CN102260516A - Method for preparing oil by thermally cracking biomass - Google Patents
Method for preparing oil by thermally cracking biomass Download PDFInfo
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- CN102260516A CN102260516A CN201110177922A CN201110177922A CN102260516A CN 102260516 A CN102260516 A CN 102260516A CN 201110177922 A CN201110177922 A CN 201110177922A CN 201110177922 A CN201110177922 A CN 201110177922A CN 102260516 A CN102260516 A CN 102260516A
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- 238000005336 cracking Methods 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000002028 Biomass Substances 0.000 title claims abstract description 25
- 239000003921 oil Substances 0.000 claims abstract description 67
- 238000000926 separation method Methods 0.000 claims abstract description 54
- 239000007788 liquid Substances 0.000 claims abstract description 42
- 239000002994 raw material Substances 0.000 claims abstract description 40
- 230000008569 process Effects 0.000 claims abstract description 23
- 238000010438 heat treatment Methods 0.000 claims abstract description 9
- 239000003502 gasoline Substances 0.000 claims abstract description 8
- 239000002283 diesel fuel Substances 0.000 claims abstract description 7
- 230000007017 scission Effects 0.000 claims description 44
- 238000003776 cleavage reaction Methods 0.000 claims description 42
- 239000007789 gas Substances 0.000 claims description 41
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 13
- 239000003546 flue gas Substances 0.000 claims description 13
- 238000000197 pyrolysis Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 238000005235 decoking Methods 0.000 claims description 7
- 238000005194 fractionation Methods 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 5
- 241000195493 Cryptophyta Species 0.000 claims description 4
- 241000196324 Embryophyta Species 0.000 claims description 4
- 235000007164 Oryza sativa Nutrition 0.000 claims description 4
- 238000006073 displacement reaction Methods 0.000 claims description 4
- 239000010903 husk Substances 0.000 claims description 4
- 239000013502 plastic waste Substances 0.000 claims description 4
- 235000009566 rice Nutrition 0.000 claims description 4
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 239000010902 straw Substances 0.000 claims description 3
- 238000005382 thermal cycling Methods 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 2
- 238000006297 dehydration reaction Methods 0.000 claims description 2
- 238000002513 implantation Methods 0.000 claims description 2
- 230000008676 import Effects 0.000 claims description 2
- 238000002347 injection Methods 0.000 claims description 2
- 239000007924 injection Substances 0.000 claims description 2
- 239000000779 smoke Substances 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims description 2
- 240000007594 Oryza sativa Species 0.000 claims 1
- 239000010724 circulating oil Substances 0.000 abstract description 7
- 238000004939 coking Methods 0.000 abstract description 7
- 230000003111 delayed effect Effects 0.000 abstract description 5
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 238000005086 pumping Methods 0.000 abstract 2
- 230000005855 radiation Effects 0.000 abstract 1
- 238000005507 spraying Methods 0.000 abstract 1
- 238000004227 thermal cracking Methods 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 4
- 241000209094 Oryza Species 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 241000282326 Felis catus Species 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000010504 bond cleavage reaction Methods 0.000 description 2
- 238000005520 cutting process Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 206010020843 Hyperthermia Diseases 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 230000036031 hyperthermia Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 239000010729 system oil Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a technology for preparing oil by thermally cracking biomass, and particularly provides a method for preparing the oil by thermally cracking biomass and the like which are taken as raw materials. The method relies on a technology similar to delayed coking. The method mainly comprises the following steps of: pumping circulating oil out from the bottom of a fractionating column, pumping into a radiation chamber furnace tube of a heating furnace by a hot oil pump, quickly heating and raising the temperature to 450 to 550 DEG C, feeding into the upper part of a thermal cracking tower, spraying onto raw material stack layers by a distributor, allowing raw material cracking oil gas and the circulating oil to flow to the bottom of the cracking tower from up to down along the raw material stack layers so as to form the temperature gradient from up to down; and allowing the raw material cracking oil gas and the circulating oil to enter a vapor-liquid separation tank, allowing the raw material cracking oil gas obtained after separation to enter the fractionating column, performing mass transfer on the raw material cracking oil and the mixed liquid of cracking liquid and the circulating oil, and fractionating to obtain gas, crude gasoline, diesel oil, wax oil and circulating oil. The method has the main characteristics of energy conservation along with reasonable process, and low cost.
Description
Technical field
The present invention relates to thermally splitting and produce the oil gas technical field, be specifically related to thermo-cracking method of making oil such as a kind of biomass.
