CN104031692B - The device and method of a kind of coking raw gas high temperature direct chilling reparation technology heat medium water - Google Patents
The device and method of a kind of coking raw gas high temperature direct chilling reparation technology heat medium water Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
A device and method for coking raw gas high temperature direct chilling reparation technology heat medium water, this device comprises effuser, mechanical settling tank A, mechanical settling tank B, water-and-oil separator, tar storage tank, remained ammonia groove, ammonia still, ammonia still feed exchanger, coal gas pre-cooler, hot water lithium bromide unit cooler, two sections of horizontal water-tube primary coolers.When producing, by setting up distilled ammonia wastewater circulation, tar circulation, tar-water mixture is adopted to carry out high-temperature quenching operation to raw gas in gas collection, change the direct quenching effect of raw gas, promote effuser temperature of exit gas, and configure coal gas pre-cooler, ensureing under raw gas cooling performance (heat-transfer effect) and the identical prerequisite of decoking effect (mass transfer effect), reclaim raw gas waste heat, produce 82 ~ 85 DEG C of technique heat medium waters, for hot water lithium bromide unit cooler producer thermal source; In addition, owing to reclaiming raw gas waste heat before primary cooler, comparatively existing procedure, the cold general facilities consumption of primary cooler significantly reduces.
Description
Technical field
The invention belongs to Coal Chemical Industry coking field, relate to the device of a kind of coking raw gas high temperature direct chilling reparation technology heat medium water.Concrete is exactly on existing raw gas emergency cooling process basis, by setting up distilled ammonia wastewater circulation, tar circulation, tar-water mixed liquid is adopted to carry out high-temperature quenching operation to raw gas in effuser, promote effuser temperature of exit gas, and configure coal gas pre-cooler, ensureing under raw gas cooling performance (heat-transfer effect) and the constant prerequisite of decoking effect (mass transfer effect), further recovery raw gas waste heat, produce about 85 DEG C technique heat medium waters, for heating the follow-up process heat trap matched.In addition, owing to reclaiming raw gas waste heat before primary cooler, compared with existing procedure, the cold general facilities consumption of primary cooler significantly reduces.
Background technology
In process of coking, be 650 ~ 750 DEG C from coke furnace carbonization chamber through the raw gas temperature that upcast is overflowed, now contain tar vapour, benzene hydrocarbon, steam, ammonia, hydrogen sulfide, prussic acid, naphthalene and other compounds in coal gas, and contain the heat of in coking about 1/3rd.Raw gas need cool, and just can obtain qualified coal gas after purifying.It is the basis of gas purification that raw gas tentatively cools, and its operation operating performance not only has impact to gas purification subsequent unit operation, and has impact to Chemicals processing and coking technique.The preliminary cooling of raw gas is carried out in two steps: the first step carries out direct chilling with a large amount of cyclic ammonia water in effuser; Second step indirectly cools by recirculated water and water at low temperature in coal gas primary cooler.
The industry of current coking of coal, raw gas is that the cyclic ammonia water of 5% is with the direct chilling of the form of sprinkling by 0.15 ~ 0.2MPa (gauge pressure), mass concentration in bridge tube and effuser.When the ammoniacal liquor of fine mist fully contacts with coal gas, because gas temperature is very high and steam-laden degree is very low, ammonia temperature is lower, so raw gas is lowered the temperature by ammoniacal liquor instantaneous cooling, the continuous condensation of heavy constituent, releases amount of heat, and ammoniacal liquor is by a large amount of gasification of raw gas heating moment, absorb the heat in raw gas, thus whole system temperature is reduced, play quenching effect.Visible moment, quenching process carried out violent heat transfer and mass transfer process.By above-mentioned quenching process, gas temperature is down to 82 ~ 86 DEG C by 650 ~ 700 DEG C, has the tar vapour condensation of about 60% to get off simultaneously.In actual production, gas temperature can be cooled to the dew-point temperature corresponding to composition 1 ~ 3 DEG C after higher than its chilling.82 DEG C of raw gas enter primary cooler and are recycled after water and water at low temperature are cooled to about 23 DEG C and enter subsequent purification workshop section.
