NO874936L - PROCEDURE AND APPARATUS FOR TEMPERATURE REGULATION OF CATALYST LAYER IN AMMONIA SUCTION SYSTEMS. - Google Patents

PROCEDURE AND APPARATUS FOR TEMPERATURE REGULATION OF CATALYST LAYER IN AMMONIA SUCTION SYSTEMS.

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Publication number
NO874936L
NO874936L NO874936A NO874936A NO874936L NO 874936 L NO874936 L NO 874936L NO 874936 A NO874936 A NO 874936A NO 874936 A NO874936 A NO 874936A NO 874936 L NO874936 L NO 874936L
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NO
Norway
Prior art keywords
gas
catalyst layer
tube
control piston
heat exchanger
Prior art date
Application number
NO874936A
Other languages
Norwegian (no)
Other versions
NO874936D0 (en
Inventor
Hans-Joachim Herbort
Heinz Graeve
Hans-Dieter Marsch
Hans-Guenter Brieke
Original Assignee
Uhde Gmbh
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Publication date
Application filed by Uhde Gmbh filed Critical Uhde Gmbh
Publication of NO874936D0 publication Critical patent/NO874936D0/en
Publication of NO874936L publication Critical patent/NO874936L/en

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    • 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
    • B01J8/001—Controlling catalytic processes
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0496—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0417—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the synthesis reactor, e.g. arrangement of catalyst beds and heat exchangers in the reactor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0482—Process control; Start-up or cooling-down procedures
    • 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
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • 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
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • 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
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00203—Coils
    • 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
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Description

Foreliggende oppfinnelse angår en fremgangsmåte for temperaturregulering av katalysatorsj ikt i ammonlakksynteseanlegg, ved hvilken det anvendes en kretsløpgass og hvor det tilføres en mengde med frisk gass tilsvarende i hovedsaken den utskilte ammoniakken. The present invention relates to a method for temperature regulation of the catalyst layer in an ammonium lacquer synthesis plant, in which a circuit gas is used and where an amount of fresh gas is supplied corresponding mainly to the separated ammonia.

Ved en slik prosess må det forefinnes en mengde med regu-leringsmuligheter med hensyn til katalysators;] iktene. Således starter først fremgangsmåten ved ammoniakksyntesen først når det hersker en bestemt temperatur i et første katalysatorsjikt. For dette formål blir f.eks. tilført fremmedenergi utenfra, f.eks. ved hjelp av en tilformet oppvarmer. Først når prosessen en gang er startet må den som regel opprett-holdes derfra på grunn av den eksoterme reaksjonen i katalysatorsj iktet uten at det er nødvendig med ytterligere tilførsel av fremmed energi. For forvarming blir derfor kretsløpgassen som regel tilført en varmeveksler koblet etter det første katalysators,] iktet, som blir oppvarmet av krets-løpgassen som forlater det første kretsløpsjiktet. Deretter kommer et ytterligere katalysatorsjikt, som igjen kan bli fulgt av et tredje katalysatorsjikt. In such a process, there must be a quantity of regulation possibilities with regard to the properties of the catalyst. Thus, the ammonia synthesis process only starts when a certain temperature prevails in a first catalyst layer. For this purpose, e.g. added foreign energy from outside, e.g. using a shaped heater. Only once the process has started does it usually have to be maintained from there due to the exothermic reaction in the catalyst layer without the need for a further supply of extraneous energy. For preheating, the circuit gas is therefore usually supplied to a heat exchanger connected after the first catalyst's,] ict, which is heated by the circuit gas leaving the first circuit layer. Then comes a further catalyst layer, which in turn can be followed by a third catalyst layer.