Background technology
At present, not outer following several with the method for biomass-making oil: destructive distillation, high-temperature flue gas heating, fluidized-bed, nitrated, fermentation.Above method exists following shortcoming to be: the destructive distillation heating efficiency is low, and thermograde is big, is difficult to heavy industrialization; High-temperature flue gas heating products oxygen level height, a large amount of low heating value gass are good utilisation not; Fluidized-bed is to the selection that processed raw material, and the raw material that molecule is processed in inconvenience uses; Nitrated use strong acid, facility investment is big, long flow path; Fermenting speed is slow, and product separation energy consumption height, difficulty are big.
From in the past relevant report as can be seen, many rural areas are all arranged because reclaim stalk every year and do not have benefit, the big area of setting fire is everywhere burned, and not only causes environmental pollution, and causes disadvantageous effect for highway communication and air transportation.That is to say that up to the present, also not having a kind of is the better method of raw material by thermo-cracking system oil with biomass, plastic waste, waste rubber and garbage organism.
Summary of the invention
Purpose of the present invention is exactly the defective that exists at prior art, provides a kind of flow process reasonable, with low cost, energy-conservation biomass through pyrolysis method of making oil.
Its technical scheme comprises: with one or more of biomass, plastic waste, waste rubber or garbage organism is raw material, through the method for making oil of thermo-cracking and fractionation process process, wherein biomass comprise the one or more combination of straw, rice husk, branch, leaf, weeds or algae.
(1), behind the populated raw material of cleavage column, from the flue gas of 180 ~ 290 ℃ of cleavage column bottom implantation temperatures, to the raw material dehydration, flue gas and take off back steam by the high some blow-off valve emptying of cleavage column top; After cleavage column upper, middle and lower temperature is all above 180 ℃, close hot smoke valve, utilize 180 ~ 300 ℃ of superheated vapours of temperature to displace flue gas and emptying, after the displacement, close superheated vapour and high some blow-off valve.
(2), after external turning oil inserts vapor-liquid separation tank, separation column bottom, process furnace successively by pipe connecting and pump, produce two loops by control valve, one the tunnel gets back to vapor-liquid separation tank, form initial cycles oil and inject and soft circulation circuit, the heating and temperature control of process furnace is at 300 ~ 350 ℃ in this circulation.
(3), after finishing turning oil injection and thermal cycling, closed control valve is to the loop of vapor-liquid separation tank, cleavage column top is inserted in another loop, be sprayed onto on the stockpile layer through sparger, the vapour that sets up separately by cleavage column bottom and bottom again, the liquid outlet imports vapor-liquid separation tank, after temperature that raw material cracking oil gas and turning oil enter vapor-liquid separation tank is higher than 375 ℃, open the fractionation column bottoms pump, use turning oil fast cooling from process interchanger at the bottom of the separation column, the temperature that enters the vapor-liquid separation tank medium is controlled at 350 ~ 370 ℃ (preventing coking), vapour after vapor-liquid separation tank separates, liquid enters the separation column bottom by pipeline separately, the separation column bottom is connected with external turning oil pipeline with interchanger by pump, forms turning oil thermo-cracking circulation loop.
(4), be provided with a plurality of discharge ports according to the separate substance different boiling on the separation column, enter oil gas in the separation column by its boiling point height successively the discharge port by separately enter the product tank field by heat exchange, cooling.
Such scheme also comprises: rise in 450 ~ 550 ℃ in the temperature that turning oil is gone out process furnace, inject dry gas from the cleavage column top and occupy the cleavage column upper space.
Oil after vapor-liquid separation tank separates, vapour insert the position of separation column by upper and lower layout.
The discharge port that is provided with on the separation column comprises turning oil, wax oil, diesel oil, gasoline and gas from bottom to top, and wherein the gasoline and the gas that produce of cracking is sent into downstream absorption-stabilizing deyice after the gas compressor compression, separate dry gas, liquefied gas and stable gasoline.
Described cleavage column has two at least, and vapor-liquid separation tank is corresponding one by one with the cleavage column formation, and described control valve is a four-way valve, and the cleavage column decoking utilizes water vapor stripping, the burnt layer of cooling to carry out after below 70 ℃.
Described biomass comprise straw, rice husk, branch, leaf, weeds, algae etc.
The present invention compared with prior art, its advantage applies is in the following aspects:
1, the high temperature circulation oil of coming from process furnace directly evenly is sprayed onto on the pile of biomass layer, the thermo-efficiency height, and the rate of heat transfer height, co-altitude raw material layer temperature is even, and different heights is the formation temperature gradient from top to bottom, does not have localized hyperthermia's phenomenon.
