CN104710281B - A kind of methanol-fueled CLC reaction gas is used for methyl alcohol pre-rectifying tower heating process - Google Patents
A kind of methanol-fueled CLC reaction gas is used for methyl alcohol pre-rectifying tower heating process Download PDFInfo
- Publication number
- CN104710281B CN104710281B CN201510117322.9A CN201510117322A CN104710281B CN 104710281 B CN104710281 B CN 104710281B CN 201510117322 A CN201510117322 A CN 201510117322A CN 104710281 B CN104710281 B CN 104710281B
- Authority
- CN
- China
- Prior art keywords
- methyl alcohol
- rectifying tower
- alcohol pre
- methanol
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention discloses a kind of methanol-fueled CLC reaction gas for methyl alcohol pre-rectifying tower heating process, mainly comprises methanol-fueled CLC reaction gas and heats thermal source as methyl alcohol pre-rectifying tower reboiler, then with methyl alcohol pre-rectifying tower charging heat exchange; Methyl alcohol pre-rectifying tower tower top working pressure is negative pressure, methyl alcohol pre-rectifying tower tower top working pressure is by water ring vacuum pump control, the tower top non-condensable gas extracted out from water ring vacuum pump send fuel gas pipe network after overcooling, water ring vacuum pump adds certain quantity of fresh water, extraction a certain amount of circulation fluid controlled circulation vacuum pump circulation fluid storage tank liquid level simultaneously, the circulation fluid of extraction send methyl alcohol pre-rectifying tower backflash as methyl alcohol pre-rectifying tower phegma.
Description
Technical field
The present invention relates to the preparing technical field of methyl alcohol, especially a kind of methanol-fueled CLC reaction gas is used for methyl alcohol pre-rectifying tower heating process.
Background technology
At present, after methyl alcohol synthetic reactor exports reaction gas and synthesizes charging inlet tower gas heat exchange, adopt water-cooled or empty cold building-up reactions gas is cooled to normal temperature, the condensations such as methyl alcohol that synthesis generates, water are got off, then through gas-liquid separation, the liquid separated is as crude carbinol, and the gas major part circulation separated, small portion of gas is as discharging gas eliminating.
Due to synthesis charging inlet tower gas heat exchange after methanol-fueled CLC reaction gas temperature be usually less than 100 DEG C, a large amount of low position heat contained in reaction gas cannot utilize, the condensation such as water-cooled or the empty cold methyl alcohol by methanol-fueled CLC generation, water can only be adopted to get off, a large amount of heat is released in condensation, it is necessary to consumes a large amount of water coolants or consumes empty cold required electric energy.
Methyl alcohol pre-rectifying tower adopts the method for rectifying to be deviate from from tower top by the light constituent in crude carbinol, methyl alcohol pre-rectifying tower tower reactor adopts steam to heat usually, methyl alcohol pre-rectifying tower tower top working pressure is about 0.02��0.05Mpa (G), bottom temperature about 82��87 DEG C. In order to the light constituent deviate from crude carbinol, methyl alcohol pre-rectifying tower needs a certain amount of quantity of reflux, namely needs to provide certain heating thermal source in tower reactor.
How to make full use of the resource in each link in methyl alcohol preparation process, reduce energy consumption, reduce cost be at present needed for.
Summary of the invention
In order to solve above technical problem, the present invention provides a kind of methanol-fueled CLC reaction gas for methyl alcohol pre-rectifying tower heating process, saves methyl alcohol pre-rectifying tower reboiler heating thermal source, reduces cooling methanol-fueled CLC reaction gas water coolant simultaneously, energy-saving and cost-reducing.
A kind of methanol-fueled CLC reaction gas solved in the present invention of above technical problem is characterized in that for methyl alcohol pre-rectifying tower heating process: comprises the following steps:
(1) methanol-fueled CLC reaction gas removes synthetic water water cooler after methyl alcohol pre-rectifying tower reboiler E1 heat exchange;
(2) crude carbinol enter methyl alcohol pre-rectifying tower feed exchanger E2 heat after, enter methyl alcohol pre-rectifying tower rectifying, tower top out gas enter overhead condenser E3, tower reactor out liquid go pressurizing tower;
(3) phlegma that overhead condenser E3 isolates enters backflash V1, then sends into methyl alcohol pre-rectifying tower tower top by reflux pump P1, and the gas isolated enters water ring vacuum pump P2 supercharging, then enters circulation liquid bath V2 and be separated;
(4) circulation liquid bath non-condensable gas out enters exhaust gas cooler E5 and cools, and the non-condensable gas after cooling send fuel pipe network or torch, and the phlegma after cooling enters circulation liquid bath V2 again;
(5) liquid in circulation liquid bath return after circulation fluid water cooler E4 cools vacuum pump isolate non-condensable gas with overhead condenser E3 together with supercharging enter circulation liquid bath V2 again, so repeatedly.