Et reguleringsproblem består nå deri at en forholdsvis stor mengde med prosessgass blir ført som kretsløpgass slik at det må sørges for at denne store mengden ved inngangen til katalysatorsjiktet blir holdt på de respektive temperaturene, som på ene siden skal være høye nok og må holde reaksjonen i gang og på den andre siden være slik at det blir tilveiebragt en høy omsetting og videre skal utgangstemperaturen fra katalysatorsjiktet være så lav at den beskytter kataly-satoren, noe som i enkelte tilfeller kan kun tilveiebringes ved hjelp av endring i temperaturen og/eller sammensetting av prosessgassen, dvs. ved hjelp av en form for kjøling. Herved fremkommer en regulering av de enkelte katalysatorsjiktene i avhengighet av hverandre. A regulation problem now consists in the fact that a relatively large amount of process gas is carried as circuit gas so that it must be ensured that this large amount at the entrance to the catalyst bed is kept at the respective temperatures, which on the one hand must be high enough and must keep the reaction in time and on the other side be such that a high conversion is provided and furthermore the outlet temperature from the catalyst bed must be so low that it protects the catalyst, which in some cases can only be provided by means of a change in temperature and/or composition of the process gas, i.e. by means of a form of cooling. This results in a regulation of the individual catalyst layers depending on each other.

Oppgaven for oppfinnelsen er å tilveiebringe en løsning ved hjelp av hvilken det er mulig såvel fremgangsmåtemessig som også innretningsmessig å kunne foreta en mest mulig individuell regulering av de enkelte katalysatorsjiktene. The task of the invention is to provide a solution with the help of which it is possible both in terms of method and also in terms of equipment to be able to carry out the most possible individual regulation of the individual catalyst layers.

Ved fremgangsmåten av den innledningsvis nevnte art blir denne oppgaven ifølge foreliggende oppfinnelse løst ved at for regulering av minst en delmengde av kretsløpgassen som forlater det nest siste katalysatorsjiktet blir tilført en dampfrembringer som varmeveksler og/eller en forbiførende ledning som omgår denne varmeveksleren, idet en delmengde av kald kretsløpgass kan tilføres for oppvarming og tilførsel som det første katalysatorsjiktet til nevnte forbiførende ledning som et kjølemiddel (Quentschmittel). In the method of the kind mentioned at the outset, this task according to the present invention is solved by, for the regulation of at least a partial amount of the circuit gas leaving the penultimate catalyst layer, a steam generator is added as a heat exchanger and/or a bypass line that bypasses this heat exchanger, with a partial amount of cold circuit gas can be supplied for heating and supply as the first catalyst layer to said passing line as a coolant (Quentschmittel).

Oppfinnelsen sørger for at reguleringen av det første katalysatorsjiktet blir foretatt dels over kjølingen (Quent-sche). Med denne utformingen kan det ved hjelp av forholdsvis enkle midler tilveiebringes at reguleringen av det første katalysatorsjiktet ikke påvirker umiddelbart det etter-følgende katalysatorsjiktet, hvorved det ved denne regu-leringstypen må også bli tatt hensyn til et lite vinsttap, med noe som kan tillates når man ser på den totale forenk-lingen av reguleringen. The invention ensures that the regulation of the first catalyst layer is carried out partly over the cooling (Quent-sche). With this design, it can be ensured by means of relatively simple means that the regulation of the first catalyst layer does not immediately affect the subsequent catalyst layer, whereby with this type of regulation a small loss of profit must also be taken into account, with something that can be allowed when one looks at the total simplification of the regulation.

Oppfinnelsen angår også en innretning for gjennomføring av fremgangsmåten som er kjennetegnet ved at den er utformet som dampfrembringende rørbuntvarmeveksler og har et forbi-ledningsrør som går gjennom rørbunten, idet det i området av samlekammeret er sørget for en tilblanding av den kjølte prosessgassen av den varme prosessgassen som strømmer gjennom forbiføringsrøret. The invention also relates to a device for carrying out the method, which is characterized by the fact that it is designed as a steam-generating tube bundle heat exchanger and has a by-pass pipe that runs through the tube bundle, as provision is made for mixing the cooled process gas with the hot process gas in the area of the collection chamber which flows through the bypass pipe.

