CA1205092A - Catalytic conversion of synthesis gas to hydrocarbons - Google Patents
Catalytic conversion of synthesis gas to hydrocarbonsInfo
- Publication number
- CA1205092A CA1205092A CA000427027A CA427027A CA1205092A CA 1205092 A CA1205092 A CA 1205092A CA 000427027 A CA000427027 A CA 000427027A CA 427027 A CA427027 A CA 427027A CA 1205092 A CA1205092 A CA 1205092A
- Authority
- CA
- Canada
- Prior art keywords
- pressure
- bar
- rate
- raised
- reactor
- 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
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 32
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 29
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 29
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 19
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 19
- 230000003197 catalytic effect Effects 0.000 title description 2
- 238000000034 method Methods 0.000 claims abstract description 33
- 239000003054 catalyst Substances 0.000 claims abstract description 31
- 239000007788 liquid Substances 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 4
- 239000001993 wax Substances 0.000 description 8
- 239000002245 particle Substances 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 241000282344 Mellivora capensis Species 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
- C07C1/0455—Reaction conditions
- C07C1/046—Numerical values of parameters
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
- C07C1/0455—Reaction conditions
- C07C1/047—Processes in which one or more parameters are changed during the process; Starting-up of the process
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
ABSTRACT
This invention relates to a method of catalytically converting synthesis gas to hydrocarbons in a continuous fixed bed catalyst reactor. The method includes operating a continuous fixed bed catalyst reactor at a pressure above a pressure of about 26 bar and at a synthesis gas feed rate above the gas feed rate characteristically used at a pressure of about 26 bar to obtain said hydrocarbons. The invention relates also to a method of operating a continuous fixed bed catalyst reactor operable at a pressure of about 26 bar to convert synthesis gas to hydrocarbons at a fixed feed rate. The method relates still further to a method of increasing the reaction rate of a continuous fixed bed catalyst reactor above the reaction rate when it is operated at a pressure of about 26 bar to convert synthesis gas to hydrocarbons at a fixed feed rate.
This invention relates to a method of catalytically converting synthesis gas to hydrocarbons in a continuous fixed bed catalyst reactor. The method includes operating a continuous fixed bed catalyst reactor at a pressure above a pressure of about 26 bar and at a synthesis gas feed rate above the gas feed rate characteristically used at a pressure of about 26 bar to obtain said hydrocarbons. The invention relates also to a method of operating a continuous fixed bed catalyst reactor operable at a pressure of about 26 bar to convert synthesis gas to hydrocarbons at a fixed feed rate. The method relates still further to a method of increasing the reaction rate of a continuous fixed bed catalyst reactor above the reaction rate when it is operated at a pressure of about 26 bar to convert synthesis gas to hydrocarbons at a fixed feed rate.
Description
THIS INVENTION relates to the catalytic conversion of synthesis gas to hydrocarbons.
According to one aspect of the-invention, there is provided a method of - 5 catalytically converting synthesis gas to hydrocarbons in a co~tinuous flxed bed catalyst reactor, which includes operating a continuous fixed bed catalyst reactor at a pressure above a pressure of about 26 bar and at a synthesis gas 10 feed rate above the gas feed rate characteristically used at a pressure of about 26 bar to obtain said hydrocarbons.
According to another aspect of the 15 invention, there is provided a me-thod of operating a continuous fixed bed catalyst reactor operable at a pressure of about 26 bar to convert syn-thesis yas to hydrocarbons at a fixed feed ratel which method includes raisiny the pressure to a level 20 above 26 bars while at the same time raising the feed rate above said fixed feed rate to obtain substantially the same type of hydrocarbons.
~ ;
According to yet another clspect of the invention, there is provided a method of increasing the reaction rate of a continuous fixed bed catalyst reactor above the reaction rate when it is operated at a pressure of about 26 bar to convert synthesis gas to hydrocarbons at a fixed feed rate, which method includes raising the pressure to a level above 26 bars while at the same time raising the feed rate above said fixed feed rate -to obtain subs-tantially the same type of 10 hydrocarbons, at an increased reaction ra-te.