Although coal gas can be cooled to 82 ~ 86 DEG C by 650 ~ 700 DEG C by existing raw gas emergency cooling process, reduce the cooling load of primary cooler, and the tar vapour of about 60% is cooled down, alleviate primary cooler coking phenomenon, but because the mass concentration of spraying ammoniacal liquor is 5%, its bubble point temperature is about 82 DEG C, effuser is caused to export raw gas temperature at 82 ~ 86 DEG C, the waste heat supply temperature reclaimed is too low, effectively cannot utilize further in subsequent recovery workshop section.In addition, because raw gas heat cannot reclaim before primary cooler, heat is finally dissipated in recirculated water (55 DEG C), water at low temperature (23 DEG C), not only causes the waste of heat, too increases the consumption of cold.
Simultaneously, there is a large amount of middle hot trap of low-temperature level in recovery of chemical products workshop section, as hot water lithium bromide refrigerator generators thermal source (85 DEG C), vacuum potassium carbonate desulfurization technique regeneration tower bottom reboiler thermal source (55 DEG C), negative pressure ammonia still process tower bottom reboiler thermal source (80 DEG C) etc., in addition need to supply amount of heat in system, to realize the effect such as pipeline companion heat, tank field dimension heat.In existing technique, above-mentioned Low Temperature Thermal trap generally adopts low-pressure steam (0.3MPa) heat supply, and 0.3MPa steam potential temperature is generally more than 130 DEG C, and this will cause high hot low use, cause energy wastage.From energy recovery aspect analyze, with can bottleneck be that a large amount of waste heats that raw gas contains cannot reclaim in high temperature section, and reclaim low-temperature heat quantity cannot with Low Temperature Thermal trap rational Match.Therefore, the recovered temperature (>=85 DEG C) improving raw gas waste heat should be managed.
Zhongye Coke Resistance Engineering Technology Co., Ltd's application develops one and utilizes raw gas waste heat, the exhaust heat recovering method of the sulfur removing pregnant solution of heating, vacuum salt of wormwood method sulfur removal technology, raw gas waste heat instead of sulfur removing pregnant solution and resolves steam source used, reduce process energy consumption, but the heat being still raw gas less than 82 DEG C used, reclaims heat grade lower.This patent No. is: CN200710086480.8.
Northeastern University develops a kind of thermal oil that adopts and reclaims raw gas heat, and produces the heat recovery technology of concerned process steps for adding thermalization, but needs to increase a set of closed heat-conducting oil system, and the easy coking of the heat taking and exchanging device of thermal oil.Changing the patent No. is: CN201110437813.3.
Shanghai Baosteel Energy Technology Co., Ltd.'s application develops a kind of waste heat of coke oven crude gas power generation assembly, in upcast, superheater is set, in bridge tube, vaporizer is set, liquid refrigerant forms superheated vapour after heat-obtaining subsystem, and the working medium in power generation sub-system heats and drives the dynamic power unit in power generation sub-system to generate electricity by superheated vapour.But be exposed to the easy coking of interior heat collecting device in raw gas, cause heat-transfer effect to decline, need frequent coke cleaning.This patent No. is: CN201210318033.1.
Summary of the invention
For above-mentioned practical situation, the invention provides the device of a kind of coking raw gas high temperature direct chilling reparation technology heat medium water, by setting up distilled ammonia wastewater circulation, tar circulation, tar-water mixture is adopted to carry out high-temperature quenching operation to raw gas in effuser, promote effuser temperature of exit gas, and configure coal gas pre-cooler, ensureing under raw gas cooling performance (heat-transfer effect) and the identical prerequisite of decoking effect (mass transfer effect), reclaim raw gas waste heat, produce 85 DEG C of technique heat medium waters, for meeting the follow-up process heat trap matched.In addition, owing to reclaiming raw gas waste heat before primary cooler, comparatively existing procedure, the cold general facilities consumption of primary cooler significantly reduces.
