CN101532785A - Rapid fuel gas condensation system with double-tower direct spray - Google Patents
Rapid fuel gas condensation system with double-tower direct spray Download PDFInfo
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- CN101532785A CN101532785A CN200810026760A CN200810026760A CN101532785A CN 101532785 A CN101532785 A CN 101532785A CN 200810026760 A CN200810026760 A CN 200810026760A CN 200810026760 A CN200810026760 A CN 200810026760A CN 101532785 A CN101532785 A CN 101532785A
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Abstract
The invention discloses a rapid fuel gas condensation system with double-tower direct spray, comprising a first stage spray tower, a second stage spray tower, a connecting pipeline communicated with the first stage spray tower and the second stage spray tower, at least one bio-oil storage tank connected with condensed bio-oil outlets of the first stage spray tower and the second stage spray tower, and at least one atomized spray sub-system. The atomized spray sub-system comprises a first atomized spray unit and a second atomized spray unit respectively arranged inside the first stage spray tower and the second stage spray tower partially and extensively. The first atomized spray unit and the second atomized spray unit respectively comprise two layers or more than two layers of spraying nozzles that are used for the atomized spray of condensed media and arranged at intervals in the height direction of the inner space of the first stage spray tower and the second stage spray tower. The system can fully inhibit the further schizolysis of condensable components and avoid the complicated process of subsequent separation caused by additional condensed media.
Description
Technical field
The present invention relates to a kind of bio oil condensing unit, relate in particular to a kind of direct spray rapid condensation device.
Background technology
Along with the continuous development of World Economics, the energy and environmental problem become increasingly conspicuous.The human main energy sources of using at present has 3 kinds of oil, natural gas and coals.According to International Energy Agency statistics, on the earth these 3 kinds of energy for time limits of human exploitation have only 40 years respectively, 50 years and 240 years.Tap a new source of energy and become to concern the key subjects of human social.
Biomass energy is the solar energy that is stored in by the photosynthesis of plant and solar energy in the plant.According to estimates, the annual energy of storing of plant is equivalent to 10 times that world's main fuel consumes, and is less than 1% of its total amount as the utilization of the energy.By the biomass energy switch technology, can utilize biomass energy efficiently, produce various clean fuels, substitute fuel such as coal, oil and natural gas.
At present, countries in the world, especially developed country all are being devoted to develop efficient, free of contamination biomass energy utilization technologies, to reach the protection mineral resources, ensure energy security, realize CO
2Reduce discharging, promote sustainable economic and social development.Biomass energy will become the future source of energy important component part, and the expert estimates that global total energy consumption in 2015 will have 40% from biomass energy, and mainly the industrialized development by biomass power generation and biomass liquid fuel realizes.
At present, changing living beings into liquid fuel (bio oil) by the high temperature fast pyrogenation is to realize one of efficient important channel that utilizes of biomass energy.According to the heat transfer type difference, the biomass through pyrolysis liquefaction process generally can be divided into 3 classes: (1) wall indirect heating type reactor.It mainly contacts with living beings by scorching hot reactor surface, thereby being delivered to living beings, heat it is rapidly heated reach fast pyrolysis, as the rotation awl biomass through pyrolysis to-oil reactor of the heat of ablation cracking reactor of Britain Aston university, Vortex reactor that NREL proposes and the design of Dutch Twente university etc.; (2) radiation heat transfer formula reactor, the principal character of this class reactor are to provide biomass through pyrolysis required heat by the surface of a high temperature or thermal source, and it mainly carries out the heat transmission by heat radiation, as the heat radiation reactor of U.S. Washington university; (3) gas-solid mixing direct-heating type reactor, it mainly is by thermal current or Dual-Phrase Distribution of Gas olid living beings to be carried out Fast Heating, it can provide the high rate of heat addition and uniform relatively reaction temperature, the carrier gas of flowing simultaneously fast is convenient to product of thermal cracking and is in time separated out, as the fluid bed heat cracking system of Canadian Waterloo university, circulating fluid bed reactor that Canadian Ensyn proposes and the quick flow type pump with injection reactor of GTFJ etc.The equipment scale of wall indirect heating type reactor is comparatively huge, and simultaneously mechanical contact wear is severe and make operation expense also higher, therefore will be restricted in scale is used, and this type of reactor is general main to provide the mechanism test required.And radiation recuperator heat exchange effect is relatively poor, and energy consumption is difficult to scale greatly.Than preceding two types, abroad developed and the biomass through pyrolysis liquefaction reaction device side of attempting scale overweights the 3rd class.Fluid bed (or recirculating fluidized bed) pyrolysis liquefaction technology makes it become the technology that the thermal cracking that development potentiality is arranged is at present most produced liquid fuel because of realizing the high rate of heat addition, the short gas phase time of staying, simple and direct temperature control, charcoal recovery easily, lower investment and ripe method for designing.
