CN112938896A - Process and process system for synthesis gas preparation and waste heat recovery - Google Patents
Process and process system for synthesis gas preparation and waste heat recovery Download PDFInfo
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- CN112938896A CN112938896A CN201911277528.2A CN201911277528A CN112938896A CN 112938896 A CN112938896 A CN 112938896A CN 201911277528 A CN201911277528 A CN 201911277528A CN 112938896 A CN112938896 A CN 112938896A
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- 239000007789 gas Substances 0.000 title claims abstract description 119
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 70
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 70
- 239000002918 waste heat Substances 0.000 title claims abstract description 28
- 238000011084 recovery Methods 0.000 title claims abstract description 24
- 238000002360 preparation method Methods 0.000 title claims abstract description 16
- 238000000034 method Methods 0.000 title abstract description 26
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 30
- 230000003197 catalytic effect Effects 0.000 claims abstract description 29
- 230000003647 oxidation Effects 0.000 claims abstract description 27
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 20
- 239000002994 raw material Substances 0.000 claims description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 239000001301 oxygen Substances 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- 239000004215 Carbon black (E152) Substances 0.000 claims description 11
- 239000000571 coke Substances 0.000 claims description 11
- 230000005611 electricity Effects 0.000 claims description 11
- 229930195733 hydrocarbon Natural products 0.000 claims description 11
- 150000002430 hydrocarbons Chemical class 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 9
- 239000003345 natural gas Substances 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/10—Adaptations for driving, or combinations with, electric generators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
- F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/06—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using mixtures of different fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
- C01B2203/0216—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step containing a non-catalytic steam reforming step
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a synthesis gas preparation and waste heat recovery process and a process system. The process system comprises a non-catalytic partial oxidation chamber and one or more turbine chambers, wherein a synthesis gas outlet of the non-catalytic partial oxidation chamber is communicated with a synthesis gas inlet of the turbine chambers through a pipeline; the turbine chamber comprises a casing, a power turbine positioned in the casing, a support shaft of the power turbine, and a power output shaft fixedly connected with the support shaft; the power output shaft is connected with the turbine generator; and a synthesis gas outlet of the turbine chamber is connected with a steam generator, and a steam outlet of the steam generator is connected with a turbine generator. The process system can prepare the synthesis gas and efficiently utilize the waste heat of the synthesis gas, and has simple process and high safety.
Description
Technical Field
The invention relates to a synthesis gas preparation and waste heat recovery process and a process system.
Background
The preparation of synthetic gas by utilizing the non-catalytic partial oxidation process of gaseous hydrocarbon substances is an important method for preparing synthetic gas in the chemical production process, and the gaseous hydrocarbon substances can be natural gas, coke oven gas, raw coke oven gas, refinery gas and the like. The synthesis gas is prepared by non-catalytic partial oxidation of gaseous hydrocarbon substances, and the raw materials of the gaseous hydrocarbon substances, air/oxygen, water vapor and the like are mainly introduced into a converter, and a series of chemical reactions occur in a hearth to generate the synthesis gas. In the conventional process, sensible heat of high-temperature synthesis gas is usually recovered by using a waste heat boiler, and steam generated by the waste heat boiler can enter a steam turbine to generate electricity. However, the waste heat boiler is used for recovering heat and the steam turbine is used for generating electricity, so that the process is complex and the heat utilization rate is low. In addition, a large amount of heat can be released in the process of generating the synthesis gas, so that the temperature of the generated synthesis gas is as high as about 1300 ℃, the heat-resisting temperature of the waste heat boiler is usually only 800-900 ℃, and in the process of recovering the heat, the waste heat boiler is difficult to bear higher temperature, is easy to damage and has poor safety.
