CN204727616U - For ammonia decontamination system and the phenol ammonia recovery unit thereof of crushed coal pressure gasifying sewage treatment process - Google Patents
For ammonia decontamination system and the phenol ammonia recovery unit thereof of crushed coal pressure gasifying sewage treatment process Download PDFInfo
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- CN204727616U CN204727616U CN201520205457.6U CN201520205457U CN204727616U CN 204727616 U CN204727616 U CN 204727616U CN 201520205457 U CN201520205457 U CN 201520205457U CN 204727616 U CN204727616 U CN 204727616U
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- tower
- ammonia decontamination
- phenol
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Abstract
The utility model belongs to coal chemical technology.Particularly, the utility model relates to a kind of ammonia decontamination system for crushed coal pressure gasifying sewage treatment process and phenol ammonia recovery unit thereof.Described ammonia decontamination system comprises: deammoniation tower, three grades of condensation liquid distributing devices, ammonia decontamination tower, lye vat and intercycle pipelines; Wherein, described deammoniation tower is connected with described ammonia decontamination tower bottom with intercycle pipeline through described three grades of condensation liquid distributing devices, and described ammonia decontamination tower is communicated with described lye vat at tower top again; Described ammonia decontamination tower circulation line in the middle part of the tower bottoms part after ammonia is incorporated to returns ammonia decontamination tower to be continued to make absorption agent, and another part returns lye vat and recycles.Utilize ammonia in alkali liquor absorption ammonia decontamination tower, phenol content in ammoniacal liquor is reached and is sent to flue gas desulfurization (FGD) unit phenol content's index, realize ammonia decontamination tower and run peace, steady, long, full, excellent benign cycle.
Description
Technical field
The utility model belongs to coal chemical technology.Particularly, the utility model relates to a kind of ammonia decontamination device of the phenol ammonia recovery unit for crushed coal pressure gasifying sewage treatment process.
Background technology
The basic characteristics of china natural resources are rich coal, oil-poor, weak breath, according to statistics, coal resources in China reserves can for country 200 years, wherein more maximum shared by brown coal and long-flame coal etc., account for more than 60%.Crushed coal pressure gasifying coal used scope is wider, and from the brown coal of low order to chinley coal, hard coal is all gasifiable.For brown coal, the coal for gasification that long-flame coal is more reasonable, cheap especially of poor quality, this part low-rank coal is converted into clean geseous fuel, especially on coal preparing natural gas, ammonia from coal, coal synthesis ammonia and ICL for Indirect Coal Liquefaction operational path, there is very strong competitive power, be the Coal Clean trans-utilization mode that country 12 planning proposes simultaneously, have vast potential for future development.
But, a large amount of high pollutions, high-concentration coal gasification waste water can be produced in crushed coal pressure gasifying Technology production process, water-quality constituents is extremely complicated, the pollution load of these waste water is very high, gas liquor after having removed oil, dirt from upstream is sent to biochemical treatment through the phenol ammonia recovery unit waste water reclaimed after valuable material (phenol and ammonia) and advanced treatment apparatus processes rear grading recycle further, realizes recycle.
Current phenol ammonia recovery unit generally adopts depickling, and---deamination---extracts---solvent stripping---operational path that solvent recuperation combines.
