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The invention relates to a device (10) for producing acetylene and synthesis gas by partially oxidizing hydrocarbons by means of oxygen. The device (10) comprises a reactor (12), wherein the reactor (12) has a burner block (14) having a combustion chamber for producing a composition Z1 containing at least acetylene and substituted acetylene, a first scrubber (22), which is designed to mix the composition Z1 with a solvent, a composition Z2 thus being obtained, a second scrubber (26), which is designed to mix the composition Z2 with the solvent, a composition Z3 thus being obtained, a first stripper (36), which is designed to strip the composition Z3, a composition Z4 containing the substituted acetylene, acetylene, and the solvent thus being obtained, and to separate the acetylene, a first column (46), which is designed to partially degas the composition Z4 at a pressure of 1.0 bar to 1.5, a composition Z5 and a first portion A1 of the solvent thus being obtained, a second stripper (56), to which the composition Z5 can be fed for stripping a composition Z9, a second portion A2 of the solvent and a composition Z6 thus being obtained, a third stripper (68), which is designed to strip the solvent from the first scrubber (22), a composition Z9 thus being obtained, a third stripper (68), which is designed to strip the solvent from the first scrubber (22), a composition Z9 thus being obtained, wherein the third stripper (68) is connected to the second stripper (56) in order to feed the composition Z9 to the second stripper (56), a device (72) for mixing the composition Z5 with a thinning gas, which device is arranged between the first column (46) and the second stripper (56), a second column (76), which is designed to mix the composition Z6 with water, a composition Z7 containing a third portion A3 of the solvent and water thus being obtained and a composition Z8 containing the substituted acetylene thus being obtained, and a direct-contact condenser (82), which is designed to mix the composition Z8 with water, a composition Z11 containing the substituted acetylene thus being obtained. The invention further relates to a method for producing acetylene and synthesis gas by partially oxidizing hydrocarbons by means of oxygen.

...

The invention relates to a method (10) for treating a synthesis gas from a gasification step, which includes: a step (105) of cooling the synthesis gas in order to condense heavy organic impurities and water; a step (110) of adsorption, at the end of the cooling step, of light organic impurities and inorganic impurities by at least one adsorption bed (230); a step (155) of separation, by decantation (135), of the water and heavy tars from the step (105) of cooling the synthesis gas; and a step (120) of regenerating at least one adsorption bed (230) by temperature-modulated or pressure-modulated desorption.

