CN217556132U - Gasification furnace system using hydrogen as cooling gas and adjusting gas - Google Patents
Gasification furnace system using hydrogen as cooling gas and adjusting gas Download PDFInfo
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- CN217556132U CN217556132U CN202220550413.7U CN202220550413U CN217556132U CN 217556132 U CN217556132 U CN 217556132U CN 202220550413 U CN202220550413 U CN 202220550413U CN 217556132 U CN217556132 U CN 217556132U
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Abstract
The utility model provides a gasification furnace system using hydrogen as cooling gas and adjusting gas, which comprises a hydrogen compression device and a gasification furnace which are communicated with each other; the gasification furnace comprises: the gasification chamber, the chilling mixing chamber and the synthesis gas cooler are communicated in sequence; the hydrogen compression device is communicated with the chilling mixing chamber; forming high-temperature synthesis gas in a state that raw materials enter a gasification chamber for gasification reaction, wherein the high-temperature synthesis gas enters a chilling mixing chamber from the gasification chamber, is mixed with low-temperature hydrogen and is cooled to form crude synthesis gas; the raw synthesis gas enters a synthesis gas cooler from the chilling mixing chamber, is cooled through water-cooling indirect heat exchange to form low-temperature raw synthesis gas, and flows out of the gasification furnace; the gasification furnace system directly adjusts the H/C atomic ratio in the gasification furnace, omits the water gas shift process, simultaneously cools the crude synthesis gas in the gasification furnace, and avoids the high-temperature fly ash from being bonded on the heat exchange surface of the synthesis gas cooler to form ash deposit.
Description
Technical Field
The utility model belongs to the field of coal chemical industry, in particular to a gasification furnace system using hydrogen as cooling gas and adjusting gas.
Background
The powdered coal pressure gasification technology is a clean and high-efficiency advanced technology for converting various solid fuels such as coal, petroleum coke and the like into synthesis gas with main components of hydrogen and carbon monoxide in a high-temperature and high-pressure environment, and the basic principle is that a high-carbon raw material is ground into dry powder with proper granularity, the dry powder is continuously fed into a gasification furnace by using high-temperature carbon dioxide/nitrogen, oxygen and water vapor are supplemented at the same time, and the dry powder and the oxygen and the water vapor jointly participate in reaction under the high-temperature and high-pressure condition to generate the hydrogen and the carbon monoxide of the crude synthesis gas. There are two basic types of pulverized coal pressurized gasifiers: a pure chilling type gasification furnace and a waste boiler type gasification furnace with heat recovery.
In the pulverized coal pressure gasification process, because the raw materials all contain a certain amount of ash content, the ash content cannot be converted into a synthesis gas product, and finally generated high-temperature synthesis gas carries a large amount of high-temperature fly ash, so that the purification treatment of the synthesis gas is difficult, and because the high-temperature fly ash has strong cohesiveness, a heat exchange tube of a waste boiler type gasification furnace is easily adhered and corroded, the heat exchange efficiency is influenced, and even the risk of tube explosion exists; the common gasification technology adopts a water chilling and gas chilling mode to cool the synthesis gas and the fly ash, the water chilling is generally combined with a water bath mode, a large amount of cooled fly ash is captured in chilling water, and the primary ash removal of the synthesis gas is realized; the gas chilling generally adopts low-temperature synthetic gas recycled at the downstream as chilling gas to be introduced into the downstream space of the combustion chamber of the gasification furnace, the synthetic gas and the fly ash are primarily cooled by utilizing gas-gas heat exchange, the caking property of the fly ash after being cooled is greatly reduced, and the contamination risk of a heat exchanger is reduced.
As the pulverized coal pressure gasification process mainly uses high-carbon raw materials, the content of CO in the generated crude synthesis gas is far higher than the content of H2, and the hydrogen content of products in the general coal chemical industry is higher, a synthesis gas conversion device is generally configured at the downstream of a gasification device in the traditional coal chemical industry production process, and a part of CO in the gasified crude synthesis gas is converted into H2 by utilizing water-gas reaction so as to meet the H/C ratio of the produced products; in the shift process, carbon dioxide and hydrogen are generated while consuming carbon monoxide and water vapor, and the shift process is one of the main sources of carbon emission of coal chemical enterprises.