In described step (1), methanol-fueled CLC reaction gas is through methyl alcohol pre-rectifying tower reboiler E1 heat exchange, then removes synthetic water water cooler after methyl alcohol pre-rectifying tower feed exchanger E2, continues to reclaim the low position heat of methyl alcohol reaction gas.
Methanol-fueled CLC reaction gas is the methanol-fueled CLC reaction gas after synthesis charging inlet tower gas heat exchange. By with synthesis charging inlet tower gas heat exchange after methanol-fueled CLC reaction gas be used for the heating of methyl alcohol pre-rectifying tower tower reactor, save thermal source needed for rectifying, reduce the required water coolant of cooling simultaneously.
In the present invention, prioritization scheme is described methyl alcohol pre-rectifying tower tower top pressure is negative pressure, and vacuum magnitude is determined according to methanol-fueled CLC reacting gas pressure.
Owing to methyl alcohol pre-rectifying tower bottom temperature is greater than 80 DEG C usually, and synthetic gas temperature is less than 100 DEG C, for the thermal Finite utilized, can not meet methyl alcohol pre-rectifying tower tower reactor institute heat requirement. Methyl alcohol pre-rectifying tower tower pre-operation pressure is negative pressure, and vacuum magnitude is determined according to building-up reactions atmospheric pressure. Synthesis pressure height, negative pressure is little; Synthesis pressure is low, and negative pressure is big. When other conditions are constant, methyl alcohol pre-rectifying tower bottom temperature changes with working pressure, working pressure height, bottom temperature height; Working pressure is low, and bottom temperature temperature is low. Thus methyl alcohol pre-rectifying tower working pressure is reduced, just can reduce tower reactor service temperature, thus strengthen building-up reactions gas and methyl alcohol pre-rectifying tower bottom temperature gap, make low position heat contained by synthetic gas meet methyl alcohol pre-rectifying tower tower reactor and heat institute's heat requirement.
Described water ring vacuum pump adds water, sends into methyl alcohol pre-rectifying tower tower top by reflux pump P1 together with the phlegma that simultaneously extraction certain quantity of fluid is isolated to backflash V1 and overhead condenser E3 from gas-liquid separator V2, with controlled circulation liquid level of liquid tank.
Described water ring vacuum pump adds the water yield according to sending methyl alcohol contained by the non-condensable gas of fuel gas pipe network or flare system to determine after cooling, and non-condensable gas, containing methyl alcohol height, adds fresh water amount big, and vice versa.
In the present invention, methanol-fueled CLC reaction gas is as the heating of methyl alcohol pre-rectifying tower reboiler and methyl alcohol pre-rectifying tower charging heating thermal source, save methyl alcohol pre-rectifying tower reboiler heating thermal source, reduce cooling methanol-fueled CLC reaction gas water coolant, to reach energy-saving and cost-reducing object simultaneously; Water ring vacuum pump extract out and in the non-condensable gas that cools methanol content low, reach the object reclaiming methyl alcohol in non-condensable gas.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of embodiment 1 in the present invention
Fig. 2 is the schematic flow sheet of embodiment 2 in the present invention
Wherein, number in the figure is specially: 1. methyl alcohol pre-rectifying tower reboiler E12. methyl alcohol pre-rectifying tower feed exchanger E23. overhead condenser E34. circulation fluid water cooler E45. exhaust gas cooler E56. synthetic water water cooler 7. methyl alcohol pre-rectifying tower 8. backflash V19. water ring vacuum pump 10. circulates liquid bath V211. reflux pump P112. pressurizing tower
Embodiment
The present invention's methanol-fueled CLC reaction gas heats thermal source as methyl alcohol pre-rectifying tower reboiler, then with methyl alcohol pre-rectifying tower charging heat exchange, methyl alcohol pre-rectifying tower working pressure is negative pressure, methyl alcohol pre-rectifying tower tower top working pressure is by water ring vacuum pump control, the tower top non-condensable gas extracted out from water ring vacuum pump send fuel gas pipe network after overcooling, water ring vacuum pump adds certain quantity of fresh water, the a certain amount of circulation fluid controlled circulation liquid level of liquid tank of extraction simultaneously, the circulation fluid of extraction send methyl alcohol pre-rectifying tower backflash as methyl alcohol pre-rectifying tower phegma.
