CN113432135A - Removing CO from gasified and transported pulverized coal2Method and device for producing methanol in gas - Google Patents
Removing CO from gasified and transported pulverized coal2Method and device for producing methanol in gas Download PDFInfo
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 156
- 239000003245 coal Substances 0.000 claims abstract description 64
- 238000000034 method Methods 0.000 claims abstract description 45
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 37
- 230000023556 desulfurization Effects 0.000 claims abstract description 37
- 238000007084 catalytic combustion reaction Methods 0.000 claims abstract description 31
- 230000008569 process Effects 0.000 claims abstract description 21
- 238000007599 discharging Methods 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 134
- 229930195733 hydrocarbon Natural products 0.000 claims description 19
- 150000002430 hydrocarbons Chemical class 0.000 claims description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 15
- 239000004215 Carbon black (E152) Substances 0.000 claims description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 8
- 230000003009 desulfurizing effect Effects 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 8
- 229910000510 noble metal Inorganic materials 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000010926 purge Methods 0.000 claims description 3
- 150000001875 compounds Chemical class 0.000 claims description 2
- 238000002309 gasification Methods 0.000 abstract description 24
- 230000007613 environmental effect Effects 0.000 abstract description 11
- 238000006243 chemical reaction Methods 0.000 abstract description 9
- 238000003795 desorption Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 12
- 238000005406 washing Methods 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 8
- 239000002151 riboflavin Substances 0.000 description 8
- 239000011787 zinc oxide Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 230000003197 catalytic effect Effects 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 230000005484 gravity Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 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
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 239000002817 coal dust Substances 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 239000002574 poison Substances 0.000 description 2
- 231100000614 poison Toxicity 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000003883 substance clean up Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 239000004149 tartrazine Substances 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000006900 dealkylation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
- F23G7/063—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating electric heating
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
- F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
- F23G7/066—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator
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- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
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Abstract
The application discloses desorption fine coal gasification coal transportation CO2A process and apparatus for the production of methanol from gas. The method comprises at least the following steps: s100, releasing pressure of the lock hopper and discharging CO2Carrying out desulfurization treatment on the gas to obtain first treated gas; s200, carrying out catalytic combustion treatment on the first treatment gas to remove methanol contained in the first treatment gas so as to obtain purified gas. The method ensures that the emission of the lock gas of the pulverized coal gasification and coal transportation meets the environmental protection requirement, and the reaction heat generated by catalytic combustion can meet the heat balance of the system without external supplementary energy consumption during normal operation.
Description
Technical Field
The application relates to removing CO from pulverized coal gasification coal transportation2A method and a device for methanol in gas, which belong to the coal chemical industry environmental protection technologyThe field of the technology.
Background
The industrial production of synthesis gas from coal has been in the history of hundreds of years, and currently, there are over ten coal gasification technologies that have been industrialized worldwide. The entrained-flow bed pressurized gasification is the most widely used gasification technology at present, and can be divided into a coal water slurry pressurized gasification technology and a pulverized coal pressurized gasification technology, wherein the pulverized coal pressurized gasification technology is represented by Shell and GSP gasification technologies internationally, and the HT-L pulverized coal pressurized gasification technology is represented domestically.
