DK166772B1 - CONTROL DEVICE SPECIAL FOR AN AMMONIA CONVERTER - Google Patents
CONTROL DEVICE SPECIAL FOR AN AMMONIA CONVERTER Download PDFInfo
- Publication number
- DK166772B1 DK166772B1 DK647587A DK647587A DK166772B1 DK 166772 B1 DK166772 B1 DK 166772B1 DK 647587 A DK647587 A DK 647587A DK 647587 A DK647587 A DK 647587A DK 166772 B1 DK166772 B1 DK 166772B1
- Authority
- DK
- Denmark
- Prior art keywords
- heat exchanger
- catalyst bed
- gas
- process gas
- centrally located
- Prior art date
Links
Classifications
-
- 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
- C01C1/0423—Cold wall reactors
-
- 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
- B01J8/0403—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 fluid flow within the beds being predominantly horizontal
- B01J8/0407—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 fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
- B01J8/0415—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 fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped 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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Control Of Non-Electrical Variables (AREA)
- Dc-Dc Converters (AREA)
- Fats And Perfumes (AREA)
- Sampling And Sample Adjustment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Exhaust Gas After Treatment (AREA)
- Investigating Or Analysing Materials By Optical Means (AREA)
- Networks Using Active Elements (AREA)
- Incineration Of Waste (AREA)
Abstract
Description
DK 166772 B1DK 166772 B1
Opfindelsen angår et apparat til regulering af specielt en ammoniakkonverter med mindst en af procesgassen først bestrøget varmeveksler og mindst et af procesgassen efterfølgende bestrøget katalysatorleje, hvorhos procesgassen efter gennem-5 strømningen af katalysatorlejet igen som varmeudvekslingsgas strømmer gennem varmeveksleren, og hvor varmeveksleren og det omgivende første katalysatorleje er rotationssymmetrisk i forhold til et centralt placeret rør, gennem hvilket der strømmer en reguleringsgas med henblik på temperaturstyringen.The invention relates to an apparatus for controlling, in particular, an ammonia converter with at least one of the process gas first coated heat exchanger and at least one of the process gas subsequently coated catalyst bed, the process gas after the flow of the catalyst bed again as heat exchange gas flows through the heat exchanger and where the heat exchanger catalyst bed is rotationally symmetrical with respect to a centrally located tube through which a control gas flows for the purpose of temperature control.
1010
Fra EP-A-0 114 138 kendes et sådant apparat, i hvilket et centralt rør med henblik på temperaturstyringen går helt gennem en varmeveksler, som et reguleringsgastilføringsrør. Dog 15 sker iblandingen af reguleringsgassen først efter, at procesgassen allerede har gennemstrømmet det første katalysatorleje.EP-A-0 114 138 discloses such an apparatus in which a central pipe for the purpose of temperature control is passed completely through a heat exchanger, such as a control gas supply pipe. However, mixing of the control gas occurs only after the process gas has already flowed through the first catalyst bed.
Det første katalysatorleje kan altså ikke selv blive bestrøget af reguleringsgassen.Thus, the first catalyst bed cannot be coated by the control gas itself.
20 Det er også ved apparater til gennemførelse af exoterme katalytiske gasreaktioner til ammoniak- eller methanolsyntese kendt, til regulering ved hjælp af en særskilt gastilførsel i trykbeholderen, at tilføre f.eks. kold friskgas til procesgasstrømmen i et forkammer til den pågældende varmeveksler, som 25 er tilknyttet det første katalysatorleje, hvorhos der ved det kendte apparat i trykbeholderen er anbragt to katalysatorlejer med hver sin koncentrisk i midten anbragte varmeveksler. Dette fremgår af DE-C-33 43 114.It is also known in the apparatus for carrying out exothermic catalytic gas reactions for ammonia or methanol synthesis, for regulation by means of a separate gas supply in the pressure vessel, to supply e.g. cold fresh gas to the process gas stream in a pre-chamber of the respective heat exchanger, which is associated with the first catalyst bed, wherein two known catalyst beds are arranged in the pressure vessel with the concentric heat exchanger, each centrally located in the middle. This is stated in DE-C-33 43 114.