Below in conjunction with embodiment, the present invention is described in further detail, but this should not being interpreted as, the scope of the above-mentioned theme of the present invention is only limitted to following embodiment:
Embodiment 1
It is as follows that the methanol-fueled CLC reaction gas of the present embodiment is used for methyl alcohol pre-rectifying tower heating procedure:
Enter the methanol-fueled CLC reaction gas temperature 85 DEG C (in 200,000 tons/year of methyl alcohol) of methyl alcohol pre-rectifying tower reboiler, pressure 6.8MPa(A).
As flow process as shown in Figure 1, methanol-fueled CLC reaction gas temperature 85 DEG C, temperature about 70 DEG C after methyl alcohol pre-rectifying tower reboiler E1 heat exchange, then through methyl alcohol pre-rectifying tower feed exchanger E2 heat exchange, methanol-fueled CLC reaction gas temperature is down to 67 DEG C of water coolers that anhydrate. Crude carbinol enters methyl alcohol pre-rectifying tower feed exchanger E2 temperature after heating about 63 DEG C, enters methyl alcohol pre-rectifying tower rectifying T. Methyl alcohol pre-rectifying tower tower top pressure controls at 0.07MPa(A) methyl alcohol pre-rectifying tower tower reactor pressure 0.1MPa(A), bottom temperature 65 DEG C. The liquid isolated from methyl alcohol pre-rectifying tower tower reactor goes pressurizing tower, tower top out gas be separated through condenser E3, outlet noncondensable gas temperature 40 DEG C, phlegma enters backflash V1, then by reflux pump P1 send into methyl alcohol pre-rectifying tower tower top; Non-condensable gas enters water ring vacuum pump P2 and is supercharged to 0.12Mpa (A), then enters circulation liquid bath V2 and is separated. Circulation liquid bath non-condensable gas out enters after exhaust gas cooler E5 is cooled to 40 DEG C again and send fuel pipe network or torch, and phlegma returns in circulation liquid bath V2; Liquid (circulation fluid) major part that circulation liquid bath V2 separates returns water ring vacuum pump after circulation fluid water cooler E4 cools, and together with isolating non-condensable gas with overhead condenser E3, supercharging enters circulation liquid bath V2 again, so repeatedly; Small portion circulation fluid extraction enters in methyl alcohol pre-rectifying tower to backflash V1 through reflux pump P1 again. Circulation fluid at water ring vacuum pump provides fresh water 0.12t/h by import with the methanol concentration in controlled circulation liquid.
In this embodiment, methyl alcohol pre-rectifying tower reboiler heating thermal source is supplied by building-up reactions air lift, steam (by 1.0Mpa saturation steam)��9.5t/h is saved compared with adopting steam heating methanol pre-rectifying tower reboiler flow process, recirculated cooling water (by 8 DEG C of temperature difference)��600t/h is saved compared with adopting building-up reactions air water cold flow, methyl alcohol pre-rectifying tower tower top is negative pressure, rectifying non-condensable gas adopts water ring vacuum pump supercharging, compared with being malleation flow process with methyl alcohol pre-rectifying tower tower top, the electricity that consumes consumes 20KW more, but reduces methyl alcohol discharge��50kg/h.
Embodiment 2
It is as follows that the methanol-fueled CLC reaction gas of the present embodiment is used for methyl alcohol methyl alcohol pre-rectifying tower heating procedure:
Enter the methanol-fueled CLC reaction gas temperature 81 DEG C (in 100,000 tons/year of methyl alcohol) of methyl alcohol pre-rectifying tower reboiler, pressure 5.2MPa(A).
As flow process as shown in Figure 2, methanol-fueled CLC reaction gas temperature 81 DEG C, temperature about 67 DEG C after methyl alcohol pre-rectifying tower reboiler E1 heat exchange, then anhydrate water cooler. Crude carbinol enters methyl alcohol pre-rectifying tower feed exchanger E2 temperature after heating about 67 DEG C, enters methyl alcohol pre-rectifying tower rectifying T. Methyl alcohol pre-rectifying tower tower top pressure controls at 0.065MPa(A) methyl alcohol pre-rectifying tower tower reactor pressure 0.094MPa(A), bottom temperature 64 DEG C. From methyl alcohol pre-rectifying tower tower top out gas cool through overhead condenser E3, outlet noncondensable gas temperature��40 DEG C, phlegma enters condensation liquid bath V1, then by reflux pump P1 send into methyl alcohol pre-rectifying tower tower top; Non-condensable gas enters water ring vacuum pump P2 and is supercharged to 0.12Mpa (A), then enters circulation liquid bath V2 with water ring vacuum pump circulation fluid and is separated. Circulation liquid bath non-condensable gas out enters after exhaust gas cooler E5 is cooled to 40 DEG C again and send fuel pipe network or torch, and phlegma returns in circulation liquid bath V2; Liquid (circulation fluid) major part that circulation liquid bath V2 separates returns water ring vacuum pump after circulation fluid water cooler E4 cools, and together with isolating non-condensable gas with overhead condenser E3, supercharging enters circulation liquid bath V2 again, so repeatedly; Small portion circulation fluid (phegma) extraction, to backflash V1, enters in methyl alcohol pre-rectifying tower through reflux pump P1 again. Fresh water 0.06t/h is provided by import with the methanol concentration in controlled circulation liquid at vacuum pump circulation fluid.