...
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Name Score Publications Conferences Grants Patents Trademarks News Webs
399.8 10 10 10 10 10 10 10
382.0 10 10 10 10 10 10 10
377.1 10 10 10 10 10 10 10
372.0 10 10 10 10 10 10 10
372.0 10 10 10 10 10 10 10
331.4 10 10 10 10 10 10 10
254.2 10 10 10 10 10 10 10
240.2 10 10 10 10 10 10 10
210.4 10 10 10 10 10 10 10
210.4 10 10 10 10 10 10 10
199.6 10 10 10 10 10 10 10
193.5 10 10 10 10 10 10 10
193.1 10 10 10 10 10 10 10
190.8 10 10 10 10 10 10 10
183.1 10 10 10 10 10 10 10
165.9 10 10 10 10 10 10 10
161.8 10 10 10 10 10 10 10
156.9 10 10 10 10 10 10 10
152.5 10 10 10 10 10 10 10
152.3 10 10 10 10 10 10 10
152.3 10 10 10 10 10 10 10
150.8 10 10 10 10 10 10 10
146.7 10 10 10 10 10 10 10
142.2 10 10 10 10 10 10 10
140.0 10 10 10 10 10 10 10
140.0 10 10 10 10 10 10 10
139.5 10 10 10 10 10 10 10
135.8 10 10 10 10 10 10 10
134.1 10 10 10 10 10 10 10
130.7 10 10 10 10 10 10 10
130.2 10 10 10 10 10 10 10
127.3 10 10 10 10 10 10 10
121.1 10 10 10 10 10 10 10
118.8 10 10 10 10 10 10 10
116.0 10 10 10 10 10 10 10
114.5 10 10 10 10 10 10 10
112.0 10 10 10 10 10 10 10
110.6 10 10 10 10 10 10 10
106.8 10 10 10 10 10 10 10
105.1 10 10 10 10 10 10 10
104.1 10 10 10 10 10 10 10
103.4 10 10 10 10 10 10 10
99.8 10 10 10 10 10 10 10
98.8 10 10 10 10 10 10 10
96.0 10 10 10 10 10 10 10
95.9 10 10 10 10 10 10 10
92.9 10 10 10 10 10 10 10
92.8 10 10 10 10 10 10 10
91.9 10 10 10 10 10 10 10
91.9 10 10 10 10 10 10 10
89.7 10 10 10 10 10 10 10
89.7 10 10 10 10 10 10 10
87.6 10 10 10 10 10 10 10
86.5 10 10 10 10 10 10 10
85.0 10 10 10 10 10 10 10
84.6 10 10 10 10 10 10 10
84.6 10 10 10 10 10 10 10
83.8 10 10 10 10 10 10 10
83.5 10 10 10 10 10 10 10
General Electric
82.5 6 3 - 10 10 10 10
Polytechnic of Milan
81.6 61 11 - 10 10 10 10
Korea Institute of Science and Technology
80.9 60 3 - 10 10 10 10
Mitsubishi Group
79.3 5 4 - 10 10 10 10
Massachusetts Institute of Technology
78.8 66 3 1 10 10 10 10
University of Toyama
77.7 49 1 - 10 10 10 10
Lurgi GMBH
77.0 2 2 - 10 10 10 10
Beijing University of Chemical Technology
75.4 56 2 - 10 10 10 10
Kunming University of Science and Technology
73.4 35 7 - 10 10 10 10
University of Saskatchewan
72.6 31 2 - 10 10 10 10
KTH Royal Institute of Technology
71.6 54 7 - 10 10 10 10
Chalmers University of Technology
71.6 37 7 - 10 10 10 10
South China University of Technology
71.4 50 3 - 10 10 10 10
National University of Singapore
71.2 43 2 - 10 10 10 10
TDA Research, Inc.
70.5 2 8 11 10 10 10 10
Tohoku University
70.5 66 8 - 10 10 10 10
Paul Scherrer Institute
70.0 53 7 - 10 10 10 10
Shanghai JiaoTong University
68.2 66 6 - 10 10 10 10
University of Chinese Academy of Sciences
67.5 198 14 - 10 10 10 10
UOP LLC
66.9 2 - - 10 10 10 10
Dalian University of Technology
66.6 64 5 - 10 10 10 10
Saudi Aramco
65.9 3 1 - 10 10 10 10
CSIC - National Coal Institute
65.8 21 1 - 10 10 10 10
Mississippi State University
65.7 23 8 - 10 10 10 10
Guradoor S.L.
65.7 - - - 10 10 10 10
Korea University
65.1 56 7 - 10 10 10 10
CSIRO
64.4 66 3 - 10 10 10 10
Lulea University of Technology
63.7 35 - - 10 10 10 10
National Cheng Kung University
62.1 35 2 - 10 10 10 10
Tianjin University
62.1 59 9 - 10 10 10 10
SABIC
60.8 3 1 - 10 10 10 10
Chulalongkorn University
60.8 38 17 - 10 10 10 10
University of Michigan
60.3 33 11 2 10 10 10 10
Japan National Institute of Advanced Industrial Science and Technology
60.2 64 1 - 10 10 10 10
Huazhong University of Science and Technology
59.9 57 4 - 10 10 10 10
Tianjin University of Technology
59.6 49 1 - 10 10 10 10
Pioneer Energy Inc.
59.3 - - - 10 10 10 10
CAS Institute of Engineering Thermophysics
58.8 59 18 - 10 10 10 10
Polytechnic University of Valencia
58.5 24 - - 10 10 10 10
University of Tokyo
58.1 51 3 - 10 10 10 10
Oklahoma State University
57.1 26 10 - 10 10 10 10

The invention relates to a device (10) for producing acetylene and synthesis gas by partially oxidizing hydrocarbons by means of oxygen. The device (10) comprises a reactor (12), wherein the reactor (12) has a burner block (14) having a combustion chamber for producing a composition Z1 containing at least acetylene and substituted acetylene, a first scrubber (22), which is designed to mix the composition Z1 with a solvent, a composition Z2 thus being obtained, a second scrubber (26), which is designed to mix the composition Z2 with the solvent, a composition Z3 thus being obtained, a first stripper (36), which is designed to strip the composition Z3, a composition Z4 containing the substituted acetylene, acetylene, and the solvent thus being obtained, and to separate the acetylene, a first column (46), which is designed to partially degas the composition Z4 at a pressure of 1.0 bar to 1.5, a composition Z5 and a first portion A1 of the solvent thus being obtained, a second stripper (56), to which the composition Z5 can be fed for stripping a composition Z9, a second portion A2 of the solvent and a composition Z6 thus being obtained, a third stripper (68), which is designed to strip the solvent from the first scrubber (22), a composition Z9 thus being obtained, a third stripper (68), which is designed to strip the solvent from the first scrubber (22), a composition Z9 thus being obtained, wherein the third stripper (68) is connected to the second stripper (56) in order to feed the composition Z9 to the second stripper (56), a device (72) for mixing the composition Z5 with a thinning gas, which device is arranged between the first column (46) and the second stripper (56), a second column (76), which is designed to mix the composition Z6 with water, a composition Z7 containing a third portion A3 of the solvent and water thus being obtained and a composition Z8 containing the substituted acetylene thus being obtained, and a direct-contact condenser (82), which is designed to mix the composition Z8 with water, a composition Z11 containing the substituted acetylene thus being obtained. The invention further relates to a method for producing acetylene and synthesis gas by partially oxidizing hydrocarbons by means of oxygen.