Disclosure of Invention
The invention aims to overcome the defects of complex high-temperature synthesis gas heat recovery process, low heat utilization rate, poor safety and the like in the traditional process for preparing synthesis gas, and provides a synthesis gas preparation and waste heat recovery process and a process system. The process system for preparing the synthesis gas can effectively recover the heat of the high-temperature synthesis gas, and has simple process and high safety.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a synthesis gas preparation and waste heat recovery process system, which comprises a non-catalytic partial oxidation chamber and one or more turbine chambers, wherein a synthesis gas outlet of the non-catalytic partial oxidation chamber is communicated with a synthesis gas inlet of the turbine chamber through a pipeline; the turbine chamber comprises a casing, a power turbine positioned in the casing, a support shaft of the power turbine, and a power output shaft fixedly connected with the support shaft, wherein the power output shaft is connected with a turbine generator; and a synthesis gas outlet of the turbine chamber is connected with a steam generator, and a steam outlet of the steam generator is connected with a turbine generator.
In the present invention, the non-catalytic partial oxidation chamber may be a reformer for producing syngas by a non-catalytic partial oxidation process, which is conventionally used in the art, and the reformer may be a top burner or a side wall burner.
In the present invention, the casing is preferably a volute structure, which facilitates the extraction of the syngas.
In the present invention, the power turbine may be a one-stage or multi-stage power turbine. The power turbine may be an axial flow turbine and a radial turbine, preferably an axial flow turbine. The turbine blades of the power turbine are preferably provided with film cooling structures. The power turbine is preferably a multi-stage axial flow turbine with film cooling.
In the present invention, the connection mode between the power output shaft and the turbine generator may be: the power output shaft is directly connected with the turbine generator; alternatively, the power output shaft is connected to the turbine generator through a gearbox.
In the present invention, the steam generator may be a steam generator conventional in the art, which may heat water to generate steam using heat of the syngas exiting from the outlet of the turbine chamber. The steam generating device is preferably a boiler.
In the present invention, the turbine generator may be a turbine generator conventional in the art, which generates electricity by being driven by a turbine. The steam turbine generator may be a steam turbine generator conventional in the art, which utilizes steam propulsion to generate electricity.
The invention also provides a synthesis gas preparation and waste heat recovery process, which is carried out in the synthesis gas preparation and waste heat recovery process system and comprises the following steps:
(1) carrying out non-catalytic partial oxidation reaction on the feed gas in the non-catalytic partial oxidation chamber to generate synthesis gas;
(2) the synthesis gas enters the turbine chamber to push the power turbine to do work, and the power output shaft drives the turbine generator to generate power;
(3) the synthesis gas enters the steam generator through the outlet of the turbine chamber, and the steam generator generates steam to push the turbine generator to generate electricity;
wherein the feed gas comprises (a) gaseous hydrocarbon material, (b) air and/or oxygen.
In the invention, the gaseous hydrocarbon material can be one or more of natural gas, shale gas, coal bed gas, coke oven gas, raw coke oven gas and refinery gas. The methane content of the gaseous hydrocarbon material is preferably in the range of 5% to 100%.
In the present invention, the raw material gas preferably further comprises (c) water vapor.
In the present invention, when natural gas, oxygen and water vapor are used as raw materials, the volume ratio of the natural gas, the oxygen and the water vapor is preferably 1: (0.65-0.85): (0 to 0.4).
In the present invention, when coke oven gas, oxygen and water vapor are used as raw materials, the volume ratio of the coke oven gas, the oxygen and the water vapor is preferably 1: (0.175-0.275): (0 to 0.1), preferably 1:0.23: 0.023.
In the present invention, the temperature of the raw material gas at the raw material gas inlet of the non-catalytic partial oxidation chamber may be 90 to 250 ℃, preferably 220 ℃. The higher the temperature, the more oxygen consumption can be saved.
In the present invention, the pressure in the non-catalytic partial oxidation chamber may be 1.0 to 8.0MPa, preferably 6.5 MPa.
In the present invention, the temperature in the non-catalytic partial oxidation chamber may be 1200 to 1350 ℃, preferably 1300 ℃.
In the present invention, no catalyst is present in the non-catalytic partial oxidation chamber.
