CN100500551C - Preparation method for hydrogen from coal-seam gas - Google Patents
Preparation method for hydrogen from coal-seam gas Download PDFInfo
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- CN100500551C CN100500551C CN 200510022208 CN200510022208A CN100500551C CN 100500551 C CN100500551 C CN 100500551C CN 200510022208 CN200510022208 CN 200510022208 CN 200510022208 A CN200510022208 A CN 200510022208A CN 100500551 C CN100500551 C CN 100500551C
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- 239000007789 gas Substances 0.000 title claims abstract description 113
- 239000001257 hydrogen Substances 0.000 title claims abstract description 66
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 66
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 238000002360 preparation method Methods 0.000 title description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 128
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 238000000034 method Methods 0.000 claims abstract description 23
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000001301 oxygen Substances 0.000 claims abstract description 7
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 7
- 239000000203 mixture Substances 0.000 claims description 23
- 238000010521 absorption reaction Methods 0.000 claims description 22
- 150000002431 hydrogen Chemical class 0.000 claims description 17
- 230000009466 transformation Effects 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 20
- 239000003054 catalyst Substances 0.000 abstract description 11
- 230000008569 process Effects 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 4
- 239000000463 material Substances 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 239000002699 waste material Substances 0.000 abstract description 2
- 239000003245 coal Substances 0.000 abstract 7
- 239000002737 fuel gas Substances 0.000 abstract 1
- 238000001179 sorption measurement Methods 0.000 abstract 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 33
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 19
- 235000011089 carbon dioxide Nutrition 0.000 description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 229910052757 nitrogen Inorganic materials 0.000 description 16
- 238000010438 heat treatment Methods 0.000 description 10
- 238000002485 combustion reaction Methods 0.000 description 7
- 238000006477 desulfuration reaction Methods 0.000 description 7
- 230000023556 desulfurization Effects 0.000 description 7
- 238000011084 recovery Methods 0.000 description 7
- 238000000629 steam reforming Methods 0.000 description 7
- 238000001816 cooling Methods 0.000 description 6
- 238000003672 processing method Methods 0.000 description 6
- 239000002918 waste heat Substances 0.000 description 6
- -1 hydrogen alkane Chemical class 0.000 description 5
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000003345 natural gas Substances 0.000 description 4
- 235000009508 confectionery Nutrition 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical class C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 102000040350 B family Human genes 0.000 description 1
- 108091072128 B family Proteins 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000002453 autothermal reforming Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003421 catalytic decomposition reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 150000002910 rare earth metals Chemical class 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000002000 scavenging effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000010512 thermal transition Effects 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
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Abstract
The invention discloses a process for producing hydrogen gas of high concentration with coal seam gas with medium methane content being 26%-70%, adding the coal seam gas into proper amount water vapor, making the methane and water vapor transform into mixing gas containing hydrogen under the action of catalyst by using the reaction heat of the fuel gas in the coal seam gas and oxygen, then getting the hydrogen production of 99-99.99% concentration through the pressure-swing adsorption process; the invention effectively solves the using problem of the coal seam gas which turns waste into useful material and produces direct economic benefit; and provides a new industrial use of the coal seam gas; the invention creates the process of producing hydrogen by using the reaction heat of the oxygen in the coal seam gas with the coal seam gas with medium methane content (volume concentration 26%-70%), which avoids the deoxidization problem in the methane chemical industrial use; the invention is characterized by the small investment, low production cost and high economic benefit.
Description
Technical field
The present invention relates to the gas preparing technical field, specifically, relate to utilize coal-seam gas to prepare the method for hydrogen.
Background technology
The colliery resource of China is extremely abundant, and the coal-seam gas of association it is predicted that stock number is equivalent to 45,000,000,000 tons of standard coals thereupon, and is suitable with the stock number of conventional gas.In the recovery process in colliery, the formidable enemy that the coal-seam gas of association is kept the safety in production really, the general practice is the discharging of ventilating, annual according to statistics to the airborne release coal-seam gas up to 200 billion cubic meters, not only polluted local environment, simultaneously Global climate change has been exerted an influence, aggravation " Greenhouse effect ".
Coal-seam gas is the mixed gas that is rich in methane, for the coal-seam gas of a large amount of medium methane contents (volumetric concentration 26-70%) usually can be directly as domestic fuel or be used for generating, but consumption is limited; If it is natural or be applied to chemical field coal-seam gas will to be made compression, then the methane content of coal-seam gas must be brought up to more than 95%, adopt transformation absorption or low ternperature separation process usually.
