CN203794819U - PET (Polyethylene Glycol Terephthalate) production system capable of recycling acetaldehyde and reducing ethanediol content at process tower top - Google Patents

PET (Polyethylene Glycol Terephthalate) production system capable of recycling acetaldehyde and reducing ethanediol content at process tower top Download PDF

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Publication number
CN203794819U
CN203794819U CN201420056102.0U CN201420056102U CN203794819U CN 203794819 U CN203794819 U CN 203794819U CN 201420056102 U CN201420056102 U CN 201420056102U CN 203794819 U CN203794819 U CN 203794819U
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tower
acetaldehyde
esterification
stripping
reflux
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周华堂
曾文兵
许贤文
李利军
顾爱军
俱虎良
陈久波
张宇航
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China National Petroleum Corp
China Kunlun Contracting and Engineering Corp
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China Textile Industry Design Institute
China Kunlun Contracting and Engineering Corp
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Abstract

The utility model relates to a PET (Polyethylene Glycol Terephthalate) production system capable of recycling acetaldehyde and reducing the ethanediol content at a process tower top, and the system comprises a process tower as well as a stripping tower and an acetaldehyde rectifying tower which are arranged in parallel, wherein an esterifying water outlet at the top end of the process tower is connected with the esterifying water inlet of the stripping tower and the esterifying water inlet of the acetaldehyde rectifying tower through an esterifying pipeline respectively; a stripping wastewater outlet of the stripping tower and a rectifying wastewater outlet of the acetaldehyde rectifying tower are connected with the backflow inlet of the process tower by virtue of corresponding backflow pipelines. When the system provided by the utility model is in normal production, the acetaldehyde rectifying tower is put into operation firstly, and the high energy consumption and low-benefit operation of the stripping tower can be avoided; during the overhauling and maintenance of the acetaldehyde rectifying tower, the stripping tower is used, uninterrupted pretreatment of the esterifying water of the PET device can be guaranteed, and adverse impact on further biochemical treatment of the process wastewater by acetaldehyde is avoided; the system has the characteristics of low energy consumption, low operation cost, high economic benefits, less environmental influence and the like.