In the present invention, the pressure of the synthesis gas at the synthesis gas inlet of the turbine chamber may be 1.0 to 8.0MPa, preferably 6.5 MPa. The pressure of the synthesis gas at the synthesis gas outlet of the turbine chamber may be 0.1 to 0.5 times the pressure of the synthesis gas at the synthesis gas inlet of the turbine chamber.
In the present invention, the temperature of the syngas at the syngas inlet of the turbine chamber may be 1200 to 1350 ℃, preferably 1300 ℃.
In the present invention, the temperature of the synthesis gas at the synthesis gas outlet of the turbine chamber may be 300 to 700 ℃, preferably 500 to 600 ℃.
In the invention, the temperature of the synthesis gas at the synthesis gas outlet of the water vapor generator can be 120-180 ℃, and preferably 140-160 ℃.
In the present invention, the synthesis gas may comprise carbon monoxide and hydrogen. When the gaseous hydrocarbon material is natural gas, the volume ratio of carbon monoxide to hydrogen is preferably 1: (1.7-2.6).
On the basis of the common knowledge in the field, the above preferred conditions can be combined randomly to obtain the preferred embodiments of the invention.
The reagents and starting materials used in the present invention are commercially available.
The positive progress effects of the invention are as follows: the synthesis gas preparation and waste heat recovery process and the process system integrate the turbine generator and the turbine generator, adopt the turbine chamber to recover the heat of the high-temperature synthesis gas synthesized in the non-catalytic partial oxidation chamber, directly utilize the high-temperature synthesis gas to push the turbine blades to do work to generate electricity, further use the synthesis gas from the turbine chamber to generate steam to push the turbine generator to generate electricity, and have high waste heat utilization rate, simple process and high safety.
Drawings
Fig. 1 is a schematic diagram of a synthesis gas preparation and waste heat recovery process system according to embodiment 1 of the present invention.
Fig. 2 is a schematic structural view of the turbine chamber of fig. 1 according to the present invention.
Description of reference numerals:
a non-catalytic partial oxidation chamber 1;
the turbine chamber 2, the casing 21, the power turbine 22, the support shaft 23 and the power output shaft 24;
a gear case 3;
a turbine generator 4;
a steam generator 5;
a turbo generator 6.
Detailed Description
The invention is further illustrated by the following examples, which are not intended to limit the scope of the invention. The experimental methods without specifying specific conditions in the following examples were selected according to the conventional methods and conditions, or according to the commercial instructions.
Example 1
A synthesis gas preparation and waste heat recovery process system, the structure schematic diagram of which is shown in fig. 1 and fig. 2. The synthesis gas preparation and waste heat recovery process system comprises a non-catalytic partial oxidation chamber 1 and a turbine chamber 2, wherein a synthesis gas outlet of the non-catalytic partial oxidation chamber 1 is communicated with a synthesis gas inlet of the turbine chamber 2 through a pipeline; the turbine chamber 2 comprises a casing 21, a power turbine 22 and a supporting shaft 23 thereof positioned in the casing 21, and a power output shaft 24 fixedly connected with the supporting shaft 23, wherein the power output shaft 24 is connected with the turbine generator 4 through a gear box 3; the synthesis gas outlet of the turbine chamber 2 is connected with a steam generator 5, and the steam outlet of the steam generator 5 is connected with a turbine generator 6. The casing 21 is a volute structure, and the power turbine 22 is a multi-stage axial flow turbine with film cooling.
An example of using the process system to prepare syngas and recover waste heat is as follows:
(1) will be generated from coke oven gas (7.5 ten thousand Nm3H), oxygen (17270 Nm)3H) and water vapor (1740 Nm)3The raw material gas consisting of the raw material gas and the catalyst is introduced into a non-catalytic partial oxidation chamber 1 without the catalyst to carry out non-catalytic partial oxidation reaction to generate synthesis gas; wherein the temperature of the raw material gas at the raw material gas inlet of the non-catalytic partial oxidation chamber 1 is 220 ℃, the pressure in the non-catalytic partial oxidation chamber 1 is 6.5MPa, and the temperature is 1300 ℃.