No matter adopt any technological method enrichment method methane, necessary first deoxidation is to get rid of explosion hazard, also want desulfurization, decarburization simultaneously, owing to contain intermediate concentration methane coal-seam gas oxygen level height, therefore adopt which kind of concentration method investment all bigger, concentrated cost is higher, and then has influenced the comprehensive utilization of coal-seam gas.
In the prior art, utilize methane to prepare hydrogen or hydrogen alkane (adulterant of 5%-50%V hydrogen and 50%-95%V Sweet natural gas) is the popular domain of scientists study, and prepare the used raw material of hydrogen with methane mainly is Sweet natural gas, and major ingredient is a methane (〉 90% in the Sweet natural gas), hydrogen is a kind of important industrial raw material and the fuel of application prospect light, traditional hydrogen production process is converted into the master with hydro carbons multistage high pressure high temperature vapor such as water electrolysis and methane, the process of hydro carbons vapor reforming hydrogen production is owing to controlled by thermodynamic(al)equilibrium, usually under worst hot case, carry out, reaction process need be burnt a large amount of Sweet natural gases to keep the required temperature of reaction, in order to obtain pure hydrogen, also need a series of conversion and scavenging process, improved pure hydrogen production cost.
Dalian Inst of Chemicophysics, Chinese Academy of Sciences discloses the method for a kind of methane catalytic decomposition hydrogen manufacturing or hydrogen alkane, and patents, and the patent No. is CN00123124.3; Methane catalytic pyrolysis under non-oxide condition is produced hydrogen or hydrogen alkane, only contains methane and hydrogen in the reactor product gas; Its reaction conditions is: temperature of reaction is 400--700 ℃, and reaction pressure is 0.05-1MPa, and the methane air speed is 0.5-50h
-1The main active component of catalyst system therefor is one or more among Fe, Co, the Ni, is properties-correcting agent with IA, IIA, IIIA, rare earth or B family transition element.
The technical scheme of this patent disclosure is: methane catalytic pyrolysis under non-oxide condition produces hydrogen or hydrogen alkane, only contain methane and hydrogen in the reactor product gas, do not contain CO, the technical scheme that analyzing this patent provides is not difficult to find out this scheme and unexposed to the instruction of those of ordinary skills according to this patent, just can implement its patent without creative work.
The applicant is that the Chinese patent application 89109001.0 of U.S. Davy Mckee Corp. discloses the preparation of hydrogen in the hydrocarbon material, by with raw material catalyzing part oxidation under the temperature of avoiding producing uncombined carbon and steam condition, it comprises hydrogen, carbon monoxide and carbonic acid gas to produce synthetic gas then; Carbon monoxide is changed into carbonic acid gas by water-gas shift reaction; Remove carbonic acid gas, from hydrocarbon material, produce hydrogen-rich gas.
The technology of utilizing coal-seam gas to prepare hydrogen in the prior art yet there are no report.
Summary of the invention
Goal of the invention of the present invention is intended to overcome above-mentioned prior art and lacks limit, a kind of method of utilizing coal-seam gas to prepare hydrogen is provided, this method can effectively solve the coal-seam gas of medium methane content (volumetric concentration 26%--70%) and be translated into hydrogen, thereby has improved the utility value of coal-seam gas.
Goal of the invention of the present invention is achieved by following technical proposals:
Coal-seam gas is added suitable water vapour, under the effect of catalyzer, utilize the inflammable gas in the coal-seam gas and the reaction heat of oxygen, make methane and water vapour generation conversion reaction, generate rich hydrogenous gas mixture,, obtain hydrogen richness and be 99-99.99% product gas again by transformation absorption.
Wherein:
The mol ratio of methane is 1-4 in water vapour and the coal-seam gas, and service temperature 400--850 ℃, working pressure are 0.15-0.7MPa, and the pressure that enters the pressure-swing absorption apparatus gas mixture is 1.4-1.8MPa;
Methane content in the coal-seam gas is 26～70%.
Above-mentioned conversion reaction is that (Autothermal Reform ATR) promptly in the presence of catalyzer, utilizes the combustion reactions heat of inflammable gas (as methane, hydrogen, carbon monoxide) and oxygen, makes methane and water vapor carry out conversion reaction, the generation synthetic gas from thermal transition.