The process and the double tower apparatus system thereof of a kind of biomass pyrolysis liquefaction that is disclosed for CN200510057215.8 number as Chinese patent.Its process comprises biological material sent into allows high-temperature stream gasification and heating medium for high temperature mix with biological material living beings are carried out the step of thermal cracking in the pyrolytic reaction tower, in separator, pyrolysis gas and carbon residue, ash are carried out the step of gas solid separation, and the step of bio oil etc. of in condenser, pyrolysis air cooling being congealed into.Wherein, thermophore is exported the circulatory system with pyrolysis gas, carbon residue etc. in the pyrolytic reaction tower; Carbon residue is used to thermophore is preheated.Its apparatus system also comprises the thermophore separator that thermophore-waste gas-ash content that thermophore and carbon residue are separated the thermophore heating tower of once initial separator, burning carbon residue earlier and be used for coming out in the thermophore heating tower with other materials together separates.But, as can be seen from the above description, the CN200510057215.8 patent has following weak point: first, the medium that is used for pyrolysis gas is carried out condensation in the condenser is a water, therefore, to contain large quantity of moisture in the bio oil that obtains, and want to use and also need adopt Special Equipment further to separate, this will increase technological process difficulty and cost; The second, its condensation process is to adopt one step an of condenser to finish, and on the one hand, may cause the not fully condensation of a part of condensable gas in the pyrolysis gas, on the other hand, may cause the further pyrolysis of part condensable gas, thereby reduce the bio oil productive rate.
Therefore, provide a kind of cracking gas rapid condensation device that can fully reduce system operation cost and can improve the bio oil productive rate to become urgent problem.
Summary of the invention
The object of the present invention is to provide a kind of rapid fuel gas condensation system with double-tower direct spray that system operation cost can fully be reduced and improve the bio oil productive rate.
A kind of double-tower direct spray cracking gas rapid condensation system that provides is provided technical scheme of the present invention, it comprises and is provided with the vent one's spleen first order spray column of import and pyrolysis gas outlet of elevated temperature heat, at least one bio oil storage tank, and at least one atomizing spray subsystem, wherein, this system further comprises the second level spray column that is provided with pyrolysis gas inlet and non-condensable gas outlet, and the connecting pipe of the pyrolysis gas inlet of the pyrolysis gas outlet of connection first order spray column and second level spray column, at least one bio oil storage tank links to each other with the condensation bio oil outlet of first order spray column and second level spray column respectively, at least one atomizing spray subsystem comprises that part is extended the first atomizing spray unit and the second atomizing spray unit that is arranged on first order spray column and spray column inside, the second level respectively, and the first atomizing spray unit and the second atomizing spray unit are included in the two-layer or two-layer above atomizer that is used for the atomizing spray cooling medium that is provided with at interval on the inner space short transverse of first order spray column and second level spray column respectively.
