CN103275767A - Method for separating high-temperature gas containing solid dust and tar gas - Google Patents
Method for separating high-temperature gas containing solid dust and tar gas Download PDFInfo
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- CN103275767A CN103275767A CN2013101969130A CN201310196913A CN103275767A CN 103275767 A CN103275767 A CN 103275767A CN 2013101969130 A CN2013101969130 A CN 2013101969130A CN 201310196913 A CN201310196913 A CN 201310196913A CN 103275767 A CN103275767 A CN 103275767A
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Abstract
The invention relates to a method for separating high-temperature gas containing solid dust and tar gas. An aluminum-series intermetal compound asymmetric film filtering material and the FeAl-series intermetal compound asymmetric film filtering material of Chengdu YITAI Science and Technology Co. Ltd are used to realize the gas-solid separation to obtain the gas with the solids removed, the gas with the solids removed is gradually condensed stage by stage, so that the heavy tar component, the light tar component, the moisture and non-condensable gas can be high-efficiently separated.
Description
Technical field
The present invention relates to the separation method that a kind of high temperature contains solid dust and contains the gas of tar gas; Say especially, the high temperature that the present invention relates to a kind of pulverized coal pyrolysis process generation contains solid dust and the separation method that contains the coal gas of tar, use the Al series intermetallic compound asymmetric membrane filtering material of Chengdu YiTai Science Co., Ltd to realize that such as FeAl series intermetallic compound asymmetric membrane filtering material gas solid separation obtains taking off solid gas, take off solid gas by condensation step by step, realize the high efficiency separation of heavy tar component, tar light oil component, moisture, non-condensable gas.
Background technology
A kind of separation method that contains the coal gas of tar gas is single-stage oil wash condensation method, the dust-laden coal gas chill oil washing method that comprises as the LCC of China Wuhuan Engineering Co., Ltd transformation and quality improvement of low-rank coal technology, perhaps the application number that prolongs oil (group) limited liability company hydrocarbon efficient technique of rainwater utilization research centre for Shaanxi is the method that a kind of fine coal pressurization method for pyrolysis of patent application of 201210418935 and device relate to, the pyrolysis gas that produces in the pyrolysis of coal device is through tornado dust collector, behind the degree of depth fly-ash separator, enter that quenching column upwards flows and the chill oil under overhead streams contacts, the non-condensable gas that the Quench cat head flows out enters electrostatic precipitator, pyrolysis gas cold oil under the condensation in quenching column mixes the back and discharge quenching column at the bottom of tower with chill oil, discharge at the bottom of the Quench Tata and be divided into two portions after oil cools off through interchanger: major part is returned quenching column, and small part is as the pyrolytic tar product.The advantage of this method is to use the oil wash method to replace method for washing, in the Quench process of oil wash coal gas, also control not condensation of water vapor in the time of the major part tar condensing, avoid mixing of condensed tar and chilled water, realized separating between " tar component " and " water ", the shortcoming of this method is:
1. do not indicate the technique means that realizes degree of depth gas solid separation;
2. single-stage condensation can't realize separating between " heavy tar component " and " the tar light oil component ";
3. just the coal gas high-temperature utilization efficiency of heat energy is low: because oil contains a large amount of tar light oil components and causes at the bottom of the tower bubble point temperature of fluid body lower at the bottom of the tower, reduced the energy energy level, the high-quality heat energy of first coal gas is not fully used.
In the branch matter conversion process of coal, the coal gas that the pyrolysis of coal process produces is that high temperature contains solid dust and the coal gas that contains tar gas, especially the coal gas of cyclonic separator was the coal gas of high temperature that contains a large amount of solid dusts and contain tar gas after the pulverized coal pyrolysis process went out pyrolyzer or goes out pyrolyzer, part dust granules diameter wherein is below 5 microns, service temperature is between 500～900 ℃, gas filtration is crossed range request and is leached diameter greater than 1 micron particle, with this understanding, conventional filter material efficient operation for a long time.The Al series intermetallic compound asymmetric membrane filtering material of Chengdu YiTai Science Co., Ltd is such as FeAl series intermetallic compound asymmetric membrane filtering material, have characteristics such as excellent high temperature oxidation resisting, easily sealing, processibility are good, particularly under severe rugged environments such as high temperature, the irreplaceable advantage of conventional filter material is arranged, and the purification, iron alloy high-temperature furnace gas that is applicable to the high temperature sulfurous gas purifies the gas solid separation purification in the technologies such as recovery, blast furnace, RECOVERY OF CONVERTER GAS utilization, coal conversions, calcium carbide industry, biological gas industry processed, oil shale industry.The first step of the present invention is, based on containing solid dust under high-temperature pressurizing (or normal pressure) condition, containing the coal-tar middle oil gas phase state that is in of coal gas of tar gas, use Al series intermetallic compound asymmetric membrane filtering material to leach diameter greater than 1 micron even leach diameter greater than 0.3 micron particle, obtain the coal gas of solid, this is first step of the present invention.In order to give full play to the filter core function, the unstripped gas that requires usually to enter strainer is the logistics of gas-solid mixed phase, does not wish to occur gas, oil, consolidates the three-phase logistics.
Second step of the present invention is, based on the coal-tar middle oil gas phase state that is in of coal gas that contains tar gas under high-temperature pressurizing (or normal pressure) condition, adopt secondary or multi-stage condensing mode, realize the separation between " heavy tar component, tar light oil component, water " polycomponent, and can improve the temperature of " heavy tar component " component material, for its high temperature pick up the heat creates favorable conditions.