Wherein, the technical process of deamination unit: the thick ammonia of deamination overhead extraction is spent behind left and right through ammonia first-stage condenser shell side and its tube side raw material sewage heat change to 125, enter one-level and divide flow container, carry out gas-liquid separation, ammonia lime set enters ammonia lime set and divides oil tank (the ammonia lime set that rear two-stage is separated is also identical); Ammonia enters secondary and divides flow container to carry out gas-liquid separation after ammonia secondary condenser shell side and its tube side recirculated cooling water heat exchange are cooled to about 90 DEG C, and ammonia enters three fraction flow containers after ammonia three grades of condenser shell sides and its tube side recirculated cooling water heat exchange are cooled to about 45 DEG C.Three fraction flow container tops rich ammonia out about 40 DEG C enters ammonia decontamination tower purification and washing, and the ammonia lime set after oil removing does cold reflux by pumping people deammoniation tower top.The heat that ammonia is released in absorption process is taken away by middle part circulating cooling system.Tower bottoms returns raw material water tank; Scavenging tower top gaseous phase enters ammonia absorber shell side fresh water and sprays, and absorbs into 15% weak ammonia, is taken away by the recirculated cooling water of tube side at absorption process liberated heat.Weak ammonia enters weak ammonia tank, is then pumped to flue gas desulfurization (FGD) unit by weak ammonia.The ammoniacal liquor design objective being sent to flue gas desulfurization is phenol < 50mg/l, H
2s < 50mg/l, CO
2< 20mg/l.
Occur containing coal gas in this technique, wash, cool and scavenging process, the material major parts such as the tar produced therebetween, phenol, ammonia enter in gas washing wastewater.Pollutants in Wastewater complicated component, belong to the poisonous refractory organic industrial sewage of high density, its sewage disposal has become the bottleneck of crushed coal pressure gasifying technological development.
The producer of the identical phenol ammonia recovery unit of the current domestic employing problems demand that operation device has all existed phenol content overproof in weak ammonia solves.Particularly, existing phenol ammonia recovery unit Problems existing mainly comprises:
1, the phenol content operated in 1. weak ammonias produced does not reach the phenol content of design, and the index of domestic same device is also to the greatest extent identical, total phenol having from about 100mg/l to more than 1000mg/l, all causes very large impact to the operation of flue gas desulfurization (FGD) unit and the quality of product sulphur ammonium.
2. when flue gas desulfurization (FGD) unit all can not consume the ammoniacal liquor of phenol remanufacture, ammoniacal liquor can only in phenol recovery system internal recycling, the content of ammonia in raw material phenol water is caused to be accumulated, increase the weight of the load of deamination unit, the final content of ammonia in the rare phenol water of outlet that can cause again increases, and affects the normal operation of biochemical device.
3. the defective a series of environmental issues caused of weak ammonia index have become the bottleneck of crushed coal pressure gasifying technique full production.
The general method adopting ammonia decontamination tower to adopt weak ammonia absorption in prior art, phenol content overproof in ammoniacal liquor, does not reach flue gas desulfurization (FGD) unit and accepts index, have impact on the normal operation of flue gas desulfurization (FGD) unit, phenol retrieving arrangement and biochemical device.And ammonia decontamination tower of the present utility model adopts alkali liquor absorption method, greatly can reduce the content of phenol in weak ammonia and sour gas, meet the needs of flue gas desulfurization (FGD) unit.Meanwhile, existing technique ammonia decontamination tower adopts weak ammonia to absorb, the steps such as the low temperature removal of impurity, alkali cleaning, absorption, long flow path, complex process, and investment is large.And the utility model just directly adopts the method for alkali cleaning at ammonia decontamination tower, technique is simple, and flow process is short, invests little.
Ammonia decontamination tower adopts alkali liquor absorption to have the following advantages by deamination system of the present utility model:
1, after using alkali liquor absorption instead, phenol, the H in weak ammonia can greatly be reduced
2the content of S, effectively can reduce the content of phenol in weak ammonia and sour gas, ensures the normal operation of flue gas desulfurization (FGD) unit, reduces sulphur emissions.
2, the quality product of flue gas desulfurization (FGD) unit sulphur ammonium can be improved, improve product price.By quality influence, some enterprises just can not be sold at all; Some enterprises can only make a price reduction process.
3, can prevent phenol from reclaiming accumulation and the fluctuation of ammonia content in raw material phenol water, ensure that in the rare phenol water of outlet, total ammonia index is stablized, and is conducive to the steady running of biochemical device, reduces cost of sewage disposal.
