CA1174245A - Method of obtaining improved equilibrium conditions and of simultaneously producing steam under high pressure in the production of methanol - Google Patents
Method of obtaining improved equilibrium conditions and of simultaneously producing steam under high pressure in the production of methanolInfo
- Publication number
- CA1174245A CA1174245A CA000382167A CA382167A CA1174245A CA 1174245 A CA1174245 A CA 1174245A CA 000382167 A CA000382167 A CA 000382167A CA 382167 A CA382167 A CA 382167A CA 1174245 A CA1174245 A CA 1174245A
- Authority
- CA
- Canada
- Prior art keywords
- water
- steam
- reactor
- feed water
- temperature
- 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
- B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
-
- 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
- B01J8/0005—Catalytic processes under superatmospheric pressure
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1512—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by reaction conditions
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00026—Controlling or regulating the heat exchange system
- B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
- B01J2208/0007—Pressure measurement
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
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- 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
Abstract
ABSTRACT OF THE DISCLOSURE:
In a method of controlling the equilibrium con-ditions and of simultaneously producing steam under high pressure in the production of methanol by a reaction of oxides of carbon and of hydrogen-containing gases at temper-atures of 200 to 300° C under a pressure of 20 to 100 bars at a copper-containing catalyst, which is contained within the reactor in tubes, which are indirectly cooled by boiling water under pressure, wherein the resulting steam is with-drawn together with circulating water and is separated from the water, the water is recycled and the evaporated water is replaced by feed water. It is proposed to carry out the method in such a manner that a perforated thin intermediate bottom is provided, which is spaced 20 to 150 cm over the lower tube plate, that the reactor is fed with the circu-lating water above that intermediate bottom and with the feed water below that intermediate bottom, that the gaseous reaction mixture is cooled by 20 to 50° C in the lower part of the catalyst-filled tubes in a tube length of 20 to 150 cm, that the feed water is heated in the reactor to temper-atures of 230 to 290° C with evaporation of part of the feed water, that the resulting mixture of steam and circulating water is separated, that the circulating water is recycled and the resulting high-pressure steam is withdrawn. In this method, steam under a pressure above 60 bars can be produced whereas only a pressure of 40 bars has been reached before.
In a method of controlling the equilibrium con-ditions and of simultaneously producing steam under high pressure in the production of methanol by a reaction of oxides of carbon and of hydrogen-containing gases at temper-atures of 200 to 300° C under a pressure of 20 to 100 bars at a copper-containing catalyst, which is contained within the reactor in tubes, which are indirectly cooled by boiling water under pressure, wherein the resulting steam is with-drawn together with circulating water and is separated from the water, the water is recycled and the evaporated water is replaced by feed water. It is proposed to carry out the method in such a manner that a perforated thin intermediate bottom is provided, which is spaced 20 to 150 cm over the lower tube plate, that the reactor is fed with the circu-lating water above that intermediate bottom and with the feed water below that intermediate bottom, that the gaseous reaction mixture is cooled by 20 to 50° C in the lower part of the catalyst-filled tubes in a tube length of 20 to 150 cm, that the feed water is heated in the reactor to temper-atures of 230 to 290° C with evaporation of part of the feed water, that the resulting mixture of steam and circulating water is separated, that the circulating water is recycled and the resulting high-pressure steam is withdrawn. In this method, steam under a pressure above 60 bars can be produced whereas only a pressure of 40 bars has been reached before.
Description
7424~
This invention relates to a method of obtaining improved equilibrium conditions and of simultaneously pro-ducing steam under high pressure in the production of metha-nol in a reactor by a reaction of oxides of carbon and of hydrogen-containing gases at temperatures of 200 to 300 C
under a pressure of 20 to 100 bars in the presence of a copper- -containing catalyst, which is contained within the reactor in tubes, which are indirectly cooled by boiling water under pressure, wherein the resulting steam is withdrawn together with circulating water and is separated from the water, the water is recycled and the evaporated water is replaced by feed water.
