CA1251019A - Synthesis converter - Google Patents
Synthesis converterInfo
- Publication number
- CA1251019A CA1251019A CA000491634A CA491634A CA1251019A CA 1251019 A CA1251019 A CA 1251019A CA 000491634 A CA000491634 A CA 000491634A CA 491634 A CA491634 A CA 491634A CA 1251019 A CA1251019 A CA 1251019A
- Authority
- CA
- Canada
- Prior art keywords
- pressure vessel
- curved head
- gas
- converter
- inlet
- 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
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0476—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds
- B01J8/0488—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds the beds being placed in separate 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
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0476—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise shaped beds
- B01J8/048—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more otherwise 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
- B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00027—Process aspects
- B01J2219/0004—Processes in series
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/19—Details relating to the geometry of the reactor
- B01J2219/194—Details relating to the geometry of the reactor round
- B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
- B01J2219/1942—Details relating to the geometry of the reactor round circular or disk-shaped spherical
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Catalysts (AREA)
Abstract
ABSTRACT
A synthesis converter system comprised of hot wall pressure vessels having generally spherical or ellipsoidal shape and catalyst beds therein with at least one heat exchanger intermediate the pressure vessels.
A synthesis converter system comprised of hot wall pressure vessels having generally spherical or ellipsoidal shape and catalyst beds therein with at least one heat exchanger intermediate the pressure vessels.
Description
~L251019 Case 196-3A
SYNTHESIS CONVERTER
Thls invention relates to converters for exothermic, catalytic reac-tions. More particularly, the invention relateæ to a converter system ~or ~i synthesis of ammonia or methanol carried out over an active, low tempera-! ture synthesis catalyst.
, .
ConventioDally, ammonia synthesis is carried out over predominantly iron catalyst at temperatures within the range from 340C to 530 and pressures within the range from 70 ~g/cm whereas methanol synthesis was carried out over predominantly zinc catalysts at temperatures as high as 450C and pressures as high as 150 kg/cm . These synthesis reactions are typically carried out in a large, single, high pressure reactor having from two to six catalyst beds arranged for series and/or parallel flow and pro-vision for inter or intra bed cooling of partially converted synthesis gas by indirect heat exchangers or by the introduction of cool quenching gas.
The catalyst beds have been arranged variously for axial, radi~l, or trans-verse flow of gas. In general, the high temperature, high pressure synthe-sis conditlons have required that the reactors be built with a double shell in order that cooling gas may be circulated in the shell annulus to cool the outer, pressure shell.
I' ¦~ Converters of the type described are not suitable for synthesis cata-¦¦ lysts that are very active at low temperatures in the range between 150 C
¦ and 435 C and employed in modern synthesis loops operating at pressures in the range between 15 kg/cm and 150 kg/cm2 owing to their si~e, co~plexity, and cost.
According to the invention, a synthesis converter system is provided with at least first and second pressure vessels, each of the vessels .
~2S~
comprised of top and bottom curved heads ~oined together at their flanges or lips and each having a single, horizontal, adiabatic, catalyst bed ex-tending across the vessel midsection, a top gas inlet and bottom gas outlet Il for flow of synthesis gas vertically downward through the catalyst bed and 5 il at least first indirect heat exchanger means disposed hydraulically between ¦I the first and second pressure vessel6 for cooling partially converted syn-ll thesis gas leaving the first pressure vessel prior to its introduction to !~ the second pressure vessel.
1, 1 Figure 1 illustrates an embodiment of the lnvention wherein the syn-10 ,, thesis converter has three pressure shells and intermediate indirect heat exchangers.
i Figure 2 illustrates an embodiment of the invention wherein the syn-thesis converter has four pressure shells and intermediate indirect heat exchangers.
lll 15 I Figure 3 illustrates an embodiment of the invention wherein the top and bottom curved heads are spherically dished heads welded together at their flanges.
. Il ,' Figure 4 illustrates an embodiment of the invention wherein the top Il and bottom curved heads are elliptically dished and flanged heads welded 20 1l together at their flanges.