The pulverized coal gasification needs to convey pulverized coal into a gasification furnace through carrier gas, and the common carrier gas is compressed nitrogen or CO2And (4) qi. The coal pressurizing and feeding unit adopts a lock hopper to complete the continuous pressurization and conveying of the pulverized coal, and the byproduct CO is washed by low-temperature methanol2After the gas is compressed, one part of the gas is used for conveying the pulverized coal to enter the gasification furnace, and the other part of the gas is used for pressurizing the lock hopper. In the primary feeding process, the pulverized coal in the pulverized coal storage tank enters the pulverized coal locking hopper under the action of gravity. After the fine coal lock fill is full of fine coal, keep apart with fine coal basin and all low-pressure equipment promptly, then pressurize, rise to as its pressure with fine coal feed jar pressure the same, and the material level in the fine coal feed jar reduces when being enough to receive a batch of fine coal, open fine coal lock fill and fine coal feed jar between balanced valve carry out pressure balance, then open two trip valves between fine coal lock fill and the fine coal feed jar in proper order, fine coal gets into fine coal feed jar through action of gravity. And after the unloading of the pulverized coal lock hopper is finished, discharging the gas to the atmosphere through a pulverized coal storage tank filter for pressure relief, communicating the discharged gas with the pulverized coal storage tank after pressure balance is finished, and at the moment, finishing one-time feeding. CO discharged in the process of pressure relief of the lock hopper2The gas comes from low-temperature methanol washing, and the direct discharge does not meet the discharge standard (the discharge concentration of the methanol is less than 50 mg/Nm) in GB31571-2015 discharge Standard of pollutants for petrochemical industry3) The requirements of (1).
For treating methanol in lock hopper discharge gas, a common scheme is washing by water, and the scheme is divided into two schemes of washing before compression and washing when the lock hopper is discharged. CO 22The washing before compression is usually arranged in a low-temperature methanol washing device, the flow is simple, the methanol in the washing water can be recycled,but CO after scrubbing2The gas contains more than 1 mol% of saturated water for CO2The investment of the compressor and the pipeline has great influence; meanwhile, saturated water vapor also has influence on coal dust transportation, and coal dust gasification patentees require CO2The water content in the gas is as low as possible. The scheme of lock hopper gas discharge washing is difficult to realize operation and the washed waste water is difficult to treat due to the influence of pressure fluctuation and coal ash impurities during discharge. Both of these schemes are currently unsuccessful.
Disclosure of Invention
According to one aspect of the application, a method for removing CO from pulverized coal gasification coal transportation is provided2The method of methanol in gas makes the lock bucket gas exhaust of coal powder gasifying and conveying meet the requirement of environment protection.
Removing CO from gasified and transported pulverized coal2Process for methanol in gas, said process at least comprising the steps of:
s100, releasing pressure of the lock hopper and discharging CO2Carrying out desulfurization treatment on the gas to obtain first treated gas;
s200, carrying out catalytic combustion treatment on the first treatment gas to remove methanol contained in the first treatment gas so as to obtain purified gas.
The application removes hydrocarbon combustible substances such as methanol and the like through oxidation reaction under the catalytic action of a noble metal catalyst, and the combustible substances are discharged after reaching the national environmental protection standard; meanwhile, a large amount of reaction heat is generated, the self-reaction heat balance is met, and no external supplementary energy consumption is caused.
Optionally, in step S100, the lock hopper releases the pressure of the exhausted CO2Gas comes from low-temperature methanol washing;
CO discharged by pressure relief of the lock hopper2The content of methanol in the gas is 150-250 ppm.
Optionally, before step S100, the method further includes: CO discharged by pressure relief of the lock hopper2Compressing the gas;
CO discharged by pressure relief of the lock hopper2The temperature of the gas after the compression treatment is 130-150 ℃;
CO discharged by pressure relief of the lock hopper2The pressure of the compressed gas is 7.5-8.0MPa。
Alternatively, in step S100, a desulfurizing agent is used in the desulfurization treatment, and the desulfurizing agent includes ZnO.
The desulfurizer is ZnO
Optionally, the desulfurizer and CO discharged by pressure relief of the lock hopper2The air speed of the gas phase to the desulfurizer is 800-1200 h-1。
Specifically, the desulfurizer and CO discharged by pressure relief of the lock hopper2The proportion relation of the gas is as follows: 1m3The desulfurizing agent corresponds to 800-1200 Nm3CO of/h2And (4) qi.
Preferably, the desulfurizer and CO discharged by pressure relief of the lock hopper2The proportion relation of the gas is as follows: 1m3Desulfurizing agent of (1) corresponds to 1000Nm3CO of/h2And (4) qi.
