CA1287480C - Device for the control of an ammonia converter etc. - Google Patents
Device for the control of an ammonia converter etc.Info
- Publication number
- CA1287480C CA1287480C CA000554318A CA554318A CA1287480C CA 1287480 C CA1287480 C CA 1287480C CA 000554318 A CA000554318 A CA 000554318A CA 554318 A CA554318 A CA 554318A CA 1287480 C CA1287480 C CA 1287480C
- Authority
- CA
- Canada
- Prior art keywords
- heat exchanger
- catalyst bed
- gas
- control
- process gas
- 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.)
- Expired - Fee Related
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)
- 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)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Sampling And Sample Adjustment (AREA)
- Fats And Perfumes (AREA)
- Exhaust Gas After Treatment (AREA)
- Investigating Or Analysing Materials By Optical Means (AREA)
- Networks Using Active Elements (AREA)
- Incineration Of Waste (AREA)
Abstract
A b s t r a c t :
"Device for the control of an ammonia converter etc,"
By means of a device for controlling an ammonia converter etc., with process gas inlet and outlet, at least one heat exchanger and at least one catalyst bed as well as another gas supply line and a central pipe as well as a process gas supply line to the heat ex-changer or, respectively, the catalyst bed, with the heat exchanger placed in a dynamically balanced position with regard to the cen-tral pipe, while the catalyst bed is likewise placed in a dynam-ically balanced position around the heat exchanger, a solution is to be provided which allows the feeding into the respective gas streams of control gas, quench gas and part of the process gas at various temperatures and/or under various conditions at any place of a reactor, the solution to be adopted being such that the admix-ture or, respectively, the bypass line can be fully shut off or partly opened or, respectively, fully opened.
The solution is effected in that, for temperature control purposes, the central pipe (14), being the control gas feedpipe, runs through the entire length of the heat exchanger (a or, respectively, 5 or, respectively, 6) and is fitted, at the latter's bottom end, with adjustable outlets (18) to allow at least partial admixture of con-trol gas to the process gas stream before the latter passes through the catalyst bed (4), or, respectively, to allow admixture of the control gas stream to the process gas stream after the latter has passed through the catalyst bed (4) and the heat exchanger (7).
"Device for the control of an ammonia converter etc,"
By means of a device for controlling an ammonia converter etc., with process gas inlet and outlet, at least one heat exchanger and at least one catalyst bed as well as another gas supply line and a central pipe as well as a process gas supply line to the heat ex-changer or, respectively, the catalyst bed, with the heat exchanger placed in a dynamically balanced position with regard to the cen-tral pipe, while the catalyst bed is likewise placed in a dynam-ically balanced position around the heat exchanger, a solution is to be provided which allows the feeding into the respective gas streams of control gas, quench gas and part of the process gas at various temperatures and/or under various conditions at any place of a reactor, the solution to be adopted being such that the admix-ture or, respectively, the bypass line can be fully shut off or partly opened or, respectively, fully opened.
The solution is effected in that, for temperature control purposes, the central pipe (14), being the control gas feedpipe, runs through the entire length of the heat exchanger (a or, respectively, 5 or, respectively, 6) and is fitted, at the latter's bottom end, with adjustable outlets (18) to allow at least partial admixture of con-trol gas to the process gas stream before the latter passes through the catalyst bed (4), or, respectively, to allow admixture of the control gas stream to the process gas stream after the latter has passed through the catalyst bed (4) and the heat exchanger (7).
Description
o 3 ~7~6-11 The inventlon relates to a device for the control o~ ~n ammonia converter etc., with a process gas lnlet and a pro~ess ya~
outlet, at least one heat exehanger and at lea~t on~ cataly3t b~
as well as another gas inlet, and a central pipe, as well a~ a process ya,s supply line to the heat excllanger or, re~pectively, catalyst bed, Wit}l the heat exchan~er placed in a clynamlc~l]-y balanced posltion wlt,h ~egarc1 ~,o the cent,ra:L pipe, whl~e the ~
catalyst hed 1~ llkewise placed ln a clynamlcally halanced positlon around the best exchanger.