¦ The catalyst bed in each pressure shell iB laterally defined by a't least one of the curved heads. When, as preferred, the curved heads are substantially identical in size and shape and the catalyst bed is at the ¦ vessel midsection, the bed will contact the inner surface of the flanges of 25 ~ both heads. The bed is supported by a foraminous, horizontal, flat member ~ 25~0~
extending across the vessel. The pressure shell require~ only sufflcient plenum above and below the catalyst bed to provide good gas distribution.
The nu~ber of pressure vessels employed in the converter is largely determined by the balance of catalyst cost and equipment cost for a spe-I cific installation but wlll typically be from two to four. Preferably, theconverter of the invention will employ three pressure vessels arranged for serial flow of gas and will have a heat exchange means between each ad~oin-ing pair of vessels. Since reaction rate is higher in the first vessel I relative to subsequent vessels, the vessels will typically have progress-10 l~ ively higher catalyst volumes.
1.
Referring to Figure 1 which illustrates an embodiment of the inven-tion wherein the synthesis converter has three integral pressure vessels and intermediate indirect heat exchangers, operation of the system in relation to ammonia synthesis is described. Preheated ammonia synthesis 15 - gas is introduced to the converter system from line 3, enters the top inlet of the first pressure vessel 4A, flows downwardly through the catalyst bed therein where a portlon of the synthesis gas is adiabatically converted to ammonia, and is removed from the bottom outlet of vessel 4A via line 17.
Il The hot, partially converted gas from first pressure vessel 4A is 20 I then introduced to hot side inlet 18 of first indirect heat exchanger 19 and cooled against boiler feed water which flows upwardly through tubes 20 within the exchanger.
l Cooled, partially converted gas from hot side outlet 21 of the first ¦ heat exchanger then flows through line 22 connected to the top inlet of ¦ second pressure vessel 4B, flows downwardly through the catalyst bed there-in where a further portion of the synthesis gas is adiabatically converted to ammonia, and is removed from the bottom outlet of vessel 4B via line 23.
1~51019 The hot, further converted gas from second pressure vessel 4B is then introduced to hot side inlet 24 of second heat exchanger 25 and again cooled agalns~ the boiler feed water Elowing upwardly through tubes 20 within the exchanger.
5 ~ll The first and second heat exchangers lllustrated sre combined in a ~ unitary heat exchanger of the shell and tube type. The unitary heat ex-¦' changer has shell side fluid fieal 26 which separates the shell or synthesis gas side into the first and second heat e~changers. ~luid seal 26 is simi-l lar to a tubesheet but does not have to be pressure tight since a moderate 10 1 leakage rom the first exchanger hot side to the second exchanger hot side i can be tolerated. Second indirect heat exchanger 25 has a cold side inlet 27 for introduction of boiler feed water which during its upward passage through tubes 20, is heated to steam which, in turn, is removed from cold side outlet 28 of first indirect exchanger 19.
i 15 j Cooled, further converted gas from hot side outlet 29 of second indi-rect heat exchanger 25 then flows through line 30 connected to the top inlet of third pressure vessel 4C, flows downwardly through the catalyst bed therein where a further portion of the synthesis gas is adiabatically ~ converted to ammonia, and is removed from the bottom outlet of vessel 4C
20 1 via line 31 for passage to an ammonia recovery system.
I
I In Figure 1, pressure vessels 4A, 4B, and 4C are supported on struc-tural ~irts 32 which, in turn, are supported on grade level foundations.
Since lndividual pressure vessels are small and light in comparison with conventional ammonia converters, they may be ~hipped and erected at any co~vetient tl=e in the , =vnia pltnt conetructio~ ~chedule.
¦I Figure 2 illustrates an e~bodiment of the invention whereln the ~yn-1~ thesis converter is employed in a large ammonia plant of about 1400 metrlc ~L25~
ton per day capacity and has four pressure vessels and intermediate heat exchangers.
, .
In Figure 2, the reference numerals have substantially the same iden-tification and purpose as in Figure 1 with the following additions.
5 ¦~ Ammonia synthesis gas is first introduced via line 1 to the cold slde of feed/effluent exchanger 2 to preheat the gas to 6ynthesis temperature.
The preheated synthesis gas then flows through the converter system as set forth in the description of Figure 1, however, converted gas from pressure 1 vessel 4C is cooled in feed/effluent exchanger 2 and further converted in 10 I pressure vessel 4D prior to passage to the ammonia recovery system via line 33.