Optionally, in step S100, H in the first process gas2The S content is 0.05ppm or less.
Optionally, before step S200, the method further includes heating the first processing gas to make the temperature of the first processing gas reach 200 to 250 ℃.
Specifically, the upper limit of the temperature of the first process gas is independently selected from 220 ℃, 230 ℃, 240 ℃, 250 ℃; the lower limit of the temperature of the first process gas is independently selected from the group consisting of 200 ℃, 210 ℃, 220 ℃, 230 ℃.
Optionally, in step S200, during the catalytic combustion treatment, hydrocarbons and inorganic combustibles contained in the first treatment gas are also removed;
the hydrocarbon comprises at least one of compounds with a chemical formula shown in a formula I;
CmHn is represented by formula I;
in the formula I, m and n respectively represent the atomic number ratio of C element and H element, the value range of m is more than or equal to 1 and less than or equal to 5, and the value range of n is more than or equal to 4 and less than or equal to 12;
the inorganic combustible comprises CO and H2At least one of (1).
Optionally, in step S200, the catalytic combustion process is performed in an oxygen-containing environment;
the volume ratio of the oxygen to the first treatment gas is 0.15-0.20%;
the temperature of the catalytic combustion treatment is 200-220 ℃.
Specifically, the upper limit of the temperature of the catalytic combustion treatment is independently selected from 205 ℃, 210 ℃, 215 ℃, 220 ℃; the lower limit of the temperature of the catalytic combustion treatment is independently selected from 200 ℃, 205 ℃, 210 ℃, 215 ℃.
Optionally, in step S200, a noble metal catalyst is used in the catalytic combustion process.
Optionally, the space velocity of the first treatment gas is 2000-20000 h-1。
In the present application, the noble metal catalyst may be obtained by purchase, for example, DGTT1 manufactured by great-chain green-resource environmental protection industry Co.
Specifically, the upper limit of the space velocity of the first process gas is independently selected from 5000h-1、6000h-1、10000h-1、20000h-1(ii) a The lower limit of the space velocity of the first process gas is independently selected from 2000h-1、4000h-1、5000h-1、10000h-1。
Optionally, in step S200, the content of total hydrocarbons in the purge gas is 20ppm or less; wherein the volume of total hydrocarbons is based on the volume of methane.
Removing CO from gasified and transported pulverized coal2The method for preparing methanol in gas comprises the following steps:
1) CO of pulverized coal conveying and air inlet furnace2The gas does not need to be treated, but only CO pressurized for the lock hopper2The overall treatment scale is small; CO 22The temperature and pressure of the compressed gas are suitable for the catalytic combustion method.
2)CO2The gas source contains trace sulfide which is a poison of the noble metal catalyst, so that desulfurization and purification are required before catalytic combustion; the compressed CO2The temperature is high, so the zinc oxide desulfurizer is suitable for being adopted.
3) The desulfurized feed gas enters a catalytic combustion decarbonization hydrogen compound purification process to remove methanol, hydrocarbon and combustible substances such as methane, carbon monoxide and the like, all the hydrocarbon is completely converted into carbon dioxide and water through catalytic oxidation, and the total hydrocarbon (calculated by methane) in the gas is reduced to be below 20ppm, thus completely meeting the strictest requirements of environmental protection standards.
4) The reaction is exothermic, the gas temperature is increased, and the heat exchanger is used as CO of the methanol removing reactor2The gas is heated to reach heat balance, and no external heat is needed during continuous operation.
According to yet another aspect of the present application, a method for removing CO from pulverized coal gasification coal transportation is provided2A plant for methanol in gas, the plant comprising a desulfurization reactor and a demethanization reactor;
the desulfurization reactor is used for releasing the pressure of the lock hopper and discharging CO2Carrying out desulfurization treatment on the gas to obtain first treated gas;
the methanol removing reactor is used for carrying out catalytic combustion treatment on the first treatment gas so as to remove methanol contained in the first treatment gas and obtain purified gas.
