前苏联专利SU1442066A3 Method of producing mixture of methanol and c sub two

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专利摘要:
A process for the production of a "fuel grade" mixture of methanol and higher alcohols from CO and H2. To reduce the amount of water contained in the mixture coming from the synthesis reactor of the alcohol synthesis the reaction product is cooled and fed to a secondary reactor wherein the reaction of conversion: CO+H2O-><-CO2+H2 is conducted in conditions near to equilibrium. The further reaction product is cooled down further so as to obtain a liquid phase constituted by the alcohols, and in which there are still dissolved some gases, and a gaseous phase containing the carbon dioxide produced in the secondary reactor together with the non-reacted gases. The gaseous phase is sent to a section of absorption of the CO2 wherein the absorbing liquid is constituted by the very alcoholic mixture produced; after removal of the CO2 the gas is partly recycled and partly let off in order to avoid the accumulation of inert gases contained in the feeding mixture. Before being used in the section of absorption of the CO2, the alcoholic mixture is sent into a stripping column to remove the gases dissolved therein; the let off gases are used as stripping agents. In the secondary reactor of conversion operation is carried out at a temperature comprised between 150 DEG C. and 250 DEG C., at a pressure equal to that of the synthesis reactor and in the presence of a copper catalyst.
公开号:SU1442066A3
申请号:SU813285557
申请日:1981-05-15
公开日:1988-11-30
发明作者:Ди Пьетро Рафаэль；Паггини Альберто；Лагана Винченцо
申请人:Снампрогетти С.П.А. (Фирма)；
IPC主号:

专利说明:

Oj
The invention relates to methods for producing a mixture of methanol and € {-04-alcohols, which can be used as a fuel by itself or in a mixture with gasoline.
The aim of the invention is to reduce the content of higher hydrocarbons in the mixture and to improve the quality of the target product.
This goal is achieved by the interaction of a gas mixture containing 25-47 vol.% CO and 47-60 vol.% H, at a temperature of 250-415 C and a pressure of 80- 260 atm in the presence of a catalyst of composition, wt.%:
ZnO 65.8
28.3
Sio 1.7
K20 0.9
MpOz 3,3 or ZnO 60,85
CuO 1.45
37.70 or ZnO 72.1
25.9
KiO2.0
or ZnO 50.4
AljOj 10.2
,one
CuO37,3
at a flow rate of the gas mixture of 7065-20900, h followed by cooling the resulting reaction mixture containing methanol, C-C alcohols, unreacted gases and water, cooled to 165-195 ° C and further interaction at 165-200 C pressure 80-260 ATM in the presence of a catalyst composition, wt.%:
ZnO 24.9-31.4
36.7-49.9
CuO 18.7-38.4 with a mixture flow rate of 3073-13125 h followed by cooling the resulting mixture to 10-50 ° C, separating it into a liquid phase containing a mixture of methanol and C-C4 alcohols of a fuel grade and a gaseous phase containing CO , CO and H, which is directed to the absorption of COj, and further recycling 97% of the gas phase purified from CO to the first stage of interaction, directing the remaining 3% of the purified gas phase to the stage of desorption of gases dissolved in the liquid phase and then the atmosphere, the direction obtained after the separation of the liquid phases to the stage of desorption of dissolved gases from it, and then its absorption of carbon dioxide from the gaseous phase supplied by the countercurrent, then removing carbon dioxide from the liquid phase and refining the target mixture of fuel grade alcohol.
The drawing shows the implementation of the proposed method.
Synthesis gas 1 and recirculated gas 3 are brought to operating pressure and fed through line 2 to reactor 17, the reaction product leaves the synthesis reactor through line 4 and after cooling to 18, it is directed to co-conversion reactor 19, where the water content in it is noticeably reduced.
The reacted gas leaves the conversion reactor through line 5, after which it is first sent to heat recuperator 20, then to condenser 21, and then to separator 22, from the head part of which the gaseous phase is regenerated through node 6, which is first cooled in heat recuperator 24 and using a refrigeration cycle 25, and then sent to the carbon dioxide absorption section of the column.
From the head of column 23, a line of carbon dioxide-free gas is taken through line 7, which is partially recirculated for synthesis using 3, and partially unloaded and directed along line 8 to column 27, where an absorbent solution is prepared that is sent to the column. 23.
From the base of the separator 22, the liquid phase, consisting of a fuel-grade alcohol mixture, which is used as the absorbing fluid in the column 23, is regenerated through the node 10.
Since the liquid contains some more dissolved gas, it is sent to a stripping column 27, into which the discharged gases enter as desorbing 1x agents, which are discharged through the node 9, through node 8.
The purified liquid is withdrawn from the column 27 by means of a pump 28 and line 11 and the said liquid is sent after cooling in paragraphs 29 and 30 to the absorption column 23.
From the bottom of this column, the alcohol mixture containing almost all of the dioxide is discharged using node 12
carbon, previously contained in the recirculation gas, and now dissolved, the liquid is regenerated and freed from carbon dioxide and from other dissolved gases by evaporation in a turbine and collected in a separator 26, from which carbon dioxide is removed from the head portion with 14 with other gases, the liquid, which possibly still contains some traces of carbon dioxide, is heated in the node 29 and finally sent 13 to the separator 31, from the bottom of which is obtained with the help of 16 the desired alcohol mixture of the fuel that, whereas from the head portion is discharged via 15 last traces of carbon dioxide.
Example 1. The compositions of the initial gas streams, intermediate reaction mixtures and final products for different points are given in table. 1. At the synthesis stage, 10 catalysts of the following composition are used.
m