In raw gas waste heat recovery process, the raw gas temperature change of the direct emergency cooling process of effuser is maximum, and heat transfer, the transport phenomenon of system are the most violent, therefore, should manage the temperature promoting effuser outlet raw gas, thus promote raw gas waste heat recovery temperature.Effuser outlet raw gas temperature is determined by the bubble point temperature spraying tar-water mixture, therefore by regulating tar-water mixture composition, improving its bubble point temperature, thus promoting the potential temperature of recovery waste heat; Meanwhile, identical for ensureing raw gas decoking effect, should consider circulation tar-water mixture composition, on the impact of volatilization tar-water-raw gas mixing system dew-point temperature, dew-point temperature is higher, and the decoking effect in uniform temp interval is better.
Adopt tar-water mixture to spray, fountain height needs to optimize further.First, fountain height should meet heat transfer requirement, and namely by heat balance, 680 ~ 700 DEG C of raw gas are enough cooled to target temperature by the tar water of sprinkling; Moreover the fountain height of tar water should meet mass transfer demand, namely by analog calculation, the tar of 60% is enough taken out of by the tar water of sprinkling from gas phase; Finally, the fountain height of tar ~ water should be able to maintain the temperature of mechanical settling tank, and making the tar-water temp of spray close to its bubble point temperature, is advisable in its temperature difference≤3 DEG C.
On the basis completing tar ~ water composition, temperature, flow optimization, related process also should make suitable adjustment.Adopt the direct chilling of tar ~ water, then cancel the relevant device (oil-circulating ammonia water tank and pipeline etc. thereof) of cyclic ammonia water, and set up a mechanical settling tank A, for the oily water separation of effuser lime set and except slag operation, oil phase after separation is divided into two strands, one is as circulation tar, and blowback effuser sprays, and another stock enters water-and-oil separator and processes; The aqueous phase of the aqueous phase after separation and mechanical settling tank B is together sent to remained ammonia groove, and lock out operation is carried out in ammonia still, top gaseous phase is delivered to Liu An workshop section and is supplemented ammonia source after dephlegmator condensation, distilled ammonia wastewater at the bottom of tower is according to the material balance of system water, one tunnel is discharged after reclaiming heat, another road is direct blowback effuser then, mixes and sprays chilling, in order to maintain spray composition, temperature, the flow of tar ~ water mixture at top with circulation tar.In addition, primary cooling process for coal gas according to indirect two-stage primary cooler, then should arrange coal gas pre-cooler, the raw gas of about 90 DEG C is cooled to 85 DEG C between effuser and two sections of primary coolers, simultaneously the technique heat medium water of obtained more than 85 DEG C; If primary cooling process for coal gas adopts three intersegmentally to connect primary cooler, then can, by adjustment hot water section hot water flow, produced hot water temperature be made to be increased to 85 DEG C.It is constant that the follow-up primary cooling process of 85 DEG C of raw gas can maintain original technique, and because the dew point of the tar-water-raw gas mixing system that volatilizees is substantially constant, the coking degree of primary cooler is substantially constant, without the need to spraying more tar ammonias; Existing technique, raw gas heat is taken out by pre-cooler (two sections of primary cooler technique) or hot water section's (three sections of primary cooler technique), and primary cooler refrigeration duty will decrease, recirculated water and the corresponding minimizing of water at low temperature consumption.
