AU602744B2 - Device for the control of an ammonia converter etc. - Google Patents
Device for the control of an ammonia converter etc. Download PDFInfo
- Publication number
- AU602744B2 AU602744B2 AU82899/87A AU8289987A AU602744B2 AU 602744 B2 AU602744 B2 AU 602744B2 AU 82899/87 A AU82899/87 A AU 82899/87A AU 8289987 A AU8289987 A AU 8289987A AU 602744 B2 AU602744 B2 AU 602744B2
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- AU
- Australia
- Prior art keywords
- control
- gas
- heat exchanger
- process gas
- catalyst bed
- 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.)
- Ceased
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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)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Control Of Non-Electrical Variables (AREA)
- Dc-Dc Converters (AREA)
- Sampling And Sample Adjustment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Fats And Perfumes (AREA)
- Exhaust Gas After Treatment (AREA)
- Networks Using Active Elements (AREA)
- Incineration Of Waste (AREA)
- Investigating Or Analysing Materials By Optical Means (AREA)
Abstract
In the converter having a process gas inlet and outlet, at least one heat exchanger and at least one catalyst bed as well as a further gas feed and having a central pipe and a process gas feed to the heat exchanger and/or catalyst bed, the heat exchanger and the first catalyst bed around the latter being arranged rotationally symmetrically to the central pipe, control gas, quench gas, a part of the process gas at a different temperature and/or under other conditions at a point of a reactor is to be added to the particular gas streams in such a way that the mixing-in and/or the by-pass line are designed for complete isolation, partial loading and/or complete opening. For this purpose, the central pipe (14) for temperature control as a control gas feedpipe completely penetrates the heat exchanger (4 and/or 5 and/or 6) and is provided at its lower end with controllable outlets (18) for at least partial mixing of the control gas with the process gas stream, before the latter flows through the catalyst bed (4), and/or for mixing the control gas stream with the process gas stream after the latter has passed through the catalyst bed (4) and the heat exchanger (7). <IMAGE>
Description
I 11 1 11 -1 f lf l I Qj7tHi I
ALLOWED
I 803-P12/AJC:kn/5045.4 602744
AUSTRALIA
PATENTS ACT 1952 COMPLETE SPECIFICATION
(ORIGINAL)
FOR OFFICE USE Application Number: Lodged: Complete Specification Lodged: Accepted: Published: Priority: Related Art: I"his docun-,(i! c tins lc j f ion 49 ci;'d is r.cr I ji-nung.j 6* Co 4 0
S
S
TO BE COMPLETED BY APPLICANT Name of Applicant: Address of Applicant: Actual Inventor: Address for Service: UHDE GMBH Friedrich-Uhde-Str. 15, 4600 Dortmund 1 Federal Republic of Germany Hans-Joachim Herbort Heinz Graeve ARTHUR S. CAVE CO.
Patent Trade Mark Attorneys Goldfields House 1 Alfred Street SYDNEY N.S.W. 2000
AUSTRALIA
Complete Specification for the invention entitled DEVICE FOR THE CONTROL OF AN AMMONIA CONVERTER ETC.
The following statement is a full description of this invention including the best method of performing it known to me:- 1 ASC 49 legalization notrequd. Declared at Dortmund this 04th d of November 19 87 To: HDE GM H The Commissioner of Patents, COMMONWEALTH OF AUSTRALIA ARTHUR S. CAVE CO. gnatu of eclarant) PATENT AND TRADE MARK ATTORNEYS SYDNEY (Meynen) (pa. Dr. Vogel) r 2 "Device for the control of an ammonia converter etc." The invention relates to a device for the control of an ammonia converter etc., with a process gas inlet and a process gas outlet, at least one heat exchanger and at least one catalyst bed, as well as another gas inlet, and a central pipe, as well as a process gas supply line to the heat exchanger or, respectively, catalyst bed, with the heat exchanger placed in a dynamically balanced position with regard to the central pipe, while the first catalyst bed is likewise placed in a dynamically balanced position around the heat exchanger.