Optionally, the number of desulfurization reactors is at least one;
the lower extreme of desulfurization reactor is equipped with gas inlet, the upper end of desulfurization reactor is equipped with gas outlet.
Specifically, the desulfurization reactors can be connected in parallel, and one is used and the other is prepared.
Optionally, a heat exchanger and an electric heater for start-up are sequentially arranged between the desulfurization reactor and the demethanization reactor along the gas flowing direction.
Optionally, an oxygen inlet is provided between the desulfurization reactor and the heat exchanger.
The beneficial effects that this application can produce include:
1) the application provides a desorption fine coal gasification coal transportation CO2The method for removing methanol in gas removes hydrocarbon combustible substances such as methanol and the like through desulfurization treatment and oxidation reaction under the catalytic action of a noble metal catalyst, and discharges the methanol after the methanol reaches the national environmental protection standard; simultaneously generates a large amount of reaction heat, meets the self-reaction heat balance, and has no external supplementAnd (5) energy charging.
2) The application provides a desorption fine coal gasification coal transportation CO2The device for producing methanol in gas meets the requirement of small occupied area on site, has simple process, high automation degree and low operation cost, and has good economic benefit and environmental protection benefit.
3) Low pressure CO will be used in this application2The idea of removing impurities by gas catalytic combustion is used for pressurized pulverized coal gasification and coal transportation CO2The gas effectively removes impurities such as methanol and the like in the lock hopper exhaust gas, so that the exhaust gas meets the requirement of environmental protection and emission.
Drawings
FIG. 1 shows the removal of CO from pulverized coal gasification coal transportation according to an embodiment of the present application2Process flow diagram for methanol in gas;
FIG. 2 shows the removal of CO from pulverized coal gasification coal transportation according to an embodiment of the present application2The structure of the device for methanol in gas is shown schematically.
List of parts and reference numerals:
a first desulfurization reactor of R-101A; a second R-101B desulfurization reactor;
an E-101 heat exchanger; e-102 turns on the electric heater.
Detailed Description
The present application will be described in detail with reference to examples, but the present application is not limited to these examples.
The invention adopts the following technical scheme:
1) CO of pulverized coal conveying and air inlet furnace2The gas does not need to be treated, and only the CO pressurized in the lock hopper is treated2The overall treatment scale is small; CO 22After the gas is compressed, the temperature is higher, and a temperature condition is provided for removing the methanol by a catalytic combustion method; at the same time, CO2The outlet pressure of the gas compressor is higher, and the resistance requirement of the catalytic combustion method is met.
2)CO2The gas source contains trace sulfide which is a poison of the noble metal catalyst, so that desulfurization and purification are required before catalytic combustion; the compressed CO2The temperature is high, so the method is suitable for adopting the zinc oxide desulfurizer, and the technical principle is as follows:
ZnO+H2S＝ZnS+H2O
the desulfurization step may be carried out with H2S is removed to be below 0.05ppm, and the requirements are met.
3) The desulfurized feed gas enters a catalytic combustion decarbonization hydrogen compound purification process to remove methanol, hydrocarbon such as methane and inorganic combustible such as carbon monoxide, all the hydrocarbon and the inorganic combustible are converted into carbon dioxide and water through catalytic oxidation, and the total hydrocarbon (calculated by methane) in the gas is reduced to be below 20ppm, thus completely meeting the strictest environmental standard requirement.