Description

Can reclaim the PET production system of acetaldehyde and reduction technique tower top ethylene glycol content
Technical field
The utility model relates to a kind of PET device, relates in particular to a kind of PET device that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content that has.
Background technology
PET device is followed a small amount of side reaction in reaction process, and by product is mainly acetaldehyde, comprises the acetaldehyde that glycol dehydration generates, the acetaldehyde that polymer degradation generates.Acetaldehyde mainly results from the esterification section of PET device, results from a small quantity polycondensation section, and acetaldehyde is discharged the main device of PET by technique tower top esterification water and process tail gas.
The esterification water growing amount of ton PET product is 0.19 ton, composed as follows: the about 97.8wt% of water, and ethylene glycol 0.3-0.8wt%, acetaldehyde 0.8-1.5wt%, 2-methyl isophthalic acid, 3-dioxolanes 0.3-0.5wt%, other are 0.1%, total COD value 20000-40000mg/l.
The growing amount of ton PET Product Process waste gas is 3-7kg, and composed as follows: acetaldehyde is 30wt%, water is 36wt%, and air is 33wt%, and other are 1wt%.
Because acetaldehyde has and suppresses and toxic action for the bacterium of processing wastewater biochemical treatment, before entering biochemical treatment, therefore the COD contribution margin (concentration) of acetaldehyde in processing wastewater must be down to below 300mg/l,, at least need the esterification water that PET device is discharged to carry out pre-treatment, remove acetaldehyde.
Pre-treatment for PET device by product acetaldehyde at present mainly contains two kinds of methods:
1, process tail gas adopts drip washing mode, and washing water and esterification steam carry acetaldehyde, and stripping tail gas is delivered to PET device matched with hot coal stove and burned, and reclaims the organic calorific values such as acetaldehyde.
2, esterification hydromining removes acetaldehyde with stripping, and the process tail gas of stripping tail gas and PET device merges sends into the burning of PET device matched with hot coal stove, reclaims the organic calorific values such as acetaldehyde.
In above-mentioned two kinds of methods, the acetaldehyde in esterification water and process tail gas after treatment, is all delivered to hot Media Oven and is burned, and can reduce on the one hand the COD of processing wastewater, reduces burden and the environmental pollution of sewage disposal.Reclaim on the other hand the calorific value of the burning generation of acetaldehyde.These two kinds of method energy consumptions are higher, and the calorific value of the method for burning recycling acetaldehyde is uneconomical, because stripping tail gas contains more than 80% water vapor, therefore the recovery calorific value signature of ton acetaldehyde oil is approximately 0.62 ton, press approximately 4000 yuan/ton of oil fuel, ton acetaldehyde burns the benefit reclaiming and only has an appointment 2480 yuan, far below approximately 7000 yuan/ton of industrial acetaldehyde selling prices.
Utility model content
The problem existing in order to solve prior art, the utility model provides a kind of PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content, has less energy-consumption, running cost is low, economic benefit is high and to features such as environmental influence are little.
The technical solution adopted in the utility model:
A kind of PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content, comprise process tower and the gas stripping column being arranged in parallel and Ethanal distillation column, the esterification water out on the top of described process tower is connected by esterification pipeline with the esterification water inlet of described gas stripping column and the esterification water inlet of described Ethanal distillation column respectively, and the air lift wastewater outlet of described gas stripping column and the outlet of the wastewater of rectification of described Ethanal distillation column are all connected with the reflux inlet of described process tower by each self-corresponding reflux line.
Preferably, described Ethanal distillation column is divided into packing section and tower plate structure section from top to bottom, is filled with efficient wire packing in described packing section, in described tower plate structure section, is provided with tower plate structure.
Conventionally, in the tower reactor of described Ethanal distillation column, heating unit can be installed.
Conventionally, the outlet of the acetaldehyde of the tower top of described Ethanal distillation column can be connected with acetaldehyde lime set receiving tank by acetaldehyde pipeline, on described acetaldehyde pipeline, acetaldehyde condenser is installed.
Conventionally, the outlet of the tail gas at the top of described gas stripping column can be connected with pipestill for heat carrier incinerator by air lift exhaust pipe; The steam-in of the tower reactor of described gas stripping column connects steam boiler by steam-pipe.