For preventing the further cracking of coagulated component from the high temperature biological fuel gas that cracking reactor comes out, farthest obtain product liquid-bio oil, need be the rapid cool to room temperature of cracked gas.The bio oil RAPID SOLIDIFICATION TECHNIQUE is a most critical link that influences the bio oil productive rate.The present invention adopts the two-stage spray column, can solve because the thoroughly condensation of high-temperature gas that single condensing tower brought, the perhaps inadequate shortcoming of low-boiling point material condensation of gas.
Preferably, the import of venting one's spleen of the elevated temperature heat of first order spray column is arranged on pyrolysis gas outlet top, and the pyrolysis gas inlet of second level spray column is arranged on non-condensable gas outlet below.Like this, first order spray column adopts the forward mode of heat exchange of gas/liquid, be that gas is entered by the spray column top, flow out by the spray column bottom again, can avoid high-temperature gas before entering condensing tower, to cause cracking gas to cause the combustion gas condensation that second pyrolysis reaction chance increases and heat dissipation of pipeline causes to cause problems such as pipeline blockage like this at the overstand of high temperature section owing to pipeline is oversize; Second level spray column has adopted the path with the reverse spray of gas, and promptly gas enters at the bottom of tower, and flow out at the top, the abundant absorption that has effectively improved heat transfer efficiency and liquid phase component.
Preferably, the atomizing spray subsystem comprises that at least one is used as the heat exchanger of the cooling medium source of supply of the first atomizing spray unit and the second atomizing spray unit.Selectively, the cooling medium of the first atomizing spray unit and the second atomizing spray unit can be directly from this system outside.
More preferably, the atomizing spray subsystem comprises further that at least one is connected and is used between bio oil storage tank and the heat exchanger bio oil in the bio oil storage tank is transported to the oil circulating pump of heat exchanger to be cooled to cooling medium and then to be delivered to the first atomizing spray unit and the second atomizing spray unit.Thereby native system can adopt bio oil that institute's condensation gets off as cooling medium, has avoided owing to the loaded down with trivial details technology that adds the further separation that cooling medium brings.
Selectively, cooling medium also can or be suitable for other condensing agent that the condensation elevated temperature heat is vented one's spleen for water.
More preferably, rapid fuel gas condensation system with double-tower direct spray comprises the first atomizing spray subsystem and the second atomizing spray subsystem, the first atomizing spray subsystem comprise the first bio oil storage tank, first oil circulating pump that links to each other with the first bio oil storage tank that links to each other with the outlet of the condensation bio oil of first order spray column and be connected first oil circulating pump and the first atomizing spray unit between first heat exchanger; The second atomizing spray subsystem comprise the second bio oil storage tank, second oil circulating pump that links to each other with the second bio oil storage tank that links to each other with the outlet of the condensation bio oil of second level spray column and be connected second oil circulating pump and the second atomizing spray unit between second heat exchanger.Thereby native system can adopt two-stage spray column serial operation, and the two-stage spray column adopts heat-exchange system separately, can solve because the thoroughly condensation of high-temperature gas that single condensing tower brought, the perhaps inadequate shortcoming of low-boiling point material condensation of gas; The problem of having avoided single condensing tower fault to shut down simultaneously.
Selectively, heat exchanger is the board-like profit indirect heat exchanger that is provided with water inlet and delivery port.Because bio oil corrosivity is stronger, so heat exchanger plate and O-ring seal can adopt the manufacturing of acid corrosion-resistant material.
Particularly, the import of venting one's spleen of the elevated temperature heat of first order spray column is arranged on the below of the superiors' atomizer of the first atomizing spray unit, and the pyrolysis gas outlet of first order spray column is arranged on the below of the orlop atomizer of the first atomizing spray unit.The pyrolysis gas inlet of second level spray column is arranged on the below of the orlop atomizer of the second atomizing spray unit, and the non-condensable gas outlet of second level spray column is arranged on the top of the superiors' atomizer of the second atomizing spray unit.