30 Fra DE-C-27 10 247 kendes en fremgangsmåde, hvor procesgasstrømmen sammensættes af to delstrømme, og hvor mindst den ene af delstrømmene er indstillelig hvad angår temperatur og/eller mængde, så man kan opnå de ønskede procesbetingelser. Sammenføringen af gasstrømmene sker i alle tilfælde før de træder 35 ind i det første katalysatorleje.DE-C-27 10 247 discloses a method in which the process gas stream is composed of two sub-streams and at least one of the sub-streams is adjustable in terms of temperature and / or quantity so that the desired process conditions can be obtained. The gas streams are combined in all cases before entering 35 into the first catalyst bed.
Ved de kendte reguleringsindretninger er det i praksis ikke DK 166772 B1 2 muligt ved en omledning at lede reguleringsgassen fuldstændig forbi det første katalysatorleje og den dertil knyttede varmeveksler og dertil at tilsætte den gasstrøm, som allerede har gennemstrømmet det første katalysatorleje og den dertil knyt-5 tede varmeveksler.In the known control devices, in practice, it is not possible in a diversion to pass the control gas completely past the first catalyst bed and the associated heat exchanger and to add to it the gas stream which has already flowed through the first catalyst bed and the associated catalyst bed. heat exchanger.
Formålet med opfindelsen er at anvise en løsning, som gør det muligt, på ethvert sted i en reaktor, at føre en reguleringsgas, en bratkølingsgas eller en del af procesgasstrømmen med 10 en anden temperatur og/eller andre betingelser ind i den til enhver tid værende gasstrøm, idet løsningen skal være valgt således, at tilsætningskanalen henholdsvis omløbskanalen er udformet fuldstændig aflukkelig eller delvis gennemstrømmelig henholdsvis kan åbnes helt.The object of the invention is to provide a solution enabling, at any point in a reactor, a regulating gas, a quenching gas or part of the process gas stream with a different temperature and / or other conditions to be present at any given time. gas flow, the solution having to be selected such that the addition duct or bypass duct is designed to be completely closable or partially flowable or fully open, respectively.
1515
Apparatet ifølge opfindelsen er ejendommeligt ved, at det centralt placerede rør går fuldstændigt igennem katalysatorlejet, og ved sin nedre ende er forsynet med regulerbare udløb med henblik på i det mindste delvis iblanding af reguleringsgas i 20 procesgasstrømmen, før dennes gennemstrømning af katalysatorlejet og med henblik på iblanding af reguleringsgasstrømmen i procesgasstrømmen efter dennes gennemstrømning af katalysatorlejet og varmeveksleren.The apparatus according to the invention is characterized in that the centrally located pipe passes completely through the catalyst bed and at its lower end is provided with adjustable outlets for at least partial mixing of control gas into the process gas stream, before its flow through the catalyst bed and for admixing the control gas stream into the process gas stream after its flow through the catalyst bed and heat exchanger.
25 Med dette apparat bliver der ved hjælp af det centralt placerede regulerbare rør ikke blot opnået, at f.eks. reguleringsgassen i den ene yderstilling løber tværs igennem varmeveksleren, og først derefter bliver ledt ind i processtrømmen, når denne er strømmet igennem det første katalysatorleje og efter-30 følgende har gennemstrømmet varmeveksleren, dvs. f.eks. i den gasstrøm, der skal bestryge det efterfølgende katalysatorleje.With this apparatus, by means of the centrally located adjustable tube, it is not only achieved that e.g. the control gas in one outer position runs transversely through the heat exchanger, and only then is fed into the process stream when it has flowed through the first catalyst bed and subsequently has flowed through the heat exchanger, ie. eg. in the gas stream which is to coat the subsequent catalyst bed.
Men det er også muligt at lede reguleringsgas ind før det første katalysatorleje og i mellemstillinger såvel før det første katalysatorleje som også før det efterfølgende kataly-35 satorleje.However, it is also possible to conduct control gas in before the first catalyst bed and in intermediate positions both before the first catalyst bed and also before the subsequent catalyst bed.
I en udførelsesform ifølge opfindelsen omgiver det gennem DK 166772 B1 3 varmeveksleren gående føringsrør for procesgassen det centralt placerede regulerbare rør i afstand. Denne opbygning har den fordel, at udformningen af såvel varmeveksleren som det centralt placerede gennemgående omløbsrør er forholdsvis enkel.In one embodiment of the invention, the conductor pipe passing through the heat exchanger surrounding the process gas surrounds the centrally located adjustable pipe at a distance. This construction has the advantage that the design of both the heat exchanger and the centrally located through-flow pipe is relatively simple.