The method of the invention is not appeared in the newspapers.
First purpose of the present invention is to propose the separation method that a kind of high temperature contains solid dust and contains the gas of tar gas.
Summary of the invention
A kind of high temperature of the present invention contains solid dust and contains the separation method of the gas of tar gas, it is characterized in that:
1. at high temperature gas-solid separate part, when containing solid dust and containing filtering surface by the strainer made by intermetallic compound asymmetric membrane filtering material of unstripped gas that the gas of tar gas constitutes by high temperature, particulate matter is blocked, and gas becomes the dust-removing gas body by filtering surface; At the filtering surface of strainer, the particulate matter that is blocked of part constitutes filter cake, breaks away from filtering surface at the regenerative process filter cake of the filtering surface of strainer, and the particulate matter of the filtering surface interception of strainer is collected as leaching solid;
2. in the first oil wash section, dust-removing gas body and the first poor washing oil mix contact after, be separated into first gas and the first rich washing oil, heavy tar component at least a portion dust-removing gas body enters the first rich washing oil, and the heavy tar component concentration in first gas is lower than the heavy tar component concentration of dust-removing gas body;
The first rich washing oil is divided into two-way, after the first via first rich washing oil passes through the step that cools, recycles as the first poor washing oil, and the second tunnel first rich washing oil is as the first oil wash section cold oil product.
In order to reclaim the tar component that is mainly middle runnings in first gas, feature of the present invention further is:
3. in the second oil wash section, first gas and the second poor washing oil mix contact after, be separated into second gas and the second rich washing oil, the tar component at least a portion first gas enters the second rich washing oil, and the tar content in second gas is lower than the tar content in first gas; The second oil wash section average operation temperature is lower than the first oil wash section average operation temperature; The average conventional boiling point of the second poor washing oil is less than the average conventional boiling point of the first poor washing oil;
The second rich washing oil is divided into two-way, after the first via second rich washing oil passes through the step that cools, recycles as the second poor washing oil, and the second tunnel second rich washing oil is as the second oil wash section cold oil product.
In order to realize the dehydration of coal gas, feature of the present invention further is:
4. in dehydrating step, the cooling of second gas cooling makes most of water condensation form gas, oil, water three-phase mixture A, and mixture A finishes gas, oil, water three phase separation, obtains branch water step and discharges gas, divides the water step to discharge oil, divides the drainage water of water step.
In order further to fall the tar content in the branch water step discharge gas, feature of the present invention further is:
5. in the 3rd oil wash section, after dividing the water step to discharge gas and the lean absorption oil mixing contacts, be separated into the 3rd gas and rich absorbent oil, the tar component that at least a portion divides the water step to discharge in the gas enters in the rich absorbent oil, and the tar content in the 3rd gas is lower than the tar content that branch water step is discharged gas; Rich absorbent oil enters separation column and is separated into oil and separation column top distilled oil at the bottom of the separation column, and oil recycles as lean absorption oil after passing through the step that cools at the bottom of at least a portion separation column.
When the further processing first rich washing oil, feature of the present invention further is: at least a portion first rich washing oil enters coking makes bituminous matter and colloid generation pyrogenic reaction produce coke, most of dust in the coking raw material oil enters in the coke, reclaims the oil gas that coking is discharged.Handle the coking of the first rich washing oil, can adopt fluidized coking process or delay coking process.
The present invention's first oil wash section operational condition is generally: 1. at high temperature gas-solid separate part, remove diameter in the unstripped gas greater than 1 micron solid particulate; 2. the first oil wash section operational condition is: temperature is that 200～430 ℃, pressure are a little less than the unstripped gas working pressure; The first rich washing oil mainly is higher than 450 ℃ fractions consisting by conventional boiling point.
The present invention's second oil wash section operational condition is generally: 3. the second oil wash section operational condition is: temperature is that 70～320 ℃, pressure are a little less than the pyrolyzer working pressure; The second rich washing oil mainly is 200～450 ℃ fractions consisting by conventional boiling point.
When the second oil wash section can obtain 2 or a plurality of cold oil product, feature of the present invention further is: 3. the second oil wash section comprises two oil wash steps at least, the progressively condensation of tar component in first gas, each oil wash step obtains cold oil product separately respectively.
Divide water step operational condition to be generally: 4. the dehydrating step operational condition is: temperature is that 10～50 ℃, pressure are a little less than the unstripped gas working pressure.
Be generally in the 3rd oil wash section operational condition: 5. the 3rd oil wash section operational condition is: temperature is 10～50 ℃, pressure is a little less than the pyrolyzer working pressure, the lean absorption oil mass rate is 4～500 with the ratio that minute water step is discharged carbon six above hydrocarbon constituent mass flows in the gas, and lean absorption oil is that 180～380 ℃ hydrocarbon is formed by conventional boiling range mainly.
The temperature range of the unstripped gas of the present invention's processing is generally 350～950 ℃.
The unstripped gas of the present invention's processing can be produced by pulverized coal pyrolysis, and its temperature is 450～750 ℃.
The unstripped gas of the present invention processing can by in the fine coal, low temperature pyrogenation produced, its temperature is 500～700 ℃.
The working pressure of the unstripped gas that the present invention handles is generally 0～4.0MPa, is generally 0.1～2.0MPa without limits.
