CN103275757B - A kind of method of oil gas coupling Poly-generation in Chemical Industry - Google Patents
A kind of method of oil gas coupling Poly-generation in Chemical Industry Download PDFInfo
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Abstract
The invention provides the method for oil gas coupling Poly-generation in a kind of Chemical Industry, comprise the following steps: the frequent decompression distillation system of coal tar and de-chemical systems process are divided into heavy oil fraction, crude phenols, dephenolize oil, thick naphthalene, de-naphtalene oil and washing oil, crude phenols and thick naphthalene are discharged, and heavy oil fraction, washing oil, dephenolize oil and de-naphtalene oil send into oil gas coupled system; Coal gas obtains LPG, gasoline, durol and de-hydrocarbon mink cell focus through methanol conversion system and the process of MTG system, and LPG, gasoline and durol are discharged, and de-hydrocarbon mink cell focus sends into oil gas coupled system; Carry out coupling hydro process at oil gas coupled system and obtain petroleum naphtha and diesel oil; Burnt oil and gas is carried out efficient coupling, avoids the wasting of resources, produce the chemicals such as high added value oil product and phenol, naphthalene, aromatic hydrocarbons; Avoid coal gas, the direct discharge of tar, reduce environmental pollution, more environmental protection.
Description
Technical field
The invention belongs to coal chemical technology, relate to oil in Chemical Industry, gas coupling Poly-generation technology, particularly relate to the method for oil gas coupling Poly-generation in a kind of Chemical Industry.
Background technology
Existing Chemical Industry comprises coking, the dry distillation of coal, gasification, DCL/Direct coal liquefaction and indirect liquefaction etc., all can produce gas and tar in wherein coking, the dry distillation of coal, gasification.At present, in coking industry, the coke-oven gas that coke-oven plant produces and tar great majority are discharged or direct burn processing, this way contaminate environment, waste resource.Be only limitted to synthesizing methanol to the recycling of coke-oven gas, added value of product is not high yet; In dry distillation of coal industry, the pyrolysis gas that pyrolysis is produced and tar, more single to coal tar processing means at present, product price is lower; The direct burn processing of pyrolysis gas, waste resource pollution environment.In gasification industry, meeting generating portion tar, existing gasification plant major part is distilled the employing of this part tar and is extracted the method for chemical, and mink cell focus is not used, and can produce phenols sewage in this technique, and products obtained therefrom quality is low, cheap.
If a kind of technique can be developed, the oil in Chemical Industry, gas are effectively utilized, the integral benefit of Chemical Industry can be improved, reduce environmental pollution.
Summary of the invention
It is low that the object of the invention is to solve coal gas and tar utilization ratio in prior art, and the problem that added value of product is low, provides the method for oil gas coupling Poly-generation in a kind of Chemical Industry, improve coal gas and tar utilization ratio, produce high value added product.
For achieving the above object, the present invention is by the following technical solutions:
A method for oil gas coupling Poly-generation in Chemical Industry, comprises the following steps:
(1) the frequent decompression distillation system of coal tar and de-chemical systems process are divided into heavy oil fraction, crude phenols, dephenolize oil, thick naphthalene, de-naphtalene oil and washing oil, crude phenols and thick naphthalene are discharged as product, and heavy oil fraction, washing oil, dephenolize oil and de-naphtalene oil send into oil gas coupled system; The coal gas produced in Chemical Industry obtains LPG, gasoline, durol and de-hydrocarbon mink cell focus through methanol conversion system and the process of MTG system, and LPG, gasoline and durol are discharged as product, and de-hydrocarbon mink cell focus sends into oil gas coupled system;
(2) carry out coupling hydro process after entering the heavy oil fraction of oil gas coupled system, washing oil, dephenolize oil, de-naphtalene oil and the mixing of de-hydrocarbon mink cell focus and obtain petroleum naphtha and diesel oil.
In described step (1), the concrete grammar of the frequent decompression distillation system of coal tar and de-chemical systems process is: coal tar is divided into light oil fraction and heavy oil fraction through atmospheric distillation tower distillation, light oil fraction enters vacuum still again and is cut into carbolic oil, naphtalene oil and washing oil, carbolic oil obtains crude phenols and dephenolize oil through proposing phenol process, and naphtalene oil obtains thick naphthalene and de-naphtalene oil through proposing naphthalene process.