As is known, devlces 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 vessels, for control purposes, via a separate gas supply, to join the process gas stream in a channel of that heat exchanger whlch is allocated to the first catalyst bed, with two catalyst beds with heat exchangers - each of the latter being placed concentrically - envisaged in the pressure vessel, as in the case in the well-known embodiment. This result ~rom German patent No.
33 43 114 of the applicant.
According to German patent No. 27 10 247 there is a well-known process, in which the process gas stream is composed of two part streams, with at least one of the lat~er being acliustable with regard to temperature and/or quantity in order to achieve the desired process conditions. In every case, the combination of the gas streams is effective prior to entry into the first catalyst bed.
These known control facilities do not allow for the control gas to completely bypass - by means of a bypass contxol C ' `~
clevice - the first catalyst bed and the heat exchanyer allocatet~
to i~ so as to admix with the gas stream whlch has alread~J pa~secl through the first catalys-t bed and the as50cia~ed heat; ex~hanyer.
The aim o~ the inventlon ls to provide a ~olution enabling control gas~ quench gas or some of the process ga,~ to be ~ed into the re~pe~tive ~a~ str~am ~t dl~ferent temper~ture~
and/or under variou~ condltlons at any place :Ln th~ reac~or. Th0 solution to be adopt~d i~ to be deslgned in suc~h a way as to make it possible for the admixture or, the bypass pipe to be completely shut or partly opened or, completely opened as desired.
The invention provides device for the control of an ammonia converter or the like havincJ a process gas inlet, an outlet, at least one heat exchanger, at least one catalyst bed, another gas supply line and a cen~ral pipe, a process gas supply line to the heat exchanger, tha ca~alyst bed, said heat exchanger being heated in a dynamically balanced position with regard to the central pipe, while the catalyst bed is likewise located in a dynamically balanced position around the heat exchanger, characterized in that, for temperature control purpose, the control gas feedpipe is a central pipe extencling through the whole length of the heat exchanger (4, 5 or 6) and being fitted, at the bottom end thereof with adjustable outlets (18) to allow at least partial admixture of control gas with the process gas stream before the latter passes through the catalyst bed (4), ancl~or to permit admixture of the control gas stream with the process gas stream after the latter has passed through the catalys~ bed (~) and the heat exchanger (7).
With the solution, the central, adjustable pipe makes it .,.~' 12l3~7~8~
4a 2704 possible, for example, for the control gas to be fed, in an extreme posltion, at rlght angles ~hrough the heat ex~hanger into the process gas stream only after the latt~r has already pa%sed through the first catalyst becl, fo1lowed by the heat exch~n~er, i.e. it can, for e~ample, be fed into ~he CJaS stream wh:Lch 1~ ~fJ
char51e th~ followincJ ~c~aly~l, becl, An embodlment of the lnventlon is desi~ned in ~!uch a wa~y that the guide pip2S for the process gas runniny through the heat exchanger surround the central, adjustable pipe at a distance from the latter. The advantage of this is the relative simplicity of desiqn both of the heat exchanger and the centrally extending 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 interdependently. 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-i~f --` ~Z87~30 ate position to be adjusted synchronously, i.e. for con~rol gas to be admixed to existing process gas streams 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 with axial o~enings, the former opening into a flow channel 'or he recycle gas. This type of control facility can be particularl~l easily ef-fected, although the invention is not restricted to this variant Thus the piston, with its aY~ial openings, can either, by way of pushing, partly open or close the lateral openings in tne lower part of the central pipe. The same effect can also be achieved by way of rotation, given the appropriate piston design.
The above embodiment of the invention, which provides ~or one part of the control facility to be designed as a cylinde-~ makes it ai-visable to design the bottom front end to be fully sealable by means of a sealing element lin~ed to the cylinder, as is likewise envisaged by the invention. It is especially with several catalyst beds, with heat exchangers fitted concentrically insiàe, 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 invent~on consists in the simplici'y o' controlling con'rol gas streams, any situation being precisely controllable owing to the fact that control gas streams can always be employed ~here they are needed.