The existing gasification technology generally adopts a water chilling type or a gas chilling type aiming at cooling crude synthesis gas, wherein the water chilling type is that crude synthesis gas is directly cooled to a temperature below 250 ℃ by a chilling ring spray mode, a chilling chamber water bath mode and other types at the downstream of a gasification chamber of a gasification furnace, the structure is simple, the water-gas ratio of the crude synthesis gas is high, and the method is very suitable for a process that products at the downstream of a gasification device need deep conversion.
The current gas chilling technology generally mixes low-temperature synthesis gas discharged from the synthesis gas cooler and low-temperature saturated synthesis gas subjected to subsequent water washing and then circulates the mixture back to the gasification furnace as the chilling gas, the gasification device of the process route has high thermal efficiency, but the circulating synthesis gas contains corrosive or easily crystallized impurities such as H2S, NH4+, CL & lt- & gt and the like, so that core parts of a circulating gas compressor are easily corroded or scaled, and the use of the compressor is influenced. And the water-gas ratio of the heat recovery type gasification furnace adopting the circulating synthesis gas as the quenching gas is lower, and steam needs to be supplemented again in a downstream conversion device in the existing device, so that the value of the heat recovery by gasification is greatly reduced. In the prior art, inert gas or water vapor can be used for replacing circulating synthesis gas, but the implementation difficulty is high, the content of effective gas is reduced by adding the inert gas, the shift reaction in the gasification furnace can be enhanced by adding the water vapor, the content of carbon dioxide is increased, the shift reaction is exothermic reaction, and the cooling effect of the water vapor can also be reduced.
Through the analysis, the water chilling type overall efficiency is lower in the existing gasification technology, the gas chilling type circulating gas compressor is easy to corrode and scale to influence use, the H/C ratio of the crude synthesis gas needs to be adjusted in a downstream conversion device in the two types of gasification technologies, the carbon discharge intensity is high, and the objective requirements for energy conservation and emission reduction in the future cannot be met.
SUMMERY OF THE UTILITY MODEL
In view of the above problems in the prior art, the present disclosure provides a gasification furnace system using hydrogen as a cooling gas and a regulating gas, which can cool a high-temperature raw synthesis gas, achieve heat recovery of the gasification furnace, and directly regulate an H/C atomic ratio by supplementing hydrogen.
In order to achieve the above object, the embodiment of the present invention adopts the following technical solutions:
a gasification furnace system using hydrogen as a cooling gas and a conditioning gas is provided, which includes a syngas reaction path; a hydrogen compression device and a gasification furnace which are communicated with each other are arranged along the synthesis gas reaction path; wherein the gasification furnace comprises: the gasification chamber, the chilling mixing chamber and the synthesis gas cooler are communicated in sequence; the hydrogen compression device is communicated with the chilling mixing chamber; the hydrogen compression device is used for compressing hydrogen to a preset pressure and conveying the hydrogen to the chilling mixing chamber; forming high-temperature synthesis gas in a state that raw materials enter the gasification chamber for gasification reaction; the high-temperature synthesis gas enters the chilling mixing chamber from the gasification chamber, and is mixed with low-temperature hydrogen and cooled to form mixed synthesis gas; and the raw synthesis gas enters the synthesis gas cooler from the chilling mixing chamber, is cooled through water cooling heat exchange to form low-temperature raw synthesis gas, and flows out of the gasification furnace.
In some embodiments of the present disclosure, the hydrogen compression device is in communication with the syngas cooler; a portion of the steam generated by the syngas cooler is returned to the hydrogen compression device as drive steam.
In some embodiments of the present disclosure, the gasifier system utilizing hydrogen as cooling gas and conditioning gas further comprises a boiler water line in communication with the syngas cooler; the boiler water line delivers boiler water for indirect cooling to the syngas cooler for heat exchange with the high temperature raw syngas to produce medium or high pressure steam.
In some embodiments of the present disclosure, the syngas cooler generates medium or high pressure steam with a pressure interval set between 5.0 and 9.8MPag.
In some embodiments of the present disclosure, the syngas cooler employs a 2-3 stage heat exchanger configuration to stage exchange the medium or high pressure steam to produce medium or high pressure superheated steam.