Den med et forbiføringsrør utførte rørbuntvarmeveksleren utgjør en spesiell hensiktsmessig utforming av innretningen ifølge foreliggende oppfinnelse da det herved ved hjelp av dampfrembringelsen i avhengighet av utførelsen er mulig med en svært følsom styring av det etterfølgende katalysatorsj iktet. The tube bundle heat exchanger made with a bypass tube constitutes a particularly suitable design of the device according to the present invention, as it is thereby possible, with the help of the steam production, depending on the design, to have a very sensitive control of the subsequent catalyst layer.

Ved en utførelsesform av oppfinnelsen er det anordnet et i det vesentlige sylindrisk føringsrør med et aksialt eller radialt innstilbart styrestempel, idet det er anordnet tilblandingsåpninger i føringsrøret og i styrestempelet, som kan lukkes helt eller delvis ved hjelp av aksiale eller radiale bevegelser. In one embodiment of the invention, an essentially cylindrical guide tube is arranged with an axially or radially adjustable control piston, as mixing openings are arranged in the guide tube and in the control piston, which can be closed completely or partially by means of axial or radial movements.

Ved hjelp av foreliggende oppfinnelse er det mulig ved en enkel aksial og radial forskyvning å kunne stille inn respektive forhold mellom varm og avkjølt gass. With the help of the present invention, it is possible by means of a simple axial and radial displacement to be able to set respective ratios between hot and cooled gas.

Ved en ytterligere utførelsesform er forblførlngslednlngen eller strømningsbanen for den kjølte prosessgassen lukket i en endestilling til styrestempelet. In a further embodiment, the supply line or flow path for the cooled process gas is closed in an end position to the control piston.

Ved en ytterligere utførelsesform av oppfinnelsen er styrestempelet i det indre av sylinderen aksialt bevegelig med et sentrisk tetningselement for forbiføringsrøret. In a further embodiment of the invention, the control piston in the interior of the cylinder is axially movable with a centric sealing element for the bypass pipe.

En ytterligere utforming av oppfinnelsen ved varmevekslere med like innløps- og utløpsstusser såvel for varm som også for avkjølt gass består deri at styrestempelet er utformet som et potteformet styreelement som griper over den frie enden til sentralrøret som leder de varme gassene til varmeveksleren, idet det i den ytre veggen til det potteformede styreelementet er anordnet tilblandingsåpninger. Oppfinnelsen sørger også for at den ytre veggen til sentral-røret har utoverpekende tetningssteg, som i bruksstillingen griper inn i tilblandingsåpningene og i avhengighet av endestillingen sentralrøret eller ringrommet tetter mellom sentralrøret og den ytre potteveggen som forbiføringsledning. A further design of the invention for heat exchangers with the same inlet and outlet nozzles for both hot and cooled gas consists in the fact that the control piston is designed as a pot-shaped control element that grips over the free end of the central pipe that leads the hot gases to the heat exchanger, as in the outer wall of the pot-shaped control element is provided with mixing openings. The invention also ensures that the outer wall of the central tube has outward-pointing sealing steps, which in the use position engage the mixing openings and, depending on the end position, the central tube or the annulus seals between the central tube and the outer pot wall as a bypass line.

Oppfinnelsen skal i det påfølgende beskrives nærmere med henvisning til tegningene, hvor: In what follows, the invention will be described in more detail with reference to the drawings, where:

Fig. 1 viser et prinsippkretsdiagram av et anlegg for gjennomføring av fremgangsmåten ifølge foreliggende opp-f innelse. Fig. 2 viser et utførelseseksempel på en innretning ifølge foreliggende oppfinnelse. Fig. 3 viser et annet utførelseseksempel av innretningen ifølge foreliggende oppfinnelse. Fig. 1 viser et første katalysatorsjikt 1, et andre katalysatorsj ikt 2 i en NH3~reaktor 3 såvel som symbolsk antydet en første varmeveksler 4 for forvarming av kretsløpgassen som strømmer gjennom ledningen 5 i retning av pilen 6. Etter gjennomstrømningen av det første katalysatorsjiktet og varmeveksleren 4 såvel som det andre katalysatorsjiktet 2 blir kretsløpgassen tilført et tredje katalysatorsjikt 7, idet det mellom det andre katalysatorsjiktet 7 og det tredje katalysatorsjiktet 3 er anordnet en reguleringsinnretning. Fig. 1 shows a principle circuit diagram of a plant for carrying out the method according to the present invention. Fig. 2 shows an embodiment of a device according to the present invention. Fig. 3 shows another embodiment of the device according to the present invention. Fig. 1 shows a first catalyst layer 1, a second catalyst layer 2 in an NH3~reactor 3 as well as symbolically indicated a first heat exchanger 4 for preheating the circuit gas that flows through the line 5 in the direction of the arrow 6. After the flow through the first catalyst layer and the heat exchanger 4 as well as the second catalyst layer 2, the cycle gas is supplied to a third catalyst layer 7, with a regulation device arranged between the second catalyst layer 7 and the third catalyst layer 3.

Denne reguleringsinnretningen består i det vesentlige av en dampfrembringer 8, en forbiføringsledning 9 og en "Quentsch-ledning" 10, som alternativt kan bli påvirket idet de mulige utformingene er nærmere beskrevet nedenfor. Kretsløpgassen blir så tilført fra det tredje katalysatorsj iktet 7 over en ytterligere dampfrembringer 11 til ene gass-/gassvarmeveksler 12, en kjøler 13 og til slutt en utskiller 14 for å kunne tilføres kretsløpkompressoren 15, som ikke skal nærmere beskrives her. This regulation device essentially consists of a steam generator 8, a bypass line 9 and a "Quentsch line" 10, which can alternatively be affected as the possible designs are described in more detail below. The circuit gas is then supplied from the third catalyst layer 7 via a further steam generator 11 to a gas/gas heat exchanger 12, a cooler 13 and finally a separator 14 in order to be supplied to the circuit compressor 15, which will not be further described here.

Fig. 2 viser muligheten av å kunne bygge inn reguleringsinnretningen i en dobbelt varmeveksler, hvor det ifølge fig. Fig. 2 shows the possibility of being able to build the regulation device into a double heat exchanger, where according to fig.

2 dette ville være den rommessige sammenfatningen av dampfrembringeren 8 med dampfrembringeren 11. For oppfinnelsen er fremfor alt dampfrembringeren 8 viktig, som har et forkammer 16, en rørbunt 17 såvel som et forbiføringsrør 18 sentrert i midten, hvilken ene ende kan lukkes fra et styrestempel 19 via en tetningskjegle 20. 2 this would be the spatial summary of the steam generator 8 with the steam generator 11. For the invention, above all, the steam generator 8 is important, which has a pre-chamber 16, a pipe bundle 17 as well as a bypass pipe 18 centered in the middle, one end of which can be closed from a control piston 19 via a sealing cone 20.

Styrestempelet 19 er anbragt i et føringsrør 21, som har tilblandingsåpninger 22 slik som styrestempelet, idet tilblandingsåpningene til styrestempelet er betegnet med henvisningstallet 23 og som kan bli åpnet helt eller delvis eller fullstendig bli lukket av styrestempelet 19 tilsvarende stillingen til støtfangeren 24 på styrestempelet 19. I avhengighet av åpningsstillingen fremkommer i føringsrøret 21 en blanding av varm ikke-avkjølt prosessgass, som gjennom-strømmer forbiledningsrøret 18, og avkjølt prosessgass, som går inn i et ikke nærmere vist tredje katalysatorsjikt. The control piston 19 is placed in a guide tube 21, which has admixture openings 22 like the control piston, the admixture openings of the control piston being denoted by the reference number 23 and which can be opened completely or partially or be completely closed by the control piston 19 corresponding to the position of the bumper 24 on the control piston 19. Depending on the opening position, a mixture of hot uncooled process gas, which flows through the bypass pipe 18, and cooled process gas, which enters a third catalyst layer not shown in detail, appears in the guide pipe 21.