The rise in the gas feed rate may be of the same order of magnitude as the rise in the pressure. The rises in the pressure and the gas 15 feed rate may be as high as a doubling or more of the pressure of about 26 bar and the feed rate characteristically used at that pressure or the fixed feed rate, respectively. Proportionally smaller rises can also lead to a higher reaction 20 rate.
The method may include converting a CO-~H2 synthesis gas in the reactor by means of a Fischer-Tropsch reaction r which may be of the type ~.Z~5~
used to produce Fischer~Tropsch waxes from the CO~H2 synthesis gas. The reactor may be a relatively elongate tubular packed catalyst fixed bed reactor surrounded by a liquid cooling medium.
The method may include effecting the reaction at a temperature between about 200C and about 250C.
The pressure may be at least 35 bar, preferably between 35 and about 60 bar.
The method may include feeding to the reactor a make up synthesis gas stream (comprising fresh gas) and, optional]y, a recycle synthesis gas stream (comprising unreacted exhaust gas), the rate of the make up stream being raised as the 15 pressure is raised and, when present, the rate of the recycle stream also being raised so that the linear velocity of the gas through the reactor remains substantially constant as the pressure is raisedO
For example, at said pressure of about 26 bar, the make up stream rate may be between about lO and about 40 normal cubic metres per hour (hereinafter referred to as "m3(n)/hr) per reactor ~2V5~
tube, and as the pressu.re is raise~ to about ~0 bar, the make up stream rate may be ralsed proportionally to between about 15 and about 60 m3 (n)/hr per reactor tube, and as the pressure is raised to about 60 bar, the make up stream rate 5 may be raised proportionally to between 23 and 92 m3(n)/hr per reactor tube.
It is to be understood that the aforementioned make up gas stream rates are 10 typical rates at the gi~en pressures. ~ccordingly the make up gas rate may also be below the lower rate hereinbefore mentioned or above the upper rate hereinbefore mentioned, at said pressure of about 26 bar~ and the make up rate will then be 15 raised proportionally as the pressure is raised above 26 bar.
It is further to be understood that, in a modificati.on of the invention, the recycle gas 20 stream rate can be raised to a lesser or greater extent so that linear velocity of the gas khrough the reactor at the elevated pressures is different to the linear velocity therethrough at the pressure of about 26 bar.
~c~
`
Typically, in fixed bed catalyst reactors of this type, the catalyst particles are relatively large (compared with ~hose of fluidized catalyst reactors used for simllar purposes) and remain stationary in the bed in use. Heat exchange between the particles and the reactor walls is relatively poor (compared with said fluidized bed reactors) and thexe is a danger that the particles will overheat when the reaction catalysed is exothermic. This overheating is generaLly 10 combatted by packing the catalyst in a plurality of smaller consecutive beds with cold gas or liquid injected between the heds to lower catalysk temperature, or the catalyst is packed into relatively long narrow tubes surrounded by a 15 liquid cooling medium.
Temperature control is important when the catalytic reaction, eg as regards its selectivity, is sensitive to temperature changes.
20 Such reactors can be operated at a pressure o about 26 bar and at an associated gas feed (comprising make up gas and recycled gas) rate to obtain a desired reaction or operating temperature. In the context of the present ~i~92 invention it is said pressure which is raised, simultaneously with -the associa~ed gas feed rate, the relatlve or proportional rise in each case being measured against said pressure of about 26 bar and said associated feed rate. A pressure of about 30 bar has hitherto been accepted as being the optimum pressure for a fixed bëd Fischer-Tropsch reactor, and such a reactor (which can be operated at 26 bar as mentioned hereinbefore) is typically operated at about 28 10 bar to obtain the desired product spectrum.
The invention extends also to hydrocarbons when produced by a method as hereinbefore described.
The invention will now be described, by way of illustrative and non-limiting example only, with reference to the below-described tests 20 conducted by the Applicant.