In order to utilize the heat of reaction génerated in the production of methanol in a process in which a synthe-sis gas which contains hydrogen and oxides of carbon (and has been produced by a cracking of hydrocarbons with steam at temperatures above 700 C in the presence of an indirectly heated, nickel-containing catalyst ) is reacted u~der pres-sures of 30 to 80 at and at temperatures of 230 to 280 C
in the presence of a copper-containing catalyst, which is contained in tubes that are indirectly cooled with water, it is known to utilize the cooling of the reactor tubes for a production of high-pressure steam (German Patent Specifi-cation 20 13 297).
A know apparatus for producing methanol in another process comprises a tubular reactor having tubes contacted by flowing boiling water under pressure. In that apparatus, the feed water enters the lower part of the reactor and the resulting strea~ is fed to a super-heater. Part of that steam can be withdrawn as high-pressure steam and another part can be supplied to a turbine, which drives a compressor.
The remaining part of the steam can be recovered as turbine ~742~5 steam (German Patent Specification 21 23 950), In the operation of the pre~iously know~ tubular reactor, circulating water from a stea~ header is fed to the tubular reactor. Part of the fed water is e~aporated at the catalyst-filled tubes, in which the components H2~, CO and C2 are reacted to form methanol. By thermosiphon action, the resulting steam together with cixculating water is forced into the steam header, where the steam is separated whereas the water, which is at its boiling point, is returned to the lower part of the reactor. The steam withdrawn from the steam header must be returned to the system as feed water. Depe~ding on the preheating of that feed water the temperature in the steam header will be more or less close to the boiling point of water. If the water is circulated about ten ti~es, feed water is fed at a temperature of 120 C and a pressure of 40 bars is maintained in the system. The circulating water fed to the lower part of the reactor will be at a temperature of about 237 C, which is 13 C under its boiling point. As a result, the temperature difference at the lower part of the reactor tubes containing catalyst at a temperature o~
about 255 C is very low and precludes an appr~ciable heat exchange and a cooling of the reacting mixed gases in the tubes.
Only steam at a pressure up to about 40 bars can be produced in the known tubular reactors for producing methanol because the copper catalyst is suscepticle to ele~
vated temperatures and a good equilibrium control is desired.
It is an object of the invention to avoid these disadvantages of the state o~ the art and to obtain a higher temperature difference in the lower part of the reactor and to effect an improved and more intense cooling of the reacting mixed gases. The equilibrium control is to be impro~ed and ~1742~5 steam under higher pressure is to be produced at the same time.
The process should involve lower energy cost.
This object is accomplished according to the inven-tion in that a perforated thin intermediate bottom is provided, which is spaced 20 to 150 cm over the lower tube plate, that the reactor is fed with the circulating water above that interme-diate bottom and with the feed water below that intermediate bottom, that the gaseous reaction mixture is cooled by 20 to 50C in the lower part of the catalyst-filled tubes over a tube length of 20 to 150 cm, that the feed water is heated in the reactor to temperatures of 230 to 290C with evaporation of part of the feed water, that the resulting mixture of steam and circulating water is separated, that the circulating wa-ter is recycled and the resulting high-pressure steam is withdrawn.
Thus, in particular the present invention provides a method of obtaining improved equilibrium conditions and of simultaneously producing steam under hiyh pressure in the pro-duction of methanol in a reactor by a gaseous reaction of oxides of carbon and hydrogen-containing gases at temperatures of 200 to 300C under a pressure of 20 to 100 bars in the presence of a copper-containing catalyst, which is contained within the reactor in reaction tubes, which are indirectly cooled by boiling water under pressure, said water being kept on a lower tube plate, wherein the resulting steam is withdrawn together with circulating water and is separated from the water, the water is recycled and the evaporated water is replaced by feed water, characterized in that the reactor is provided with a perforated thin intermediate bottom which is spaced 20 to 150 cm over the lower tube plate, that the reactor is fed with the circulating water above -that intermediate bottom and with the feed water below that intermediate bottom, that the gaseous reaction mixture is cooled by 20 to 50C in the lower ~ ~7~2~5 part of the catalyst-filled reaction tubes over a tube length of 20 to 150 cm, that the feed water is heated in the reactor to temperatures of 230 to 290C with evaporation of part of the feed water, that the resulting mixture of steam and circulating water is separated, that the circulatiny water is recycled and the resulting high-pressure steam is withdrawn.