2, two above cleavage column blocked operations just as delayed coking unit, can be handled raw material on a large scale, realize the industrialization continuous operation.
3, utilize high temperature circulation oil to provide heat to biomass through pyrolysis, do not have air to exist in the cleavage column, also do not need indifferent gas heating fluidisation, the product oxygen level is lower naturally, and dry gas also is a high heat value gas.
4, high temperature circulation oil directly evenly is sprayed onto on the pile of biomass layer, is easy to control thermo-cracking speed and reaction depth, has also just realized the control of split product yield and quality.
5, can use this technological transformation to have delayed coking unit, less investment, instant effect.
6, cracking stock wide material sources, not only can handle biomass, as stalk, rice husk, branch, leaf, weeds, algae etc., all right treatment of waste plastics, waste rubber and garbage organism, both can the same class raw material of individual curing, also can handle different types of raw material simultaneously.
7, cracking stock does not need to be ground into small-particle, only needs simple cutting, and the raw materials pretreatment expense is lower.
8, high temperature circulation oil directly evenly is sprayed onto on the pile of biomass layer, and biomass can arrive the thermo-cracking temperature fast, and the sophisticated fractionating technology of product utilization is cut, and energy consumption is low, easily handles.
Description of drawings
Fig. 1 is a schematic flow sheet of the present invention.
Among Fig. 1, marking explanation is as follows: 1 is process furnace, 2,3 (can be provided with N cleavage column according to process scale for cleavage column, only be illustrated in the accompanying drawing 1 with 2 cleavage columns), 4,5 is vapor-liquid separation tank, and 6 is separation column, 7 is the overhead product vapor-liquid separation tank, and 8 is the diesel oil stripping tower, and 9 are cracking liquid and turning oil mixing liquid pump, 10 is the raw gasline pump, and 11 is the cat head recycle pump, and 12 is the stage casing recycle pump, 13 is diesel oil pump, and 14 is the wax oil pump, and 15 is circulating oil pump, 16 are the fractionation column bottoms pump, and 17 ~ 21 is water cooler, and 22 ~ 26 is interchanger, 27 is four-way valve, and 28 is product gas, and 29 is raw gasline, 30 is diesel oil, 31 is wax oil, and 32 is turning oil, and 33 is coke, 34,35 is raw material, 36 is dry gas, and 37 is the emptying of high point, and 38 is hot flue gas, 39 is superheated vapour, and 40 is stripping oil gas and safety valve emptying oil gas before the decoking.
Embodiment
Below in conjunction with accompanying drawing 1, be described further with 20,000 tons of/year biomass through pyrolysis method of making oil.
As can be seen from Figure 1, at first, turning oil 32 enters vapor-liquid separation tank 4 or 5 by water cooler 21 and 25,26 pairs of lines of interchanger outside installing, after setting up liquid level, start cracking liquid and turning oil mixing liquid pump 9, after liquid level is set up in separation column 6 bottoms, start circulating oil pump 15, turning oil is squeezed into process furnace 1 radiator tube be warming up to 300 ~ 350 ℃, enter vapor-liquid separation tank 4 or 5, set up the turning oil thermal cycling by four-way valve 27.(preparation step 1 before going into operation)
Simultaneously, raw material 34 through simple cutting, the 35(raw material comprises biomass, plastic waste, waste rubber and garbage organism) enter cleavage column 2 or 3 by the feeder (not shown), after being added to proper height, open hot flue gas 38(130 ~ 250 ℃) enter the cleavage column bottom, in the process that rises, dewater to raw material, flue gas and take off back steam by the emptying 37 of high point, when cleavage column upper, middle and lower homo(io)thermism after 180 ~ 200 ℃, close hot flue gas 38, unlatching superheated vapour 39(180 ~ 300 ℃) displacement flue gas and emptying after the displacement, is closed superheated vapour 39 and the emptying 37 of high point.(preparation step 2 before going into operation)
Then, turning oil is changed into cleavage column 2 or 3 tops by four-way valve 27, be sprayed onto on the stockpile layer through sparger, at this moment, the temperature that turning oil is gone out process furnace 1 rises to 450 ~ 550 ℃ (the raw material scission reaction needs high temperature), (heat scission reaction is thermo-negative reaction to need supply response heat simultaneously, these heats need bring raw material from the turning oil of process furnace fully), raw material cracking oil gas and turning oil flow to the cleavage column bottom along raw material layer from top to bottom, lower floor's raw material has obtained the heat that upper strata raw material cracking oil gas and turning oil carry, form thermograde (550 ~ 320 ℃) from top to bottom, the outlet that is positioned at centrum bottom is mainly used in cracking liquid and the turning oil mixed solution goes out tower, another or a plurality of outlet that is positioned on centrum limit wall or the vertical tower wall are mainly used in raw material cracking oil gas and go out tower, and cracking liquid converges to after turning oil goes out cleavage column and enters vapor-liquid separation tank 4 or 5.