Technical scheme of the present invention is as follows:
A device for coking raw gas high temperature direct chilling reparation technology heat medium water, comprises effuser, mechanical settling tank A, mechanical settling tank B, water-and-oil separator, tar storage tank, remained ammonia groove, ammonia still, ammonia still feed exchanger, coal gas pre-cooler, hot water lithium bromide unit cooler, two sections of horizontal water-tube primary coolers.The discharging of effuser lime set is connected with mechanical settling tank A, and the discharging of mechanical settling tank A aqueous phase is connected with remained ammonia groove, and the discharging of mechanical settling tank A oil phase divides two-way to connect: (1) mechanical settling tank A oil phase discharging one tunnel is connected with effuser; (2) another road of mechanical settling tank A oil phase discharging is connected with water-and-oil separator opening for feed; Remained ammonia groove discharge port is connected with ammonia still feed exchanger shell side inlet; Ammonia still feed exchanger shell-side outlet is connected with ammonia still opening for feed; Ammonia still process top gaseous phase is desulfuration ammonia workshop section after dephlegmator condensation; Distilled ammonia wastewater at the bottom of ammonia still divides two-way to connect: (1) distilled ammonia wastewater one tunnel is connected with effuser; (2) another road of distilled ammonia wastewater is connected with ammonia still feed exchanger tube-side inlet; Ammonia still feed exchanger tube side outlet material is sent to biochemical treatment; The discharging of effuser gas phase is connected with coal gas pre-cooler shell side inlet; Coal gas pre-cooler condensate outlet is connected with mechanical settling tank B opening for feed; Coal gas pre-cooler shell-side outlet is connected with two sections of horizontal water-tube primary cooler shell side inlet; Follow-up gas purification workshop section is sent in the discharging of two sections of horizontal water-tube primary cooler shell sides; Two sections of horizontal water-tube primary cooler lime sets divide two-way to connect: water at low temperature section circulated sprinkling is returned on (1) two section of horizontal water-tube primary cooler lime set one road; (2) two sections of another road dischargings of horizontal water-tube primary cooler lime set are connected with mechanical settling tank B opening for feed; Hot water lithium bromide unit cooler hot water outlet is connected with the import of coal gas pre-cooler tube side; Hot water lithium bromide unit cooler hot water inlet exports with coal gas pre-cooler tube side and is connected; Hot water lithium bromide unit cooler cooling water outlet is connected with two sections of horizontal water-tube primary cooler cold water inlets; Hot water lithium bromide unit cooler cold water inlet is connected with two sections of horizontal water-tube primary cooler cooling water outlets; The discharging of mechanical settling tank B oil phase is connected with water-and-oil separator opening for feed; The outlet of water-and-oil separator oil phase is connected with tar reservoir inlet.
Its technological process is as follows:
(1) 650 ~ 700 DEG C of raw gas from coke oven mix spray chilling by circulation tar, circulation distilled ammonia wastewater in effuser, the mass ratio of its mixing spray composition profit is 1.2 ~ 2:1, mixing spray temperature is 88 ~ 92 DEG C, effuser lime set temperature is 88 ~ 92 DEG C, lime set pumps into mechanical settling tank A, mechanical settling tank A aqueous phase pump is to remained ammonia groove, and oil phase in proportion 35 ~ 40:1 is divided into two-way: the former is sent to effuser and mixes with distilled ammonia wastewater and spray chilling; The latter is sent to water-and-oil separator, dewaters or is sent to tar storage tank.After chilling, raw gas temperature is 88 ~ 92 DEG C, enters coal gas pre-cooler and cools further.
(2) 88 ~ 92 DEG C of raw gas come by effuser, shell side is entered bottom coal gas pre-cooler, coal gas pre-cooler top tube side passes into 72 ~ 78 DEG C of circulating hot waters, raw gas and circulating hot water countercurrent flow, raw gas heat exchange to 82 ~ 85 DEG C, then enter two sections of horizontal water-tube primary cooler coolings through the outlet of coal gas pre-cooler top tube side; Circulating hot water is heated to 82 ~ 85 DEG C, this temperature has reached the requirement of technique heat medium water, the heat supply of process heat trap can be sent to, hot water lithium bromide unit cooler is sent in this technique, as hot water lithium bromide unit cooler producer thermal source, 72 ~ 78 DEG C of hot water blowback coal gas pre-cooler circulation heat-obtainings after heat supply, reparation technology heat medium water; Coal gas pre-cooler lime set pumps into mechanical settling tank B by bottom condensate outlet.
(3) 82 ~ 85 DEG C of raw gas come by raw gas pre-cooler, shell side is entered from two sections of horizontal water-tube primary cooler tops, cooled by 35 DEG C of recirculated waters and 16 DEG C of water at low temperature respectively upper and lower section of two sections of horizontal water-tube primary coolers, be finally cooled to 22 ~ 25 DEG C and send into follow-up gas purification workshop section; Hypomere cooling 16 DEG C of water at low temperature used are supplied by hot water lithium bromide unit cooler, and after heat exchange, 23 DEG C of water at low temperature backwater are to hot water lithium bromide unit cooler; Lime set pumps into mechanical settling tank B by condensate outlet bottom two sections of horizontal water-tube primary coolers.