5 Som regel kan særlige rørbøjninger og lignende så undgås.5 As a rule, special pipe bends and the like can be avoided.
I en speciel fordelagtig udførelsesform for opfindelsen er fordelingsåbningerne i det centralt placerede rør udformet synkront styrbare i forhold til hinanden. Med denne regulering 10 er det ikke blot muligt at opnå enkelte reguleringsindstillinger, f.eks. på den måde, at et udløb på reguleringsrøret er fuldstændigt lukket, medens det andet er fuldstændigt åbent og omvendt, men man kan også indstille enhver mellemstilling synkront, dvs. reguleringsgassen kan i enhver ønsket delmængde 15 blandes i de til enhver tid værende procesgasstrømme.In a particularly advantageous embodiment of the invention, the distribution openings in the centrally located tube are designed to be synchronously controllable relative to one another. With this control 10 it is not only possible to obtain individual control settings, e.g. in that one outlet of the control tube is completely closed while the other is completely open and vice versa, but you can also set any intermediate position synchronously, ie. the control gas can be mixed in any desired subset 15 in the process gas streams at any given time.
Det har vist sig at være hensigtsmæssigt, at det centralt placerede rør med henblik på gennemstrømningsreguleringen har et med aksiale génnembrydninger forsynet lukkestempel, hvorved 20 reguleringsgassens gennemstrømning gennem åbninger i røret kan styres i en strømningskanal, som procesgassen kommer ind i efter den første gennemstrømning af varmeveksleren. Uden at det ville være en begrænsning af opfindelsen, kan denne styremulighed udføres særlig enkelt. Således kan det med aksiale 25 gennembrydninger forsynede stempel enten ved forskydning delvis åbne eller lukke sideåbningerne i den nederste del af det centralt placerede rør, eller det kan ske ved rotation ved en passende stempelopbygning.It has been found to be convenient that the centrally located pipe for the flow control has an axial breakthrough closure piston, whereby the control gas flow through openings in the pipe can be controlled in a flow channel into which the process gas enters after the first flow of the heat exchanger. . Without limiting the invention, this control option can be performed particularly simply. Thus, the piston provided with axial breakthroughs can either partially open or close the side openings in the lower part of the centrally located tube, or it can be rotated by a suitable piston structure.
30 Ved den før omtalte udførelsesform for opfindelsen med en del af styreorganet opbygget som en cylinder, er det hensigtsmæssigt, at den nedre frie ende af det centralt anbragte rør udmunder i et fordelerkammer for den procegas, som netop for anden gang har gennemstrømmet varme vekslenren, og via et med 35 stemplet forbundet tætningselement er udformet fuldstændig tætnelig.In the aforementioned embodiment of the invention, with a portion of the control means constructed as a cylinder, it is desirable that the lower free end of the centrally located pipe opens into a distributor chamber for the process gas which has just flowed through the heat exchanger for the second time. and through a sealing element connected to 35, a completely sealable design is provided.
DK 166772 B1 4DK 166772 B1 4
Specielt ved flere katalysatorlejer med dertil indvendigt koncentrisk anbragte varmevekslere, kan ifølge opfindelsen det centralt placerede rør og/eller funktionen af de regulerbare udløb i det mindste gå igennem en yderligere varmeveksler. Her 5 gælder stadigvæk det i indledningen fremførte, nemlig at den særlige fordel ved opfindelsen består i den enkle styring af reguleringsgasstrømmene, hvorved den til enhver tid herskende situation bliver ganske nøjagtig styrbar, da reguleringsgasstrømme altid vil kunne indsættes, der hvor de er påkrævede.In particular, in the case of several catalyst beds with concentrically disposed heat exchangers therein, according to the invention, the centrally located pipe and / or the function of the adjustable outlets can at least go through an additional heat exchanger. Here 5 still applies to what has been stated in the introduction, namely that the particular advantage of the invention consists in the simple control of the regulating gas streams, whereby the situation prevailing at any time becomes quite precisely controllable, since regulating gas streams can always be inserted where they are required.