Said catalyzer is the Ni catalyst series.
Under the guidance of above-mentioned principle, coal-seam gas is pressurized to enters desulfurizer, add water vapour in the coal-seam gas after desulfurization, enter into from heat conversion device, utilize combustion reactions heat to make methane and water vapour generation conversion reaction, generate hydrogen, carbon monoxide and carbonic acid gas and nitrogen etc., the gas mixture that contains hydrogen, carbon monoxide and carbonic acid gas and nitrogen etc. directly enters pressure-swing absorption apparatus through waste heat recovery heat and cooling pressurization, obtains the hydrogen product of 99-99.99% (volume fraction); Present method is applicable to the coal-seam gas hydrogen manufacturing that contains methane 26%---40%.
Perhaps, the coal-seam gas pressurization is entered desulfurizer, add water vapour in the coal-seam gas after desulfurization, enter into self-heating pre-converted device, utilize combustion reactions heat to make methane and water vapour generation conversion reaction, generate hydrogen, carbon monoxide, carbonic acid gas and methane etc., contain hydrogen, carbon monoxide, the gas mixture of carbonic acid gas and methane etc. enters the steam reforming reaction device, unreacted methane further reacts with water vapour, methane concentration is further reduced, outer heating of steam reforming reaction device, gas mixture passes through waste heat recovery, the pressurization of cooling back enters pressure-swing absorption apparatus, obtains the hydrogen product that purity is 99-99.99% (volume fraction) by transformation absorption; Present method is applicable to that containing methane surpasses 40% to 70% coal-seam gas hydrogen manufacturing.
In addition, the coal-seam gas pressurization is entered desulfurizer, add water vapour in the coal-seam gas after desulfurization, enter into self-heating pre-converted device, utilize combustion reactions heat to make methane and water vapour generation conversion reaction, generate hydrogen, carbon monoxide, carbonic acid gas and methane etc., contain hydrogen, carbon monoxide, the gas mixture of carbonic acid gas and methane etc. enters the steam reforming reaction device, unreacted methane further reacts with water vapour, methane concentration is further reduced, outer heating of steam reforming reaction device, gas mixture produces steam and enters changing device afterwards by waste heat recovery, is hydrogen and carbonic acid gas at this carbon monoxide and water vapour response transform, the gas mixture cooling and the pressurization of the hydrogeneous and carbonic acid gas after conversion enter pressure-swing absorption apparatus, obtain the hydrogen product that purity is 99-99.99% (volume fraction) by transformation absorption; Present method is applicable to that containing methane surpasses 45% to 70% coal-seam gas hydrogen manufacturing.
Compared with prior art, the present invention has outstanding feature in following several respects:
First: effectively solved the problems affect of utilizing of coal-seam gas, turned waste into wealth, and can produce direct economic benefit.
Second: the new industrial use that the invention provides the coal-seam gas of medium methane content (volumetric concentration 26%--70%).
The the 3rd: initiated the processing method of carrying out the autothermal reforming hydrogen manufacturing, avoided the deoxygenation problem of methane chemical utilization to oxygen in the gas utilization coal-seam gas of medium methane content (volumetric concentration 26%--70%).
The 4th: this method investment is little, and product cost is hanged down the economic benefit height.
Description of drawings
Fig. 1 is a process flow sheet of the present invention;
Fig. 2 is a process flow sheet of the present invention;
Fig. 3 is a process flow sheet of the present invention.
Embodiment
Below in conjunction with embodiment the present invention is further described.
Embodiment 1: as shown in Figure 1, coal-seam gas is pressurized to enters desulfurizer, add water vapour in the coal-seam gas after desulfurization, heating enters into from heat conversion device, utilize combustion reactions heat to make methane and water vapour generation conversion reaction, generate hydrogen, carbon monoxide and carbonic acid gas and nitrogen, the gas mixture that contains hydrogen, carbon monoxide and carbonic acid gas and nitrogen is forced into through the cooling of waste heat recovery heat and directly enters pressure-swing absorption apparatus, obtains the hydrogen product of 99.9% (volume fraction);
Unstripped gas consist of methane 30%, surplus is air, is 500 ℃ from the heat conversion device inlet temperature, pressure 0.65MPa, H
2O/C=4, temperature out are 670 ℃; The gained gas mixture is formed (butt): H
245.8%, CO 4.9%, N
235.3%, CO
212.2%, CH
41.8%; Enter pressure-swing absorption apparatus pressure 1.8MPa, catalyzer is the Ni catalyst series.