(4) lime set collected by coal gas pre-cooler, two sections of horizontal water-tube primary coolers, be divided into three layers in mechanical settling tank B clarification, upper strata is ammoniacal liquor, and middle level is tar, and lower floor is coke tar refuse.Upper strata aqua ammonia pump to remained ammonia groove, and then carries out ammonia still process operation at ammonia still.The discharging of ammonia still process top gaseous phase is after dephlegmator cooling, ammonia is sent to ammonium sulfate workshop section saturex and supplements ammonia amount, distilled ammonia wastewater at the bottom of ammonia still is divided into two bursts of dischargings, partition ratio is 1:6 ~ 8: be sent to biochemical treatment after the former and ammonia still charging heat exchange, the flow of this strand of distilled ammonia wastewater should equal coal oven dithio-gas from water amount, and the water yield that this water yield brings system into by raw gas determines; The latter is pumped to effuser top, mixes spray with circulation tar, ensures that tar ~ Water spray profit mass ratio is 1.2 ~ 2:1, and mixing spray temperature is 88 ~ 92 DEG C.The part oil phase of mechanical settling tank B enters in water-and-oil separator, and after carrying out oily water separation, oil phase enters tar storage tank.
Compared with existing flow process, the present invention is by setting up distilled ammonia wastewater circulation, tar circulation, tar ~ water mixture is adopted to carry out high-temperature quenching operation to raw gas in gas collection, change the direct quenching effect of raw gas, promote effuser temperature of exit gas, and configure coal gas pre-cooler, ensureing under raw gas cooling performance (heat-transfer effect) and the identical prerequisite of decoking effect (mass transfer effect), reclaim raw gas waste heat, produce 82 ~ 85 DEG C of technique heat medium waters, for hot water lithium bromide unit cooler producer thermal source; In addition, owing to reclaiming raw gas waste heat before primary cooler, comparatively existing procedure, the cold general facilities consumption of primary cooler significantly reduces.
Accompanying drawing explanation
Accompanying drawing is the appliance arrangement structural representation of raw gas high temperature direct chilling reparation technology heat medium water.
Embodiment
Below in conjunction with technical scheme and accompanying drawing, describe the specific embodiment of the present invention in detail.
As shown in the figure, the discharging of effuser lime set is connected with mechanical settling tank A, the discharging of mechanical settling tank aqueous phase is connected with remained ammonia groove, and the discharging of mechanical settling tank oil phase divides two-way to connect: (1) mechanical settling tank oil phase discharging one tunnel is connected with effuser; (2) another road of mechanical settling tank oil phase discharging is connected with water-and-oil separator opening for feed; Remained ammonia groove discharge port is connected with ammonia still feed exchanger shell side inlet; Ammonia still feed exchanger shell-side outlet is connected with ammonia still opening for feed; Ammonia still process top gaseous phase is desulfuration ammonia workshop section after dephlegmator condensation; Distilled ammonia wastewater at the bottom of ammonia still divides two-way to connect: (1) distilled ammonia wastewater one tunnel is connected with effuser; (2) another road of distilled ammonia wastewater is connected with ammonia still feed exchanger tube-side inlet; Ammonia still feed exchanger tube side outlet material is sent to biochemical treatment; The discharging of effuser gas phase is connected with coal gas pre-cooler shell side inlet; Coal gas pre-cooler condensate outlet is connected with mechanical settling tank B opening for feed; Coal gas pre-cooler shell-side outlet is connected with two sections of horizontal water-tube primary cooler shell side inlet; Follow-up gas purification workshop section is sent in the discharging of two sections of horizontal water-tube primary cooler shell sides; Two sections of horizontal water-tube primary cooler lime sets divide two-way to connect: water at low temperature section circulated sprinkling is returned on (1) two section of horizontal water-tube primary cooler lime set one road; (2) two sections of another road dischargings of horizontal water-tube primary cooler lime set are connected with mechanical settling tank opening for feed; Hot water lithium bromide unit cooler hot water outlet is connected with the import of coal gas pre-cooler tube side; Hot water lithium bromide unit cooler hot water inlet exports with coal gas pre-cooler tube side and is connected; Hot water lithium bromide unit cooler cooling water outlet is connected with two sections of horizontal water-tube primary cooler cold water inlets; Hot water lithium bromide unit cooler cold water inlet is connected with two sections of horizontal water-tube primary cooler cooling water outlets; The discharging of mechanical settling tank oil phase is connected with water-and-oil separator opening for feed; The outlet of water-and-oil separator oil phase is connected with tar reservoir inlet.