EXAMPLE
Sasol One (Proprietary) Limited operates on a commercial scale at Sasolburg, South Africa, fixed vc~
~ed catalyst reactors comprising elongate tubes surxounded by a liquid cooling medium. The tubes are between about 6 and about 12 m long and have an internal diameter of about 5 cm. They are pacXed with a Fischer-Tropsch-type catalyst (eg an extruded precipitated iron catalyst having a surfaoe area (when fresh) of about 200 m2/gm), and are used for converting a CO+H2 synthesis gas into waxes by means of a Fischer-Tropsch reac'cion. The packed density of the catalyst in the reactors is 10 about 1 kg/litre of reactor, and about 20 kg o~
catalyst is packed into each reactor tube.
Reaction selectivity for wax production is promoted. As this selectivity decreases rapidly with increasLng reaction temperatures, temperature 15 rises above the desired operating temperatures (between 200C and 250~C)are kept to a minimum.
The reactors are normally operated at a pressure of about 30 bar, eg at 28 bar.
Three series of tests were conducted on the reactors, the operating pressure relative to the normal presssure being reduced to 26 bar and lncreased respectively to 4d and 60 bar. The rnake up gas feed rate was varied in proportion to the s~
pressuxe variations, relative to the normal make up gas feed rate associated with -the operating pre.ssure of 28 bar. Where necessary, the recycle gas stream rate was also raised 50 tha-t the gas linear velocity through the tubes at different S pressures was substantially the same as the linear velocity at the normal operating pressure of 28 bar. Results of these tests are shown in the accompanying drawings, in which:
Figure 1 shows a plot of the wax selectivity 10 of the reaction against time; and Figure 2 shows a plot of the percentage conversion (H2~CO) against time.
Figure 3 shows a plot of make up gas rate against operating pressure.
Figure l shows that a simultaneous and proportional increase in operating pressure and gas feed rate has no significant effect on wax selectivity or on the rate at which it decreases 20 in time; Figure 2 shows that a simultaneous and proportional increase in operating pressure and gas feed rate has no significant effect on the degree of conversion obtained or on the rate at which it decreases with time; and Figure 3 shows ~2~
that the make up gas feed rate is increased proportionally as the operating pressure is increased.
A significant and unexpected advantage o~ the invention is that the catalyst does not appear to age significantly faster at higher pressures, although more Fischer- Tropsch reaction products are being produced per unit time.
Furthermore, selectivity appears to be unaffected.
The Applicant expected from the literature (eg the article by R.B. Anderson in 'Catalysis', Vol. IV, P H Emmett - Editor, NY
Reinhold 1956) that an optimum operating pressure 15 for the fixed bed Fischer-Tropsch reaction would be in the region of 30 bar. It was assumed that a simultaneous raise in reactor pressure and gas feed rate would result in an increased reaction rate, and that the higher reaction rate would lead 20 to a temperature increase with a drop in wax selectivity, the higher temperature in turn increasing the reaction rate with the danger of a temperature run-away, catalyst coking and reactor blocking.
~2~
Without being bound by theory, the Applicant believes that the key to the unexpected success of the present invention is the use of the raised gas feed rate together with the raised pressure, ~he relative raise in the gas feed rate being about equal to the relative raise in ; pressure. The Applicant believes that the actuaL
linear velocity of the gas through the packed catalyst bed remains substantially unchanged, and this, together with the fact that the mass of gas 10 sweeplng past the catalyst particles has increased, ensures that the rate of heat exchange between the catalyst, the gas and the reactor walls remains high enough to cope with the additional reaction heat released.
Bearing in mind that as the percentage conversion (H2+CO) and selectivity appear to remain unchanged, the amount of wax produced per reactor tube per unit time appears to increase in 20 proportion with the raise in ga~ feed rate. This leads to the materiaL advantages, particularly in the light of the apparent absence of accelerated catalyst ageing, that fewer reactors are required and less catalyst is consumed per ton of wax ~. .
~o~
produced from the same feedstock. Furthermore, these advantages appear to be attainable in simple, easily applicable fashion, with no undue problems associated with the raise in pressure and gas feed rate. Although the tests have taken the pressure up to only 60 bar, higher pressures are in principle psssible, and the optimum pressure and feed rate for each particular application will be found by routine experimentation taking various economic and technical factors into account.
Similar results were obtained in tests in which the operating pressuxe was increased to about 35 and to about 50 bars.
