CN104132321A - Method for recycling and utilizing waste heat of raw coke oven gas - Google Patents
Method for recycling and utilizing waste heat of raw coke oven gas Download PDFInfo
- Publication number
- CN104132321A CN104132321A CN201410410929.1A CN201410410929A CN104132321A CN 104132321 A CN104132321 A CN 104132321A CN 201410410929 A CN201410410929 A CN 201410410929A CN 104132321 A CN104132321 A CN 104132321A
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- steam
- coke oven
- waste heat
- water
- raw coke
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- 239000000571 coke Substances 0.000 title claims abstract description 48
- 239000007789 gas Substances 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000002918 waste heat Substances 0.000 title claims abstract description 22
- 238000004064 recycling Methods 0.000 title claims abstract description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 70
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 53
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 35
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 19
- 238000010438 heat treatment Methods 0.000 claims abstract description 11
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N benzene Substances C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 8
- 238000005192 partition Methods 0.000 claims description 6
- 238000007701 flash-distillation Methods 0.000 claims description 5
- 230000001502 supplementing effect Effects 0.000 claims description 5
- 239000013589 supplement Substances 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 abstract description 5
- 230000008020 evaporation Effects 0.000 abstract 2
- 238000001704 evaporation Methods 0.000 abstract 2
- 238000013021 overheating Methods 0.000 abstract 2
- 238000012824 chemical production Methods 0.000 abstract 1
- 239000003034 coal gas Substances 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 7
- 239000003245 coal Substances 0.000 description 5
- 239000008234 soft water Substances 0.000 description 5
- 238000004939 coking Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000003763 carbonization Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000014171 carbonated beverage Nutrition 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to the technical field of recycling and utilizing of waste heat of raw coke oven gas, in particular to a method for recycling and utilizing the waste heat of raw coke oven gas. According to the method for recycling and utilizing the waste heat of raw coke oven gas, an evaporation system is connected with a steam overheating system. The steam overheating system is connected with an ammonia still, a debenzolization tower and a rich-oil heater. The ammonia still and the rich-oil heater are both connected with a flash tank through a condensate water pipe. The flash tank is connected with a flash steam pipe and a water supply pipe. The flash tank is connected with the evaporation system through a water pump. By the adoption of the method for recycling and utilizing the waste heat of raw coke oven gas, the waste heat of part of raw coke oven gas in a coke oven uptake pipe is recycled, saturated vapor at a certain pressure is generated, the saturated steam is heated to become overheated steam through the waste heat of part of raw coke oven gas in the coke oven uptake pipe, the overheated steam is adopted by the ammonia sill and the debenzolization tower in a chemical production workshop and applied to heating of rich oil, generated condensate water flows back to a raw coke oven gas waste heat recycling system after flash to be heated into saturated steam, so that a steam-water circulation system is formed, and the problems of the background technology are solved.
Description
Technical field:
The present invention relates to waste heat of coke oven crude gas recovery and utilization technology field, be specifically related to the method for utilizing of steam that waste heat recovery produces in tedge on a kind of coking industry coke oven.
Background technology:
The general carbonization chamber method that just uses of coking enterprise is fired this traditional handicraft of coke, add the heated rear a large amount of raw coke oven gas that produces of coking coal in carbonization chamber, its temperature is at 650 DEG C--and 800 DEG C, tedge belongs to an equipment on coke oven, its effect is exactly that the high temperature raw coke oven gas that carbonization chamber is produced imports discharge, and the waste heat of high temperature raw coke oven gas in tedge just fails to utilize for many years always, can only heat be wasted with cyclic ammonia water cooling.
The task of producing workshop in coking industryization is by raw coke oven gas cooling, separates, in this process, there is the operation such as ammonia still process, de-benzene, need a large amount of steam in these operations, traditional method is: in boiler, emit heat by burning coal gas or fire coal, soft water heating is produced to saturated vapor for operations such as ammonia stills; And needed superheated steam is to adopt to emit heat by burning coal gas in tube furnace saturated vapor is heated up as superheated steam in the process of de-benzene, in debenzolizing tower, required rich oil also need to be heated to the temperature needing entering in tube furnace before debenzolizing tower.Therefore, the heating of the production of saturated vapor and overheated and rich oil all needs a large amount of coal gas that burns, and needs to consume coal gas and produces again a large amount of CO2 emissions; Steam adds the waste water producing again after ammonia still and debenzolizing tower with the steam equivalent adding, and has increased the expense of wastewater treatment; The tube furnace of heating steam is in production area, belongs to naked light operation, brings hidden danger to safety in production.