In order to strengthen the first oil wash section washing effect, feature of the present invention further is: 2. the first oil wash section adopts tray column or packing tower, at the first oil wash pars infrasegmentalis stage casing that increases the washing oil mass is set and circulates, stage casing turning oil is extracted the back out and is returned an extraction mouthful upper position without heat exchange step in tower.
In order to strengthen the second oil wash section washing effect, feature of the present invention further is: 3. the second oil wash section adopts tray column or packing tower, at the second oil wash pars infrasegmentalis stage casing that increases the washing oil mass is set and circulates, stage casing turning oil is extracted the back out and is returned an extraction mouthful upper position without heat exchange step in tower.
In order to strengthen the 3rd oil wash section washing effect, feature of the present invention further is: 5. the 3rd oil wash section adopts tray column or packing tower, at the 3rd oil wash section middle part the stage casing that increases the washing oil mass is set and circulates, return after stage casing turning oil is extracted out in tower and extract a mouthful upper position out.
Feature of the present invention further is: 3. do not contain free-water in the second rich washing oil.
The present invention is particularly suitable for high temperature, contain solid dust, contain the sepn process of the coal gas of tar gas.
Feature of the present invention further is: 3. do not contain free-water in the second rich washing oil.
The present invention handles contains solid dust, contain the gas of tar gas, its dust content be in this gas coal tar weight 0～30% or higher, most of dust granules diameter: be generally less than 100 microns, usually less than 50 microns.
The present invention handles contains solid dust, contain the gas of tar gas, its tar component content for the coal feed weight that produces this coal gas 0～20% or higher.
The present invention can arrange filtration step to remove solid particulate to the first rich washing oil or the first via first rich washing oil or the second tunnel first rich washing oil.
Embodiment
Below describe the present invention in detail.
Pressure of the present invention refers to absolute pressure.
A kind of high temperature of the present invention contains solid dust and contains the separation method of the gas of tar gas, it is characterized in that:
1. at high temperature gas-solid separate part, when containing solid dust and containing filtering surface by the strainer made by intermetallic compound asymmetric membrane filtering material of unstripped gas that the gas of tar gas constitutes by high temperature, particulate matter is blocked, and gas becomes the dust-removing gas body by filtering surface; At the filtering surface of strainer, the particulate matter that is blocked of part constitutes filter cake, breaks away from filtering surface at the regenerative process filter cake of the filtering surface of strainer, and the particulate matter of the filtering surface interception of strainer is collected as leaching solid;
2. in the first oil wash section, dust-removing gas body and the first poor washing oil mix contact after, be separated into first gas and the first rich washing oil, heavy tar component at least a portion dust-removing gas body enters the first rich washing oil, and the heavy tar component concentration in first gas is lower than the heavy tar component concentration of dust-removing gas body;
The first rich washing oil is divided into two-way, after the first via first rich washing oil passes through the step that cools, recycles as the first poor washing oil, and the second tunnel first rich washing oil is as the first oil wash section cold oil product.
In order to reclaim the tar component that is mainly middle runnings in first gas, feature of the present invention further is:
3. in the second oil wash section, first gas and the second poor washing oil mix contact after, be separated into second gas and the second rich washing oil, the tar component at least a portion first gas enters the second rich washing oil, and the tar content in second gas is lower than the tar content in first gas; The second oil wash section average operation temperature is lower than the first oil wash section average operation temperature; The average conventional boiling point of the second poor washing oil is less than the average conventional boiling point of the first poor washing oil;
The second rich washing oil is divided into two-way, after the first via second rich washing oil passes through the step that cools, recycles as the second poor washing oil, and the second tunnel second rich washing oil is as the second oil wash section cold oil product.
In order to realize the dehydration of coal gas, feature of the present invention further is:
4. in dehydrating step, the cooling of second gas cooling makes most of water condensation form gas, oil, water three-phase mixture A, and mixture A finishes gas, oil, water three phase separation, obtains branch water step and discharges gas, divides the water step to discharge oil, divides the drainage water of water step.
In order further to fall the tar content in the branch water step discharge gas, feature of the present invention further is:
5. in the 3rd oil wash section, after dividing the water step to discharge gas and the lean absorption oil mixing contacts, be separated into the 3rd gas and rich absorbent oil, the tar component that at least a portion divides the water step to discharge in the gas enters in the rich absorbent oil, and the tar content in the 3rd gas is lower than the tar content that branch water step is discharged gas; Rich absorbent oil enters separation column and is separated into oil and separation column top distilled oil at the bottom of the separation column, and oil recycles as lean absorption oil after passing through the step that cools at the bottom of at least a portion separation column.
When the further processing first rich washing oil, feature of the present invention further is: at least a portion first rich washing oil enters coking makes bituminous matter and colloid generation pyrogenic reaction produce coke, most of dust in the coking raw material oil enters in the coke, reclaims the oil gas that coking is discharged.Handle the coking of the first rich washing oil, can adopt fluidized coking process or delay coking process.
The present invention's first oil wash section operational condition is generally: 1. at high temperature gas-solid separate part, remove diameter in the unstripped gas greater than 1 micron solid particulate; 2. the first oil wash section operational condition is: temperature is that 200～430 ℃, pressure are a little less than the unstripped gas working pressure; The first rich washing oil mainly is higher than 450 ℃ fractions consisting by conventional boiling point.