According to one aspect of the-invention, there is provided a method of - 5 catalytically converting synthesis gas to hydrocarbons in a co~tinuous flxed bed catalyst reactor, which includes operating a continuous fixed bed catalyst reactor at a pressure above a pressure of about 26 bar and at a synthesis gas 10 feed rate above the gas feed rate characteristically used at a pressure of about 26 bar to obtain said hydrocarbons.
According to another aspect of the 15 invention, there is provided a me-thod of operating a continuous fixed bed catalyst reactor operable at a pressure of about 26 bar to convert syn-thesis yas to hydrocarbons at a fixed feed ratel which method includes raisiny the pressure to a level 20 above 26 bars while at the same time raising the feed rate above said fixed feed rate to obtain substantially the same type of hydrocarbons.
~ ;
According to yet another clspect of the invention, there is provided a method of increasing the reaction rate of a continuous fixed bed catalyst reactor above the reaction rate when it is operated at a pressure of about 26 bar to convert synthesis gas to hydrocarbons at a fixed feed rate, which method includes raising the pressure to a level above 26 bars while at the same time raising the feed rate above said fixed feed rate -to obtain subs-tantially the same type of 10 hydrocarbons, at an increased reaction ra-te.
The rise in the gas feed rate may be of the same order of magnitude as the rise in the pressure. The rises in the pressure and the gas 15 feed rate may be as high as a doubling or more of the pressure of about 26 bar and the feed rate characteristically used at that pressure or the fixed feed rate, respectively. Proportionally smaller rises can also lead to a higher reaction 20 rate.
The method may include converting a CO-~H2 synthesis gas in the reactor by means of a Fischer-Tropsch reaction r which may be of the type ~.Z~5~
used to produce Fischer~Tropsch waxes from the CO~H2 synthesis gas. The reactor may be a relatively elongate tubular packed catalyst fixed bed reactor surrounded by a liquid cooling medium.
The method may include effecting the reaction at a temperature between about 200C and about 250C.
The pressure may be at least 35 bar, preferably between 35 and about 60 bar.
The method may include feeding to the reactor a make up synthesis gas stream (comprising fresh gas) and, optional]y, a recycle synthesis gas stream (comprising unreacted exhaust gas), the rate of the make up stream being raised as the 15 pressure is raised and, when present, the rate of the recycle stream also being raised so that the linear velocity of the gas through the reactor remains substantially constant as the pressure is raisedO
For example, at said pressure of about 26 bar, the make up stream rate may be between about lO and about 40 normal cubic metres per hour (hereinafter referred to as "m3(n)/hr) per reactor ~2V5~
tube, and as the pressu.re is raise~ to about ~0 bar, the make up stream rate may be ralsed proportionally to between about 15 and about 60 m3 (n)/hr per reactor tube, and as the pressure is raised to about 60 bar, the make up stream rate 5 may be raised proportionally to between 23 and 92 m3(n)/hr per reactor tube.
It is to be understood that the aforementioned make up gas stream rates are 10 typical rates at the gi~en pressures. ~ccordingly the make up gas rate may also be below the lower rate hereinbefore mentioned or above the upper rate hereinbefore mentioned, at said pressure of about 26 bar~ and the make up rate will then be 15 raised proportionally as the pressure is raised above 26 bar.
It is further to be understood that, in a modificati.on of the invention, the recycle gas 20 stream rate can be raised to a lesser or greater extent so that linear velocity of the gas khrough the reactor at the elevated pressures is different to the linear velocity therethrough at the pressure of about 26 bar.
~c~
`
Typically, in fixed bed catalyst reactors of this type, the catalyst particles are relatively large (compared with ~hose of fluidized catalyst reactors used for simllar purposes) and remain stationary in the bed in use. Heat exchange between the particles and the reactor walls is relatively poor (compared with said fluidized bed reactors) and thexe is a danger that the particles will overheat when the reaction catalysed is exothermic. This overheating is generaLly 10 combatted by packing the catalyst in a plurality of smaller consecutive beds with cold gas or liquid injected between the heds to lower catalysk temperature, or the catalyst is packed into relatively long narrow tubes surrounded by a 15 liquid cooling medium.
Temperature control is important when the catalytic reaction, eg as regards its selectivity, is sensitive to temperature changes.
