CN110523230A - A kind of energy-efficient deacidifion technique and system - Google Patents
A kind of energy-efficient deacidifion technique and system Download PDFInfo
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- CN110523230A CN110523230A CN201910924155.7A CN201910924155A CN110523230A CN 110523230 A CN110523230 A CN 110523230A CN 201910924155 A CN201910924155 A CN 201910924155A CN 110523230 A CN110523230 A CN 110523230A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
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Abstract
The present invention relates to a kind of energy-efficient deacidifion techniques and system, set gradually depickling section from top to bottom the system comprises deacidifion tower, in deacidifion tower, waste water distilling period, wash ammonia distillation section；Depickling section distills to obtain hot lean solution, and waste water distilling period distills to obtain the distilled ammonia wastewater that ammon amount is 200mg/l, and that washes that ammonia distillation section distills to obtain ammon amount 50mg/l washes ammonium hydroxide.The present invention is using the multistage substep way of distillation, and while obtaining meeting discharge standard distilled ammonia wastewater, high quality of having got back washes ammonium hydroxide, while reducing heating steam consumption quantity and consumption of cooling-water.
Description
Technical field
The present invention relates to coke oven gas purification technical field, more particularly to a kind of energy-efficient deacidifion technique and it is
System.
Background technique
Desulphurization Technology Coke Oven Gas has two kinds of dry and wet, and wet desulfurizing process includes wet absorption method and wet type oxygen again
Two class of change method, wherein have without using catalyst, ammonia sulphur while removing, nothing using ammonia in coal gas as the wet absorption method technique of alkali source
The advantages of waste residue/discharging of waste liquid, has been to be concerned by more and more people under the increasingly harsh background of environmental protection standard.
Ammonium hydroxide technique is medium containing ammonia solution, is washed and removed using ammonia sulfur cycle using the ammonia in coke-stove gas as alkali source
H in coal gas2S and NH3Method.The method is made of washing unit and deacidifion unit two parts, and washing unit is H2S and NH3
Etc. components absorption part, deacidifion unit is H2S and NH3Etc. components desorption part.In gas washing unit, by desulfurization
Tower configuration is before Ammonic washing tower, to wash the rich ammonium hydroxide that ammonia obtains and the depickling lean solution that deacidifion unit returns as washing medium
Remove the H in coal gas2S is formed and is contained H2S and NH3Rich solution be sent to deacidifion unit.In deacidifion unit, rich solution passes through water
The depickling lean solution and low concentration ammonium hydroxide that steam stripping desorption obtains return again to the recycling of gas washing unit, and extra waste water is sent
Toward water treatment unit, what is desorbed contains H2S acidity steam can be used for producing sulphur or sulfuric acid.
To reduce the ammon amount after purification in coal gas, soft water section is set usually in Ammonic washing tower, using ammonia very soluble in
The characteristic of water strengthens the ammonia absorbed in coal gas.The Chinese patent of Patent No. CN201710898781 discloses a kind of " refining crude
The method of ammonia " uses the technique for first washing alkali cleaning again to obtain net ammonia.The China of Patent No. CN201120022278
Patent discloses " a kind of coke oven gas desulfurization deamination combined purifying device ", and soft water absorption ammonia can be used in Ammonic washing tower top.
Though the ammon amount in purified gas can be reduced using soft water absorption ammonia, also will increase simultaneously soft water consumption, soft water with
After rich solution enters junior's ammonia steaming system, it also will increase heating steam and cooling water consumption and increase efflux wastewater amount.If energy
Soft water is substituted using the water after deacidifion tower stripping, then can avoid the above problem.
Under the premise of guaranteeing that coal gas washes ammonia effect, replace soft water that need to be down to the ammon amount washed in ammonium hydroxide with ammonium hydroxide is washed
50mg/l, this index are higher than the requirement of efflux wastewater ammon amount 200mg/l.Obviously, all washing rich solutions are distilled to outlet
Waste water standard is difficult to meet coal gas and efficiently washes ammonia requirement, but all distillation to wash ammonium hydroxide standard again and will increase heating steam with
Cooling-water consumption, it is unreasonable from the angle of production run.
