords
product mixture
energy
synthesis
synthesis reactor
compression
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Withdrawn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
EP16745693.8A
Other languages
German (de)
English (en)
Inventor
Alexander Tremel
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
Publication of EP3307700A1 publication Critical patent/EP3307700A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/1512—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by reaction conditions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0005—Catalytic processes under superatmospheric pressure
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/02—Monohydroxylic acyclic alcohols
    • C07C31/04—Methanol
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00539—Pressure

Definitions

  • the present invention relates to a method and a plant for carrying out an exothermic chemical synthesis, in particular the methanol synthesis, in which methanol in a Synthe ⁇ sereaktor from the starting materials hydrogen and a carbon-containing gas is generated ⁇ .
  • reaction products methanol and water are liquid, they can continuously the equilibrium depleted methanol synthesis reaction can be withdrawn.
  • a disadvantage of the process described is that the compression of the educts hydrogen and carbon dioxide to the desired pressure requires a high expenditure of energy, whereby the economic applicability is significantly reduced.
  • the object of the present invention is to provide a synthesis process and an installation for the synthesis which reduce the aforementioned disadvantage.
  • This object is achieved by a Ver ⁇ drive with the features of claim 1 concerning the method.
  • gaseous starting materials are compressed and brought to a working pressure of at least 200 bar, in particular between 250 bar and 500 bar.
  • the starting materials react to give a product mixture which is at least largely liquid in the synthesis reactor.
  • the product mixture which also typically contains small admixtures of the educts in dissolved form, is removed from the synthesis reactor. Furthermore, the product mixture is deprived of mechanical energy by lowering the pressure. This energy is used for the compression of the educts.
  • the plant according to the invention for chemical synthesis ⁇ includes a device for the compression of educts to a working pressure of at least 200 barWeiterhin the system comprises a synthesis reactor, means for supplying the reactants to the synthesis reactor and means for discharging a liquid product mixture from the synthesis reactor. Finally, the plant comprises a device for the removal of mechanical Energy from the product mixture through pressure reduction and transfer of energy to the device for compression.
  • the product mixture can be brought at least partially in the gaseous phase before the removal of energy.
  • the means for removing the energy can beispielswei ⁇ se be a turbine, a screw expander or a piston expander.
  • a reciprocating compressor can be used, initiated in the gaseous parts of the product mixture as a drive gas to remove the energy who ⁇ .
  • the product mixture advantageously operates the compression directly without detour via an intermediate form of energy such as electrical energy.
  • a turbine system In order to remove the energy from the at least partially gas ⁇ shaped product mixture, a turbine system may be used.
  • gaseous parts of the envisionge ⁇ premixture for removal of the energy by the turbine plant directed and thus provided kinetic energy.
  • the Be ⁇ wegungs energie can now be used to generate electrical energy by means of a generator mechanically connected to the turbine system.
  • the electrical energy is then at least partially verwen ⁇ det for compression.
  • the advantage here is that the electrical energy is versatile.
  • the turbine system may be directly connected via a shaft mecha nically ⁇ with a compressor used for the compression of the starting materials.
  • the compression also works without detours via electrical energy.
  • the product mixture can be expanded in a valve to lower pressure. Further, before, during and / or heat from the synthesis reactor or even from the product mixture, at an upstream location, and fed to the product mixture ⁇ Pro after relaxation.
  • the removal of energy from the at least partially gas ⁇ shaped product mixture can also be done in several stages. In this case, after removal of the product mixture, two or more turbine systems are run through. In this case, before passing through each of the turbines, heat can be supplied to the product mixture from the synthesis reactor in order to increase the gaseous fraction of the product mixture and / or to achieve overheating.
  • FIG. 1 shows a plant for the synthesis of methanol with a Kol ⁇ benver Actuallyr
  • Figure 2 shows a plant for the synthesis of methanol with a tur ⁇ binenstrom
  • FIG. 3 shows a plant for methanol synthesis with a multi- stage process for generating electricity.
  • FIG. 1 shows a first exemplary system 10 for
  • the system 10 are fed educts in the form of carbon dioxide 13 and hydrogen 14.
  • the hydrogen 14 comes from an electrolysis plant.
  • water is split into hydrogen and oxygen.
  • electricity from renewable energies is used or surplus electricity that is generated when there is a large supply of renewable energies and at the same time low demand for electricity.
  • the educts are fed to a piston compressor 12 in the first step.
  • the piston compressor 12 brings the educts to ei ⁇ nen working pressure of 300 bar. Under this pressure, the reactants are fed via a feed line into the synthesis reactor 11.