4, the removal efficiency of deamination unit can be improved, increase the output being sent to the weak ammonia of flue gas desulfurization (FGD) unit, reduce outsourcing liquefied ammonia amount.
5, the steady running of phenol retrieving arrangement deamination unit, can greatly reduce the pollution that ammonia emptying produces environment.
6, ensure that the ammonia that phenol retrieving arrangement removes can be sent outside to greatest extent, be conducive to the stable of ammonia content in raw water, reduce the fluctuation of total ammonia index in the rare phenol water of outlet, ensure the steady running of biochemical device.Realize phenol retrieving arrangement peace, steady, long, full, excellent benign cycle.
Summary of the invention
For above technical problem, an object of the present utility model is to provide a kind of ammonia decontamination system for crushed coal pressure gasifying production technique.Another object of the present utility model is to provide a kind of phenol ammonia recovery unit produced for crushed coal pressure gasifying using ammonia decontamination system as previously mentioned.
In order to solve the problems of the technologies described above and realize foregoing invention object, the utility model has carried out large quantifier elimination and exploration, creatively proposes to utilize phenol, CO
2and H
2there is the character of chemical reaction in S and NaOH, is changed into by former ammonia decontamination tower absorbing by NaOH solution by ammonia absorption.Equation is:
C
6H
5OH+NaOH＝C
6H
5ONa+H
2O；
CO
2+2NaOH＝Na
2CO
3+H
2O；
H
2S+2NaOH＝Na
2S+2H
2O。
Particularly, the utility model provides following technical scheme:
On the one hand, the utility model provides a kind of ammonia decontamination system for crushed coal pressure gasifying production technique, and described ammonia decontamination system comprises:
Deammoniation tower, three grades of condensation liquid distributing devices, ammonia decontamination tower, lye vat and intercycle pipelines;
Wherein, described deammoniation tower is connected with described ammonia decontamination tower bottom with intercycle pipeline through described three grades of condensation liquid distributing devices, and described ammonia decontamination tower is communicated with described lye vat at tower top again; Described ammonia decontamination tower circulation line in the middle part of the tower bottoms part after ammonia is incorporated to returns ammonia decontamination tower to be continued to make absorption agent, and another part returns lye vat and recycles.
Preferably, according to foregoing ammonia decontamination system, described three grades of condensation liquid distributing devices comprise:
First-stage condenser, its shell side and its tube side raw material sewage heat change to 125 enter one-level and divide flow container to carry out gas-liquid separation after spending left and right;
Secondary condenser, enters secondary after its shell side and its tube side recirculated cooling water heat exchange are cooled to about 90 DEG C and divides flow container to carry out gas-liquid separation;
Three grades of condensers, enter three fraction flow containers after its shell side and its tube side recirculated cooling water heat exchange are cooled to about 45 DEG C and carry out gas-liquid separation;
Ammonia lime set after upper described one to three fraction flow container carries out gas-liquid separation enters ammonia lime set respectively and divides oil tank.
Preferably, according to foregoing ammonia decontamination system, described ammonia decontamination system also to comprise at the bottom of described lye vat to the reflux pump source line of described ammonia decontamination tower, utilizes this pump using NaOH solution as trim the top of column, in tower, adds NaOH solution continuously.
Preferably, according to foregoing ammonia decontamination system, described ammonia decontamination tower is connected with the tower reactor pump discharge pipeline of deriving described tower bottoms, increase before variable valve from described tower reactor pump discharge pipeline one go in the pipeline of SAPMAC method pump discharge, the NaOH solution of non-complete reaction in tower reactor can be recycled, retain and SAPMAC method amount in increasing simultaneously.
Preferably, according to foregoing ammonia decontamination system, described ammonia decontamination tower is connected with the tower reactor pump discharge pipeline of deriving described tower bottoms, from described tower reactor pump discharge pipeline, after variable valve, increase the pipeline of a lixiviating liquid bath, the NaOH solution of tower reactor can be sent into lye vat to keep the normal level of tower.