In this embodiment, methyl alcohol pre-rectifying tower reboiler heating thermal source is supplied by building-up reactions air lift, steam (by 1.0Mpa saturation steam)��4.8t/h is saved compared with adopting steam heating methanol pre-rectifying tower reboiler flow process, recirculated cooling water (by 8 DEG C of temperature difference)��300t/h is saved compared with adopting building-up reactions air water cold flow, methyl alcohol pre-rectifying tower tower top is negative pressure, rectifying non-condensable gas adopts water ring vacuum pump supercharging, compared with being malleation flow process with methyl alcohol pre-rectifying tower tower top, the electricity that consumes consumes 12KW more, but reduces methyl alcohol discharge��25kg/h.
Claims (5)
1. a methanol-fueled CLC reaction gas is used for methyl alcohol pre-rectifying tower heating process, it is characterised in that: comprise the following steps:
Methanol-fueled CLC reaction gas is through methyl alcohol pre-rectifying tower reboiler E1(1) remove synthetic water water cooler (6) after heat exchange;
Crude carbinol enters methyl alcohol pre-rectifying tower feed exchanger E2(2) heating after, enter methyl alcohol pre-rectifying tower rectifying (7), tower top out gas enter overhead condenser E3(3), tower reactor out liquid go pressurizing tower (12);
(3) overhead condenser E3(3) phlegma isolated enters backflash V1(8), then by reflux pump P1(11) send into methyl alcohol pre-rectifying tower (7) tower top, the gas isolated enters water ring vacuum pump P2(9) supercharging, then enter circulation liquid bath V2(10) separation;
(4) circulation liquid bath V2(10) gas out enters exhaust gas cooler E5(5) cooling, the non-condensable gas after cooling send fuel pipe network or torch, and the phlegma after cooling enters circulation liquid bath V2(10 again);
(5) circulation liquid bath V2(10) in liquid through circulation fluid water cooler E4(4) cooling after return water ring vacuum pump (9) and overhead condenser E3(3) isolate gas together with supercharging enter circulation liquid bath V2(10 again), so repeatedly.
2. a kind of methanol-fueled CLC reaction gas according to claim 1 is used for methyl alcohol pre-rectifying tower heating process, it is characterized in that: in described step (1), methanol-fueled CLC reaction gas is through methyl alcohol pre-rectifying tower reboiler E1(1) heat exchange, then through methyl alcohol pre-rectifying tower feed exchanger E2(2) after remove synthetic water water cooler (6).
3. a kind of methanol-fueled CLC reaction gas according to claim 1 and 2 is used for methyl alcohol pre-rectifying tower heating process, it is characterised in that: described methyl alcohol pre-rectifying tower (7) tower top pressure is negative pressure, and vacuum magnitude is determined according to methanol-fueled CLC reacting gas pressure.
4. a kind of methanol-fueled CLC reaction gas according to claim 1 and 2 is used for methyl alcohol pre-rectifying tower heating process, it is characterized in that: described water ring vacuum pump adds water in (9), simultaneously from circulation liquid bath V2(10) extraction certain quantity of fluid to backflash V1(8) with overhead condenser E3(3) together with the phlegma isolated by reflux pump P1(11) send into methyl alcohol pre-rectifying tower (7) tower top, with controlled circulation liquid bath V2(10) liquid level.