In some embodiments of the present disclosure, hydrogen entering the quench mixing chamber from the hydrogen compression device is input at a preset H/C atomic ratio to raw syngas entering the quench mixing chamber from the gasification chamber.
In some embodiments of the disclosure, the temperature of the mixed raw syngas within the quench mixing chamber is set at 700-900 ℃.
In some embodiments of the present disclosure, the hydrogen compressor of the hydrogen compression device is driven by a steam turbine.
In some embodiments of the present disclosure, the raw material is formed by mixing pulverized coal, oxygen, steam, and carbon dioxide/nitrogen in a preset ratio.
Compared with the prior art, the beneficial effects of the utility model reside in that:
the embodiment of the utility model provides an utilize gasification furnace system of hydrogen as cooling gas and regulation gas, compress the hydrogen of external input as the chilling gas of gasifier, directly get into the chilling mixing chamber of gasifier to adjust the H/C atomic ratio in chilling mixing chamber, save the water gas conversion flow, reduce or avoid energy consumption and high carbon that the low reaches transform technology brought and discharge; meanwhile, the purpose of cooling the crude synthesis gas entering the chilling mixing chamber through the gasification chamber is achieved, the high-temperature fly ash is effectively prevented from being bonded on the heat exchange surface of the synthesis gas cooler to form ash deposit, and the heat in the crude synthesis gas is effectively recovered.
The utility model discloses utilize gasifier system of hydrogen as cooling gas and regulation gas, be particularly suitable for with multiple hydrogen manufacturing mode couplings such as electrolysis water hydrogen manufacturing, coke-oven gas hydrogen manufacturing, propane dehydrogenation, waste gas recovery purification, both be applicable to newly-built gasification equipment, also be applicable to current gasification equipment and reform transform, can effectively improve the whole efficiency of coal chemical industry mill to reduce whole carbon emission, accord with the long-range development direction of coal chemical industry low carbon energy-conservation, multipotency coupling.
In addition, the utility model discloses a gasifier system that utilizes hydrogen as cooling gas and regulation gas can also effectively reduce the size and the investment of the gasification chamber of gasifier.
Drawings
Fig. 1 is a schematic structural diagram of a gasifier system using hydrogen as a cooling gas and a conditioning gas according to an embodiment of the present invention.
Description of the reference numerals
1-a hydrogen compression unit; 2-a gasification chamber; 3-chilling the mixing chamber; 4-syngas cooler
Detailed Description
The following detailed description of the embodiments of the present invention is provided with reference to the accompanying drawings, but not intended to limit the invention thereto. For a better understanding of the technical aspects of the present disclosure, reference is made to the following detailed description taken in conjunction with the accompanying drawings. Embodiments of the present disclosure are described in further detail below with reference to the figures and the detailed description, but the present disclosure is not limited thereto.
All terms (including technical or scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs unless specifically defined otherwise. It will be further understood that terms, such as those defined in commonly used dictionaries, should be interpreted as having a meaning that is consistent with their meaning in the context of the relevant art and will not be interpreted in an idealized or overly formal sense unless expressly so defined herein.
Techniques, methods, and apparatus known to those of ordinary skill in the relevant art may not be discussed in detail but are intended to be part of the specification where appropriate.
For solving traditional water chilling gasifier heat utilization rate low, traditional gas chilling gasifier circulating gas compressor is perishable or scale deposit, the steam reinjection low reaches device of output causes heat loss to and gasifier low reaches carry out a large amount of carbon dioxide emissions and the problem of energy consumption that shift reaction caused for adjusting synthetic gas H/C ratio, the utility model provides a solution is specifically as follows.