In Figure 2, as in Figure 1, pressure vessels 4 A-D are supported on 1 structural skirts 32, however, the vessels are stacked in pairs to reduce ¦I plot space requirements.
ll Figure 3 illustrates an embodiment of a pressure vessel of the inven-, tion wherein the top curved head 5 and bottom curved head 6 are spherical 1- heads welded together at their flanges 7. Synthesis gas inlet 8 and gas distributor 9 are located in the top curved head on the vertical axis of , the vessel. The gas distributor comprises a spaced series of annular 20 ~ plates to provide even flow of gas through the upper plenum defined by the j inner surface of the top curved head and the top surface of catalyst bed 10. The gas distributor is removable so that gas inlet 8 may be used as a manway for inspection and catalyst loading.
Ca~alyst bed 10 is supported by a wire screen, in turn, supported by ¦ perforated~ horizont:al support plate 11, in turn, supported by lower ring 1 12 which is fixed to the bottom curved head. The catalyst bed i8 comprised 1:~5~L0~L9 of a layer of highly active 6ynthesis catalyst underlaid by coarse inert , materlal and e~tends horizontally across the pressure vessel at its verti-il cal midpoint to the inner surface of the curved heads at thelr ~unction. A
I, perforated, flat gas distributor plate 13 supported by upper ring 14 is 5 ¦I removably mounted above the catalyst bed to provide uniform distribution of¦¦ synthesis gas from the upper plenum into the catalyst bed. Partially con-¦, verted gas leaving the bottom surface of the catalyst bed passes throughsupport plate 11 and into a lower plenum defined by the inner surface of 1 the bottom curved head and bottom surface of the catalyfit bed and leaves the vessel through gas outlet 15.
' Figure 4 illustrates an embodiment of a pressure vessel of the inven-tion wherein the top curved head 5 and bottom curved head 6 are elliptical-ly dished and flanged heads. Beyond the difference in volume of the Il plenums, the elements of the vessel of fi~ure 4 are the same as in Figure 3.
SYNTHESIS CONVERTER
Thls invention relates to converters for exothermic, catalytic reac-tions. More particularly, the invention relateæ to a converter system ~or ~i synthesis of ammonia or methanol carried out over an active, low tempera-! ture synthesis catalyst.
, .
ConventioDally, ammonia synthesis is carried out over predominantly iron catalyst at temperatures within the range from 340C to 530 and pressures within the range from 70 ~g/cm whereas methanol synthesis was carried out over predominantly zinc catalysts at temperatures as high as 450C and pressures as high as 150 kg/cm . These synthesis reactions are typically carried out in a large, single, high pressure reactor having from two to six catalyst beds arranged for series and/or parallel flow and pro-vision for inter or intra bed cooling of partially converted synthesis gas by indirect heat exchangers or by the introduction of cool quenching gas.
The catalyst beds have been arranged variously for axial, radi~l, or trans-verse flow of gas. In general, the high temperature, high pressure synthe-sis conditlons have required that the reactors be built with a double shell in order that cooling gas may be circulated in the shell annulus to cool the outer, pressure shell.
I' ¦~ Converters of the type described are not suitable for synthesis cata-¦¦ lysts that are very active at low temperatures in the range between 150 C
¦ and 435 C and employed in modern synthesis loops operating at pressures in the range between 15 kg/cm and 150 kg/cm2 owing to their si~e, co~plexity, and cost.
According to the invention, a synthesis converter system is provided with at least first and second pressure vessels, each of the vessels .
~2S~
comprised of top and bottom curved heads ~oined together at their flanges or lips and each having a single, horizontal, adiabatic, catalyst bed ex-tending across the vessel midsection, a top gas inlet and bottom gas outlet Il for flow of synthesis gas vertically downward through the catalyst bed and 5 il at least first indirect heat exchanger means disposed hydraulically between ¦I the first and second pressure vessel6 for cooling partially converted syn-ll thesis gas leaving the first pressure vessel prior to its introduction to !~ the second pressure vessel.