Preferably, according to foregoing ammonia decontamination system, described lye vat is connected with blow-down pipe, increases vacuum pressure valves, only have when described lye vat internal pressure reaches design pressure 0.2MPa, just can enter air at described blow-down pipe.Further preferably, for preventing described vacuum pressure valves from blocking, in vacuum pressure valves lower pipelines, wash-down water is increased.
Preferably, according to foregoing ammonia decontamination system, for keeping the backflow of ammonia decontamination column overhead and entering alkali concn stable of deammoniation tower, described lye vat is connected with lye dissolving tank, mends alkali by lye dissolving tank continuously to lye vat.Further preferably, for preventing lye dissolving tank pump from suppressing pump, described lye dissolving tank arranges pump return line.
On the other hand, the utility model provides a kind of phenol ammonia recovery unit produced for crushed coal pressure gasifying, and described phenol ammonia recovery unit comprises:
Deacidification system;
Foregoing ammonia decontamination system;
Extracting system;
Solvent air lift system;
Solvent recovering system.
This ammonia decontamination tower alkali liquor absorption method, is applicable to that Shandong is strange, crushed coal pressure gasifying phenol ammonia reclaiming process.
Accompanying drawing explanation
The utility model is explained below in conjunction with accompanying drawing, wherein:
Fig. 1 is the process flow sheet of deamination system described in the utility model embodiment 1;
Fig. 2 is the process flow sheet of alkali cleaning operation in deamination system described in the utility model embodiment 1;
Fig. 3 is the soda liquor absorption technique schema of ammonia decontamination tower described in the utility model embodiment 2.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is further described in detail, embodiment given below only in order to illustrate the utility model, instead of in order to limit protection domain of the present utility model.
embodiment 1
Present embodiment describes the deamination system according to a kind of specific embodiments of the present utility model and technical process thereof:
As shown in accompanying drawing 1,2, the thick ammonia that deammoniation tower C902 pushes up extraction is spent behind left and right through ammonia first-stage condenser E909 shell side and its tube side raw material sewage heat change to 125, enter one-level and divide flow container T903, carry out gas-liquid separation, ammonia lime set enters ammonia lime set and divides oil tank T906 (the ammonia lime set that rear two-stage is separated is also identical); Ammonia enters secondary and divides flow container T904 to carry out gas-liquid separation after ammonia secondary condenser E910 shell side and its tube side recirculated cooling water heat exchange are cooled to about 90 DEG C, and ammonia enters three fraction flow container T905 after ammonia three grades of condenser E911 shell sides and its tube side recirculated cooling water heat exchange are cooled to about 45 DEG C.Three fraction flow container T905 tops rich ammonia out about 40 DEG C enters ammonia decontamination tower C906 purification and washing; Ammonia lime set after oil removing is incorporated to the hot feed pipeline of extracting tower C901 by P903 pump, prevents phenol and sour gas in ammonia lime set from accumulating in three grades of fractional condensation systems, reduces the concentration of phenol in ammonia decontamination tower C906 ammonia and sour gas.
The ammonia entering ammonia decontamination tower C906 from bottom contacts with the backflow weak ammonia (from lye vat T911) of tower top is reverse, the impurity such as the H2S in removing ammonia and phenol.The heat that ammonia is released in absorption process is taken away by middle part circulating cooling system.A tower bottoms part is incorporated to middle part circulation line and returns and can continue to make absorption agent by C906 tower; A part returns lye vat and recycles.Saturated dirty alkali lye sends into raw material water tank.Scavenging tower top gaseous phase enters ammonia absorber E908 shell side fresh water and sprays, and absorbs into 15% weak ammonia, is taken away at absorption process liberated heat by the recirculated cooling water of tube side.Weak ammonia enters weak ammonia tank
T908, then delivers to flue gas desulfurization (FGD) unit by weak ammonia pump P907.
embodiment 2
Present embodiment describes the ammonia decontamination system according to another kind of specific embodiments of the present utility model and technical process thereof:
As shown in Figure 3, for reducing cost of investment, also can carry out changing (referring to accompanying drawing 2) on the equipment of embodiment 1 and pipeline basic.Concrete measure is as follows:
1, to increase at the bottom of lye vat to ammonia decontamination tower reflux pump source line (in figure material 1), utilize this pump using NaOH solution as trim the top of column, in tower, add NaOH solution continuously.