A more specialized embodiment of the invention envisages a control element in the case of a cen~ra.l infiow of cold process gas into the channel of ~he second heat e.~:chan~er, ~or cooling the vessel shell, from below via a third catal st bed. This control element allows the admixture o. at least par~ of the colder shell gas to the process qas before the latter en.ers the third catalyst bed. In this way, the colder shell gas cannot only be heated up in the tra-ditional fashion via the second and the first heat exchanger. .~t the same time, it is possible to use part o~ the control gas for the third catalys~ bed. Vice versa, it is, o~ cou-se, possible to r ,;YC5_ "~7 ~
.
~` lZ87~80 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 cont-ol gas streams to be fed simultaneously, is not confined ~o t~.is type of dual embodiment. Depending on ~he number of steps, se-veral concentric lines of this type can be envisaged, too.
- In the following, the invention is desoribed in detail with the help of drawings, which show the following:
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 three catalyst beds.
Fig. 3 a modified embodiment in accordance with the type of ar-rangement illustraled in Fig. 2.
Fig. 4 another embodiment of the invention~
Fig. S a modified embodiment of a control facility in accordance with the type of embodiment shown in Fig. a .~V~ oC~ 1&, , . ~ - 7 -, ~Z8'7480 Device 1 consists chiefly of a pressure vessel 2, with the embod-lment illustrated in Fig. 1 having two catalyst beds, t~e embod-iments illustrated in Fig. 2-4 having three catalyst beds arranged concentrically around the cen~re line. The upper and first catalyst bed is marked 4, the second belng marked 5, and ~he 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 cata-lyst bed 5 in embodiments according to Fig. 2-~, with heat exchang-ers 7 and 8, in the latter case being connected in series as r~
gards their function. The catalysts including the heat exchangers are surrounded by an encasing wall 9, whose ~imensions are such as to provide for the for~ation of a continuous annular space 10 be-tween the inner surface of the vessel wali and the encasing wall 9.
The e~bodiment illustrated in Fig. 1 provides for a cooling gas to enter device 1 at the top via a noz~le 11, 10wing through an annu-lar 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 in-side the heat exchanger 7 and to be filled with gas for control purposes via an intake nozzle 15.
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.
The invention provi~les for another distribution chamber 17 to be fi~ted below the first heat e~:changer 14 and separated gas-tight from the distribution chamber 16, into which the ~rocess 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 'he control pipe 14 can flow into the distri~ution cnamber 17. By means of a contro.l rod 19, whicn is r-it.ed with the s~op piston ^û with axiai openin~s R~?:~002Q7;i~7 -.~ ~
Z87~80 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 dis~ributed on a percentage basis to the distribution chambers 16 and 17.
The mode of operation is as follows:
If, for example, the control rod 15 is raised as shown by the dou-ble arrow 22, the plug 21 shuts off the bottom free end OI the cen-tral pipe 1~, 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 la'ter ?asses through the catalyst bed 4.
If th^ control rod (19) ls moved down, the stop plug 21 will open '_he bottom o~ening-to-the--extent that the slots 18 are being --opened, so that the latter are fully closed in the bottom dead cen-tre oosition, while the bottom onening of the central ~ioe 14 is fully open at the dist~ibution chamber 16, so that the entire con-trol 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 inside and th~ough the heat exchanger 7 on the outside.
Functionally identical Darts of the following embodiments are marked with the same reference number, supplemented by lo~er-case letters.
The embodiment shown in Fig. 2 has the sa~e basic arrangement, the only variation being that the process gas is centrally feà from above as a Dart stream -~ia a pipe nozzle 13a, another ~ar~ 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 low first through the second heat exchanger ~ and then through the miY~ing chamber 17a. Here again, the control gas is dis-tributed in the same way as in the embodiment iilustrated by Flg. 1.
RV~?~002Q71137 ',-..,: ,.. ..
~- 1287480 The embodimen1 illustrated by Fig. 3 is similar, although, in this case, the recycle gas is fed, in three part streams, through one upper feed no~zl~ 13b, one upper first shell gas fe~d no~zle llb, as well as, additionally, one lower shell gas feed nozzle 24. In this embodiment, the shell ga$ streams ed from above and below are collected by m~ans of radial headers 25 below the second heat 9X-changer 8b in a joint channel 26 and subsequently channelled up-wards. In this embodiment, too, the admi~ture OI control gas is ef-fected ln the same way.