72.1 25.9 2.0
Temperature, pressure 260 atm, hourly “1a gas velocity 7064.9. The reaction mixture after the synthesis reactor is cooled to a temperature and sent to the Conversion reactor, in which 20 m of catalyst composition is used, wt.%:
ZnO 31.4
CrrOz 49.9
CCA 18.7
Temperature 200 C, pressure 260 atm, gas hourly gas velocity 3073.4.
The product after the conversion reactor is cooled to 10 ° C to obtain a liquid and gaseous phase. The liquid phase containing a certain amount of dissolved gases is sent to the desorber, and the gaseous phase is sent to the carbon dioxide absorption column, where the purified liquid phase flows in countercurrently. The liquid phase after the absorption column is adjusted to a lower pressure and collected in a separator to obtain a mixture of fuel grade of the composition shown in table. 1 The mixture has a color index of APNA-30 (American Healthcare Association).
ten
PRI mme R 2. The process is carried out according to the scheme shown in the drawing.
Synthesis reaction The composition of the catalyst, may.%:
ZnO 65.8
SgdOz 28.3
Sio 1.7
0.9
MnOj 3.3
100 ata (9.9 MPa)
15
Pressure Temperature Volume of catalyst Volume Reaction rate of conversion, mash, wt.%: ZnO
375-415 ° C 20 m 11140 h - Composition katali20
Cr-jiO}
Cuo
Pressure
24.9 36.7 38.4
100 ATA (9.9 MPa) 1b5-168 from 20 m
one

Temperature Volume of catalyst 25 Bulk speed 10520 h
The index of the color of the reaction mixture after the conversion of ARNA-90.
The material balance of the example is given in table. 2
30 The temperature of the cooling downstream of the reactor is the conversion of the reaction mass to 20 ° C. Example 3 Synthesis reaction
The composition of the catalyst, wt.%:
oo
40
five
10 m
20900 h
-t
0
Catalyst volume
Volumetric reaction rate of conversion.
The composition of the catalyst:, wt.X:
ZnO 28.6
40.7
SIO 30.7
Pressure
five
Temperature Volume of catalyst
Volumetric speed
150 ATA (14.9 MPa) 195-198 С
15 m
13125 h
The temperature of the cooling ambassador of the reactor, the conversion of the reaction mixture 40
The chromaticity index is reactive after the stage of conversion of state 85 APNA.
The material balance is given in table. 3
PRI me R 4.
A gas-gas mixture of the following composition is fed to the synthesis reactor:
Nmz / h
Carbon monoxide carbon dioxide CO 2
47.52 55218.20 23.76
Hydrogen Hj 158170.21 Nitrogen N2 7460.63 Methane CH4 t6608.23 MeOH 71.45. In the synthesis reactor, the catal has the following composition, May

before
65.90 3.28 7.36
1.22 0.01 0.02
0.09 0.006
0.08
This reaction product is cooled to 50 ° C to cure liquid and gas.
The shaped phase, the solid phase containing some dissolved gases is sent to the stripper, and the gaseous phase is sent to the carbon dioxide absorption column.
In this column absorption post
pressure is 80 atm, temperature is 165 C.
A product is discharged from the conversion reactor:
% by
volume
CO 47924.85 21.10 SOA 2112.33 0.93
55
Color index ARNA-95.
The proposed method allows to improve the quality of the target mixture of fuel grade alcohols in comparison with the known method due to a decrease in the yield of hydrocarbons compared to alcohols, an improvement in the color of CMP.SI
one
a deck whose color is less than 100 APHA (in the known more than 100 APHA), as well as an improvement in odor (in a known method, sulfur compounds are present in the mixture). The resulting mixtures contain very little water (less than 200 parts per million).
The liquid mixture of methanol and alcohols obtained by the proposed method has a transparency comparable to that of industrially produced gasolines, it has no edges with 1 substance and an unpleasant smell that are found in alcohol mixtures obtained by Fischer-Tropsch synthesis.