In accordance with the invention the intermediate bottom can be spaced 20 to 80 cm ~rom the lower tube plate and is suitably spaced 50 cm from the lower tube plate.
The circulating water fed to the reactor is desirably at a temperature of 200 to 300C, preferably at a temperature of 230 to 290C, and the feèd water is fed at a temperature of 100 to 180C, preferably 110 to 150C.
The advantages afforded by the invention reside particularly in that the temperature difference between the cooliny fluid and the catalyst contained in the tubes can be increased in the lower part of the reactor in a simple, energy-saving process. As a result, the heat exhange is increased and the reacting yas mixture is cooled to a lower
This invention relates to a method of obtaining improved equilibrium conditions and of simultaneously pro-ducing steam under high pressure in the production of metha-nol in a reactor by a reaction of oxides of carbon and of hydrogen-containing gases at temperatures of 200 to 300 C
under a pressure of 20 to 100 bars in the presence of a copper- -containing catalyst, which is contained within the reactor in tubes, which are indirectly cooled by boiling water under pressure, wherein the resulting steam is withdrawn together with circulating water and is separated from the water, the water is recycled and the evaporated water is replaced by feed water.
In order to utilize the heat of reaction génerated in the production of methanol in a process in which a synthe-sis gas which contains hydrogen and oxides of carbon (and has been produced by a cracking of hydrocarbons with steam at temperatures above 700 C in the presence of an indirectly heated, nickel-containing catalyst ) is reacted u~der pres-sures of 30 to 80 at and at temperatures of 230 to 280 C
in the presence of a copper-containing catalyst, which is contained in tubes that are indirectly cooled with water, it is known to utilize the cooling of the reactor tubes for a production of high-pressure steam (German Patent Specifi-cation 20 13 297).
A know apparatus for producing methanol in another process comprises a tubular reactor having tubes contacted by flowing boiling water under pressure. In that apparatus, the feed water enters the lower part of the reactor and the resulting strea~ is fed to a super-heater. Part of that steam can be withdrawn as high-pressure steam and another part can be supplied to a turbine, which drives a compressor.
The remaining part of the steam can be recovered as turbine ~742~5 steam (German Patent Specification 21 23 950), In the operation of the pre~iously know~ tubular reactor, circulating water from a stea~ header is fed to the tubular reactor. Part of the fed water is e~aporated at the catalyst-filled tubes, in which the components H2~, CO and C2 are reacted to form methanol. By thermosiphon action, the resulting steam together with cixculating water is forced into the steam header, where the steam is separated whereas the water, which is at its boiling point, is returned to the lower part of the reactor. The steam withdrawn from the steam header must be returned to the system as feed water. Depe~ding on the preheating of that feed water the temperature in the steam header will be more or less close to the boiling point of water. If the water is circulated about ten ti~es, feed water is fed at a temperature of 120 C and a pressure of 40 bars is maintained in the system. The circulating water fed to the lower part of the reactor will be at a temperature of about 237 C, which is 13 C under its boiling point. As a result, the temperature difference at the lower part of the reactor tubes containing catalyst at a temperature o~
about 255 C is very low and precludes an appr~ciable heat exchange and a cooling of the reacting mixed gases in the tubes.
Only steam at a pressure up to about 40 bars can be produced in the known tubular reactors for producing methanol because the copper catalyst is suscepticle to ele~
vated temperatures and a good equilibrium control is desired.
It is an object of the invention to avoid these disadvantages of the state o~ the art and to obtain a higher temperature difference in the lower part of the reactor and to effect an improved and more intense cooling of the reacting mixed gases. The equilibrium control is to be impro~ed and ~1742~5 steam under higher pressure is to be produced at the same time.
The process should involve lower energy cost.
This object is accomplished according to the inven-tion in that a perforated thin intermediate bottom is provided, which is spaced 20 to 150 cm over the lower tube plate, that the reactor is fed with the circulating water above that interme-diate bottom and with the feed water below that intermediate bottom, that the gaseous reaction mixture is cooled by 20 to 50C in the lower part of the catalyst-filled tubes over a tube length of 20 to 150 cm, that the feed water is heated in the reactor to temperatures of 230 to 290C with evaporation of part of the feed water, that the resulting mixture of steam and circulating water is separated, that the circulating wa-ter is recycled and the resulting high-pressure steam is withdrawn.