Summary of the invention:
The object of this invention is to provide a kind of method that waste heat of coke oven crude gas reclaims and utilizes, it is by the raw coke oven gas waste heat recovery in part coke oven coke oven uprising tube, produce the saturated vapor of certain pressure, saturated vapor is heated into superheated steam by raw coke oven gas waste heat in recycling part coke oven coke oven uprising tube, for changing the ammonia still, debenzolizing tower and the heating rich oil that produce workshop, the condensed water generating returns waste heat of coke oven crude gas recovery system again and is heated into saturated vapor after flash distillation, form steam-water circulation system, solve the problem existing in background technology.
In order to solve the existing problem of background technology, the present invention is by the following technical solutions: it comprises vapo(u)rization system 1, steam superheating system 2, ammonia still 3, debenzolizing tower 4, rich oil heater 5, condensate pipe 6, flash-off steam pipe 7, flash tank 8, supplement water pipe 9, water pump 10, vapo(u)rization system 1 is connected with steam superheating system 2, steam superheating system 2 respectively with ammonia still 3, debenzolizing tower 4, rich oil heater 5 connects, ammonia still 3, rich oil heater 5 is all connected with flash tank 8 by condensate pipe 6, flash tank 8 respectively with flash-off steam pipe 7, supplementing water pipe 9 connects, and flash tank 8 is connected with vapo(u)rization system 1 by water pump 10.
Described vapo(u)rization system 1 is made up of n tedge, drum, circulating pump etc., in each tedge, evaporimeter is installed, the water heating in evaporimeter is produced the saturated vapor higher than steam boiler institute producing steam pressure by high temperature raw coke oven gas in tedge, if do not consider the recovery of flash-off steam, the pressure of the superheated steam that vapo(u)rization system 1 and steam superheating system 2 form is arbitrarily.
Described steam superheating system 2 is made up of n tedge, in each tedge, superheater is installed, and the high temperature raw coke oven gas in tedge produces being heated into of saturated vapor in superheater the superheated steam of the required temperature in workshop.
Workflow of the present invention is: superheated steam is guided to the reboiler of ammonia still 3, the ammoniacal liquor in heating ammonia still 3; Guide to rich oil heat exchanger 5 and heat the rich oil into debenzolizing tower; Guide to the de-benzene of the interior rectifying of debenzolizing tower 4; Superheated steam through with ammonia still 3, rich oil heat exchanger 5 in medium become condensed water after by partition heat exchange, condensed water flashes off low-pressure steam after entering flash tank 8, is incorporated to the pipe network of saturated vapor that steam boiler produces; Water after flash distillation and the water newly covering return in vapo(u)rization system 1 by water pump 10, continue and high temperature raw coke oven gas heat exchange generation steam in n props up tedge, form recycling of water.
The present invention has following beneficial effect:
Change coal chemical enterprise steam coal or gas-fired generation steam in the past, in tube furnace, by burning coal gas, the saturated vapor of boiler for producing is heated into superheated steam again, simultaneously, rich oil lower temperature is heated to the method for the 180 DEG C left and right required into debenzolizing tower, use instead and reclaim the interior high temperature raw coke oven gas waste heat for generating steam of coke oven coke oven uprising tube and be superheated to ammonia still, debenzolizing tower and the temperature required superheated steam of rich oil heater, cut off the tube furnace that brings hidden danger to safety in production, save again a large amount of fire coals, coal gas, the expense of soft water and processing waste water, the remarkable in economical benefits of bringing to enterprise.
Brief description of the drawings:
Fig. 1 is structural representation of the present invention.
Detailed description of the invention:
With reference to Fig. 1, this detailed description of the invention is by the following technical solutions: it comprises vapo(u)rization system 1, steam superheating system 2, ammonia still 3, debenzolizing tower 4, rich oil heater 5, condensate pipe 6, flash-off steam pipe 7, flash tank 8, supplement water pipe 9, water pump 10, vapo(u)rization system 1 is connected with steam superheating system 2, steam superheating system 2 respectively with ammonia still 3, debenzolizing tower 4, rich oil heater 5 connects, ammonia still 3, rich oil heater 5 is all connected with flash tank 8 by condensate pipe 6, flash tank 8 respectively with flash-off steam pipe 7, supplementing water pipe 9 connects, and flash tank 8 is connected with vapo(u)rization system 1 by water pump 10.
Described vapo(u)rization system 1 is made up of n tedge, drum, circulating pump etc., in each tedge, evaporimeter is installed, the water heating in evaporimeter is produced the saturated vapor higher than steam boiler institute producing steam pressure by high temperature raw coke oven gas in tedge, if do not consider the recovery of flash-off steam, the pressure of the superheated steam that vapo(u)rization system 1 and steam superheating system 2 form is arbitrarily.