5. a kind of methanol-fueled CLC reaction gas according to claim 4 is used for methyl alcohol pre-rectifying tower heating process, it is characterised in that: described water ring vacuum pump (9) add the water yield according to sending after cooling methyl alcohol contained by the non-condensable gas of fuel gas pipe network or flare system determine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510117322.9A CN104710281B (en) | 2015-03-18 | 2015-03-18 | A kind of methanol-fueled CLC reaction gas is used for methyl alcohol pre-rectifying tower heating process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510117322.9A CN104710281B (en) | 2015-03-18 | 2015-03-18 | A kind of methanol-fueled CLC reaction gas is used for methyl alcohol pre-rectifying tower heating process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104710281A CN104710281A (en) | 2015-06-17 |
| CN104710281B true CN104710281B (en) | 2016-06-01 |
Family
ID=53410076
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510117322.9A Active CN104710281B (en) | 2015-03-18 | 2015-03-18 | A kind of methanol-fueled CLC reaction gas is used for methyl alcohol pre-rectifying tower heating process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104710281B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106699610B (en) * | 2016-12-21 | 2019-01-18 | 武汉青江化工黄冈有限公司 | The dimethyl suflfate production process and device of low content dimethyl ether |
| CN112142559A (en) * | 2020-09-22 | 2020-12-29 | 吕永华 | Waste heat recovery device for methanol production |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201291075Y (en) * | 2008-10-21 | 2009-08-19 | 高恒 | High-efficiency environmental-protection methanol pre-rectifying device |
| CN101570466B (en) * | 2009-05-18 | 2012-07-04 | 西安石油大学 | Multi-effect rectifying process of methanol |
| CN203007175U (en) * | 2012-12-19 | 2013-06-19 | 新奥科技发展有限公司 | Heat integration device for methanol synthesis and rectification |
| CN204051035U (en) * | 2014-07-10 | 2014-12-31 | 师宗煤焦化工有限公司 | Utilize the rectifier unit of reformed gas condensate liquid waste-heat crude carbinol |
-
2015
- 2015-03-18 CN CN201510117322.9A patent/CN104710281B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN104710281A (en) | 2015-06-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103566613B (en) | A kind of low-concentration organic solvent aqueous solution reclaims heat pump distillation apparatus and technique | |
| CN104086371B (en) | The processing method that in the cyclohexene method preparing cyclohexanone production process, hexalin is separated | |
| CN104710281B (en) | A kind of methanol-fueled CLC reaction gas is used for methyl alcohol pre-rectifying tower heating process | |
| CN102643195A (en) | Production method of n-butyl acetate | |
| CN203095912U (en) | Methanol synthesis system | |
| CN102423539B (en) | Energy-saving technology of catalytic reaction distillation process and device thereof | |
| CN106380376A (en) | Synthesis system and preparation equipment | |
| CN205035295U (en) | Methanol synthesis reaction gas is used for methyl alcohol pre -rectifying tower heating system | |
| CN103288601A (en) | Cyclohexanol distillation method | |
| CN211111789U (en) | Thermal coupling device for recovering ethylene glycol rectification low-grade steam | |
| CN105130760A (en) | New technology for preparation of high purity MTBE | |
| CN105777491A (en) | Coarse methanol gas separation system and method | |
| CN102977989B (en) | Waste lubricating oil recycling regeneration production process | |
| CN113842852B (en) | Process and system for annual production of 20 ten thousand tons of methylamine | |
| CN203976674U (en) | Hexalin tripping device in the cyclohexene method preparing cyclohexanone production process | |
| CN212262408U (en) | Energy-saving carrier gas stripping system | |
| CN210314061U (en) | Rectification and purification device for synthesizing dimethyl oxalate by carbonylation of coal-made ethylene glycol | |
| CN107501100A (en) | A kind of evacuation process system of m-phenylene diamine (MPD) vacuum rectification tower | |
| CN106316800B (en) | A kind of low power consuming by preparing dimethyl ether from methanol method | |
| CN113546438A (en) | Heat integration system and method for gas-steam combined cycle, methanol synthesis and five-tower rectification | |
| CN203907580U (en) | Condensate water recovery system based on condensation water returning heat exchanger | |
| CN103588734B (en) | Recovery method and recovery device of butyl ester and acetone in ketene dimer production | |
| CN105175223A (en) | Methanol pre-rectifying tower heating system utilizing methanol synthesis reaction gas | |
| CN203568999U (en) | Reaction separation system and device for preparing polyoxymethylene dimethyl ethers | |
| CN207267848U (en) | A kind of evacuation process system of m-phenylene diamine (MPD) vacuum rectification tower |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee after: Haohua Chemical Technology Group Co., Ltd. Address before: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee before: Tianyi Science and Technology Co., Ltd., Sichuan Prov |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200427 Address after: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee after: SOUTHWEST RESEARCH & DESIGN INSTITUTE OF CHEMICAL INDUSTRY Address before: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610041 Patentee before: Haohua Chemical Technology Group Co., Ltd. |