Preferably, on the esterification main pipeline of the esterification pipeline between the esterification pipeline between the esterification water out on the top of described process tower and the esterification water inlet of described gas stripping column and the esterification water out on top of described process tower and the esterification water inlet of described Ethanal distillation column, overhead condenser, esterification water collecting groove and esterification water fresh feed pump are installed, wherein said overhead condenser is relatively short with the distance of the described process tower of described esterification water collecting groove distance, and described esterification water collecting groove is between described esterification water fresh feed pump and described overhead condenser.
Further, the utility model also comprises process tower tail gas elution device, and described esterification water collecting groove can also be connected with described process tower tail gas elution device.
Preferably, the air lift wastewater outlet of described gas stripping column and the reflux line between the reflux inlet of described process tower is divided into main return line and stripping reflux is in charge of, the wastewater of rectification outlet of described Ethanal distillation column and reflux line between the reflux inlet of described process tower are divided into main reflux line and rectifying and reflux and be in charge of, from described process tower to described main reflux line, described stripping reflux, be in charge of and junction that described rectifying backflow is in charge of main reflux line recirculation water transferpump and backflow lime set receiving tank are installed successively.
Conventionally, described stripping reflux is in charge of can be provided with air lift waste water transferpump, stripping reflux between described air lift waste water transferpump and described process tower is in charge of can be provided with stripping reflux arm, and the other end of described stripping reflux arm can connect air lift sewage works.
Conventionally, described rectifying refluxes to be in charge of wastewater of rectification transferpump can be installed, rectifying between described wastewater of rectification transferpump and described process tower refluxes to be in charge of and can be provided with rectifying backflow arm, and the other end of described rectifying backflow arm can connect rectifying sewage works.
The beneficial effects of the utility model:
The utility model adopts the form of Ethanal distillation column and stripping tower parallel connection, has both guaranteed, to the continual pre-treatment of PET device esterification water, to have avoided again higher energy consumption and running cost.When normal production, Ethanal distillation column preferentially puts into operation, can avoid high energy consumption, the poor benefit operation of stripping tower, when Ethanal distillation column maintenance, maintenance period, use gas stripping column, assurance is carried out pre-treatment to the esterification water of PET device is continual, and further biochemical treatment has a negative impact to processing wastewater to avoid acetaldehyde.
The special construction of Ethanal distillation column is the advantage of packing tower and tray column comprehensively.Its upper semisection adopts efficient wire packing design, improves gas-to-liquid contact area, improves separation efficiency, because upper semisection acetaldehyde concentration is higher, by reducing the liquid phase residence time, can reduce acetaldehyde autohemagglutination and occur; Lower semisection adopts tower plate structure design, and the overflow weir of column plate adopts increases processing, extends the stripping section liquid phase residence time.Provide 2-methyl isophthalic acid, the condition that 3-dioxolanes hydrolysis reaction forward carries out.
The utility model adopts the process water that removes acetaldehyde of Ethanal distillation column or gas stripping column tower reactor as the backflow of PET device process tower.Due to acetaldehyde in recirculation water and 2-methyl isophthalic acid, the concentration of 3-dioxolanes is very low, can impel 2-methyl isophthalic acid in process tower liquid phase, the hydrolysis of 3-dioxolanes is carried out to positive dirction, significantly reduces technique tower top acetaldehyde and 2-methyl isophthalic acid, the concentration of 3-dioxolanes, alleviate the reactive force between polar molecule, thereby the concentration that reduces technique tower top ethylene glycol, can make the concentration of technique tower top ethylene glycol be reduced to below 0.1wt% from 0.3-0.8wt%, reduce the ethylene glycol unit consumption of PET device.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of a kind of embodiment of the present utility model.
Embodiment