Preferably, the first atomizing spray unit and the second atomizing spray unit comprise the atomizer more than three layers or three layers respectively, wherein the superiors' atomizer lays respectively at the epimere of the inner space of first order spray column and second level spray column, and wherein the orlop atomizer lays respectively at the hypomere of the inner space of first order spray column and second level spray column.
The invention has the beneficial effects as follows: 1. system of the present invention can be cooled to 500 ℃ high-temperature fuel gas rapidly below 50 ℃, the condensation efficiency height, and cooling velocity is fast, satisfies cracking gas substantially and cools off requirement rapidly, has at utmost suppressed to coagulate the further cracking of component; 2. system of the present invention has adopted bio oil that institute's condensation gets off as cooling medium, has avoided owing to the loaded down with trivial details technology that adds the further separation that cooling medium brings; 3. system of the present invention is provided with three groups of spray equipments in the differing heights position of spray column, by the high-speed rotational atomizer, bio oil is atomized into the atomizing particle that is lower than 0.2mm, thereby has improved the heat transfer area of gas-liquid heat-transfer greatly, accelerates the condensation rate of high-temperature gas; 4. system of the present invention adopts two-stage spray column serial operation, can solve because the thoroughly condensation of high-temperature gas that single condensing tower brought, the perhaps inadequate shortcoming of low-boiling point material condensation of gas; 5. system of the present invention first order spray column adopts the forward mode of heat exchange of gas/liquid, can avoid because high-temperature gas causes combustion gas to cause second pyrolysis reaction chance to increase at the overstand of high temperature section owing to pipeline is oversize before entering condensing tower; Second level spray column has adopted the path with the reverse spray of gas, has effectively improved the abundant absorption of heat transfer efficiency and liquid phase component; 6. the oil of system of the present invention/water heat-exchange system adopts plate type heat exchanger, and this heat exchanger has the heat exchange efficiency height, and the recirculated cooling water amount is few, and volume compact is easy to advantages such as layout.
Below in conjunction with drawings and Examples, further specify the present invention, but the present invention is not limited to these embodiment, any on essence spirit of the present invention improvement or substitute, still belong to scope required for protection in claims of the present invention.
Description of drawings
Fig. 1 is the schematic diagram of rapid fuel gas condensation system with double-tower direct spray embodiment 1 of the present invention.
The specific embodiment
Embodiment 1
Please refer to Fig. 1, double-tower direct spray cracking gas rapid condensation of the present invention system comprises being provided with the vent one's spleen first order spray column 10 of import 101 and pyrolysis gas outlet 102 of elevated temperature heat, be provided with the second level spray column 30 of pyrolysis gas inlet 302 and non-condensable gas outlet 303, the connecting pipe 130 that is communicated with pyrolysis gas outlet 102 with the pyrolysis gas inlet 302 of second level spray column 30 of first order spray column 10, the bio oil storage tank 108 that links to each other with the condensation bio oil outlet of first order spray column 10, the bio oil storage tank 308 that links to each other with the condensation bio oil outlet of second level spray column 30, the first atomizing spray subsystem (comprises the first atomizing spray unit 104 in the present embodiment, first oil circulating pump 106 that links to each other with the first bio oil storage tank 108, and be connected first heat exchanger 105 between first oil circulating pump 106 and the first atomizing spray unit 104), and second the atomizing spray subsystem (comprise the second atomizing spray unit 304 in the present embodiment, second oil circulating pump 306 that links to each other with the second bio oil storage tank 308, and be connected second heat exchanger 305 between second oil circulating pump 306 and the second atomizing spray unit 304).
The first atomizing spray unit 104 and the second atomizing spray unit 304 part extension respectively are arranged on first order spray column 10 and second level spray column 30 inside.The first atomizing spray unit 104 and the second atomizing spray unit 304 are included in three layers of atomizer 1044,3044 that is used for the atomizing spray cooling medium that are provided with at interval on the inner space short transverse of first order spray column 10 and second level spray column 30 respectively.