(2) The synthetic gas enters the turbine chamber 2 to push the power turbine 22 to do work, and the power output shaft 24 and the gear box 3 drive the turbine generator 4 to generate electricity; wherein the pressure of the synthesis gas at the synthesis gas inlet of the turbine chamber 2 is 6.5MPa, and the temperature is 1300 ℃; the pressure of the synthesis gas at the synthesis gas outlet of the turbine chamber 2 is 0.8MPa, and the temperature is 525 ℃; the inlet and outlet enthalpy difference of the synthesis gas in the turbine chamber 2 is 38.1 MW.
(3) The synthetic gas enters a steam generator 5 through the outlet of the turbine chamber 2, the steam generator 5 generates 8.0MPaG saturated steam with the enthalpy value of 13.2MW for 20.8t/h, the steam turbine generator 6 is pushed to generate electricity, and the temperature of the synthetic gas at the synthetic gas outlet of the steam generator 5 is 140 ℃.
The generating efficiency of the turbine generator is 80%, the generating efficiency of the turbine generator is 50%, and the output electric power is 38.1 × 0.8+13.2MW × 0.5-37 MW.
From coke oven gas (7.5 ten thousand Nm) using methods conventional in the art3H), oxygen (17270 Nm)3H) and water vapor (1740 Nm)3The synthesis gas is prepared from raw material gas consisting of the raw material gas and is connected with a fire tube boiler behind a converter to generate 8.0MPaG saturated steam with the enthalpy of 86t/h (55.4 MW) to drive the steam turbine generator to generate electricity, the generating efficiency of the steam turbine is 50%, and the output electric power is 55.4MW multiplied by 0.5 MW which is 27.7 MW. Compared with the conventional method, the power generation of the process system disclosed by the invention is increased by 34%. Therefore, the process system can prepare the synthesis gas and efficiently utilize the waste heat of the synthesis gas.
Claims (10)
1. A synthesis gas preparation and waste heat recovery process system comprises a non-catalytic partial oxidation chamber and one or more turbine chambers, wherein a synthesis gas outlet of the non-catalytic partial oxidation chamber is communicated with a synthesis gas inlet of the turbine chambers through a pipeline; the turbine chamber comprises a casing, a power turbine positioned in the casing, a support shaft of the power turbine, and a power output shaft fixedly connected with the support shaft, wherein the power output shaft is connected with a turbine generator; and a synthesis gas outlet of the turbine chamber is connected with a steam generator, and a steam outlet of the steam generator is connected with a turbine generator.
2. The syngas production and heat recovery process system of claim 1, wherein the non-catalytic partial oxidation chamber is a top burner furnace or a side wall burner furnace;
and/or the casing is of a volute structure, so that the synthesis gas can be led out conveniently.
3. The syngas production and heat recovery process system of claim 1, wherein the power turbine is a one-stage or multi-stage power turbine;
and/or, the power turbine is an axial flow turbine and a radial turbine, preferably an axial flow turbine;
and/or an air film cooling structure is arranged on the turbine blade of the power turbine.
4. The syngas production and heat recovery process system of claim 3, wherein the power turbine is a multi-stage axial flow turbine with film cooling.
5. The syngas production and heat recovery process system of claim 1, wherein the power output shaft is directly connected to the turbine generator; alternatively, the power output shaft is connected to the turbine generator through a gearbox.
6. A synthesis gas preparation and waste heat recovery process carried out in the synthesis gas preparation and waste heat recovery process system of any one of claims 1 to 5, comprising the steps of:
(1) carrying out non-catalytic partial oxidation reaction on the feed gas in the oxidation chamber to generate synthesis gas;
(2) the synthesis gas enters the turbine chamber to push the power turbine to do work, and the power output shaft drives the turbine generator to generate power;
(3) the synthesis gas enters the steam generator through the outlet of the turbine chamber, and the steam generator generates steam to push the turbine generator to generate electricity;
wherein the feed gas comprises (a) gaseous hydrocarbon material, (b) air and/or oxygen.