Referring to Fig. 1, the utility model relates to a kind of PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content, the gas stripping column 2 that comprises process tower 1 and be arranged in parallel and Ethanal distillation column 3, the esterification water out on the top of described process tower is connected by esterification pipeline with the esterification water inlet of described gas stripping column and the esterification water inlet of described Ethanal distillation column respectively, and the air lift wastewater outlet of described gas stripping column and the outlet of the wastewater of rectification of described Ethanal distillation column are all connected with the reflux inlet of described process tower by each self-corresponding reflux line.The utility model adopts the form of Ethanal distillation column and stripping tower parallel connection, has both guaranteed, to the continual pre-treatment of PET device esterification water, to have avoided again higher energy consumption and running cost; The process water that removes acetaldehyde of Ethanal distillation column or gas stripping column tower reactor is as the backflow of PET device process tower.Due to acetaldehyde in recirculation water and 2-methyl isophthalic acid, the concentration of 3-dioxolanes is very low, can impel 2-methyl isophthalic acid in process tower liquid phase, the hydrolysis of 3-dioxolanes is carried out to positive dirction, significantly reduces technique tower top acetaldehyde and 2-methyl isophthalic acid, the concentration of 3-dioxolanes, alleviate the reactive force between polar molecule, thereby the concentration that reduces technique tower top ethylene glycol, can make the concentration of technique tower top ethylene glycol be reduced to below 0.1wt% from 0.3-0.8wt%, reduce the ethylene glycol unit consumption of PET device.
Preferably, described Ethanal distillation column is divided into packing section and tower plate structure section from top to bottom, is filled with efficient wire packing in described packing section, in described tower plate structure section, is provided with tower plate structure.The comprehensive advantage of packing tower and tray column.Its upper semisection adopts efficient wire packing design, improves gas-to-liquid contact area, improves separation efficiency, because upper semisection acetaldehyde concentration is higher, by reducing the liquid phase residence time, can reduce acetaldehyde autohemagglutination and occur; Lower semisection adopts tower plate structure design, and the overflow weir of column plate adopts increases processing, extends the stripping section liquid phase residence time.Provide 2-methyl isophthalic acid, the condition that 3-dioxolanes hydrolysis reaction forward carries out.
Conventionally, in the tower reactor of described Ethanal distillation column, heating unit 33 can be installed.The thermal source of described heating unit can be selected steam or heat conduction wet goods, and its type of heating is partition heating.
Conventionally, the outlet of the acetaldehyde of the tower top of described Ethanal distillation column can be connected with acetaldehyde lime set receiving tank 8 by acetaldehyde pipeline, on described acetaldehyde pipeline, acetaldehyde condenser 32 is installed.On acetaldehyde pipeline between described acetaldehyde condenser and described acetaldehyde lime set receiving tank, can be provided with acetaldehyde arm, its other end is connected with Ethanal distillation column.Ethanal distillation column top gaseous phase becomes phlegma after acetaldehyde condenser, and a phlegma part is as the backflow of rectifying tower, and a part is qualified rear as technique acetaldehyde product stock by analysis.
Conventionally, the outlet of the tail gas at the top of described gas stripping column can be connected 4 with pipestill for heat carrier incinerator by air lift exhaust pipe; The organic combustion heat values such as efficient recovery acetaldehyde.The steam-in of the tower reactor of described gas stripping column connects steam boiler 5 by steam-pipe.
Preferably, on the esterification main pipeline of the esterification pipeline between the esterification pipeline between the esterification water out on the top of described process tower and the esterification water inlet of described gas stripping column and the esterification water out on top of described process tower and the esterification water inlet of described Ethanal distillation column, overhead condenser 11, esterification water collecting groove 13 and esterification water fresh feed pump 14 are installed, wherein said overhead condenser is relatively short with the distance of the described process tower of described esterification water collecting groove distance, and described esterification water collecting groove is between described esterification water fresh feed pump and described overhead condenser.
Further, the utility model also comprises process tower tail gas elution device 12, and described esterification water collecting groove can also be connected with described process tower tail gas elution device.Its washing water can adopt low temperature de-salted water.The process tail gas of PET device adopts the drip washing of low temperature de-mineralized water, and acetaldehyde is soluble in water, and washing water can absorb most acetaldehyde in tail gas.The whole esterification hydrations of washing water and PET device technique tower top also flow to esterification water collecting groove certainly, and in like manner, the esterification water of described process tower also utilizes its difference of altitude gravity flow to enter described esterification water collecting groove.