10Nm
3It is that 99.9% pure hydrogen production gas is 5.6Nm that unstripped gas obtains purity
3
Embodiment 2: as shown in Figure 3, the coal-seam gas pressurization is entered desulfurizer, add water vapour in the coal-seam gas after desulfurization, heating enters into self-heating pre-converted device, utilize combustion reactions heat to make methane and water vapour generation conversion reaction, generate hydrogen, carbon monoxide, carbonic acid gas, methane and nitrogen, contain hydrogen, carbon monoxide, carbonic acid gas, the gas mixture of methane and nitrogen enters the steam reforming reaction device, unreacted methane further reacts with water vapour, methane concentration is reduced to below 2%, outer heating of steam reforming reaction device, gas mixture passes through waste heat recovery, enter changing device after producing steam, at this carbon monoxide and water vapour response transform is hydrogen and carbonic acid gas, the gas mixture cooling and the pressurization of the hydrogeneous and carbonic acid gas after conversion enter pressure-swing absorption apparatus, obtain the hydrogen product that purity is 99.99% (volume fraction) by transformation absorption; Present method is applicable to that containing methane surpasses 45% to 70% coal-seam gas hydrogen manufacturing.
Unstripped gas consist of methane 60%, surplus is air, is 500 ℃ from the heat conversion device inlet temperature, pressure 0.65MPa, H
2O/C=3, steam reforming temperature out are 820 ℃; The gained gas mixture is formed (butt): H
269.6%, CO 2.4%, N
210.6%, CO
216.9%, CH
40.5%; Enter pressure-swing absorption apparatus pressure 1.4MPa, catalyzer is the Ni catalyst series.
10Nm
3It is that 99.99% pure hydrogen production gas is 17.3Nm that unstripped gas obtains purity
3
Embodiment 3: as shown in Figure 2, coal-seam gas is pressurized to enters desulfurizer, add water vapour in the coal-seam gas after desulfurization, heating enters into self-heating pre-converted device, utilize combustion reactions heat to make methane and water vapour generation conversion reaction, generate hydrogen, carbon monoxide and carbonic acid gas and nitrogen etc., the gas mixture that contains hydrogen, carbon monoxide and carbonic acid gas and nitrogen etc. directly enters pressure-swing absorption apparatus through waste heat recovery heat cooling pressurization, obtains the hydrogen product of 99% (volume fraction);
Unstripped gas consist of methane 50%, surplus is air, is 500 ℃ from the heat conversion device inlet temperature, pressure 0.65MPa, H
2820 ℃ of O/C=4 steam reformer reactors temperature outs; The gained gas mixture is formed (butt): H
262.9%, CO 10.5%, N
216.5%, CO
29.9%, CH
40.2%; Enter pressure-swing absorption apparatus pressure 1.6MPa, catalyzer is the Ni catalyst series.
10Nm
3It is that 99% pure hydrogen production gas is 12.2Nm that unstripped gas obtains purity
3
Embodiment 4: press the processing method of embodiment 2, unstripped gas consist of methane 30%, surplus is air, is 600 ℃ from the heat conversion device inlet temperature, pressure 0.65MPa, H
2O/C=1,787 ℃ of steam reformer reactors temperature outs; The gained gas mixture is formed (butt): H
241.8%, CO 13.1%, N
237.9%, CO
25.3%, CH
41.9%; Enter pressure-swing absorption apparatus pressure 1.8MPa, catalyzer is the Ni catalyst series.
10Nm
3It is that 99% pure hydrogen production gas is 4.7Nm that unstripped gas obtains purity
3
Embodiment 5: press the processing method of embodiment 1, unstripped gas consist of methane 50%, surplus is air, is 400 ℃ from the heat conversion device inlet temperature, pressure 0.65MPa, H
2O/C=3,820 ℃ of steam reformer reactors temperature outs; The gained gas mixture is formed (butt): H
262.0%, CO 12.3%, N
216.9%, CO
28.4%, CH
40.4%; Enter pressure-swing absorption apparatus pressure 1.8MPa, catalyzer is the Ni catalyst series.