As is known, devices for effecting exothermic, catalytic gas reactions for ammonia or methanol synthesis are designed so as to allow, for example, cold feed gas to be fed into the pressure veso. sels, for control purposes, via -a separate gas supply, to join the process gas stream in a channel of that heat exchanger which is alo o located to the first catalyst bed, with two catalyst beds with heat 0 0 0 :2Q exchangers each of the latter being placed concentrically envisaged in the pressure vessel, as in the case in the well-known embodiment. This results from patent No. 33 43 114 of the applicant.
0 According to DE-PS 27 10 247, there is a well-known process, in t which the process gas stream is composed of two part streams, with at least one of the latter being adjustable with regard to temperature and/or quantity in order to achieve the desired process coni, ditions. In every case, the combination of the gas streams is effected prior to entry into the first catalyst bed.
SC tI The well-known control facilities do not allow for the control gas to completely bypass by means of a bypass control device the first catalyst bed and the heat exchanger allocated to it so as to admix it to the gas stream which has already passed through the first catalyst bed and the heat exchanger allocated to the latter.
The aim of the invention is to provide a solution enabling control gas, quench gas or some of the process gas to be fed into the re- RV;- 0 2 2Q7 118 7 .JITNI T -BMm 3 spective gas streams at different temperaturus and/or under various conditions at any place of the reactor. The solution to be adopted is to be designed in such a way as to make it possible for the admixture or, respectively, the bypass pipe to be completely shut or partly opened or, respectivel-y, completely opened.
With a device of the type described above, the invention allows for this aim to be achieved in that, for temperature control purpose, the central pipe, being the control gas feedpipe, runs through the entire length of the heat exchanger and is fitted, at the bottom end, with adjustable outlets to allow at least partial admixture of control gas to the process gas stream before the latter passes through the catalyst bed and/or to allow the admixture of the control gas stream to the process gas stream after the latter has p assed through the catalyst bed and the heat exchanger a o o 09 0 0 With this solution, the central, adjustable pipe makes it, for exo 0 ample, possible for the control gas to be fed, in an extreme posi- S tion, at a right angle through the heat exchanger into the process S 0 gas stream only after the latter has already passed through the first catalyst bed, followed by the heat exchanger, i.e. it can, o for example, be fed into the gas stream which is to charge the fol- 0 lowing catalyst bed.
S 0 c An embodiment of the invention is designed in such a way that the guide pipes for the process gas running through the heat exchanger surround the central, adjustable pipe at a distance from the latter. The advantage of this design consists in the relative simplicity of design both of the heat exchanger and the centrally passing bypass pipe. As a rule, special elbows or similar components can be dispensed with as a result.
A particularly favourable embodiment of the invention also provides for the distribution holes of the central pipe to be synchronously adjustable by way of mutual dependence. This type of control allows not only for some control positions to be attained in that, for example, one outlet of the control pipe is fully closed, while the other is fully opened and vice versa but also for any intermedi- RV??WC'02Q711i7 4 ate position to be adjusted synchronously, be admixed to -existing process gas streams 8i i.e. for control gas to in any partial quantity.
For flow control purposes, it is advisable to fit the central pipe, at the bottom end, with adjustable openings via a piston wi'th axial openings, the former opening into a flow channel for the recycle gas. This type of control facility can be particularly easily effected, although the invention is not restricted to this variant.
Thus the piston, with its axial openings, can either, by way of pushing, partly open or close the lateral openings in the lower part of the central pipe. The same effect can also be achieved by way of rotation, given the appropriate piston design.
5545 0 #9 4
S
ro te 25
S.
S5: t The above embodiment of the invention, which provides for one part of the control facility to be designed as a cylinder, makes it ad-.
visable to design the bottom front end to be fully sealable by means of a sealing element linked to the cylinder, as is likewise envisaged by the invention. It is especially with several catalyst beds, with heat exchangers fitted concentrically inside, that the invention provides for the central pipe and/or the actuator of the adjustable outlets to run through at least one more heat exchanger.