20 Such reactors can be operated at a pressure o about 26 bar and at an associated gas feed (comprising make up gas and recycled gas) rate to obtain a desired reaction or operating temperature. In the context of the present ~i~92 invention it is said pressure which is raised, simultaneously with -the associa~ed gas feed rate, the relatlve or proportional rise in each case being measured against said pressure of about 26 bar and said associated feed rate. A pressure of about 30 bar has hitherto been accepted as being the optimum pressure for a fixed bëd Fischer-Tropsch reactor, and such a reactor (which can be operated at 26 bar as mentioned hereinbefore) is typically operated at about 28 10 bar to obtain the desired product spectrum.
The invention extends also to hydrocarbons when produced by a method as hereinbefore described.
The invention will now be described, by way of illustrative and non-limiting example only, with reference to the below-described tests 20 conducted by the Applicant.
EXAMPLE
Sasol One (Proprietary) Limited operates on a commercial scale at Sasolburg, South Africa, fixed vc~
~ed catalyst reactors comprising elongate tubes surxounded by a liquid cooling medium. The tubes are between about 6 and about 12 m long and have an internal diameter of about 5 cm. They are pacXed with a Fischer-Tropsch-type catalyst (eg an extruded precipitated iron catalyst having a surfaoe area (when fresh) of about 200 m2/gm), and are used for converting a CO+H2 synthesis gas into waxes by means of a Fischer-Tropsch reac'cion. The packed density of the catalyst in the reactors is 10 about 1 kg/litre of reactor, and about 20 kg o~
catalyst is packed into each reactor tube.
Reaction selectivity for wax production is promoted. As this selectivity decreases rapidly with increasLng reaction temperatures, temperature 15 rises above the desired operating temperatures (between 200C and 250~C)are kept to a minimum.
The reactors are normally operated at a pressure of about 30 bar, eg at 28 bar.
Three series of tests were conducted on the reactors, the operating pressure relative to the normal presssure being reduced to 26 bar and lncreased respectively to 4d and 60 bar. The rnake up gas feed rate was varied in proportion to the s~
pressuxe variations, relative to the normal make up gas feed rate associated with -the operating pre.ssure of 28 bar. Where necessary, the recycle gas stream rate was also raised 50 tha-t the gas linear velocity through the tubes at different S pressures was substantially the same as the linear velocity at the normal operating pressure of 28 bar. Results of these tests are shown in the accompanying drawings, in which:
Figure 1 shows a plot of the wax selectivity 10 of the reaction against time; and Figure 2 shows a plot of the percentage conversion (H2~CO) against time.
Figure 3 shows a plot of make up gas rate against operating pressure.
Figure l shows that a simultaneous and proportional increase in operating pressure and gas feed rate has no significant effect on wax selectivity or on the rate at which it decreases 20 in time; Figure 2 shows that a simultaneous and proportional increase in operating pressure and gas feed rate has no significant effect on the degree of conversion obtained or on the rate at which it decreases with time; and Figure 3 shows ~2~
that the make up gas feed rate is increased proportionally as the operating pressure is increased.
A significant and unexpected advantage o~ the invention is that the catalyst does not appear to age significantly faster at higher pressures, although more Fischer- Tropsch reaction products are being produced per unit time.
Furthermore, selectivity appears to be unaffected.
The Applicant expected from the literature (eg the article by R.B. Anderson in 'Catalysis', Vol. IV, P H Emmett - Editor, NY
Reinhold 1956) that an optimum operating pressure 15 for the fixed bed Fischer-Tropsch reaction would be in the region of 30 bar. It was assumed that a simultaneous raise in reactor pressure and gas feed rate would result in an increased reaction rate, and that the higher reaction rate would lead 20 to a temperature increase with a drop in wax selectivity, the higher temperature in turn increasing the reaction rate with the danger of a temperature run-away, catalyst coking and reactor blocking.
~2~
Without being bound by theory, the Applicant believes that the key to the unexpected success of the present invention is the use of the raised gas feed rate together with the raised pressure, ~he relative raise in the gas feed rate being about equal to the relative raise in ; pressure. The Applicant believes that the actuaL
linear velocity of the gas through the packed catalyst bed remains substantially unchanged, and this, together with the fact that the mass of gas 10 sweeplng past the catalyst particles has increased, ensures that the rate of heat exchange between the catalyst, the gas and the reactor walls remains high enough to cope with the additional reaction heat released.