  • the conversion to methanol and water according to the above-mentioned reaction formula 1 takes place. While the educts remain gaseous at the working pressure of 300 bar, the products methanol and water are liquid at this pressure and at the temperatures used of 200 ° C to 300 ° C. They therefore settle in a collection zone 17 and can be removed from there from the synthesis reactor 11.
  • the exact reaction procedure within the synthesis Actors 11 is irrelevant to the invention and will therefore not be further described.
  • the product mixture of methanol, water, by-products and admixtures of the educts is passed in a laxative line 16 to a valve 15, at which the product mixture is expanded to a lower pressure of for example 100 bar.
  • the product mixture may already become partially gaseous.
  • a heat exchanger 18 in Synthe ⁇ sereaktor 11 and a heat exchanger coupled thereto 19 heat is removed from the synthesis reactor 11 and fed to the product mixture behind the valve 15, whereby a further part of the product mixture is gaseous.
  • the gaseous portion of the product mixture will be the reciprocating compressor 12 supplied ⁇ leads and drives there the compaction of the starting materials.
  • the pressure-charged product mixture serves as a drive medium for the compression of the educts via a mechanical piston system. As a result, the product mixture is fed to further processing.
  • the heat exchanger 18 in the synthesis reactor 11 can be designed, for example, as part of the cooling structure, not shown, for the synthesis reactor 11.
  • the cooling structure is used to keep the temperature in the synthesis reactor 11 at the end of the exothermic reaction according to reaction formula 1 in the ge ⁇ desired range. Since heat has to be dissipated anyway, it is advantageous to use these to supply heat to the product mixture and thus to bring larger proportions into the gaseous phase.
  • the methanol synthesis is performed on a work ⁇ pressure, which can be liquid products.
  • DA by the reaction products of the reaction formula 1 are ste ⁇ tig removed from the reaction so that the equilibrium is strongly shifted towards the products.
  • the reaction products do not have to pass through the synthesis Reactor 11 are led to achieve a good implementation.
  • the increased energy expenditure in providing the educts at the working pressure of 300 bar is again absorbed by using energy of the product mixture, which is also under the high working pressure.
  • the waste heat of the synthesis reaction is also advantageously used by being fed to the product mixture.
  • FIG. 1 Another embodiment of the invention is shown in FIG.
  • the system 20 according to Figure 2 corresponds here in ⁇ in parts of the system 10 of the first embodiment.
  • the system 20 of the second exemplary embodiment comprises a further heat exchanger 21, which is arranged in the outgoing line 16 upstream of the valve 15. This takes the product mixture heat and leads them to the valve 15 in the heat exchanger 19 again.
  • the product mixture is supplied in this embodiment, a turbine unit 22 to drive the compression of the educts.
  • the turbine unit 22 is mechanically coupled via a shaft directly to a compressor 23, which brings the educts to the working pressure.
  • the turbine installation 22 can also be used in parallel with the generation of electricity, in that it is additionally connected to a generator, which is not shown in FIG. 2, however.
  • the genes ⁇ rator may also be designed as a motor and thus provide additional electrical energy from an external source for compression. Since the product mixture is under a considerable working pressure, a further improved utilization of the energy can take place, in which a multi-stage process is used.
  • a corresponding system 30 according to a third embodiment ⁇ example of the invention is shown in Figure 3.
  • the plant 30 contains, like the plants 10, 20 already described, a synthesis reactor 11 with collecting area 17 and a heat exchanger 18 on the synthesis reactor 11.
  • a turbine system 22 is similar to the second plant 20 the product ⁇ mixture fed, before heat is conducted from the synthesis reactor 11 by means of the heat exchanger 19 to ⁇ . After passing through the turbine system 22, however, in contrast to the previously described systems 10, 20, the product mixture of a further turbine plant
  • the two-stage process can also be extended to more than two stages .
  • the turbine systems 22, 31 feed it directly or indirectly as described previously, the compres sion ⁇ the starting materials and also useful, for example, an overall erator for generating electrical energy.
  • the compression of the educts can be done in several stages.
  • the product mixture is not brought into the gaseous phase, but instead leads directly to an engine such as a turbine in liquid form ⁇ leads. Due to the high temperature of the product mixture, partial vaporization of the products in the product mixture may occur in the engine. That can be accepted; Alternatively, the product mixture can be cooled before being introduced into the engine but also by means of an intermediate heat exchanger.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Procédé de synthèse et installation pour une synthèse chimique. Selon ce procédé, la synthèse s'effectue à une pression de travail supérieure ou égale à 200 bars. Selon ce procédé, l'énergie mécanique est extraite du mélange résultant de la synthèse, et utilisée pour la compression de la matière de départ à la pression de travail.
EP16745693.8A 2015-08-05 2016-07-27 Procédé et installation pour une synthèse chimique Withdrawn EP3307700A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102015214943.9A DE102015214943A1 (de) 2015-08-05 2015-08-05 Verfahren und Anlage für eine chemische Synthese
PCT/EP2016/067861 WO2017021245A1 (fr) 2015-08-05 2016-07-27 Procédé et installation pour une synthèse chimique