A modified version of the control device, as illustrated ~y Fig. 4 consists in that the control rod l9c runs th-ough the entire l--ngth of the iirst heat excnanger 7c and the second heat exchanger 8c, adjusting the supply of the shell gas, which is fed from below via the central supply lins 23c, to the channel 26c of the second heat exchan~er 8c. Here, for e~apmle, a hol-lo~ cylinder sealing element is envisaged, bearing reference number 27. If it is lifted, it will enable at least one part stream to escape laterally and to mi~ ~ith the process gas direct which will subseauently cha~ge the lowe- and 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 u~ward clirection, no admixing being possible in this case.
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 w`nich is illustrated. The central pipe, marked l~d, contains another central pipe 28 to the extent that the latter ends in the area of the first channel 25d of ~he second heat ex-changer 8d. This embodiment envisages radiai distribuiion lines 29, which ma~.e it possible ~or control gas to be admi~ed .to ~he gas stream escaping rom the second heat e~changer 8d in order to be channelied to the third catalyst bed 6d.
The above embodiments of the invenrion can, of course, be modified in many respects without afîecting the basic idea. Thus flow ad-justment for each channel ~ay be designed witn piston/cylir.der ele-ments etc. - in the e~odimenl illustrated by ~g. 5, ~or e~ample, in conjunc.ion with ~he cen{.ral pipes 20 and i4d.
r~'i? - ~ , C ~ /; l ô, ~. ,. . . ~
outlet, at least one heat exehanger and at lea~t on~ cataly3t b~
as well as another gas inlet, and a central pipe, as well a~ a process ya,s supply line to the heat excllanger or, re~pectively, catalyst bed, Wit}l the heat exchan~er placed in a clynamlc~l]-y balanced posltion wlt,h ~egarc1 ~,o the cent,ra:L pipe, whl~e the ~
catalyst hed 1~ llkewise placed ln a clynamlcally halanced positlon around the best exchanger.
As is known, devlces 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 vessels, for control purposes, via a separate gas supply, to join the process gas stream in a channel of that heat exchanger whlch is allocated to the first catalyst bed, with two catalyst beds with heat exchangers - each of the latter being placed concentrically - envisaged in the pressure vessel, as in the case in the well-known embodiment. This result ~rom German patent No.
33 43 114 of the applicant.
According to German patent No. 27 10 247 there is a well-known process, in which the process gas stream is composed of two part streams, with at least one of the lat~er being acliustable with regard to temperature and/or quantity in order to achieve the desired process conditions. In every case, the combination of the gas streams is effective prior to entry into the first catalyst bed.
These known control facilities do not allow for the control gas to completely bypass - by means of a bypass contxol C ' `~
clevice - the first catalyst bed and the heat exchanyer allocatet~
to i~ so as to admix with the gas stream whlch has alread~J pa~secl through the first catalys-t bed and the as50cia~ed heat; ex~hanyer.
The aim o~ the inventlon ls to provide a ~olution enabling control gas~ quench gas or some of the process ga,~ to be ~ed into the re~pe~tive ~a~ str~am ~t dl~ferent temper~ture~
and/or under variou~ condltlons at any place :Ln th~ reac~or. Th0 solution to be adopt~d i~ to be deslgned in suc~h a way as to make it possible for the admixture or, the bypass pipe to be completely shut or partly opened or, completely opened as desired.
The invention provides device for the control of an ammonia converter or the like havincJ a process gas inlet, an outlet, at least one heat exchanger, at least one catalyst bed, another gas supply line and a cen~ral pipe, a process gas supply line to the heat exchanger, tha ca~alyst bed, said heat exchanger being heated in a dynamically balanced position with regard to the central pipe, while the catalyst bed is likewise located in a dynamically balanced position around the heat exchanger, characterized in that, for temperature control purpose, the control gas feedpipe is a central pipe extencling through the whole length of the heat exchanger (4, 5 or 6) and being fitted, at the bottom end thereof with adjustable outlets (18) to allow at least partial admixture of control gas with the process gas stream before the latter passes through the catalyst bed (4), ancl~or to permit admixture of the control gas stream with the process gas stream after the latter has passed through the catalys~ bed (~) and the heat exchanger (7).