In this context, the above-mentioned once again applies, i.e. the fact that the specific advantage of the invention consists in the simplicity of controlling control gas streams, any situation being precisely controllable owing to the fact that control gas streams can always be employed where they are needed.
c A more specialized embodiment of the invention envisages a control element in the case of a central inflow of cold process gas into the channel of the second heat exchanger, for cooling the vessel shell, from below via a third catalyst bed. This control element allows the admixture of at least part of the colder shell gas to 4 the process gas before the latter enters the third catalyst bed. Inthis way, the colder shell gas cannot only be heated up in the traditional fashion via the second and the first he it exchanger. At the same time, it is possible to use part of the control gas for the third catalyst bed. Vice versa, it is, of course, possible to V r' r 1Z n .1 I r, l- L control, by means of these designs, the quantities of shell gas to be fed into the upper first and second catalyst beds.
Finally, it may be of advantage if a second central pipe runs through the first central pipe, with the former running to below the following heat exchanger and serving to admix control gas to the process gas stream before the latter reaches the third catalyst bed.
At this point, mention must be made of the fact that the stepped arrangement of concentric lines, which make it possible for several control gas streams to be fed simultaneously, is not confined to this type of dual embodiment. Depending on the number of steps, several concentric lines of this type can be envisaged, too.
o e o In the following, the invencion is described in detail with the help of drawings, which show the following: o o S Fig. 1 a cross-sectional view of a device in accordance with the invention, with two catalyst beds and a control facility.
Fig. 2 a cross-sectional view of a different embodiment, with 0 0 three catalyst beds.
00 o3: Fig. 3 a modified embodiment in accordance with the type of aro rangement illustrated in Fig. 2.
S Fig. 4 another embodiment of the invention.
S Fig. 5 a modified embodiment of a control facility in accordance with the type of embodiment shown in Fig. 4.
FPVFHWOO 2Q7 857 6- Device 1 consists chiefly of a pressure vessel 2, w'th the embodiment illustrated in Fig. 1 having two catalyst beds, the embodiments illustrated in Fig. 2-4 having thr.e catalyst beds arranged concentrically around the centre line. The upper and first catalyst bed is marked 4, the second being marked 5, and the lower and last (in embodiments according to Fig. 2-4) being marked 6.
A first heat exchanger 7 is fitted inside the first catalyst bed 4 while a second heat exchanger 8 is fitted inside the second catalyst bed 5 in.embodiments according to Fig. 2-4, with heat exchangers 7 and 8, in the latter case being connected in series as regards their function. The catalysts including the heat exchangers are surrounded by an encasing wall 9, whose dimensions are such as S* to provide for the formation of a continuous annular space 10 be- 1 tween the inner surface of the vessel wall and the encpsing wall 9.
0.
The embodiment illustrated in Fig. 1 provides for a cooling gas to enter device 1 at the top via a nozzle 11, flowing through an annular space 10 and escaping, together with the recycle gas, at the bottom via a nozzle 12. The upper nozzle for the recycle gas is marked 13. A pipe 14 is envisaged to be concentrically fitted ine 0 side the heat exchanger 7 and to be filled with gas for control 0 purposes via an intake nozzle *4 This central pipe joins a distribution chamber 16 for the process gas which has already passed through the first catalyst bed 4 on the inside and through the heat exchanger 7 on the outside.
4 4 iThe invention provides for another distribution chamber 17 to be '4 fitted below the first heat exchanger 14 and separated gas-tight from the distribution chamber 16, into which the process gas flows after passing through the guide tubes 30 of the heat exchanger 7, in order to be channelled from there to the catalyst bed 4. In this area, the central pipe 14 has openings 18, through which at least some of the control gas passing through the control pipe 14 can flow into the distribution chamber 17. By means of a control rod 19, which is fitted with the stop piston 20 with axial openings RVFHWO02Q71187 7 in the area of the slots 18 and with a stop plug 21 at the bottom free end, the control gas can be adjusted and part streams can be distributed on a percentage basis to the distribution chambers 16 and 17.