De respektive gasstrømningene er vist på fig. 2 såvel som på fig. 3 med små piler. The respective gas flows are shown in fig. 2 as well as in fig. 3 with small arrows.

Fig. 3 viser en noe annen oppbygning, idet her er varmeveksleren 8 kun antydet. Over den nedre høyre antydede tilførselsledning 25 blir den varme prosessgassen innført. Den strømmer ved den viste stillingen til styrestempelet 19a inn i en sentral tilførselsledning 26 til varmeveksleren 8, strømmer gjennom denne og kommer etter kjølingen gjennom ringrommet 27 tilbake for å strømme gjennom en ytterligere ledning 28. Fig. 3 shows a somewhat different structure, as here the heat exchanger 8 is only indicated. The hot process gas is introduced over the supply line 25 indicated on the lower right. It flows at the shown position of the control piston 19a into a central supply line 26 to the heat exchanger 8, flows through this and, after cooling, returns through the annulus 27 to flow through a further line 28.

En del av den varme gassen strømmer imidlertid også mellom den indre veggen til styrestempelet 19a og den ytre veggen til det sentrale røret 26 gjennom en form for forbiførings-ledning direkte inn i ledningen 28 og blander seg der med den avkjølte gassen fra ringrommet 27. However, part of the hot gas also flows between the inner wall of the control piston 19a and the outer wall of the central tube 26 through a form of bypass line directly into the line 28 and mixes there with the cooled gas from the annulus 27.

For innstilling av de respektive tilblandingsforholdene har den frie enden til senteralrøret tetningsskiver 29, som griper inn i en sliss 30 i den ytre veggen til styrestempelet 19a. Blir nå f.eks. styrestempelet 19a trukket helt ned i samsvar med dobbeltpilen 31 så støter den øvre begrensnings- kanten til slissen 30 på respektive skiver 29 og sperrer fullstendig forblførlngslednlngen mens sentralrøret 26 står til rådighet på det fulle strømningstverrsnittet. Ved omvendt stilling, dvs. ved en forskyvning av styrestempelet 19a helt opp i samsvar med dobbeltpilen 31 støter den nedre sliss-begrensningen mot skiven 29 og sperrer således fullstendig tilgangen til sentralrøret 26 slik at den totale varme gassmengden strømmer gjennom forblførlngslednlngen direkte inn i stussen 28. For setting the respective mixing ratios, the free end of the central tube has sealing washers 29, which engage in a slot 30 in the outer wall of the control piston 19a. Will now e.g. the control piston 19a pulled all the way down in accordance with the double arrow 31, then the upper limiting edge of the slot 30 abuts the respective discs 29 and completely blocks the supply line while the central tube 26 is available at the full flow cross-section. In the opposite position, i.e. when the control piston 19a is moved all the way up in accordance with the double arrow 31, the lower slot restriction abuts against the disc 29 and thus completely blocks access to the central pipe 26 so that the total amount of hot gas flows through the supply line directly into the spigot 28 .

Dessuten er det anordnet en ytterligere rørstuss 32, til hvilken kan tilsluttes en kjøleledning ("Quentsch-ledning") betegnet med henvisningstallet 10 på fig. 1, gjennom hvilken ubehandlet kretsløpsgass kan bli tilført ledningen 28 henholdsvis forblførlngslednlngen. In addition, a further pipe connection 32 is arranged, to which a cooling line ("Quentsch line") can be connected, denoted by the reference number 10 in fig. 1, through which untreated circuit gas can be supplied to line 28 or the maintenance line.