The invention relates to a method (10) for treating a synthesis gas from a gasification step, which includes: a step (105) of cooling the synthesis gas in order to condense heavy organic impurities and water; a step (110) of adsorption, at the end of the cooling step, of light organic impurities and inorganic impurities by at least one adsorption bed (230); a step (155) of separation, by decantation (135), of the water and heavy tars from the step (105) of cooling the synthesis gas; and a step (120) of regenerating at least one adsorption bed (230) by temperature-modulated or pressure-modulated desorption.


Patent
Lufthansa AG | Date: 2017-09-06

The invention relates to a method and plant for producing synthesis gas (3) from hydrocarbons (1). In the method, in a first step, hydrocarbons are split, using a plasma gas at high temperatures, into hydrogen (6) and carbon (5). Said product is mixed with steam (8) and carbon dioxide (9), and the carbon (5) is almost entirely converted to hydrogen and carbon monoxide in a temperature range from 800 C to 1700 C. Heat (10) is supplied to maximize the conversion. The product is then quenched (13). Synthesis gas (3) can be partially (3a) fed back and used as plasma gas. In further steps, such as Fischer-Tropsch synthesis, the synthesis gas (3) is further converted and then separated into various fractions.


Patent
Primus Green Energy Inc. | Date: 2017-02-09

The present invention provides apparatuses and processes for producing high octane fuel from synthesis gas. The process combines transalkylation and zeolite-forming/aromatization in conjunction with a single recycle loop configuration in order to effectively promote the fuel quality, particularly octane rating. The process involves adding a step for enriching octane of the fuel coming from the single recycle loop process. Preferably, the enrichment step takes place in an octane enrichment reactor containing two different catalysts, a zeolite-forming/aromatization catalyst followed by a transalkylation catalyst. The final fuel product preferably has an octane of about 92 to about 112.

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2. The process of claim 1 wherein the medium octane fuel is produced by i. passing the synthesis gas to convert synthesis gas to methanol and water, which produces a first exit through a first reactor stream; ii. passing the first exit stream through a second reactor to convert methanol to dimethylether, which produces a second exit stream; iii. passing the second exit stream through a third reactor to convert methanol and dimethylether to fuel and heavy gasoline, which produces a third exit stream; iv. passing the third exit stream through a fourth reactor to convert the heavy gasoline to isoparaffins, naphthenes, and less substituted aromatics, which produces a fourth exit stream; v. passing the fourth exit stream through a condenser to separate unreacted synthesis gas from the medium octane fuel; and vi. recycling the unreacted synthesis gas to the first reactor; wherein no removal or separation of the first, second or third exit streams are effected during steps a) to d).

3. The process of claim 1 wherein the medium octane fuel is produced by i. passing the synthesis gas through a first reactor to convert synthesis gas to methanol and water, which produces the first exit stream; ii. passing the first exit stream through a second reactor to convert methanol to dimethylether, which produces a second exit stream; iii. passing the second exit stream through a third reactor containing a third catalyst for converting methanol and dimethylether to fuel and heavy gasoline, and a fourth catalyst for converting the heavy gasoline to isoparaffins, naphthenes, and less substituted aromatics, which produces a third exit stream; iv. passing the third exit stream through a condenser to separate unreacted synthesis gas from the medium octane fuel; and v. recycling the unreacted synthesis gas, wherein no removal or separation of the first, second, or third exit streams are effected during steps a) to c).

13. The system of claim 12, wherein the single loop system for making a medium octane fuel comprises i. a first reactor containing a first catalyst for converting synthesis gas to methanol and water; ii. a second reactor containing a second catalyst for converting methanol to dimethylether; iii. a third reactor containing a third catalyst for converting methanol and dimethylether to fuel and heavy gasoline; iv. a fourth reactor containing a fourth catalyst for converting the heavy gasoline to isoparaffins, naphthenes, and less substituted aromatics; and v. a separator for separating a product exiting the third reactor into a first stream containing the medium octane fuel, a second stream containing water, and a third stream containing unreacted synthesis gas.

14. The system of claim 12, wherein the single loop system for making a medium octane fuel comprises i. a first reactor containing a first catalyst for converting synthesis gas to methanol and water; ii. a second reactor containing a second catalyst for converting methanol to dimethylether; iii. a third reactor to containing a third catalyst for converting methanol and dimethylether to fuel and heavy gasoline and a fourth catalyst for converting the heavy gasoline to isoparaffins, naphthenes, and less substituted aromatics; and iv. a separator for separating a product exiting the third reactor into a first stream containing the medium octane fuel, a second stream containing water, and a third stream containing unreacted synthesis gas.


Patent
IHI Corporation and Japan International Research Center For Agricultural Science | Date: 2017-03-22

A liquid fuel production method of the present invention includes: a saccharification step in which a biomass is saccharified; a methane fermentation step in which a saccharified liquid acquired in the saccharification step undergoes methane fermentation; and a biogas to liquid (BTL) step in which a liquid fuel is generated from a biogas acquired in the methane fermentation step.