With the solution, the central, adjustable pipe makes it .,.~' 12l3~7~8~
4a 2704 possible, for example, for the control gas to be fed, in an extreme posltion, at rlght angles ~hrough the heat ex~hanger into the process gas stream only after the latt~r has already pa%sed through the first catalyst becl, fo1lowed by the heat exch~n~er, i.e. it can, for e~ample, be fed into ~he CJaS stream wh:Lch 1~ ~fJ
char51e th~ followincJ ~c~aly~l, becl, An embodlment of the lnventlon is desi~ned in ~!uch a wa~y that the guide pip2S for the process gas runniny through the heat exchanger surround the central, adjustable pipe at a distance from the latter. The advantage of this is the relative simplicity of desiqn both of the heat exchanger and the centrally extending 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 interdependently. 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-i~f --` ~Z87~30 ate position to be adjusted synchronously, i.e. for con~rol gas to be admixed to existing process gas streams 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 with axial o~enings, the former opening into a flow channel 'or he recycle gas. This type of control facility can be particularl~l easily ef-fected, although the invention is not restricted to this variant Thus the piston, with its aY~ial openings, can either, by way of pushing, partly open or close the lateral openings in tne lower part of the central pipe. The same effect can also be achieved by way of rotation, given the appropriate piston design.
The above embodiment of the invention, which provides ~or one part of the control facility to be designed as a cylinde-~ makes it ai-visable to design the bottom front end to be fully sealable by means of a sealing element lin~ed to the cylinder, as is likewise envisaged by the invention. It is especially with several catalyst beds, with heat exchangers fitted concentrically insiàe, 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 invent~on consists in the simplici'y o' controlling con'rol gas streams, any situation being precisely controllable owing to the fact that control gas streams can always be employed ~here they are needed.
A more specialized embodiment of the invention envisages a control element in the case of a cen~ra.l infiow of cold process gas into the channel of ~he second heat e.~:chan~er, ~or cooling the vessel shell, from below via a third catal st bed. This control element allows the admixture o. at least par~ of the colder shell gas to the process qas before the latter en.ers the third catalyst bed. In this way, the colder shell gas cannot only be heated up in the tra-ditional fashion via the second and the first heat exchanger. .~t the same time, it is possible to use part o~ the control gas for the third catalys~ bed. Vice versa, it is, o~ cou-se, possible to r ,;YC5_ "~7 ~
.
~` lZ87~80 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 cont-ol gas streams to be fed simultaneously, is not confined ~o t~.is type of dual embodiment. Depending on ~he number of steps, se-veral concentric lines of this type can be envisaged, too.
- In the following, the invention is desoribed in detail with the help of drawings, which show the following:
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 three catalyst beds.
Fig. 3 a modified embodiment in accordance with the type of ar-rangement illustraled in Fig. 2.
Fig. 4 another embodiment of the invention~
Fig. S a modified embodiment of a control facility in accordance with the type of embodiment shown in Fig. a .~V~ oC~ 1&, , . ~ - 7 -, ~Z8'7480 Device 1 consists chiefly of a pressure vessel 2, with the embod-lment illustrated in Fig. 1 having two catalyst beds, t~e embod-iments illustrated in Fig. 2-4 having three catalyst beds arranged concentrically around the cen~re line. The upper and first catalyst bed is marked 4, the second belng marked 5, and ~he 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 cata-lyst bed 5 in embodiments according to Fig. 2-~, with heat exchang-ers 7 and 8, in the latter case being connected in series as r~
gards their function. The catalysts including the heat exchangers are surrounded by an encasing wall 9, whose ~imensions are such as to provide for the for~ation of a continuous annular space 10 be-tween the inner surface of the vessel wali and the encasing wall 9.
The e~bodiment illustrated in Fig. 1 provides for a cooling gas to enter device 1 at the top via a noz~le 11, 10wing through an annu-lar 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 in-side the heat exchanger 7 and to be filled with gas for control purposes via an intake nozzle 15.
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.