Claims (8)

1. Fremgangsmåte for temperaturregulering av katalysatorsjiktet i ammonlakksynteseanlegg, ved hvilken det anvendes en kretsløpgass og hvor det tilføres en friskgassmengde tilsvarende den i det vesentlige utskilte ammoniakken, karakterisert ved at for regulering tilføres minst en delmengde av kretsløpsgassen som forlater det nest siste katalysatorsjiktet til en dampfrembringer som varmeveksler og/eller til en forbiføringsledning som går forbi varmeveksleren, idet en delmengde kald kretsløpgass kan tilføres før oppvarmingen og tilførselen til det første katalysatorsjiktet den nevnte forbiføringsledning som "Ouentschmittel" ("kjølemiddel" ).1. Method for temperature regulation of the catalyst layer in an ammonium lacquer synthesis plant, in which a cycle gas is used and where a quantity of fresh gas corresponding to the essentially excreted ammonia is supplied, characterized in that for regulation at least a partial quantity of the cycle gas that leaves the penultimate catalyst layer is supplied to a steam generator as a heat exchanger and/or to a bypass line that goes past the heat exchanger, a partial amount of cold circuit gas can be supplied before the heating and supply to the first catalyst layer the said bypass line as "Ouentschmittel" ("coolant"). 2. Fremgangsmåte ifølge krav 1, karakterisert ved at for regulering av det første katalysatorsjiktet foretar i det minste delvis over en "Quentsch".2. Method according to claim 1, characterized in that for the regulation of the first catalyst layer, a "Quentsch" is carried out at least partially. 3. Innretning for gjennomføring av fremgangsmåten ifølge et av de foregående krav, karakterisert ved at den er utformet som en dampfrembringende rørbuntvarmeveksler (8) og at den har et forbiføringsrør (18) som går gjennom rørbunten (17), idet det i endeområdet av samlekammeret sørges for at den avkjølte prosessgassen tilblandes en varm prosessgass gjennomstrømmende forblførlngslednlngen (18).3. Device for carrying out the method according to one of the preceding claims, characterized in that it is designed as a steam-producing tube bundle heat exchanger (8) and that it has a bypass tube (18) that passes through the tube bundle (17), in that in the end area of the collection chamber provision is made for that the cooled process gas is mixed with a hot process gas flowing through the expansion line (18). 4 . Innretning ifølge krav 3, karakterisert ved at som tilblanding er anordnet et i det vesentlige sylindrisk føringsrør 21 med aksialt eller radialt innstillbart styrestempel (19), idet det i føringsrøret (21) og i styrestempelet (19) er anordnet tilblandingsåpninger (22) hen holdsvis (23), som kan lukkes helt eller delvis ved aksial eller radial bevegelse.4. Device according to claim 3, characterized in that an essentially cylindrical guide tube 21 with an axially or radially adjustable control piston (19) is arranged as admixture, with admixture openings (22) arranged in the guide tube (21) and in the control piston (19) respectively (23), which can be closed completely or partially by axial or radial movement. 5. Innretning ifølge krav 3 eller 4, karakterisert ved at i endestillingen til styrestempelet (19) er forblførlngslednlngen (18) eller strømningsbanen for den avkjølte prosessgassen lukket.5. Device according to claim 3 or 4, characterized in that in the end position of the control piston (19) the supply line (18) or the flow path for the cooled process gas is closed. 6. Innretning ifølge kravene 3-5, karakterisert ved at styrestempelet (19) kan beveges aksialt i det indre av føringsrøret (21) med et sentrisk tetningselement (20) for forbiføringsrøret (18).6. Device according to claims 3-5, characterized in that the control piston (19) can be moved axially in the interior of the guide tube (21) with a centric sealing element (20) for the bypass tube (18). 7. Innretning ved varmevekslere med samme innløps- og utløps-stuss såvel for varm som også for avkjølt gass, karakterisert ved at styrestempelet (19) er utformet som et potteformet styreelement som griper om den frie enden til sentralrøret (26) som leder den varme gassen til varmeveksleren (8), idet det er anordnet tilblandingsåpninger (30) i det potteformede styreelementets vegg.7. Device for heat exchangers with the same inlet and outlet connection both for hot and for cooled gas, characterized in that the control piston (19) is designed as a pot-shaped control element that grips the free end of the central pipe (26) which leads the hot gas to the heat exchanger (8), as mixing openings (30) are arranged in the wall of the pot-shaped control element. 8. Innretning ifølge krav 7, karakterisert ved at det på den ytre veggen til sentralrøret er anordnet utoverpekende tetningssteg, som i brukerstillingen griper inn i tilblandingsåpningen (30) og i avhengighet av endestillingen avtetter sentralrøret (26) eller ringrommet mellom sentralrøret (26) og den pottelignende ytterveggen til styreelementet som forbiføringsledning.8. Device according to claim 7, characterized in that the outer wall of the central tube is arranged with outward-pointing sealing steps, which in the user position engage the mixing opening (30) and, depending on the end position, seal the central tube (26) or the annular space between the central tube (26) and the pot-like the outer wall of the control element as a bypass line.
NO874936A 1986-12-22 1987-11-26 PROCEDURE AND APPARATUS FOR TEMPERATURE REGULATION OF CATALYST LAYER IN AMMONIA SUCTION SYSTEMS. NO874936L (en)