The present invention's second oil wash section operational condition is generally: 3. the second oil wash section operational condition is: temperature is that 70～320 ℃, pressure are a little less than the pyrolyzer working pressure; The second rich washing oil mainly is 200～450 ℃ fractions consisting by conventional boiling point.
When the second oil wash section can obtain 2 or a plurality of cold oil product, feature of the present invention further is: 3. the second oil wash section comprises two oil wash steps at least, the progressively condensation of tar component in first gas, each oil wash step obtains cold oil product separately respectively.
Divide water step operational condition to be generally: 4. the dehydrating step operational condition is: temperature is that 10～50 ℃, pressure are a little less than the unstripped gas working pressure.
Be generally in the 3rd oil wash section operational condition: 5. the 3rd oil wash section operational condition is: temperature is 10～50 ℃, pressure is a little less than the pyrolyzer working pressure, the lean absorption oil mass rate is 4～500 with the ratio that minute water step is discharged carbon six above hydrocarbon constituent mass flows in the gas, and lean absorption oil is that 180～380 ℃ hydrocarbon is formed by conventional boiling range mainly.
The temperature range of the unstripped gas of the present invention's processing is generally 350～950 ℃.
The unstripped gas of the present invention's processing can be produced by pulverized coal pyrolysis, and its temperature is 450～750 ℃.
The unstripped gas of the present invention processing can by in the fine coal, low temperature pyrogenation produced, its temperature is 500～700 ℃.
The working pressure of the unstripped gas that the present invention handles is generally 0～4.0MPa, is generally 0.1～2.0MPa without limits.
In order to strengthen the first oil wash section washing effect, feature of the present invention further is: 2. the first oil wash section adopts tray column or packing tower, at the first oil wash pars infrasegmentalis stage casing that increases the washing oil mass is set and circulates, stage casing turning oil is extracted the back out and is returned an extraction mouthful upper position without heat exchange step in tower.
In order to strengthen the second oil wash section washing effect, feature of the present invention further is: 3. the second oil wash section adopts tray column or packing tower, at the second oil wash pars infrasegmentalis stage casing that increases the washing oil mass is set and circulates, stage casing turning oil is extracted the back out and is returned an extraction mouthful upper position without heat exchange step in tower.
In order to strengthen the 3rd oil wash section washing effect, feature of the present invention further is: 5. the 3rd oil wash section adopts tray column or packing tower, at the 3rd oil wash section middle part the stage casing that increases the washing oil mass is set and circulates, return after stage casing turning oil is extracted out in tower and extract a mouthful upper position out.
Feature of the present invention further is: 3. do not contain free-water in the second rich washing oil.
The present invention is particularly suitable for high temperature, contain solid dust, contain the sepn process of the coal gas of tar gas.
Feature of the present invention further is: 3. do not contain free-water in the second rich washing oil.
The present invention handles contains solid dust, contain the gas of tar gas, its dust content be in this gas coal tar weight 0～30% or higher, most of dust granules diameter: be generally less than 100 microns, usually less than 50 microns.
The present invention handles contains solid dust, contain the gas of tar gas, its tar component content for the coal feed weight that produces this coal gas 0～20% or higher.
The present invention can arrange filtration step to remove solid particulate to the first rich washing oil or the first via first rich washing oil or the second tunnel first rich washing oil.
For the sepn process of pulverized coal pyrolysis coal gas, compare with cold oil single-stage washing condensation method, the present invention changes first wash into two sections or multistage washing step, produces following effect:
1. the first step condensation process condensation coal tar heavy duty component only realizes the relative separation between " coal tar heavy duty component " and " coal tar light constituent ", and dust only mixes with the coal tar heavy duty component;
The first step condensation process forms the deep fat washing process, reclaims a large amount of heats of coal gas process of cooling, and the high potential temperature heat energy energy level height of recovery is such as being used for taking place medium pressure steam; By changing first poor washing oil flow and the temperature, can control the tar condensing amount flexibly, control washing oil initial boiling point;
The first step condensation process, adopt hot oiling, so the washing oil flow is big, viscosity is little, wash result is scattered in a large amount of washing oils dust, do not influence its flowability, in washing oil recycle step, can use filter method or distillation separation method or coking method to remove solid particulate in the part washing oil and recycle wherein tar;
2. in the second step condensation process, take off solid particulate coal gas and adopt the oil wash method to replace water directly to cool off, realize the relative separation of " coal tar middle runnings " and " coal tar light constituent, moisture "; And can control the condensation ratio flexibly;
3. be the condensation process of water in the 3rd step condensation process, realize the relative separation of " coal tar lighting end " and " moisture "; Water does not contain coal-tar pitch substantially, and it is further utilized or processing, has created condition;
4. in the 4th step condensation process, adopt the intermediate oil washing methods, reduce the coal-tar middle oil light constituent content of coal gas, both increased the tar rate of recovery, reduced the detarred burden of follow-up gas purification process again.
Reference examples
Certain pulverized coal pyrolysis process, the pyrolyzer material enters the gas solid separation jar, the gas solid separation jar is discharged gas and is removed particle greater than 150 microns particle through primary cyclone, primary cyclone is discharged gas and is removed particle greater than 40 microns particle through secondary cyclone, secondary cyclone is discharged granularity that gas contains and is mainly particle diameter less than 40 microns particle, and secondary cyclone is discharged gas and is unstripped gas of the present invention.