1, 1 Figure 1 illustrates an embodiment of the lnvention wherein the syn-10 ,, thesis converter has three pressure shells and intermediate indirect heat exchangers.
i Figure 2 illustrates an embodiment of the invention wherein the syn-thesis converter has four pressure shells and intermediate indirect heat exchangers.
lll 15 I Figure 3 illustrates an embodiment of the invention wherein the top and bottom curved heads are spherically dished heads welded together at their flanges.
. Il ,' Figure 4 illustrates an embodiment of the invention wherein the top Il and bottom curved heads are elliptically dished and flanged heads welded 20 1l together at their flanges.
¦ The catalyst bed in each pressure shell iB laterally defined by a't least one of the curved heads. When, as preferred, the curved heads are substantially identical in size and shape and the catalyst bed is at the ¦ vessel midsection, the bed will contact the inner surface of the flanges of 25 ~ both heads. The bed is supported by a foraminous, horizontal, flat member ~ 25~0~
extending across the vessel. The pressure shell require~ only sufflcient plenum above and below the catalyst bed to provide good gas distribution.
The nu~ber of pressure vessels employed in the converter is largely determined by the balance of catalyst cost and equipment cost for a spe-I cific installation but wlll typically be from two to four. Preferably, theconverter of the invention will employ three pressure vessels arranged for serial flow of gas and will have a heat exchange means between each ad~oin-ing pair of vessels. Since reaction rate is higher in the first vessel I relative to subsequent vessels, the vessels will typically have progress-10 l~ ively higher catalyst volumes.
1.
Referring to Figure 1 which illustrates an embodiment of the inven-tion wherein the synthesis converter has three integral pressure vessels and intermediate indirect heat exchangers, operation of the system in relation to ammonia synthesis is described. Preheated ammonia synthesis 15 - gas is introduced to the converter system from line 3, enters the top inlet of the first pressure vessel 4A, flows downwardly through the catalyst bed therein where a portlon of the synthesis gas is adiabatically converted to ammonia, and is removed from the bottom outlet of vessel 4A via line 17.
Il The hot, partially converted gas from first pressure vessel 4A is 20 I then introduced to hot side inlet 18 of first indirect heat exchanger 19 and cooled against boiler feed water which flows upwardly through tubes 20 within the exchanger.
l Cooled, partially converted gas from hot side outlet 21 of the first ¦ heat exchanger then flows through line 22 connected to the top inlet of ¦ second pressure vessel 4B, flows downwardly through the catalyst bed there-in where a further portion of the synthesis gas is adiabatically converted to ammonia, and is removed from the bottom outlet of vessel 4B via line 23.
1~51019 The hot, further converted gas from second pressure vessel 4B is then introduced to hot side inlet 24 of second heat exchanger 25 and again cooled agalns~ the boiler feed water Elowing upwardly through tubes 20 within the exchanger.
5 ~ll The first and second heat exchangers lllustrated sre combined in a ~ unitary heat exchanger of the shell and tube type. The unitary heat ex-¦' changer has shell side fluid fieal 26 which separates the shell or synthesis gas side into the first and second heat e~changers. ~luid seal 26 is simi-l lar to a tubesheet but does not have to be pressure tight since a moderate 10 1 leakage rom the first exchanger hot side to the second exchanger hot side i can be tolerated. Second indirect heat exchanger 25 has a cold side inlet 27 for introduction of boiler feed water which during its upward passage through tubes 20, is heated to steam which, in turn, is removed from cold side outlet 28 of first indirect exchanger 19.
i 15 j Cooled, further converted gas from hot side outlet 29 of second indi-rect heat exchanger 25 then flows through line 30 connected to the top inlet of third pressure vessel 4C, flows downwardly through the catalyst bed therein where a further portion of the synthesis gas is adiabatically ~ converted to ammonia, and is removed from the bottom outlet of vessel 4C
20 1 via line 31 for passage to an ammonia recovery system.
I
I In Figure 1, pressure vessels 4A, 4B, and 4C are supported on struc-tural ~irts 32 which, in turn, are supported on grade level foundations.
Since lndividual pressure vessels are small and light in comparison with conventional ammonia converters, they may be ~hipped and erected at any co~vetient tl=e in the , =vnia pltnt conetructio~ ~chedule.