Coal gas through the concrete grammar of methanol conversion system and the process of MTG system is: coal gas obtains crude carbinol through the process of methanol conversion system, and crude carbinol is sent into the process of MTG system and obtained LPG, gasoline, durol and de-hydrocarbon mink cell focus.
The concrete grammar that coal gas produces crude carbinol through the process of methanol conversion system is: coal gas enters in low-temperature rectisol reactor and removes CO
2, SO
2and COS, then enter pure oxygen catalytic partial oxidation conversion system, by the CH in coal gas
4and C
mh
nchange into CO and H
2, be converted into crude carbinol finally by methanol-fueled CLC device.
The concrete grammar that crude carbinol sends into the process of MTG system is: crude carbinol is through MTG reactor methanol synthetic oil, methanol-fueled CLC oil carries out gas-liquid separation through degassing tower, isolated liquid enters liquefied gas knockout tower and obtains C3 hydrocarbon and C4 hydrocarbon mixture and LPG, with more than C4 hydro carbons and raw gasline, raw gasline is sent into rectifying tower process and is obtained petroleum naphtha and heavy petrol, and heavy petrol enters rectifying tower and obtains durol and arrive de-hydrocarbon mink cell focus.
The concrete grammar of coupling hydro process is in described step (2): after heavy oil fraction, washing oil, dephenolize oil, de-naphtalene oil and the mixing of de-hydrocarbon mink cell focus and hydrogen reaction carry out pre-treatment, feed again and obtain the thick oil product of hydrogenation into hydrofining reactor process, the thick oil product of hydrogenation enters gas-liquid separator and carries out gas-liquid separation, isolate hydrogen and thick oil product, thick oil product enters in separation column and carries out cut cutting, obtains petroleum naphtha and diesel oil.
Described coal tar be coking produce coal tar, pyrolysis produce coal tar, gasification produce tar in one or more mixture.
Described coal gas be pyrolysis produce pyrolysis gas, coking produce coke(oven)gas, gasification produce synthetic gas in one or more mixture.
Compared with prior art, beneficial effect of the present invention is:
(1) maximally utilise in Chemical Industry and produce coal tar oil and gas burnt oil and gas is carried out efficient coupling, avoid the wasting of resources, produce the chemicals such as high added value oil product and phenol, naphthalene, aromatic hydrocarbons, solve existing coal gas, tar production means mode is single, the problem that product price is lower, has more economy.
(2) to the further coupling hydro process of mink cell focus that tar distillation produces, the method that prior art tar adopts distillation extraction chemical is solved, the problem that mink cell focus is not used.
(3) avoid coal gas and tar to be discharged or direct burn processing, reduce environmental pollution, more environmental protection.
(4) technological flexibility is strong, and the various kinds of coal gas of Chemical Industry and coal tar all can make raw materials for production, are applicable to coking industry, are applicable to again dry distillation of coal industry, are also applicable to gasification industry.
Accompanying drawing explanation
Fig. 1 is system of the present invention composition structure iron.
Fig. 2 is the process flow sheet of the embodiment of the present invention one.
Fig. 3 is the process flow sheet of the embodiment of the present invention two.
1 tar storage tank, 2 atmospheric distillation towers, 3 vacuum stills, 4 mink cell focus tempering tanks, 5 soda-wash towers, 6 decomposition towers, 7 naphthalene distillation towers, 8 gas holders, 9 low-temperature rectisol reactors, 10 pure oxygen catalytic partial oxidation conversion systems, 11 methanol-fueled CLC devices, 12MTG reactor, 13 degassing towers, 14 liquefied gas knockout towers, 15 rectifying tower, 16 aromatic hydrocarbons rectifying tower, 17 pressure-swing absorption apparatuss, 18 pre-hydrogenators, 19 hydrofining reactors, 20 gas-liquid separators, 21 separation columns, 22 raw coal screening plants, 23 gas retorts, 24 pit kiln, 25 efficient cyclones, 26 vapourizing furnaces.
Embodiment
Describe the present invention below in conjunction with accompanying drawing:
As shown in Figure 1, be the composition structure iron of present system.