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2. The liquid fuel production method according to claim 1, wherein the BTL step includes:a synthesis gas generation step in which a synthesis gas is generated from the biogas acquired in the methane fermentation step;an FT synthesis step in which the synthesis gas acquired in the synthesis gas generation step is subjected to a Fischer-Tropsch (FT) synthesis process; andan upgrade step in which an FT synthetic oil acquired in the FT synthesis step is subjected to an upgrade process.

3. The liquid fuel production method according to claim 2, wherein drainage water acquired in the FT synthesis step and the upgrade step is processed in the methane fermentation step.


The present invention provides a method and apparatus for producing liquid hydrocarbonaceous product (1) such as biofuel from solid biomass (2), the method comprising: gasifying solid biomass (2) in a gasifier (6) to produce raw synthesis gas (3); conditioning of the raw synthesis gas (3) to purify the raw synthesis gas (3) to obtain purified synthesis gas (4) having a molar ratio of hydrogen to carbon monoxide between 2.5 to 1 and 0.5 to 1, preferably between 2.1 to 1 and 1.8 to 1, more preferably about 2 to 1, the conditioning comprising removing sulfur species from the raw synthesis gas (3) using a guard bed reactor (25); and subjecting the purified synthesis gas (4) to a Fischer-Tropsch synthesis in a Fischer- Tropsch reactor (5) to produce liquid hydrocarbonaceous product (1); wherein the solid biomass (2) is fed to the gasifier (6) using a lock hopper (10).

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1. A method for producing liquid hydrocarbonaceous product (1) such as biofuel from solid biomass (2), the method comprising:feeding solid biomass (2) to a gasifier (6) using a lock hopper (10);gasifying the solid biomass (2) in the gasifier (6) to produce raw synthesis gas (3);conditioning the raw synthesis gas (3) to purify the raw synthesis gas (3) to obtain purified synthesis gas (4) having a molar ratio of hydrogen to carbon monoxide between 2.5 to 1 and 0.5 to 1, preferably between 2.1 to 1 and 1.8 to 1, more preferably about 2 to 1, the conditioning comprising removing sulfur species from the synthesis gas using a guard bed reactor (25); andsubjecting the purified synthesis gas (4) to a Fischer-Tropsch synthesis in a Fischer-Tropsch reactor (5) to produce liquid hydrocarbonaceous product (1).

2. A method according to claim 1, characterized in that the gasification step includes gasifying of solid biomass (2) in a gasifier (6) comprising a fluidized bed reactor, wherein oxygen (7) and steam (8) are used as fluidizing media in the fluidized bed reactor, and wherein tail gas (9) from the Fischer-Tropsch reactor (5) is preferably also used as a gasification and fluidizing medium in the fluidized bed reactor.

3. A method according to claim 1 or claim 2, characterized by feeding the raw synthesis gas (3) into a first particle separator (16) to separate particles such as ash, char and bed material from the raw synthesis gas (3),

4. A method according to claim 3, characterized by feeding the raw synthesis gas (3) from the first particle separator (16) to a second particle separator (17) for performing a dust separation step which lowers the dust content of the raw synthesis gas (3).

5. A method according to any of claims 1 to 4, characterized by the conditioning of the raw synthesis gas (3) including one or more of the following:catalytic treatment of the raw synthesis gas (3) in a reformer (18) for converting tar and methane present in the raw synthesis gas (3) into carbon monoxide and hydrogen;lowering the temperature of the raw synthesis gas (3) to about 250C in a cooler (19);filtering the raw synthesis gas (3) in a filter (20) to remove particles such as ash, entrained bed material and soot from the raw synthesis gas (3);subjecting the raw synthesis gas (3) to a water-gas-shift reaction in a water-to-gas shift reactor (20) to adjust the molar ratio of hydrogen to carbon monoxide to between 2.5 to 1 and 0.5 to 1, preferably between 2.1 to 1 and 1.8 to 1, more preferably about 2 to 1;scrubbing the raw synthesis gas (3) to remove solids and tar components from the raw synthesis gas (3); andan ultra-purification step for removing sulfur components, CO_(2) (carbon dioxide), H_(2)O (water), HCN (hydrogen cyanide), CH_(3)Cl (methyl chloride), carbonyls, Cl (chloride) and NO_(x) (nitrogen oxide) from the raw synthesis gas (3).

8. An apparatus for producing liquid hydrocarbonaceous product (1) such as biofuel from solid biomass (2), the apparatus comprising:a gasifier (6) for gasifying solid biomass (2) to produce raw synthesis gas (3);a lock hopper (10) for feeding the solid biomass (2) to the gasifier (6);means for conditioning the raw synthesis gas (3) to obtain purified synthesis gas (4) having a molar ratio of hydrogen to carbon monoxide between 2.5 to 1 and 0.5 to 1, preferably between 2.1 to 1 and 1.8 to 1, more preferably about 2 to 1, the conditioning means comprising a guard bed reactor (25) for removing sulfur species from the synthesis gas; anda Fischer-Tropsch reactor (5) for subjecting the purified synthesis gas (4) to a Fischer-Tropsch synthesis to produce liquid hydrocarbonaceous product (1).