Summary of the invention
The present invention provides a kind of energy-efficient deacidifion techniques and system to be obtained using the multistage substep way of distillation
To while meeting discharge standard distilled ammonia wastewater, high quality of having got back washes ammonium hydroxide, at the same reduce heating steam consumption quantity and
Consumption of cooling-water.
In order to achieve the above object, the present invention is implemented with the following technical solutions:
A kind of energy-efficient deacidifion technique, includes the following steps:
1) enter deacidifion after poor rich liquid heat exchanger and the heat exchange of hot lean solution from cold rich solution a part that washing unit is come
Tower, another part are directly entered deacidifion tower；
2) it distills to obtain hot lean solution in the depickling section of deacidifion top of tower and exchange heat through poor rich liquid heat exchanger, then followed through lean solution
Washing unit desulfurization is sent to after ring water cooler and lean solution low temperature water cooler are cooling；
3) waste water distilling period is set in the middle part of deacidifion tower, the waste water of extraction is through waste water water recirculator and waste water low temperature
Water treatment unit is sent to after water cooler is cooling；
4) the ammonia distillation section of washing that remaining liquid phase after depickling and distillation enters deacidifion tower lower part continues to distill, and takes off
The ammonium hydroxide of washing of sour ammonia still process tower bottom exchanges heat pumped to ammonium hydroxide heat exchanger and remained ammonia, then washed ammonia circulation water cooler and
After washing the cooling of ammonium hydroxide low temperature water cooler, it is sent to washing unit and washes ammonia；
5) depickling section, waste water distilling period and heat needed for washing ammonia distillation section are provided by steam, external steam and wash ammonia
The steam that water is generated by flash tank is added in deacidifion tower by steam jet ejector, and the sour vapour that tower top steams is sent to subsequent list
Member processing.
The ammon amount of the distilled ammonia wastewater is 100~300mg/l, and the ammon amount for washing ammonium hydroxide is 10~100mg/l.
A kind of energy-efficient deacidifion system, including deacidifion tower；In the deacidifion tower from top to bottom according to
Secondary setting depickling section, washes ammonia distillation section at waste water distilling period；Sour vapor outlet is set at the top of deacidifion tower and rich solution first enters
Mouthful, rich solution first entrance is connected with rich solution conveyance conduit；Rich solution second entrance is set on tower body above depickling section, rich solution second enters
Mouth is connected by poor rich liquid heat exchanger with rich solution conveyance conduit；Lean solution outlet is set on the tower body of depickling section bottom, lean solution outlet is logical
It crosses lean solution conveyance conduit and connects external washing unit, be successively arranged rich or poor liquid along lean solution flow direction on lean solution conveyance conduit and exchange heat
Device, lean solution water recirculator and lean solution low temperature water cooler；Set on tower body above waste water distilling period steam first entrance and
Remained ammonia entrance, the steam conveying pipe outside the connection of steam first entrance, remained ammonia entrance connected by ammonium hydroxide heat exchanger
Connect remained ammonia conveyance conduit；Wastewater outlet is set on the tower body of waste water distilling period bottom, wastewater outlet passes through waste water conveyance conduit
Water treatment system is connected, is successively arranged waste water water recirculator and waste water low temperature along waste water flow direction on waste water conveyance conduit
Water cooler；It washes on the tower body of ammonia distillation section bottom and sets steam second entrance, steam second entrance is connected by ammonia still process injector
Connect steam conveying pipe；The bottom of deacidifion tower, which is set, washes ammonium hydroxide storage tank, and steam third is set on the tower body washed above ammonium hydroxide storage tank
Entrance, steam third entrance connect steam conveying pipe；It washes on the tower body of ammonium hydroxide storage tank side to set and washes ammonium hydroxide outlet, wash ammonium hydroxide and go out
The liquid inlet on mouthful connection flash tank top, the steam (vapor) outlet at the top of flash tank connect steam jet ejector, the liquid of flash drum bottom
Body outlet connection washes ammonium hydroxide conveyance conduit, wash on ammonium hydroxide conveyance conduit along wash ammonium hydroxide flow direction be successively arranged pump, ammonium hydroxide heat exchange
Device washes ammonia circulation water cooler and washes ammonium hydroxide low temperature water cooler.