In Chemical Industry, oil gas coupling polygenerations systeme comprises atmospheric and vacuum distillation system A, de-chemical systems B, methanol conversion system C, MTG system D and oil gas coupled system E.Atmospheric and vacuum distillation system A take coal tar as raw material, be provided with 4 outlets, be carbolic oil outlet, naphtalene oil outlet, washing oil outlet, mink cell focus outlet respectively, carbolic oil outlet, naphtalene oil outlet, washing oil outlet are connected with de-chemical systems B entrance, and mink cell focus outlet is connected with oil gas coupled system E.
De-chemical systems B is provided with 2 products exports and 1 intermediate outlet, 2 products exports are crude phenols products export and thick naphthalene products export respectively, 1 intermediate outlet is dephenolize oil, takes off naphtalene oil, washing oil, mink cell focus mixture outlet, and dephenolize oil, de-naphtalene oil, washing oil are connected with oil gas coupled system E entrance with mink cell focus mixture outlet.
Methanol conversion system C take coal gas as raw material, exports and is connected with MTG system D entrance.
MTG system D is provided with 3 products exports and 1 intermediate outlet, products export is LPG products export, gasoline products outlet, durol products export respectively, 1 intermediate outlet is de-hydrocarbon mink cell focus outlet, and de-hydrocarbon mink cell focus outlet is connected with oil gas coupled system E entrance.
Oil gas coupled system E is provided with 2 products exports, is naphtha product outlet and diesel product outlet respectively.
Technique below in conjunction with accompanying drawing 2 pairs of present system is described in detail.
Embodiment one
Atmospheric and vacuum distillation system A comprises tar storage tank 1, atmospheric distillation tower 2, vacuum still 3.Tar storage tank 1 is connected with the entrance of atmospheric distillation tower 2, the lightweight oil outlet on atmospheric distillation tower 2 top is connected with vacuum still 3 entrance, the mink cell focus outlet of atmospheric distillation tower 2 bottom is connected with mink cell focus tempering tank 4 entrance in oil gas coupled system E, the carbolic oil outlet of vacuum still 3 top is connected with soda-wash tower 5 entrance in de-chemical systems B, in the middle part of vacuum still 3, naphtalene oil outlet is connected with naphthalene rectifying tower 7 entrance in de-chemical systems B, and washing oil outlet in vacuum still 3 bottom is connected with mink cell focus tempering tank 4 entrance in oil gas coupled system E.
De-chemical systems B comprises soda-wash tower 5, decomposition tower 6, naphthalene rectifying tower 7.Soda-wash tower 5 outlet at bottom is connected with decomposition tower 6 entrance, and soda-wash tower 5 top dephenolize oil export is connected with mink cell focus tempering tank 4 entrance in oil gas coupled system E.Bottom naphthalene rectifying tower 7, de-naphtalene oil outlet is connected with mink cell focus tempering tank 4 entrance in oil gas coupled system E.
Methanol conversion system C comprises gas holder 8, low-temperature rectisol reactor 9, pure oxygen catalytic partial oxidation conversion system 10, methanol-fueled CLC device 11.Gas holder 8 is connected with low-temperature rectisol reactor 9 entrance, low-temperature rectisol reactor 9 exports and is connected with pure oxygen catalytic partial oxidation conversion system 10 entrance, pure oxygen catalytic partial oxidation conversion system 10 exports and is connected with methanol-fueled CLC device 11 entrance, methanol-fueled CLC device 11 liquid exit is connected with MTG reactor 12 entrance, and methanol-fueled CLC device 11 pneumatic outlet is connected with pressure swing adsorber 17 entrance in oil gas coupled system E.
MTG system D comprises MTG reactor 12, degassing tower 13, liquefied gas knockout tower 14, rectifying tower 15, aromatic hydrocarbons rectifying tower 16.MTG reactor 12 exports and is connected with degassing tower 13 entrance, degassing tower 13 pneumatic outlet is connected with gas holder 8, degassing tower 13 liquid exit is connected with liquefied gas knockout tower 14 entrance, liquefied gas knockout tower 14 outlet at bottom is connected with rectifying tower 15 entrance, rectifying tower 15 outlet at bottom is connected with aromatic hydrocarbons rectifying tower 16 entrance, and the de-hydrocarbon ils outlet bottom aromatic hydrocarbons rectifying tower 16 is connected with the mink cell focus tempering tank 4 in oil gas coupled system E.