3, former middle SAPMAC method retains, and one is the washing effect increasing stage casing filler, and two is extraction heat.
4, before LV017 variable valve tower reactor pump discharge pipeline, increase the pipeline (in figure material 2) that one is removed middle SAPMAC method pump discharge, the NaOH solution of the non-complete reaction of tower reactor can be recycled, SAPMAC method amount in simultaneously increasing.
5, after LV017 variable valve tower reactor pump discharge pipeline, increase the pipeline (in figure material 3) of a lixiviating liquid bath, the NaOH solution of tower reactor can be sent into lye vat to keep the normal level of tower.
6, containing C
6h
5oNa, Na
2cO
3and Na
2send in deammoniation tower C902 through adding alkali squirt pump after mixing with the fresh NaOH solution of supplementing after the NaOH solution of S enters lye vat.
7, in deammoniation tower and follow-up three grades of segregation process, sodium phenylate can with residual CO
2phenol and sodium bicarbonate are produced in reaction.Reaction equation:
C
6H
5ONa+CO
2+H
2O—C
6H
5OH+NaHCO
3；
Na
2cO
3and Na
2s enters tower reactor phenol water.
8, C906 tower reactor NaOH solution out can dissolve more ammonia, can discharge into the atmosphere after entering lye vat T911 and affect environment, therefore increase by a vacuum pressure valves at blow-down pipe (in figure material 4), only have when T911 internal pressure reaches design pressure 0.2MPa, just can enter air.For preventing vacuum pressure valves from blocking, in vacuum pressure valves lower pipelines, increase wash-down water (in figure material 5).
9, for keeping C906 trim the top of column and entering alkali concn stable of deammoniation tower C902, alkali is mended by lye dissolving tank T913 continuously to alkali groove T911.For preventing molten alkali pump 203P906 from suppressing pump, pump return line (in figure material 6) is set.
embodiment 3
The present embodiment have detected the technique effect index adopting deamination system of the present utility model and currently available technology to have deamination system and contrasts:
The restriction point that the weak ammonia of current domestic same or analogous ammonia decontamination explained hereafter is directly used in flue gas desulfurization (FGD) unit is that the phenol content in weak ammonia is high.After using alkali liquor absorption ammonia instead, in ammoniacal liquor, phenol content can reach the index being sent to flue gas desulfurization, and what use Aspen software simulation the results are shown in Table 1.
Table 1 Aspen software simulation result
Calculate to produce 4,000,000 side's Sweet natural gases daily, phenol reclaims and produces ammoniacal liquor 20t/h, and about produce 11.64t/h sulphur ammonium, produce 9.3 ten thousand tons per year, raising per ton 100 yuan, can increase income 9,300,000 yuan year more.
Claims (9)
1. for an ammonia decontamination system for crushed coal pressure gasifying sewage treatment process, it is characterized in that, described ammonia decontamination system comprises:
Deammoniation tower, three grades of condensation liquid distributing devices, ammonia decontamination tower, lye vat and intercycle pipelines;
Wherein, described deammoniation tower is connected with described ammonia decontamination tower bottom with intercycle pipeline through described three grades of condensation liquid distributing devices, and described ammonia decontamination tower is communicated with described lye vat at tower top again; Described ammonia decontamination tower circulation line in the middle part of the tower bottoms part after ammonia is incorporated to returns ammonia decontamination tower to be continued to make absorption agent, and another part returns lye vat and recycles.