Thus, in particular the present invention provides a method of obtaining improved equilibrium conditions and of simultaneously producing steam under hiyh pressure in the pro-duction of methanol in a reactor by a gaseous reaction of oxides of carbon and hydrogen-containing gases at temperatures of 200 to 300C under a pressure of 20 to 100 bars in the presence of a copper-containing catalyst, which is contained within the reactor in reaction tubes, which are indirectly cooled by boiling water under pressure, said water being kept on a lower tube plate, wherein the resulting steam is withdrawn together with circulating water and is separated from the water, the water is recycled and the evaporated water is replaced by feed water, characterized in that the reactor is provided with a perforated thin intermediate bottom which is spaced 20 to 150 cm over the lower tube plate, that the reactor is fed with the circulating water above -that intermediate bottom and with the feed water below that intermediate bottom, that the gaseous reaction mixture is cooled by 20 to 50C in the lower ~ ~7~2~5 part of the catalyst-filled reaction tubes over a tube length of 20 to 150 cm, that the feed water is heated in the reactor to temperatures of 230 to 290C with evaporation of part of the feed water, that the resulting mixture of steam and circulating water is separated, that the circulatiny water is recycled and the resulting high-pressure steam is withdrawn.
In accordance with the invention the intermediate bottom can be spaced 20 to 80 cm ~rom the lower tube plate and is suitably spaced 50 cm from the lower tube plate.
The circulating water fed to the reactor is desirably at a temperature of 200 to 300C, preferably at a temperature of 230 to 290C, and the feèd water is fed at a temperature of 100 to 180C, preferably 110 to 150C.
The advantages afforded by the invention reside particularly in that the temperature difference between the cooliny fluid and the catalyst contained in the tubes can be increased in the lower part of the reactor in a simple, energy-saving process. As a result, the heat exhange is increased and the reacting yas mixture is cooled to a lower
2~0 temperature so that the thermodynamic equilibrium is promoted.
The temperature used~are within the limits determined by the recrystallizing characteristics of the catalyst. Methanol can be produced more economically in accordance with the invention.
~ ' ,~,r"~
,f~
~/
~2'~ ~ 3a -:~742~5 The invention is shown diagrammatically and by way of example on the drawing and will now be described more in detail:
The drawing shows the reactor 1, catalyst tubes 2, the lower tube plate 3, the intermediate bottom 4, a feeding of feed water at 5, a feeding of circulating water at 6, a mixture of steam and circulating water at 7, a separation of steam from the circulating water in the steam header at 8 and a withdrawal of high-pressure steam at 9.
Example A reactor 1 for producing methanol contains tubes 2, which contain the catalyst. An intermediate bottom 4 is spaced 50 cm above the lower tube plate 3 and may consist of a thin sheet steel which has apertures consisting of bores small in diameter. The feed water at a temperature of 120 C
is introduced into the reactor through a supply conduit 5 closely above the lower tube plate 3. That unmixed feed water contacts the lower part of the catalyst tubes 2 and cools the reacting mixed gases by 35 C ln a pipe length of 50 cm.
~s a result, the feed water is heated to 280 C and a small part of it is evaporated.
Circulating water at a temperature of 280 C is introduced through a conduit 6 into the reactor 1 closely above the intermediate bottom 4. The colder feed water 5 fed below the intermediate bot~om 4 is uniformly distributed by the latter whereas on the other side a backmixing with the hotter circulating water fed above the intermediate bottom 4 is prevented.