The dealkylation reaction is carried out at the temperature of more than 200 ℃, the total hydrocarbon in the feed gas needs to consume 0.17 percent (v/v) of oxygen when being completely combusted, and the total volatile hydrocarbon is removed by catalytic oxidation and combustible is purified by a combustible system and is completely converted into CO2And H2O。
The reaction principle for removing the total volatile hydrocarbon and the combustible substance is as follows:
CH4O+O2→CO2+2H2O；
H2+O2→H2O；
CO+O2→CO2；
CH4+O2→CO2+H2O；
CmHn+O2→CO2+H2O；
the value range of m is more than or equal to 1 and less than or equal to 5, and the value range of n is more than or equal to 4 and less than or equal to 12.
4) The reaction is exothermic, the gas temperature is increased, and the heat exchanger is used as CO of the methanol removing reactor2The gas is heated to reach heat balance, and no external heat is needed during continuous operation.
The device is comprehensively considered, meets the requirement of small occupied area on site, and has the advantages of simple process, high automation degree, low operation cost, and good economic benefit and environmental protection benefit.
Example 1
The following describes in detail an embodiment of the present invention with reference to fig. 1 and 2.
FIG. 1 shows the removal of pulverized coal gasChemical coal transportation CO2A method for producing methanol in gas. FIG. 2 shows the removal of pulverized coal gasification coal transportation CO2A device for producing methanol in gas.
As shown in fig. 1, the method of the present embodiment includes: s100, releasing pressure of the lock hopper and discharging CO2Carrying out desulfurization treatment on the gas to obtain first treated gas; s200, carrying out catalytic combustion treatment on the first treatment gas to remove methanol contained in the first treatment gas so as to obtain purified gas.
In the apparatus of the present application shown in FIG. 2, the desulfurization reactor comprises two parallel reactors, a first desulfurization reactor R-101A and a second desulfurization reactor R-101B, one for the use reactor and one for the spare reactor. The lower end of the desulfurization reactor is provided with a gas inlet, and the lock hopper releases CO discharged by pressure2Gas enters the desulfurization reactor from the inlet; the upper end of the desulfurization reactor is provided with a gas outlet, first treatment gas flows out of the gas outlet and enters a heat exchanger E-101, meanwhile, oxygen also enters the heat exchanger E-101, the first treatment gas is mixed with the oxygen and is subjected to temperature rise heat exchange treatment in the heat exchanger E-101, then the first treatment gas enters a methanol removal reactor R-102 through an operating electric heater E-102 to be subjected to catalytic combustion treatment, the obtained purified gas is discharged from a lower gas outlet of the methanol removal reactor R-102 and enters the heat exchanger E-101 to be subjected to temperature reduction heat exchange treatment, and then the purified gas is discharged into the environment.
The proposal is matched with a pulverized coal gasification furnace with 3000 tons of coal input per day, and CO is used for total coal transportation2Gas flow about 15000Nm3The gas consumption of the lock hopper is about 6000Nm3/h。
High pressure CO discharged from compressor2Gas with the temperature of about 130 ℃ and the pressure of 7.495MPa is firstly desulfurized by R-101A and R-101B, the desulfurized gas is subjected to heat exchange by a heat exchanger E-101 and is heated to 200 ℃ (when starting, the desulfurized gas is preheated by E-102) to enter a catalytic combustion reaction, and 5000h is adopted-1Operation space velocity, CO and H removal2And methanol, which can meet the national standard of GB 31571-2015.
Specifically, the desulfurization section considers the space velocity of gas, and the dosage of ZnO as a desulfurizing agent is 6000Nm3The treatment capacity per hour, the annual operation time is 8000 hours, and the bulk specific gravity of the desulfurizing agent is 1.0 ton/m3Accounting, adopting double towers (R-101A and R-101B) to operate in parallel, and the effective volume of a single tower is 3.5m3The consumption of the single-tower desulfurizer is 3.5 tons, and the space velocity is 1714h-1And replacing in 2 years.
H in the first treatment gas after desulfurization treatment2The S content was about 0.04 ppm.