Wherein, the import 101 of venting one's spleen of the elevated temperature heat of first order spray column 10 is arranged on pyrolysis gas outlet 102 tops, and the pyrolysis gas inlet 302 of second level spray column 30 is arranged on non-condensable gas and exports 303 belows.Particularly, the import 101 of venting one's spleen of the elevated temperature heat of first order spray column 10 is arranged on the below of the superiors' atomizer 1044 of the first atomizing spray unit 104, and the pyrolysis gas outlet 102 of first order spray column 10 is arranged on the below of the orlop atomizer 1044 of the first atomizing spray unit 104.The pyrolysis gas inlet 302 of second level spray column 30 is arranged on the below of the orlop atomizer 3044 of the second atomizing spray unit 304, and the non-condensable gas outlet 303 of second level spray column 30 is arranged on the top of the superiors' atomizer 3044 of the second atomizing spray unit 304.
And, the superiors' atomizer 1044,3044 lays respectively at the epimere of the inner space of first order spray column 10 and second level spray column 30, and orlop atomizer 1044,3044 lays respectively at the hypomere of the inner space of first order spray column 10 and second level spray column 30.
The workflow of system of the present invention is as follows:
Vent one's spleen through entering the first order spray column 10 and the second level spray column 30 of series connection after the dust removal process from the elevated temperature heat of cracking reactor, in spray column, directly carry out the solution-air contact heat-exchanging with the bio oil of the atomizing condensation that sprays from atomizer 1044,3044, pyrolysis temperature degree is cooled to rapidly below 50 ℃ from 450-500 ℃.The coagulated component of carrying in the pyrolysis gas is through 30 coolings of first order spray column 10, second level spray column and absorb and be condensed into bio oil and enter oil storage tank 105,305, and other can not coagulate the combustion gas component, and to enter gas storage holder through air-introduced machine standby.The condensate liquid that native system adopted is the bio oil that the fast pyrogenation process obtains itself, part biological oil enters oil/water indirect heat exchanger 105,305 through oil circulating pump 106,306, recycle as cooling medium through heat exchange cooling back, other biological oil is stored in the bio oil storage tank 108,308.
Embodiment 2
As another kind of scheme of the present invention, other parts are identical with embodiment 1, and difference is:
The cooling medium that is used for the first atomizing spray unit 10 and the second atomizing spray unit 30 can promptly, not adopt the bio oil of system generation itself from this system outside, and this system can not be provided with first heat exchanger 10 and second heat exchanger 30 so.
And the import 101 of venting one's spleen of the elevated temperature heat of first order spray column 10 is arranged on pyrolysis gas outlet 102 belows, that is, first order spray column also adopts the path with the reverse spray of gas.
Embodiment 3
As another kind of scheme of the present invention, other parts are identical with embodiment 1, and difference is:
Adopt a heat exchanger, an oil circulating pump and a bio oil storage tank, the bio oil that first order spray column 10, second level spray column 30 produce all enters same bio oil storage tank, and part biological oil is transported to same heat exchanger cooling and then is delivered to the first atomizing spray unit 104 and the second atomizing spray unit 304 respectively by same oil circulating pump.
Embodiment 4
As another kind of scheme of the present invention, other parts are identical with embodiment 1, and difference is:
The cooling medium that is used for the first atomizing spray unit 10 and the second atomizing spray unit 30 can be water, and this system can not be provided with first heat exchanger 105, second heat exchanger 305, first oil circulating pump 106 and second oil circulating pump 306 so.
Claims (10)
1, a kind of rapid fuel gas condensation system with double-tower direct spray, comprise and be provided with the vent one's spleen first order spray column of import and pyrolysis gas outlet of elevated temperature heat, at least one bio oil storage tank, and at least one atomizing spray subsystem, it is characterized in that, described rapid fuel gas condensation system with double-tower direct spray further comprises the second level spray column that is provided with pyrolysis gas inlet and non-condensable gas outlet, and the connecting pipe that is communicated with the described pyrolysis gas inlet of the described pyrolysis gas outlet of described first order spray column and described second level spray column, described at least one bio oil storage tank links to each other with the condensation bio oil outlet of described first order spray column and described second level spray column respectively, described at least one atomizing spray subsystem comprises that part is extended the first atomizing spray unit and the second atomizing spray unit that is arranged on described first order spray column and spray column inside, the described second level respectively, and described first atomizing spray unit and the described second atomizing spray unit are included in the two-layer or two-layer above atomizer that is used for the atomizing spray cooling medium that is provided with at interval on the inner space short transverse of described first order spray column and described second level spray column respectively.