The feed water 5 is mixed with the circulating water 6 only above the intermediate bottom 4. As a result, that portion of the catalyst tubes 2 which is disposed above the intermediate bottom 4 is operated at a temperature of ~ 4 ~7~5 280 C so that a pressure of more than 60 bars is obtained in the water-circulating system whereas only pressures up to 40 bars can be obtained in the previous processes. When the mixture of water vapor and circulating water has been wlthdrawn at 7 and has been separatcd into its two com-ponents at 8, high-pressure steam under a pressure in excess of 60 bars is recovered at 9 and can be used for numerous purposes in the same plant, e.g., for expansion with per-formance of work, for instance, in condensing steam turbines, or for a generation of electric power for driving gas com-pressures, or for supplying the energy required for the final distillation of the methanol, or for other purposes. Owing to the considerable advantages by the process as regards energy consumption, the process i5 particularly economical.
The temperature used~are within the limits determined by the recrystallizing characteristics of the catalyst. Methanol can be produced more economically in accordance with the invention.
~ ' ,~,r"~
,f~
~/
~2'~ ~ 3a -:~742~5 The invention is shown diagrammatically and by way of example on the drawing and will now be described more in detail:
The drawing shows the reactor 1, catalyst tubes 2, the lower tube plate 3, the intermediate bottom 4, a feeding of feed water at 5, a feeding of circulating water at 6, a mixture of steam and circulating water at 7, a separation of steam from the circulating water in the steam header at 8 and a withdrawal of high-pressure steam at 9.
Example A reactor 1 for producing methanol contains tubes 2, which contain the catalyst. An intermediate bottom 4 is spaced 50 cm above the lower tube plate 3 and may consist of a thin sheet steel which has apertures consisting of bores small in diameter. The feed water at a temperature of 120 C
is introduced into the reactor through a supply conduit 5 closely above the lower tube plate 3. That unmixed feed water contacts the lower part of the catalyst tubes 2 and cools the reacting mixed gases by 35 C ln a pipe length of 50 cm.
~s a result, the feed water is heated to 280 C and a small part of it is evaporated.
Circulating water at a temperature of 280 C is introduced through a conduit 6 into the reactor 1 closely above the intermediate bottom 4. The colder feed water 5 fed below the intermediate bot~om 4 is uniformly distributed by the latter whereas on the other side a backmixing with the hotter circulating water fed above the intermediate bottom 4 is prevented.
The feed water 5 is mixed with the circulating water 6 only above the intermediate bottom 4. As a result, that portion of the catalyst tubes 2 which is disposed above the intermediate bottom 4 is operated at a temperature of ~ 4 ~7~5 280 C so that a pressure of more than 60 bars is obtained in the water-circulating system whereas only pressures up to 40 bars can be obtained in the previous processes. When the mixture of water vapor and circulating water has been wlthdrawn at 7 and has been separatcd into its two com-ponents at 8, high-pressure steam under a pressure in excess of 60 bars is recovered at 9 and can be used for numerous purposes in the same plant, e.g., for expansion with per-formance of work, for instance, in condensing steam turbines, or for a generation of electric power for driving gas com-pressures, or for supplying the energy required for the final distillation of the methanol, or for other purposes. Owing to the considerable advantages by the process as regards energy consumption, the process i5 particularly economical.
Claims (10)
1. A method of obtaining improved equilibrium conditions and of simultaneously producing steam under high pressure in the production of methanol in a reactor by a gaseous reaction of oxides of carbon and hydrogen containing gases at temperatures of 200 to 300°C under a pressure of 20 to 100 bars in the pre-sence of a copper-containing catalyst, which is contained within the reactor in reaction tubes, which are indirectly cooled by boiling water under pressure, said water being kept on a lower tube plate, wherein the resulting steam is withdrawn together with circulating water and is separated from the water, the water is recycled and the evaporated water is replaced by feed water, characterized in that the reactor is provided with a perforated thin intermediate bottom which is spaced 20 to 150 cm over the lower tube plate, that the reactor is fed with the circulating water above that intermediate bottom and with the feed water below that intermediate bottom, that the gaseous reaction mixture is cooled by 20 to 50°C in the lower part of the catalyst-filled reaction tubes over a tube length of 20 to 150 cm, that the feed water is heated in the reactor to temperatures of 230 to 290°C with evaporation of part of the feed water, that the resulting mixture of steam and circulating water is separated, that the circulating water is recycled and the resulting high pressure steam is withdrawn.
2. A method according to claim 1, characterized in that the intermediate bottom is spaced 50 cm from the lower tube plate.