Bearing in mind that as the percentage conversion (H2+CO) and selectivity appear to remain unchanged, the amount of wax produced per reactor tube per unit time appears to increase in 20 proportion with the raise in ga~ feed rate. This leads to the materiaL advantages, particularly in the light of the apparent absence of accelerated catalyst ageing, that fewer reactors are required and less catalyst is consumed per ton of wax ~. .
~o~
produced from the same feedstock. Furthermore, these advantages appear to be attainable in simple, easily applicable fashion, with no undue problems associated with the raise in pressure and gas feed rate. Although the tests have taken the pressure up to only 60 bar, higher pressures are in principle psssible, and the optimum pressure and feed rate for each particular application will be found by routine experimentation taking various economic and technical factors into account.
Similar results were obtained in tests in which the operating pressuxe was increased to about 35 and to about 50 bars.
Claims (18)
1. A method of catalytically converting synthesis gas to hydrocarbons in a continuous fixed bed catalyst reactor, which includes operating a continuous fixed bed catalyst reactor at a pressure above a pressure of about 26 bar and at a synthesis gas feed rate above the gas feed rate characteristically used at a pressure of about 26 bar to obtain said hydrocarbons.
2. A method according to Claim 1 which includes converting a CO + H2 synthesis gas in the reactor by means of a Fischer Topsch reaction.
3. A method according to Claim 2 which includes effecting the reaction at a temperature between about 200°C and about 250°C, and wherein the pressure is at least 35 bar.
4. A method according to Claim 3 which includes feeding to the reactor a make up synthesis gas stream and,optionally, a recycle synthesis gas stream, the rate of the make up stream being raised as the pressure is raised, and, when present, the rate of the recycle stream also being raised, so that the linear velocity of the gas through the reactor remains substantially constant as the pressure is raised.
5. A method of operating a continuous fixed bed catalyst reactor operable at a pressure of about 26 bar to convert synthesis gas to hydrocarbons at a fixed feed rate, which method includes raising the pressure to a level above 26 bar while at the same time raising the feed rate above said fixed feed rate to obtain substantially the same type of hydrocarbons.
6. A method according to Claim 5 which includes converting a CO + H2 synthesis gas in the reactor by means of a Fischer Topsch reaction.
7. A method according to Claim 6 which includes effecting the reaction at a temperature between about 200°C and about 250°C, and wherein the pressure is at least 35 bar.
8. A method according to Claim 7 which includes feeding to the reactor a make up synthesis gas stream and,optionally, a recycle synthesis gas stream, the rate of the make up stream being raised as the pressure is raised, and, when present, the rate of the recycle stream also being raised, so that the linear velocity of the gas through the reactor remains substantially constant as the pressure is raised.
9. A method of increasing the reaction rate of a continuous fixed bed catalyst reactor above the reaction rate when it is operated at a pressure of about 26 bar to convert synthesis gas to hydrocarbons at a fixed feed rate, which method includes raising the pressure to a level above 26 bar while at the same time raising the feed rate above said fixed feed rate to obtain substantially the same type of hydrocarbons, at an increased reaction rate.
10. A method according to Claim 9, wherein the rise in the gas feed rate is of the same order of magnitude as the rise in the pressure.
11. A method according to Claim 9, which includes converting a CO+H2 synthesis gas in the reactor by means of a Fischer-Tropsch reaction.
12. A method according to Claim 11, which includes converting the synthesis gas in a relatively elongate tubular packed catalyst reactor surrounded by a liquid cooling medium.
13. A method according to Claim 11 which includes effecting the reaction at a temperature between about 200°C and about 250°C.
14. A method according to Claim 11, wherein the pressure is at least 35 bar.
15. A method according to Claim 14, wherein the pressure is between 35 and about 60 bar.
16. A method according to Claim 11 which includes feeding to the reactor a make up synthesis gas stream and,optionally, a recycle synthesis gas stream, the rate of the make up stream being raised as the pressure is raised, and, when present, the rate of the recycle stream also being raised, so that the linear velocity of the gas through the reactor remains substantially constant as the pressure is raised.