2, double-tower direct spray cracking gas rapid condensation as claimed in claim 1 system, it is characterized in that, the import of venting one's spleen of the described elevated temperature heat of described first order spray column is arranged on described pyrolysis gas outlet top, and the described pyrolysis gas inlet of described second level spray column is arranged on described non-condensable gas outlet below.
3, double-tower direct spray cracking gas rapid condensation as claimed in claim 2 system, it is characterized in that described atomizing spray subsystem comprises that at least one is used as the heat exchanger of the cooling medium source of supply of described first atomizing spray unit and the described second atomizing spray unit.
4, double-tower direct spray cracking gas rapid condensation as claimed in claim 3 system, it is characterized in that described atomizing spray subsystem comprises further that at least one is connected and is used between described bio oil storage tank and the described heat exchanger bio oil in the described bio oil storage tank is transported to the oil circulating pump of described heat exchanger to be cooled to cooling medium and then to be delivered to described first atomizing spray unit and the described second atomizing spray unit.
5, rapid fuel gas condensation system with double-tower direct spray as claimed in claim 4 is characterized in that, described heat exchanger is the profit indirect heat exchanger that is provided with water inlet and delivery port.
6, as the described double-tower direct spray cracking gas of one of claim 1～5 rapid condensation system, it is characterized in that, the import of venting one's spleen of the described elevated temperature heat of described first order spray column is arranged on the below of the superiors' atomizer of the described first atomizing spray unit, and the described pyrolysis gas outlet of described first order spray column is arranged on the below of the orlop atomizer of the described first atomizing spray unit.
7, double-tower direct spray cracking gas rapid condensation as claimed in claim 6 system, it is characterized in that, the described pyrolysis gas inlet of described second level spray column is arranged on the below of the orlop atomizer of the described second atomizing spray unit, and the described non-condensable gas outlet of described second level spray column is arranged on the top of the superiors' atomizer of the described second atomizing spray unit.
8, double-tower direct spray cracking gas rapid condensation as claimed in claim 7 system, it is characterized in that, described first atomizing spray unit and the described second atomizing spray unit comprise the atomizer more than three layers or three layers respectively, wherein the superiors' atomizer lays respectively at the epimere of the inner space of described first order spray column and described second level spray column, and wherein the orlop atomizer lays respectively at the hypomere of the inner space of described first order spray column and described second level spray column.
9, as the described double-tower direct spray cracking gas of one of claim 1～8 rapid condensation system, it is characterized in that, described rapid fuel gas condensation system with double-tower direct spray comprises the first atomizing spray subsystem and the second atomizing spray subsystem, the described first atomizing spray subsystem comprise the first bio oil storage tank, first oil circulating pump that links to each other with the described first bio oil storage tank that links to each other with the outlet of the condensation bio oil of described first order spray column and be connected described first oil circulating pump and the described first atomizing spray unit between first heat exchanger.
10, double-tower direct spray cracking gas rapid condensation as claimed in claim 9 system, it is characterized in that, the described second atomizing spray subsystem comprise the second bio oil storage tank, second oil circulating pump that links to each other with the described second bio oil storage tank that links to each other with the outlet of the condensation bio oil of described second level spray column and be connected described second oil circulating pump and the described second atomizing spray unit between second heat exchanger.