9. An apparatus according to claim 8, characterized in that the gasifier (6) includes a fluidized bed reactor and means for feeding oxygen (7) and steam (8) into the gasifier (6) for use as fluidizing media in the fluidized bed reactor, and the apparatus preferably includes means for feeding tail gas from the Fischer-Tropsch reactor (5) into the gasifier (6) for use as a fluidizing medium in the fluidized bed reactor.

11. An apparatus according to any of claims 8 to 10, characterized by comprising a first particle separator (16) for separating particles such as ash, char and bed material particles from the raw synthesis gas (3).

12. An apparatus according to claim 11, characterized by comprising a second particle separator (17) downstream of the first particle separator (16) for separating dust from the raw synthesis gas (3).

13. An apparatus according to any of claims 8 to 11, characterized by comprising one or more of the following:a reformer (18) for catalytic treatment of the raw synthesis gas (3) to convert tar and methane present in the raw synthesis gas (3) into carbon monoxide and hydrogen;a cooler (19) for lowering the temperature of the raw synthesis gas (3) to about 250C.a filter (20) for removing ash, entrained bed material and/or soot from the raw synthesis gas (3);a water-gas-shift reactor (21) for adjusting the molar ratio of hydrogen and carbon monoxide in the raw synthesis gas (3) to between 2.5 to 1 and 0.5 to 1, preferably between 2.1 to 1 and 1.8 to 1, more preferably about 2 to 1;a scrubber (22) for removing solids and tar components from the raw synthesis gas (3); andultra-purification means (23) for removing sulfur components, CO_(2) (carbon dioxide), H_(2)O (water), HCN (hydrogen cyanide), CH_(3)Cl (methyl chloride), carbonyls, Cl (chloride) and NO_(x) (nitrogen oxide) from the raw synthesis gas (3).

14. An apparatus according to claim 13, characterized by comprising ultra-purification means (23) and a compressor (24) for raising the pressure of the raw synthesis gas (3) to about 30 to 40 bar pressure before leading the raw synthesis gas (3) into the ultra-purification means (23).


Patent
CCP Technology GmbH | Date: 2015-05-13

A method for producing -rich synthesis gas comprises the following steps: decomposing a hydrocarbon-containing fluid into an H_(2)/C-aerosol in a first hydrocarbon converter by supplying energy which is at least partly provided in the form of heat; introducing at least a first stream of the H_(2)/C-aerosol into a first sub-process which comprises the following steps: directing at least a part of the H_(2)/C-aerosol from the first hydrocarbon converter into a first C-converter; introducing CO_(2 )into the first C-converter and mixing the CO_(2 )with the H_(2)/C-aerosol introduced into the first C-converter; converting the mixture of H_(2)/C-aerosol and CO_(2 )into a synthesis gas at a temperature of 800 to 1700 C.; mixing additional H_(2 )with the synthesis gas for the production of H_(2)-rich synthesis gas. In a second sub-process running in parallel with the first sub-process, hydrogen H_(2 )and carbon dioxide CO_(2 )are produced from a hydrocarbon-containing fluid, wherein at least a portion of the CO_(2 )produced in the second sub-process is introduced into the first C-converter; and wherein at least a portion of the H_(2 )produced in the second sub-process is mixed with the synthesis gas from the first C-converter. The CO_(2 )which is needed for the conversion of C in the first C-converter can thereby be provided independently of an external source, and the entire operational sequence is easily controllable.

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18. A method for producing H _(2)-rich synthesis gas comprising the following steps: decomposing a hydrocarbon-containing fluid into an H_(2)/C-aerosol in a first hydrocarbon converter (9, 9) by supplying energy which is at least partly provided in the form of heat; introducing at least a first stream of the H_(2)/C aerosol into a first sub-process which comprises the following steps: directing at least a part of the H_(2)/C-aerosol from the first hydrocarbon converter (9, 9) into a first C converter (14). introducing CO_(2 )into the first C-converter (14) and mixing the CO_(2 )with the H_(2)/C-aerosol introduced into the first C-converter (14); converting the mixture of H_(2)/C-aerosol and CO_(2 )into a synthesis gas at a temperature of 800 to 1700 C.; mixing additional H_(2 )with the synthesis gas for producing H_(2)-rich synthesis gas; producing the additional hydrogen H_(2 )and the carbon dioxide CO_(2 )from a hydrocarbon-containing fluid in a second sub-process running in parallel with the first sub-process, wherein the CO_(2 )and a portion of the additional H_(2 )produced in the second sub-process are produced from CO and H_(2)O by a water-gas-shift-reaction, and wherein the CO which is introduced into the water-gas-shift-reaction is produced in a second C-converter (30) from carbon C and water H_(2)O at a temperature of 800 to 1700 C.; wherein the CO_(2 )produced in the second sub-process is introduced into the first C-converter (14); and wherein only a portion of the additional H_(2 )produced in the second sub-process is mixed with the synthesis gas from the first C-converter (14).

23. The method according to claim 18, wherein the ratio of CO to H _(2 )in the H _(2)-rich synthesis gas is set to a value of greater than 1:1 to 1:3.