It is successively arranged rich solution spray equipment, liquid distribution trough, packing section, tower tray from top to bottom in the tower body of the depickling section
And disconnected liquid disk.
Remained ammonia spray equipment is successively arranged in the tower body of the waste water distilling period from top to bottom, liquid distribution trough, is filled out
Expect section, tower tray and disconnected liquid disk.
The ammonia distillation section of washing is equipped with multiple filling layers and tower tray.
Compared with prior art, the beneficial effects of the present invention are:
1) it using the NH3 washed in ammonium hydroxide substitution soft water removing coal gas, is consumed without soft water, reduces rich solution amount and outer waste discharge
Water；
2) using multistage substep distillation technique, reduce heating steam consumption quantity and consumption of cooling-water, have the characteristics that energy conservation；
3) it improves and washes ammonium hydroxide quality, ammonia content therein is made to be down to 50mg/l, the high-efficient deamination requirement of coal gas can be met；
4) process flow is simple, investment operating cost is few, it is easy to accomplish and promote
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the energy-efficient deacidifion system of one kind of the present invention
In figure: 1. deacidifion tower, I, depickling section, II, waste water distilling period, III, washes 2. flash tank 3. of ammonia distillation section
4. poor rich liquid heat exchanger of steam jet ejector, 5. lean solution water recirculator, 6. lean solution low temperature water cooler 7. pumps 8. ammonium hydroxide and changes
Hot device 9. washes ammonia circulation water cooler 10., and to wash ammonium hydroxide low temperature water cooler 11. waste water water recirculator, 12. waste water low
Warm water cooler
Specific embodiment
Specific embodiments of the present invention will be further explained with reference to the accompanying drawing:
As shown in Figure 1, the deacidifion technique that one kind of the present invention is energy-efficient, includes the following steps:
1) enter deacidifion after poor rich liquid heat exchanger 4 and the heat exchange of hot lean solution from cold rich solution a part that washing unit is come
Tower 1, another part are directly entered deacidifion tower 1；
2) distillation of depickling section I at the top of deacidifion tower 1 obtains hot lean solution and exchanges heat through poor rich liquid heat exchanger 4, then through poor
Washing unit desulfurization is sent to after liquid water recirculator 5 and lean solution low temperature water cooler 6 are cooling；
3) waste water distilling period II is set in the middle part of deacidifion tower 1, the waste water of extraction through waste water water recirculator 11 and gives up
Water treatment unit is sent to after water low temperature water cooler 12 is cooling；
4) the ammonia distillation section II of washing that remaining liquid phase after depickling and distillation enters 1 lower part of deacidifion tower continues to steam
It evaporates, the ammonium hydroxide of washing of 1 bottom of deacidifion tower is sent through pump 7 to ammonium hydroxide heat exchanger 8 and remained ammonia heat exchange, then is washed ammonia circulation water
Cooler 9 and after washing ammonium hydroxide low temperature water cooler cold 10 but, is sent to washing unit and washes ammonia；
5) depickling section I, waste water distilling period II and heat needed for washing ammonia distillation section are provided by steam, external steam and are washed
The steam that ammonium hydroxide is generated by flash tank 2 is added in deacidifion tower 1 by steam jet ejector 3, and the sour vapour that tower top steams is sent to
Subsequent cell processing.
The ammon amount of the distilled ammonia wastewater is 100~300mg/l, and the ammon amount for washing ammonium hydroxide is 10~100mg/l.