Oil gas coupled system E comprises mink cell focus tempering tank 4, pressure swing adsorber 17, pre-hydrogenator 18, hydrofining reactor 19, gas-liquid separator 20, separation column 21 form.Pressure swing adsorber 17 exports and is connected with pre-hydrogenator 18 gas inlet, hydrogenator 19 gas inlet respectively, mink cell focus tempering tank 4 exports and is connected with pre-hydrogenator 18 liquid inlet, pre-hydrogenator 18 exports and is connected with hydrofining reactor 19 liquid inlet, hydrofining reactor 19 exports and is connected with gas-liquid separator 20 entrance, gas-liquid separator 20 liquid exit is connected with separation column 21 entrance, and gas-liquid separator 20 pneumatic outlet is connected with pressure-swing absorption apparatus 17 entrance.
Adopt the Poly-generation method of this polygenerations systeme process coal tar oil and gas specific as follows:
With the coal tar that coking produces, the coal tar that pyrolysis produces or the tar that gasification produces or above 3 mixture or above 3 in any 2 mixture be raw material, send into atmospheric and vacuum distillation system A,
Tar enters in atmospheric distillation tower 2 through tar storage tank 1, tar is divided into the light oil fraction of boiling point≤270 DEG C and the heavy oil fraction of boiling point > 270 DEG C, light oil fraction enters vacuum still 3 and is cut into carbolic oil (IBP ~ 210 DEG C), naphtalene oil (210 ~ 230 DEG C), washing oil (230 ~ 270 DEG C), and the mink cell focus tempering tank 4 in oil gas coupled system E sent to by heavy oil fraction and washing oil.
The carbolic oil that de-chemical systems B produces with atmospheric and vacuum distillation system A, naphtalene oil are for raw material, carbolic oil enters soda-wash tower 5, the phenols in carbolic oil is extracted with the NaOH solution wash-out of massfraction 5% ~ 10% in soda-wash tower 5, top obtains dephenolize oil, bottom obtains crude phenols sodium solution, crude phenols sodium solution enters decomposition tower 6 top, is the CO of 10% ~ 16% with containing volume fraction
2back flow of gas contacts, and generates crude phenols and soda ash solution.Carbolic oil is put forward phenol technology and is not limited only to NaOH solution elution method herein, also can adopt the precipitator method and solvent extration, can select to put forward phenol technology according to practical situation.Naphtalene oil enters naphthalene rectifying tower 7 and reclaims thick naphthalene, and top obtains thick naphthalene, and bottom obtains de-naphtalene oil, dephenolize oil and de-naphtalene oil enter mink cell focus tempering tank 4 mix with the washing oil that the heavy distillate produced through air distillation, underpressure distillation produce prepare against hydrogenation use.
With pyrolysis produce pyrolysis gas, coking produce coke(oven)gas or gasification produce synthetic gas or above 3 gas mixtures or 3 in any 2 gas mixture for raw material, enter in methanol conversion system C, coal gas enters low-temperature rectisol reactor 9 through gas holder 8, gas removal CO
2, SO
2, after the impurity such as COS, enter pure oxygen catalytic partial oxidation conversion system 10, by the CH in coal gas
4synthetic gas effective constituent CO and H is changed into CmHn
2, synthesis gas through methanol synthesizer 11 is converted into crude carbinol, and unreacted synthesis gas enters pressure-swing absorption apparatus 17 through methanol-fueled CLC device 11 pneumatic outlet and produces hydrogen for hydrogenation of tar hydrogen.
The crude carbinol that MTG system D produces with methanol conversion system C is for raw material, through MTG reactor 12, methanol synthetic oil, comprise the gasoline of about 89%, the LPG of 10%, 1% fuel gas, methanol-fueled CLC oil carries out gas-liquid separation through degassing tower 13, unreacted synthesis gas, C1 ~ C2 hydro carbons enters gas holder 8 through degassing tower top and recycles, liquid enters liquefied gas knockout tower 14, tower top obtains C3 hydrocarbon and C4 hydrocarbon mixture and LPG, be more than C4 hydro carbons and raw gasline at the bottom of tower, raw gasline enters rectifying tower 15, top obtains petroleum naphtha, bottom obtains heavy petrol, heavy petrol enters rectifying tower 16, tower top obtains durol, de-hydrocarbon mink cell focus is obtained at the bottom of tower, de-hydrocarbon mink cell focus enters mink cell focus tempering tank 4 and produces mink cell focus with atmospheric and vacuum distillation system A, the dephenolize oil that de-chemical systems produces, de-naphtalene oil, hydrogenating materials is made after washing oil mixing.