Described steam superheating system 2 is made up of n tedge, in each tedge, superheater is installed, and the high temperature raw coke oven gas in tedge produces being heated into of saturated vapor in superheater the superheated steam of the required temperature in workshop.
The operation principle of this detailed description of the invention is: the soft water of outer confession enters vapo(u)rization system 1 through water pump 10, after being heated by high temperature raw coke oven gas in the evaporimeter arranging in n props up tedge, in drum, carry out carbonated drink separation, steam devaporation superheating system 2, water under separating and the water newly being covered by water pump 10 go the evaporimeter in tedge to continue and the heat exchange of high temperature raw coke oven gas again, circulation and so forth; Steam enters steam superheating system 2, is propped up the superheated steam that is continued the required temperature in becoming of heating product workshop in the superheater arranging in tedge by high temperature raw coke oven gas at another part by n; Entering of superheated steam produced workshop for ammonia still 3, debenzolizing tower 4 and rich oil heater 5, has two schemes at this:
Scheme one: superheated steam enter respectively in the reboiler of ammonia still 3 and in rich oil heater 5 with ammonia still 3 in ammoniacal liquor and the rich oil partition heat exchange in rich oil heater 5, superheated steam is passed to ammoniacal liquor and rich oil by entrained heat by tube wall, after ammoniacal liquor is heated, realizes separating of ammonia and water; Rich oil enters debenzolizing tower 4 after heated rich oil heat exchanger 5 is interior, and another part superheated steam also adds debenzolizing tower 4, adopts rectification method to realize separating and crude benzol being taken out of outside debenzolizing tower of crude benzol and rich oil.Superheated steam through with ammonia still 3 in ammoniacal liquor, rich oil in rich oil heat exchanger 5 lower the temperature after by partition heat exchange, become condensed water.Condensed water is discharged in flash tank 8 through condensate pipe 6, flash off steam 7 and send into Boiler Steam pipe network, condensed water after flash distillation together with the supplementing water filling into 9 through water pump 10 be admitted to again vapo(u)rization system 1 enter in the evaporimeter in tedge again heated, circulation and so forth.
Scheme two: superheated steam directly enters in ammonia still 3, steam is passed to heat self to become condensed water after ammoniacal liquor and mix with the waste water after ammonia still process; Enter steam in rich oil heater 5 by with the heat exchange of rich oil partition after lower the temperature, become condensed water; Another part superheated steam also adds debenzolizing tower 4, adopts rectification method to realize separating and crude benzol being taken out of outside debenzolizing tower of crude benzol and rich oil.Be discharged in flash tank 8 at the condensed water of rich oil heater 5 interior generations, flash off steam 7 and send into Boiler Steam pipe network, condensed water after flash distillation together with the supplementing water filling into 9 through water pump 10 be admitted to again vapo(u)rization system 1 enter in the evaporimeter in tedge again heated, circulation and so forth.
Scheme one and scheme two compare: in scheme one, steam is added in the reboiler of ammonia still 3, and steam and ammoniacal liquor are partition heat exchange, and its condensed water does not enter in the waste water after ammonia still process, but recycles; And in scheme two, steam is to be introduced directly in the ammoniacal liquor of ammonia still 3, its condensed water has been stayed in the waste water after ammonia still process, scheme two had both caused the waste of soft water by contrast, because of after condensed water stayed in the waste water after ammonia still process, be finally will be discharged to wastewater treatment center to go again, so not only caused the waste of soft water, meanwhile, also increased the disposal cost of waste water.Be not difficult to find out that scheme one is better than scheme two.
The pressure of the superheated steam that described process vapo(u)rization system 1 and steam superheating system 2 form is the saturated vapour pressure that produces higher than boiler; If do not consider the recovery of flash-off steam, the pressure of the superheated steam that vapo(u)rization system 1 and steam superheating system 2 form is arbitrarily.
This detailed description of the invention can make the waste heat of raw coke oven gas in coke oven coke oven uprising tube be recycled utilization; Change product workshop and thoroughly eliminate the potential safety hazard that tube furnace brings; The coal gas that saving boiler fired coal and boiler, tube furnace burn, for enterprise brings good economic benefit.