24. The method according to claim 18, wherein the ratio of CO to H _(2 )in the H-rich synthesis gas is set to a value of approximately 1:2.1.

25. A method for producing synthetic hydrocarbons in which an H _(2)-rich synthesis gas is produced by a method in accordance with claim 18, and wherein the H _(2)-rich synthesis gas is brought into contact with a catalyst and the temperature of the catalyst and/or that of the synthesis gas is controlled or regulated within a pre-determined temperature range in order to produce synthetic functionalised and/or non-functionalised hydrocarbons.

27. An apparatus ( 1) for producing H _(2)-rich synthesis gas which comprises at least one first hydrocarbon converter ( 9, 9) for decomposing a hydrocarbon-containing fluid into an H _(2)/C-aerosol which comprises at least one process chamber having at least one hydrocarbon inlet ( 11) for a hydrocarbon-containing fluid and at least one first aerosol outlet ( 12) for a H _(2)/C-aerosol and at least one unit for bringing energy into the process chamber, wherein the energy consists at least partly of heat; wherein the apparatus (1) further comprises a first group of converters (3) for the implementation of a first sub-process and a second group of converters (5) for the implementation of a second sub-process, wherein the first group of converters (3) comprises the following a first C-converter (14) for the conversion of C and CO_(2 )into CO, wherein the first C-converter (14) comprises at least one further process chamber having at least one CO_(2 )inlet (16) for CO_(2), at least one aerosol inlet (15) for an H_(2)/C-aerosol and at least one outlet (17), wherein the aerosol inlet (15) of the first C-converter (14) is connected directly to the at least one aerosol outlet (12) of the first hydrocarbon converter (9, 9); a first mixer (20) which comprises a synthesis gas inlet that is connected to the outlet (17) of the first C-converter (14) and an H_(2 )inlet for additional H_(2 )and the mixer being adapted for mixing incoming synthesis gas and additional H_(2 )to form an H_(2)-rich synthesis gas; wherein the second croup of converters (5) comprises a second CO-converter (37) which is suitable for implementing a water-gas-shift-reaction in which CO and H_(2)O are converted into CO_(2 )and H_(2), and wherein the second CO-converter (37) has at least one CO_(2 )outlet (41) for CO_(2 )and an H_(2 )outlet (40) for H_(2 )and at least one inlet (38) for at least synthesis gas, wherein the outlet (41) for CO_(2 )is connected to the CO_(2 )inlet (16) of the first C-converter (14); wherein the H_(2 )outlet (40) is connected to the H_(2 )inlet of the mixer (20); wherein a H_(2 )line (24) is connected at a point between the second CO-converter (37) and the mixer (20) for feeding off H_(2); and wherein the second group of converters (5) comprises a second C-converter (30) for the conversion of C and H_(2)O into CO and H_(2), wherein the second C-converter (30) comprises at least one process chamber having at least one H_(2)O inlet (32) for H_(2)O, at least one aerosol inlet (31) for H_(2)/C-aerosol and at least one outlet (33) for synthesis gas, and wherein the outlet (33) for synthesis gas of the second C-converter (30) is connected to the inlet (38) for at least synthesis gas of the second CO-converter (37).

28. The apparatus ( 1) according to claim 27, wherein the inlet ( 38) for at least synthesis gas is provided (or the purposes of introducing the H _(2)O and the synthesis gas together into the second CO-converter ( 30); or wherein the second CO-converter ( 30) composes a separate H _(2)O-inlet ( 32) for introducing the H _(2)O separately from the synthesis gas.

33. An apparatus ( 2) or producing synthetic functionalised and/or non-functionalised hydrocarbons which comprises an apparatus according to claim 27; and a first CO-converter ( 7) which comprises a process chamber in which a catalyst is arranged and further comprises at least one inlet ( 22) for synthesis gas which is connected to the outlet ( 17) of the first C-converter ( 14) c to the mixer ( 20), means for directing a synthesis gas into contact with the catalyst, and a control unit to controlling or regulating the temperature of the catalyst and/or that of the synthesis gas at a pre-determined temperature.


The present invention provides an apparatus and a method which are suitable for producing an organic substance using a synthesis gas from a waste gasification furnace. The apparatus 1 for producing an organic substance from waste comprises a synthesis gas generation furnace 11 for generating a synthesis gas by partial oxidation of the waste; and an organic substance production unit 12 for producing an organic substance from the synthesis gas. The organic substance production unit 12 further comprises: a synthesis unit 13 for synthesizing an organic substance by subjecting the synthesis gas to catalytic reaction in the presence of a metal catalyst, and a fermenter 14 for producing an organic substance by subjecting the synthesis gas to microbial fermentation.

Claims which contain your search:

1. An apparatus for producing an organic substance from waste, comprising:a synthesis gas generation furnace for generating a synthesis gas by partial oxidation of the waste; andan organic substance production unit for producing an organic substance from the synthesis gas,the organic substance production unit further comprising:a synthesis unit for synthesizing an organic substance by subjecting the synthesis gas to catalytic reaction in the presence of a metal catalyst, anda fermenter for producing an organic substance by subjecting the synthesis gas to microbial fermentation.