Referring to fig. 1, there is provided a gasification furnace system using hydrogen as a cooling gas and a conditioning gas, which includes a syngas reaction path; a hydrogen compression device 1 and a gasification furnace which are communicated with each other are arranged along the synthesis gas reaction path; wherein the gasification furnace comprises: the gasification chamber 2, the chilling mixing chamber 3 and the synthesis gas cooler 4 are communicated in sequence; the hydrogen compression device 1 is communicated with the chilling mixing chamber 3; the hydrogen compression device 1 is used for compressing hydrogen to a preset pressure and conveying the hydrogen to the chilling mixing chamber 3; forming high-temperature synthesis gas in a state that the raw materials enter the gasification chamber 2 for gasification reaction; the high-temperature synthesis gas enters a chilling mixing chamber 3 from a gasification chamber 2, and is mixed with low-temperature hydrogen and cooled to form crude synthesis gas; here, the temperature of the mixed raw synthesis gas in the quench mixing chamber 3 is set to 700-900 ℃, preferably 800 ℃, but is not limited thereto, and can be adjusted accordingly as required; and the crude synthesis gas enters the synthesis gas cooler 4 from the chilling mixing chamber, is cooled through water cooling heat exchange to form low-temperature crude synthesis gas, and flows out of the gasification furnace.
Through the embodiment of the utility model provides an utilize the gasification furnace system of hydrogen as cooling gas and regulation gas, both can cool off the flying dust in the crude synthesis gas, realize the heat recovery of gasifier again to through replenishing hydrogen and directly adjusting the H/C atomic ratio in quench mixing chamber 3, reduce or avoid because energy consumption and the high carbon that the condition that transform technology probably appears in low reaches brought discharges.
Further, in the present embodiment, the hydrogen entering the quench mixing chamber 3 from the hydrogen compression device 1 and the raw syngas entering the quench mixing chamber 3 from the gasification chamber 2 may be input at a preset H/C atomic ratio. In practical application, the H/C atomic ratio can also be determined according to the product process requirements, and is not limited herein.
In the above embodiment, the raw materials are formed by mixing coal powder, oxygen, steam, carbon dioxide/nitrogen in a preset ratio. In practical application, the proportion can be adjusted according to different proportion requirements, and the corresponding proportion can be correspondingly adjusted according to the produced products and intermediate products with different specifications.
Further, referring to fig. 1, the hydrogen compression device 1 is also in communication with a syngas cooler 4; a portion of the steam exits the syngas cooler 4 and is recycled to the hydrogen compression unit 1 as the drive steam for the hydrogen compressor. Through the arrangement mode, the energy of part of steam produced by the synthesis gas cooler is fully recycled and used as driving steam, and the effects of energy conservation and emission reduction are achieved.
In an embodiment, referring to fig. 1, the gasifier system utilizing hydrogen as cooling gas and conditioning gas further comprises a boiler water line in communication with the syngas cooler 4; the boiler water pipeline transmits boiler water for indirect cooling to the synthesis gas cooler 4 for heat exchange with the high-temperature crude synthesis gas to generate medium-pressure steam or high-pressure steam, and the boiler water for cooling generates steam after heat exchange and is sent out; one part of the steam is used as the driving steam of the hydrogen compression device, and the other part of the steam is directly sent out and enters a downstream process. With reference to the above embodiment, the quench mixing chamber 3 mixes and cools the hydrogen from the hydrogen compression device 1 and the raw material from the gasification chamber 2 and sends the mixture to the syngas cooler 4 of the gasification furnace as high-temperature ash-bearing high-temperature raw syngas; in the process, hydrogen basically does not participate in gasification reaction and is only used as cooling gas and components for regulating synthesis gas, wherein a very small amount of hydrogen and carbon dioxide undergo inverse transformation reaction to generate carbon monoxide and water vapor, but the influence on the total components of the synthesis gas is not large, and the inverse transformation reaction is endothermic reaction, so that the temperature of the crude synthesis gas is favorably reduced; the synthesis gas cooler 4 reduces the temperature of the raw synthesis gas through the indirect heat exchange of boiler water, and sends out the heat after recovering the heat.
Further, in the foregoing embodiment, the pressure interval of the medium-pressure steam or the high-pressure steam generated by the syngas cooler is set to 5.0 to 9.8MPag. In practical application, the pressure value can be adjusted correspondingly according to downstream requirements and specific application scenarios, and a suitable pressure value is specifically selected without further limitation.
In one embodiment, the syngas cooler 4 employs a 2-3 stage heat exchanger configuration to generate medium or high pressure superheated steam by staged heat exchange of the medium or high pressure steam. The heat exchanger structure in which mode is adopted can be correspondingly adjusted according to the field application scene.