Preferably, the air lift wastewater outlet of described gas stripping column and the reflux line between the reflux inlet of described process tower is divided into main return line and stripping reflux is in charge of, the wastewater of rectification outlet of described Ethanal distillation column and reflux line between the reflux inlet of described process tower are divided into main reflux line and rectifying and reflux and be in charge of, from described process tower to described main reflux line, described stripping reflux, be in charge of and junction that described rectifying backflow is in charge of main reflux line recirculation water transferpump 15 and backflow lime set receiving tank 16 are installed successively.
The utility model is also provided with interchanger, and the heat tunnel of described interchanger is connected with the esterification pipeline between described rectifying tower with described process tower, and the thermal source passage of described interchanger refluxes to be in charge of with described rectifying and is connected.Esterification water is first and rectifying tower processing wastewater heat exchange before entering rectifying tower, the waste heat of recovery process waste water.
Conventionally, described stripping reflux is in charge of can be provided with air lift waste water transferpump 21, stripping reflux between described air lift waste water transferpump and described process tower is in charge of can be provided with stripping reflux arm, and the other end of described stripping reflux arm can connect air lift sewage works 6.
Conventionally, described rectifying refluxes to be in charge of wastewater of rectification transferpump 31 can be installed, rectifying between described wastewater of rectification transferpump and described process tower refluxes to be in charge of and can be provided with rectifying backflow arm, and the other end of described rectifying backflow arm can connect rectifying sewage works 7.
Certainly, described air lift sewage works and described rectifying sewage works can be same sewage works.
In actual use, the valve of controlling gas stripping column and the corresponding esterification pipeline break-make of process tower can be set on esterification pipeline that can be between gas stripping column and process tower and the esterification pipeline between rectifying tower and process tower, when normal production, Ethanal distillation column preferentially puts into operation, can avoid high energy consumption, the poor benefit operation of stripping tower, when Ethanal distillation column maintenance, maintenance period, use gas stripping column, assurance is carried out pre-treatment to the esterification water of PET device is continual, and further biochemical treatment has a negative impact to processing wastewater to avoid acetaldehyde.
The utility model is compared simple steam stripping processing method (method 1 and method 2 in background technology), about cost of investment doubles, but because the added value of industrial acetaldehyde is higher, described in above, air lift tail gas is delivered to pipestill for heat carrier and is burned, approximately 2480 yuan/ton of acetaldehyde are only rolled in the contribution of incinerating combustion value, compare 7000 yuan/ton of the selling prices of industrial acetaldehyde, benefit of the present utility model is 2.8 times of simple steam stripping processing method, running cost, the utility model is lower than adopting simple steam stripping processing method.
The utility model is with respect to the method (number of patent application: 201010602167.7) that reclaims ethylene glycol and acetaldehyde in polyester waste water, income, the yield difference of acetaldehyde is little, recovery for ethylene glycol, originally be the ethylene glycol content that fundamentally reduces technique tower top from being, and the ethylene glycol water content that contrast patent need adopt the method for distillation to reclaim is higher, the ability of need to further dewatering in process tower reuse, and contain plurality of impurities, reuse grade is poor.
From cost of investment, the utility model has lacked ethylene glycol distillation tower and supporting heating and e Foerderanlage, and the stripping tail gas condensing that may need and storage handling equipment, and therefore, the investment of conservative estimation the utility model saves at least 40%.
From running cost, according to conservative measuring and calculating, more than the energy consumption of contrast patent is amounted to 1.2 tons of mark oil/ton acetaldehyde, and energy consumption cost of the present utility model measuring and calculating is as follows:
Energy consumption of the present utility model is only 36.3% of contrast patent, and energy-conservation amplitude is obvious, and energy-saving effect is remarkable.