10 I en mere speciel udførelsesform for opfindelsen kan ved en centreret tilstrømning af beholdersvøbet afkølende kold procesgas nedefra gennem et tredje katalysatorleje i forkammeret til den anden varmeveksler være tilvejebragt et reguleringsor-15 gan, som muliggør iblanding af i det mindste en del af den koldere kappegas i procesgassen, før den strømmer ind i det tredje katalysatorleje. Herved kan den koldere kappegas ikke kun gå den sædvanlige opvarmningsvej gennem den anden og den første varmeveksler, men det er derved samtidig muligt at 20 anvende en del som reguleringsgas for det tredje katalysator-leje. Omvendt kan mængderne af kappegas, som bliver ført til ovenfor nævnte første og andet katalysatorleje, naturligvis også styres ved hjælp af dette kredsløb.In a more particular embodiment of the invention, a centralized influx of the container wrap cooling cold process gas from below through a third catalyst bed in the front chamber to the second heat exchanger may provide a control means which allows mixing of at least a portion of the colder cutting gas in the process gas before flowing into the third catalyst bed. In this way, the colder cutting gas can not only pass the usual heating path through the second and the first heat exchanger, but at the same time it is possible to use part as control gas for the third catalyst bed. Conversely, the amounts of cutting gas supplied to the above-mentioned first and second catalyst beds can, of course, also be controlled by means of this circuit.
25. Endelig kan det være fordelagtigt, når et andet centralt placeret rør går gennem det første centralt placerede rør, hvorhos det andet centralt placerede rør er ført ned til under den følgende varmeveksler og tjener til iblandingen af reguleringsgas i procesgasstrømmen, før det tredje katalysatorleje.25. Finally, it may be advantageous when a second centrally located pipe passes through the first centrally located pipe, the second centrally located pipe being passed down below the following heat exchanger and serving to incorporate control gas into the process gas stream before the third catalyst bed.
30 På dette sted skal det bemærkes, at den trinvise opbygning af i hinanden anbragte centrerede rør, der muliggør tilstrømning af flere reguleringsgasstrømme, ikke kun er begrænset til den todelte opbygning. Afhængigt af antallet af trin kan der være 35 tilvejebragt flere sådanne koncentriske rør.30 At this point, it should be noted that the incremental construction of interconnected centered pipes, enabling the flow of multiple control gas flows, is not limited to the two-part structure. Depending on the number of steps, several such concentric tubes may be provided.
5 DK 166772 Bl5 DK 166772 Bl
Opfindelsen forklares nedenfor under henvisning til tegningen, hvor fig. 1 viser et snit gennem et apparat ifølge opfindelsen med 5 to katalysatorlejer og en reguleringsindretning, fig. 2 snit gennem en anden udførelsesform med tre katalysatorlejer, 10 fig. 3 en anden udførelsesform for opbygningen vist i fig. 2, fig. 4 endnu en udførelsesform for opfindelsen, og fig. 5 en anden opbygning af en regulering som den, der anven-15 des i udførelsesformen i fig. 4.The invention is explained below with reference to the drawing, in which fig. 1 shows a section through an apparatus according to the invention with two catalyst bearings and a control device; FIG. 2 is a section through another embodiment with three catalyst bearings; FIG. 3 shows another embodiment of the structure shown in FIG. 2, FIG. 4 shows another embodiment of the invention; and FIG. 5 shows another structure of a control such as that used in the embodiment of FIG. 4th
Apparatet, som helhed betegnet med 1, består i det væsentlige af en trykbeholder 2, hvor der i det i fig. 1 viste eksempel er to katalysatorlejer. I de udførelsesformer, der er vist i 20 fig. 2 til 4, er tre katalysatorlejer anbragt koncentrisk i forhold til centeraksen 3. Det øverste og første katalysatorleje er betegnet med 4, det andet med 5 og det nederste og sidste (i den udførelsesform, der er vist i fig. 2 til 4) med 6.The apparatus, generally denoted by 1, consists essentially of a pressure vessel 2, in which, in the embodiment shown in FIG. 1 is two catalyst beds. In the embodiments shown in FIG. 2 to 4, three catalyst bearings are arranged concentrically relative to the center axis 3. The upper and first catalyst bearings are designated 4, the second with 5, and the lower and last (in the embodiment shown in Figures 2 to 4) with 6th
2525
Inden i det første katalysatorleje 4 er der anbragt en første varmeveksler 7, hvorhos der i udførelsesformerne ifølge fig.Within the first catalyst bed 4 is provided a first heat exchanger 7, which in the embodiments of FIG.