The mode of operation is as follows: If, for example, the control rod 19 is raised as shown by the double arrow 22, the plug 21 shuts off the bottcm free end of the central pipe 14, while the slots 18 are fully opened. The control gas now flows entirely through the slots 18 into the space 17, i.e. it mixes with the process gas stream before the latter passes through the catalyst bed 4.
a If the control rod (19) is moved down, the stop plug 21 will open S the bottom opening to the extent that the slots 18 are being S.C'2 opened, so that the latter are fully closed in the bottom dead cent tre position, while the bottom opening of the central pipe 14 is ,t fully open at the distribution chamber 16, so that the entire control gas stream is fed into it as a bypass mixing with the process gas stream which has passed through the first catalyst bed on the i inside and through the heat exchanger 7 on the outside.
Functionally identical parts of the following embodiments are marked with the same reference number, supplemented by lower-case S letters.
SThe embodiment shown in Fig. 2 has the same basic arrangement, the only variation being that the process gas is centrally fed from above as a part stream via a pipe nozzle 13a, another part being fed via a pipe nozzle lla as a cooling shell gas which passes, via a riser 23, the centre of the third catalyst bed 6a from below, in order to flow first through the second heat exchanger 8 and then through the mixing chamber 17a. Here again, the control gas is distributed in the same way as in the embodiment illustrated by Fig. 1.
RVPHW002Q711307 8 The embodiment illustrated by Fig. 3 is similar, although, in this case, the recycle gas is fed, in three part streams, through one upper feed nozzle 1Ib, one upper first shell gas feed nozzle 11b, as well as, additionally, one lower shell gas feed nozzle 24. In this embodiment, the shell gas streams fed from above and below are collected by means of radial headers 25 below the second heat exchanger 8b in a joint channel 26 and subsequently channelled upwards. In this embodiment, too, the admixture of control gas is effected in the same way.
A modified version of the control device, as illustrated by Fig. 4 consists in that the control rod 19c runs through the entire length of the first heat exchanger 7c and the second heat exchanger 8c, adjusting the supply of the shell gas, which is fed from below via the central supply line 23c, to the channel 26c of the second heat exchanger Sc.-Here, for exapmle, a hollow-cylinder sealing element is envisaged, bearing reference number 27. If it is lifted, it will S enable at least one part stream to escape laterally and to mix with S the process gas direct which will subsequently charge the lower and S* third catalyst bed 6c. If the control rod is moved downwards, the hollow cylinder 27 will only allow the shell gas to pass through in an unward direction, no admixing being possible in this case.
S Finally, Fig. 5 illustrates a possibility of feeding in several control gas streams. In this drawing, it is merely the principle of the control facility which is illustrated. The central pipe, marked S 14d, contains another central pipe 28 to the extent that the latter c ends in the area of the first channel 26d of the second heat exchanger 8d. This embodiment envisages radial distribution lines 29, ttm-.t c to Ths S which make it possible for control gas to be admixed to the gas stream escaping from the second heat exchanger Sd in order to be channelled to the third catalyst bed 6d.
The above embodiments of the invention can, of course, be modified in many respects without affecting the basic idea. Thus flow adjustment for each channel may be designed with piston/cylinder ele- S ments etc. in the embodiment illustrated by Fig. 5, for example, in conjunction with the central pipes 28 and 14d.