Claims (10)

1. the PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content, comprise process tower, characterized by further comprising gas stripping column and the Ethanal distillation column of setting parallel with one another, the esterification water out on the top of described process tower is connected by esterification pipeline with the esterification water inlet of described gas stripping column and the esterification water inlet of described Ethanal distillation column respectively, and the air lift wastewater outlet of described gas stripping column and the outlet of the wastewater of rectification of described Ethanal distillation column are connected with the reflux inlet of described process tower by each self-corresponding reflux line respectively.
2. the PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content according to claim 1, it is characterized in that described Ethanal distillation column is divided into packing section and tower plate structure section from top to bottom, in described packing section, be filled with efficient wire packing, in described tower plate structure section, be provided with column plate.
3. the PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content according to claim 2, is characterized in that being provided with heating unit in the tower reactor of described Ethanal distillation column.
4. the PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content according to claim 3, the acetaldehyde outlet that it is characterized in that the tower top of described Ethanal distillation column is connected with acetaldehyde lime set receiving tank by acetaldehyde pipeline, on described acetaldehyde pipeline, acetaldehyde condenser is installed.
5. the PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content according to claim 1, the tail gas outlet that it is characterized in that the top of described gas stripping column is connected with pipestill for heat carrier incinerator by air lift exhaust pipe, and the steam-in of the tower reactor of described gas stripping column is connected with steam boiler by steam-pipe.
6. according to the PET production system that can reclaim acetaldehyde and reduction technique tower top ethylene glycol content described in claim 1-5 any one, it is characterized in that, on the esterification main pipeline of the esterification water out on top of described process tower and the esterification water out on top of the esterification pipeline between the esterification water inlet of described gas stripping column and described process tower and the esterification pipeline between the esterification water inlet of described Ethanal distillation column, overhead condenser is installed, esterification water collecting groove and esterification water fresh feed pump, wherein said overhead condenser is short with respect to the distance of the described process tower of described esterification water collecting groove distance, described esterification water collecting groove is between described esterification water fresh feed pump and described overhead condenser.
7. the PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content according to claim 6, characterized by further comprising process tower tail gas elution device, and described esterification water collecting groove is also connected with described process tower tail gas elution device.
8. according to the PET production system that can reclaim acetaldehyde and reduction technique tower top ethylene glycol content described in claim 1-5 any one, it is characterized in that the air lift wastewater outlet of described gas stripping column and the reflux line between the reflux inlet of described process tower is divided into main return line and stripping reflux is in charge of, the wastewater of rectification outlet of described Ethanal distillation column is divided into main reflux line with reflux line between the reflux inlet of described process tower and rectifying backflow is in charge of, from described process tower to described main reflux line, the main reflux line that described stripping reflux is in charge of and described rectifying refluxes between the junction of being in charge of is provided with recirculation water transferpump and backflow lime set receiving tank successively.
9. the PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content according to claim 8, it is characterized in that described stripping reflux is in charge of is provided with air lift waste water transferpump, stripping reflux between described air lift waste water transferpump and described process tower is in charge of and is provided with stripping reflux arm, and the other end of described stripping reflux arm connects air lift sewage works.
10. the PET production system that can reclaim acetaldehyde and reduce technique tower top ethylene glycol content according to claim 8, it is characterized in that described rectifying refluxes to be in charge of is provided with wastewater of rectification transferpump, rectifying between described wastewater of rectification transferpump and described process tower refluxes to be in charge of and is provided with rectifying backflow arm, and the other end of described rectifying backflow arm connects rectifying sewage works.
CN201420056102.0U 2014-01-29 2014-01-29 PET (Polyethylene Glycol Terephthalate) production system capable of recycling acetaldehyde and reducing ethanediol content at process tower top Active CN203794819U (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107445802A (en) * 2017-08-21 2017-12-08 上海聚友化工有限公司 A kind of method that ethylene glycol and acetaldehyde are reclaimed in polyester waste water

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107445802A (en) * 2017-08-21 2017-12-08 上海聚友化工有限公司 A kind of method that ethylene glycol and acetaldehyde are reclaimed in polyester waste water
CN107445802B (en) * 2017-08-21 2020-12-08 上海聚友化工有限公司 Method for recovering ethylene glycol and acetaldehyde from polyester wastewater

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Address after: 100037 Beijing city Haidian District Zengguang Road No. 21

Patentee after: China Kunlun Engineering Co., Ltd.

Patentee after: China Textile Industrial Engineering Institute

Address before: 100037 Beijing city Haidian District Zengguang Road No. 21

Patentee before: China Kunlun Contracting & Engineering Corporation

Patentee before: China Textile Industrial Engineering Institute

Address after: 100037 Beijing city Haidian District Zengguang Road No. 21

Patentee after: China Kunlun Engineering Co., Ltd.

Patentee after: China Textile Industrial Engineering Institute

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Address after: 100037 Beijing city Haidian District Zengguang Road No. 21

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