The invention provi~les for another distribution chamber 17 to be fi~ted below the first heat e~:changer 14 and separated gas-tight from the distribution chamber 16, into which the ~rocess 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 'he control pipe 14 can flow into the distri~ution cnamber 17. By means of a contro.l rod 19, whicn is r-it.ed with the s~op piston ^û with axiai openin~s R~?:~002Q7;i~7 -.~ ~
Z87~80 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 dis~ributed on a percentage basis to the distribution chambers 16 and 17.
The mode of operation is as follows:
If, for example, the control rod 15 is raised as shown by the dou-ble arrow 22, the plug 21 shuts off the bottom free end OI the cen-tral pipe 1~, 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 la'ter ?asses through the catalyst bed 4.
If th^ control rod (19) ls moved down, the stop plug 21 will open '_he bottom o~ening-to-the--extent that the slots 18 are being --opened, so that the latter are fully closed in the bottom dead cen-tre oosition, while the bottom onening of the central ~ioe 14 is fully open at the dist~ibution chamber 16, so that the entire con-trol 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 inside and th~ough the heat exchanger 7 on the outside.
Functionally identical Darts of the following embodiments are marked with the same reference number, supplemented by lo~er-case letters.
The embodiment shown in Fig. 2 has the sa~e basic arrangement, the only variation being that the process gas is centrally feà from above as a Dart stream -~ia a pipe nozzle 13a, another ~ar~ 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 low first through the second heat exchanger ~ and then through the miY~ing chamber 17a. Here again, the control gas is dis-tributed in the same way as in the embodiment iilustrated by Flg. 1.
RV~?~002Q71137 ',-..,: ,.. ..
~- 1287480 The embodimen1 illustrated by Fig. 3 is similar, although, in this case, the recycle gas is fed, in three part streams, through one upper feed no~zl~ 13b, one upper first shell gas fe~d no~zle llb, as well as, additionally, one lower shell gas feed nozzle 24. In this embodiment, the shell ga$ streams ed from above and below are collected by m~ans of radial headers 25 below the second heat 9X-changer 8b in a joint channel 26 and subsequently channelled up-wards. In this embodiment, too, the admi~ture OI control gas is ef-fected ln the same way.
A modified version of the control device, as illustrated ~y Fig. 4 consists in that the control rod l9c runs th-ough the entire l--ngth of the iirst heat excnanger 7c and the second heat exchanger 8c, adjusting the supply of the shell gas, which is fed from below via the central supply lins 23c, to the channel 26c of the second heat exchan~er 8c. Here, for e~apmle, a hol-lo~ cylinder sealing element is envisaged, bearing reference number 27. If it is lifted, it will enable at least one part stream to escape laterally and to mi~ ~ith the process gas direct which will subseauently cha~ge the lowe- and 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 u~ward clirection, no admixing being possible in this case.
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 w`nich is illustrated. The central pipe, marked l~d, contains another central pipe 28 to the extent that the latter ends in the area of the first channel 25d of ~he second heat ex-changer 8d. This embodiment envisages radiai distribuiion lines 29, which ma~.e it possible ~or control gas to be admi~ed .to ~he gas stream escaping rom the second heat e~changer 8d in order to be channelied to the third catalyst bed 6d.
The above embodiments of the invenrion can, of course, be modified in many respects without afîecting the basic idea. Thus flow ad-justment for each channel ~ay be designed witn piston/cylir.der ele-ments etc. - in the e~odimenl illustrated by ~g. 5, ~or e~ample, in conjunc.ion with ~he cen{.ral pipes 20 and i4d.
r~'i? - ~ , C ~ /; l ô, ~. ,. . . ~
Claims (8)
1. Device for the control of an ammonia converter or the like having a process gas inlet, an outlet, at least one heat exchanger, at least one catalyst bed, another gas supply line and a central pipe, a process gas supply line to the heat exchanger, the catalyst bed, said heat exchanger being heated in a dynamically balanced position with regard to the central pipe, while the catalyst bed is likewise located in a dynamically balanced position around the heat exchanger, characterized in that, for temperature control purpose, the control gas feedpipe is a central pipe extending through the whole length of the heat exchanger and being fitted, at the bottom end thereof with adjustable outlets to allow at least partial admixture of control gas with the process gas stream before the latter passes through the catalyst bed, and/or to permit admixture of the control gas stream with the process gas stream after the latter has passed through the catalyst bed and the heat exchanger.