Unstripped gas of the present invention is made up of dust, tar component, water, conventional gas.Conventional gas refers under normal temperature, the normal pressure for the material of gaseous state, as H
2, CO, CO
2, N
2, H
2S, NH
3, C
1Hydrocarbon is to C
4Hydrocarbon, O
2Deng.Impurity composition refers to sulfur component, nitrogen component etc.
Unstripped gas temperature of the present invention is that 550 ℃, pressure are 0.15MPaA, contains tar component 10t/h, and dust quantity is that 5% of tar content is 0.5t/h, and the water number amount is 12.511t/h, conventional gas quantity be 25000 standard cubic meter/time, form and see Table 1-1.
According to cold oil single-stage washing condensation method, the oil wash section adopts tower washer, use 20 blocks of column plates, be that the temperature of 121.533t/h is 90 ℃ poor washing oil counter current contact from the tower bottom unstripped gas that enters washer and the flow that enters washer from top of tower, the tar condensing of 8.467t/h in the coal gas has entered in the rich washing oil, and the above dust of 90% in the coal gas has entered in the rich washing oil; Temperature is that 256 ℃ rich washing oil is discharged from the washer bottom, the process strainer removes the dust more than 20 microns, the rich washing oil that takes off behind the dirt is divided into two-way, the rich washing oil of the first via recycles as poor washing oil after being cooled to 90 ℃ of heat energy of emitting about 10.3MMkcal/h, and the second tunnel richness washing oil is recovered as cold oil.
Clearly, the tar of about 85% in the unstripped gas is mixed into a logistics, becomes little dust-laden tar products after filtering.
Rich washing oil removes dust through strainer, after the dust accumulation causes concentration to increase, cleans with outside oil product displacement.
The coal-tar middle oil character of dust-laden tar products sees Table 1-2.
Table 1-1 reference examples non-condensable gas is formed
| Component | Form v% |
| H 2 | 21.31％ |
| N 2 | 4.36％ |
| CH 4 | 23.82％ |
| C 2H 4 | 1.49％ |
| C 2H 6 | 0.79％ |
| C 3H 6 | 1.71％ |
| C 3H 8 | 2.40％ |
| CO | 13.71％ |
| CO 2 | 29.60％ |
| H 2O | 0.00％ |
| H 2S | 0.00％ |
| COS | 0.00％ |
| O 2 | 0.51％ |
| CS 2 | 0.00％ |
| Impurity composition | 0.30％ |
| Add up to | 100.00％ |
Table 1-2 reference examples cold oil rerum natura
| Project | Data |
| SPGR | 1.0086 |
| ASTM?D86?at?760mm?Hg | ? |
| ? | ? |
| 1?LV?Percent | 258.64 |
| 5 | 279.08 |
| 10 | 294.30 |
| 30 | 345.65 |
| 50 | 390.84 |
| 70 | 466.32 |
| 90 | 657.92 |
| 95 | 696.67 |
| 98?LV?Percent | 723.89 |
The coal-tar middle oil component rerum natura of coal gas behind the table 1-3 reference examples oil wash
| Project | Data |
| SPGR | 0.8837 |
| ASTM?D86?at?760mm?Hg | ? |
| ? | ? |
| 1?LV?Percent | 149.38 |
| 5 | 156.23 |
| 10 | 159.77 |
| 30 | 175.09 |
| 50 | 192.93 |
| 70 | 211.33 |
| 90 | 246.05 |
| 95 | 255.92 |
| 98?LV?Percent | 267.10 |
Table 1-4 reference examples tar distributes
| ? | Logistics | Flow, kg/h | Ratio, w% |
| 1 | Oil wash section cold oil | 8478 | 84.8％ |
| 2 | Cat head coal gas is coal-tar middle oil | 1522 | 15.2％ |
| ? | Add up to | 10000 | 100.0％ |
Embodiment
The same reference examples of unstripped gas adopts the inventive method to separate, and each step operating parameters is as follows:
1. at high temperature gas-solid separate part, when unstripped gas passed through by the filtering surface of the strainer of intermetallic compound asymmetric membrane filtering material making, diameter was blocked greater than 1 micron particulate matter, and gas becomes the dust-removing gas body by filtering surface; At the filtering surface of strainer, the particulate matter that is blocked of part constitutes filter cake, breaks away from filtering surface in the regenerative process of the filtering surface of strainer, and the particulate matter of the filtering surface interception of strainer is collected as leaching solid; The Al series intermetallic compound asymmetric membrane filtering material FeAl series intermetallic compound asymmetric membrane strainer tube filter core that described intermetallic compound asymmetric membrane filtering material is Chengdu YiTai Science Co., Ltd, have excellent high temperature resistant, characteristic such as easily sealing, processibility are good;
2. in the first oil wash section, adopt tower washer, use 10 blocks of column plates, be that the temperature of 348.153t/h is 330 ℃ the first poor washing oil counter current contact from tower bottom the dust-removing gas body that enters washer and the flow that enters washer from top of tower, the tar heavy constituent condensation of 1.522t/h in the coal gas has entered in the first rich washing oil, and the dust more than 90% in the dust-removing gas body has entered in the first rich washing oil; Temperature is that 356 ℃ the first rich washing oil is discharged from the washer bottom, the first rich washing oil is divided into two-way, the first via first rich washing oil is emitted and is cooled to 330 ℃ behind about 5.61MMkcal/h and recycles as the first via first poor washing oil, and the second tunnel first rich washing oil is recovered as the first oil wash section cold oil.
Clearly, the coke tar refuse oil ingredient that accounts for tar total amount 15% in the dust-removing gas body is separated, and becomes little dust-laden tar products.