权利要求:
Claims (1)
[1]
Invention Formula
20
CuO 18.7-38.4 with a mixture flow rate of 3073-13125 h, the resulting reaction mixture containing methanol, Cj-C alcohols, unreacted gases, and a method for producing a mixture of methanol and.-Alcohols of the fuel grade based on the interaction of carbon monoxide and hydrogen at elevated temperature and pressure in the presence of a catarrhal phase containing a mixture of metacompound alkaline gas and traces of water, cooled to 10–50 ° C, and then divided into
The LIZ atom containing the metal metal, characterized in that, in order to reduce the content of higher hydrocarbons, improve the quality of the target product, the gas mixture containing 25-47 vol, 7, CO and 47-60 vol.% H, is subjected interaction at a temperature of 250-415 C and a pressure of 80-260 bar in the presence of a catalyst composition, wt.%:
iola and C, -C 4-alcohols in the fuel variety, and to the gaseous phase containing CO, CO g and H, which is directed to CO absorption, and 97% purified
30 CO i gas phase is recycled to the first stage of interaction, the remaining 3% of the purified gaseous phase is directed to the desorption stage dissolved in the liquid phase.
35 gases and then discharged to atmospheres the liquid phase obtained after separation is directed to the stage of desorption of dissolved gases from it, which are then used as desorbents, and then
Zno
Cuo
K-iO
MnOz ZnO
Cuo
whether ZnO
,
65.8 28.3
1.7
0.9
3.3
60.85
1.45
37.70
72.1
25.9
eight
2.0 50.4 10.2 2.1 37.3
or ZnO A1.0
five
0
at a gas flow rate of 7065-20900 h, the resulting reaction mixture containing methanol, C2-C4 alcohols, unreacted gases and water is cooled to 165-195 C and subjected to further interaction at a temperature of 1–5–200 C and a pressure of 80– 260 atm in the presence of a catalyst composition, wt.%:
ZnO 24.9-31.4
36.7-49.9
CuO 18.7-38.4 at a flow rate of 3073-13125 h of the mixture, the resulting reaction mixture containing methanol, Cj-C is alcohols, unreacted gases, an aggressive phase containing a mixture, a meta-phase containing a mixture of meta-
ventilated gas and traces of water, cooled to 10-50 ° C, and then divided into
the liquid phase containing the meta
iola and C, -C 4 -alcohol-grade alcohols, and to a gaseous phase containing CO, CO g and H, which is directed to CO absorption, and 97% purified from
The CO i gas phase is recycled to the first reaction stage, the remaining 3% of the purified gas phase is directed to the desorption stage dissolved in the liquid phase.
gases and then dumped into the atmosphere, the liquid phase obtained after separation is directed to the stage of desorption of dissolved gases from it, then used as desorbents, and then to absorb carbon dioxide from the gaseous phase supplied by countercurrent, then carbon dioxide is removed from the liquid phase target mixture of methanol and C-C alcohols is isolated
fuel grade.
"
EX
about
TO
1 tables 2
Table EG
:

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同族专利:

公开号 | 公开日

NZ196806A|1984-03-16|

ZA813274B|1982-05-26|

ES502752A0|1982-04-01|

DE3119306C2|1984-04-19|

GB2076423A|1981-12-02|

IE51105B1|1986-10-01|

BR8102808A|1982-02-02|

AT379580B|1986-01-27|

PH16550A|1983-11-16|

AU543346B2|1985-04-18|

DE3119306A1|1982-03-04|

LU83366A1|1982-01-20|

FI811517L|1981-11-17|

PL129214B1|1984-04-30|

FR2482584A1|1981-11-20|

BE888799A|1981-11-16|

NL8102404A|1981-12-16|

ATA179881A|1985-06-15|

RO82284A|1983-08-03|

ES8204760A1|1982-04-01|

US4460378A|1984-07-17|

DD158913A5|1983-02-09|

KR840001860B1|1984-10-23|

GR75228B|1984-07-13|

KR830006406A|1983-09-24|

IT8022117D0|1980-05-16|

TR20809A|1982-09-16|

FI75142B|1988-01-29|

YU121281A|1983-04-30|

NO811644L|1981-11-17|

GB2076423B|1984-07-04|

FR2482584B1|1984-05-04|

IE810787L|1981-11-16|

DK203681A|1981-11-17|

CU21284A3|1985-12-16|

FI75142C|1988-05-09|

CS224613B2|1984-01-16|

EG15388A|1986-09-30|

RO82284B|1983-07-30|

CH648342A5|1985-03-15|

NO154171B|1986-04-21|

CA1159256A|1983-12-27|

SE8103073L|1981-11-17|

IT1148864B|1986-12-03|

PL231186A1|1981-12-23|

IN155671B|1985-02-23|

SE451142B|1987-09-07|

NO154171C|1986-07-30|

AU7059081A|1981-11-19|

JPS5710690A|1982-01-20|

JPH0232312B2|1990-07-19|

引用文献:

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

BE342014A|

US1791568A|1923-02-22|1931-02-10|Ig Farbenindustrie Ag|Manufacture of oxygenated organic compounds|

US1569775A|1924-09-04|1926-01-12|Basf Ag|Synthetic manufacture of methanol|

US2010005A|1932-04-06|1935-08-06|Du Pont|Motor fuel|

US2281228A|1939-03-03|1942-04-28|Solvay Process Co|Process for synthesizing methanol|

DE824038C|1949-11-10|1951-12-10|Basf Ag|Process for the production of isobutyl alcohol|

DE936715C|1950-12-10|1955-12-22|Linde Eismasch Ag|Process for purifying gases by deep freezing|

DE944186C|1950-12-22|1956-06-07|Basf Ag|Process for the production of hydrogen-containing synthesis gases|

US2964551A|1957-03-27|1960-12-13|Ici Ltd|Production of unsaturated hydrocarbons and methanol|

DE1442981A1|1963-07-30|1969-01-02|Basf Ag|Process for the production of hydrogen|

GB1159035A|1965-08-18|1969-07-23|Ici Ltd|Methanol Synthesis.|

FR1521405A|1966-01-22|1968-04-19|Metallgesellschaft Ag|Process for the partial elimination of carbon dioxide in the gases used for the synthesis of methanol|

DE1290123B|1966-11-11|1969-03-06|Union Rheinische Braunkohlen|Process for the continuous purification of methanol synthesis gas|

US3950369A|1968-04-08|1976-04-13|Imperial Chemical Industries Limited|Methanol production|

US3940428A|1968-12-30|1976-02-24|Imperial Chemical Industries Limited|Methanol production|

US3763205A|1971-05-10|1973-10-02|Du Pont|Methanol process with recycle|

CA1136114A|1978-05-15|1982-11-23|Harley F. Hardman|Preparation of alcohols from synthesis gas|

EP0011404B1|1978-11-10|1982-12-29|Imperial Chemical Industries Plc|Integrated process for synthesis of methanol and of ammonia|

DE2904008C2|1979-02-02|1988-03-17|Linde Ag, 6200 Wiesbaden, De|US4787915A|1981-03-24|1988-11-29|Carbon Fuels Corporation|Method of varying rheology characteristics of novel coal derived fuel system|

IT1169281B|1981-12-02|1987-05-27|Assoreni & Snamprogetti Spa|CATALYTIC SYSTEM AND PROCEDURE FOR THE PRODUCTION OF METHANOL MIXTURES AND HIGHER ALCOHOLS|

FR2529544B1|1982-07-05|1987-11-13|Inst Francais Du Petrole|ALCOHOL PRODUCT FROM SYNTHETIC GAS|

US4705532A|1985-07-15|1987-11-10|The Standard Oil Company|Alcohol compositions for blending with gasoline|

US4762858A|1985-09-16|1988-08-09|The Dow Chemical Company|Syngas conversion to oxygenates by reduced yttrium/lanthanide/actinide-modified catalyst|

JP2560311B2|1987-02-27|1996-12-04|三菱瓦斯化学株式会社|Method for producing methanol or mixed alcohol|

DE3810421A1|1988-03-26|1989-10-05|Union Rheinische Braunkohlen|IMPROVED METHOD FOR CATALYTICALLY PRODUCING AN ALCOHOL MIXTURE WITH INCREASED ISOBUTANOL CONTENT|

IT1276931B1|1995-10-13|1997-11-03|Snam Progetti|PROCEDURE FOR PRODUCING MIXTURES OF METHANOL AND HIGHER ALCOHOLS|

DE69831261D1|1997-10-28|2005-09-22|Univ Kansa Ct For Res Inc|FUEL MIXTURE FOR COMPRESSION SPARKERS WITH LIGHT SYNTHETIC RAW AND MIXED COMPONENTS|

US20080260631A1|2007-04-18|2008-10-23|H2Gen Innovations, Inc.|Hydrogen production process|

法律状态:

优先权:

申请号 | 申请日 | 专利标题

IT22117/80A|IT1148864B|1980-05-16|1980-05-16|PROCESS FOR THE PRODUCTION OF A MIXTURE OF METHANOL AND HIGHER ALCOHOLS FUEL DEGREE|

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