2. Device according to claim 1, characterized in that guide pipes for the process gas extend through the heat exchanger surround the central pipe at a distance from the latter.
3. Device according to claim 1 or 2, characterized in that the central pipe has distribution outlets that are devised in such a manner as to be synchronously adjustable interdependently.
4. Device according to claim 1 or 2 characterized in that, in order to control throughput, the adjustable outlets of said central pipe are closable via a piston having axial openings, the closable openings joining a flow channel for the recycle gas.
5. Device according to claim 4, characterized in that the bottom end of said central pipe is devised to be completely sealable by way of a sealing element linked to the piston.
6. Device according to any one of claims 1, 2 or 5, characterized in that, with more than two catalyst beds having heat exchangers, the central pipe and/or the actuator of the adjustable outlets run through at least one more heat exchanger.
7. Device according to claim 6, characterized in that, cold process gas used to cool the vessel shell, enters from the bottom end via a third catalyst bed into a channel of the second heat exchanger, there being a control facility allowing at least partial admixture of the colder shell gas with the process gas before the latter enters the third catalyst bed.
8. Device according to claim 6, characterized in that, a second central pipe runs through the first central pipe, with the former continuing to below the following heat exchanger in order to allow the admixture of control gas with the process gas stream before the latter reaches the third catalyst bed.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3643856.1 | 1986-12-22 | ||
| DE19863643856 DE3643856A1 (en) | 1986-12-22 | 1986-12-22 | DEVICE FOR REGULATING, IN PARTICULAR, AN AMMONIA CONVERTER |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1287480C true CA1287480C (en) | 1991-08-13 |
Family
ID=6316843
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000554318A Expired - Fee Related CA1287480C (en) | 1986-12-22 | 1987-12-15 | 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 |
| JPH06500764A (en) * | 1990-09-24 | 1994-01-27 | シー・エフ・ブラウン・インコーポレイテッド | 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 |
| BR112013028447A2 (en) * | 2011-06-16 | 2018-06-19 | Haldor Topsoe As | method for performing exothermic catalytic reactions and 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 EP EP87117925A patent/EP0273231B1/en not_active Expired - Lifetime
- 1987-12-04 AT AT87117925T patent/ATE72423T1/en not_active IP Right Cessation
- 1987-12-04 ES ES198787117925T patent/ES2029260T3/en not_active Expired - Lifetime
- 1987-12-04 DE DE8787117925T patent/DE3776634D1/en not_active Expired - Fee Related
- 1987-12-09 NO NO875137A patent/NO168020C/en unknown
- 1987-12-09 DK DK647587A patent/DK166772B1/en not_active IP Right Cessation
- 1987-12-09 FI FI875417A patent/FI875417A/en not_active Application Discontinuation
- 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 |
|---|---|
| CN87108165A (en) | 1988-08-03 |
| EP0273231A2 (en) | 1988-07-06 |
| EP0273231A3 (en) | 1988-10-05 |
| EP0273231B1 (en) | 1992-02-05 |
| JPS63248431A (en) | 1988-10-14 |
| ZA879320B (en) | 1988-06-15 |
| FI875417A0 (en) | 1987-12-09 |
| ATE72423T1 (en) | 1992-02-15 |
| DE3643856A1 (en) | 1988-06-30 |
| DE3776634D1 (en) | 1992-03-19 |
| DK166772B1 (en) | 1993-07-12 |
| NO168020C (en) | 1992-01-08 |
| DK647587A (en) | 1988-06-23 |
| AU8289987A (en) | 1988-06-23 |
| DK647587D0 (en) | 1987-12-09 |
| NO875137L (en) | 1988-06-23 |
| FI875417A (en) | 1988-06-23 |
| ES2029260T3 (en) | 1992-08-01 |
| NO168020B (en) | 1991-09-30 |
| DE3643856C2 (en) | 1989-10-12 |
| AU602744B2 (en) | 1990-10-25 |
| NO875137D0 (en) | 1987-12-09 |
| CN1013664B (en) | 1991-08-28 |
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| Date | Code | Title | Description |
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| MKLA | Lapsed |