The mink cell focus that oil gas coupled system E produces with atmospheric and vacuum distillation system A, the dephenolize oil that de-chemical systems B produces, de-naphtalene oil, washing oil, the de-hydrocarbon mink cell focus that MTG system D produces is raw material, mink cell focus tempering tank 4 is entered after mixing, oil product in mink cell focus tempering tank 4 enters pre-hydrogenator 18, the hydrogen reaction produced with pressure-swing absorption apparatus 17, carry out pre-treatment, enter hydrofining reactor 19 again and obtain the thick oil product of hydrogenation, the thick oil product of hydrogenation enters gas-liquid separator 20 and carries out gas-liquid separation, unreacting gas enters pressure-swing absorption apparatus 17 and recycles, thick oil product enters in separation column 21 and carries out cut cutting, produce petroleum naphtha and diesel oil.
Embodiment two
In order to improve whole system further, raw coal pretreatment system F can be increased.Concrete technology flow process is shown in Fig. 3
Feedstock pre-processing system F comprises raw coal screening plant 22, gas retort 23, pit kiln 24, efficient cyclone 25, vapourizing furnace 26 form.The coking coal outlet of raw coal screening plant 22 is connected with pit kiln 24, and non-coking coal outlet is connected with gas retort 23, and powder coal export is connected with vapourizing furnace 26.The pneumatic outlet of gas retort 23, the pneumatic outlet of vapourizing furnace 26 are connected with efficient cyclone 25 entrance, the pneumatic outlet of pit kiln 24 is connected with gas holder 8 entrance in methanol conversion system C, the solid outlet of gas retort 23, the solid outlet of pit kiln 24 are connected with vapourizing furnace 26 entrance, efficient cyclone 25 liquid exit is connected with tar storage tank 1 entrance in atmospheric and vacuum distillation system A, and efficient cyclone 25 pneumatic outlet is connected with gas holder 8 entrance in methanol conversion system C.
Feed coal is divided into powder coal (particle diameter≤20mm) and lump coal (particle diameter >20mm) through raw coal screening plant 22, powder coal is all sent to vapourizing furnace 26 and is used as gasification, in lump coal, coking property and the good coal of agglutinating value(of coal) are sent to pit kiln 24 and are done coking coal, and in lump coal, all the other coals are sent to gas retort 23 and done destructive distillation use.The semicoke solid that gas retort 23 produces and the coke that pit kiln 24 produces are sent to vapourizing furnace 26 and are done gasification, the raw gas that the raw gas that gas retort 23 produces, vapourizing furnace 26 produce enters after efficient cyclone 25 isolates tar and enters gas holder 8, tar enters tar storage tank 1, and the coke(oven)gas that pit kiln 24 produces directly enters gas holder 8.All the other processes are identical with embodiment one.
Claims (7)
1. in Chemical Industry oil gas coupling Poly-generation a method, it is characterized in that comprising the following steps:
(1) the frequent decompression distillation system of coal tar and de-chemical systems process are divided into heavy oil fraction, crude phenols, dephenolize oil, thick naphthalene, de-naphtalene oil and washing oil, crude phenols and thick naphthalene are discharged as product, and heavy oil fraction, washing oil, dephenolize oil and de-naphtalene oil send into oil gas coupled system; The coal gas produced in Chemical Industry obtains LPG, gasoline, durol and de-hydrocarbon mink cell focus through methanol conversion system and the process of MTG system, and LPG, gasoline and durol are discharged as product, and de-hydrocarbon mink cell focus sends into oil gas coupled system;
The concrete grammar of the frequent decompression distillation system of coal tar and de-chemical systems process is: coal tar is divided into light oil fraction and heavy oil fraction through atmospheric distillation tower (2) distillation, light oil fraction enters vacuum still (3) again and is cut into carbolic oil, naphtalene oil and washing oil, carbolic oil obtains crude phenols and dephenolize oil through proposing phenol process, and naphtalene oil obtains thick naphthalene and de-naphtalene oil through proposing naphthalene process;
(2) carry out coupling hydro process after entering the heavy oil fraction of oil gas coupled system, washing oil, dephenolize oil, de-naphtalene oil and the mixing of de-hydrocarbon mink cell focus and obtain petroleum naphtha and diesel oil.