¦I Figure 2 illustrates an e~bodiment of the invention whereln the ~yn-1~ thesis converter is employed in a large ammonia plant of about 1400 metrlc ~L25~
ton per day capacity and has four pressure vessels and intermediate heat exchangers.
, .
In Figure 2, the reference numerals have substantially the same iden-tification and purpose as in Figure 1 with the following additions.
5 ¦~ Ammonia synthesis gas is first introduced via line 1 to the cold slde of feed/effluent exchanger 2 to preheat the gas to 6ynthesis temperature.
The preheated synthesis gas then flows through the converter system as set forth in the description of Figure 1, however, converted gas from pressure 1 vessel 4C is cooled in feed/effluent exchanger 2 and further converted in 10 I pressure vessel 4D prior to passage to the ammonia recovery system via line 33.
In Figure 2, as in Figure 1, pressure vessels 4 A-D are supported on 1 structural skirts 32, however, the vessels are stacked in pairs to reduce ¦I plot space requirements.
ll Figure 3 illustrates an embodiment of a pressure vessel of the inven-, tion wherein the top curved head 5 and bottom curved head 6 are spherical 1- heads welded together at their flanges 7. Synthesis gas inlet 8 and gas distributor 9 are located in the top curved head on the vertical axis of , the vessel. The gas distributor comprises a spaced series of annular 20 ~ plates to provide even flow of gas through the upper plenum defined by the j inner surface of the top curved head and the top surface of catalyst bed 10. The gas distributor is removable so that gas inlet 8 may be used as a manway for inspection and catalyst loading.
Ca~alyst bed 10 is supported by a wire screen, in turn, supported by ¦ perforated~ horizont:al support plate 11, in turn, supported by lower ring 1 12 which is fixed to the bottom curved head. The catalyst bed i8 comprised 1:~5~L0~L9 of a layer of highly active 6ynthesis catalyst underlaid by coarse inert , materlal and e~tends horizontally across the pressure vessel at its verti-il cal midpoint to the inner surface of the curved heads at thelr ~unction. A
I, perforated, flat gas distributor plate 13 supported by upper ring 14 is 5 ¦I removably mounted above the catalyst bed to provide uniform distribution of¦¦ synthesis gas from the upper plenum into the catalyst bed. Partially con-¦, verted gas leaving the bottom surface of the catalyst bed passes throughsupport plate 11 and into a lower plenum defined by the inner surface of 1 the bottom curved head and bottom surface of the catalyfit bed and leaves the vessel through gas outlet 15.
' Figure 4 illustrates an embodiment of a pressure vessel of the inven-tion wherein the top curved head 5 and bottom curved head 6 are elliptical-ly dished and flanged heads. Beyond the difference in volume of the Il plenums, the elements of the vessel of fi~ure 4 are the same as in Figure 3.
Claims (6)
1. A synthesis converter system comprising:
(a) first and second pressure vessels, each of said pressure vessels having a top curved head and a bottom curved head contiguous at their flanges, a gas inlet disposed in the top curved head, a gas outlet disposed in the bottom curved head, a single, adiabatic, catalyst bed con-taining synthesis catalyst horizontally disposed at substantially the pres-sure vessel midsection and extending across the entire cross-section of said pressure vessel, said catalyst bed being defined at its bottom surface by a foraminous, flat, horizontal support extending across the pressure vessel and at its horizontal extremities by at least one of the curved heads, the top surface of said catalyst being in fluid communication with the inner surface of said top curved head and said gas inlet and the bottom surface of said catalyst bed being in fluid communication with the inner surface of said bottom curved head and said gas outlet; and (b) first indirect heat exchange means having a hot side inlet and a hot side outlet, the hot side inlet being in fluid communication with the first pressure vessel gas outlet and the hot side outlet being in fluid communication with the second pressure vessel gas inlet.