After temperature that raw material cracking oil gas and turning oil enter vapor-liquid separation tank 4 or 5 is higher than 375 ℃, open fractionation column bottoms pump 16, use turning oil fast cooling from process interchanger 26 at the bottom of the separation column, the temperature that enters vapor-liquid separation tank 4 or 5 media is controlled at 350 ~ 370 ℃ (preventing coking), raw material cracking oil gas after the separation enters separation column 6, cracking liquid and turning oil mixed solution are squeezed into separation column 6 through pump 9, and it is gone into the tower height degree and goes on the tower mouth at raw material cracking oil gas.
Rise in 450 ~ 550 ℃ in the temperature that turning oil is gone out process furnace 1, open dry gas 36 in right amount and inject, occupy the cleavage column upper space, can reduce raw material cracking oil gas, to reduce the secondary cracking ratio in the cleavage column residence time with dry gas from the cleavage column top.
In separation column, according to the boiling point difference, tell turning oil 32, wax oil 31, diesel oil 30 successively, cat head distillates raw gasline 29 and gas 28, the gas 28 that cracking produces is delivered to downstream absorption-steady component (not shown) together with raw gasline 29 after gas compressor compression (not shown), separate dry gas, liquefied gas and stable gasoline, this patent separation column and downstream absorption-steady component and delayed coking unit in like manner just repeat no more.
When cleavage column thermograde from top to bottom progressively is changed to 550 ~ 530 ℃ from 550 ~ 320 ℃, and the amount that raw material cracking oil gas enters separation column 6 sharply reduces, at this moment, can determine that the raw material thermo-cracking finishes in this cleavage column, simultaneously turning oil be changed into another cleavage column top by four-way valve 27.
Cleavage column originally then utilizes water vapor stripping, the burnt layer of cooling (with steam and water) to begin decoking after below 70 ℃, and stripping oil gas and safety valve emptying oil gas 40 enter downstream cooling system (not shown) before the decoking.The program of cleavage column decoking and delayed coking unit coke drum in like manner just repeat no more here.
In the cleavage column decoking, remove vapor-liquid separation tank 4 or 5 deposit coke.
Claims (5)
1. biomass through pyrolysis method of making oil, with one or more of biomass, plastic waste, waste rubber or garbage organism is raw material, method of making oil through thermo-cracking and fractionation process process, wherein biomass comprise the one or more combination of straw, rice husk, branch, leaf, weeds or algae, it is characterized in that:
(1), behind the populated raw material of cleavage column, from the flue gas of 180 ~ 290 ℃ of cleavage column bottom implantation temperatures, to the raw material dehydration, flue gas and take off back steam by the high some blow-off valve emptying of cleavage column top; After cleavage column upper, middle and lower temperature is all above 180 ℃, close hot smoke valve, utilize 180 ~ 300 ℃ of superheated vapours of temperature to displace flue gas and emptying, after the displacement, close superheated vapour and high some blow-off valve;
(2), after external turning oil inserts vapor-liquid separation tank, separation column bottom, process furnace successively by pipe connecting and pump, produce two loops by control valve, one the tunnel gets back to vapor-liquid separation tank, form initial cycles oil and inject and soft circulation circuit, the heating and temperature control of process furnace is at 300 ~ 350 ℃ in this circulation;
(3), after finishing turning oil injection and thermal cycling, closed control valve is to the loop of vapor-liquid separation tank, cleavage column top is inserted in another loop, be sprayed onto on the stockpile layer through sparger, the vapour that sets up separately by cleavage column bottom and bottom again, the liquid outlet imports vapor-liquid separation tank, after temperature that raw material cracking oil gas and turning oil enter vapor-liquid separation tank is higher than 375 ℃, open the fractionation column bottoms pump, use turning oil fast cooling from process interchanger at the bottom of the separation column, the temperature that enters the vapor-liquid separation tank medium is controlled at 350 ~ 370 ℃, vapour after vapor-liquid separation tank separates, liquid enters the separation column bottom by pipeline separately, the separation column bottom is connected with external turning oil pipeline with interchanger by pump, forms turning oil thermo-cracking circulation loop;
(4), be provided with a plurality of discharge ports according to the separate substance different boiling on the separation column, enter oil gas in the separation column by its boiling point height successively the discharge port by separately enter the product tank field by heat exchange, cooling.