7. The syngas production and waste heat recovery process of claim 6, wherein the gaseous hydrocarbon is one or more of natural gas, coke oven gas, raw gas and refinery gas;
and/or the methane content of the gaseous hydrocarbon material ranges from 5% to 100%.
8. The syngas production and waste heat recovery process of claim 7,
the feed gas further comprises (c) steam;
when natural gas, oxygen and water vapor are used as raw materials, the volume ratio of the natural gas to the oxygen to the water vapor is 1: (0.65-0.85): (0 to 0.4);
when coke oven gas, oxygen and water vapor are used as raw materials, the volume ratio of the coke oven gas, the oxygen and the water vapor is 1: (0.175-0.275): (0 to 0.1), preferably 1:0.23: 0.023.
9. The syngas production and waste heat recovery process of claim 6,
the temperature of the raw material gas at the raw material gas inlet of the non-catalytic partial oxidation chamber is 90-250 ℃, and preferably 220 ℃;
and/or the pressure in the non-catalytic partial oxidation chamber is 1.0-8.0 MPa, preferably 6.5 MPa;
and/or the temperature in the non-catalytic partial oxidation chamber is 1200-1350 ℃, preferably 1300 ℃.
10. The syngas production and waste heat recovery process of claim 6,
the pressure of the synthetic gas at the synthetic gas inlet of the turbine chamber is 1.0-8.0 MPa, preferably 6.5 MPa;
and/or the pressure of the synthetic gas at the synthetic gas outlet of the turbine chamber is 0.1-0.5 times of the pressure of the synthetic gas at the synthetic gas inlet of the turbine chamber;
and/or the temperature of the synthesis gas at the synthesis gas inlet of the turbine chamber is 1200-1350 ℃, preferably 1300 ℃;
and/or the temperature of the synthetic gas at the synthetic gas outlet of the turbine chamber is 300-700 ℃, preferably 500-600 ℃;
and/or the temperature of the synthetic gas at the synthetic gas outlet of the water vapor generator is 120-180 ℃, preferably 140-160 ℃.
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| CN201911277528.2A CN112938896A (en) | 2019-12-11 | 2019-12-11 | Process and process system for synthesis gas preparation and waste heat recovery |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4099383A (en) * | 1976-06-21 | 1978-07-11 | Texaco Inc. | Partial oxidation process |
| CN1891619A (en) * | 2005-07-05 | 2007-01-10 | 通用电气公司 | Syngas turbine |
| CN102923657A (en) * | 2012-11-16 | 2013-02-13 | 华东理工大学 | Method capable of recovering heat and used for producing synthesis gas through oxidation of non-catalytic part of gaseous hydrocarbon |
| CN203383889U (en) * | 2013-06-07 | 2014-01-08 | 德州学院 | Waste-gas turbine generator of automobile |
| CN108313981A (en) * | 2018-04-03 | 2018-07-24 | 西安交通大学 | A kind of solar hydrogen electricity methanol with joint production energy-storage system and its application method |
| CN211496937U (en) * | 2019-12-11 | 2020-09-15 | 华东理工大学 | Process system for synthesis gas preparation and waste heat recovery |
-
2019
- 2019-12-11 CN CN201911277528.2A patent/CN112938896A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4099383A (en) * | 1976-06-21 | 1978-07-11 | Texaco Inc. | Partial oxidation process |
| CN1891619A (en) * | 2005-07-05 | 2007-01-10 | 通用电气公司 | Syngas turbine |
| CN102923657A (en) * | 2012-11-16 | 2013-02-13 | 华东理工大学 | Method capable of recovering heat and used for producing synthesis gas through oxidation of non-catalytic part of gaseous hydrocarbon |
| CN203383889U (en) * | 2013-06-07 | 2014-01-08 | 德州学院 | Waste-gas turbine generator of automobile |
| CN108313981A (en) * | 2018-04-03 | 2018-07-24 | 西安交通大学 | A kind of solar hydrogen electricity methanol with joint production energy-storage system and its application method |
| CN211496937U (en) * | 2019-12-11 | 2020-09-15 | 华东理工大学 | Process system for synthesis gas preparation and waste heat recovery |
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