(a) first and second pressure vessels, each of said pressure vessels having a top curved head and a bottom curved head contiguous at their flanges, a gas inlet disposed in the top curved head, a gas outlet disposed in the bottom curved head, a single, adiabatic, catalyst bed con-taining synthesis catalyst horizontally disposed at substantially the pres-sure vessel midsection and extending across the entire cross-section of said pressure vessel, said catalyst bed being defined at its bottom surface by a foraminous, flat, horizontal support extending across the pressure vessel and at its horizontal extremities by at least one of the curved heads, the top surface of said catalyst being in fluid communication with the inner surface of said top curved head and said gas inlet and the bottom surface of said catalyst bed being in fluid communication with the inner surface of said bottom curved head and said gas outlet; and (b) first indirect heat exchange means having a hot side inlet and a hot side outlet, the hot side inlet being in fluid communication with the first pressure vessel gas outlet and the hot side outlet being in fluid communication with the second pressure vessel gas inlet.
2. The converter of claim 1 wherein the top and bottom curved heads are spherical heads.
3. The converter of claim 1 wherein the top and bottom curved heads are elliptical dished and flanged heads.
4. The converter of either claim 2 having three pressure vessels, the third pressure vessel having a top curved head and a bottom curved head contiguous at their flanges, a gas inlet disposed in the top curved head, a gas outlet disposed in the bottom curved head, a single, adiabatic, catalyst bed containing synthesis catalyst horizontally disposed at substantially the third pressure vessel midsection and extending across the entire cross-section of the third pressure vessel, said catalyst bed being defined at its bottom surface by a foraminous, flat, horizontal sup-port extending across the third pressure vessel and at its horizontal extremities by at least one of the curved heads, the top surface of said catalyst bed being in fluid communication with the inner surface of said top curved head and said gas inlet and the bottom surface of said catalyst bed being in fluid communication with the inner surface of said bottom curved head and said gas outlet, the converter additionally comprising second, indirect heat exchange means having a hot side inlet and a hot side outlet, the hot side inlet of the second indirect heat exchanger being in fluid communication with the second pressure vessel gas outlet and the hot side outlet of the second, indirect heat exchanger being in fluid communi-cation with the third pressure vessel gas inlet.
5. The converter of claim 4 wherein the first and second indirect heat exchange means are a unitary heat exchanger having a cold side inlet and a cold side outlet.
6. The converter of claim 5 wherein the cold side inlet of the uni-tary heat exchanger is a water inlet and the cold side outlet of the uni-tary heat exchanger is a steam outlet.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US66147984A | 1984-10-16 | 1984-10-16 | |
| US661,479 | 1984-10-16 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1251019A true CA1251019A (en) | 1989-03-14 |
Family
ID=24653776
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000491634A Expired CA1251019A (en) | 1984-10-16 | 1985-09-26 | Synthesis converter |
Country Status (6)
| Country | Link |
|---|---|
| AU (1) | AU4842685A (en) |
| CA (1) | CA1251019A (en) |
| ES (1) | ES8608919A1 (en) |
| IN (1) | IN165277B (en) |
| YU (1) | YU156885A (en) |
| ZA (1) | ZA857361B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012146904A1 (en) | 2011-04-27 | 2012-11-01 | Davy Process Technology Limited | Process for the synthesis of methanol |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IN165276B (en) * | 1984-10-16 | 1989-09-09 | Kellogg M W Co | |
| GB0113078D0 (en) | 2001-05-30 | 2001-07-18 | Kvaerner Process Tech Ltd | Process and plant |
-
1985
- 1985-08-23 IN IN702/DEL/85A patent/IN165277B/en unknown
- 1985-09-24 ZA ZA857361A patent/ZA857361B/en unknown
- 1985-09-26 CA CA000491634A patent/CA1251019A/en not_active Expired
- 1985-10-03 YU YU01568/85A patent/YU156885A/en unknown
- 1985-10-09 AU AU48426/85A patent/AU4842685A/en not_active Abandoned
- 1985-10-16 ES ES547935A patent/ES8608919A1/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012146904A1 (en) | 2011-04-27 | 2012-11-01 | Davy Process Technology Limited | Process for the synthesis of methanol |
Also Published As
| Publication number | Publication date |
|---|---|
| AU4842685A (en) | 1986-04-24 |
| YU156885A (en) | 1987-10-31 |
| ES547935A0 (en) | 1986-09-01 |
| ES8608919A1 (en) | 1986-09-01 |
| IN165277B (en) | 1989-09-09 |
| ZA857361B (en) | 1986-05-28 |
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