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Cited By (8)
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| CN101851520A (en) * | 2010-04-29 | 2010-10-06 | 江苏中容电气有限公司 | Sludge pyrolysis gas fractional condensation method for recycling biological oil |
| CN102435079A (en) * | 2011-10-12 | 2012-05-02 | 厦门大学 | Condensation system of biomass pyrolyzed steam |
| CN102732269A (en) * | 2011-03-29 | 2012-10-17 | 何巨堂 | Coke dry quenching method for coal coking device |
| CN103768926A (en) * | 2014-01-18 | 2014-05-07 | 浙江诸暨泓泰环境科技有限公司 | Efficient desulfurization spraying tower |
| CN104236324A (en) * | 2014-09-16 | 2014-12-24 | 昆山黑格特温控设备有限公司 | Low-lying condenser |
| CN104976864A (en) * | 2014-04-09 | 2015-10-14 | 天华化工机械及自动化研究设计院有限公司 | Fine-particle high-viscosity terephthalic acid drying method |
| CN107619670A (en) * | 2017-10-20 | 2018-01-23 | 北京神雾电力科技有限公司 | A kind of pyrolysis oven and method for pyrolysis |
| CN111661995A (en) * | 2020-05-29 | 2020-09-15 | 中国海洋石油集团有限公司 | Oil-based drilling waste recycling and harmless treatment system and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US5306331A (en) * | 1993-03-18 | 1994-04-26 | Permea, Inc. | Process for cooling the feed gas to gas separation systems |
| DE60003689T2 (en) * | 1999-05-05 | 2004-04-15 | Svedala Industries, Inc., Waukesha | CONDENSATION AND RECOVERY OF OIL FROM PYROLYSE GAS |
| CN1190476C (en) * | 2002-09-28 | 2005-02-23 | 中国科学院广州能源研究所 | Cracking purification method for combustible gas produced by gasifying crude material |
| CN100348295C (en) * | 2006-02-17 | 2007-11-14 | 绍兴永利环保科技有限公司 | Exhaust gas treatment device |
| CN201262521Y (en) * | 2008-03-11 | 2009-06-24 | 广州迪森热能技术股份有限公司 | Dual-column direct spraying fast gas condensation system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101851520A (en) * | 2010-04-29 | 2010-10-06 | 江苏中容电气有限公司 | Sludge pyrolysis gas fractional condensation method for recycling biological oil |
| CN101851520B (en) * | 2010-04-29 | 2013-04-10 | 江苏中容电气有限公司 | Sludge pyrolysis gas fractional condensation method for recycling biological oil |
| CN102732269A (en) * | 2011-03-29 | 2012-10-17 | 何巨堂 | Coke dry quenching method for coal coking device |
| CN102435079A (en) * | 2011-10-12 | 2012-05-02 | 厦门大学 | Condensation system of biomass pyrolyzed steam |
| CN103768926A (en) * | 2014-01-18 | 2014-05-07 | 浙江诸暨泓泰环境科技有限公司 | Efficient desulfurization spraying tower |
| CN103768926B (en) * | 2014-01-18 | 2015-05-06 | 浙江诸暨泓泰环境科技有限公司 | Efficient desulfurization spraying tower |
| CN104976864A (en) * | 2014-04-09 | 2015-10-14 | 天华化工机械及自动化研究设计院有限公司 | Fine-particle high-viscosity terephthalic acid drying method |
| CN104976864B (en) * | 2014-04-09 | 2017-10-03 | 天华化工机械及自动化研究设计院有限公司 | A kind of drying means of fine grained, high viscosity terephthalic acid (TPA) |
| CN104236324A (en) * | 2014-09-16 | 2014-12-24 | 昆山黑格特温控设备有限公司 | Low-lying condenser |
| CN107619670A (en) * | 2017-10-20 | 2018-01-23 | 北京神雾电力科技有限公司 | A kind of pyrolysis oven and method for pyrolysis |
| CN111661995A (en) * | 2020-05-29 | 2020-09-15 | 中国海洋石油集团有限公司 | Oil-based drilling waste recycling and harmless treatment system and method |
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