Detailed process is:
(1) as shown in the figure, treatment capacity is that the raw gas of 320kg/h mixes spray chilling by circulation tar, circulation distilled ammonia wastewater in effuser C101, spray flux is 1900kg/h, mixing spray temperature is 90 DEG C, effuser C101 lime set pumps into mechanical settling tank A, mechanical settling tank B aqueous phase pump is to remained ammonia groove B101, and oil phase divides two-way: a road flow is 1100kg/h, is sent to effuser and mixes with distilled ammonia wastewater and spray chilling; Water-and-oil separator B105 is sent on another road, dewaters or is sent to tar storage tank B106.After chilling, raw gas temperature is 90 DEG C, and enters coal gas pre-cooler C102 and cool further.
(2) the 90 DEG C of raw gas come by effuser C101, flow is 530kg/h, shell side is entered bottom coal gas pre-cooler C102, C102 top tube side passes into 75 DEG C of circulating hot waters, raw gas and circulating hot water countercurrent flow, raw gas heat exchange to 85 DEG C, is sent to two sections of horizontal water-tube primary cooler C103 by the outlet of C102 top tube side and cools; Circulating hot water is heated to 85 DEG C, this temperature has reached the requirement of technique heat medium water, the heat supply of process heat trap can be sent to, hot water lithium bromide unit cooler is sent in this technique, as BrLi chiller producer thermal source, 75 DEG C of hot water blowback C102 circulation heat-obtainings after heat supply, reparation technology heat medium water; C102 lime set pumps into mechanical settling tank B104 by bottom condensate outlet.
(3) the 85 DEG C of raw gas come by raw gas pre-cooler C102, shell side is entered from two sections of horizontal water-tube primary cooler C103 tops, cooled by 35 DEG C of recirculated waters and 16 DEG C of water at low temperature respectively upper and lower section of C103, be finally cooled to 22 ~ 25 DEG C and send into follow-up gas purification workshop section; Hypomere cooling 16 DEG C of water at low temperature used are supplied by hot water lithium bromide unit cooler, and after heat exchange, 23 DEG C of water at low temperature backwater are to hot water lithium bromide unit cooler; Lime set pumps into mechanical settling tank B104 by condensate outlet bottom C103.
(4) collect by coal gas pre-cooler C102, two sections of horizontal water-tube primary cooler C103 the lime set come, be divided into three layers in mechanical settling tank B104 clarification, upper strata is ammoniacal liquor, and middle level is tar, and lower floor is coke tar refuse.Upper strata aqua ammonia pump to remained ammonia groove B101, and then carries out ammonia still process operation at ammonia still.The discharging of ammonia still process top gaseous phase is after dephlegmator cooling, ammonia is sent to ammonium sulfate workshop section saturex and supplements ammonia amount, distilled ammonia wastewater at the bottom of ammonia still is divided into two bursts of dischargings, biochemical treatment is sent to after one and ammonia still charging heat exchange, the flow of this strand of distilled ammonia wastewater should equal to join coal oven dithio-gas from water amount, and the water yield that this water yield brings system into by raw gas determines; Another plume amount is 700kg/h, is pumped to effuser C101 top, mixes spray with circulation tar, ensures that tar ~ Water spray water oil ratio (massfraction) is 1.2 ~ 2:1, and mixing spray temperature is 90 DEG C.The part oil phase of mechanical settling tank B104 enters in water-and-oil separator B105, and after carrying out oily water separation, oil phase enters tar storage tank B106.
Compared with existing flow process, the present invention is by setting up distilled ammonia wastewater circulation, tar circulation, tar ~ water mixture is adopted to carry out high-temperature quenching operation to raw gas in gas collection, change the direct quenching effect of raw gas, promote effuser temperature of exit gas, and configure coal gas pre-cooler, ensureing under raw gas cooling performance (heat-transfer effect) and the identical prerequisite of decoking effect (mass transfer effect), reclaim raw gas waste heat, produce 82 ~ 85 DEG C of technique heat medium waters, for hot water lithium bromide unit cooler producer thermal source; In addition, owing to reclaiming raw gas waste heat before primary cooler, comparatively existing procedure, the cold general facilities consumption of primary cooler significantly reduces.