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EP0550525B1 (en) * 1990-09-24 1995-08-02 C F Braun Inc. High conversion ammonia synthesis
DE102004028200B3 (en) 2004-05-28 2005-12-15 Hippweb E.K. Method for carrying out heterogeneous catalytic exothermic gas phase reactions for the synthesis of methanol
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GB1574723A (en) * 1976-03-10 1980-09-10 Haldor Topsoe As Apparatus for the synthesis of ammonia
GB1601475A (en) * 1977-04-18 1981-10-28 Ici Ltd Catalytic reactor
EP0011404B1 (en) * 1978-11-10 1982-12-29 Imperial Chemical Industries Plc Integrated process for synthesis of methanol and of ammonia
FR2460707B1 (en) * 1979-07-13 1986-09-05 Ammonia Casale Sa SYNTHESIS REACTOR, IN PARTICULAR FOR THE CATALYTIC SYNTHESIS OF AMMONIA AND METHANOL
DE3066990D1 (en) * 1979-09-14 1984-04-19 Ici Plc Synthesis reactor and processes
IT1141102B (en) * 1980-11-28 1986-10-01 Ammonia Casale Sa AXIAL-RADIAL REACTOR FOR HETEROGENEOUS SYNTHESIS
DE3343114C2 (en) * 1983-11-29 1985-11-07 Uhde Gmbh, 4600 Dortmund Device for carrying out exothermic, catalytic gas reactions for ammonia or methanol synthesis
US4655277A (en) * 1984-04-27 1987-04-07 Phillips Petroleum Company Process control for parallel heat exchangers
US4568530A (en) * 1984-10-16 1986-02-04 The M. W. Kellogg Company Ammonia synthesis
US4568532A (en) * 1984-10-16 1986-02-04 The M. W. Kellogg Company Supplemental ammonia synthesis
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DK612487A (en) 1988-06-23
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NO874936D0 (en) 1987-11-26
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ZA879164B (en) 1988-06-03
JPS63214339A (en) 1988-09-07
AU8241287A (en) 1988-06-23
FI875283A0 (en) 1987-11-30
JPH0471574B2 (en) 1992-11-16
CN87107464A (en) 1988-07-06
EP0272449A3 (en) 1988-12-21
EP0272449A2 (en) 1988-06-29
CN1009434B (en) 1990-09-05
DE3643858A1 (en) 1988-06-30

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