The first rich washing oil after the dust accumulation causes concentration to increase, cleans with the displacement of the second oil wash section condensation wet goods oil product;
3. in the second oil wash section, divide three to go on foot condensation step by step, do not contain free-water in the second rich washing oil:
The first step, in two sections one-level washing zones, adopt tower washer, use 10 blocks of column plates, be that the temperature of 185.260t/h is 250 ℃ the poor washing oil counter current contact of two sections one-levels from tower bottom first gas that enters washer and the flow that enters washer from top of tower, the tar wax oil components condense of 2.193t/h in the coal gas has entered in the rich washing oil of two sections one-levels, and the dust in first gas has entered in the rich washing oil of two sections one-levels; Temperature is that the rich washing oil of two sections one-levels of 268 ℃ is discharged from the washer bottom, the process strainer removes the dust more than 20 microns, the rich washing oils of two sections one-levels that take off behind the dirt are divided into two-way, the rich washing oil of two sections one-levels of the first via is emitted and is cooled to 250 ℃ behind about 1.90MMkcal/h and recycles as two sections poor washing oils of one-level of the first via, and the second tunnel two section one-level richness washing oil is recovered as two sections one-level oil wash section cold oils.Clearly, the tar wax slop component that accounts for tar total amount 22% in the unstripped gas is separated, and becomes little dust-laden tar products after filtering;
Second step, in two sections secondary washing zones, adopt tower washer, use 10 blocks of column plates, it is that the temperature of 151.097t/h is 210 ℃ the poor washing oil counter current contact of two sections secondarys that two sections one-levels that enter washer from tower bottom are discharged gas and the flow that enters washer from top of tower, and the tar diesel component condensation of the 1.196t/h in the coal gas has entered in the rich washing oils of two sections secondarys; Temperature is that the rich washing oil of two sections secondarys of 221 ℃ is divided into two-way from the discharge of washer bottom, the rich washing oil of two sections secondarys of the first via is emitted and is cooled to 210 ℃ behind about 0.883MMkcal/h and recycles as two sections poor washing oils of secondary of the first via, and the second tunnel two section secondary richness washing oil is recovered as two sections secondary oil wash section cold oils.Clearly, the tar light wax oil component of about 12.0% in the unstripped gas is separated.
The 3rd step, in two sections three grades washing zones, adopt tower washer, use 10 blocks of column plates, it is that the temperature of 66.003t/h is two sections three grades of poor washing oil counter current contact of 90 ℃ that two sections secondarys that enter washer from tower bottom are discharged gas and the flow that enters washer from top of tower, and the tar gasoline component condensation of the 3.648t/h in the coal gas has entered in two sections three grades of rich washing oils; Temperature is that two sections three grades of rich washing oils of 161 ℃ are divided into two-way from the discharge of washer bottom, two sections three grades of rich washing oils of the first via are emitted and are cooled to 90 ℃ behind about 2.264MMkcal/h and recycle as two sections three grades of poor washing oils of the first via, the second tunnel two section three grades of rich washing oil is recovered as two sections three grades oil wash section cold oils, and the tar diesel component of about 36.5% in the unstripped gas is separated.
4. in dehydrating step, divide two to go on foot condensation step by step:
At the one-level dewatering period, second gas cooling is cooled to 40 ℃, make most of water condensation form gas, oil, water three-phase mixture A, mixture A finishes gas, oil, water three phase separation, obtains first fen water step and discharges the first fen water step discharge oil of gas, 0.875t/h, first fen water step drainage water of 11.451t/h.
At the secondary dewatering period, first fen water step discharged air cooling and but is cooled to 20 ℃, the profit condensation forms gas, oil, water three-phase mixture B, mixture B finishes gas, oil, water three phase separation, obtains second fen water step and discharges the second fen water step discharge oil of gas, 0.136t/h, second fen water step drainage water of 0.685t/h;
5. in the 3rd oil wash section, after the lean absorption oil mixing of branch water step discharge gas and 110.220t/h contacts, be separated into the 3rd gas and rich absorbent oil, the tar component of 0.449t/h enters in the rich absorbent oil; The 3rd oil wash section average operation temperature is 20 ℃; Lean absorption oil is that 218～400 ℃ hydrocarbon is formed by conventional boiling range mainly; Rich absorbent oil enters separation column and is separated into oil and separation column top distilled oil at the bottom of the separation column, and oil recycles as lean absorption oil after passing through the step that cools at the bottom of at least a portion separation column.
The coal-tar middle oil content of the 3rd gas is 0.011t/h, amounts to 0.445 gram/standard cubic meter.
The ratio of discharging carbon six above hydrocarbon constituent mass flows in the gas in the 3rd oil wash section lean absorption oil mass rate and minute water step is 239.6.
In the present embodiment, the first oil wash section and the second oil wash section can be combined as Yi Taita, the condensation process coal-tar middle oil for coal gas, and this tower becomes the multi-stage condensing tower, has possessed the partial function of separation column.
Table 2-1 has listed cold oil rerum naturas at different levels to showing 2-6.
Table 2-7 has listed the 3rd oil wash section washing oil rerum natura.
Table 2-8 has listed the coal-tar middle oil component rerum natura of the 3rd gas.
Table 2-9 has listed material balance.
The circulation cleaning oil cooling thermal load of the table 2-10 first oil wash section and the second oil wash section.