Claims (2)
1. a device for coking raw gas high temperature direct chilling reparation technology heat medium water, comprises effuser, mechanical settling tank A, mechanical settling tank B, water-and-oil separator, tar storage tank, remained ammonia groove, ammonia still, ammonia still feed exchanger, coal gas pre-cooler, hot water lithium bromide unit cooler and two sections of horizontal water-tube primary coolers;
The lime set discharging of effuser is connected with mechanical settling tank A, and the discharging of mechanical settling tank A aqueous phase is connected with remained ammonia groove, and the discharging of mechanical settling tank A oil phase divides two-way to connect: (1) mechanical settling tank A oil phase discharging one tunnel is connected with effuser; (2) another road of mechanical settling tank A oil phase discharging is connected with water-and-oil separator opening for feed; Remained ammonia groove discharge port is connected with ammonia still feed exchanger shell side inlet; Ammonia still feed exchanger shell-side outlet is connected with ammonia still opening for feed; Ammonia still process top gaseous phase is desulfuration ammonia workshop section after dephlegmator condensation; Distilled ammonia wastewater at the bottom of ammonia still divides two-way to connect: (1) distilled ammonia wastewater one tunnel is connected with effuser; (2) another road of distilled ammonia wastewater is connected with ammonia still feed exchanger tube-side inlet; Ammonia still feed exchanger tube side outlet material is sent to biochemical treatment; The discharging of effuser gas phase is connected with coal gas pre-cooler shell side inlet; Coal gas pre-cooler condensate outlet is connected with mechanical settling tank B opening for feed; Coal gas pre-cooler shell-side outlet is connected with two sections of horizontal water-tube primary cooler shell side inlet; Follow-up gas purification workshop section is sent in the discharging of two sections of horizontal water-tube primary cooler shell sides; Two sections of horizontal water-tube primary cooler lime sets divide two-way to connect: water at low temperature section circulated sprinkling is returned on (1) two section of horizontal water-tube primary cooler lime set one road; (2) two sections of another road dischargings of horizontal water-tube primary cooler lime set are connected with mechanical settling tank B opening for feed; Hot water lithium bromide unit cooler hot water outlet is connected with the import of coal gas pre-cooler tube side; Hot water lithium bromide unit cooler hot water inlet exports with coal gas pre-cooler tube side and is connected; Hot water lithium bromide unit cooler cooling water outlet is connected with two sections of horizontal water-tube primary cooler cold water inlets; Hot water lithium bromide unit cooler cold water inlet is connected with two sections of horizontal water-tube primary cooler cooling water outlets; The discharging of mechanical settling tank B oil phase is connected with water-and-oil separator opening for feed; The outlet of water-and-oil separator oil phase is connected with tar reservoir inlet.