Claims (4)
1. the method that waste heat of coke oven crude gas reclaims and utilizes, it is characterized in that it comprises vapo(u)rization system (1), steam superheating system (2), ammonia still (3), debenzolizing tower (4), rich oil heater (5), condensate pipe (6), flash-off steam pipe (7), flash tank (8), supplement water pipe (9), water pump (10), vapo(u)rization system (1) is connected with steam superheating system (2), steam superheating system (2) respectively with ammonia still (3), debenzolizing tower (4), rich oil heater (5) connects, ammonia still (3), rich oil heater (5) is all connected with flash tank (8) by condensate pipe (6), flash tank (8) respectively with flash-off steam pipe (7), supplementing water pipe (9) connects, and flash tank (8) is connected with vapo(u)rization system (1) by water pump (10).
2. the method that a kind of waste heat of coke oven crude gas according to claim 1 reclaims and utilizes, is characterized in that its workflow is: superheated steam is guided to the reboiler of ammonia still (3), the ammoniacal liquor in heating ammonia still (3); Guide to rich oil heat exchanger (5) and heat the rich oil into debenzolizing tower; Guide to the de-benzene of the interior rectifying of debenzolizing tower (4); Superheated steam through and ammonia still (3), rich oil heat exchanger (5) in medium become condensed water after by partition heat exchange, condensed water flashes off low-pressure steam after entering flash tank (8), is incorporated to the pipe network of saturated vapor that steam boiler produces; Water after flash distillation and the water newly covering return in vapo(u)rization system (1) by water pump (10), continue and high temperature raw coke oven gas heat exchange generation steam in n props up tedge, form recycling of water.
3. the method that a kind of waste heat of coke oven crude gas according to claim 1 reclaims and utilizes, it is characterized in that described vapo(u)rization system (1) is made up of n tedge, drum, circulating pump etc., in each tedge, evaporimeter is installed, the water heating in evaporimeter is produced the saturated vapor higher than steam boiler institute producing steam pressure by high temperature raw coke oven gas in tedge, if do not consider the recovery of flash-off steam, the pressure of the superheated steam that vapo(u)rization system (1) and steam superheating system (2) form is arbitrarily.
4. the method that a kind of waste heat of coke oven crude gas according to claim 1 reclaims and utilizes, it is characterized in that described steam superheating system (2) is made up of n tedge, in each tedge, superheater is installed, the high temperature raw coke oven gas in tedge produces being heated into of saturated vapor in superheater the superheated steam of the required temperature in workshop.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410410929.1A CN104132321A (en) | 2014-08-20 | 2014-08-20 | Method for recycling and utilizing waste heat of raw coke oven gas |
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| CN201410410929.1A CN104132321A (en) | 2014-08-20 | 2014-08-20 | Method for recycling and utilizing waste heat of raw coke oven gas |
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| CN104132321A true CN104132321A (en) | 2014-11-05 |
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| CN201410410929.1A Pending CN104132321A (en) | 2014-08-20 | 2014-08-20 | Method for recycling and utilizing waste heat of raw coke oven gas |
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Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108151547A (en) * | 2018-01-31 | 2018-06-12 | 济南冶金化工设备有限公司 | Recycling waste heat of coke oven crude gas is used to take off the device and method of benzene and ammonia still process |
| CN108424793A (en) * | 2018-05-17 | 2018-08-21 | 山东焦化技术咨询服务有限公司 | Rich oil de-benzene system and rich oil de-benzene method |
| CN109054887A (en) * | 2018-10-17 | 2018-12-21 | 北京华泰焦化工程技术有限公司 | Equipment, the method for de- benzene rich oil |
| CN109777448A (en) * | 2019-03-28 | 2019-05-21 | 陕西驭腾实业有限公司 | A kind of coke oven coke oven uprising tube raw coke oven gas waste heat is used to that tube furnace to be replaced to take off benzene device |
| CN110307535A (en) * | 2019-07-30 | 2019-10-08 | 山东凯瑞英材料科技有限公司 | A kind of system and method for superheated water low-pressure steam |
| CN111217664A (en) * | 2019-07-30 | 2020-06-02 | 杨承诣 | Device for heating rich oil and distilling crude benzene by using waste heat of raw gas and producing crude benzene by negative pressure |