The table 2-1 first oil wash section cold oil rerum natura
| Project | Data |
| SPGR | 1.1149 |
| ASTM?D86?at?760mm?Hg，℃ | ? |
| ? | ? |
| 1?LV?Percent | 374.59 |
| 5 | 480.62 |
| 10 | 517.13 |
| 30 | 551.94 |
| 50 | 631.21 |
| 70 | 734.94 |
| 90 | ? |
| 95 | ? |
| 98?LV?Percent | ? |
Two sections one-levels of table 2-2 are washed regional cold oil rerum natura
| Project | Data |
| SPGR | 1.0335 |
| ASTM?D86?at?760mm?Hg，℃ | ? |
| ? | ? |
| 1?LV?Percent | 315.10 |
| 5 | 384.12 |
| 10 | 408.76 |
| 30 | 440.00 |
| 50 | 469.12 |
| 70 | 495.81 |
| 90 | 520.35 |
| 95 | 529.86 |
| 98?LV?Percent | 539.45 |
Two sections secondarys of table 2-3 wash regional cold oil rerum natura
| Project | Data |
| SPGR | 1.0006 |
| ASTM?D86?at?760mm?Hg，℃ | ? |
| ? | ? |
| 1?LV?Percent | 272.61 |
| 5 | 334.48 |
| 10 | 362.87 |
| 30 | 384.62 |
| 50 | 396.94 |
| 70 | 412.99 |
| 90 | 444.87 |
| 95 | 455.86 |
| 98?LV?Percent | 468.38 |
Two sections three grades regional cold oil rerum naturas of washing of table 2-4
| Project | Data |
| SPGR | 0.9526 |
| ASTM?D86?at?760mm?Hg，℃ | ? |
| ? | ? |
| 1?LV?Percent | 217.77 |
| 5 | 243.74 |
| 10 | 259.02 |
| 30 | 283.68 |
| 50 | 307.31 |
| 70 | 338.21 |
| 90 | 377.71 |
| 95 | 386.36 |
| 98?LV?Percent | 396.92 |
Table 2-5 one-level dewatering period cold oil rerum natura
| Project | Data |
| SPGR | 0.8926 |
| ASTM?D86?at?760mm?Hg，℃ | ? |
| ? | ? |
| 1?LV?Percent | 60.06 |
| 5 | 160.04 |
| 10 | 177.40 |
| 30 | 194.68 |
| 50 | 209.49 |
| 70 | 226.12 |
| 90 | 254.13 |
| 95 | 263.20 |
| 98?LV?Percent | 273.77 |
Table 2-6 secondary dewatering period cold oil rerum natura
| Project | Data |
| SPGR | 0.8708 |
| ASTM?D86?at?760mm?Hg，℃ | ? |
| ? | ? |
| 1?LV?Percent | -107.10 |
| 5 | 142.68 |
| 10 | 156.52 |
| 30 | 166.25 |
| 50 | 175.57 |
| 70 | 186.70 |
| 90 | 205.87 |
| 95 | 213.47 |
| 98?LV?Percent | 222.13 |
Table 2-7 the 3rd oil wash section washing oil rerum natura
| Project | Data |
| SPGR | 0.9526 |
| ASTM?D86?at?760mm?Hg，℃ | ? |
| ? | ? |
| 1?LV?Percent | 217.77 |
| 5 | 243.74 |
| 10 | 259.02 |
| 30 | 283.68 |
| 50 | 307.31 |
| 70 | 338.21 |
| 90 | 377.71 |
| 95 | 386.36 |
| 98?LV?Percent | 396.92 |
The coal-tar middle oil component rerum natura of table 2-8 the 3rd gas
| Project | Data |
| Tar content, milligram/standard cubic meter | 445 |
Table 2-9 material balance
The circulation cleaning oil cooling thermal load of the table 2-10 first oil wash section and the second oil wash section
| Sequence number | Heat source position | MMkcal/h | Remarks |
| 1 | The heat release of first oil wash section circulation cleaning oil | 5.614 | ? |
| 2 | The heat release of two sections one-level circulation cleaning oil | 1.900 | ? |
| 3 | The heat release of two sections secondary circulation cleaning oil | 0.883 | ? |
| 4 | The heat release of two sections three grades of circulation cleanings oil | 2.264 | ? |
| ? | ? | ? | ? |
| ? | Add up to | 10.661 | ? |
Claims (19)
1. a high temperature contains solid dust and the separation method that contains the gas of tar gas, it is characterized in that:
1. at high temperature gas-solid separate part, when containing solid dust and containing filtering surface by the strainer made by intermetallic compound asymmetric membrane filtering material of unstripped gas that the gas of tar gas constitutes by high temperature, particulate matter is blocked, and gas becomes the dust-removing gas body by filtering surface; At the filtering surface of strainer, the particulate matter that is blocked of part constitutes filter cake, breaks away from filtering surface at the regenerative process filter cake of the filtering surface of strainer, and the particulate matter of the filtering surface interception of strainer is collected as leaching solid;
2. in the first oil wash section, dust-removing gas body and the first poor washing oil mix contact after, be separated into first gas and the first rich washing oil, heavy tar component at least a portion dust-removing gas body enters the first rich washing oil, and the heavy tar component concentration in first gas is lower than the heavy tar component concentration of dust-removing gas body;
The first rich washing oil is divided into two-way, after the first via first rich washing oil passes through the step that cools, recycles as the first poor washing oil, and the second tunnel first rich washing oil is as the first oil wash section cold oil product.