A kind of energy-efficient deacidifion system, including deacidifion tower 1；In the deacidifion tower 1 from top to bottom
It sets gradually depickling section I, waste water distilling period II, wash ammonia distillation section III；The top of deacidifion tower II sets sour vapor outlet and richness
Liquid first entrance, rich solution first entrance are connected with rich solution conveyance conduit；Rich solution second entrance is set on the tower body of I top of depickling section,
Rich solution second entrance is connected by poor rich liquid heat exchanger 4 with rich solution conveyance conduit；Lean solution is set on the tower body of I bottom of depickling section to go out
Mouthful, lean solution, which exports, passes through the external washing unit of lean solution conveyance conduit connection, on lean solution conveyance conduit successively along lean solution flow direction
Equipped with poor rich liquid heat exchanger 4, lean solution water recirculator 5 and lean solution low temperature water cooler 6；The tower body of II top of waste water distilling period
On set steam first entrance and remained ammonia entrance, the steam conveying pipe outside the connection of steam first entrance, remained ammonia enters
Mouth connects remained ammonia conveyance conduit by ammonium hydroxide heat exchanger 8；Wastewater outlet, waste water are set on the tower body of II bottom of waste water distilling period
Outlet connects water treatment system by waste water conveyance conduit, is successively arranged waste water along waste water flow direction on waste water conveyance conduit and follows
Ring water cooler 11 and waste water low temperature water cooler 12；It washes on the tower body of III bottom of ammonia distillation section and sets steam second entrance, steam
Vapour second entrance connects steam conveying pipe by ammonia still process injector 3；The bottom of deacidifion tower 1, which is set, washes ammonium hydroxide storage tank, washes ammonia
Steam third entrance is set on tower body above water storage tank, steam third entrance connects steam conveying pipe；Wash ammonium hydroxide storage tank side
Tower body on set and wash ammonium hydroxide outlet, wash the liquid inlet on ammonium hydroxide outlet connection 2 top of flash tank, the steam at the top of flash tank 2 goes out
Ammonium hydroxide conveyance conduit is washed in the liquid outlet connection of mouth connection steam jet ejector 3,2 bottom of flash tank, washes edge on ammonium hydroxide conveyance conduit
Ammonium hydroxide flow direction is washed to be successively arranged pump 7, ammonium hydroxide heat exchanger 8, wash ammonia circulation water cooler 9 and wash ammonium hydroxide low temperature water cooler
10。
It is successively arranged rich solution spray equipment, liquid distribution trough, packing section, tower from top to bottom in the tower body of the depickling section I
Disk and disconnected liquid disk.
Be successively arranged from top to bottom in the tower body of the waste water distilling period II remained ammonia spray equipment, liquid distribution trough,
Packing section, tower tray and disconnected liquid disk.
The ammonia distillation section III of washing is equipped with multiple filling layers and tower tray.
The energy-efficient deacidifion system of one kind of the present invention is first high by ammon amount using the multistage substep way of distillation
Water treatment unit is sent in distilled ammonia wastewater (ammon amount 200mg/l) extraction, then remaining fluid is mutually continued distillation and (is contained to washing ammonium hydroxide standard
Ammonia amount 50mg/l) after be sent to washing unit.
In the present invention, deacidifion tower 1 can also be replaced by the independent tower body with multiple similar functions, such as deacidifion
The depickling section I of tower 1 is replaced by independent extracting tower, and the waste water distilling period II of deacidifion tower 1 is by independent waste water destilling tower generation
It replaces, the ammonia distillation section III of washing of deacidifion tower 1 is replaced by independent ammonia distillation tower of washing.Steam feedway is sprayed in addition to steam
It, can also be using equipment such as reboilers outside emitter 3, flash tank 2.
It can only obtain the ammonium hydroxide of washing of ammon amount 50mg/l using whole distillation techniques, but using multistage substep distillation technique
Afterwards, the distilled ammonia wastewater of ammon amount 200mg/l can be obtained and obtain the ammonium hydroxide of washing of ammon amount 50mg/l again, while using whole
Distillation technique ratio uses a part heating steam and cooling circulating water using multistage substep distillation technique more.Obtaining equal quality
Under the premise of washing ammonium hydroxide (ammon amount 50mg/l), the present invention is to using whole distillation techniques and using multistage substep distillation technique
Energy consumption is calculated, and often obtains 1m after multistage substep distillation technique compared to using whole distillation techniques3Ammonia still process is useless
Water will save the steam and 0.5m that 10.4kg pressure is 0.4MPa3The recirculated water that temperature is 32~45 DEG C.