| CN111594826A (en) * | 2020-06-08 | 2020-08-28 | 唐山市宝凯科技有限公司 | A kind of oil-rich debenzene condensed water recycling system and method |
| CN112275104A (en) * | 2020-10-16 | 2021-01-29 | 北京中航泰达环保科技股份有限公司 | A comprehensive utilization system of flue gas waste heat for coke oven flue gas semi-dry process |
| WO2021097905A1 (en) * | 2019-11-19 | 2021-05-27 | 南京华电节能环保设备有限公司 | Recycling device for high-temperature sensible heat of raw coke oven gas in coke oven ascension pipe |
| CN113061442A (en) * | 2021-03-30 | 2021-07-02 | 太原理工大学 | A rising pipe for wet oxidation treatment of wastewater |
| CN113444548A (en) * | 2021-07-13 | 2021-09-28 | 山东钢铁股份有限公司 | Rich oil debenzolization heating system utilizing coke oven crude gas heat |
| CN114543576A (en) * | 2022-01-25 | 2022-05-27 | 中建石化工程有限公司 | System and method for utilizing waste heat of byproduct steam of coal-to-ethylene glycol device |
| CN114774137A (en) * | 2022-04-29 | 2022-07-22 | 中冶焦耐(大连)工程技术有限公司 | Coke oven riser waste heat steam production heating reheating method and system |
| CN115790189A (en) * | 2022-12-30 | 2023-03-14 | 东北大学设计研究院（有限公司） | System and method for preparing steam by using coke waste heat after high-temperature calcination of pot-type calciner |
| CN118602799A (en) * | 2024-06-26 | 2024-09-06 | 中冶焦耐(大连)工程技术有限公司 | A method for extracting steam by combining high-temperature condensate with rising pipe |
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Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108151547A (en) * | 2018-01-31 | 2018-06-12 | 济南冶金化工设备有限公司 | Recycling waste heat of coke oven crude gas is used to take off the device and method of benzene and ammonia still process |
| CN108424793A (en) * | 2018-05-17 | 2018-08-21 | 山东焦化技术咨询服务有限公司 | Rich oil de-benzene system and rich oil de-benzene method |
| CN109054887A (en) * | 2018-10-17 | 2018-12-21 | 北京华泰焦化工程技术有限公司 | Equipment, the method for de- benzene rich oil |
| CN109777448A (en) * | 2019-03-28 | 2019-05-21 | 陕西驭腾实业有限公司 | A kind of coke oven coke oven uprising tube raw coke oven gas waste heat is used to that tube furnace to be replaced to take off benzene device |
| CN110307535A (en) * | 2019-07-30 | 2019-10-08 | 山东凯瑞英材料科技有限公司 | A kind of system and method for superheated water low-pressure steam |
| CN111217664A (en) * | 2019-07-30 | 2020-06-02 | 杨承诣 | Device for heating rich oil and distilling crude benzene by using waste heat of raw gas and producing crude benzene by negative pressure |
| WO2021097905A1 (en) * | 2019-11-19 | 2021-05-27 | 南京华电节能环保设备有限公司 | Recycling device for high-temperature sensible heat of raw coke oven gas in coke oven ascension pipe |
| CN111594826A (en) * | 2020-06-08 | 2020-08-28 | 唐山市宝凯科技有限公司 | A kind of oil-rich debenzene condensed water recycling system and method |
| CN112275104A (en) * | 2020-10-16 | 2021-01-29 | 北京中航泰达环保科技股份有限公司 | A comprehensive utilization system of flue gas waste heat for coke oven flue gas semi-dry process |
| CN112275104B (en) * | 2020-10-16 | 2025-11-25 | 北京中航泰达环保科技股份有限公司 | A comprehensive waste heat utilization system for semi-dry coke oven gas process |
| CN113061442A (en) * | 2021-03-30 | 2021-07-02 | 太原理工大学 | A rising pipe for wet oxidation treatment of wastewater |
| CN113061442B (en) * | 2021-03-30 | 2022-03-11 | 太原理工大学 | A rising pipe for wet oxidation treatment of wastewater |
| CN113444548A (en) * | 2021-07-13 | 2021-09-28 | 山东钢铁股份有限公司 | Rich oil debenzolization heating system utilizing coke oven crude gas heat |
| CN114543576A (en) * | 2022-01-25 | 2022-05-27 | 中建石化工程有限公司 | System and method for utilizing waste heat of byproduct steam of coal-to-ethylene glycol device |
| CN114543576B (en) * | 2022-01-25 | 2023-08-18 | 中建石化工程有限公司 | A system and method for utilizing waste heat of by-product steam in a coal-to-ethylene glycol plant |
| CN114774137A (en) * | 2022-04-29 | 2022-07-22 | 中冶焦耐(大连)工程技术有限公司 | Coke oven riser waste heat steam production heating reheating method and system |
| CN115790189A (en) * | 2022-12-30 | 2023-03-14 | 东北大学设计研究院（有限公司） | System and method for preparing steam by using coke waste heat after high-temperature calcination of pot-type calciner |
| CN118602799A (en) * | 2024-06-26 | 2024-09-06 | 中冶焦耐(大连)工程技术有限公司 | A method for extracting steam by combining high-temperature condensate with rising pipe |
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Application publication date: 20141105 |