2-4, er anbragt en anden varmeveksler 8 inden i det andet katalysatorleje 5, og hvor varmevekslerne 7 og 8 i sidstnævnte 30 tilfælde funktionsmæssigt er koblet efter hinanden. Katalysatorerne, inklusive varmevekslerne, er omgivet af en indhyld-ningsvæg 9, der er således afpasset, at der mellem den indvendige overflade af beholdervæggen og indhylningsvæggen 9 opstår et gennemgående ringformet hulrum 10.2-4, a second heat exchanger 8 is disposed within the second catalyst bed 5 and the heat exchangers 7 and 8 in the latter 30 cases are functionally coupled one after the other. The catalysts, including the heat exchangers, are surrounded by an envelope wall 9 which is adapted so that a continuous annular cavity 10 is formed between the inner surface of the container wall and the envelope wall 9.
3535
Ved udførelsesformen i fig. 1 strømmer en kølegas ind fra oven i apparatet 1 gennem en studs 11, derefter gennem det ringfor- DK 166772 B1 6 mede hulrum 10 og kommer ud forneden sammen med kredsløbsgassen gennem en studs 12. Den øvre indgangsstuds for kredsløbs-gassen er betegnet med 13. Koncentrisk anbragt inden i varmeveksleren 7 er et rør 14, som gennem en tilførselsstuds 15 kan 5 forsynes med gas til reguleringen.In the embodiment of FIG. 1, a cooling gas flows in from above the apparatus 1 through a stud 11, then through the annulus 10 through cavity 10 and exits below the circulation gas through a stud 12. The upper inlet of the circulating gas is designated 13 Concentrically disposed within the heat exchanger 7 is a pipe 14 which can be supplied with gas through the supply nozzle 15 for control.
Dette centralt placerede rør udmunder i et fordelerkammer 16 for den procesgas, som allerede har gennemstrømmet det første katalysatorleje 4 både indvendigt og udvendigt på varmeveksle-10 ren 7 og føringsrørene 30.This centrally located pipe opens into a distributor chamber 16 for the process gas which has already flowed through the first catalyst bed 4 both internally and externally on the heat exchanger 7 and the guide pipes 30.
Nedenfor den første varmeveksler 7 er tilvejebragt endnu et fordelerkammer 17 gastæt adskilt fra fordelerkammeret 16, hvortil procesgassen når, efter at den er strømmet udvendigt 15 på føringsrørene 30 i varmeveksleren 7, og hvorfra den tilføres katalysatorlejet 4. I dette område har det centralt placerede rør 14 åbninger 18, hvorigennem i det mindste en del af den gennem det centralt, placerede rør 14 strømmende reguleringsgas kan strømme ind i fordelerkammeret 17. Ved hjælp af 20 en styrestang 19, som i området ved slidserne 18 har et med aksiale gennemgående huller forsynet aflukningsstempel 20, og som i sin nedre frie ende har en lukkeprop 21, kan opnås en regulering af styregassen og en procentuel fordeling af del-strømme af styregassen til fordelerkammeret 16 og fordelerkam-25 meret 17.Below the first heat exchanger 7 there is provided another distributor chamber 17 gas-tightly separated from the distributor chamber 16, to which the process gas reaches, after being flowed externally 15 on the guide pipes 30 in the heat exchanger 7, and from which it is fed to the catalyst bed 4. In this region, the centrally located pipe 14 openings 18, through which at least a portion of the regulating gas flowing through the centrally located tube 14 can flow into the distributor chamber 17. By means of a control rod 19, which in the region of the slots 18 has a closure piston fitted with axial through holes. 20, and having at its lower free end a closing plug 21, a control of the control gas and a percentage distribution of partial flows of the control gas to the distributor chamber 16 and the distributor chamber 17 can be obtained.
Apparatet fungerer som følger:The device works as follows:
Hvis f.eks. styrestangen 19 er blevet trukket helt op i ret-30 ning af dobbeltpilen 22, så lukker proppen 21 den nedre frie ende af det centralt placerede rør 14 samtidig med, at slidserne 18 er fuldstændigt åbne. Reguleringsgassen strømmer nu kun gennem slidserne 18 ind i rummet 17, dvs. den blandes med procesgasstrømmen, før dennes gennemstrømning af katalysator-35 lejet 4.For example, the guide rod 19 has been pulled fully in the direction of the double arrow 22, so the plug 21 closes the lower free end of the centrally located tube 14 while leaving the slots 18 completely open. The control gas now only flows through the slots 18 into the space 17, ie. it is mixed with the process gas stream prior to its flow through the catalyst bed 4.