2. The apparatus according to claim 1, wherein the fermenter is connected downstream of the synthesis unit.

4. The apparatus according to claim 1 or 2, wherein the organic substance synthesized in the synthesis unit and the organic substance produced in the fermenter are different from each other.

5. An apparatus for producing an organic substance from waste, comprising:a synthesis gas generation furnace for generating a synthesis gas by partial oxidation of the waste; andan organic substance production unit for producing an organic substance from the synthesis gas,the organic substance production unit further comprising:a synthesis unit for synthesizing a first organic substance by subjecting the synthesis gas to catalytic reaction in the presence of a metal catalyst, anda fermenter for producing a second organic substance by subjecting the first organic substance to microbial fermentation, the fermenter being connected in series to the synthesis unit.

7. A method for producing an organic substance from waste, comprising:a synthesis gas-generating step for generating a synthesis gas by partial oxidation of waste; andan organic substance-producing step for producing an organic substance from the synthesis gas,the organic substance-producing step further comprising:a synthesizing step for synthesizing an organic substance by subjecting the synthesis gas to catalytic reaction in the presence of a metal catalyst in a synthesis unit; anda fermentation step for producing an organic substance by subjecting the synthesis gas to microbial fermentation in a fermenter.

11. A method for producing an organic substance from waste, comprising:a synthesis gas-generating step for generating a synthesis gas by partial oxidation of waste; andan organic substance-producing step for producing an organic substance from the synthesis gas,the organic substance-producing step further comprising:a synthesizing step for synthesizing a first organic substance by subjecting the synthesis gas to catalytic reaction in the presence of a metal catalyst in a synthesis unit; anda fermentation step for producing a second organic substance by subjecting the first organic substance to microbial fermentation in a fermenter which is connected in series to the synthesis unit.


The present invention provides an apparatus and a method which can be used for producing an organic substance effectively from a synthesis gas obtained from a waste incinerator. The apparatus 1 for producing an organic substance from waste, comprises a synthesis gas generation furnace 11, a fermenter 13, and a nutrient feeder. The synthesis gas generation furnace 11 generates a synthesis gas by partial oxidation of waste. The fermenter 13 contains a microorganism which produces an organic substance from the synthesis gas. The nutrient feeder 12 feeds a solid or liquid nutrient to the fermenter 13 when an amount of the synthesis gas supplied to the fermenter 13 is insufficient.

Claims which contain your search:

1. An apparatus for producing an organic substance, comprising:a synthesis gas generation furnace for generating a synthesis gas by partial oxidation of waste;a fermenter containing a microorganism which produces an organic substance from the synthesis gas; anda nutrient feeder for feeding a solid or liquid nutrient to the fermenter when an amount of the synthesis gas supplied to the fermenter is insufficient.

2. The apparatus according to claim 1, wherein the nutrient feeder feeds the nutrient to the fermenter when the amount of the synthesis gas supplied to the fermenter is insufficient for one day or more.

5. A method for producing an organic substance, comprising:a synthesis gas generation step of generating a synthesis gas by partial oxidation of waste in a synthesis gas generation furnace;a step of allowing a microorganism to produce an organic substance from the synthesis gas in a fermenter; anda nutrient feeding step of feeding a solid or liquid nutrient to the fermenter when an amount of the synthesis gas supplied to the fermenter is insufficient.

6. The method according to claim 5, wherein the solid or liquid nutrient is fed to the fermenter in the nutrient feeding step when the amount of the synthesis gas supplied to the fermenter is insufficient for one day or more.


Patent
CCP Technology GmbH | Date: 2017-05-03

A method for producing -rich synthesis gas comprises the following steps: decomposing a hydrocarbon- containing fluid into an H2/C-aerosol in a first hydrocarbon converter by supplying energy which is at least partly provided in the form of heat; introducing at least a first stream of the H2/C-aerosol into a first sub-process which comprises the following steps: directing at least a part of the H2/C-aerosol from the first hydrocarbon converter into a first C-converter; introducing CO2 into the first C-converter and mixing the CO2 with the H2/C-aerosol introduced into the first C-converter; converting the mixture of H2/C-aerosol and CO2 into a synthesis gas at a temperature of 800 to 1700C; mixing additional H2 with the synthesis gas for the production of H2-rich synthesis gas. In a second sub-process running in parallel with the first sub-process, hydrogen H2 and carbon dioxide CO2 are produced from a hydrocarbon-containing fluid, wherein at least a portion of the CO2 produced in the second sub-process is introduced into the first C-converter; and wherein at least a portion of the H2 produced in the second sub-process is mixed with the synthesis gas from the first C-converter. The CO2 which is needed for the conversion of C in the first C-converter can thereby be provided independently of an external source, and the entire operational sequence is easily controllable.