2. method according to claim 1 is characterized in that:
3. in the second oil wash section, first gas and the second poor washing oil mix contact after, be separated into second gas and the second rich washing oil, the tar component at least a portion first gas enters the second rich washing oil, and the tar content in second gas is lower than the tar content in first gas; The second oil wash section average operation temperature is lower than the first oil wash section average operation temperature; The average conventional boiling point of the second poor washing oil is less than the average conventional boiling point of the first poor washing oil;
The second rich washing oil is divided into two-way, after the first via second rich washing oil passes through the step that cools, recycles as the second poor washing oil, and the second tunnel second rich washing oil is as the second oil wash section cold oil product.
3. method according to claim 2 is characterized in that:
4. in dehydrating step, the cooling of second gas cooling makes most of water condensation form gas, oil, water three-phase mixture A, and mixture A finishes gas, oil, water three phase separation, obtains branch water step and discharges gas, divides the water step to discharge oil, divides the drainage water of water step.
4. method according to claim 3 is characterized in that:
5. in the 3rd oil wash section, after dividing the water step to discharge gas and the lean absorption oil mixing contacts, be separated into the 3rd gas and rich absorbent oil, the tar component that at least a portion divides the water step to discharge in the gas enters in the rich absorbent oil, and the tar content in the 3rd gas is lower than the tar content that branch water step is discharged gas; Rich absorbent oil enters separation column and is separated into oil and separation column top distilled oil at the bottom of the separation column, and oil recycles as lean absorption oil after passing through the step that cools at the bottom of at least a portion separation column.
5. method according to claim 1 is characterized in that:
At least a portion first rich washing oil enters coking makes bituminous matter and colloid generation pyrogenic reaction produce coke, and the most of dust in the coking raw material oil enters in the coke, reclaims the oil gas that coking is discharged.
6. method according to claim 5 is characterized in that:
Handle the coking of the first rich washing oil, adopt fluidized coking process or delay coking process.
7. according to claim 1 or 2 or 3 or 4 or 5 described methods, it is characterized in that:
1. at high temperature gas-solid separate part, remove diameter in the unstripped gas greater than 1 micron solid particulate;
2. the first oil wash section operational condition is: temperature is that 200～430 ℃, pressure are a little less than the unstripped gas working pressure; The first rich washing oil mainly is higher than 450 ℃ fractions consisting by conventional boiling point.
8. according to claim 2 or 3 or 4 described methods, it is characterized in that:
3. the second oil wash section operational condition is: temperature is that 70～320 ℃, pressure are a little less than the pyrolyzer working pressure; The second rich washing oil mainly is 200～450 ℃ fractions consisting by conventional boiling point.
9. according to claim 2 or 3 or 4 described methods, it is characterized in that:
3. the second oil wash section comprises two oil wash steps at least, progressively condensation of the tar component in first gas, and each oil wash step obtains cold oil product separately respectively.
10. according to claim 3 or 4 described methods, it is characterized in that:
4. the dehydrating step operational condition is: temperature is that 10～50 ℃, pressure are a little less than the unstripped gas working pressure.
11. method according to claim 4 is characterized in that:
5. the 3rd oil wash section operational condition is: temperature is 10～50 ℃, pressure is a little less than the pyrolyzer working pressure, the lean absorption oil mass rate is 4～500 with the ratio that minute water step is discharged carbon six above hydrocarbon constituent mass flows in the gas, and lean absorption oil is that 180～380 ℃ hydrocarbon is formed by conventional boiling range mainly.
12. according to claim 1 or 2 or 3 or 4 or 5 described methods, it is characterized in that: 1. the temperature of unstripped gas is 100～950 ℃.
13. method according to claim 12 is characterized in that: 1. unstripped gas is produced by pulverized coal pyrolysis, its temperature is 100～750 ℃.
14. method according to claim 12 is characterized in that: 1. unstripped gas by in the fine coal, low temperature pyrogenation produced, its temperature is 400～650 ℃.
15. method according to claim 12 is characterized in that: 1. the working pressure of unstripped gas is 0.01～5.0MPa.
16. method according to claim 1, it is characterized in that: 2. the first oil wash section adopts tray column or packing tower, at the first oil wash pars infrasegmentalis stage casing that increases the washing oil mass is set and circulates, stage casing turning oil is extracted the back out and is returned an extraction mouthful upper position without heat exchange step in tower.
17. method according to claim 2, it is characterized in that: 3. the second oil wash section adopts tray column or packing tower, at the second oil wash pars infrasegmentalis stage casing that increases the washing oil mass is set and circulates, stage casing turning oil is extracted the back out and is returned an extraction mouthful upper position without heat exchange step in tower.
18. method according to claim 4 is characterized in that: 5. the 3rd oil wash section adopts tray column or packing tower, and arranging at the 3rd oil wash section middle part increases the circulation of the stage casing of washing oil mass, returns after stage casing turning oil is extracted out in tower and extracts a mouthful upper position out.
19. method according to claim 2 is characterized in that: 3. do not contain free-water in the second rich washing oil.
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| CN105779021A (en) * | 2016-03-10 | 2016-07-20 | 王平山 | Method for recovering energy of gas in coking riser and separating coal tar in gas |
| CN106007284A (en) * | 2016-05-04 | 2016-10-12 | 杰瑞环保科技有限公司 | Oil-containing-waste deep treatment method and system |
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