Bliver styrestangen 19 nu ført nedad, åbner aflukningsproppen DK 166772 B1 7 21 den nedre afgangsåbning, efterhånden som slidserne 18 bliver lukket, så at der ved den nedre hvilestilling aflukkes fuldstændigt for slidserne 18, medens den nedre åbning af det centralt placerede rør 14 er fuldstændigt åben ud mod forde-5 lerkammeret 16, således at den totale reguleringsgasstrøm faktisk tilføres i form af en omledning dertil og blandes med procesgasstrømmen, som både har gennemstrømmet det første katalysatorleje og varmeveksleren 7 indvendigt og udvendigt.If the guide rod 19 is now directed downwards, the closure plug DK 166772 B1 7 21 opens the lower outlet opening as the slots 18 are closed, so that at the lower rest position, the slots 18 are completely closed, while the lower opening of the centrally located tube 14 is complete. open to the distributor chamber 16 so that the total regulating gas stream is actually supplied in the form of a diversion thereto and mixed with the process gas stream which has flowed through both the first catalyst bed and the heat exchanger 7 internally and externally.
10 Dele i de efterfølgende udførelsesformer, der er funktionsmæssigt ens, er betegnet med det samme henvisningstal efterfulgt af små bogstaver:Parts of the following embodiments, which are functionally similar, are denoted by the same reference numeral followed by lowercase letters:
Ved udførelsesformen ifølge fig. 2 er forholdene i det væsent-15 lige de samme, dog med den ændring, at procesgassen bliver tilført fra oven som en delstrøm centralt gennem en rørstuds 13a og en del gennem en rørstuds 11a som afkølende kappegas, der derefter gennemstrømmer det tredje katalysatorleje 6a nedefra gennem et i dennes midte placeret stigrør 23, og der-20 efter den anden varmeveksler 8 og til sidst ind i blandings-kammeret 17a. Fordelingen af styregassen løses her på samme måde, som i udførelsesformen ifølge fig. 1.In the embodiment of FIG. 2, the conditions are essentially the same, with the change, however, that the process gas is fed from above as a partial flow centrally through a pipe nozzle 13a and a part through a pipe nozzle 11a as cooling cutting gas, which then flows through the third catalyst bed 6a from below. through a riser 23 located in the middle thereof and thereafter 20 after the second heat exchanger 8 and finally into the mixing chamber 17a. The distribution of the control gas is solved here in the same way as in the embodiment of FIG. First
Det forholder sig på lignende måde med udførelsesformen i fig.It is similar to the embodiment of FIG.
25 3; her bliver i hvert fald kredsløbsgassen tilført i tre del strømme via en øvre til føringsstuds 13b, en øvre første kap-pegastilføringsstuds llb og yderligere via en nedre kappegastilførselsstuds 24. Her bliver via radielle sammenføringskanaler 25 kappegasstrømmen fra oven og fra neden, nedenunder den 30 anden varmeveksler 8b, samlet i et fælles forkammer 26 og ført opefter. Iblandingen af reguleringsgas opnås her igen på samme vis.25 3; here at least the circulating gas is supplied in three parts streams via an upper to guide nozzle 13b, an upper first cap gas supply nozzle 11b and further via a lower cap gas supply nozzle 24. Here, via radial connecting channels 25, the gas gas flow from above and below, below the second 30 heat exchanger 8b, assembled in a common front chamber 26 and led upwards. The mixture of control gas is again obtained in the same way.
I en anden udførelsesform består styringen ifølge fig. 4 i, at 35 styrestangen 19c der går fuldstændigt igennem den første varmeveksler 7c og den anden varmeveksler 8c og regulerer tilførselen af den nedefra gennem den centralt placerede tilførsels-In another embodiment, the control of FIG. 4 in that the control rod 19c passes completely through the first heat exchanger 7c and the second heat exchanger 8c and regulates the supply thereof from below through the centrally located supply line.