Publications (1)

Publication Number Publication Date
EP3307700A1 true EP3307700A1 (fr) 2018-04-18

Family

ID=56561360

Family Applications (1)

Application Number Title Priority Date Filing Date
EP16745693.8A Withdrawn EP3307700A1 (fr) 2015-08-05 2016-07-27 Procédé et installation pour une synthèse chimique

Country Status (7)

Country Link
US (1) US10336674B2 (fr)
EP (1) EP3307700A1 (fr)
CN (1) CN107922298A (fr)
AU (1) AU2016302420B2 (fr)
CL (1) CL2018000202A1 (fr)
DE (1) DE102015214943A1 (fr)
WO (1) WO2017021245A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102015214943A1 (de) 2015-08-05 2017-02-09 Siemens Aktiengesellschaft Verfahren und Anlage für eine chemische Synthese
KR20250005537A (ko) 2015-08-05 2025-01-09 에자이 알앤드디 매니지먼트 가부시키가이샤 균질한 올리고머의 제조를 위한 키랄 시약
EP4414352A1 (fr) * 2023-02-07 2024-08-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de production de méthanol à partir de gaz de synthèse contenant une teneur élevée en composants de gaz inertes

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4239693A (en) * 1979-06-22 1980-12-16 Foster Wheeler Energy Corporation Process for production of methanol
DE102004059315A1 (de) * 2004-11-30 2006-06-01 Michael Prestel Kompressor-Arbeitsmaschine

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1667322A1 (de) 1967-11-21 1971-06-09 Uhde Gmbh Friedrich Verfahren zur Hochdrucksynthese
US3649208A (en) * 1969-09-25 1972-03-14 Ingersoll Rand Co Fluid compressor system
JPS5839572B2 (ja) 1979-04-03 1983-08-31 東洋エンジニアリング株式会社 反応器およびその使用法
GB2082574A (en) * 1980-08-21 1982-03-10 Davy Mckee Oil & Chem Methanol synthesis
GB8803766D0 (en) * 1988-02-18 1988-03-16 Ici Plc Methanol
NO322472B1 (no) * 2002-04-24 2006-10-09 Geba As Fremgangsmater for produksjon av mekanisk energi ved hjelp av sykliske termokjemiske prosesser samt anlegg for samme
US6881759B2 (en) 2003-04-07 2005-04-19 Haldor Topsoe A/S Process for the preparation of methanol
EP1904426B1 (fr) 2005-07-06 2009-08-26 BP Chemicals Limited Procede de conversion de gaz de synthese en composes oxygenes contenant des alcools c2+
EP2228357A1 (fr) * 2009-03-12 2010-09-15 Methanol Casale S.A. Processus de synthèse de méthanol
EP2301886A1 (fr) * 2009-09-03 2011-03-30 Ammonia Casale S.A. Récupération de chaleur de déchets d'un procédé chimique et installation, en particulier pour la synthèse d'ammoniac
DE102012204985A1 (de) 2012-03-28 2013-10-02 Siemens Aktiengesellschaft Verfahren und Anordnung für die Hochtemperaturelektrolyse
DE102015214943A1 (de) 2015-08-05 2017-02-09 Siemens Aktiengesellschaft Verfahren und Anlage für eine chemische Synthese

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4239693A (en) * 1979-06-22 1980-12-16 Foster Wheeler Energy Corporation Process for production of methanol
DE102004059315A1 (de) * 2004-11-30 2006-06-01 Michael Prestel Kompressor-Arbeitsmaschine

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of WO2017021245A1 *

Also Published As

Publication number Publication date
WO2017021245A1 (fr) 2017-02-09
US10336674B2 (en) 2019-07-02
AU2016302420B2 (en) 2019-02-14
DE102015214943A1 (de) 2017-02-09
AU2016302420A1 (en) 2018-02-01
CN107922298A (zh) 2018-04-17
CL2018000202A1 (es) 2018-07-13
US20180221841A1 (en) 2018-08-09

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