RVHWCO2Q7 13 87
Claims (9)
1. A device for the control of an ammonia converter, or the like, compcising: a pressure vessel having a process gas inlet at a first end thereof, a process gas outlet at a second end thereof, and having an encased chamber intermediate said process gas inlet and outlet; a heat exchanger, provided about a longitudinal control gas pipe, and, having a first catalyst bed therearound within 0 '00:0 said encased chamber, said heat exchanger being connected to a 00 o* further process gas inlet for the supply of recycled process S* gas; oo o a said control gas pipe being connected at a first end thereof to a control gas inlet and being optionally connected at a second end thereof to at least one of a pair of 0000 oo distribution chambers, said optional connection being achieved ooo oo o by means of movement of a control rod; said control rod having a stop plug provided on the extremety thereof and having a stop piston provided in spaced a relationship from said stop plug, such that, when said control o ao rod is in a first position, said control gas is permitted to a flow into a first distribution chamber to said catalyst bed, when said control rod is in a second position, said control gas is permitted to flow into a second distribution chamber connected to said process gas outlet, and, when said control rod is in an intermediate position the proportion of control gas flowing into each of said first and second distribution chambers is controlled. -9-
2. The device as claimed in claim i, wherein guide tubes for the process gas are provided, the guide tubes extending through the heat exchanger being arranged to surround and be spaced from the central pipe.
3. The device as claimed in claims 1 or 2, wherein the adjustable outlets and the discharge outlet of the central pipe are synchronously adjustable and being mutually dependent.
4. The device as claimed in any one of the preceding claims, wherein, in order to control throughput, the central pipe is provided, adjacent its bottom end, with openings closable via a S piston having axial openings, the closable openings S communicating with a flow channel for the recycle gas. 0000
5. The device as claimed in claim 4, wherein the discharge outlet at the bottom front end of the central pipe is adapted to be completely sealable by means of a sealing element linked o to the piston. *440 00
6. The device as claimed in any one of the preceding claims, comprising more than two catalyst beds, and at least two heat exchangers, at least one of the central pipe and the actuator for the adjustable outlets and for the discharge outlet ,j extending through at least one more heat exchanger.
7. The device as claimed in claim 6, wherein cold process gas enters a third catalyst bed centrally from below after having cooled the vessel shell, and is fed into a chamber of the second heat exchanger, a control facility being £rovided to allow at least partial admixture of the colder shell gas with the process gas before the process gas enters the third catalyst bed. -A -,AMD/0212a 10
8. The device as claimed in any one of the preceding claims, in which a second central pipe extends through the first central pipe the second central pipe continuing to below the second heat exchanger in order to allow the admixture of control gas with the process gas stream before the process gas reaches the third catalyst bed.
9. A device for the control of an ammonia converter, substantially as herein described with reference to the accompanying drawings. t I t f rf DATED this 18th day of July, 1990. UHDE GMBH By Its Patent Attorneys St* ARTHUR S. CAVE CO. 9 t f 4 444 44 4 i *O 11
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 (2)
| Publication Number | Publication Date |
|---|---|
| AU8289987A AU8289987A (en) | 1988-06-23 |
| AU602744B2 true AU602744B2 (en) | 1990-10-25 |
Family
ID=6316843
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU82899/87A Ceased AU602744B2 (en) | 1986-12-22 | 1987-12-17 | Device for the control of an ammonia converter etc. |
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 |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU518643B2 (en) * | 1976-11-15 | 1981-10-15 | Ici Ltd. | Exothermic catalytic process |
| GB2152405A (en) * | 1983-11-29 | 1985-08-07 | Uhde Gmbh | Device for performing exothermic catalytic gas reactions for synthesis under pressure |
| AU581221B2 (en) * | 1984-04-23 | 1989-02-16 | Mitsubishi Gas Chemical Company, Inc. | Reaction vessel |
Family Cites Families (5)
| 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 |
| 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 |
-
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
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU518643B2 (en) * | 1976-11-15 | 1981-10-15 | Ici Ltd. | Exothermic catalytic process |
| GB2152405A (en) * | 1983-11-29 | 1985-08-07 | Uhde Gmbh | Device for performing exothermic catalytic gas reactions for synthesis under pressure |
| AU581221B2 (en) * | 1984-04-23 | 1989-02-16 | Mitsubishi Gas Chemical Company, Inc. | Reaction vessel |
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 |
| 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 |
| DK166772B1 (en) | 1993-07-12 |
| 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 |
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