The foregoing is only a preferred embodiment of the present invention, but scope of protection of the present invention is not limited thereto,
Anyone skilled in the art in the technical scope disclosed by the present invention, according to the technique and scheme of the present invention and its
Inventive concept is subject to equivalent substitution or change, should be covered by the protection scope of the present invention.
Claims (6)
1. a kind of energy-efficient deacidifion technique, which comprises the steps of:
1) enter deacidifion tower after poor rich liquid heat exchanger and the heat exchange of hot lean solution from cold rich solution a part that washing unit is come, separately
A part is directly entered deacidifion tower；
2) it distills to obtain hot lean solution in the depickling section of deacidifion top of tower and exchange heat through poor rich liquid heat exchanger, then through lean solution recirculated water
Washing unit desulfurization is sent to after cooler and lean solution low temperature water cooler are cooling；
3) waste water distilling period is set in the middle part of deacidifion tower, the waste water of extraction is through waste water water recirculator and waste water low temperature water cooling
But water treatment unit is sent to after device is cooling；
4) the ammonia distillation section of washing that remaining liquid phase after depickling and distillation enters deacidifion tower lower part continues to distill, and depickling is steamed
The ammonium hydroxide of washing of ammonia tower bottom exchanges heat pumped to ammonium hydroxide heat exchanger and remained ammonia, then is washed ammonia circulation water cooler and wash ammonia
After water low temperature water cooler is cooling, it is sent to washing unit and washes ammonia；
5) depickling section, waste water distilling period and heat needed for washing ammonia distillation section are provided by steam, external steam and to wash ammonium hydroxide logical
The steam for crossing flash tank generation is added in deacidifion tower by steam jet ejector, and the sour vapour that tower top steams is sent at subsequent cell
Reason.
2. a kind of energy-efficient deacidifion technique as described in claim 1, which is characterized in that the distilled ammonia wastewater contains
Ammonia amount is 100~300mg/l, and the ammon amount for washing ammonium hydroxide is 10~100mg/l.
3. a kind of energy-efficient deacidifion system for realizing technique described in claim 1, including deacidifion tower；Its
It is characterized in that, sets gradually depickling section in the deacidifion tower from top to bottom, waste water distilling period, washes ammonia distillation section；Depickling
Sour vapor outlet and rich solution first entrance are set at the top of ammonia still, rich solution first entrance is connected with rich solution conveyance conduit；In depickling section
Rich solution second entrance is set on the tower body of side, rich solution second entrance is connected by poor rich liquid heat exchanger with rich solution conveyance conduit；Depickling
Lean solution outlet is set on the tower body of section bottom, lean solution outlet connects external washing unit, lean solution delivery pipe by lean solution conveyance conduit
Poor rich liquid heat exchanger, lean solution water recirculator and lean solution low temperature water cooler are successively arranged along lean solution flow direction on road；It is useless
Steam first entrance and remained ammonia entrance are set on tower body above water distilling period, the steam outside the connection of steam first entrance is defeated
Pipeline is sent, remained ammonia entrance connects remained ammonia conveyance conduit by ammonium hydroxide heat exchanger；On the tower body of waste water distilling period bottom
If wastewater outlet, wastewater outlet connects water treatment system by waste water conveyance conduit, along waste water flowing side on waste water conveyance conduit
To being successively arranged waste water water recirculator and waste water low temperature water cooler；It washes on the tower body of ammonia distillation section bottom and sets steam
Two entrances, steam second entrance connect steam conveying pipe by ammonia still process injector；The bottom of deacidifion tower, which is set, washes ammonium hydroxide storage
Slot, steam third entrance is set on the tower body washed above ammonium hydroxide storage tank, and steam third entrance connects steam conveying pipe；Wash ammonium hydroxide storage
It is set on the tower body of slot side and washes ammonium hydroxide outlet, wash the liquid inlet on ammonium hydroxide outlet connection flash tank top, the steaming at the top of flash tank
Vapor outlet connects steam jet ejector, and the liquid outlet connection of flash drum bottom is washed ammonium hydroxide conveyance conduit, washed on ammonium hydroxide conveyance conduit
It is successively arranged pump, ammonium hydroxide heat exchanger, wash ammonia circulation water cooler and washes ammonium hydroxide low temperature water cooler along ammonium hydroxide flow direction is washed.