2. in Chemical Industry according to claim 1 oil gas coupling Poly-generation method, it is characterized in that: coal gas through the concrete grammar of methanol conversion system and the process of MTG system is: coal gas obtains crude carbinol through the process of methanol conversion system, crude carbinol is sent into the process of MTG system and is obtained LPG, gasoline, durol and de-hydrocarbon mink cell focus.
3. in Chemical Industry according to claim 2 oil gas coupling Poly-generation method, it is characterized in that: the concrete grammar that coal gas produces crude carbinol through the process of methanol conversion system is: coal gas enters in low-temperature rectisol reactor (9) and removes CO
2, SO
2and COS, then enter pure oxygen catalytic partial oxidation conversion system (10), by the CH in coal gas
4and C
mh
nchange into CO and H
2, be converted into crude carbinol finally by methanol-fueled CLC device (11).
4. in Chemical Industry according to claim 2 oil gas coupling Poly-generation method, it is characterized in that: the concrete grammar that crude carbinol sends into the process of MTG system is: crude carbinol is through MTG reactor (12) methanol synthetic oil, methanol-fueled CLC oil carries out gas-liquid separation through degassing tower (13), isolated liquid enters liquefied gas knockout tower (14) and obtains C3 hydrocarbon and C4 hydrocarbon mixture and LPG, with more than C4 hydro carbons and raw gasline, raw gasline is sent into rectifying tower (15) process and is obtained petroleum naphtha and heavy petrol, heavy petrol enters rectifying tower (16) and obtains durol and arrive de-hydrocarbon mink cell focus.
5. the method for oil gas coupling Poly-generation in the Chemical Industry according to any one of claim 1-4, it is characterized in that: in described step (2), the concrete grammar of coupling hydro process is: heavy oil fraction, washing oil, dephenolize oil, de-naphtalene oil and de-hydrocarbon mink cell focus mix afterwards and hydrogen reaction carries out pre-treatment, feed again and obtain the thick oil product of hydrogenation into hydrofining reactor (19) process, the thick oil product of hydrogenation enters gas-liquid separator (20) and carries out gas-liquid separation, isolate hydrogen and thick oil product, thick oil product enters in separation column (21) and carries out cut cutting, obtain petroleum naphtha and diesel oil.
6. in the Chemical Industry according to any one of claim 1-4 oil gas coupling Poly-generation method, it is characterized in that: described coal tar be coking produce coal tar, pyrolysis produce coal tar, gasification produce tar in one or more mixture.
7. in the Chemical Industry according to any one of claim 1-4 oil gas coupling Poly-generation method, it is characterized in that: described coal gas be pyrolysis produce pyrolysis gas, coking produce coke(oven)gas, gasification produce synthetic gas in one or more mixture.
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| CN105062591B (en) * | 2015-07-31 | 2017-07-11 | 赛鼎工程有限公司 | A kind of technique of coke oven through methanol synthesized gasoline, coproduction natural gas and hydrogen |
| CN105062590B (en) * | 2015-07-31 | 2017-07-11 | 赛鼎工程有限公司 | A kind of comprehensive utilization process of coke-stove gas through methanol synthesized gasoline, co-production of liquefied natural gas and tar deep processing |
| CN105779028B (en) * | 2016-04-07 | 2019-04-19 | 青岛科大隆腾科技发展有限公司 | Raw coke oven gas heat and change based on washing rectifying produce the method recycled simultaneously |
| CN107460005B (en) * | 2017-07-26 | 2019-05-21 | 天津大学 | The method and device of aromatic hydrocarbon and alkene is prepared using bio oil catalytic hydrogenation coupling and catalyzing cracking |
| CN109954515B (en) * | 2019-04-11 | 2022-08-19 | 陕西煤业化工技术研究院有限责任公司 | Catalyst for synthesizing benzene by oxygen-free aromatization of raw coke oven gas and preparation method and application thereof |
| CN110551524B (en) * | 2019-07-25 | 2022-03-04 | 新奥科技发展有限公司 | Oil product refining method |
| CN114763497B (en) * | 2021-01-11 | 2023-01-10 | 中国石油化工股份有限公司 | Biomass hydropyrolysis-gasification co-production process and system |
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