3. A process according to claim 1, characterized in that the circulating water is fed at a temperature of 200 to 300° C.
4. A process according to claim 2, characterized in that the circulating water is fed at a temperature of 200 to 300° C.
5. A process according to claim 1, characterized in that the circulating water is fed at a temperature of 230 to 290° C.
6. A process according to claim 2, characterized in that the circulating water is fed at a temperature of 230 to 290° C.
7. A process according to anyone of the preceding claims 1 to 3, characterized in that the feed water is fed at a temperature of 100 to 180° C.
8. A process according to anyone of the preceding claims 4 to 6, characterized in that the feed water is fed at a temperature of 100 to 180° C.
9. A process according to anyone of the preceding claims 1 to 3, characterized in that the feed water is supplied at a temperature of 110 to 150° C.
10. A process according to anyone of the preceding claims 4 to 6, characterized in that the feed water is supplied at a temperature of 110 to 150° C.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP3028646.5 | 1980-07-29 | ||
| DE19803028646 DE3028646A1 (en) | 1980-07-29 | 1980-07-29 | METHOD FOR IMPROVING BALANCE AND SIMULTANEOUSLY GENERATING HIGH-PRESSURE STEAM IN THE PRODUCTION OF METHANOL |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1174245A true CA1174245A (en) | 1984-09-11 |
Family
ID=6108325
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000382167A Expired CA1174245A (en) | 1980-07-29 | 1981-07-21 | Method of obtaining improved equilibrium conditions and of simultaneously producing steam under high pressure in the production of methanol |
Country Status (12)
| Country | Link |
|---|---|
| US (1) | US4369255A (en) |
| JP (1) | JPS5753420A (en) |
| AR (1) | AR229872A1 (en) |
| AU (1) | AU545496B2 (en) |
| BR (1) | BR8104842A (en) |
| CA (1) | CA1174245A (en) |
| DE (1) | DE3028646A1 (en) |
| FR (1) | FR2487820B1 (en) |
| MX (1) | MX157474A (en) |
| NL (1) | NL8102704A (en) |
| NO (1) | NO155000C (en) |
| SE (1) | SE8104582L (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL8204820A (en) * | 1982-12-14 | 1984-07-02 | Stamicarbon | METHOD FOR THE PREPARATION OF METHANOL. |
| DE3310772A1 (en) * | 1983-03-24 | 1984-09-27 | Interatom Internationale Atomreaktorbau Gmbh, 5060 Bergisch Gladbach | Methanol synthesis reactor with low-boiling coolant |
| IN161263B (en) * | 1983-06-30 | 1987-10-31 | Halcon Sd Group Inc | |
| JPS60106527A (en) * | 1983-11-14 | 1985-06-12 | Mitsubishi Heavy Ind Ltd | Double pipe reactor for exothermic reaction |
| US4721611A (en) * | 1984-03-02 | 1988-01-26 | Imperial Chemical Industries Plc | Hydrogen production |
| US4946477A (en) * | 1988-04-07 | 1990-08-07 | Air Products And Chemicals, Inc. | IGCC process with combined methanol synthesis/water gas shift for methanol and electrical power production |
| GB9904649D0 (en) * | 1998-05-20 | 1999-04-21 | Ici Plc | Methanol synthesis |
| US6152099A (en) * | 1998-12-21 | 2000-11-28 | Urich; Carl L. | Apparatus and method of supplying additive to internal combustion engine |
| JP2006513839A (en) * | 2003-01-31 | 2006-04-27 | マン、デーヴェーエー、ゲーエムベーハー | Multi-tank jacket tube reactor for exothermic gas phase reaction |
| WO2006084286A2 (en) * | 2005-01-31 | 2006-08-10 | Exxonmobil Chemical Patents Inc. | Hydrocarbon compositions useful for producing fuels |