Claims which contain your search:

1. A method for producing H2-rich synthesis gas comprising the following steps: decomposing a hydrocarbon-containing fluid into an H2/C-aerosol in a first hydrocarbon converter (9, 9) by supplying energy which is at least partly provided in the form of heat; introducing at least a first stream of the H2/C-aerosol into a first sub-process which comprises the following steps: directing at least a part of the H2/C-aerosol from the first hydrocarbon converter (9, 9) into a first C-converter (14); introducing C02 into the first C-converter (14) and mixing the C02 with the H2/C-aerosol introduced into the first C-converter (14); converting the mixture of H2/C-aerosol and C02 into a synthesis gas at a temperature of 800 to 1700C; mixing additional H2 with the synthesis gas for producing H2-rich synthesis gas; producing hydrogen H2 and carbon dioxide C02 from a hydrocarbon-containing fluid in a second sub-process running in parallel with the first sub-process, wherein the C02 and a portion of the H2 in the second sub-process are produced from CO and H20 by a water-gas-shift-reaction, and wherein the CO which is introduced into the water-gas-shift-reaction is produced in a second hydrocarbon converter (30, 25/30) from carbon C and water H20 at a temperature of 800 to 1700C; wherein the C02 produced in the second sub-process is introduced into the first C-converter (14); and wherein only a portion of the H2 produced in the second sub-process is mixed with the synthesis gas from the first C-converter (14).

6. The method according to any of the preceding Claims, wherein the ratio of CO to H2 in the H2- rich synthesis gas is set to a value of greater than 1 : 1 to 1 :3, in particular to a value of approximately 1 :2.1.

7. A method for producing synthetic hydrocarbons in which an H2-rich synthesis gas is produced by a method in accordance with any of Claims 1 to 6, and wherein the H2-rich synthesis gas is brought into contact with a catalyst and the temperature of the catalyst and/or that of the synthesis gas is controlled or regulated within a pre-determined temperature range in order to produce synthetic functionalised and/or non-functionalised hydrocarbons.

9. An apparatus (1) for producing H2-rich synthesis gas which comprises at least one first hydrocarbon converter (9, 9) for decomposing a hydrocarbon-containing fluid into an H2/C-aerosol which comprises at least one process chamber having at least one hydrocarbon inlet (11) for a hydrocarbon-containing fluid and at least one first aerosol outlet (12) for a H2/C-aerosol and at least one unit for bringing energy into the process chamber, wherein the energy consists at least partly of heat; wherein the apparatus (1) further comprises a first group of converters (3) for the implementation of a first sub-process and a second group of converters (5) for the implementation of a second sub- process, wherein the first group of converters (3) comprises the following: a first C-converter (14) for the conversion of C and C02 into CO, wherein the first C-converter (14) comprises at least one further process chamber having at least one C02 inlet (16) for C02, at least one aerosol inlet (15) for an H2/C-aerosol and at least one outlet (17), wherein the aerosol inlet (15) of the first C-converter (14) is connected directly to the at least one aerosol outlet (12) of the first hydrocarbon converter (9, 9); a first mixer (20) which comprises a synthesis gas inlet that is connected to the outlet (17) of the first C-converter (14) and an H2 inlet for additional H2 and the mixer being adapted for mixing incoming synthesis gas and additional H2 to form an H2-rich synthesis gas; wherein the second group of converters (5) comprises a second CO-converter (37) which is suitable for implementing a water-gas-shift-reaction in which CO and H20 are converted into C02 and H2, and wherein the second CO-converter (37) has at least one C02 outlet (41) for C02 and an H2 outlet (40) for H2 and at least one inlet (38) for at least synthesis gas, wherein the outlet (41) for C02 is connected to the C02 inlet (16) of the first C-converter (14); and wherein the H2 outlet (40) is connected to the H2 inlet of the mixer (20); and wherein the second group of converters (5) comprises a second C-converter (30) for the conversion of C and H20 into CO and H2, wherein the second C-converter (30) comprises at least one process chamber having at least one H20-inlet (32) for H20, at least one aerosol inlet (31) for H2/C-aerosol and at least one outlet (33) for synthesis gas, and wherein the outlet (33) for synthesis gas of the second C-converter (30) is connected to the inlet (38) for at least synthesis gas of the second CO-converter (37).

10. The apparatus (1) according to Claim 9, wherein the inlet (38) for at least synthesis gas is provided for the puiposes of introducing the H20 and the synthesis gas together into the second CO- converter (30); or wherein the second CO-converter (30) comprises a separate H20-inlet (32) for introducing the H20 separately from the synthesis gas.

15. An apparatus (2) for producing synthetic functionalised and/or non-functionalised hydrocarbons which comprises an apparatus according to any of the Claims 9 to 14; and a first CO-converter (7) which comprises a process chamber in which a catalyst is arranged and further comprises at least one inlet (22) for synthesis gas which is connected to the outlet (17) of the first C-converter (14) or to the mixer (20), means for directing a synthesis gas into contact with the catalyst, and a control unit to controlling or regulating the temperature of the catalyst and/or that of the synthesis gas at a pre-determined temperature.