In summary, the gasification furnace system using hydrogen as the cooling gas and the adjusting gas according to the present embodiment can provide advantages such as, for example, cooling the raw syngas and the entrained fly ash mixed in the quench mixing chamber 3, and adjusting the H/C ratio of the syngas according to the product requirement.
Moreover, although illustrative embodiments have been described herein, the scope includes any and all embodiments having equivalent elements, modifications, omissions, combinations (e.g., of aspects across various embodiments), adaptations or alterations based on the present disclosure. The elements of the claims are to be interpreted broadly based on the language employed in the claims and not limited to examples described in the specification or during the life of the application. Further, the steps of the disclosed methods may be modified in any manner, including by reordering steps or inserting or deleting steps. It is intended, therefore, that the description be regarded as examples only, with a true scope being indicated by the following claims and their full scope of equivalents.
The above description is intended to be illustrative and not restrictive. For example, the above-described examples (or one or more aspects thereof) may be used in combination with each other. Other embodiments may be utilized, for example, by one of ordinary skill in the art, upon reading the above description. Also, in the foregoing detailed description, various features may be combined together to simplify the present disclosure. This should not be interpreted as intending that an unclaimed disclosed feature is essential to any claim. Thus, the following claims are hereby incorporated into the detailed description as examples or embodiments, with each claim standing on its own as a separate embodiment, and it is contemplated that these embodiments may be combined with each other in various combinations or permutations. The scope of the invention should be determined with reference to the appended claims, along with the full scope of equivalents to which such claims are entitled.
Claims (8)
1. A gasification furnace system using hydrogen as cooling gas and regulating gas is characterized by comprising a synthesis gas reaction path; a hydrogen compression device and a gasification furnace which are communicated with each other are arranged along the synthesis gas reaction path; wherein the content of the first and second substances,
the gasification furnace includes: the gasification chamber, the chilling mixing chamber and the synthesis gas cooler are communicated in sequence;
the hydrogen compression device is communicated with the chilling mixing chamber; the hydrogen compression device is used for compressing hydrogen to a preset pressure and conveying the hydrogen to the chilling mixing chamber;
forming high-temperature synthesis gas in a state that raw materials enter the gasification chamber for gasification reaction; the high-temperature synthesis gas enters the chilling mixing chamber from the gasification chamber, and is mixed with low-temperature hydrogen and cooled to form crude synthesis gas; and the crude synthesis gas enters the synthesis gas cooler from the chilling mixing chamber, is cooled through water cooling heat exchange to form low-temperature crude synthesis gas, and flows out of the gasification furnace.
2. A gasifier system using hydrogen as a cooling gas and a conditioning gas according to claim 1, wherein the hydrogen compression device is in communication with the syngas cooler; a portion of the steam generated by the syngas cooler is returned to the hydrogen compression device as drive steam.
3. A gasifier system utilizing hydrogen as a cooling gas and a conditioning gas according to claim 1, further comprising a boiler water line in communication with the syngas cooler; the boiler water line delivers boiler water for indirect cooling to the syngas cooler for heat exchange with the high temperature raw syngas to produce medium or high pressure steam.
4. A gasifier system according to claim 3, wherein the syngas cooler generates medium or high pressure steam in a pressure interval of 5.0-9.8 MPag.
5. A gasifier system according to claim 3 wherein the syngas cooler employs a 2-3 stage heat exchanger configuration to stage exchange heat with the medium or high pressure steam to generate medium or high pressure superheated steam.
6. A gasifier system according to claim 1, wherein the hydrogen entering the quench mixing chamber from the hydrogen compressor and the raw syngas entering the quench mixing chamber from the gasification chamber are fed in a predetermined H/C atomic ratio.
7. The gasifier system according to claim 1, wherein the temperature of the mixed raw syngas in the quench-mixing chamber is set to 700-900 ℃.
8. A gasifier system using hydrogen as a cooling gas and a conditioning gas as claimed in claim 1, wherein the hydrogen compressor of the hydrogen compressor is driven by a steam turbine.
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| CN202220550413.7U CN217556132U (en) | 2022-03-14 | 2022-03-14 | Gasification furnace system using hydrogen as cooling gas and adjusting gas |
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| CN202220550413.7U CN217556132U (en) | 2022-03-14 | 2022-03-14 | Gasification furnace system using hydrogen as cooling gas and adjusting gas |
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