| US7678953B2 (en) * | 2005-01-31 | 2010-03-16 | Exxonmobil Chemical Patents Inc. | Olefin oligomerization |
| US8354564B2 (en) * | 2006-04-07 | 2013-01-15 | BHS Technology LLC | Production of dry alcohol |
| DE102007024934B4 (en) | 2007-05-29 | 2010-04-29 | Man Dwe Gmbh | Tube bundle reactors with pressure fluid cooling |
| KR101643045B1 (en) * | 2013-09-17 | 2016-07-27 | 주식회사 엘지화학 | Heat recovery apparatus |
| CA2993958A1 (en) * | 2015-07-29 | 2017-02-02 | Primus Green Energy Inc. | Two-stage reactor for exothermal and reversible reactions and methods thereof |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB680821A (en) * | 1949-11-08 | 1952-10-15 | Ruhrchemie Ag | Process and apparatus for the catalytic hydrogenation of carbon monoxide |
| DE2013297B2 (en) * | 1970-03-20 | 1973-10-25 | Metallgesellschaft Ag, 6000 Frankfurt | Process for utilizing the heat of reaction in the production of methanol |
| DE2123950C3 (en) * | 1971-05-14 | 1975-06-12 | Metallgesellschaft Ag, 6000 Frankfurt | Method and device for the production of methanol in tube furnaces |
| IT986732B (en) * | 1973-04-30 | 1975-01-30 | Snam Progetti | PROCEDURE FOR CONDUCTING PARTIAL OXIDATION REACTIONS WITH OXY GENO OF ORGANIC COMPOUNDS IN THE STEAM PHASE AND EQUIPMENT SUITABLE TO CARRY OUT THIS PROCEDURE |
| GB1484366A (en) * | 1974-07-02 | 1977-09-01 | Ici Ltd | Methanol |
| US4074660A (en) * | 1975-11-24 | 1978-02-21 | The Lummus Company | Waste heat recovery from high temperature reaction effluents |
| DE2603204C2 (en) * | 1976-01-29 | 1982-12-02 | Metallgesellschaft Ag, 6000 Frankfurt | Process for the production of methanol |
| DE2603291C2 (en) * | 1976-01-29 | 1984-01-12 | Metallgesellschaft Ag, 6000 Frankfurt | Process for the production of methanol |
| DE2846693A1 (en) * | 1978-10-26 | 1980-05-08 | Metallgesellschaft Ag | METHOD FOR PRODUCING GASOLINE FROM SYNTHESIS GAS |
-
1980
- 1980-07-29 DE DE19803028646 patent/DE3028646A1/en active Granted
-
1981
- 1981-06-04 NL NL8102704A patent/NL8102704A/en not_active Application Discontinuation
- 1981-06-26 NO NO812206A patent/NO155000C/en unknown
- 1981-07-01 MX MX188115A patent/MX157474A/en unknown
- 1981-07-17 FR FR8113984A patent/FR2487820B1/en not_active Expired
- 1981-07-21 CA CA000382167A patent/CA1174245A/en not_active Expired
- 1981-07-23 AR AR286186A patent/AR229872A1/en active
- 1981-07-24 JP JP56117007A patent/JPS5753420A/en active Granted
- 1981-07-27 US US06/287,007 patent/US4369255A/en not_active Expired - Fee Related
- 1981-07-27 AU AU73475/81A patent/AU545496B2/en not_active Ceased
- 1981-07-28 BR BR8104842A patent/BR8104842A/en unknown
- 1981-07-28 SE SE8104582A patent/SE8104582L/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| MX157474A (en) | 1988-11-24 |
| AU7347581A (en) | 1982-04-08 |
| DE3028646C2 (en) | 1989-01-19 |
| SE8104582L (en) | 1982-01-30 |
| JPH0136449B2 (en) | 1989-07-31 |
| NL8102704A (en) | 1982-02-16 |
| BR8104842A (en) | 1982-04-13 |
| NO812206L (en) | 1982-02-01 |
| FR2487820B1 (en) | 1985-06-21 |
| AR229872A1 (en) | 1983-12-30 |
| JPS5753420A (en) | 1982-03-30 |
| AU545496B2 (en) | 1985-07-18 |
| NO155000B (en) | 1986-10-20 |
| US4369255A (en) | 1983-01-18 |
| NO155000C (en) | 1987-01-28 |
| DE3028646A1 (en) | 1982-03-04 |
| FR2487820A1 (en) | 1982-02-05 |
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