17. A method according to Claim 16 wherein, at said pressure of about 26 bar, the make up stream rate is between about 10 and about 40 m3(n)/hr per reactor tube, and as the pressure is raised to about 40 bar, the make up stream rate is raised proportionally to between about 15 and about 60 m3(n)/hr per reactor tube.
18. A method according to Claim 16 wherin at said pressure of about 26 bar, the make up stream rate is between about 10 and about 40 m3(n)/hr per reactor tube, and as the pressure is increased to about 60 bar, the make up stream rate is raised proportionally to between about 23 and about 92m3(n)/hr per reactor tube.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ZA823092 | 1982-05-05 | ||
| ZA82/3092 | 1982-05-05 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1205092A true CA1205092A (en) | 1986-05-27 |
Family
ID=25576056
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000427027A Expired CA1205092A (en) | 1982-05-05 | 1983-04-29 | Catalytic conversion of synthesis gas to hydrocarbons |
Country Status (4)
| Country | Link |
|---|---|
| AU (1) | AU561831B2 (en) |
| CA (1) | CA1205092A (en) |
| DE (1) | DE3316444A1 (en) |
| NZ (1) | NZ204095A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018144840A1 (en) * | 2017-02-06 | 2018-08-09 | Dow Global Technologies Llc | Processes for improving the activity of hybrid catalysts for fischer-tropsch reactions |
| WO2018146276A1 (en) * | 2017-02-10 | 2018-08-16 | Bp P.L.C. | Start-up procedure for a fischer-tropsch process |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ZA9711090B (en) * | 1996-12-13 | 1998-06-15 | Shell Int Research | Process for the preparation of hydrocarbons. |
| RU2212376C1 (en) * | 2002-04-10 | 2003-09-20 | Общество с ограниченной ответственностью "Научно-исследовательский институт природных газов и газовых технологий-ВНИИГАЗ" | Method of producing distillate fractions from furnace black production emission gases |
-
1983
- 1983-04-29 CA CA000427027A patent/CA1205092A/en not_active Expired
- 1983-05-03 NZ NZ204095A patent/NZ204095A/en unknown
- 1983-05-04 AU AU14220/83A patent/AU561831B2/en not_active Ceased
- 1983-05-05 DE DE19833316444 patent/DE3316444A1/en not_active Withdrawn
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018144840A1 (en) * | 2017-02-06 | 2018-08-09 | Dow Global Technologies Llc | Processes for improving the activity of hybrid catalysts for fischer-tropsch reactions |
| CN110234619A (en) * | 2017-02-06 | 2019-09-13 | 陶氏环球技术有限责任公司 | For promoting the active method of mixed catalyst for being used for the uncommon reaction of Fischer-Top |
| US10703689B2 (en) | 2017-02-06 | 2020-07-07 | Dow Global Technologies Llc | Processes for improving the activity of hybrid catalysts |
| CN110234619B (en) * | 2017-02-06 | 2022-06-21 | 陶氏环球技术有限责任公司 | Method for increasing the activity of mixed catalysts for fischer-tropsch reactions |
| WO2018146276A1 (en) * | 2017-02-10 | 2018-08-16 | Bp P.L.C. | Start-up procedure for a fischer-tropsch process |
| US10954450B2 (en) | 2017-02-10 | 2021-03-23 | Bp P.L.C. | Start-up procedure for a Fischer-Tropsch process |
| EA039032B1 (en) * | 2017-02-10 | 2021-11-24 | Бп П.Л.К. | Start-up procedure for a fischer-tropsch process |
| AU2018219673B2 (en) * | 2017-02-10 | 2023-11-23 | Bp P.L.C. | Start-up procedure for a fischer-tropsch process |
Also Published As
| Publication number | Publication date |
|---|---|
| AU561831B2 (en) | 1987-05-21 |
| AU1422083A (en) | 1983-11-10 |
| NZ204095A (en) | 1986-03-14 |
| DE3316444A1 (en) | 1983-11-10 |
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