Claims (7)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19863643856 DE3643856A1 (en) | 1986-12-22 | 1986-12-22 | DEVICE FOR REGULATING, IN PARTICULAR, AN AMMONIA CONVERTER |
| DE3643856 | 1986-12-22 |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| DK647587D0 DK647587D0 (en) | 1987-12-09 |
| DK647587A DK647587A (en) | 1988-06-23 |
| DK166772B1 true DK166772B1 (en) | 1993-07-12 |
Family
ID=6316843
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| DK647587A DK166772B1 (en) | 1986-12-22 | 1987-12-09 | CONTROL DEVICE SPECIAL FOR AN AMMONIA CONVERTER |
Country Status (12)
| Country | Link |
|---|---|
| EP (1) | EP0273231B1 (en) |
| JP (1) | JPS63248431A (en) |
| CN (1) | CN1013664B (en) |
| AT (1) | ATE72423T1 (en) |
| AU (1) | AU602744B2 (en) |
| CA (1) | CA1287480C (en) |
| DE (2) | DE3643856A1 (en) |
| DK (1) | DK166772B1 (en) |
| ES (1) | ES2029260T3 (en) |
| FI (1) | FI875417A (en) |
| NO (1) | NO168020C (en) |
| ZA (1) | ZA879320B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3710004A1 (en) * | 1987-03-26 | 1988-10-06 | Uhde Gmbh | DEVICE FOR THE CATALYTIC TREATMENT OF NITROGEN AND HYDROGEN |
| DE3819451A1 (en) * | 1988-06-08 | 1989-12-14 | Uhde Gmbh | DEVICE FOR CARRYING OUT EXOTHERMAL, CATALYTIC GAS REACTIONS FOR AMMONIA OR METHANOL SYNTHESIS |
| DE69111820T2 (en) * | 1990-09-24 | 1995-12-14 | Braun C F Inc | HIGH CONVERSION AMMONIA SYNTHESIS. |
| US7081230B2 (en) * | 2002-11-15 | 2006-07-25 | Kellogg Brown & Root Llc | Split-flow, vertical ammonia converter |
| EP1442786A1 (en) * | 2003-01-29 | 2004-08-04 | Methanol Casale S.A. | Pseudo isothermal radial reactor |
| US7371361B2 (en) * | 2004-11-03 | 2008-05-13 | Kellogg Brown & Root Llc | Maximum reaction rate converter system for exothermic reactions |
| US7867465B2 (en) * | 2008-05-29 | 2011-01-11 | Kellogg Brown & Root Llc | Cold wall horizontal ammonia converter |
| WO2012172065A1 (en) * | 2011-06-16 | 2012-12-20 | Haldor Topsøe A/S | Method for carrying out exothermic catalytic reactions and a reactor for use in the method |
| CN105621454A (en) * | 2016-02-25 | 2016-06-01 | 山东奥能电力科技有限公司 | Integrated liquid ammonia consumption and conversion device |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1715928U (en) * | 1954-09-18 | 1956-02-02 | Adolf Dipl Ing Schild | HEAT EXCHANGER WITH COOLING WATER VOLUME REGULATOR. |
| US3852147A (en) * | 1972-04-24 | 1974-12-03 | W Wilson | Heat exchanger |
| GB1574723A (en) * | 1976-03-10 | 1980-09-10 | Haldor Topsoe As | Apparatus for the synthesis of ammonia |
| GB1565824A (en) * | 1976-11-15 | 1980-04-23 | Ici Ltd | Exothermic process and apparatus therefor |
| CH646618A5 (en) * | 1981-03-26 | 1984-12-14 | Ammonia Casale Sa | REACTOR FOR CATALYTIC HETEROGENEOUS SYNTHESIS. |
| FR2539524B1 (en) * | 1983-01-17 | 1986-08-22 | Azote & Prod Chim | METHOD FOR REGULATING THE OPERATING TEMPERATURES OF A SYNTHESIS REACTOR AND INTERNAL IMPLEMENTATION EQUIPMENT |
| 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 |
| JPS60225632A (en) * | 1984-04-23 | 1985-11-09 | Mitsubishi Heavy Ind Ltd | Reactor |
-
1986
- 1986-12-22 DE DE19863643856 patent/DE3643856A1/en active Granted
-
1987
- 1987-12-04 ES ES198787117925T patent/ES2029260T3/en not_active Expired - Lifetime
- 1987-12-04 EP EP87117925A patent/EP0273231B1/en not_active Expired - Lifetime