10Nm
3It is that 99.9% pure hydrogen production gas is 11.7Nm that unstripped gas obtains purity
3
Embodiment 6: press the processing method of embodiment 2, unstripped gas consist of methane 30%, surplus is air, is 600 ℃ from the heat conversion device inlet temperature, pressure 0.16MPa, H
2O/C=3,707 ℃ of steam reformer reactors temperature outs; The gained gas mixture is formed (butt): H
247.6%, CO 7.6%, N
234.1%, CO
210.5%, CH
40.2%; Enter pressure-swing absorption apparatus pressure 1.8MPa, catalyzer is the Ni catalyst series.
10Nm
3It is that 99% pure hydrogen production gas is 6.0Nm that unstripped gas obtains purity
3
Embodiment 7: press the processing method of embodiment 2, unstripped gas consist of methane 26%, surplus is air, is 854 ℃ from the heat conversion device inlet temperature, pressure 0.65MPa, H
2820 ℃ of O/C=4 steam reformer reactors temperature outs; The gained gas mixture is formed (butt): H
241.7%, CO 8.9%, N
240.5%, CO
28.8%, CH
40.1%; Enter pressure-swing absorption apparatus pressure 1.8MPa, catalyzer is the Ni catalyst series.
10Nm
3It is that 99% pure hydrogen production gas is 4.7Nm that unstripped gas obtains purity
3
Embodiment 8: press the processing method of embodiment 1, unstripped gas consist of methane 70%, surplus is air, is 600 ℃ from the heat conversion device inlet temperature, pressure 0.65MPa, H
2O/C=3,840 ℃ of steam reformer reactors temperature outs; The gained gas mixture is formed (butt): H
269.8%, CO 14.2%, N
27.7%, CO
27.8%, CH
40.5%; Enter pressure-swing absorption apparatus pressure 1.8MPa, catalyzer is the Ni catalyst series.
10Nm
3It is that 99% pure hydrogen production gas is 17.8Nm that unstripped gas obtains purity
3
Claims (1)
1, a kind of coal-seam gas prepares the method for hydrogen, it is characterized in that: this method adds suitable water vapour with coal-seam gas, under the effect of catalyzer, utilize the reaction heat of the oxygen in inflammable gas and the coal-seam gas, make methane and water vapour generation conversion reaction, generate rich hydrogenous gas mixture, by transformation absorption, obtain product hydrogen again;
Wherein:
The mol ratio of methane is 1-4 in water vapour and the coal-seam gas, and service temperature 400--850 ℃, working pressure are 0.15-0.7MPa, and the pressure that enters the pressure-swing absorption apparatus gas mixture is 1.4-1.8MPa;
Methane content in the described coal-seam gas is 26～70%.
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| CN102225745B (en) * | 2010-07-29 | 2012-11-21 | 西南化工研究设计院 | Preparation process for power generation fuel gas from low-quality coal bed gas |
| CN102502496A (en) * | 2011-10-10 | 2012-06-20 | 西南化工研究设计院 | Method for manufacturing ammonia synthesis gas by using low-quality coal bed methane |
| US20220298086A1 (en) * | 2019-09-03 | 2022-09-22 | National University Corporation Shizuoka University | Methane producing method and production system |
| CN115259085A (en) * | 2022-07-04 | 2022-11-01 | 广东能源集团科学技术研究院有限公司 | Preparation method of high-purity hydrogen |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1420077A (en) * | 2001-11-16 | 2003-05-28 | 张惊涛 | Method for producing synthetic gas from coal mine gas |
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| CN1420077A (en) * | 2001-11-16 | 2003-05-28 | 张惊涛 | Method for producing synthetic gas from coal mine gas |
Non-Patent Citations (2)
| Title |
|---|
| 甲烷制备高纯度氢气的实验研究. 李传统.南京师范大学学报（工程技术版），第4卷第4期. 2004 |
| 甲烷制备高纯度氢气的实验研究. 李传统.南京师范大学学报（工程技术版），第4卷第4期. 2004 * |
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Effective date of registration: 20191216 Address after: 611430 No.777, Xinghua 10th Road, dengshuang Town, Xinjin County, Chengdu City, Sichuan Province (Industrial Park) Patentee after: HAO HUA (CHENGDU) TECHNOLOGY Co.,Ltd. Address before: 610255 box 445, South Airport Road, Sichuan, Chengdu Patentee before: SOUTHWEST RESEARCH & DESIGN INSTITUTE OF CHEMICAL INDUSTRY |
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