4. the energy-efficient deacidifion system of one kind according to claim 3, which is characterized in that the tower of the depickling section
It is successively arranged rich solution spray equipment, liquid distribution trough, packing section, tower tray and disconnected liquid disk from top to bottom in vivo.
5. the energy-efficient deacidifion system of one kind according to claim 3, which is characterized in that the waste water distilling period
Tower body in be successively arranged remained ammonia spray equipment, liquid distribution trough, packing section, tower tray and disconnected liquid disk from top to bottom.
6. the energy-efficient deacidifion system of one kind according to claim 3, which is characterized in that described to wash ammonia distillation
Section is equipped with multiple filling layers and tower tray.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201910924155.7A CN110523230A (en) | 2019-09-27 | 2019-09-27 | A kind of energy-efficient deacidifion technique and system |
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| CN201910924155.7A CN110523230A (en) | 2019-09-27 | 2019-09-27 | A kind of energy-efficient deacidifion technique and system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114797380A (en) * | 2022-03-09 | 2022-07-29 | 铜陵泰富特种材料有限公司 | System and method for efficiently washing ammonia with phosphoric acid and producing high-purity ammonia water |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0062684A1 (en) * | 1981-04-09 | 1982-10-20 | Ruhrkohle Aktiengesellschaft | Process for removing ammonia and hydrogen sulfide from gases, in particular coal distillation gases |
| CN105984886A (en) * | 2015-02-05 | 2016-10-05 | 薛斌 | Process for producing anhydrous ammonia by ammonia distillation and deacidification |
| CN106673014A (en) * | 2016-12-29 | 2017-05-17 | 天津市创举科技有限公司 | Process of removing sulfur and ammonia from coke gas to prepare ammonia water |
| CN107935086A (en) * | 2017-12-22 | 2018-04-20 | 中冶焦耐(大连)工程技术有限公司 | A kind of efficiently deacidifion tower |
| CN207738709U (en) * | 2017-12-15 | 2018-08-17 | 中冶焦耐(大连)工程技术有限公司 | A kind of multifunctional combined scrubbing tower |
| CN210845815U (en) * | 2019-09-27 | 2020-06-26 | 中冶焦耐(大连)工程技术有限公司 | Energy-conserving efficient deacidification ammonia distillation system |
-
2019
- 2019-09-27 CN CN201910924155.7A patent/CN110523230A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0062684A1 (en) * | 1981-04-09 | 1982-10-20 | Ruhrkohle Aktiengesellschaft | Process for removing ammonia and hydrogen sulfide from gases, in particular coal distillation gases |
| CN105984886A (en) * | 2015-02-05 | 2016-10-05 | 薛斌 | Process for producing anhydrous ammonia by ammonia distillation and deacidification |
| CN106673014A (en) * | 2016-12-29 | 2017-05-17 | 天津市创举科技有限公司 | Process of removing sulfur and ammonia from coke gas to prepare ammonia water |
| CN207738709U (en) * | 2017-12-15 | 2018-08-17 | 中冶焦耐(大连)工程技术有限公司 | A kind of multifunctional combined scrubbing tower |
| CN107935086A (en) * | 2017-12-22 | 2018-04-20 | 中冶焦耐(大连)工程技术有限公司 | A kind of efficiently deacidifion tower |
| CN210845815U (en) * | 2019-09-27 | 2020-06-26 | 中冶焦耐(大连)工程技术有限公司 | Energy-conserving efficient deacidification ammonia distillation system |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114797380A (en) * | 2022-03-09 | 2022-07-29 | 铜陵泰富特种材料有限公司 | System and method for efficiently washing ammonia with phosphoric acid and producing high-purity ammonia water |
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