2. ammonia decontamination system according to claim 1, is characterized in that, described three grades of condensation liquid distributing devices comprise:
First-stage condenser, its shell side and its tube side raw material sewage heat change to 125 enter one-level and divide flow container to carry out gas-liquid separation after spending left and right;
Secondary condenser, enters secondary after its shell side and its tube side recirculated cooling water heat exchange are cooled to about 90 DEG C and divides flow container to carry out gas-liquid separation;
Three grades of condensers, enter three fraction flow containers after its shell side and its tube side recirculated cooling water heat exchange are cooled to about 45 DEG C and carry out gas-liquid separation;
Ammonia lime set after described one, two, three point of flow container carries out gas-liquid separation enters ammonia lime set respectively and divides oil tank.
3. ammonia decontamination system according to claim 1 and 2, is characterized in that, described ammonia decontamination system also comprises the reflux pump source line to described ammonia decontamination tower at the bottom of described lye vat.
4. ammonia decontamination system according to claim 1 and 2, it is characterized in that, described ammonia decontamination tower is connected with the tower reactor pump discharge pipeline of deriving described tower bottoms, increase before variable valve from described tower reactor pump discharge pipeline one go in the pipeline of SAPMAC method pump discharge.
5. ammonia decontamination system according to claim 1 and 2, is characterized in that, described ammonia decontamination tower is connected with the tower reactor pump discharge pipeline of deriving described tower bottoms, increases the pipeline of a lixiviating liquid bath from described tower reactor pump discharge pipeline after variable valve.
6. ammonia decontamination system according to claim 1 and 2, is characterized in that, described lye vat is connected with blow-down pipe, increases vacuum pressure valves at described blow-down pipe.
7. ammonia decontamination system according to claim 1 and 2, is characterized in that, described lye vat is connected with lye dissolving tank.
8. ammonia decontamination system according to claim 7, is characterized in that, described lye dissolving tank arranges pump return line.
9. for a phenol ammonia recovery unit for crushed coal pressure gasifying sewage disposal, it is characterized in that, described phenol ammonia recovery unit comprises:
Deacidification system;
Ammonia decontamination system according to any one of claim 1-8;
Extracting system;
Solvent air lift system;
Solvent recovering system.
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|---|---|---|---|
| CN201520205457.6U CN204727616U (en) | 2015-04-07 | 2015-04-07 | For ammonia decontamination system and the phenol ammonia recovery unit thereof of crushed coal pressure gasifying sewage treatment process |
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|---|---|---|---|
| CN201520205457.6U CN204727616U (en) | 2015-04-07 | 2015-04-07 | For ammonia decontamination system and the phenol ammonia recovery unit thereof of crushed coal pressure gasifying sewage treatment process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108249501A (en) * | 2018-03-10 | 2018-07-06 | 河南晋煤天庆煤化工有限责任公司 | A kind of lurgi gasifier gasifying smokeless device for coal coal gas water treatment system |
| CN110723771A (en) * | 2019-11-07 | 2020-01-24 | 伊犁新天煤化工有限责任公司 | Novel phenol ammonia recovery device for efficiently recovering ammonia |
-
2015
- 2015-04-07 CN CN201520205457.6U patent/CN204727616U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108249501A (en) * | 2018-03-10 | 2018-07-06 | 河南晋煤天庆煤化工有限责任公司 | A kind of lurgi gasifier gasifying smokeless device for coal coal gas water treatment system |
| CN108249501B (en) * | 2018-03-10 | 2023-09-22 | 河南晋控天庆煤化工有限责任公司 | Coal gas water treatment system of Lurgi furnace gasification anthracite device |
| CN110723771A (en) * | 2019-11-07 | 2020-01-24 | 伊犁新天煤化工有限责任公司 | Novel phenol ammonia recovery device for efficiently recovering ammonia |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20151028 |