2. biomass through pyrolysis method of making oil according to claim 1 is characterized in that: rise in 450 ~ 550 ℃ in the temperature that turning oil is gone out process furnace, inject dry gas from the cleavage column top and occupy the cleavage column upper space.
3. biomass through pyrolysis method of making oil according to claim 1 and 2 is characterized in that: the oil after vapor-liquid separation tank separates, vapour insert the position of separation column by upper and lower layout.
4. biomass through pyrolysis method of making oil according to claim 3, it is characterized in that: the discharge port that is provided with on the separation column comprises turning oil, wax oil, diesel oil, gasoline and gas from bottom to top, wherein the gasoline and the gas that produce of cracking is sent into downstream absorption-stabilizing deyice after the gas compressor compression, separate dry gas, liquefied gas and stable gasoline.
5. biomass through pyrolysis method of making oil according to claim 4, it is characterized in that: described cleavage column has two at least, vapor-liquid separation tank constitutes corresponding one by one with cleavage column, described control valve is a four-way valve, and the cleavage column decoking utilizes water vapor stripping, the burnt layer of cooling to carry out after below 70 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110177922 CN102260516B (en) | 2011-06-29 | 2011-06-29 | Method for preparing oil by thermally cracking biomass |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110177922 CN102260516B (en) | 2011-06-29 | 2011-06-29 | Method for preparing oil by thermally cracking biomass |
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| Publication Number | Publication Date |
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| CN102260516A true CN102260516A (en) | 2011-11-30 |
| CN102260516B CN102260516B (en) | 2013-06-19 |
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| CN 201110177922 Expired - Fee Related CN102260516B (en) | 2011-06-29 | 2011-06-29 | Method for preparing oil by thermally cracking biomass |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103571527A (en) * | 2013-11-15 | 2014-02-12 | 合肥工业大学 | Preparation method of high-calorific-value nonpolar bio-oil/gasoline homogeneous fuel oil |
| TWI490052B (en) * | 2012-02-07 | 2015-07-01 | ||
| CN105716052A (en) * | 2014-12-02 | 2016-06-29 | 上海优华系统集成技术有限公司 | High-temperature flue gas heat joint optimization system |
| CN108611104A (en) * | 2018-06-19 | 2018-10-02 | 天津大学 | A kind of method and apparatus that the separation of oil-sand pyrolysis oil gas is integrated with energy regenerating |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1891789A (en) * | 2005-07-06 | 2007-01-10 | 华东理工大学 | Delayed coking treatment method for waste biomass |
-
2011
- 2011-06-29 CN CN 201110177922 patent/CN102260516B/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1891789A (en) * | 2005-07-06 | 2007-01-10 | 华东理工大学 | Delayed coking treatment method for waste biomass |
Non-Patent Citations (1)
| Title |
|---|
| 张振华，汪华林，陈于勤，胥培军: "利用延迟焦化方法处理生物质的技术可行性分析", 《可再生能源》 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI490052B (en) * | 2012-02-07 | 2015-07-01 | ||
| CN103571527A (en) * | 2013-11-15 | 2014-02-12 | 合肥工业大学 | Preparation method of high-calorific-value nonpolar bio-oil/gasoline homogeneous fuel oil |
| CN103571527B (en) * | 2013-11-15 | 2015-07-01 | 合肥工业大学 | Preparation method of high-calorific-value nonpolar bio-oil/gasoline homogeneous fuel oil |
| CN105716052A (en) * | 2014-12-02 | 2016-06-29 | 上海优华系统集成技术有限公司 | High-temperature flue gas heat joint optimization system |
| CN105716052B (en) * | 2014-12-02 | 2018-04-06 | 上海优华系统集成技术有限公司 | A kind of high-temperature flue gas heat integration optimizes system |
| CN108611104A (en) * | 2018-06-19 | 2018-10-02 | 天津大学 | A kind of method and apparatus that the separation of oil-sand pyrolysis oil gas is integrated with energy regenerating |
| CN108611104B (en) * | 2018-06-19 | 2024-05-24 | 天津大学 | Integrated method and equipment for separating and recovering energy of oil sand pyrolysis oil gas |
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| CN102260516B (en) | 2013-06-19 |
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Granted publication date: 20130619 |