The desulfurized gas (i.e., the first process gas) is heated by a heat exchanger E-101 and then enters a methanol removal reactor R-102, and CO and H are removed2And methanol removal, specifically, heat exchange is carried out between the desulfurized gas (180 ℃) and the purified gas (220 ℃) so that the desulfurized gas (180 ℃) is heated to 200 ℃.
Because the catalytic combustion needs oxygen to participate, the oxygen supplement amount is carried out according to the stoichiometric excess of 10 percent, and the oxygen supplement amount is 11.2Nm3Per, 56Nm in compressed air3The volume ratio of the oxygen to the first process gas was 0.17%.
The adiabatic temperature rise of the R-102 of the methanol removal reactor is about 20 ℃, the heat exchange is carried out between the R-102 and the desulfurized gas, the desulfurized gas after the heat exchange reaches the catalytic combustion reaction temperature (220 ℃), the heat is balanced, the heat release of the reaction can ensure the normal operation of the whole system, the external heating is not needed, the power consumption of a continuous operation system is avoided, the effective filling amount of the R-102 of the methanol removal reactor is 1.2m3In the catalytic combustion process, the catalyst is DGTT1 which is a product of a large-scale continuous-processing green-resource environmental protection industry Limited company, and the space velocity is 5000h-1。
And (3) introducing purified gas obtained after catalytic combustion into a heat exchanger E-101, performing heat exchange to reduce the temperature to 150 ℃, and discharging. The purge gas was tested for methane content and the test result was 18 ppm.
Although the present application has been described with reference to a few embodiments, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the application as defined by the appended claims.
Claims (10)
1. Removing CO from gasified and transported pulverized coal2Method for methanol in gas, characterized in that it comprises at least the following steps:
s100, releasing pressure of the lock hopper and discharging CO2Carrying out desulfurization treatment on the gas to obtain first treated gas;
s200, carrying out catalytic combustion treatment on the first treatment gas to remove methanol contained in the first treatment gas so as to obtain purified gas.
2. The method of claim 1, wherein in step S100, the lock hopper is vented of vented CO2The content of methanol in the gas is 150-250 ppm.
3. The method according to claim 1, before step S100, further comprising: CO discharged by pressure relief of the lock hopper2Compressing the gas;
CO discharged by pressure relief of the lock hopper2The temperature of the gas after the compression treatment is 130-150 ℃;
CO discharged by pressure relief of the lock hopper2The pressure of the compressed gas is 7.5-8.0 MPa.
4. The method according to claim 1, wherein in step S100, a desulfurizing agent is used in the desulfurization treatment, and the desulfurizing agent includes ZnO.
5. The method of claim 4, wherein the desulfurizing agent and the lock hopper release CO discharged under pressure2The space velocity of gas phase to the desulfurizer is 800-2000 h-1。
6. The method of claim 1, wherein in step S100, H in the first process gas2The S content is 0.05ppm or less.
7. The method according to claim 1, further comprising heating the first processing gas to a temperature of 200 to 250 ℃ before step S200;
preferably, in step S200, during the catalytic combustion treatment, hydrocarbons and inorganic combustibles contained in the first treatment gas are also removed;
the hydrocarbon comprises at least one of compounds with a chemical formula shown in a formula I;
CmHn is represented by formula I;
in the formula I, m and n respectively represent the atomic number ratio of C element and H element, the value range of m is more than or equal to 1 and less than or equal to 5, and the value range of n is more than or equal to 4 and less than or equal to 12;
the inorganic combustible comprises CO and H2At least one of;
preferably, in step S200, the catalytic combustion process is performed in an oxygen-containing environment;
the volume ratio of the oxygen to the first treatment gas is 0.15-0.20%;
the temperature of the catalytic combustion treatment is 200-220 ℃;
preferably, in step S200, a noble metal catalyst is used during the catalytic combustion process;
the airspeed of the first treatment gas is 2000-20000 h-1；
Preferably, in step S200, the content of total hydrocarbons in the purge gas is 20ppm or less;
wherein the volume of total hydrocarbons is based on the volume of methane.