- 1987-12-04 DE DE8787117925T patent/DE3776634D1/en not_active Expired - Fee Related
- 1987-12-04 AT AT87117925T patent/ATE72423T1/en not_active IP Right Cessation
- 1987-12-09 NO NO875137A patent/NO168020C/en unknown
- 1987-12-09 FI FI875417A patent/FI875417A/en not_active Application Discontinuation
- 1987-12-09 DK DK647587A patent/DK166772B1/en not_active IP Right Cessation
- 1987-12-11 ZA ZA879320A patent/ZA879320B/en unknown
- 1987-12-15 CA CA000554318A patent/CA1287480C/en not_active Expired - Fee Related
- 1987-12-16 JP JP62316364A patent/JPS63248431A/en active Pending
- 1987-12-17 AU AU82899/87A patent/AU602744B2/en not_active Ceased
- 1987-12-22 CN CN87108165A patent/CN1013664B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| ES2029260T3 (en) | 1992-08-01 |
| EP0273231A3 (en) | 1988-10-05 |
| EP0273231A2 (en) | 1988-07-06 |
| AU8289987A (en) | 1988-06-23 |
| DK647587A (en) | 1988-06-23 |
| DK647587D0 (en) | 1987-12-09 |
| JPS63248431A (en) | 1988-10-14 |
| AU602744B2 (en) | 1990-10-25 |
| NO875137D0 (en) | 1987-12-09 |
| NO875137L (en) | 1988-06-23 |
| DE3776634D1 (en) | 1992-03-19 |
| ZA879320B (en) | 1988-06-15 |
| CA1287480C (en) | 1991-08-13 |
| CN1013664B (en) | 1991-08-28 |
| EP0273231B1 (en) | 1992-02-05 |
| NO168020C (en) | 1992-01-08 |
| CN87108165A (en) | 1988-08-03 |
| DE3643856C2 (en) | 1989-10-12 |
| DE3643856A1 (en) | 1988-06-30 |
| NO168020B (en) | 1991-09-30 |
| ATE72423T1 (en) | 1992-02-15 |
| FI875417A (en) | 1988-06-23 |
| FI875417A0 (en) | 1987-12-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| DK166772B1 (en) | CONTROL DEVICE SPECIAL FOR AN AMMONIA CONVERTER | |
| DE102004010910B4 (en) | Compact steam reformer | |
| DE554856C (en) | Process for the synthetic production of ammonia | |
| KR102295920B1 (en) | Cylindrical multi-pipe equipment with bypass | |
| JP3003050B2 (en) | Quench cooler | |
| NO157866B (en) | DEVICE FOR THE MANUFACTURING OF BANDS WITH LOCAL CIRCUITS IN A DIVISION. | |
| NO116715B (en) | ||
| DK165404B (en) | AMMONIA REACTOR | |
| US4494484A (en) | Heat exchanger for a process gas | |
| US3622266A (en) | Method and apparatus for reaction heat recovery in catalytic high-pressure synthesis, particularly in ammonia and methanol synthesis | |
| RU2275559C1 (en) | Device for contact heat recovery | |
| JP2514521B2 (en) | Waste heat smoke tube boiler for gas reforming | |
| US3459511A (en) | Exothermic catalytic reaction apparatus | |
| CN111164046B (en) | Novel layout for inter-bed cooling in sulfuric acid plant | |
| US688020A (en) | Apparatus for the manufacture of sulfuric anhydrid. | |
| JPH0421536B2 (en) | ||
| US3363679A (en) | Heat exchangers | |
| US20240240882A1 (en) | Shell-and-tube heat exchanger and method for changing the temperature of a medium | |
| JPH0471574B2 (en) | ||
| JPH08145590A (en) | Temperature regulator for heat exchanger | |
| AT226741B (en) | Process for increasing the waste heat-steam yield in catalytic high-pressure gas syntheses | |
| SU1699593A1 (en) | Multitubular film reactor | |
| PL56425B1 (en) | ||
| DE567329C (en) | Pressure room for carrying out the ammonia synthesis under very high pressures | |
| PL26922B1 (en) | An apparatus for carrying out catalytic reactions and a method for carrying out catalysis in this apparatus. |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| B1 | Patent granted (law 1993) | ||
| PBP | Patent lapsed |