2. utilize device reparation technology heat medium water described in claim 1 method, its feature comprises the following steps:
(1) 650 ~ 700 DEG C of raw gas from coke oven mix spray chilling by circulation tar, circulation distilled ammonia wastewater in effuser, the mass ratio of its mixing spray composition profit is 1.2 ~ 2:1, mixing spray temperature is 88 ~ 92 DEG C, effuser lime set temperature is 88 ~ 92 DEG C, lime set pumps into mechanical settling tank A, mechanical settling tank A aqueous phase pump is to remained ammonia groove, and oil phase in proportion 35 ~ 40:1 is divided into two-way: the former is sent to effuser and mixes with distilled ammonia wastewater and spray chilling; The latter is sent to water-and-oil separator, dewaters or is sent to tar storage tank; After chilling, raw gas temperature is 88 ~ 92 DEG C, enters coal gas pre-cooler and cools further;
(2) 88 ~ 92 DEG C of raw gas come by effuser, shell side is entered bottom coal gas pre-cooler, coal gas pre-cooler top tube side passes into 72 ~ 78 DEG C of circulating hot waters, raw gas and circulating hot water countercurrent flow, raw gas heat exchange to 82 ~ 85 DEG C, then enter two sections of horizontal water-tube primary cooler coolings through the outlet of coal gas pre-cooler top tube side; Circulating hot water is heated to 82 ~ 85 DEG C, is sent to hot water lithium bromide unit cooler, as BrLi chiller producer thermal source; 72 ~ 78 DEG C of hot water blowback coal gas pre-cooler circulation heat-obtainings after heat supply, reparation technology heat medium water; Coal gas pre-cooler lime set pumps into mechanical settling tank B by bottom condensate outlet;
(3) 82 ~ 85 DEG C of raw gas come by raw gas pre-cooler, shell side is entered from two sections of horizontal water-tube primary cooler tops, cooled by 35 DEG C of recirculated waters and 16 DEG C of water at low temperature respectively upper and lower section of two sections of horizontal water-tube primary coolers, be finally cooled to 22 ~ 25 DEG C and send into follow-up gas purification workshop section; Hypomere cooling 16 DEG C of water at low temperature used are supplied by hot water lithium bromide unit cooler, and after heat exchange, 23 DEG C of water at low temperature backwater are to hot water lithium bromide unit cooler; Lime set pumps into mechanical settling tank B by condensate outlet bottom two sections of horizontal water-tube primary coolers;
(4) lime set collected by coal gas pre-cooler, two sections of horizontal water-tube primary coolers, be divided into three layers in mechanical settling tank B clarification, upper strata is ammoniacal liquor, and middle level is tar, and lower floor is coke tar refuse; Upper strata aqua ammonia pump to remained ammonia groove, and then carries out ammonia still process operation at ammonia still; The discharging of ammonia still process top gaseous phase is after dephlegmator cooling, ammonia is sent to ammonium sulfate workshop section saturex and supplements ammonia amount, distilled ammonia wastewater at the bottom of ammonia still is divided into two bursts of dischargings, partition ratio is 1:6 ~ 8: be sent to biochemical treatment after the former and ammonia still charging heat exchange, the flow of this strand of distilled ammonia wastewater should equal coal oven dithio-gas from water amount, and the water yield that this water yield brings system into by raw gas determines; The latter is pumped to effuser top, mixes spray with circulation tar, ensures that the mass ratio of tar ~ Water spray profit is 1.2 ~ 2:1, and mixing spray temperature is 88 ~ 92 DEG C; The part oil phase of mechanical settling tank B enters in water-and-oil separator, and after carrying out oily water separation, oil phase enters tar storage tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410246529.1A CN104031692B (en) | 2014-06-05 | 2014-06-05 | The device and method of a kind of coking raw gas high temperature direct chilling reparation technology heat medium water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410246529.1A CN104031692B (en) | 2014-06-05 | 2014-06-05 | The device and method of a kind of coking raw gas high temperature direct chilling reparation technology heat medium water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
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| CN104629816B (en) * | 2015-01-30 | 2016-09-28 | 济南冶金化工设备有限公司 | From the preliminary chiller of refrigeration mode coal oven dithio-gas |
| CN105062571B (en) * | 2015-08-05 | 2017-08-25 | 华陆工程科技有限责任公司 | Energy-saving and emission-reduction method and its device in a kind of coal coal gas |
| CN106915862B (en) * | 2015-12-24 | 2020-08-07 | 中国科学院过程工程研究所 | Coal chemical wastewater treatment system based on gas secondary gas-liquid separation and treatment method thereof |
| CN106766342B (en) * | 2016-12-12 | 2022-07-05 | 松下制冷（大连）有限公司 | System for recovering ammonia steam waste heat at top of ammonia still tower by using lithium bromide absorption heat pump |
| CN107021590B (en) * | 2017-04-24 | 2020-02-21 | 莱芜市泰山焦化有限公司 | Method for reducing harmful components in ammonia distillation wastewater through step-by-step separation based on high dry distillation of coal cakes |
| CN111363567A (en) * | 2018-12-26 | 2020-07-03 | 苏州永峰联环保科技有限公司 | Coking indirect cooling tower cleaning process and cleaning device thereof |
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