8. Removing CO from gasified and transported pulverized coal2A device for methanol in gas, which is characterized by comprising a desulfurization reactor and a methanol removal reactor;
the desulfurization reactor is used for releasing the pressure of the lock hopper and discharging CO2Carrying out desulfurization treatment on the gas to obtain first treated gas;
the methanol removing reactor is used for carrying out catalytic combustion treatment on the first treatment gas so as to remove methanol contained in the first treatment gas and obtain purified gas.
9. The apparatus of claim 8, wherein the number of desulfurization reactors is at least one;
the lower extreme of desulfurization reactor is equipped with gas inlet, the upper end of desulfurization reactor is equipped with gas outlet.
10. The device of claim 9, wherein a heat exchanger and an electric heater for start-up are arranged between the desulfurization reactor and the methanol removal reactor in sequence along the gas flowing direction;
preferably, an oxygen inlet is arranged between the desulfurization reactor and the heat exchanger.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001017835A (en) * | 1999-07-09 | 2001-01-23 | Nissan Motor Co Ltd | Method for cleaning exhaust gas of fuel cell system and exhaust gas cleaning device |
| CN1335198A (en) * | 2000-07-24 | 2002-02-13 | 中国石油化工股份有限公司 | Method of treating waste gas containing sulfur and flammable component |
| CN1611291A (en) * | 2003-10-31 | 2005-05-04 | 中国石油化工股份有限公司 | Method for purifying organic waste gas with high concentration |
| CN1702149A (en) * | 2005-06-28 | 2005-11-30 | 庞玉学 | Safety sealing and air flow conveying method for fine coal gasification process |
| CN201093512Y (en) * | 2007-04-04 | 2008-07-30 | 中国石油化工股份有限公司 | Mobile waste gas treater |
| CN102049181A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Purification method of sulfur-containing organic waste gas |
| CN106215631A (en) * | 2016-08-15 | 2016-12-14 | 航天长征化学工程股份有限公司 | System and method for treating methanol in pulverized coal gasification vented carbon dioxide |
| CN108554150A (en) * | 2018-07-04 | 2018-09-21 | 宁波大学 | A kind of pre-heated catalytic combustion system of purifying volatile organic exhaust gas |
-
2020
- 2020-03-23 CN CN202010209726.1A patent/CN113432135A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001017835A (en) * | 1999-07-09 | 2001-01-23 | Nissan Motor Co Ltd | Method for cleaning exhaust gas of fuel cell system and exhaust gas cleaning device |
| CN1335198A (en) * | 2000-07-24 | 2002-02-13 | 中国石油化工股份有限公司 | Method of treating waste gas containing sulfur and flammable component |
| CN1611291A (en) * | 2003-10-31 | 2005-05-04 | 中国石油化工股份有限公司 | Method for purifying organic waste gas with high concentration |
| CN1702149A (en) * | 2005-06-28 | 2005-11-30 | 庞玉学 | Safety sealing and air flow conveying method for fine coal gasification process |
| CN201093512Y (en) * | 2007-04-04 | 2008-07-30 | 中国石油化工股份有限公司 | Mobile waste gas treater |
| CN102049181A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Purification method of sulfur-containing organic waste gas |
| CN106215631A (en) * | 2016-08-15 | 2016-12-14 | 航天长征化学工程股份有限公司 | System and method for treating methanol in pulverized coal gasification vented carbon dioxide |
| CN108554150A (en) * | 2018-07-04 | 2018-09-21 | 宁波大学 | A kind of pre-heated catalytic combustion system of purifying volatile organic exhaust gas |
Non-Patent Citations (1)
| Title |
|---|
| 谢克昌等: "化石能源的清洁高效可持续开发利用：第二届"中国工程院/国家能源局能源论坛"论文集", 中国石化出版社, pages: 700 - 702 * |
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